Method and system for processing aquatic organisms

FIELD: food industry.

SUBSTANCE: invention relates to a method for manufacture of multiple products from aquatic plant species biomass. Biomass is obtained, destroyed and separated to produce juice and solid phase; the juice is filtered and clarified. Protein is coagulated from the clarified juice to produce broth including a wet protein concentrate. The said concentrate is separated from broth. The wet protein concentrate is dried to obtain dry protein concentrate. The solid phase is used for wet biological raw materials production. The said biological raw materials are dried to produce at least one product selected from among dry biological raw materials and meal rich in carbohydrates. At least 50% of protein in the multiple products is present in dry protein concentration.

EFFECT: method is environmentally friendly and allows production of multiple products selected from among dry biological raw materials and meal rich in carbohydrates.

35 cl, 39 dwg, 7 tbl, 25 ex

 

CROSS-REFERENCE TO RELATED APPLICATION

The present application claims priority under §119(e) 35 U. S. C. provisional patent application U.S. 61/314736, filed March 17, 2010, which is hereby fully incorporated by reference.

The LEVEL of TECHNOLOGY

Marine protein sources are often used in pet foods because they are an excellent source of essential amino acids, fatty acids, vitamins and minerals, and because they usually improve palatability. Alternative ingredients can be used in the feed industry fish instead of fish meal. For this reason, many studies have been conducted to replace the expensive marine proteins with cheaper ingredients. Considerable attention was paid to the replacement of fish meal with vegetable protein; duckweed, as a natural source of protein, contains the best set of essential amino acids compared with most other vegetable proteins and more similar to animal protein. Freshly harvested duckweed contains 43% protein in dry weight and can be used without additional processing as a complete feed for fish. Compared with most other plants, the leaves of the duckweed contain few fibers (5% in dry matter for cultivated plants) and little, or virtually free, non-digestible material d�same for monogastric animals. This differs from the compositions of many crops, such as soybeans, rice and corn, approximately 50% of the biomass which is formed by residues with high fiber content and low digestibility.

Lemna is a genus of free-floating aquatic plants from the duckweed family, also known as the family Ryaskovye (Lemnaceae). These rapidly growing plants have found uses as a model system for studies of the basic biology of plants, ecotoxicology, in the production of Biopharmaceuticals, and as a source of animal feed for agriculture and fish farms.

Types of rasoc grow in the form of a simple free floating thalli on the surface or slightly below the surface of the water. Most is a small, not exceeding 5 mm in length of the plant, except for duckweed trilobal (Lemna trisulca), which is elongated and has a branched structure. The thalli of duckweed have the same root. The plants are mainly propagated vegetatively. This growth form may allow very rapid colonization of the new water.

The rapid growth of duckweed is used in the biological treatment of polluted waters and as test organisms for environmental studies. It is also used as expression systems for cost-effective production�of DSTV complex biopharmaceutical.

Dried duckweed can be good fodder for cattle. It may contain 25-45% protein (depending on growing conditions), to 4.4% fat, and 8-10% of the fibers in the measurement of a relatively dry mass.

Duckweed can be grown organically, with the use of nutrients available from a variety of sources, such as cattle manure, pig waste, vegetable mass for the production of biogas or other organic substances in the form of a liquid mass.

Summary of the INVENTION

Embodiments of the present invention provide a method of separating multiple products from biomass of aquatic organisms. The method may include: obtaining biomass; destruction of biomass with getting destroyed biomass; the separation of the destroyed biomass with getting juice and the first solid phase; forming a wet protein concentrate using the juice; drying the wet protein concentrate to produce dry protein concentrate; production of wet biosyrya by using the first solid phase; drying the wet biosyrya obtaining at least one product selected from a dry biosyrya and carbohydrate-rich feed flour; where many products may include products selected from the dry protein concentrate, dry biosyrya and carbohydrate-rich feed flour, and where according to møn�Shea least 50% of the protein in the multiple products is present on a dry protein concentrate. In some embodiments, the step of obtaining can include: obtaining biomass of aquatic organisms on an industrial scale and collection of biomass. In some embodiments, phase separation may include pressing the destroyed biomass. Similarly, in some embodiments, the method may include filtering the juice with obtaining the filtered juice and the second solid phase; clarification of filtered juice with obtaining a clarified juice and a third solid phase; coagulating protein from the clarified juice with obtaining broth comprising a wet protein concentrate; and the allocation of the wet protein concentrate from the broth.

In some embodiments, at least one of: the first solid phase, the second solid phase, a third solid phase and the broth can be used to obtain biosyrya and/or carbohydrate-rich feed flour. Aquatic organisms may include, for example, Duckweed species. Destruction may include the use of at least one of: a ball mill, colloid mill, cutter mill, hammer mill, crusher, puree the machine and filter press. The pressure can include the application of at least one of the belt press, centrifugal filter press, rotary press, screw press, filter press, press and finishing. Juice can include races�worky protein. The method can include pressing at least one of the first hard phase, the second solid phase or a third solid phase with a second juice and biosyrya. In some embodiments, the second the juice can be combined with juice. Similarly, in some embodiments, additional compaction may be performed using a screw press. In some embodiments, the method may further include drying biosyrya. Drying may be performed using at least one of: a turbulent dryers, spray dryer, drum dryer, flash dryer, fluidized bed dryer, double-drum dryers and rotary dryers. The filtering may be performed using at least one of: vibration separator, vibrating screen filter, vibrating separator, circular steps, linear vibrating sieve/horizontal motion, decanter centrifuges and filter press. The vibratory separator may include at least one vibrating screen filter. Clarification may include centrifugation and/or filtration of the filtered juice, for example, using at least one high-speed multi-disc centrifuge, microfiltration ultrafiltration, etc.

� some embodiments, the implementation of the clarified juice can be stored in storage tanks, such as, for example, a cooled storage tank. Coagulating may include lowering the pH of the clarified juice, for example, to a pH below about 6, or below about 5, or about 4.5, or less. The decrease in pH may include the use of at least one acid selected from hydrochloric acid, nitric acid, sulfuric acid, etc. Coagulation can be performed with the use of a precipitant comprising at least one heat exchanger, such as, for example, at least one plate heat exchanger or tubular heat exchanger or a heat exchanger with steam injection, or the like. Coagulating may include heating the clarified juice to a first temperature with obtaining broth; and cooling the broth to a second temperature. In some embodiments, the first temperature may be from about 40°C to about 100°C, similarly, the second temperature can be below about 40°C or below about 30°C, for example. The separation may include the use of high-speed multi-disc centrifuge. In some embodiments, the wet protein concentrate may be stored in storage containers, such as, for example, a cooled storage tank. The method may further include drying the wet protein�vågå concentrate to produce dry protein concentrate. Drying may be performed using, for example, spray dryer, drum dryer, turbulent dryers, flash dryers, fluidized bed dryer, double-drum driers, rotary driers, etc. In some embodiments, the method may additionally include a contact material selected from the group consisting of: a third solid phase and a clarified juice with at least one of, for example, alcohol, solvent, water, etc., and further the contact of the material with an acid catalyst with the formation of the mixture, separation of the mixture into liquid and solid phase, resulting in lipids and ash forming components, etc. in the material is separated with liquid. The method may further comprise, before or immediately after the destruction, the washing of the biomass with an aqueous solvent or the like.

Embodiments of the invention also provide a system for the allocation of multiple products from biomass of aquatic organisms; such systems may include, for example: block destruction for destruction of biomass with getting destroyed biomass; a separation unit for separating the destroyed biomass with getting juice and a solid phase; a unit for forming a wet protein concentrate using the juice; a drying unit of protein for drying the wet protein concentrate Poluchenie dry protein concentrate; and block drying of wet biosyrya obtaining at least one product selected from a dry biosyrya and carbohydrate-rich feed flour moist biological raw materials may include a solid phase; and where many products may include products selected from, for example, the dry protein concentrate, dry bioserie rich in carbohydrates feed flour, etc., and where at least about 50% of the protein in the multiple products is present on a dry protein concentrate. The unit of damage may include at least one device selected from a colloid mill, cutter mill, ball mill, hammer mill, crusher, puree the machine and filter press. The separation unit may include at least one device selected from a belt press, decanter centrifuge, centrifugal filter press, rotary press, screw press, filter press, press and finishing. Unit for forming a wet protein concentrate using the juice may include at least one unit selected from, for example, a filter unit, a polishing block, the block coagulation of protein and protein. In some embodiments, the filtration unit may include at least one device selected from, for example, vibratory separator, vibrating mesh fil�RA, vibrating separator, circular steps, linear vibrating sieve/horizontal motion, decanter centrifuge, filter press, etc. Unit clarification may include at least one device or method selected from, for example, high-speed disc centrifuge, microfiltration, ultrafiltration, etc. In some embodiments, the block coagulation protein may include at least one device selected from, for example, thermostates, acid deposition, etc. the protein may include at least one device selected from, for example, high-speed multi-disc centrifuge, settling tank, clarifier, decanter centrifuge, etc. the drying Unit of the protein may include at least one device selected from, for example, spray dryer, double-drum dryer, flash dryer, etc. the Unit for drying biosyrya may include at least one device selected from, for example, fluidized bed drier, turbulent dryers, flash dryers, drum dryers, rotary dryers, etc. similarly, in some embodiments, the system may further include a block sanitization.

BRIEF DESCRIPTION of FIGURES

Fig.1A is a block diagram showing an example of a sub�production raskovich as feedstock for production of biofuel and protein concentrate.

Fig.1B is a block diagram showing an example of a method of growing, harvesting and processing of micro-cultures.

Fig.2 is a block diagram showing an example of a method of separating protein from fresh duckweed.

Fig.3 is the histogram, which shows the comparative yield of the dried protein (dry protein concentrate) and comparative output biosyrya of expeller.

Fig.4 is a histogram showing an example of the moisture content in the wet protein concentrate obtained in the method shown in Fig.2.

Fig.5 is the histogram, which shows the purity of the protein produced in the method shown in Fig.2, depending on the party.

Fig.6 is the histogram, which shows the moisture content in wet biological raw materials obtained in the method shown in Fig.2.

Fig.7 - histogram, which shows the composition of dry biosyrya obtained in the method shown in Fig.2, depending on the party.

Fig.8 - histogram showing the relative efficiency of the experimental farms in different occasions.

Fig.9 is a histogram showing an example of the relative content of the solid phase after the destruction and compaction of fresh duckweed, as described in Fig.2.

Fig.10 is a histogram showing an example of the relative content of the solid phase after the transmission of the combined raw juice� via vibrating separator, as shown in Fig.2.

Fig.11 shows an example of a calculation of the relative content of materials using the results shown in Fig.10 and Fig.11.

Fig.12 is a bar graph showing exemplary test of the relative content of the solid phase after clarification of the filtered juice in a centrifuge, as shown in Fig.2.

Fig.13 is a histogram that shows the trial test of the relative content of the solid phase after precipitation of the spun filtered juice with the purpose of coagulation of the protein.

Fig.14 is a histogram showing an example of the efficiency of collecting the product of a spray dryer, as shown in Fig.2.

Fig.15 is a histogram showing an example of the relative content of the solid phase after each of the model operation.

Fig.16 shows how to calculate the yield of protein (dry protein concentrate), on the basis of the mass flow of solids through the unit operations.

Fig.17 is a block diagram showing an example of a method of separating protein from duckweed.

Fig.18 is a more detailed block diagram of the method shown in Fig.17, which shows an example of a method of separating protein from duckweed.

Fig.19 is a histogram that shows the relative content of the solid phase under typical operations in the method shown in Fig.17 and Fig.18.

Fig.20 shows an example of calculating the contents�of materials after Extraction and Drying #1 and Extraction Drying #2, shown in Fig.19.

Fig.21 shows an example of how to calculate the yield (dry protein concentrate), on the basis of the mass flow of solids through the unit operations.

Fig.22 is a histogram that shows the relative extraction of protein with typical operations in the method shown in Fig.17 and Fig.18.

Fig.23 shows an example of how to calculate the yield of protein based on protein mass flow through the model operation.

Fig.24 is a histogram that shows the relative content of the solid phase after clarification of the raw juice/processed juice (E1 and E2) in the centrifuge.

Fig.25 is a histogram showing the relative solids content after pasteurization clarified juice with the purpose of coagulation of the protein.

Fig.26 is a histogram that shows the relative content of the solid phase after the passage of the broth obtained during the coagulation of the protein, using a centrifuge to separate the protein.

Fig.27 is a histogram that shows the relative content of the solid phase after drying the wet protein concentrate by spray drying.

Fig.28 shows a diagram of the test Protocol with examples of the mass flow of the solid phase, shown in Fig.24-27.

Fig.29 is a block diagram showing an example of a method of separating protein and other foods from fresh duckweed.

F�G. 30 - a block diagram of an exemplary method of isolating the protein from fresh duckweed.

Fig 31 is a block diagram showing an exemplary method of isolating the protein from fresh duckweed.

Fig.32 is a block diagram showing an exemplary method of isolating the protein from fresh duckweed with optional regulation of pH and flushing wet squirrel.

Fig.33 is a block diagram showing an exemplary method of isolating the protein from fresh duckweed with a reverse mixing and optional flushing of protein, and obtaining other products (for example, biosyrya).

Fig.34 is a block diagram showing an exemplary method of isolating the protein from fresh duckweed with a reverse mixing and the addition of water in a mixing tank.

Fig.35 is a block diagram showing an exemplary method for isolating the protein and other foods from fresh duckweed using a ball mill, and sedimentation.

Fig.36 is a block diagram showing an exemplary method of growing and harvesting fresh duckweed.

Fig.37 is a block diagram showing an exemplary method for isolating the protein and other foods from fresh duckweed.

Fig.38 is a block diagram showing an exemplary method for isolating the protein and other foods from fresh duckweed.

DETAILED DESCRIPTION

In some embodiments, the numbers expressing quantities of ingredients, properties such as molecular weight, reaction conditions�AI etc. used to describe statements and certain uses, should be considered to be supplemented in some instances by the term "approximately". Thus, in some embodiments, the numerical parameters given in the written description and attached claims are approximations that may vary depending on the desired properties, which are obtained in accordance with the specific variant implementation. In some embodiments, the numerical parameters should be considered taking into account the specified number of significant digits and by applying standard rounding methods. Notwithstanding that the numerical ranges and parameters involving a wide scope of some applications are approximations, the numerical values shown in the specific examples presented as accurately as possible.

Any discussion of the prior art throughout the present description in no way be seen as an admission that such prior art is widely known or forms part of common knowledge in this field.

Unless explicitly stated otherwise, throughout the present description and the claims, the words "include", "includes", etc., should be considered in inclusive �thinking, as opposed to an exclusive or exhaustive sense; that is, in the sense of "including without limitation".

Types of plants in the familyLemnaceae(or Ryaskovye) are widely distributed in many parts of the world and, thus, have been widely studied for potential industrial applications, including use as feed. Species in this family contain high levels of protein in the range from about 15% to 43% (from dry weight) that is of potential value for applications in feed quality, which calls for concentrated sources of protein. Given this defining feature, these types may be suitable as an alternative protein source for feed in fish farms, animal feed and for other uses.

Modern conditions covering climate change and sustainable use of resources, encourage the development of production materials from Raskovich as feedstock for the biofuel industry and protein concentrate. Fig.1A shows a block diagram of an exemplary production of duckweed to produce raw materials for biofuels and protein concentrate. Carbohydrates can be separated from the raw material for the biofuel industry, while the protein fraction (which also contains a significant amount of fat) can be used for feed applications. In particular, given the scale of the biofuel industry, commercialization of such methods can lead to large-scale availability of this balanced protein source. In addition, can be obtained protein concentrate, containing up to 65-70% protein (dry weight) or more. Table 1 shows typical data on the composition, the content of essential amino acids and digestibility preliminary data duckweed, which can illustrate the potential effectiveness of this protein source for feed applications for fisheries.

Table 1
The profile of essential amino acids in the protein concentrate duckweed
Essential amino acidProtein (g/100g)
Lysine5,9
Leucine9,7
Isoleucine5,1
Methionine2,4
Phenylalanine6,3
Threonine4,4
Tryptophan 2,0
Valine6,3
Histidine2,7
Arginine6,8

As shown in Fig.1A, aquatic organisms, for example, agricultural micro cultures, such as duckweed, can be grown in the production system. The production system may include one or more bioreactors. The bioreactor(s) can be large scale, medium scale or small scale, or a combination of the above. The scale of the bioreactor(s) may be selected based on factors including, for example, the space available for the establishment of a system of cultivation and/or processing facilities, source of water (or other nutrient media for agricultural microculture), etc. the Bioreactor(s) can be open bioreactor, closed bioreactor or semi-open bioreactor, or a combination of the above. The production system may include a monitoring system. The bioreactor(s) may include a built-in monitoring system. The monitoring system may regulate working conditions, including, for example, the feed rate of nutrients and/or CO2in the bioreactor(s), illumination time and/or frequency of harvest, or the like, or kombinatsionnogo. Such regulation can be performed in real time or periodically. Such regulation can optimize the speed of growth and/or productivity of aquatic organisms. Just as an example, agricultural microculture grown in large-scale outdoor bioreactors, equipped with built-in monitoring systems that provide optimal illumination and a mixture of nutrients for optimised growth.

After ripening aquatic organism, it can be collected from the cultivation system. In some embodiments, as shown in Fig.1A, water body, for example, microculture, can be collected by using vacuum from the surface of the bioreactor through the stationary mesh filter. In some embodiments, the slurry of biomass, including the collected water body with a great deal of water or any other medium for cultivation, can be obtained for inclined vibrating screen filter, where the biomass, including the water body, can be separated from water or environment for cultivation, due to the fact that the water or the culture medium can pass through the strainer. At least 40% or at least 50% or at least 60% or at least 70% or at least 80% or at least 90% or at least 95% water ilirida for cultivation, collected with the help of vacuum, can be returned into the cycle for future use. Just as an example, returned to the water cycle or the culture medium can flow back into the bioreactor and used repeatedly.

The collected biomass, including aquatic organisms, can be processed with the receipt of two components: a carbohydrate-rich solid phase and a protein-rich liquid phase, also called juice. The procedure can be performed by means of a screw press, belt press, cutter mill, ball mill, etc., or combinations thereof. Just as an example, the collected biomass can be destroyed in the cutting mill. Used in this description of the "destruction" of biomass covers mechanical or chemical treatments that disrupt the organization of the body at the level of individual cells or multicellular structures that allows to make carbohydrates, proteins and micronutrients that are present in the biomass of organisms that are more accessible to further processing to obtain purified protein, carbohydrate-containing materials or micronutrient liquids. Destruction may include, for example, chopping, cutting, crushing, pressing, tearing, lysis under the action of osmotic pressure, or chemical treatments that break down the biologist�ical structure. Destroyed biomass can be pressed into a belt press with getting juice and the first solid phase; and the first solid phase can be pressed in a screw press to obtain additional quantities of juice and wet material, called " wet "biosystem". Wet biological raw materials may include carbohydrate-rich solid phase and can be processed further. The juice obtained in the various procedures of extrusion, can be combined for further processing.

"Biological raw materials" and "biological raw materials" are used interchangeably. Wet biological raw materials can be processed taking into account such factors as, for example, suitability for subsequent applications. Just as an example, biological raw materials can be dried for use as feedstock for power plants. In other embodiments, biological raw materials can be optimized by means of granulation, etc. for co-firing with other hydrocarbon fuel, such as coal. In other embodiments, biological raw materials used as feedstock for biofuel production. In other embodiments, biological raw materials additionally treated using physical or chemical methods to further extraction of the protein components. In other embodiments, biological raw materials can be processed, for example, through the Gran�of debugger, for the needs of users.

As shown in Fig.1A, in some embodiments, the implementation of SAP, including protein-rich liquid phase, process for coagulation and/or precipitation of the protein with a solid phase with a high content of proteins, which in some embodiments is further treated with getting more protein in high purity. The solid phase with a high content of proteins suitable as animal feed.

Fig.1B shows a block diagram of an exemplary method of cultivation, collection and processing of microculture. This approximate method is developed for use as starting material of large amounts of microculture", for example, duckweed, and production of several products, including protein concentrate, raw material for fuel (also called "biosystem") and rich in carbohydrates animal feed (called "flour from duckweed"). Number, outputs and distribution of final products can be different and are determined under certain protocols. Fig.1B is shown in basic block diagram. Other factors that can be optimized include the identification and use, as part of the process, the typical operations that can be scaled depending on the intended result. This analysis includes whether the process is periodic and�and a continuous mode and may have an impact on the final product and/or the received outputs.

An exemplary method includes a part held outdoors and part indoors. An exemplary method begins with bioreactors, which represent the production ponds, designed to provide optimal growth conditions for the production of surface microculture. The automated system controls the levels of nutrients and regulates a given composition of nutrients in the ponds. While gathering automated harvesting system extracts a certain number of micro cultures with certain areas in the ponds and delivers the biomass through a pumping system in an inclined vibrating screen filter to separate the wet biomass from the water and residue. More than 99% of the water back into the ponds through the return tubing to ensure uniform mixing in the pond. Wet biomass is harvested and fed to the recycling centre (located in the premises of the processing plant). When it arrives at the processing facility wet biomass destroy (by using a ball mill, hammer mill or other similar technologies) with the release of internal water. The SAP derived from proteins and subjected to further processing for the purpose of extraction of protein getting protein concentrate, suitable as component�the animal feed and potentially food for humans. Soluble protein in the coagulated juice when using thermostates, acid deposition or similar technology. Then, the protein precipitate is separated, using high-speed multi-disc centrifuge. The supernatant liquid is recycled back to the ponds, whereas the wet protein concentrate is dried using dryers, specially selected for optimization of the final product (including spray dryer, drum dryer, etc.). The dried product is then packaged. The material remaining after extraction of juice, is rich in carbohydrates suspension. This suspension was subjected to additional processing to receive one of biosyrya used for burning, biosyrya used as a coke feedstock (a refinery) or fish meal of duckweed used as feed for animals. Each application has specific (and different) characteristics of the final product, which determine acceptable quality. They include particle size, moisture content, ash content, etc. the drying Mechanism is different and is selected to improve or optimize these properties depending on the final product. In some cases, to reduce the ash content may be subject to additional processing. The procedure to remove ash (if used) additional�individual described below.

In some embodiments, the choice of surface micro cultures, choosing the dominant local view with the selected characteristics of the composition and growth, historically developed in the local natural conditions. Dominant native species may compete with other species in open ponds or bioreactors (and sometimes even in closed environments or bioreactors). The selection procedure starts with the selection of several types of local ponds and lakes, and studies of their potential growth and production (i.e., composition). A mixture of the dominant species may change depending on the season. This allows you to identify potential micro cultures that grow in different seasons and in different climatic conditions. Select a few local species. Required colonies obtained in the result of selection for use in larger-scale production outside of the premises.

In some embodiments, the bioreactor (e.g., a pond) is an earthen basin with embankments made of compacted soil, extracted from the bottom of the bioreactor. Multiple bioreactors arranged in line and are designed to provide optimal conditions for the growth of duckweed (including nutrient availability, water quality, etc.). The bioreactor has a size that is selected to optimize the capital�tion costs and operating costs by maximizing the amount of collected material. The surface area needs to accommodate normal precipitation over a defined area. Excess water is removed in the tank for collecting rainwater (for example, a pool for collecting rainwater).

In some embodiments, microculture grows rapidly and forms a floating Mat on the water surface of the bioreactor (e.g., pond). To maintain in the bioreactor constant levels of nutrients and the right temperature, different methods of recycling (propulsion, a paddle wheel, etc.) are used and regulated to create better growing conditions for the carpet. During recirculation the water quality can be checked and, if necessary, to add the required nutrients that include a balanced composition of all nutrients (macro - nutrients and trace elements needed microculture, to maintain the nutritional content at the specified level.

In some embodiments, the culture medium includes water. Water includes a balanced composition of nutrients for micro cultures. In other embodiments, one or more nutrients required for micro cultures, added to growth media. Just as an example, the culture medium includes artesian water that has acceptable quality, and appropriate quantitative�of balanced nutrients.

In some embodiments, the bioreactor (i.e., ponds) smaller are of such size and design to properly perform the function of "recharging" bioreactors for larger bioreactor. Smaller bioreactors are first seeded and grown to high density, after which they can be optimally used for sowing larger bioreactor in a manner that provides a more rapid growth.

In some embodiments, the culture medium (e.g. water) is added to the bioreactor (e.g., a pond) and is maintained at a predetermined level. For optimum productivity micro cultures (or biomass) water check to maintain nutrients and compounds within standard levels. Sensors installed in a biosensor to monitor and record the levels of nutrients and compounds, including, for example, ammonia, pH, redox potential (ORP) and temperature, etc., or a combination of both. The ammonia sensor is used as feedback to control the levels of nitrogen in bioreactor via the delivery system of nutrients from the tank. In the bioreactor installed a level sensor, ensuring that the water level does not drop below the required depth.

In some embodiments, the bioreactor equipment�IAOD one or more sensors for monitoring and controlling various aspects, including water quality, nutrients, environmental conditions, etc., or a combination of both. Such parameters are monitored and regulated by means of specialized control systems, including data management systems and PLC.

For optimum productivity micro cultures (or biomass) thickness of the layer of micro cultures test and maintain at the required value. Collection of culture can be carried out using several physical mechanisms and at different times during the year (depending on environmental conditions and the corresponding growth of certain types).

In some embodiments, when the conditions of data collection, a layer of micro cultures is passed over the Assembly unit and is pumped through a vibrating sieve where microculture separated and collected in the hopper for further processing. The liquid phase is collected and recycled back into the pond.

The collection procedure is controlled by programmable logic controller (PLC) and human machine interface (HMI).

Further discussion regarding the choice of the type of micro cultures, as well as its cultivation and harvesting can be found, for example, in published patent application U.S. 20080096267, filed March 15, 2007, and PCT published application WO 2007109066, filed March 15, 2007, entitled "SYSTEMS AND METHODS FOR LARGE-SCALE PRODUTION AND HARVESTING OF OIL-RICH ALGAE"; published patent application U.S. 20100151558, filed on March 12, 2009 and published PCT application WO 2008033573, filed September 13, 2007, entitled "TUBULAR MICROBIAL GROWTH SYSTEM"; provisional application for U.S. patent 61/171036, filed April 20, 2009 and published PCT application WO 2010123943, filed April 20, 2010, entitled "CULTIVATION, HARVESTING AND PROCESSING OF FLOATING AQUATIC SPECIES WITH HIGH GROWTH RATES"; and provisional application for U.S. patent 61/186349, filed on June 11, 2009, PCT published application WO 2010144877, filed on June 11, 2010, entitled "VEGETATION INDICES FOR MEASURING MULTILAYER MICROCROP DENSITY AND GROWTH". All prior patent applications are hereby incorporated by reference.

The method and system produce a variety of products in industrial production of biomass described in the present application may be adapted to obtain a product with the desired characteristics with a certain kind/mix of types of micro cultures that are used as raw materials. For illustration purposes, duckweed (growing in Florida) is indicated in the moment. In some part of the application duckweed is also specified as Duckweed. Products, described below, include protein concentrate (suitable, for example, as animal feed) and carbohydrate-rich stream that can be recycled in "biological raw materials" (suitable, for example, as raw material for the production of fuel) or a feed additive to�I is referred to as "flour of duckweed". It is intended solely as an example and should not limit the scope of the invention. The average specialist in the art will understand that the method and/or system described in the present application, are suitable for processing other microculture or organisms. Just as an example, the method and/or the processing system suitable for processing of marine algae, duckweed, websteri shipped, azolly, Salvini, water lettuce, etc., or a certain type/mixture of species of micro cultures, the raw material which is available in production volume.

Some advantages of the method and system produce a variety of products from industrial production of biomass described in the present application, include at least the following. The method and system may provide efficient production of commercially valuable products (for example, the dry protein concentrate, dry biosyrya suitable for the production of fuel, feed for animals or fish, etc) from cheap raw materials. The method and system can be environmentally friendly. The feedstock may include species or mixture of species that can be local and/or growing. In addition, many waste process (for example, water, the liquid phase obtained in the process, etc.) can be returned to the process with or without treatment. Just as an example, when biomass,�lucuuu water body, harvested for processing, significant amounts of water (or any other medium for cultivation) may be removed from the biomass and can be used again, for example, as the medium for cultivation, with or without treatment. The method and system are suitable for use on an industrial scale.

Used in this application "industrial scale" indicates that the method and system commercially applicable or suitable for the processing of large amounts of feedstock. Just as an example, the method and system described in the present application, allow processing of at least 100 kg, or at least 500 kg, or at least 1000 kg, or at least 1500 kg, or at least 2000 kg, or at least 2500 kg, or at least 3000 kg or more of raw materials per day, and can be carried out in a continuous or periodic mode.

Embodiments of the present invention provide a method of producing multiple products from biomass of aquatic organism. The method may include: obtaining biomass; destruction of biomass with getting destroyed biomass; separating the destroyed biomass with getting juice and the first solid phase; forming a wet protein concentrate using the juice; drying the wet protein concentrate to produce dry protein concentrate; production�tvo wet biosyrya by using the first solid phase; drying wet biosyrya obtaining at least one product selected from a dry biosyrya and carbohydrate-rich feed flour; where many products may include products selected from the dry protein concentrate, dry biosyrya and carbohydrate-rich feed flour, and where at least 50% of the protein in the multiple products is present on a dry protein concentrate.

The feedstock can be collected from the cultivation system, as described above. The feedstock may include biomass and water, or medium for the cultivation of the cultivation system. Biomass can include at least one of the following properties: rapid growth, low costs of cultivation, collection and processing, the high content of proteins, ecology or similar. In some embodiments, the biomass may include duckweed, seaweed, websteri shipped, Azolla, Salvinia, water lettuce, etc., or a combination thereof.

The feedstock can be transported using, for example, inclined vibrating screen, from the bioreactor to the dehydration. Dehydration can be located in the main processing building or facility, or within the bioreactor itself, depending on the needs of the consumer/local conditions or the size of the equipment. Water can flow through a sieve, then �AK wet biomass can enter the lower part of the sieve. The separation of water from the wet biomass can be amplified, for example, using low-amplitude vibration. Water can be pumped back to the bioreactor. Optional, to pump water back into the bioreactor, the level or composition of nutrients in it can be measured and/or modified, if necessary. A sieve can put the wet biomass collection system in which wet biomass is then transferred and fed to a typical grinding operation. Phase dehydration may include multiple passes and/or the types of dewatering methods in addition to inclined vibrating screen.

In some embodiments, the implementation of "dehydration" can refer to the procedure for removal of water from the feedstock. In some embodiments, the implementation of "dehydration" can refer to the procedure for removal of the juice (e.g., protein juice) from the solid phase.

In some embodiments, the destruction is carried out by mechanical means (also called grinding), for example, by prokalyvanie, shredding or slicing biomass with getting destroyed biomass. Thus, prokalyvanie can essentially rip, shred and slice biomass and listary biomass with the destruction of cell walls and release of water, protein and other components that become available. Interchangeable tipo�s operations include ball mill, colloid mill, knife mill, hammer mill, crusher, puree machine, filter press, etc., or a combination thereof.

Ball mill can operate in the presence of a horizontal or vertical cylinder, rotating on its axis, with abrasive materials inside. Just as an example, the rotation speed is 1 Hz, 10 Hz, or 20 Hz or 30 Hz, or 40 Hz, or 50 Hz, or 60 Hz, or 70 Hz, or 80 Hz, or 90 Hz, or 100 Hz, or 100 Hz, or 1 Hz to 10 Hz, or 10 Hz to 30 Hz, or 30 Hz to 50 Hz or from 50 Hz to 70 Hz 70 Hz to 90 Hz, from 90 Hz to 120 Hz. Typical abrasive materials may include balls, which consist of ceramic, stainless steel, glass, etc., or combinations thereof. Abrasives can rotate in a circular motion a ball mill. When lifting the abrasive material on the inner wall, then they can fall back down, splitting the duckweed. The constant movement of the balls moving against each other, can also provide the effect of grinding, which helps to grind the duckweed.

Colloid mill can operate by introducing the duckweed in a rotating series of grooves that provide high intensity grinding and shearing. Such forces can lead to rupture of duckweed.

In the cutting mill can be used rotating shaft on which the blades installed. The rotor may be rotational, oscillating�Xia at high speed the material is fed through a small hopper located inside. The material can be cut and removed through a mesh filter at the bottom of the mill. This is essentially to break listary duckweed, exposing the internal structure of the cell that allows you to remove more water and protein.

Hammer mill can operate similarly to the cutting mill, but instead of blades can be used large obtuse lobes. The blades can push the duckweed to corrugated the screen, creating high tension and shear, which can lead to rupture of the structure of plants. Once the structure is quite destroyed, a portion or essentially all of the internal components may be made available for extraction.

Examples of devices for grinding or crushing wet biomass, such as duckweed, are described solely for illustrative purposes and are not intended to limit the scope of the invention. The average person skilled in the art, after reading the descriptions, will be able to understand that other devices may be used to perform the function of shredding or destruction.

In some embodiments, the biomass is fed to the procedure of crushing (or grinding) with a constant speed, while in other embodiments, it comes with variable speed. In some�x embodiments, the biomass is fed to the procedure of crushing (or grinding) is continuous, while in other embodiments it arrives periodically. The speed and/or the method of delivery can be determined taking into account factors including the desired speed of production, the device(s) used in the process, the properties of raw materials, etc., or a combination of the above. In some embodiments, the feed rate is at least 10 kg/hour, or at least 50 kg/HR, or at least 100 kg/hour, or at least 200 kg/hour, or at least 300 kg/hour, or at least 400 kg/HR, or at least 500 kg/hour, or at least 600 kg/hour, or at least 700 kg/hour, or at least 800 kg/h, or at least 900 kg/hour, or at least 1000 kg/hour, or higher than 1000 kg/hour. In some embodiments, the feed rate ranges from 10 kg/HR to 200 kg/hour, or from 200 kg/HR to 400 kg/hour, or from 400 kg/HR to 600 kg/hour, or 600 kg/HR to 800 kg/hour, or from 800 kg/h to 1000 kg/hour, or higher than 1000 kg/hour.

In some embodiments, for the destruction of wet biomass using chemical methods. In specific embodiments, the destruction is carried out by changing the pH of the wet biomass. The pH value can be increased to more than 7.0, or above 7.5, or higher 8,0, 8,5 or higher, or higher to 9.0, or above 9.5, of 10.0 or higher. The pH of the wet biomass can be maintained within the limits of�Ah from 7.0 to 7.5, or from 7.5 to 8.0, or from 8.0 to 8.5, or from 8.5 to 9.0, or from 9.0 to 9.5, or from 9.5 to 10.0. The pH of the wet biomass may be in the range of from 7.0 to 14.0, or from 7.0 to 13.0, or from 7.0 to 12.0, or from 7.0 to 11.0, or from 7.0 to 10.0, or from 7.0 to 10.5, or from 7.0 to 10.0, or from 7.0 to 9.5, or from 7.0 to 9.0, or from 7.0 to 8.5, or about 7.0 to 8.0, or from 7.0 to 7.5. The pH value may be lowered to a pH below about 7.0, or below 6.5 or below 6.0 or below 5.5, or 5.0, or below 4.5 or below 4.0 or below 3.5, or less than 3.0. The pH of the wet biomass can be maintained in the range from 3.0 to 3.5, or from 3.5 to 4.0, or from 4.0 to 4.5, or from 4.5 to 5.0, or from 5.0 to 5.5 or from 5.5 to 6.0, or from 6.0 to 6.5, or 6.5 to 7.0. The pH of the wet biomass may be in the range of from 3.0 to 7.0, or from 3.5 to 7.0, or from 4.0 to 7.0, or from 4.5 to 7.0, or from 5.0 to 7.0, or from 5.5 to 7.0, or from 6.0 to 7.0, or from 6.5 to 7.0. In some embodiments, the feedstock comprising biomass and destroyed water or growth media after the destruction, flows directly to the following procedure for isolating the protein; in other embodiments, the feedstock is neutralized before being fed to the following procedure for the isolation of protein and/or other product(s).

In other embodiments, the destruction is carried out using a combination of mechanical and chemical methods.

In some embodiments, the bit�ions produced at room temperature or at atmospheric pressure. In other embodiments, the destruction is carried out at elevated temperature or pressure.

In some embodiments, the duckweed biomass is in the process of sanitary treatment (e.g. washing) before or after the procedure of destruction, for the purpose of removing toxins on the surface or included in the duckweed during the growth of organisms. This can be accomplished by contact of the duckweed biomass with a solution or solvent, or by immersion, spraying, or using other methods known in the art. The solution or the solvent can be an aqueous solution or solvent. The solution or the solvent may have a fever. The solution or the solvent can be sprayed under high pressure. In a variant implementation as a solution or solvent is water. There are several stages of washing. In some embodiments, the duckweed biomass is first subjected to contact with a solution or a solvent containing one or more components typically used for cleaning of crops such as fatty acids, alcohols or chlorine. After treatment in such a solution, or solvent-biomass is then again washed with water. This solution or the solvent can act as a disinfectant and Zn�significantly reduce the number of microorganisms, such as bacteria, viruses and fungi. The level of reduction of these microorganisms depends on several factors, including, for example, the concentration of oxidizing agents, the duration of contact, etc., or a combination thereof.

Just as an example, after dehydration of wet biomass, including duckweed, passes sanitization. In block sanitization separated macroscopic balances and larger natural organisms such as plants and animals (if possible or necessary). Then duckweed washed with water containing oxidizing solution or solvent. This solution or the solvent can act as a disinfectant and can significantly reduce the number of microorganisms, such as bacteria, viruses and fungi. The level of reducing the number of microorganisms depends on factors, including, for example, the concentration of oxidizing agents, the duration of contact with the duckweed, etc., or combinations thereof.

In some embodiments, crushed or destroyed duckweed is separated into a first solid phase and the juice. In some embodiments, the undefeated duckweed (e.g., duckweed, resulting from the dehydration procedures without grinding or crushing) process for separating the first solid phase and juice. In some embodiments �of sushestvennee a mixture of crushed or destroyed duckweed and undefeated duckweed process for separating the first solid phase and juice. The challenge was to provide an efficient method for processing large injection volumes with simultaneous implementation of separation where the maximum amount of soluble protein may continue with the flow of juice duckweed. Interchangeable typical operations include decanter centrifuge, belt press, centrifugal filter press, rotary press, screw press, filter press, finishing press, etc., or a combination thereof.

The decanter can be done by pumping a mixture comprising a solid phase and the juice, in a rotating cylinder. When the centrifugal force presses the solid material to the outer wall, the inner rotatable auger can move the solid material on the wall in the direction of the outlet at one end. End portion for release of solid material may have a decreasing radius along the screw, corresponding to the decreasing size. As you move the solid material along the slope formed by the decreasing radius, the solid material can flow from the sump depth in the rotor of the centrifuge, providing additional dehydration. Dewatered solids can then be continuously discharged. The juice can be pushed to the other end of the decanter under the action of centrifugal force, and during his transition to the other side of the solid phase can� to retire under the action of centrifugal force.

In the belt press can be used for mechanical compression, shredded or destroyed duckweed is placed between two tight straps with small micron-sized holes. Then the straps can pass through a series of rollers that squeeze the juice through the holes in the belt. Compacted solid material can then be extracted when these two straps are disconnected at the end of the model operation. The juice can drain in the tank in the bottom of the unit, where when you use the gravity he could go through the normal hole and go below for further processing.

In a screw press can be used mechanical compression to squash the inner juice of the destroyed litecom biomass. Screw press can perform the operation of presenting the material in a device that resembles a screw auger. The rotating shaft of the screw press can apply the material in the equipment, where as the material of the coils or the interval between the threads of the screw or decrease the shaft gets wider. Decreasing the spacing of the turns of the total volume between the threads is reduced, creating a compression effect. Duckweed can be compressed between such coils, and juice can be removed. The rotating shaft may be surrounded by a mesh filter small micron size, which can keep the wet biological raw materials in the pipe but allow the juice to come out. Remove juice can reduce the total moisture content in wet biological raw materials.

The filter press can operate using a piston pump and pump it out of the ground or destroyed duckweed in a number of filtration chambers. The filtration chamber can have a small micron-sized holes through which may extend juice and water under pressure of the piston pump. With sufficient accumulation of solid material in the filter, and when the juice is already impossible to continue to derive, the "spin" can be produced by spraying water or air into the elastic chamber between the filter chambers, exerting additional pressure on the pressed sludge. When inflating elastic chambers at the filter chamber may be additional pressure as the compression of the walls inside. Can "free" additional liquid (e.g. juice). Once removed a sufficient amount of juice, chamber filter press can be opened and hard pressed sludge can be discharged, then the solid material is supplied below for further processing, e.g., processing of biological raw materials in and/or processed into flour from duckweed.

Finish the press can operate similarly to a screw press, but instead of the screw threaded therein a rotating shaft with blades that can push the material along the sieve. The remaining solid phase material mo�em then be removed from the finish of the press.

In some embodiments, the separation procedure is performed with constant speed or variable speed. The separation procedure performed continuously or periodically.

In some embodiments, the separation procedure is carried out at room temperature or at atmospheric pressure. In other embodiments, the separation procedure is carried out at elevated temperatures or atmospheric pressures.

In some embodiments, the separation procedure involves a one-step separation, and wet biological raw materials includes a first solid phase. In other embodiments, the separation procedure involves a two-stage separation, or the separation is performed in three or more stages, with the first solid phase is treated in order to extract more juice, and the solid phase obtained in one stage may enter the next stage of separation. Several stages of separation can be performed using the same device for the separation. At least one stage can be performed using the device for separating different from the device used in another stage or stages. Additional removal of juice from the first solid phase has one or more advantages including a reduction in overall llagosta�Jania wet biosyrya, lower operating costs and the capital cost of the dryer for biosyrya, increased the efficiency of separation of juice from biomass; increased efficiency of isolating the protein from biomass, etc.

Just as an example, biomass in press belt press with getting juice and the first solid phase; and the first solid phase squeezed in a screw press to obtain additional quantities of juice and wet biosyrya. In some embodiments, belt press is the primary stage of pressing (or primary stage of separation of the juice) biomass. Biomass destroyed (or crushed) or undefeated, or any combination thereof, is fed from the hopper between the two perforated belt filters. These straps hold the biomass among themselves, passing through a series of rollers. As the belts pass through the rollers, the inner juice is removed from the biomass with getting juice and the first solid phase. The extracted juice consists of water and water-soluble compounds, such as soluble protein and minerals. When passing through the press the first solid phase is removed, e.g. by scraping. In some embodiments, the first solid phase is fed to the additional step of pressing. In some embodiments, in optional stage extrusion screw is used PR�SS. In a screw press using mechanical compression screw for pressing the remaining internal juice from the first solid phase with getting juice and wet biosyrya. In some embodiments, the juice obtained at this stage, combine with the juice obtained in the primary pressing stage and/or at any other stage(s) for further processing. After passing through a screw press, a pressed solid material, i.e., wet biological raw materials, are collected, for example, large mobile bins for subsequent processing such as drying.

As another example, the biomass destroyed (or crushed) or undefeated, or a combination, served in a decanter centrifuge for primary separation, for the purpose of extracting the juice and the first solid phase. The first solid phase is fed to one or more stages of mechanical compaction to further separate the juice from the first solid phase. The juice obtained in the centrifuge and in one or more stages of mechanical pressing, combine for further processing. If using single stage mechanical pressing, mechanical pressing get wet biological raw materials. If you use more than one stage of mechanical pressing, the solid phase obtained in one pressing stage may enter the next stage of pressing, and in the last� pressing stage biological raw materials get wet. One or more stages of mechanical pressing can be performed using a pressing device comprising a belt press, screw press, filter press, etc., or a combination thereof.

Examples of devices for separating the juice and the solid phase biomass, such as duckweed, are described solely for illustrative purposes and should not limit the scope of the invention. Average expert in the art when reading the description will be able to understand what to perform such functions can be used with other devices.

In some embodiments, the juice obtained in the procedure of separation, filtered to obtain a filtered juice and the second solid phase. Several different interchangeable standard operations can be used to filter large solids from the juice. Such common operations include the use, for example, vibrating separator, circular steps, linear vibrating screens/inclined movement, decanter centrifuge, filter press, etc., or combinations thereof.

Circular vibration separator operation can function and remove excess solid material when a stream of liquid (e.g. juice) on round vibrating surface. The surface of the separator may include a filter screen through which liquid can flow, and solid Mat�Rial may remain on the filter. Circular motion vibration provides pushing through the solid phase to the outer wall of the circular sieve, constant vibration and removal of the fluid. The solid phase can then be removed through the side opening where she can return to the process or be processed with wet biosystem. The liquid that passes through the first sieve, may be subjected to a second (or third) screening located below the sieve with holes of a smaller size. At the end of the process fluid (e.g., filtered juice) is collected in a solid container at the bottom of the unit and is removed where it can be fed below for further processing.

Vibrating sieve linear (or oblique) motion can function similarly to vibratory separators, circular steps, but instead of pushing the material to the outer wall of the circle to the solid phase can continuously vibrate along the stroke trajectory of linear vibrating screens until unloaded at the other end. Fluid can pass through the filter mesh in the same way as in the case of vibratory separators, circular steps, with the formation of the filtered juice, and to go below for further processing.

Can be used decanter centrifuge. The liquid with the solid phase may be fed into the cylindrical member that rotates, creating a centrifugal force on the Solid phase can be pressed against the outer wall, where a rotating auger conveys the solid phase to the outlet. The juice can come out on the other end, where the centrifugal force continues to separate the solid phase from the liquid with the formation of the filtered juice.

The filter press described elsewhere in the present description, can also be used to remove solid material from a liquid (e.g. juice), with the formation of the filtered juice.

Just as an example, the filtering may be performed using a filter. In some embodiments, used vibrating screen filter with holes 106 micrometers. The filter hole size than 106 micrometers, or filters avibration type can also be used. Suitable sizes of apertures for filtering procedures include the sizes of less than 1000 micrometers, or less than 800 micrometers, or less than 600 micrometers, or less than 500 micrometers, or less than 400 micrometers, or less than 300 micrometers, or less than 200 micrometers, or less than 180 micrometers, or less than 150 micrometers, or less than 120 micrometers, or less than 100 micrometers, or less than 90 micrometers, or smaller than 80 micrometers, or less than 70 micrometers, or less than 60 micrometers, or less than 50 micrometers, or less than 40 micrometers, or less than 30 micrometers, or less than 20 micrometers.

In some embodiments, the OSU�of estline filtration is carried out at room temperature or at atmospheric pressure. In other embodiments, the filtration is carried out at elevated or low temperatures or pressures, or vacuum.

In some embodiments, the second solid phase is fed to the separation procedure. In other embodiments, the second solid phase is combined with the wet biosystem obtained in the separation procedure, for further processing. In specific embodiments, the moisture content in wet biological raw materials is less than 90%, or less than 80%, or less than 70%, or less than 60%, or less than 50%, or less than 40% by weight.

In some embodiments, the filtered juice is clarified with obtaining a clarified juice and a third solid phase. The Brightener may be the final separation of the smaller particles in the filtered juice that were not removed in the filtering procedure before protein purification. This procedure is also referred to as tertiary treatment. This procedure may be optional, depending on a particular purpose of the target product. This residual solid material can have a very small particle size. The filtered juice may be clarified by, for example, high-speed disc centrifuge, microfiltration, ultrafiltration, etc., or combinations thereof. When using lightening fil�stimulated juice centrifuges, the clarified juice obtained in the Brightener, also known as filtered by centrifugation of the juice.

Can be used the high-speed disc centrifuge. The filtered juice can be fed into the centrifuge where centrifugal force can push the filtered juice outside of inclined disks in the direction of motion. The solid phase may be pushed down by the slope of the disks, and the juice is pushed up the discs to the outlet. The solid phase may be discharged continuously or periodically. Facing the solid phase forms a third solid phase, and leaving the juice forms a clarified juice.

In microfiltration and ultrafiltration can be used a porous membrane for separating unwanted particles depending on the particle size. The size and type of filter medium may vary for selective separation of the various components of the filtered juice.

The Brightener can ensure the removal of most of the carbohydrates and fiber in a third solid phase. In some embodiments, the third solid phase is supplied to the separation device, for example, decanter, belt press, screw press, etc., for additional protein in the third solid phase, reducing, thus, the loss of protein. In other embodiments, the third solid f�for may be combined with wet biosystem for further processing.

In some embodiments, the clarified juice is fed into the storage tank, for example, refrigerated container for storage until further processing. Cooled storage tank is maintained at a temperature below room temperature. In specific embodiments, a cooled storage tank is maintained at a temperature below 50°C or below 40°C, or below 30°C or below 25°C or below 20°C or below 15°C or below 10°C or below 5°C or below 2°C. Storage of the clarified juice at a low temperature until further processing can reduce proteolytic activity and, thus, can improve the separation efficiency of the protein during subsequent processing described below. The juice obtained in the Brightener may be called the clarified juice" or "post-treated juice". For example, the juice obtained in the Brightener is called "post-treated juice" before it goes into the storage container (e.g., container for juice), and is called "clarified juice after it comes out of storage containers (e.g., containers for juice). See, for example, Fig.37. In other embodiments, the clarified juice flows directly to subsequent processing without storage in storage tanks.

Blockadeha liquid may be processed for the purpose of coagulation of the protein from it � obtaining broth, comprising a wet protein concentrate. This procedure can also be defined as the deposition of protein. The protein deposition may be performed using heat treatment, acid treatment or other various methods. Blockadeha liquid may include clarified (or cleared) juice, filtered juice (if the Brightener did not), etc. In some part of the application blockadeha of the liquid is the clarified juice.

In some embodiments, the protein in the clarified juice is coagulated by treatment with acid (also called acid deposition), with decreasing, thus, the pH of the clarified juice. The pH value may be lowered to a pH below about 7.0, or below 6.5 or below 6.0 or below 5.5, or 5.0, or below 4.5. Lowering the pH of the clarified juice can cause some coagulation proteins and their deposition from the clarified juice with obtaining broth comprising a wet protein concentrate.

The pH of the clarified juice can be reduced using, for example, hydrochloric acid, sulfuric acid, etc., or combinations thereof. Acid can be added in a form in which it is used in the procedure. In alternative acid can be obtained byin situ. In the examples of implementation, which uses hydrochloric acid, the acid may b�you received in the form of anhydrous hydrochloric acid, or can be obtained byin situby adding sulfuric acid and sodium chloride to the clarified juice.

The temperature of the clarified juice with low pH can be maintained at room temperature, or below room temperature. Just as an example, may be maintained at a temperature below 30°C or below 25°C or below 20°C or below 15°C or below 10°C or below 5°C or below 0°C.

In other embodiments, the protein in the clarified juice can be coagulated by manipulation of temperature. In the present description, the procedure will be listed as thermocoagulation or thermoreceptive. In certain embodiments of the clarified juice can be fed at an appropriate rate in TermoSanitari (like a heat exchanger), which contains a number of heat exchangers. Heat exchangers can be with plate heat exchangers or heat exchangers type "pipe in pipe". Heating can also be achieved by a coolant, such as oil, water, steam, etc., or a combination of both. The coolant and clarified juice can interact in a co-current or counter flow. Used in the present application is co-current flow indicates that the temperature gradient of the coolant flow is oriented essentially in the same direction as the flow of the clarified juice in TermoSanitari; and the counter indicates that the temperature� gradient flow of the coolant is oriented essentially in the opposite direction relative to the flow of the clarified juice in TermoSanitari. In TermoSanitari clarified juice may be heated to a first temperature of from 40°C to 100°C, or from 50°C to 95°C, or from 60°C to 90°C, or from 70°C to 90°C, or from 80°C to 85°C. In TermoSanitari clarified juice may be heated to a first temperature above 40°C or above 50°C, or above 60°C or above 70°C, or above 80°C. Hot clarified juice can then be quickly cooled to a second temperature below 100°C, or below 90°C, or below 80°C, or below 70°C, or below 60°C or below 50°C or below 40°C, or below 30°C. the Cooling can be performed in less than 60 minutes, or less than 50 minutes, or less than 40 minutes, or less than 30 minutes, or less than 20 minutes, or less than 15 minutes, or less than 10 minutes or in less than 5 minutes, or less than 3 minutes, or less than 2 minutes, or less than 1 minute. Such heating and cooling may cause coagulation of the protein and its deposition from the clarified juice with obtaining broth comprising a wet protein concentrate. It should be understood that the heating and/or cooling can be performed in a device different from that described above.

Used in this application "broth" refers to a mixture comprising a wet protein concentrate, which is obtained by coagulation of the protein, e.g. by treatment with an acid or thermocoagulation (or thermopile�ation), etc., or combinations thereof.

Protein in the clarified juice can be coagulated by a combination of changes in pH and temperature changes. In certain embodiments of the protein in the clarified juice can be coagulated by manipulation of the temperature with obtaining broth comprising a wet protein concentrate. The broth, before or after partial removal of the wet protein concentrate can then go through the secondary coagulation of the protein by lowering the pH of the broth with the purpose of deposition of at least part of the protein remaining in the broth.

In some embodiments, a broth comprising a wet protein concentrate can be further processed to collect the wet protein concentrate. The remaining liquid phase is referred to as "waste liquid". This can be achieved, for example, using filtration, centrifugation or the like, or combinations thereof. Just as an example, the wet protein concentrate is collected from the broth by filtration using a membrane filter.

In other embodiments of the applied high-speed multi-disc centrifuge. Wet protein concentrate can be separated from the supernatant (referred to as "waste liquid"), using centrifugation. In the centrifuge waste liquid pushes�I in the upper part of the centrifuge under the influence of centripetal force and can be pumped, while more dense wet protein concentrate can be collected at the bottom and is periodically or continuously removed from the centrifuge. The spent fluid may undergo the process of coagulation and/or procedure for isolating the protein, as described above, the second time for the purpose of additional extraction of protein components. After performing these procedures liquid waste may be disposed or returned to a production system.

Wet protein concentrate, isolated from the broth can be washed with, e.g., water, to remove impurities. This washing procedure is optional. Just as an example, water is added to the wet protein concentrate and stirred for some time mixing, sufficient to achieve the desired mixing. The quantity and/or condition (e.g., temperature, pH, active cleaning agent, etc., or a combination) of water can be selected to optimize operation. If necessary, the water may also include an active cleaning agent. Washed wet protein concentrate can be collected at a mixture concentration of protein and wet wash water when using, for example, high-speed disc centrifuge, settling tank (or clarifier), decanter centrifuge, etc., or combinations thereof.

CME�ü wet protein concentrate and wash water can be subjected to another centrifugation with the use, for example, the high-speed disc centrifuge, in which washing liquid is removed (or supernatant) and extracted washed wet protein concentrate.

The settling tank or clarifier can operate at feed a mixture of wet protein concentrate and wash water in the tank, where the aggregation of coagulated proteins. The heavier particles containing the protein, separated from the washing liquid during the deposition under the action of gravity. The settling tank or clarifier may include a number of plates and/or plates, designed to improve the separation. The flush fluid is released from the sump, which may contribute to optimized allocation of protein (removal of the mixture).

Washed wet protein concentrate can then be dried using the dryer for protein.

Wet protein concentrate, isolated from the broth, or washed wet protein concentrate, if you use the washing procedure, can be chilled for storage with the aim of reducing the decomposition and preservation of high quality prior to further processing, including, for example, evaporation, drying, etc., or a combination of both. Just as an example, the wet protein concentrate (or washed wet protein concentrate) stored in refrigerated containers for storage until further about�of abode. Cooled storage tank can be maintained at a temperature below room temperature. In specific embodiments, a cooled storage tank is maintained at a temperature below 50°C or below 40°C, or below 30°C or below 25°C or below 20°C or below 15°C or below 10°C or below 5°C or below 0°C or below -5°C or below -10°C.

The wet protein concentrate (or washed wet protein concentrate) may have high moisture content (or water content), depending on the combination of unit operations. High moisture content (or water content) can directly affect costs and operating costs of the process, including, for example, the drying operation of the protein. Different moisture content (or water content) can also affect the types of protein dryers that are appropriate. Optional, may be included in the procedure to reduce evaporation of moisture content (or water content) of the wet protein concentrate (or washed wet protein concentrate) before the drying procedure. The evaporation may be performed, for example, by mechanical means, thermal (evaporation) funds, etc., or combinations thereof. Just as an example, evaporation is carried out using a filter press, evaporator, or the like, or combinations thereof.

Wyvern�th machine can remove moisture and/or volatile components from the material flow (e.g., the wet protein concentrate (or washed wet protein concentrate). Evaporator can be selected based on physical and morphological properties of the wet protein concentrate (or washed wet protein concentrate). Examples or types of evaporators include evaporator rising film evaporator falling film evaporator with natural circulation (vertical or horizontal), film evaporator with a stirrer, Multihull evaporator, etc. the Heat may be directly fed to the evaporation apparatus or indirectly via a heating jacket. Heat can come from a raw source (for example, burning natural gas, propane, etc. or steam from the evaporator), or from the waste heat stream (dryer exhaust). When you remove moisture from the wet protein concentrate (or washed wet protein concentrate), moisture content (or water content) can be reduced, reducing, thus, the total quantity of water that must be removed with a drying of the protein.

In some embodiments, the wet protein concentrate is dried to obtain a dry protein concentrate. The procedure of drying can reduce the moisture content in the wet protein concentrate (or washed wet baie�signed concentrate with or without the procedure of vaporization) to the desired level. The temperature of the drying procedure may not exceed the value that may have an adverse impact on the essential characteristics of the target product. Dry protein concentrate can be used as feed for fish, animal feed, feedstock for further processing (e.g., granulation), or the like, or combinations thereof. Just as an example, the dry protein concentrate used as a raw material to obtain a protein product with a higher concentration of proteins for human use. In particular, the dry protein concentrate some of the options for implementing an effective replacement of soy protein isolates, which are currently used in a large number of food products.

The drying procedure may be performed using, for example, spray dryer, double-drum dryer, flash dryer, etc., or combinations thereof. In some embodiments, inlet temperature (temperature at the inlet to the dryer) exceeds 25°C or below 50°C or above 75°C, or greater than 100°C, or exceeds 125°C, or higher than 150°C, or greater than 175°C, or greater than 200°C, or greater than 225°C, or greater than 250°C, or greater than 275°C, or greater than 300°C, or greater than 325°C, or exceeds�t 350°C, or exceeds 375°C, or greater than 400°C, or greater than 425°C, or greater than 450°C, or greater than 475°C, or greater than 500°C. In some embodiments, the inlet temperature is from 25°C to 50°C, or from 50°C to 75°C, or from 75°C to 100°C, or from 100°C to 125°C, or from 125°C to 150°C, or from 150°C to 175°C, or from 175°C to 200°C, or from 200°C to 225°C, or from 225°C to 250°C, or from 250°C to 275°C, or from 275°C to 300°C, or from 300°C to 325°C, or from 325°C to 350°C, or from 350°C to 375°C, or from 375°C to 400°C, or from 400°C to 425°C, or between 425°C and 450°C, or from 450°C to 475°C, or from 475°C to 500°C, or greater than 500°C. In some embodiments, the inlet temperature is from 50°C to 100°C, or from 100°C to 150°C, or from 150°C to 200°C, or from 200°C to 250°C, or from 250°C to 300°C, or from 300°C to 350°C, or from 350°C to 400°C, or from 400°C to 450°C, or from 450°C to 500°C, or greater than 500°C. In some embodiments, a target temperature (temperature at the exit from the dryer) is below 300°C, or below 275°C, or below 250°C, or below 225°C, or below 200°C. or below 175°C, or below 150°C or below 125°C, or below 100°C, or below 75°C, or below 50°C or below 25°C. In some embodiments, the final temperature is from 300°C to 275°C, or from 275°C to 250°C, or from 250°C to 225°C, or from 225°C to 200°C, or from 200°C to 175°C, or from 175°C to 150°C, or from 150°C to 125°C, or from 125°C to 100°C, from 100°C to 75°C, or from 75°C to 50°C, or from 50°C to 25°C or below 25°C. In some embodiments, about�of westline final temperature is from 300°C to 250°C, or from 250°C to 200°C, or from 200°C to 150°C, or from 150°C to 100°C, or from 100°C to 50°C, or from 50°C to 25°C or below 25°C.

Spray dryer can operate by feeding the material through a nozzle or spray gun, to create small droplets containing protein, which have a larger surface area (or increased ratio of surface area to volume). Increased surface area (or increased ratio of surface area to volume) can provide drying with increased efficiency. Hot air is fed directly into the drying chamber to dry the droplets containing protein, which can then be carried away by a current of air in the collection, such as a cyclone, a dust chamber or the like, or a combination of both. Just as an example, the wet protein concentrate (or washed wet protein concentrate) is fed from a cooled storage or centrifuges, or other, located at the entrance of the device to the spray dryer. In the spray dryer can be used high-speed centrifugal atomizer to spray a fine mist into a hot drying chamber. Fine mist can create a large surface area and, thus, increase the efficiency of drying. Water can evaporate when falling of small particles down. Dry� protein concentrate, also called dry of protein flour can then be collected using a cyclone separator, dust chamber or the like, or combinations thereof.

Double-drum dryer can be operated by rotating the two cylinders in opposite directions. The wet protein concentrate (or washed wet protein concentrate) can be fed to the surface of the cylinders or drums can be indirectly heated by steam. Direct contact with the hot surface can dry the wet protein concentrate (or washed wet protein concentrate). Then flakes (or dry protein concentrate) can be removed with a scraper from the surface of the cylindrical drums and to gather.

A flash dryer, and can take a wet protein concentrate (or washed wet protein concentrate) in a closed loop system, in which the hot air enters tangentially at the boundary. Hot air can carry wet protein concentrate (or washed wet protein concentrate) along the outer edge of the contour with the implementation of continuous drying and reducing the particle size. Once the particle size and moisture content (or water content) is reduced to the required levels, the product (dry protein concentrate) may be pneumatically fed into the trap, such as qi�LON, dust box or similar, or a combination thereof.

In some embodiments, the implementation uses the inverse of the mixing, when, for example, the moisture content (or water content) of the wet protein concentrate (or washed wet protein concentrate) is higher than a certain dryer can accept as input. Return the mixing is performed by mixing the dried end product (dry protein concentrate) with the wet protein concentrate (or washed wet protein concentrate), to increase the solids content in the feed to the dryer material.

In some embodiments, the dry protein concentrate, which comes out of the dryer, pack and/or hermetically Packed in a package or steel barrel industry standard having different sizes. Method of hermetic packaging industry compliant, can be used to guarantee proper conditions of storage and transportation. Package or barrel may include printed instructions or descriptions regarding, for example, their intended application, the expiration date, recommended storage conditions, transport conditions, composition, etc., or a combination thereof.

In some embodiments, the wet protein concentrate (or washed in�important protein concentrate) is subjected to the procedure of drying to reduce the moisture content (or water content), to obtain a dry protein concentrate. The moisture content (or water content) in a dry protein concentrate is less than 40%, or less than 30%, or less than 20%, or less than 10%, or less than 5% of the weight of the dry protein concentrate. The dry substance content in dry biological raw materials is at least 60% or at least 70% or at least 80% or at least 90% or at least 95% by weight of the dry biosyrya.

In some embodiments, the protein concentration (or purity) of dry protein concentrate can be from 30% to 95%, or from 40% to 90%, or from 50% to 85%, or from 60% to 80%, or from 70% to 75% by weight of the dry protein concentrate. In some embodiments, the protein concentration (or purity) of dry protein concentrate is more than 30%, or greater than 40%, or greater than 50% or exceeds 60%, or greater than 70%, or greater than 75%, or greater than 80% by weight of the dry protein concentrate. Other components of the dry protein concentrate can include carbohydrates, minerals, etc., or a combination thereof.

In some embodiments, the dry protein concentrate includes one or more essential amino acids. In some embodiments, the dry protein concentrate includes one or more amino acids selected from leucine, isoleucine, lysine, methionine, phenylalanine, threonine, tryptophan, valine, histidine, arginine, aspartic acid,serine, glutamic acid, Proline, glycine, alanine, tyrosine and cysteine. In some embodiments, the concentration of one essential amino acid is at least 1 g/100 g of dry protein concentrate, or at least 1.5 g/100 g of dry protein concentrate, or at least 2 g/100 g of dry protein concentrate, or at least 2.5 g/100 g of dry protein concentrate, or at least 3 g/100 g of dry protein concentrate, or at least 4 g/100 g of dry protein concentrate, or at least 5 g/100 g of dry protein concentrate, or at least 6 g/100 g of dry protein concentrate, or at least 7 g/100 g of dry protein concentrate, or at least 8 g/100 g of dry protein concentrate, or at least 9 g/100 g of dry protein concentrate, or at least 10 g/100 g of dry protein concentrate. In some embodiments, the concentration of one essential amino acid is evaluated by the percentage of the weight of the protein, purified from the dry protein concentrate, and is at least 1 g/100 g protein, or at least 1.5 g/100 g protein, or at least 2 g/100 g protein, or at least 2.5 g/100 g protein, or at least 3 g/100 g protein, or at least 4 g/100 g protein, or at least 5 g/100 g protein, or at least 6 g/100 g protein, or at least 7 g/100 g �tree, or at least 8 g/100 g protein, or at least 9 g/100 g protein, or at least 10 g/100 g protein.

In some embodiments, the dry protein concentrate includes the fat content is below 50% or below 40% or below 30% or below 25%, or below 20% or below 15% or below 10% or below 5% or below 4% or below 3% or below 2% or below 1% by weight of the dry protein concentrate. In some embodiments, the dry protein concentrate includes the fat content from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% by weight of the dry protein concentrate. In some embodiments, the dry protein concentrate includes the fat content from 1% to 50%, or from 2% to 40%, or from 5% to 30%, or from 8% to 20%, or from 10% to 15% by weight of the dry protein concentrate. Dry protein concentrate can be further processed to meet a desired fat content.

In some embodiments, the dry protein concentrate includes ash residue less than 50% or less 40% or less 30% or less 25% or less 20% or less 15% or less 10% or less 5% or less 4% or less 3% or less 2%, or less than 1% of the weight of the dry protein concentrate. In some embodiments, the dry protein concentrate includes bottom ash from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% by weight of dry boe�protein concentrate. In some embodiments, the dry protein concentrate includes bottom ash from 1% to 50%, or from 2% to 40%, or from 3% to 30%, or from 3% to 20%, or from 3% to 15%, or from 3% to 10%, or from 5% to 10%, or from 5% to 15% by weight of the dry protein concentrate. Dry protein concentrate can be further processed to meet a desired ash content.

In some embodiments, the dry protein concentrate includes a carbohydrate content less than 50% or less 40% or less 30% or less 25% or less 20% or less 15% or less 10% or less 5% or less 4% or less 3% or less 2%, or less than 1% of the weight of the dry protein concentrate. In some embodiments, the dry protein concentrate includes a carbohydrate content of from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% by weight of the dry protein concentrate. In some embodiments, the dry protein concentrate includes a carbohydrate content of from 1% to 50%, or from 2% to 40%, or from 5% to 30%, or from 8% to 20%, or from 10% to 15% by weight of the dry protein concentrate. Dry protein concentrate can be further processed to comply with the required carbohydrate content.

In some embodiments, the dry protein concentrate includes a fiber content less than 20% or less 15% or less 10% or less 8% or less 5% or less 4% or m�3%, or less than 2%, or less than 1% of the weight of the dry protein concentrate.

Just as an example, the dry protein concentrate obtained by the method described in the present application, includes the following composition shown in Table 2.

Table 2
Approximate composition of dry concentrated protein product
Product 1Product 2Product 3
% The solid phase≥90≥88-90≥95
% Moisture≤10≤12-10≤5
% Protein≥50from 60 to 80≥65-75
% Fat≤20from 5 to 20≤5-15
% Ash content≤15from 1 to 10≤2-10
% Carbohydrates≤20 from 5 to 20≤10-15
% Fibers≤10≤5≤5
%Other105-2010-15

In some embodiments, other characteristics of the dry protein concentrate, for example, particle size, bacterial composition, etc., or their combination, are appropriate for the intended purpose. In some embodiments, total contamination by bacteria is less than 100,000 CFU/g, or less than 80,000 CFU/g, or less than 60000 CFU/g, or less than 50,000 CFU/g, or at least 40,000 CFU/g, or less than 30,000 CFU/g, or less than 25,000 CFU/g, or less than 20,000 CFU/g, or less than 15,000 CFU/g. In some embodiments, the flour does not contain detectable level ofE. coli. In some embodiments, the flour does not contain detectable levels of Salmonella. In some embodiments, the flour includes yeast/fungi in an amount of less than 500/g, or less than 400/g, or less than 300/g, or less than 250/g, or less than 200/g, or less than 150/g, or less than 100/g, or less than 50/year.

Wet biological raw materials can be obtained by using any one or combination of the following procedures described above: procedures destruction procedures section�Oia, the filtering procedure and the procedure of clarification. Wet biological raw materials can be processed, as described above, for the purpose of additional extraction of protein components. Wet biological raw materials can be further processed, for example, by drying, to achieve the required characteristics (for example, the desired particle size and/or moisture content) for other applications. Dry biological raw materials can be used as feedstock for power plants, raw materials for biofuel production, etc., or combinations thereof. Dry biological raw materials can be further processed, for example, the granulation method, storage or use. Drying biosyrya may be performed using, for example, fluidized bed drier, turbulent dryers, flash dryers, drum dryers, rotary dryers, etc., or combinations thereof. In some embodiments, inlet temperature (temperature at the inlet to the dryer) exceeds 25°C or below 50°C or above 75°C, or greater than 100°C, or exceeds 125°C, or higher than 150°C, or greater than 175°C, or greater than 200°C, or greater than 225°C, or greater than 250°C, or greater than 275°C, or greater than 300°C, or greater than 325°C, or greater than 350°C, or exceeds 375°C, or greater than 400°C, or greater than 425°C, or greater than 450°C, or greater than 475°C, or greater than 500°C. In some embodiments, the input�the first temperature is from 25°C to 50°C, or from 50°C to 75°C, or from 75°C to 100°C, or from 100°C to 125°C, or from 125°C to 150°C, or from 150°C to 175°C, or from 175°C to 200°C, or from 200°C to 225°C, or from 225°C to 250°C, or from 250°C to 275°C, or from 275°C to 300°C, or from 300°C to 325°C, or from 325°C to 350°C, or from 350°C to 375°C, or from 375°C to 400°C, or from 400°C to 425°C, or between 425°C and 450°C, or from 450°C to 475°C, or from 475°C to 500°C, or exceeds 500°C. In some embodiments, the inlet temperature is from 50°C to 100°C, or from 100°C to 150°C, or from 150°C to 200°C, or from 200°C to 250°C, or from 250°C to 300°C, or from 300°C to 350°C, or from 350°C to 400°C, or from 400°C to 450°C, or from 450°C to 500°C, or greater than 500°C. In some embodiments, a target temperature (temperature at the exit from the dryer) is below 300°C, or below 275°C, or below 250°C, or below 225°C, or below 200°C, or below 175°C, or below 150°C or below 125°C, or below 100°C, or below 75°C, or below 50°C, or below 25°C. In some embodiments, the final temperature is from 300°C to 275°C, or from 275°C to 250°C, or from 250°C to 225°C, or from 225°C to 200°C, or from 200°C to 175°C, or from 175°C to 150°C, or from 150°C to 125°C, or from 125°C to 100°C, from 100°C to 75°C, or from 75°C to 50°C, or from 50°C to 25°C or below 25°C. In some embodiments, the final temperature is from 300°C to 250°C, or from 250°C to 200°C, or from 200°C to 150°C, or from 150°C to 100°C, from 100°C to 50°C, or from 50°C to 25°C or below 25°C.

The fluidized bed dryer can options�to uniroute and drying the material (for example, wet biological raw materials), feeding it on a vibrating surface, wherein hot air is supplied directly or indirectly to the material. Vibration and air can create a fluid suspension of material, which may increase the surface area exposed to drying. This effect can make the drying in a fluidized bed effective and scalable solution for drying wet biosyrya to the required parameters.

Turbulent dryer to dry wet biological raw materials in a container with a stirrer, in which the material is suspended under the action of air pressure, which creates the effect of a suspension. Reduced in size, the particles can then pass through the sorting device in the upper part of the drying chamber in the air flow in the trap, such as a cyclone, a dust chamber, etc., where the material is collected.

Flash dryers can operate with a supply of wet biosyrya in a closed loop. Hot air can be fed tangentially along the walls of the circuit that can cause wet biological raw materials constantly moving in the circuit and subjected to drying along the wall. During rotation of the material along the wall, which creates the air flow may be created by the effect of reduction of particle size, and as soon as the particle size becomes sufficiently small, the particles can flow freely from the air and post�AMB exhaust pipe, located in the inner part of the contour in the trap, such as a cyclone, a dust box, etc., for collection.

Drum dryer can be large capacity. It can work in batch mode, continuous mode or in semi-continuous mode. Capacity, when you turn on the dryer, can be rotated along the axis, the heat can come directly into the container, or indirectly through the heating jacket on the vessel. Hot air can be fed directly into a container for drying wet biosyrya directly; or heating oil may be fed into the heating jacket capacity for indirect heating and/or drying). Wet biological raw materials can be rotated until the moisture content (or water content) will not decrease sufficiently, and then deleted in a batch mode or in continuous mode.

Rotary dryer consists of a long cylindrical dryer in which wet biological raw materials may enter at one end and either under gravity or pneumatically, to go to the opposite end of the dryer. Heat can be supplied directly with the hot air enters the dryer in a co-current or counter-current, or indirectly, using warmed oil in the heating jacket, surrounding the outer wall of the dryer.

About�as an example, turbulent dryer is used for drying of wet biosyrya. Wet biological raw materials can be gathered in mobile bunkers and act in a turbulent dryer. In the turbulent dryer wet biological raw materials falls into equipped with a stirrer supply capacity turbulent dryer and then enters the drying chamber, equipped with a rotating stirrer. Hot air can flow through the wet biological raw materials, while the agitator breaks up any large lumps of wet biosyrya. Wet, heavy biological raw materials may be in the drying chamber until the water content is sufficiently low to biological raw materials has become quite easy to the flow of hot air could carry it in a cyclone separator. Dry biological raw materials can then be collected at the bottom of the cyclone.

In some embodiments, wet biological raw materials is subjected to the procedure of drying to reduce the moisture content (or water content), to obtain dry biosyrya. The moisture content (or water content) of dry biosyrya is less than 40%, or less than 30%, or less than 20%, or less than 10%, or less than 5% of the weight of the dry biosyrya. The content of solids in dry biological raw materials is at least 60% or at least 70% or at least 80% or at least 90% or at least 95% by weight of the dry biosyrya.

In some embodiments, the dry BIOSes�rd includes a protein content less than 50%, or less 40% or less 30% or less 25% or less than 20%, or less than 15%, or less than 10%, or less than 5% of the weight of the dry biosyrya. In some embodiments, dry biological raw materials includes the protein content from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% by weight of the dry biosyrya. In some embodiments, dry biological raw materials includes the protein content from 1% to 50%, or from 5% to 40%, or from 5% to 30%, or from 5% to 20%, or from 5% to 15%, or from 5% to 10%, or from 10% to 50%, or from 10% to 40%, or from 10% to 30%, or from 10% to 20%, or from 10% to 15% by weight of the dry biosyrya. Dry biological raw materials can be further processed to comply with the required protein content.

In some embodiments, dry biological raw materials includes the fiber content of less than 50%, or less than 40%, or less than 30%, or less than 20%, or less than 15%, or less than 10% of the weight of the dry biosyrya. In some embodiments, dry biological raw materials includes the fiber content from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% by weight of the dry biosyrya. In some embodiments, dry biological raw materials includes the fiber content from 1% to 50%, or from 5% to 40%, or from 5% to 30%, or from 5% to 20%, or from 5% to 15%, or from 5% to 10%, or from 10% to 50%, or from 10% to 40%, or from 10% to 30%, or from 10% to 20%, or from 10% to 15% by weight of the dry biosyrya. Dry biological raw materials can be further processed to�correspond to a desired fiber content.

In some embodiments, dry biological raw materials includes bottom ash in an amount of less than 50%, or less than 40%, or less than 30%, or less than 25%, or less than 20%, or less than 15%, or less than 10%, or less than 5% of the weight of the dry biosyrya. In some embodiments, dry biological raw materials includes bottom ash in an amount of from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% by weight of the dry biosyrya. In some embodiments, dry biological raw materials includes bottom ash in an amount of from 1% to 50%, or from 2% to 40%, or from 3% to 30%, or from 3% to 20%, or from 3% to 15%, or from 3% to 10%, or from 5% to 10%, or from 5% to 15%, or from 5% to 20% by weight of the dry biosyrya. Dry biological raw materials can be further processed to correspond to desired ash content.

In some embodiments, dry biological raw materials includes the fat content less than 50%, or less than 40%, or less than 30%, or less than 25%, or less than 20%, or less than 15%, or less than 10%, or less than 5% of the weight of the dry biosyrya. In some embodiments, dry biological raw materials includes the fat content from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% by weight of the dry biosyrya. In some embodiments, dry biological raw materials includes the fat content from 1% to 50%, or from 1% to 40%, or from 1% to 30%, or from 1% to 20%, or from 1% to 15%, or from 1% to 10%, or from 1% to 5%, or from 2% to 40%, or from 2% to 30%, or from 2% to 20%, or �t 2% to 15%, or from 2% to 10%, or from 2% to 5%, or from 3% to 30%, or from 3% to 20%, or from 3% to 15%, or from 3% to 10%, or from 3% to 5%, or from 5% to 10%, or from 5% to 15%, or from 5% to 20% by weight of the dry biosyrya. Dry biological raw materials can be further processed to meet a desired fat content.

In some embodiments, dry biological raw materials includes the carbohydrate content of more than 30%, or 40% or more 50% or more 60% or more 65% or 70%, or 75%, or 80%, or 85% of the weight of the dry biosyrya. In some embodiments, dry biological raw materials includes the carbohydrate content of from 30% to 90% or from 40% to 90%, or from 50% to 90%, or from 60% to 90%, or from 70% to 90%, or from 80% to 90%, or from 30% to 85%, or from 40% to 85%, or from 50% to 85%, or from 60% to 85%, or from 70% to 85%, or from 30% up to 80%, or from 40% to 80%, or from 50% to 80%, or from 60% to 80%, or from 70% to 80% by weight of the dry biosyrya. Dry biological raw materials can be further processed to comply with the required carbohydrate content.

In some embodiments, dry biological raw materials includes small quantities of volatile substances. In some embodiments, dry biological raw materials includes volatile substance in an amount of less than 1%, or less than 2%, or less than 5%, or less than 10%, or less than 15%, or less than 20% by weight of the dry biosyrya. In some embodiments, dry biological raw materials includes volatile substance in a quantity�TVE from 1% to 5%, or from 1% to 10%, or from 1% to 15%, or from 1% to 20%, from 2% to 10%, or from 2% to 15%, or from 2% to 20%, from 5% to 10%, or from 5% to 15%, or from 5% to 20% by weight of the dry biosyrya.

In some embodiments, dry biological raw materials includes energy value above 3 MJ/kg, or above 5 MJ/kg, or above 8 MJ/kg, or higher than 10 MJ/kg, or above 12 MJ/kg, or higher than 15 MJ/kg, or above 18 MJ/kg, or above 20 MJ/kg Dry biological raw materials can be further processed to correspond to the desired energy value.

Just as an example, dry biological raw materials obtained by the method described in the present application, includes the following composition shown in Table 3.

Table 3
The approximate composition of the product - dry biosyrya
Product AProduct BProduct C
% The solid phase≥90≥88-92≥95
% Moisture≤10≤12-10≤5
% Protein≤20from 10 to 20 ≤15-20
% Fat≤20from 5 to 20≤5-10
% Ash content≤15from 1 to 15≤5-10
% Carbohydrates≥50from 60 to 90≥65-70
% Fibers≤50≤40≤30-35
Energy (MJ/kg)≥10≥10≥15
%Other10%5-20%10-15%

Depending on the design of the dryer used in the drying procedure biosyrya, and/or customer requirements to product may not necessarily be performed granulation. Each dryer can produce a slightly different product and can be evaluated in order to determine the optimum dryer for the product parameters. Such parameters can also be compared with the customer requirements and to determine whether to produce the granulation of the final product�, or not.

Just as an example, if you perform granulation, then optimally matched the dryer is used for drying of wet biosyrya to a specific range of moisture content (or water content), and then dry biological raw materials is injected into small holes in the mold (or any form of on-demand customer or consumer) and compacted with rollers.

In some embodiments, dry biological raw materials that come out of the dryer and/or granulator, packing and/or hermetically Packed in a package or steel barrel industry standard having different sizes. Method of hermetic packaging industrial standard can be used to ensure proper conditions of storage and transportation. Package or barrel may include printed instructions or descriptions regarding, for example, their intended application, the expiration date, recommended storage conditions, transport conditions, composition, etc., or a combination thereof.

In some embodiments, dry biological raw materials used as feedstock for fuel production. Dry biological raw materials can be used as raw materials for oil refineries or coke oven plant. Dry biological raw materials can be used as raw material for burning. Dry biological raw materials can also be used as raw material for fer�entitiy.

In some embodiments, the flour (feeding meal for animals or fish), for example, flour of duckweed, if duckweed is used as a starting material, prepared from wet biosyrya through procedures similar to those used in the production of dry biosyrya. The differences in the final processing of flour (which can serve as a forage to cattle, pigs, fish, etc.) based on certain combinations of dryers and/or granulators. This combination should guarantee certain characteristics or properties of the product, which is required for the purpose of feeding, including, for example, moisture content (water content), shelf life, storage, grain size, grain size, texture, etc., or a combination of both. The need for a low moisture content (or water content) and/or a granulation can be performed using variants of the apparatus described above (or combinations thereof), regarding the production of dry biosyrya.

In some embodiments, wet biological raw materials is subjected to the procedure of drying to reduce the moisture content (or water content), to obtain flour. Moisture content (or water content) of flour is less than 40%, or less than 30%, or less than 20%, or less than 10%, or less than 5% of the flour weight. The solids content in the flour is at least 60%, or �ENISA least 70%, or at least 80% or at least 90% or at least 95% by weight of flour.

In some embodiments, the flour includes the protein content is below 50% or below 40% or below 30% or below 25%, or below 20% or below 15% or below 10% or below 5% of the dry weight of the flour. In some embodiments, the flour includes the protein content from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% of the flour weight. In some embodiments, the flour includes the protein content from 1% to 50%, or from 5% to 40%, or from 5% to 30%, or from 5% to 20%, or from 5% to 15%, or from 5% to 10%, or from 10% to 50%, or from 10% to 40%, or from 10% to 30%, or from 10% to 20%, or from 10% to 15% of the flour weight. Flour can be further processed to comply with the required protein content.

In some embodiments, the flour includes fiber content less than 50%, or less than 40%, or less than 30%, or less than 20%, or less than 15%, or less than 10% of the flour weight. In some embodiments, the flour includes fiber content from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% of the dry weight of the flour. In some embodiments, the flour includes fiber content from 1% to 50%, or from 5% to 40%, or from 5% to 30%, or from 5% to 20%, or from 5% to 15%, or from 5% to 10%, or from 10% to 50%, or from 10% to 40%, or from 10% to 30%, or from 10% to 20%, or from 10% to 15% of the flour weight. Flour can be added�individual processed to comply with the required fiber content.

In some embodiments, the flour comprises bottom ash in an amount of less than 50%, or less than 40%, or less than 30%, or less than 25%, or less than 20%, or less than 15%, or less than 10%, or less than 5% of the dry weight of the flour. In some embodiments, the flour comprises bottom ash in an amount of from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% of the flour weight. In some embodiments, the flour comprises bottom ash in an amount of from 1% to 50%, or from 2% to 40%, or from 3% to 30%, or from 3% to 20%, or from 3% to 15%, or from 3% to 10%, or from 5% to 10%, or from 5% to 15%, or from 5% to 20% of the flour weight. Flour can be further processed to meet a desired ash content.

In some embodiments, the flour comprises a fat content of less than 50%, or less than 40%, or less than 30%, or less than 25%, or less than 20%, or less than 15%, or less than 10%, or less than 5% of the dry weight of the flour. In some embodiments, the flour includes the fat content from 1% to 10%, or from 10% to 20%, or from 20% to 30%, or from 30% to 40% or from 40% to 50% of the flour weight. In some embodiments, the flour includes the fat content from 1% to 50%, or from 1% to 40%, or from 1% to 30%, or from 1% to 20%, or from 1% to 15%, or from 1% to 10%, or from 1% to 5%, or from 2% to 40%, or from 2% to 30%, or from 2% to 20%, or from 2% to 15%, or from 2% up to 10% or from 2% to 5%, or from 3% to 30%, or �t 3% to 20%, or from 3% to 15%, or from 3% to 10%, or from 3% to 5%, or from 5% to 10%, or from 5% to 15%, or from 5% to 20% of the flour weight. Flour can be further processed to meet a desired fat content.

In some embodiments, the flour comprises a carbohydrate content of more than 30%, or 40% or more 50% or more 60% or more 65% or 70%, or 75%, or 80%, or 85% of the flour weight. In some embodiments, the flour comprises a carbohydrate content of 30% to 90% or from 40% to 90%, or from 50% to 90%, or from 60% to 90%, or from 70% to 90%, or from 80% to 90%, or from 30% to 85%, or from 40% to 85%, or from 50% to 85%, or from 60% to 85%, or from 70% to 85%, or from 30% up to 80%, or from 40% to 80%, or from 50% to 80%, or from 60% to 80%, or from 70% to 80% by weight of flour. Flour can be further processed to comply with the required carbohydrate content.

In some embodiments, other parameters of flour, for example, particle size, texture, bacterial composition, etc., or a combination, are suitable for the intended purpose. In some embodiments, total contamination by bacteria is less than 100,000/g, or less than 80,000/g, or less than 60000/g, or less than 50,000/g, or less than 40000/g, or less than 30000/g, or less than 25,000/g, or less than 20,000/g, or less than 15000/g. In some embodiments, the flour does not contain detectable level ofE. coli. In some embodiments, implemented�I flour does not contain detectable levels of Salmonella. In some embodiments, the flour includes yeast/fungi in an amount of less than 500/g, or less than 400/g, or less than 300/g, or less than 250/g, or less than 200/g, or less than 150/g, or less than 100/g, or less than 50/year.

In some embodiments, the method provides for obtaining a variety of products from industrial production of feedstock biomass aquatic organism. Many products include dry protein concentrate and at least one selected from dry biosyrya and feed flour. The yield of each product can be estimated based on dry weight of the feedstock. Used in this application "dry weight" refers to weight of raw materials after drying, for example, in the drying chamber. This drying chamber may be, for example, a vacuum oven or the like.

In some embodiments, the yield of dry protein concentrate is at least 5% or at least 10% or at least 15% or at least 20% or at least 25% or at least 30% of the dry weight of the feedstock. In some embodiments, the yield of dry protein concentrate is from 5% -50%, or from 5% -40%, or from 5% -30%, or from 5% -25%, or from 5% -20%, or from 10% -50%, or from 10%-40%, or from 10%-30%, or from 10%-25%, or from 10%-20%, or from 15%-50%, or from 15%-40%, or from 15%-30%, or from 15%-25%, or from 15%-20%, or from 20%-50%, or from 20%-0%, or from 20% -30%, or between 20% -25% of the dry weight of the feedstock.

In some embodiments, the yield of dry biosyrya is at least 10% or at least 15% or at least 20% or at least 25% or at least 30% or at least 40% of the dry weight of the feedstock. In some embodiments, the yield of dry biosyrya is from 5% -60%, or 5% -50%, or from 5% -40%, or from 5% -30%, or from 5% -25%, or from 5% -20%, or from 10%-60%, or from 10% -50%, or from 10%-40%, or from 10%-30%, or from 10%-25%, or from 10%-20%, or from 15%-60%, or from 15%-50%, or from 15%-40%, or from 15%-30%, or from 15%-25%, or from 15%-20%, or from 20%-60%, or from 20%-50%, or from 20%-40%, or from 20% -30%, or between 20% -25% of the dry weight of the feedstock.

In some embodiments, the yield of flour is at least 10% or at least 15% or at least 20% or at least 25% or at least 30% or at least 40% of the dry weight of the feedstock. In some embodiments, the yield of flour is from 5% -60%, or 5% -50%, or from 5% -40%, or from 5% -30%, or from 5% -25%, or from 5% -20%, or from 10%-60%, or from 10% -50%, or from 10%-40%, or from 10%-30%, or from 10%-25%, or from 10%-20%, or from 15%-60%, or 15%-50%, or from 15%-40%, or from 15%-30%, or from 15%-25%, or from 15%-20%, or from 20%-60%, or from 20%-50%, or from 20%-40%, or from 20% -30%, or between 20% -25% of the dry weight of the feedstock.

In some embodiments, relative to the total amount of protein in many �of Reducto, at least 30% or at least 35% or at least 40% or at least 45% or at least 50% or at least 55% or at least 60% or at least 65% or at least 70% or at least 75% or at least 80% or at least 85% is present in the dry protein concentrate. In some embodiments, relative to the total amount of protein in many products, less than 70%, or less than 65% or less 60% or less 55% or less 50% or less 45% or less 40% or less 35% or less 30% or less 25% or less than 20%, or less than 15% is present in dry biological raw materials and/or flour.

Any of a liquid phase (for example, juice, filtered juice, clarified or cleared juice) or solid phase (for example, the first hard phase, the second solid phase, the third solid phase, wet biosyrya) obtained in the same procedure may be stored in storage tanks before entering one or more subsequent procedures or units. This can help you obtain a homogeneous liquid phase or solid phase for subsequent procedures (procedures) or system(s). This may allow to harmonize the various graphics or technological regimes, including, for example, continuous mode, periodic mode, or multiple feed streams in one or more subsequent procedures and/or devices. �idky phase in storage tanks can be maintained at required temperature to reduce the decomposition and preservation of high quality prior to further processing. Just as an example, the wet protein concentrate (or washed wet protein concentrate) stored in refrigerated containers for storage until further processing. Cooled storage tank can be maintained at a temperature below room temperature. In specific embodiments, a cooled storage tank maintained at a temperature below 50°C, or below 40°C, or below 30°C or below 25°C or below 20°C or below 15°C or below 10°C or below 5°C or below 0°C or below -5°C or below -10°C.

The efficiency of the process of isolating the protein from biomass, comprising a water body can be further improved by using any one or combination of the following procedures.

In some embodiments of the biomass, including the water body, can be processed to extract the lipid components using a solvent and/or water, for example, hexane, ethanol, etc., or combinations thereof, as a preliminary preparation before the process of isolating the protein or further processing. In other embodiments of the biomass, including the water body may be treated to remove components of biomass, which can be such as lipids. This procedure can be immediately applied to wet biomass before drying, or it may be applied with the juice�m, obtained after separation of the initial biomass (or dehydrated biomass). The procedure can be performed by adding solvent or water to the material, followed by the addition of acid (hydrochloric, nitric or other). The material is then mixed, in some embodiments, in conditions of high temperature or pressure. In other embodiments, the mixing is carried out at room temperature and atmospheric pressure. Then the mixture enters the decanter. In the specified machine the mixture is rotated at high speed, and the liquid contained therein is forced through holes for separating the solid mass from the liquid.

In some examples of the implementation of the pH-value of one or more of the following: feedstock, comprising the destroyed biomass, juice obtained by the procedure of separation, filtered juice obtained by the filtering procedure, or the clarified juice obtained by the procedure of clarification, can be changed. In certain embodiments of the pH value of raw materials, including the destroyed biomass, can be raised to a pH above 7.0, or above 7.5, or higher 8,0, 8,5 or higher, or higher to 9.0, or above 9.5, of 10.0 or higher. The pH value of the raw material can be enhanced, for example, by adding NaOH or other substances known �verifizierung specialists. Similarly, can improve the pH value of the filtered juice. The pH value can be maintained throughout the rest of the process for isolating the protein. The pH change can be neutralized after the procedure, which must be altered pH value.

Stay within any part of the process of isolating the protein can be optimized to increase the efficiency of the process. In some embodiments of the residence time can be selected to increase the secretion of soluble proteins in the unclarified juice after passage through the filter press.

In other examples of implementation procedures to improve the effectiveness of the process include the dilution of the destroyed biomass with water to increase the excretion of soluble protein components in the unclarified juice after passage through a filter press, sonication destroyed biomass for increasing the allocation of soluble protein components in the unclarified juice after passage through a filter press, destroyed processing of biomass enzymes by carbohydrazone, individually or in combination, the processing of any of the solid phases obtained in the processes described above, enzymes proteases, individually or in combination, to reduce the protein content and/or ash residue, and increase with�holding of carbohydrates, the performance of chromatographic processes and solubilization water-insoluble protein (e.g., by changing pH) in any of the solid phases obtained in the process of isolating the protein described above.

Embodiments of the invention also provide a system for the allocation of multiple products from biomass of aquatic organism; such systems may include, for example: block destruction for destruction of biomass with getting destroyed biomass; a separation unit for separating the destroyed biomass with getting juice and a solid phase; block forming a wet protein concentrate using the juice; a drying unit of protein for drying the wet protein concentrate to produce dry protein concentrate; and drying unit wet biosyrya obtaining at least one product selected from a dry biosyrya and carbohydrate-rich flour, where wet biological raw materials may include a solid phase; and where many products may include products selected from, for example, the dry protein concentrate, dry biosyrya, carbohydrate-rich flour, etc., and where at least about 50% of the protein in the multiple products is present on a dry protein concentrate.

Table 4 presents an exemplary apparatus that may be included in the blocks described above.

tr>
Table 4
Exemplary devices
Option
Block destructionColloid mill, cutter mill, ball mill, hammer mill, crusher, puree machine, filter press
The separation unitBelt press, decanter centrifuge, centrifugal filter press, rotary press, screw press, filter press, finishing press
Block forming a wet protein concentrateVibration separator, vibrating screen filter, vibrating separator, circular steps, linear vibrating screen/horizontal motion, decanter centrifuge, filter press, high speed disc centrifuge, microfiltration, ultrafiltration, TermoSanitari, acid deposition, settling tank, clarifier
Block drying proteinSpray dryer, drum dryer, flash dryer

It should be understood that the exemplary apparatus for each block are listed solely for the purpose of illustration, and are not intended to limit the scope of the invention. A combination from�azannyh or other devices or units may be included in such a system for the intended application based on the descriptions in this application.

EXAMPLES

The following non-limiting examples are presented to further illustrate the embodiments of the present invention. Qualified specialists will be obvious that the techniques disclosed in the examples that follow represent approaches the inventors of that function well in the practice of the invention, and thus, as one can imagine, are examples of ways of its practical implementation. However, professionals in the art, given the present description should be understood that in certain embodiments of the disclosed, may be made many changes, and thus can be obtained in this or a similar result, without deviation from the essence and scope of the present invention.

Example 1 - Exemplary method for processing duckweed

In the present application describes an exemplary method for processing of duckweed. The method was verified experimentally.

During harvest the automated collection system extracted an equal number of micro cultures, for example, duckweed, with certain areas in the production system, including ponds (bioreactors), and a slurry containing the biomass (also called feedstock), is fed through the pump system on the tilt of vibration�e sieve. Suspension of biomass sieve was collected and fed into the hammer mill blade type in which listary wet biomass was destroyed with the release of internal water and protein. Alexdurai juice of these litecom then removed by successive pressing in a belt press and screw press. Wet biological raw materials discharged from the screw press, and collected for drying in the turbulent dryer, while the juice was filtered using vibrating separator. The filtered juice is comprised of fine solid particles were removed by centrifugation. Then the protein in the centrifuged juice was subjected to coagulation by reducing the pH centrifuged juice or thermocoagulation when using the heat exchanger with obtaining broth comprising a wet protein concentrate. Wet protein concentrate was then separated using a high-speed multi-disc centrifuge. The supernatant was discarded, whereas the wet protein concentrate was subjected to drying using spray dryer. The dried product was Packed.

Although in this example it is not fulfilled, the duckweed biomass can be further processed to reduce the amount of ash, lipids, or other undesirable components in the final product.

After washing rack� homogenized, mixed, pressed juice, clarified by centrifugation, filtered and the solution was subjected to exposure to low pH for the precipitation of proteins and obtain a broth comprising a wet protein concentrate. The broth is centrifuged to obtain a precipitate comprising a wet protein concentrate. The precipitate is then washed and clarified by centrifugation, and then subjected to drying to obtain a dry protein concentrate.

Dry protein concentrate thus obtained consisted of 50-80% protein by weight.

The suspension of the biomass collected from the cultivation system, filed in the industrial building, where it was evaporated and extruded in a number of stages to extract its inner juice. Larger particles (first solid phase) is then removed from the juice by filtration using a vibratory separator (vibrating screen filter).

a. Obtaining

i. Inclined vibrating screen

Suspension of biomass is hydraulically applied in industrial building, pumping biomass with a large portion of water in the production building. The biomass was separated from water by using an inclined vibrating screen. Water is passed through a sieve and came back to the ponds (bioreactors), whereas biomass was held in the lower part of the sieve under the action of low-amplitude vibration. With SITA wet biomass was received into the hopper sloping�about the auger. In this feed auger was used Archimedes screw for feeding the fresh biomass into the hopper of hammer mill flat-blade (cutter mill) at a constant speed. Additional benefits when using the screw conveyor was the fact that he allowed the excess water to drain from the wet biomass due to the inclination of the auger.

ii. Knife mill

In the cutting mill used horizontal rotating shaft on which the blades were installed. The rotor is rotated at high speed, the suspension of the biomass was done through a small hopper mounted inside. Suspension of biomass destroyed and removed through a sieve at the bottom of the mill. This mill cut listary biomass with the release of internal cell structures, which ensured the removal of a larger amount of internal water and protein.

iii. Belt press

Belt press was the primary stage of pressing for the destroyed biomass. Destroyed biomass was pumped from the hopper to the space between the two perforated belt filters. These belts are passed through a series of rollers. With the passage of the belt through the rollers were removed, the internal juice. The juice consisted of water and water-soluble compounds, such as soluble protein and minerals. After pressing the first solid phase was removed with a scraper and hearth�Ali secondary pressing stage.

iv. Screw press

Screw press was a secondary pressing stage to the first solid phase of the destroyed biomass. Use mechanical compression screw for pressing at least part of the remaining internal juice from the first solid phase. After passing through the screw press extruded solid material (also called wet biosystem) were collected in large mobile bins for drying.

v. Vibration separator

The juice flowed from the screw press vibrating screen filter with holes of 10-200 microns. It was filtered large particles that passed through a screw press. Solids (purees), also called the second solid phase, came back in a screw press, while the filtered juice was sent to the protein purification. Return to the process of the second solid phase allow pressing an additional quantity of juice from the second solid phase.

b. The protein purification

After filtering through a vibrating sieve, filtered juice is then purified to highlight concentrated protein. During this purification used centrifugation and coagulation.

i. Centrifuge (bleaching)

The filtered juice was pumped through the high-speed multi-disc centrifuge for removal of smaller particles that were not removed in a vibratory separator. On Dunn�m phase was also removed most of the carbohydrates, and also fibers. A third solid phase leaving the centrifuge, were sent back to the screw press to reduce the loss of protein. Then centrifuged juice (also called clarified juice) pumped in a cooled container for storage until further processing.

ii. Coagulation protein

Proteins in the centrifuged juice is coagulated by lowering the pH. The pH was lowered to pH below 5 when using either hydrochloric or sulfuric acid. The process of processing the acid was causing coagulation and precipitation of at least part of the protein, resulting in the received broth comprising a wet protein concentrate.

In the alternative, the centrifuged juice was pumped with adjustable flow rate in the precipitator containing a number of plate heat exchangers. In the heating zone of the precipitator centrifuged juice was heated to about 40-90°C. Then centrifuged juice, which is now called bouillon, quickly cooled to a temperature in the range of 10-40°C. Such heating and cooling caused coagulation and precipitation of protein from centrifuged juice with obtaining broth comprising a wet protein concentrate.

iii. Centrifuge (Separation of protein)

Wet protein concentrate was separated from the rest of the broth. The broth was passed through a high-speed multi-disc centrifuge holds�have to separate the wet protein concentrate from the supernatant, called "liquid waste". In the centrifuge waste liquid is pushed into the upper part of the centrifuge under the influence of centripetal force and was evacuated, while more dense protein wet concentrate is collected at the bottom and is periodically unloaded from the centrifuge. Wet protein concentrate was then washed with water to remove impurities and centrifuged again. Wet protein concentrate after this second centrifugation was cooled in storage for reducing the decomposition and preservation of high quality before drying.

c. Drying

Wet biological raw materials and wet protein concentrate was applied to a drying process to reduce their water content to 8-12%. Wet biological raw materials are dried using turbulent drier, while wet protein concentrate was dried using a spray dryer. After drying the wet protein concentrate called dry protein concentrate.

i. Drying biosyrya

Wet biological raw materials after the screw press is collected in mobile bunkers. Wet biological raw materials are then filed in a turbulent dryer via a supply capacity turbulent dryer, equipped with a stirrer. Wet biological raw materials were delivered from the supply tank into the drying chamber, equipped with a rotating stirrer. The hot air passed through the wet biological raw materials, p�and this stirrer smashed any large lumps. Wet, heavy biological raw materials remained in the drying chamber until the water content (also called moisture content) does not become low enough that the material is becoming quite easy, could be carried away by the cyclone separator a stream of hot air. Then dry biological raw materials collected in the lower part of the cyclone.

ii. Drying protein

Wet protein concentrate was pumped from a refrigerated store in a spray dryer. In the spray dryer was used a high-speed centrifuge spray gun to spray a fine mist into a hot drying chamber. Fine mist created a larger surface area, enhancing, thus, the drying efficiency. The water evaporated in the fall of small particles to the bottom. Then dry protein concentrate, also called dry of protein flour was collected using a combination cyclone separator and dust camera.

iii. Packing

Dry biological raw materials and dry protein concentrate coming out of the dryer, Packed in bags of varying size and tightly Packed after analysis on moisture content.

It should be understood that some of the steps described above are optional, and to obtain the same or similar functions can be used in devices other than those listed in the example. Some advanced�tive exemplary processing methods described elsewhere in this application.

Example 2 - protein expression

This example describes a method of separating protein from duckweed. The method was tested experimentally.

During harvest automated data acquisition system was periodically extracted equal amounts of micro cultures, for example, duckweed, with certain areas in the production system, including ponds (bioreactors), and containing biomass slurry (also called feedstock) was supplied by a pumping system for inclined vibrating screen. Suspension of biomass collected and fed into the hammer mill blade type in which the wet listary biomass destroyed with the release of internal water and protein. Containing large amounts of protein the juice of these litecom then removed by successive pressing in a belt press and screw press. Wet biological raw materials extracted from the screw press, and collected for drying in the turbulent dryer, while the juice was filtered using a vibratory separator. The filtered juice is comprised of fine solid particles were removed by centrifugation. Protein in the centrifuged juice is then coagulated by heating using a heat exchanger, having a broth comprising a wet protein concentrate. Then the wet protein concentrate was separated using high-speed multi-drive prices�refuge. The supernatant was discarded and the wet protein concentrate was dried using a spray dryer. The dried product was Packed up.

a. Obtaining

i. Inclined vibrating screen

Suspension of biomass is hydraulically applied in industrial building, pumping biomass with a large portion of water in the production building. The biomass was separated from water by using an inclined vibrating screen. Water is passed through a sieve and came back to the ponds, whereas biomass was held in the lower part of the sieve under the action of low-amplitude vibration. With SITA wet biomass is unloaded into the hopper inclined screw conveyor. At the specified feed auger was used Archimedes screw for feeding the fresh biomass into the hopper of hammer mill flat-blade (cutter mill) at a constant speed. Additional benefits when using the screw conveyor was the fact that he allowed the excess water to drain from the wet biomass due to the inclination of the auger.

ii. Knife mill

In the cutting mill used horizontal rotating shaft on which the blades were installed. The rotor is rotated at high speed, the suspension of the biomass was done through a small hopper mounted inside. Suspension of biomass destroyed and removed through a sieve at the bottom of the mill. This mill cut sheet�biomass particle with the release of the internal structure of cells which ensured the removal of a larger amount of internal water and protein.

iii. Belt press

Belt press was the primary stage of pressing for the destroyed biomass. Destroyed biomass was pumped from the hopper to the space between the two perforated belt filters. These belts are passed through a series of rollers. With the passage of the belt through the rollers were removed, the internal juice. The juice consisted of water and water-soluble compounds, such as soluble protein and minerals. After pressing the first solid phase was removed with a scraper and filed at the secondary stage of pressing.

iv. Screw press

Screw press was a secondary pressing stage to the first solid phase of the destroyed biomass. Use mechanical compression screw for pressing at least part of the remaining internal juice from the first solid phase. After passing through the screw press extruded solid material (also called wet biosystem) were collected in large mobile bins for drying.

v. Vibration separator

The juice flowed from the screw press vibrating screen filter with holes of 10-200 microns. It was filtered large particles that passed through a screw press. Solids (purees), also called the second solid phase, came back to snakemistress, whereas the filtered juice was sent to the protein purification. Return to the process of the second solid phase allow pressing an additional quantity of juice from the second solid phase.

b. The protein purification

After filtering through a vibrating sieve, filtered juice is then purified to highlight concentrated protein. During this purification used centrifugation and coagulation.

i. Centrifuge (bleaching)

The filtered juice was pumped through the high-speed multi-disc centrifuge for removal of smaller particles that were not removed in a vibratory separator. At this stage we also removed a large portion of carbohydrates, and fibers. A third solid phase leaving the centrifuge, were sent back to the screw press to reduce the loss of protein. Then centrifuged juice (also called clarified juice) pumped in a cooled container for storage until further processing.

ii. Coagulation protein

Centrifuged juice was pumped with adjustable flow rate in the precipitator containing a number of plate heat exchangers. In the heating zone of the precipitator centrifuged juice was heated from about 80°C to 85°C. Then centrifuged juice, which is now called bouillon, rapidly cooled to 10-40°C. Such heating and cooling caused coagulation and sardanapale of centrifuged juice with obtaining broth, comprising a wet protein concentrate.

iii. Centrifuge (Separation of protein)

Wet protein concentrate was separated from the rest of the broth. The broth was passed through a high-speed multi-disc centrifuge for separation of wet protein concentrate from the supernatant, called the waste liquid. In the centrifuge waste liquid is pushed into the upper part of the centrifuge under the influence of centripetal force and was evacuated, while more dense protein wet concentrate is collected at the bottom and is periodically unloaded from the centrifuge. Wet protein concentrate was then washed with water to remove impurities and centrifuged again. Wet protein concentrate after this second centrifugation was cooled in storage for reducing the decomposition and preservation of high quality before drying.

c. Drying

Wet biological raw materials and wet protein concentrate was applied to a drying process to reduce their water content to 8-12%. Wet biological raw materials are dried using turbulent drier, while wet protein concentrate was dried using a spray dryer. After drying the wet protein concentrate called dry protein concentrate.

i. Drying biosyrya

Wet biological raw materials after the screw press is collected in mobile bunkers. �lanoe biological raw materials are then filed in a turbulent dryer, throwing it into the supply capacity of the turbulent dryer, equipped with a stirrer. Wet biological raw materials were received in a drying chamber equipped with a rotating stirrer. The hot air passed through the wet biological raw materials, while the agitator smashed any large lumps. Wet, heavy biological raw materials remained in the drying chamber until the water content (also called moisture content) does not become low enough that the material is becoming quite easy, could be carried away by the cyclone separator a stream of hot air. Then dry biological raw materials collected in the lower part of the cyclone.

ii. Drying protein

Wet protein concentrate was pumped from a refrigerated store in a spray dryer. In the spray dryer was used a high-speed centrifuge spray gun to spray a fine mist into a hot drying chamber. Fine mist created a larger surface area, enhancing, thus, the drying efficiency. The water evaporated in the fall of small particles to the bottom. Then dry protein concentrate, also called dry of protein flour was collected using a combination cyclone separator and dust camera.

iii. Packing

Dry biological raw materials and dry protein concentrate coming out of the dryer, Packed in bags of varying size and tightly Packed� after analysis on moisture content.

Example 3 is a Block diagram of an exemplary method of separating protein

Fig.2 shows a block diagram of an exemplary method of separating protein from aquatic organism, for example, fresh duckweed.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a knife mill, in which the wet listary biomass destroyed with the release of internal water and protein. Destroyed biomass filed on belt press, which destroyed the biomass is extruded with the first solid phase (as indicated on the Figure as "Wet biological raw materials belt press") and juice (indicated on the Figure as "Raw juice belt press"). The first solid phase was applied to a screw press for more pressing since the juice (indicated on the Figure as "Raw juice expeller") and wet biosyrya. The first solid phase is, remaining in a belt press, washed with water (as indicated on the Figure as "Flush water belt filter"). The washed solid phase band filter, thus obtained, was served in a screw press for additional compaction. Wet biological raw materials extracted from the screw press, and collected for drying using a dryer biosyrya turbulent dryers) obtaining dry biosyrya. Raw juice belt press, and the raw juice of screws�th press was combined with the receipt of the combined raw juice and it was served in a vibrating sieve, in which the combined raw juice was filtered with getting puree, involving recycled solid phase), and filtered juice. Mashed potatoes were served in a screw press for additional compaction. The filtered juice was stored in containers for juice 1. The juice container 1 is cooled storage tank. The filtered juice from the tank for clarified juice of 1 when using centrifuges with obtaining centrifuged the solid phase from the filtered juice and filtered juice by centrifugation (also called "clarified juice"). Centrifuged solids from filtered juice was served in a screw press for subsequent pressing. Centrifuged solids from filtered juice was used as a wet biosyrya. Filtered by centrifuging the juice is kept in the tank for juice 2 and its pH was adjusted to pH below 7,0. Then filtered by centrifugation of the juice was processed in the precipitator to cause thermoinduced coagulation protein with obtaining broth comprising a wet protein concentrate. In other embodiments, a protein in is filtered by centrifuging the juice is coagulated by acid treatment, combination treatment with acid and heat treatment. To separate the protein from the rest of the broth, the broth is centrifuged with a semi�the amount of waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. Wet protein concentrate was washed or diluted by adding water to the wet protein concentrate, with formation of a solution of a wet protein concentrate. The wet protein concentrate to water is from 1:1 to 1:10 by weight. The resulting solution was wet protein concentrate was dried using the dryer for protein (spray dryer) to produce dry protein concentrate. Dry protein concentrate packaged for later use or analysis.

Fig.2, each dotted line represents recyclezone mass flow, and each letter or combination of letters/numbers in the hexagon indicates a sampling or material code.

Example 4 - the Yield of dry protein concentrate and wet exit biosyrya

Fresh duckweed was processed according to the method shown in Fig.2 and described in Example 2, for about one month.

Fig.3 shows the output of the wet biosyrya (indicated by "biological raw materials"), selected in D3 in Fig.2, and the yield of dry protein concentrate (labeled "Dried protein") selected in O1 in Fig.2. In this application axes, t�such as D1, D2, D3 and so on, denote the number of batches of samples analyzed.

Results are expressed as the ratio of the mass biosyrya or dry protein concentrate to the mass of fresh duckweed, processed to obtain these products. The horizontal axis indicates the code of the party. With regard to each pair of columns for the same code party, the left column shows the result for biosyrya, and the right column shows the result for the dried protein.

The relative data are shown in Fig.3. This chart demonstrated that a significantly higher proportion of the solid phase remains in the stream biosyrya compared with the protein flow.

Example 5 - the Output of wet and dry protein concentrate

Fig.4 shows the moisture content (water content) in the wet protein concentrate at the point I1 in the process shown in Fig.2 and performed in Example 4. Results are expressed as a percentage of mass of water to the weight of the wet protein concentrate. The horizontal axis indicates the codes of the party.

Fig.5 shows the purity of the protein obtained in the same process, depending on the party. Results are expressed as the percentage weight of a protein by weight of dry protein concentrate. The horizontal axis indicates the codes of the party.

Fig.5 shows that the purity of the protein obtained in a dry protein concentrate� showed a range 52-67% for this time period.

Example 6 - Out wet and dry biosyrya

Fig.6 shows the moisture content (water content) in wet biological raw materials obtained from the screw press and selected at the point D3 in Fig.2. Results are expressed as the percentage ratio of water mass to the total mass of wet biosyrya. The horizontal axis indicates the codes of the party.

Fig.7 shows the composition of dry biosyrya depending on the party obtained in the process shown in Fig.2. Results are expressed as the percentage ratio of the mass of a certain product to the total mass of dry biosyrya. The horizontal axis indicates the codes of the party. In each column corresponding to one of the party, from the bottom up, the first bar indicates the moisture content; the second bar indicates the protein content; the third band indicates the ash content; the fourth band indicates the fat content; the fifth band indicates the content of crude fibre; and the sixth bar shows the available carbohydrates.

Fig.7 shows that the dry biological raw materials were rich in carbohydrates, in the form of available carbohydrate and crude fiber.

Example 7 - out wet and dry biosyrya

Fig.8 shows the volume of harvested duckweed in a pilot facility in two months. The dark gray bar indicates the weight of wet duckweed, which was processed soon after harvest; the light grey bar indicates wet weight OC�Ki, which was placed in storage for subsequent processing; and a strip of medium-gray color indicates the weight of wet duckweed, which is sent for processing to the adjacent object.

Example 8 - the Distribution of the solid phase in the model operations

Fig.9 shows an example of the distribution of the solid phase after the destruction and pressing, as described in Fig.2, fresh duckweed, obtained as described above. The pressing was carried out sequentially belt press and screw press. The belt is washed using water for washing the belt filter, and washed solid phase with a band filter returned in a screw press. Results are expressed as the percentage ratio of the mass of the solid phase in a biological raw materials (corresponding to wet bisiriyu (D3) of Fig.2) or juice (corresponding to combined raw juice (E1) of Fig.2) to the mass of the solid phase in the destroyed biomass (C1 in Fig.2). These figures, and the figures relating to the distribution of the solid phase in different flows of products in the following examples, were obtained by drying samples biosyrya and juice with obtaining the weight of solids contained in them. The quantities specified put, getting the total amount of the solid phase in the destroyed biomass. The horizontal axis indicates the codes of the party. With regard to each pair of columns to the same code of the party, �the left column shows the amount of solid phase in a biological raw materials, and the right column shows the amount of solids in the juice. The average mass of the solid phase in a biological raw materials was 23.5% by weight of the destroyed biomass, of which 21% was from wet biological raw materials, while 2.5 percent were solid phase, washed with a band filter. Solids in the juice were, on average, 76.5% of the solid phase in the destroyed biomass.

Fig.10 shows an example of the distribution of the solid phase after the transmission of the combined raw juice through vibration separator, as shown in Fig.2. Results are expressed as the percentage ratio of the mass of the solid phase in puree (Q1 corresponding to "Puree (Recyclebank solid phase)" (Q1) in Fig.2) or juice (F1 corresponding to "Filtered juice" from the container for juice 1 Fig.2) to the mass of the solid phase in the combined raw juice (E1) in Fig.2. The horizontal axis indicates the codes of the party. With regard to each pair of columns to the same code of the party, the left column lists the result for mashed potatoes (Q1), and the right column shows the results for juice (F1).

Fig.10 shows an exemplary test result of the solid phase distribution for a vibratory separator.

Fig.11 shows a rough calculation of how you can calculate the distribution of the material in Fig.9 and Fig.10. Box is bounded by a dashed line and marked "A" corresponds to the results shown in the �IG.9, and the box is bounded by a dashed line and labeled "B" corresponds to the results shown in Fig.10. In A, after the destruction and pressing on a belt filter press (FP) and a screw press (SP), the average solid phase in a biological raw materials (corresponding to "Wet bioart" (D3) of Fig.2) was 23.5% of the solid phase in the biomass of fresh duckweed, while the average solids in the juice (the corresponding "Combined raw juice" (E1) of Fig.2), was 76.5% of the solid phase in the biomass of fresh duckweed. In B, after passing through the vibratory separator in the second stage of dehydration, the average mashed potatoes (Q1, corresponding to "Puree (Recyclebank solid phase)" in Fig.2) was 28% solids in combined raw juice, while the average solids in the filtered juice (F1 corresponding to "Filtered juice" from the container for juice 1 Fig.2) was 72% of the solid phase in the combined raw juice. Thus, on average the combined wet biological raw materials, including wet biological raw materials obtained after passing through a filter press and screw press, and recyclezone solid phase obtained after filtration of the combined raw juice when using vibratory separator accounted for 44.9% of the solid phase in the biomass of fresh duckweed, while the average solids in the filtered juice with�Talala 55% of the solid phase in the biomass of fresh duckweed.

Fig.12 shows the distribution of the solid phase after the filtered juice was subjected to bleaching in a centrifuge, as shown in Fig.2. Results are expressed as the percentage ratio of the mass of solids in centrifuged the solid phase (Q2 corresponding to "the Centrifuged solid phase from the filtered juice" in Fig.2) or juice (F5 corresponding to "Filtered by centrifugation juice" in Fig.2) to the mass of solids in the filtered juice (F1) in Fig.2. The horizontal axis indicates the codes of the party. With regard to each pair of columns to the same code of the party, the left column shows the result for mashed potatoes centrifuge (centrifuged solids, Q2), and the right column shows the result for juice (F5).

Fig.12 shows an exemplary test of the solid phase distribution and clarifying centrifuges.

Fig.13 shows the result of an approximate test of the distribution of the solid phase after the transmission of the filtered juice by centrifugation through a precipitant for protein coagulation. Results are expressed as a percentage (estimated) lost a solid phase ("Loss") or mass of solids in the broth (H1 in Fig.2) to the mass of solids in the filtered juice by centrifugation prior to the deposition (F6 in Fig.2). The horizontal axis indicates the codes of the party. With regard to each pair of columns for the same code pairs�AI, the left column shows lost weight, and the right column shows the mass of the broth precipitator (H1).

Fig.13 shows that a large part of the solid phase has passed through the precipitator for further processing.

Also evaluated the distribution of the solid phase resulting from the separation of protein in the centrifuge. In this example (step 6, Fig.15) the solid phase in the waste liquid (supernatant) was 70% of the solid mass of the broth before centrifugation, whereas the solid phase in a wet protein concentrate obtained from sludge, 30% solids in the broth.

Fig.14 shows an example of selection of product that relates to the efficiency of the dryer of protein. Fig.14 shows that, on average, the dry protein concentrate was 63% weight solids wet protein concentrate, while an average of 37% weight solids wet protein concentrate was lost in the drying procedure.

For example, Table 5 summarizes the results shown in Fig.9-14.

Table 5
The summarized results of the solid phase distribution
Typical operationStageThe mass of solids in the juice (thread protein)The mass of solids in t�Erdem product (other streams/ stream biosyrya) Total
Knife millStage 1100,0%0,0%100%
Belt + screw press + filter beltStage 276,5%23,5%100%
Vibration separatorStage 372,0%28,0%100%
Clarifying centrifugeStage 471,0%29,0%100%
The protein precipitantStage 587,0%13,0%100%
Separation centrifugeStage 630,0%70,0%100%
Spray dryerStage 763,0%37,0%100%

On f�G. 15 shows an example of the results presented in Table 5. With regard to each pair of columns for the same stage, the left column shows the proportion of the mass of solids to the treatment received in the juice passed into protein, and the right column shows the proportion of the mass of solids prior to treatment obtained in the solid phase, transformed into other/biological raw materials.

Fig.16 shows an example of calculating the release of the protein product. Stages 1-3 in Table 5 and Fig.15 include "Dehydration - extraction solid phase" in Fig.16, while Steps 4 through 7 in Table 5 and Fig.15 include a "separation of the solid phase" in Fig.16. In this example, the dry protein concentrate averaged 6% of the mass of solids in the biomass of duckweed. It was confirmed quantities of the dried protein, obtained experimentally, as shown in Fig.3.

Example 9 is a Block diagram of an exemplary method of separating protein

Fig.17 shows a block diagram of an exemplary method of separating protein from duckweed.

In General terms, this method involves the destruction and/or compaction of the biomass of duckweed (also called suspension of biomass or feedstock) to produce juice and biosyrya ("biological raw materials large press"; the process is called "the Destruction of dehydration #1" and "Extraction #1"); filtration and/or clarification of the juice with other juice and additional biosyrya ("biological raw materials small Pres�a"; the process is called "Dehydration #2 clarification" or "Extraction #2"); coagulating protein from the filtered or clarified juice with obtaining blocksdelaware broth (called "Coagulation protein"); and the division of broth with obtaining the protein product and the waste liquid (called "protein Separation"). The spent fluid is returned to the pond (bioreactor).

Fig.18 contains a more detailed block diagram showing an exemplary method of isolating the protein from duckweed, shown in Fig.17.

As shown in Fig.18, duckweed cultivated in the system of cultivation, as described above. Suspension of biomass, including the collected duckweed (also called feedstock), is fed through a pumping system (e.g., Pump station) on a vibrating sieve (A0-A5), and then in the upper part of the inclined screw conveyor (B). From the top of the inclined screw conveyor (B) suspension of biomass was served in a knife mill (C), in which the wet listary biomass was destroyed with the release of internal water and protein. Destroyed biomass was served in a large screw press, which destroyed the biomass is extruded with getting wet biosyrya (D2) and juice. Wet biological raw materials (D2) dried (Drying manufacturer"), to obtain dried biosyrya (called "Dried biosystem big press" (P2), while the juice was filtered using vibra�ion separator with getting puree (recyclebank solid phase, Q1) and juice (called "Raw juice/dry juice) (E1 and E2). Mashed potatoes (Q1) was served in a small screw press for more pressing since the juice and extra wet biosyrya (D1). It's a wet biological raw materials (D1) was dried using turbulent dryer to obtain dried biosyrya (called "Dried biosystem small press" (P1), whereas the second juice was served in a vibratory separator for filtering. Raw or processed juice (E1 and E2), leaving SITA, was clarified using a centrifuge with getting puree (Puree centrifuge") (Q2) and the clarified juice. This stage is also called "Centrifuge #1." Clarified juice was stored in a cooled container, where it says "Filtered juice refrigerated volume (F and G). Clarified juice then passes through the precipitator or treatment with an acid for coagulation proteins with obtaining broth comprising a wet protein concentrate. The broth was stored in tanks of broth (H1 and H2). To separate the protein from the rest of the broth, the broth is centrifuged to obtain the waste liquid (J1 and J2) and the wet protein concentrate (I1 and I2). This stage is also called "Centrifuge #2." The spent fluid is returned back to the pond for cultivation (bioreactor) or disposed of. Wet protein concentrate was washed or R�bavlyali water. Wet protein concentrate was dried using spray drying to obtain dried protein product (dry protein concentrate, O1 and O2). The dried protein product packaged for later use or analysis.

Example 10 - Distribution of the solid phase in the model operations

Duckweed was treated according to the method shown in Fig.17 and Fig.18 and described in Example 9.

Fig.19 shows the relative allocation of the solid phase on standard operations in the process shown in Fig.17 and Fig.18. The results are shown as the percentage ratio of the mass of solids in the juice or protein product (raw juice or processed E1 and E2 juice, clarified juice or broth), or in other products (puree, wet biological raw materials, waste liquid, etc.) to the mass of the solid phase in primary source material, each individual unit operations. The horizontal axis are standard operations. "Extraction dehydration #1" corresponds to the "Extraction #1" in Fig.17; "Extraction dehydration #2" corresponds to the "Extraction #2" in Fig.17;" the Deposition" is the process of the coagulation of protein in the precipitator of Fig.18; whereas processes, called "Centrifuge #1", "Centrifuge #2" and "spray Drying" correspond to the same processes as shown in Fig.18. With regard to each pair of columns to the same code of the party, l�the first column shows the flow biosyrya, and the right column shows the flow of protein.

Fig.20 shows an example of the distribution of the solid phase after Extraction, Dehydration #1 and Extraction Dewater #2 shown in Fig.19. Box surrounded by a dotted line and marked "A" corresponds to the Extraction process, Dewater #1, and the field is surrounded by a dotted line and marked "B" corresponds to the Extraction process, Dewater #2. Fig.20 shows that in this example, after the processes of Extraction, Dehydration #1 and Extraction Dewater #2, on average, 62% of the solid phase in the biomass of duckweed is present in biological raw materials, including biological raw materials large press and small biological raw materials of the press," whereas 38% of the solid phase in the original duckweed biomass is present in the juice.

Fig.21 shows an example of the calculation of the yield of dry protein concentrate-based mass flow in standard operations. "Solid phase extraction" in the Figure includes the Extraction, Dehydration #1 and Extraction Dewater #2 of Fig.19, while "the Separation of the solid phase" of the Figure includes the processes "Centrifuge #1", "Deposition", "Centrifuge #2" and "spray Drying Fig.19. On average, the dry protein concentrate is 8.5% of the initial biomass of duckweed by weight.

Example 11 - protein expression in the model operations

The duckweed biomass was processed in accordance with the methods shown in Fig.17 and Fig.18, and described in Example 9.

Fig.22 shows protein expression in typical operations in the way shown in Fig.17 and Fig.18. Results are expressed as the percentage weight of a protein or blocksdelaware juice or other products that lead to biseru or other products (puree, wet biological raw materials, waste liquid, etc.) by weight of the composition forming the starting material of the respective individual unit operations. The horizontal axis are the individual unit operations. "Extraction, Dehydration #1" corresponds to the "Extraction #1" of Fig.17; "Extraction, Dehydration #2" corresponds to the "Extraction #2" Fig.17"; "Precipitator" corresponds to the process of coagulation of the protein in the precipitator shown in Fig.18; and "Centrifuge #1", "Centrifuge #2" and "spray Drying" are the same processes in Fig.18, respectively. For each pair of columns corresponding to the same code of the party, the left column shows the results for biosyrya and other products, and the right column shows the results for protein and blocksdelaware juice. For example, the starting material in the Extraction process, Dewater #1 is duckweed biomass; Fig.22 shows that after the biomass is in the process of Extraction, Dehydration #1, biological raw materials ("biological raw materials large press") is on average 20% of the mass of the initial biomass, whereas in environments�eat resulting juice was 80% of the biomass of duckweed.

Fig.23 shows how the computation of the output protein based on the mass flow in standard operations. At this Shape "Protein Extraction" includes the processes of Extraction, Dehydration #1 and Extraction Dewater #2 of Fig.22, while "protein Separation" includes the processes Centrifuge #1, Deposition, Centrifuge #2 and spray Drying of this Shape. Protein yield is on average 12% of the duckweed biomass by weight.

Example 12 - Distribution of the solid phase in the model operations

The duckweed biomass was processed in accordance with the methods shown in Fig.17 and Fig.18 and described in Example 9.

Fig.24 shows the distribution of the solid phase after clarification, raw or processed juice (E1 and E2) in the centrifuge. Specified lightness corresponds to the first centrifugation process in Fig.18, which got mashed potatoes (Fig.18 "Exit puree with centrifuges" (Q2)) and the filtered juice. "Exit puree with centrifuges" (Q2) in Fig.18 corresponds to the "Puree centrifuges" for which Fig.24 presents data on the composition, whereas the filtered juice of Fig.18 corresponds to the broth prior to the deposition, for which data are also shown in Fig.24. Results are expressed as a percentage of the mass of an individual component puree centrifuges or broth prior to the deposition of the weight of the same component in the material subjected to the process of�of wetline, which in this case was raw or processed juice (E1 and E2). On the horizontal axis components are specified. For each pair of columns of the same component, in the left column shows the results for puree of the centrifuge, while the right column shows the results of the broth prior to the deposition.

Fig.25 shows the distribution of the solid phase after precipitation of the filtered juice to coagulate the protein. Precipitation at this Shape corresponds to the process thermoinduced coagulation of protein in the precipitator of Fig.18. "Calculation of losses" indicates the estimated amount of solid phase, lost in the procedure of deposition, whereas the Broth after the precipitation" refers to the broth obtained after deposition procedure. Results are expressed as a percentage of the mass of an individual component in the calculated loss or broth after the precipitation of the weight of the same component in the pasteurized stuff that was broth before precipitation, the composition of which is shown in Fig.24. The horizontal axis shows the various components. For each pair of columns of the same component, in the left column shows the results for estimated losses, and the right column is the number of the component in the broth after deposition.

Fig.26 shows the distribution of the solid phase after the broth obtained in the process to�gulali protein centrifuged in order to isolate proteins (this corresponds to the process Centrifuge #2 in Fig.18). "WPC" corresponds to the wet protein concentrate obtained after the removal of the waste liquid from the broth after the precipitation. Results are expressed as a percentage of the mass of an individual component in a WPC or in the waste liquid to the weight of the same component in the material, subjected to a process Centrifuge #2, who was the broth after deposition Fig.25. The horizontal axis shows the various components. For each pair of columns of the same component, in the left column shows the amount of a component in a WPC, whereas the right column shows the amount of constituent in the waste liquid.

Fig.27 shows the distribution of the solid phase after drying the wet protein concentrate spray. Spray drying WPC, obtained from the second centrifugation, gives a dry protein concentrate (Dry protein"). Some solid mass lost ("Water + estimated losses"). Results are expressed as a percentage of the mass of the dry protein or lost in weight to the weight of the same component in the material, which was dried by spraying, which was wet protein concentrate, obtained from the second centrifugation. On the horizontal axis are different�e components. For each pair of columns of the same component, in the left column shows the number of the component in a Dry protein, whereas the right column shows the quantity of a component in the lost weight.

Fig.28 shows the summarized results of the mass flow associated with the results shown in Fig.24-27. After extraction of the solid phase from biomass (including the Extraction of #1 and/or Extraction #2, shown in Fig.17), 38% of the solid phase in the original biomass remained in the raw juice. The raw juice is on average contained 38% of the solid phase in the original biomass of duckweed. The raw juice was subjected to centrifugation (Centrifuge #1 in Fig.28) for clarification of juice. There was obtained puree (solid precipitate) comprising, on average, 31% of solids in the raw juice, and the juice (supernatant) comprising, on average, 66% of solids in the raw juice. The juice was subjected to thermal or acid treatment for coagulation proteins, with obtaining broth. On average, 5% of the solid phase present in the juice before treatment, were lost during processing, while the average 95% of the solid phase present in the juice before treatment, remained in the broth after treatment. Specified the treated broth is then centrifuged (Centrifuge #2) for separation of proteins; in this process, on average, lost 14% of the solid phase in broth, whereas 86% t�ERDAS phase in broth remained in the protein product (wet protein concentrate). The protein product was subjected to spray drying, during which, on average, lost 41% of the solid phase in a wet protein concentrate, whereas 59% of the solid phase in a wet protein concentrate remained in the final protein product (dry protein concentrate). Thus, on average, 8.4% of the solid phase in the duckweed was turned into the final protein product (dry protein concentrate). This result is consistent with the result shown in Fig.21.

Example 13 is a Block diagram of the process and the place of sampling

Fig.29 shows a block diagram of an exemplary method of separating protein from aquatic organism, for example, fresh duckweed. The method was tested experimentally.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a knife mill, in which the wet listary biomass destroyed with the release of internal water and protein. Destroyed biomass filed in the belt press with water for washing the belt filter and extruded destroyed biomass with a first solid phase (as indicated on the Figure as "Wet biological raw materials belt press") and juice (indicated on the Figure as "Raw juice belt press"). The first solid phase was served in a screw press with a second juice (indicated on the Figure as "Raw juice expeller") and wet biosyrya. First�th solid phase, remaining in a belt press, washed with water (as indicated on the Figure as "flush Water belt filter"). The washed solid phase band filter, thus obtained, was served in a screw press for additional compaction. Wet biological raw materials extracted from the screw press, and collected for drying using a dryer for biosyrya turbulent dryers) obtaining dry biosyrya. Raw juice belt press, and the raw juice of a screw press was combined with the formation of the combined raw juice and served in a vibratory separator in which the combined raw juice was filtered with getting puree, including recyclezone solid phase, and filtered juice. Mashed potatoes were served in a screw press for additional compaction. The filtered juice was stored in containers for juice 1. The juice container 1 was a storage tank, preferably cooled. The filtered juice from the tank for clarified juice of 1 when using centrifuges with obtaining centrifuged the solid phase from the filtered juice and filtered juice by centrifugation (also called "clarified juice"). Centrifuged solids from filtered juice was served in a screw press for additional compaction. Centrifuged solids� of filtered juice was used as a wet biosyrya. Filtered by centrifuging the juice stored in the juice container 2 and adjusted to a pH below 5 and left overnight. The temperature was maintained below 35°C. is Filtered by centrifuging the juice was processed in the precipitator to cause thermoinduced coagulation protein with obtaining broth comprising a wet protein concentrate. The broth is centrifuged to obtain the waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. The wet protein concentrate ("WPC") is washed three times after dilution by adding water to the wet protein concentrate with the formation of the washed wet protein concentrate. The wet protein concentrate to water ranged from 1:1 to 1:10 by weight. The resulting washed wet protein concentrate was dried using the dryer for protein (spray dryer) to produce dry protein concentrate.

Fig.29, each solid arrow indicates the flow of the process, each dotted arrow indicates recyclezone mass flow, whereas each letter or combination of letters/numbers in the hexagon indicates the location of the selection of the sample or material code. �of tetki "pH was adjusted to < 5 and left at night, the Temperature was maintained at <35°C and WPC (I1) were washed 3 times with (1:1-1:10 WPC:H20) and re-centrifuged" are corrections made to the method.

Example 14 is a Block diagram of a method

Fig.30 shows a block diagram of an exemplary method of separating protein from aquatic organism, for example, fresh duckweed. The method was tested experimentally.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a knife mill, in which the wet listary biomass destroyed with the release of internal water and protein. Destroyed biomass filed in the belt press, which destroyed the biomass is extruded with the first solid phase (as indicated on the Figure as "Wet biological raw materials belt press") and juice (indicated on the Figure as "Raw juice belt press"). The first solid phase was applied to a screw press for more pressing since the juice (indicated on the Figure as "Raw juice expeller") and wet biosyrya. The first solid phase is, remaining in a belt press, washed with water (as indicated on the Figure as "flush Water belt filter"). The washed solid phase band filter, thus obtained, was served in a screw press for additional compaction. Wet biological raw materials, otvlechenno� of expeller, collected for drying when using the dryer for biosyrya turbulent dryers) obtaining dry biosyrya. Raw juice belt press, and the raw juice of a screw press was combined with the formation of the combined raw juice and served in a vibratory separator in which the combined raw juice was filtered with getting puree, including recyclezone solid phase, and filtered juice. Mashed potatoes were served in a screw press for additional compaction. The filtered juice was placed for storage in the juice container 1. The filtered juice from the tank for clarified juice of 1 when using centrifuges with obtaining centrifuged the solid phase from the filtered juice and filtered juice by centrifugation (also called "clarified juice"). Centrifuged solids from filtered juice was served in a screw press for additional compaction. Centrifuged solids from filtered juice was used as a wet biosyrya. Filtered by centrifuging the juice is kept in the tank for juice 2, while its pH was adjusted to 8.5, stood at 8.5 for one hour and then adjusted to a final pH of 7.0. Then filtered by centrifugation of the juice was processed in the precipitator to cause thermoinduced coagulation baie�ka with obtaining broth, comprising a wet protein concentrate. In other embodiments, a protein in is filtered by centrifuging the juice is coagulated by treatment with acid, the combination of acid treatment and heat treatment. To separate the protein from the rest of the broth, the broth is centrifuged to obtain the waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. Wet protein concentrate was washed or diluted by adding water to the wet protein concentrate with the formation of the washed wet protein concentrate. The resulting washed wet protein concentrate was dried using a protein of the dryer (spray dryer) to produce dry protein concentrate. Dry protein concentrate packaged for later use or analysis.

Fig.30 each solid arrow indicates the flow of the process, each dotted arrow indicates recyclezone mass flow, and each letter or combination of letters/numbers in the hexagon indicates the location of the selection of the sample or material code. The grade of "Bringing pH (NaOH) to 8.5, soak for one hour, and then brought to a final pH of 7.0" suggests�t correction method.

Example 15 is a Block diagram of a method

Fig.31 shows a block diagram of an exemplary method of separating protein from aquatic organism, for example, fresh duckweed. The method was tested experimentally.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a knife mill, in which the wet listary biomass destroyed with the release of internal water and protein. Destroyed biomass filed in the belt press, which destroyed the biomass is extruded with the first solid phase (as indicated on the Figure as "Wet biological raw materials belt press") and juice (indicated on the Figure as "Raw juice belt press"). The first solid phase was applied to a screw press for more pressing since the juice (indicated on the Figure as "Raw juice expeller") and wet biosyrya. The first solid phase is, remaining in a belt press, washed with water (as indicated on the Figure as "flush Water belt filter"). The washed solid phase band filter, thus obtained, was served in a screw press for additional compaction. Part wet biosyrya extracted from the screw press was returned back in a screw press. Wet biological raw materials extracted from the screw press, and collected for drying when using the dryer for biosyrya (turbo�/ dryers) obtaining dry biosyrya. Raw juice belt press, and the raw juice of a screw press was combined with the formation of the combined raw juice and it was served in vibrazione the separator, in which the combined raw juice was filtered with getting puree, including recyclezone solid phase, and filtered juice. Mashed potatoes were served in a screw press for additional compaction. The filtered juice was stored in containers for juice 1. The juice container 1 was cooled storage tank. The filtered juice from the tank for clarified juice of 1 when using centrifuges with obtaining centrifuged the solid phase from the filtered juice and filtered juice by centrifugation (also called "clarified juice"). Centrifuged solids from filtered juice was served in a screw press for additional compaction. Centrifuged solids from filtered juice was used as a wet biosyrya. Filtered by centrifuging the juice is kept in the tank for juice 2, while its pH was adjusted to 8.5, and the temperature was adjusted to 15°C at night. Then filtered by centrifugation of the juice was processed in the precipitator to cause thermoinduced coagulation protein with obtaining broth comprising a wet protein concentrate. In other embodiments, the protein � filtered by centrifuging the juice is coagulated by treatment with an acid, the combination of acid treatment and heat treatment. To separate the protein from the rest of the broth, the broth is centrifuged to obtain the waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. Wet protein concentrate was washed or diluted by adding water to the wet protein concentrate with the formation of the washed wet protein concentrate. The wet protein concentrate to water was 4:1 by weight. The resulting washed wet protein concentrate was dried using the dryer for protein (spray dryer) to produce dry protein concentrate. Dry protein concentrate packaged for later use or analysis.

Duckweed, water for washing the belt filter, wet biological raw materials, dry biological raw materials, adjusting the pH and bring the temperature of the wet protein concentrate and dry protein concentrate represent the measured values. Destroyed biomass, wet biological raw materials of the belt press, the raw juice belt press, the raw juice expeller, combined raw juice and broth are calculated values. Filtered juice, Fi�trevanny juice by centrifugation and liquid waste are the materials for which the received amount, and the mass calculated on the basis of density. The washed solids belt filter and mashed potatoes (recicladora solid phase) are re-used material. Centrifuged solids from filtered juice is weighted and recyclable material.

Fig.31 each black arrow indicates the flow of the process; each dotted arrow indicates recycled materials; each dotted arrow indicates a balanced and recycled material; each letter or combination of letters/numbers in the hexagon indicates the location of sample code or material; Fresh duckweed, Water for washing the belt filter, Wet biological raw materials, Dry biological raw materials, Wet protein concentrate and Dry protein concentrate are the measured values, the destruction of biomass, Wet biological raw materials of the belt press, the Raw juice belt press, the Raw juice expeller, Combined raw juice and Broth indicate the computed values; the Filtered juice, Filtered juice by centrifugation, the spent fluid is returned back to the ponds for cultivation) indicate mass values calculated from the measured volume and known density; the Washed solids belt filter and mashed potatoes (recicladora solid phase) decrees�up with re-used material; and Centrifuged solids from filtered juice specifies weighed and recycled material.

Example 16 is a flowchart of a method

Fig.32 shows a block diagram of an exemplary method of separating protein from aquatic organism, for example, fresh duckweed, optionally adjusting pH and flushing wet protein. The method was tested experimentally.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a knife mill, in which the wet listary biomass destroyed with the release of internal water and protein. Destroyed biomass filed in the belt press, which destroyed the biomass is extruded with the first solid phase (as indicated on the Figure as "Wet biological raw materials belt press") and juice (indicated on the Figure as "Raw juice belt press"). The first solid phase was applied to a screw press for more pressing since the juice (indicated on the Figure as "Raw juice expeller") and wet biosyrya. The first solid phase is, remaining in a belt press, washed with water (as indicated on the Figure as "flush Water belt filter"). The washed solid phase band filter, thus obtained, was served in a screw press for additional compaction. Part wet biosyrya extracted from tied�new press, returned back in a screw press. Wet biological raw materials extracted from the screw press, and collected for drying when using the dryer for biosyrya turbulent dryers) obtaining dry biosyrya. Raw juice belt press, and the raw juice of a screw press was combined with the formation of the combined raw juice and served in a vibratory separator in which the combined raw juice was filtered with getting puree, including recyklovana solid phase and the filtered juice. Mashed potatoes were served in a screw press for additional compaction. The filtered juice was stored in containers for juice 1. The juice container 1 was cooled storage tank. The filtered juice from the tank for juice 1 clarified using a centrifuge, to obtain centrifuged the solid phase from the filtered juice and filtered juice by centrifugation (also called "clarified juice"). Centrifuged solids from filtered juice were selected to obtain samples. Centrifuged solids from filtered juice was used as a wet biosyrya. Filtered by centrifuging the juice is kept in the tank for juice 2, while its pH was adjusted to a pH below 7. Then filtered by centrifugation of the juice was processed in the precipitator to cause terming�cireundeu coagulation protein with obtaining broth, comprising a wet protein concentrate. In other embodiments, a protein in is filtered by centrifuging the juice is coagulated by treatment with acid, the combination of acid treatment and heat treatment. To separate the protein from the rest of the broth, the broth is centrifuged to obtain the waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. Wet protein concentrate was washed by adding water to the wet protein concentrate, with the formation of the washed wet protein concentrate and impurities washed from the final product. The wet protein concentrate to water was 4:1-10:1 by weight. The resulting washed wet protein concentrate was dried using the dryer for protein (spray dryer) to produce dry protein concentrate. Dry protein concentrate packaged for later use or analysis.

Fig.32 each black arrow indicates the flow of the process; each dotted arrow indicates re-used material; the grade of "bring the pH to a pH below 7 and processing precipitator", "Day" loops "Broth", "Washed wet protein concentrate, "12" and "4:1 Ratio of water added to the protein concentrate, and washed final product" are the corrections made to the method; "Sampling in 1 day, Sampling on day 2 and the Temperature was adjusted to 15°C at night" are parameters that are excluded from the way; and every letter or combination of letters/numbers in the hexagon indicates the location of the selection of the sample or material code.

Example 17 is a Block diagram of a method

Fig.33 shows a block diagram of an exemplary method of separating protein from aquatic organism, for example, fresh duckweed, with a reverse mixing and optional flushing of protein. The method was tested experimentally.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a knife mill, in which the wet listary biomass destroyed with the release of internal water and protein. Destroyed biomass was served in a mixing tank, which added R/O water. The ratio of water to biomass was 1:1. Destroyed biomass filed in the belt press, which destroyed the biomass is extruded with the first solid phase (as indicated on the Figure as "Wet biological raw materials belt press"), juice (indicated on the Figure as "Raw juice belt press") and the removed solid phase (as indicated on the Figure as "Filtered solids belt press". The first solid phase was served in a screw press #1 to receive a second juice (indicated on the Figure as "Raw juice expeller") and wet biosyrya. Biological raw materials applied in a screw press #2 for additional pressing with juice (indicated on the Figure as "Raw juice expeller") and wet biosyrya. The first solid phase is, remaining in a belt press, washed with water (as indicated on the Figure as "flush Water belt filter"). The washed solid phase band filter, thus obtained, was disposed of. Part wet biosyrya extracted from screw press #1 and screw press #2, filed in the capacitance reverse mixing. Wet biological raw materials extracted from screw press #2, collected for drying when using the dryer for biosyrya turbulent dryers) obtaining dry biosyrya. Raw juice belt press, and the raw juice of a screw press screw press #1 and screw press #2 was combined with the formation of the combined raw juice and served in a vibratory separator in which the combined raw juice was filtered with getting puree, including recyclezone solid phase and the filtered juice. Mashed potatoes were served in the capacity of a reverse mixing. The filtered juice was stored in containers for juice 1. The juice container 1 �vslas a cooled storage tank. The filtered juice from the tank for juice 1 clarified using a centrifuge, to obtain centrifuged the solid phase from the filtered juice and filtered juice by centrifugation (also called "clarified juice"). Centrifuged solids from filtered juice was served in the capacity of a reverse mixing. Filtered by centrifuging the juice is kept in the tank for juice 2. Then filtered by centrifugation of the juice was processed in the precipitator to cause thermoinduced coagulation protein with obtaining broth comprising a wet protein concentrate. In other embodiments, a protein in is filtered by centrifuging the juice is coagulated by treatment with acid, the combination of acid treatment and heat treatment. To separate the protein from the rest of the broth, the broth is centrifuged to obtain the waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. Wet protein concentrate was washed with optional or was diluted by adding water to the wet protein concentrate, with the formation of the washed wet protein concentrate. The wet protein concentrate to water status�managed 4:1 by weight. The resulting washed wet protein concentrate was dried using a dryer for protein (spray dryer), to obtain a dry protein concentrate. Dry protein concentrate packaged for later use or analysis.

Fig.33 each black arrow indicates the flow of the process, each dotted line and arrow indicate the additional steps of the process, each dotted arrow indicates recycled material, and each letter or combination of letters/numbers in the hexagon indicates the location of the selection of the sample or material code.

Example 18 is a Block diagram of a method

Fig.34 shows a block diagram of an exemplary method of separating protein from aquatic organism, for example, fresh duckweed, with a reverse mixing and the addition of water in a mixing tank. The method was tested experimentally.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a knife mill, in which the wet listary biomass destroyed with the release of internal water and protein. Destroyed biomass was served in a mixing tank, which added R/O water. The ratio of water to biomass was 1:1-5:1. Destroyed biomass filed in the belt press, which destroyed the biomass is extruded with the first solid phase (as indicated on the Figure as "Wet BIOSes�rd belt press"), juice (indicated on the Figure as "Raw juice belt press") and the removed solid phase (as indicated on the Figure as "Filtered solids belt press"). The first solid phase was served in a screw press #1 and screw press #2 for more pressing since the juice (indicated on the Figure as "Raw juice expeller") and wet biosyrya. The first solid phase is, remaining in a belt press, washed with water (as indicated on the Figure as "flush Water belt filter"). The washed solid phase band filter, thus obtained, was served in the capacity of a reverse mixing. Part wet biosyrya extracted from the screw press filed a capacitance reverse mixing. Wet biological raw materials extracted from screw press #2, collected for drying when using the dryer for biosyrya turbulent dryers) obtaining dry biosyrya. Raw juice belt press, and the raw juice of a screw press screw press #1 and screw press #2 was combined with the formation of the combined raw juice and served in a vibratory separator in which the combined raw juice was filtered with getting puree, including recyclezone solid phase and the filtered juice. Mashed potatoes were served in the capacity of a reverse mixing. The filtered juice x�anili in the tank for juice 1. The juice container 1 was cooled storage tank. The filtered juice from the tank for juice 1 clarified using a centrifuge, to obtain centrifuged the solid phase from the filtered juice and filtered juice by centrifugation (also called "clarified juice"). Centrifuged solids from filtered juice was served in the capacity of a reverse mixing. Protein is filtered by centrifuging the juice is coagulated by treatment with acid, combinations adding the acid and/or thermocoagulation. To separate the protein from the rest of the broth, the broth is centrifuged to obtain the waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. Wet protein concentrate was washed or diluted by adding water (1:1-10:1) to the wet protein concentrate, with the formation of the washed wet protein concentrate. The resulting wet protein concentrate was dried using the dryer for protein (spray dryer) to produce dry protein concentrate. Dry protein concentrate packaged for later use or analysis.

Fig.34 each black arrow indicates �Otok process each dotted arrow indicates recycled material, and each letter or combination of letters/numbers in the hexagon indicates the location of the selection of the sample or material code.

Example 19 is a Block diagram of a method

Fig.35 shows a diagram of an exemplary method of separating protein from aquatic organism, for example, fresh duckweed, using a ball mill and a decanter. The method was tested experimentally.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a ball mill, which added R/O water, where the wet listary biomass destroyed with the release of internal water and protein. The ratio of water to biomass was 1:1-5:1. Destroyed biomass was served in the decanter, which destroyed the biomass is extruded with the first solid phase (as indicated on the Figure as "Wet biological raw materials") and juice (indicated on the Figure as "Raw juice"). The first solid phase was served in a screw press #2 for more pressing since the juice (indicated on the Figure as "Raw juice") and wet biosyrya. Wet biological raw materials extracted from screw press #2, collected for drying when using the dryer for biosyrya turbulent dryers) obtaining dry biosyrya. The raw juice from screw press #1 and the raw juice from screw �ressa #2 was combined with the formation of the combined raw juice, and served in the tank for receiving acid (mixing vessels for processing), which protein is filtered by centrifuging the coagulated juice by adding acid (H2SO4). To separate the protein from the rest of the broth, the broth is centrifuged in the centrifuge #1 with the receipt of the waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. Wet protein concentrate was washed by adding a known amount of water (1:1-10:1) to the wet protein concentrate, with the formation of the washed wet protein concentrate. Protein was separated in a centrifuge #2 with receiving the washing liquid, which is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the flushing fluid is recycled. The resulting washed wet protein concentrate was dried using the dryer for protein (spray dryer) to produce dry protein concentrate. Dry protein concentrate packaged for later use or analysis.

Fig.35 each black arrow indicates the flow of the process, each dotted arrow indicates recycled material, and each letter or combination of letters/numbers in the hexagon indicates the location�agenie selection of the sample or material code.

Example 20 is a Block diagram of the method of growing and harvesting the duckweed with the use of experimental industrial installation

Fig.36 shows a block diagram of an exemplary method of growing and harvesting aquatic organism, for example, fresh duckweed. The method was tested experimentally.

Bioreactors, also called the "reactor for growing", filled with artesian water, which meets the requirements of acceptable water quality, and appropriate to the balanced composition of nutrients. The smaller ponds were of such a configuration and size so that they could serve as a "supply" of ponds for larger bioreactors. Small ponds was first inoculable and were grown to high density, after which they can be optimally used for seeding large ponds thus, to support the most rapid growth. Fertilizer was applied to the station of nutrients, and applied nutrients in the reactor for growing duckweed.

Artesian water filed at a rapid filtration through the sand with water from a pumping station, which pumps water in and out of the water tank. Some of the water after a quick filtration through the sand and artesian water was added at the station of nutrients. Some of the water after a quick filtration through the sand and artesian water was added to reaction�'or for growing duckweed, to maintain the reactor at a prescribed value. Some of the water after a quick filtration through the sand and artesian water was added to the sprinklers, which acted as a cooling system of a reactor for growing duckweed. For optimal performance micro cultures water carefully checked to maintain the necessary nutrients and trace elements in water within standard levels. Sensors installed in ponds, controlled and recorded levels of ammonia, oxidation-reduction potential (ORP) and temperature. Ammonia sensor used for feedback to control the levels of nitrogen in the ponds through the supply system capacity of nutrients. The liquid level sensor installed in each pond, ensured that the water level does not drop below the required depth.

For maximum performance of biomass thickness of the surface layer micro cultures was checked and maintained at the required thickness. The harvest was carried out by several physical mechanisms, and at different times during the year, depending on environmental conditions and the corresponding growth of certain species. When harvesting conditions meet the requirements, the surface layer of micro cultures conveys�Aravali on the device collection and was pumped into vibration sieve, where microculture was separated and collected in the hopper for further processing. The collection process was controlled via a programmable logic controller (PLC) and human machine interface (HMI).

Drain outlet from the reactor for growing duckweed and output stream after harvesting crops filed into the receiving sump. The water from the receiving sump filed in the equalizing reservoir from which water is fed to a pump station and water tank.

Material from the receiving sump was served in a mechanical scraper. Wet duckweed submitted to the dehydration to obtain a dehydrated duckweed for further processing.

Fig.36 each black text indicates the flow of the process; "Artesian water #1", "Rapid filtration through sand, Pumping station, water reservoir and Equalizing reservoir" indicate the flow of water; "Station " nutrients" and "Fertilizer" indicate nutrients; "sump sump", "Mechanical scraper" and "dehydration" indicate dehydration harvest; and each number inside the diamond indicates a typical operation.

Example 21 is a Block diagram of a method of separating protein from duckweed with the use of experimental industrial installation

Fig.37 shows a diagram of an exemplary method of separating protein from aquatic organism, for example, fresh duckweed. Method test�Ali experimentally.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a sanitary treatment system, top of the plums and solid waste which was disposed of. The material filed in a dewatering centrifuge, or a conveyor system, vibrating screen, and separated water is returned back to the system during the treatment. The material filed on the conveyor, and then into a ball mill, in which the wet listary biomass destroyed with the release of internal water and protein. Destroyed biomass was served in a decanter feed tank for the mixing stage. Destroyed biomass was served in the decanter, which received the raw juice decanter. The solid phase was applied for mechanical pressing stage #1 with the second juice (indicated on the Figure as "Raw juice") and biosyrya. Biological raw materials applied for mechanical pressing stage #2 for additional pressing with juice (indicated on the Figure as "Raw juice expeller") and wet biosyrya. Wet biological raw materials applied for mechanical pressing stage #3. Wet biological raw materials extracted from screw press #3, collected for drying when using the dryer for biosyrya turbulent dryers) obtaining dry biosyrya.

Raw juice decanter and unprocessed juice from the screw press mechanical�ical pressing #1 and mechanical pressing stage #2 was combined with the formation of the combined raw juice and it was served in the capacity for filtration of coarse solid phase, in which the combined raw juice was filtered with getting puree, including recyclezone solid phase, and filtered juice. Mashed potatoes were served in the capacity of a reverse mixing. The filtered juice was stored in containers for juice. The juice container is connected to the cooler. The filtered juice from the tank for juice was clarified using a centrifuge thin clearing of obtaining centrifuged the solid phase from the filtered juice and clarified juice. Centrifuged solids from filtered juice was served in the capacity of a reverse mixing. Clarified juice was served in TermoSanitari to cause thermoinduced coagulation protein with obtaining broth comprising a wet protein concentrate. In other embodiments, a protein in is filtered by centrifuging the juice is coagulated by acid treatment, combination treatment with acid and/or heat treatment. To separate the protein from the rest of the broth, the broth is centrifuged to obtain the waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. Wet protein concentrate was washed in the tank for protein, adding water to wet protein conc�STRATO, with the formation of the washed wet protein concentrate. Protein was separated in a centrifuge with receiving the washing liquid, which is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the flushing fluid is recycled. The resulting washed wet protein concentrate was dried using a dryer for protein (spray dryer) to produce dry protein concentrate.

Fig.37 each black arrow indicates the flow of the process; each dotted arrow indicates a reusable stream; each dotted arrow indicates application; "cleaning System", "Dewatering Centrifuge" and "Pipeline" indicates the treatment system; "Ball mill", "Decentrali feeder bowl (mixing)", "Settler", "mechanical pressing stage #1", "mechanical pressing stage #2", "mechanical pressing stage #3", "Dryer biosyrya" and "Reverse confusion" indicate processing biosyrya; and "Coarse filtration of the solid phase", "the juice Container, Centrifuge polishing", "Cooler", "the juice Container from the centrifuge, Thermostatical", "protein Separation (Centrifuge)", "the Reservoir for protein Machine protein)", "Department of washed protein (Centrifuge)", "Tank protein" and "Tumble protein" indicates the processing of the protein.

PR�measures 22 - The block diagram of the certification cycle of isolating the protein from duckweed

Fig.38 shows a diagram of an exemplary certification cycle for isolating the protein from the water body, such as fresh duckweed. The method was tested experimentally.

Fresh duckweed (also called suspension of biomass or feedstock) was served in a ball mill in which the wet listary biomass is mixed with water and destroyed with the release of internal water and protein. Destroyed biomass filed in decentrali supply tank to the mixing stage. Destroyed biomass was served in the decanter, which produces a raw juice decanter and wet biological raw materials of the decanter. Wet biological raw materials decanter filed for mechanical pressing stage #1 with the receipt of raw juice and biosyrya the first press. Biological raw materials of the first press filed at mechanical pressing stage #2 with obtaining raw juice expeller and biosyrya second press. Biological raw materials of the second press gathered for drying when using the dryer for biosyrya turbulent dryers) obtaining dry biosyrya.

Raw juice decanter, the raw juice of a screw press with mechanical pressing stage #1 and the raw juice of a screw press with mechanical pressing stage #2 was combined with the formation of combined�about raw juice and it was served in the capacity of a coarse filtration of the solid phase, in which the combined raw juice was filtered with getting puree, including recyclezone solid phase, and filtered juice. Mashed potatoes were served on a mechanical pressing stage #1. The filtered juice was stored in containers for juice. The filtered juice from the tank for juice was clarified using a centrifuge thin clean, and washed with water to obtain the centrifuged solid phase from the filtered juice and clarified juice. Clarified juice was served in TermoSanitari to cause thermoinduced coagulation protein with obtaining broth comprising a wet protein concentrate. To separate the protein from the rest of the broth, the broth is centrifuged to obtain the waste liquid and wet protein concentrate. The spent fluid is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the implementation of the waste fluid is disposed of. Wet protein concentrate was washed in the tank for protein, adding water (1:1-10:1) to the wet protein concentrate, with the formation of the washed wet protein concentrate. Protein was separated in a centrifuge with receiving the washing liquid, which is returned back to the ponds for cultivation (also called bioreactors). In other embodiments, the flushing fluid disposed�. The resulting washed wet protein concentrate was dried using a dryer for protein (spray dryer), to obtain a dry protein concentrate.

Fig.38 arrow each block represents a process flow, each dotted arrow indicates a reusable stream; each dotted arrow indicates the recyclable stream; and every letter or combination of letters/numbers in the hexagon indicates the location of the selection of the sample or material code. A0, P1 and O1-W denote the samples taken for internal and external analysis. C1, K2, D2, D3, F5, Q2, J1, J1-W I1 and W denote the samples taken for internal analysis.

Example 23 a Company that is growing and processing of duckweed

In this example, the described method of growing and harvesting the duckweed. The method was tested experimentally.

a. Channel bioreactors

The company has developed to use multiple channel bioreactors. Each closed channel inside posted LDPE (30 mils or 0.75 mm) polymer on the geomembrane (8 ounces or 226.8 g). Windproof PE material provided protection from the wind.

Water flow in the channel is carried out via the return pump, the exhaust from the Main pond. Spare the water supply is discussed below in section Water supply and storage. A full flow of water in each channel is controlled. The flow of water in each to�nal harvest was controlled automatically.

There were several alternatives for supplying water in the channel when you use automatic valves that were operated by the Central PLC. The water flow can be directed through a pair of water-spray distribution pipe distribution pipe cleaning blade wheel or the distribution piping water collector. In the spray, centrifugal purifier and a water collector flow rate is adjustable. The water flow can be directed through the underwater suction/irrigation distribution tubing.

In some embodiments, the flow in the channel is directed through the impeller. The impeller is located outside of the rotary end of each of the closed channel, which is the working end. The frequency of rotation of the impeller controls the variable frequency drive (VFD), and the surface speed is adjusted automatically.

Duckweed was collected from the canal for cultivation with submerged devices for the collection. In each channel were set two harvesting module. The first device was located after an external rotation about the impeller. The second device was located after internal rotation. Collection devices were made of PVC tubes that are installed in submerged concrete blocks. Cycle collection� consisted of collecting duckweed on each device to collect in the channel. During the collection cycle duckweed collection devices raised above the surface of the pond by means of a linear actuator and mechanical linkage. Collecting duckweed produced by suction through the conduit devices for the collection through one of two parallel pumps to collect a layer of duckweed. The collected duckweed pumped into a processing enclosure for processing into various products, including, without limitation, protein concentrate, biological raw materials and flour (feed) of the duckweed. The flow through the Pump for collecting a layer of duckweed were governed by Valves flow devices for the collection to match the specified value for FIC-141. Two pumps to collect a layer of duckweed served all three channels. The pumps were located at the Station collecting duckweed on the working end of the channels.

Detritus biomass was collected from the bottom of the Channel with underwater gathering system. The underwater flow of biomass provided by suction with the help of the Underwater cleaning of the pump. Detritus biomass pumped into a Processing enclosure for processing along with the harvest collected from the surface. Underwater biomass was collected continuously from all three Channels. During the underwater collection of flow controlled and summarized using the computer. Underwater biomass was recovered from the Canal with the use of automatic valves, which were driven by a Central PLC (�programmiruemyi logic controller). In the alternative, underwater biomass can be directed from underwater strainer biomass in each Channel or from an underwater suction pipe in each Channel.

Analysis of the water in the canals and use of technical means was performed by controlling the water level and temperature. The water level in the Channels was controlled, while alarms were signaled by the PLC, if achieved a high or low level alarm. Water level control can be performed by means of automation or without it. The temperature of the water in the Channels is also controlled, while alarms were signaled by the PLC, if achieved a high or low level alarm. The water temperature control can be performed by means of automation or without it.

In the Automated sampling system Pump analytical sampling can pump water from any of the three Channels, opening the sampling valve. The issue of sampling Pump passes through the Filter samples for the purpose of removing particles of a certain size.

The channels are protected from overflow during heavy rain with a passive system, located in perelivom the end of each channel. Pipe to the S-shaped curve, set at a level below the height of the canal wall, allows you to drain the water.

b. Water and vault�nie

Water can be supplied to the plant pumps for water supply or well pump. Surface or well water is pumped through a mechanical filter to remove particles of a certain size. Filtered water is passed through sand filters for water and fed into a system of growing and gathering. Water recovered from the process is discharged by gravity from the reservoirs for reclaimed water in the industrial building in the channels and holding ponds.

In the System return water return pumps to supply water from the main cumulative pond in the channels and production building. In the alternative, return the pumps can draw water from an auxiliary cumulative pond and serve it on the premises or in the main cumulative pond. Return water is pumped through a mechanical filter to remove particles of a certain size.

Subsidiary cumulative pond is used as a reservoir for process water to feed the main cumulative pond if necessary. Water can enter from the Main pond and cumulative of gravity.

c. System nutrients

System nutrients consists of a pair of Reservoirs for nutrients where nutrient solution is mixed in portions received in the channels of the Mixing of nutrients is a semi-automated process, when water is dosed into the Tanks for nutrients. The operator uses automatic valves for filling the Reservoir for nutrients. Dry nutrient mixture is added manually or automatically, in accordance with the required concentration of dosing. When adding dry nutrient mixture Pumps for nutrient mixed water in the Reservoirs for nutrients through recycling.

When filling out the Channels for commissioning serves a starting dose of nutrients. The maintenance dose level nutrients required continuously to maintain the necessary concentration of nutrients in the water in the Channels. Each dose is a mixture of nutrients in such concentration that allows to maintain the required levels of nutrients. After the nutrient solution was mixed, and Nutrient Reservoir contains a ready solution, the submission process is semi-automatic. Any Pump for nutrients may deliver the dose in any of the Channels by means of automatic valves.

ii. Processing of duckweed

a. Dehydration and screening

Duckweed collected by Devices to collect with the help of Pumps collecting surface layer was evaporated using a Sieve for the collected duckweed, cat�Roy is bunk sieve, separating the oversized material and debris from the duckweed. Detritus was removed from the Channels using an Underwater pump Assembly and weed out by means of Sieve for underwater biomass. Water from the channels after collecting duckweed on both sieves was collected in Tanks for reclaimed water, which represent the two horizontal tank mounted on an elevated platform located immediately below the intermediate tier of sieves. Tanks for reclaimed water hydraulically connected to the effective Association volume and flow of regenerated water from both Sith. The reservoirs also serve the following smaller output flows of the process: Exhaust pressed juice from Screw press #3, the Spent liquid from the Centrifuge for protein broth, the Spent fluid from the Centrifuge washed protein and Recirculating cooling water from the Cooler for juice. The tanks were merged by gravity through a PVC pipe into the Main cumulative pond. When the high level switch high level signal and is blocked, stopping the Pumps collecting surface layer and an Underwater pump collection. As for measuring the speed of collecting duckweed collected duckweed from SITA for the collected duckweed and detritus from submerged sieve to collect enters the Weigh belt feeder for VSUES�tion with the help of load cell mechanical load, during transportation to the processing.

b. Pulse hopper for dehydrated duckweed

Pulse hopper for dehydrated duckweed is a rectangular steel bunker, the size of which is chosen so that it provided a certain number of channels in production. Pulse hopper for dehydrated duckweed is a hopper with a movable bottom, emptied by a screw conveyor which feeds the collected duckweed grinding. The speed of the conveyor VFD adjusts to match the flow of the subsequent grinding process.

c. Grinding duckweed

The feeder of the ball mill adopts the Pulse stream from hopper for dehydrated duckweed and regulates the flow of Ball mill. Duckweed is ground in a Ball mill to puree and discharged in the Mixing bowl for mashed potatoes. The desired total solids concentration of the crushed puree optimize for ease of processing in the Decanter duckweed. The feeder of the Ball mill can accept the flow of recycled flow from Mixing tank for mashed potatoes, Blocksdelaware juice from the receiver fluid Decanter duckweed and water from the collector of the Production building. Crushed puree duckweed stood in a Mixing tank for mashed potatoes - capacity with a stirrer, fully able to accommodate the expected total number of hedgehog�fluorescently dehydrated collect duckweed from all Channels.

d. Decanting duckweed

The flow speed in the Decanter duckweed regulated VFD Pump for mashed potatoes. All automated functions on the platform of Decanter duckweed controlled Remote control platform decanter duckweed. Solid phase biosyrya from a decanter initiated flow biosyrya. Biological raw materials filed from the issue of decanter in the pressing Unit biosyrya by a Conveyor wet biosyrya. The liquid coming out of the decanter, initiated the flow of protein. Alexdurai the juice is drained from the decanter in the juice Receiver and fed from the receiver to the Sieve for juice Pump for juice. Recirculating flows that include the Pressed juice from Screw press #1, Pressed the juice from Screw press #2 and mashed fine cleaning of the Centrifuge, also filed in the juice Receiver. Combined Alexdurai juice and recirculation flows from the Receiver juice, served in a Filter juice Pump for juice. Suspended substances from a stream of Blocksdelaware juice was removed using a Filter juice. Solid phase discharged from the strainer the juice directly into the wet Conveyor biosyrya for submission to the Compression biosyrya. The juice was coming out from the Tank for filtered juice and served in a juice Container #1 Pump for filtered juice.

iii. Processing biosyrya

a. Pressing biosyrya

Screw press #1

On�OK biosyrya from a Decanter dehydrated duckweed in preparation for drying through a number of presses. Screw press #1 was the first stage. The expected daily production of the first line biosyrya varies depending on the number of bioreactors and size of the processing center.

Screw press #2

Biological raw materials additionally dehydrated after direct discharge from Screw press #1 on Screw press #2. The expected daily production of the second pressing biosyrya varies depending on the number of bioreactors and size of the processing plant.

Collection of pressed juice

Combined Pressed juice from Screw press #1 and Screw press #2 filed in the Receiver pressed juice. Assembled the pressed juice was returned back to the Conveyor wet biosyrya Pump for pressed juice.

Screw press #3

Biological raw materials were further dehydrated with a direct discharge from Screw press #2 on Screw press #3. Optional operations include steam to the Screw press #3. The expected daily production of the third line biosyrya varies depending on the number of bioreactors and size of the processing facility. Extruded biological raw materials discharged from Screw press #3 to the Conveyor biosyrya, which filed Extruded biological raw materials into the Hopper for biosyrya.

Regeneration of spent pressed juice

Pressed� juice from Screw press #3 filed in the Receiver to extract juice. Extract the juice was pumped by Pump exhaust juice in the Tanks for reclaimed water to return to the Main cumulative pond.

b. Drying biosyrya

The tank is pressed biosyrya had a nominal capacity of 125% of the estimated total daily production of Pressed biosyrya. Daily product kept in the hopper until the next business day when it is dried and Packed. Extruded biological raw materials was served by a Conveyor for pressed biosyrya into the hopper of the dryer at a speed which is regulated VFD, maintaining a working level in the hopper dryer for biosyrya.

Extruded biological raw materials are dried using dryers for biosyrya. In some embodiments, the dryer biosyrya is turbulent dryer heated inlet by means of the Heater, heated with natural gas. Tanks for liquefied natural gas (LNG) are located on the land to supply the burner. Dried biological raw materials were unloaded into the hopper of the product and supplied to the packaging unit. Automated functions on the Platform of the dryer biosyrya are controlled by a dedicated remote control.

c. Packing biosyrya

The packing house is a room with controlled atmosphere to reduce the influence of Llanos�and the product (biological raw materials). Biological raw materials packaged into suitable for specific product packages, cardboard drums or other containers.

iv. Processing of protein concentrate

a. Centrifugation of thin clearing

Clarification of juice to Shine

The residual solid phase from the Filtered blocksdelaware of the juice is removed through a fine filter.

Recycling puree

Solid phase leaving the Centrifuge thin clearing, filed in the Receiver decanter of juice, from which the solid phase is returned to the Filter juice and a Conveyor for wet duckweed.

b. Deposition of protein

Deposition with the introduction of steam

Liquid proteins in the Clarified to Shine juice was precipitated to separate, using Steam precipitator.

c. Centrifugation of the protein broth

Concentrated protein broth

Protein broth was concentrated using centrifugation for protein broth. The broth was served in a Centrifuge for protein broth using a Pump storage tank for the broth.

Regeneration of waste liquid

Complementary phase from the Centrifuge for protein broth is the waste of the liquid phase. The spent fluid is diverted to storage Tanks for reclaimed water for the purpose of returning to the Main cumulative pond.

d. Washing of the protein broth and centrifuging

Concentri�created protein broth were washed for further concentration of precipitated solid phase protein. Front of the cleaning vessel of concentrated broth, the broth was mixed with wash water. The washed Broth was served in a Centrifuge, washed broth. The broth was served to Wash the centrifuge for washing Pump for the washed broth. The washed broth was separated from the wash water to Wash the centrifuge. The washed broth was served from the centrifuge in the Capacity for protein. The flow rate was controlled and sent on a control Panel of Washing machine. The expected daily production of washed broth varies depending on the number of bioreactors and size of the processing facility. The spent liquid phase that is separated in a Washing centrifuge, filed in the Tanks for reclaimed water to return to the Main cumulative pond.

e. Drying protein

The capacity for protein has a face value of 125% of the estimated total daily production of Washed protein concentrate. The capacity for protein is supplied with cooled water jacket to maintain the temperature of the contents at the required level. Daily production was kept in the vessel prior to its drying and packing. Concentrated protein was dried using the Dryer for protein. In some embodiments, the Dryer protein is a spray dryer, the inlet of which is heated In�schonegevel, heated with natural gas. Tanks for liquefied natural gas (LNG) are located on the land to supply the burner. The expected daily production of Dry protein concentrate varies depending on the number of bioreactors and size of the processing facility. The dried protein concentrate was supplied in the hopper for the product and transported to the packing station.

f. Packing protein

The packing house is a room with controlled atmosphere to reduce the influence of humidity on the product (protein concentrate). Protein concentrate is Packed in suitable for specific product bags or cardboard drums.

v. Cooling and storage of working fluid

a. Purpose and basic principles of system design

Cooling system and storing the working fluid is designed to store partially processed puree, juice or broth during the technological process violations. The following blocks of the process may transmit the partially processed product in or out of the System for cooling and storage Filtered Juice, Clarified to Shine juice, Besieged broth, Concentrated broth and Washed broth.

b. System components

Primary cooling

Working fluid from Filtered juice, Clarified to Shine juice, Besieged by buglio�and, Concentrated broth and Washed broth pass through the Cooler juice to establish or maintain the temperature at the right level.

Rapid cooling

The working fluid leaving the Chiller juice, also pass through the Cooling heat exchanger juice to establish or maintain the temperature at the desired level. Coolant feed is carried out on the platform cooling unit, which operates in a closed cycle. The temperature of the working fluid exiting the Cooling heat exchanger juice, govern.

Cumulative capacity

Cooled the juice container has a nominal capacity of 100% of the estimated total daily production of Crushed puree duckweed. Cooled the juice container equipped with a cooled water jacket to maintain the temperature of the contents at the required set value.

vi. The system of cleaning in place (CIP)

a. Platform CIP

Platform CIP is equipped with two tanks, the size of which is suitable for the volume of material being processed. Wash tub CIP typically contains hot water used for cleaning process equipment before and after cleaning with a solution of caustic soda, the caustic soda solution is used for cleaning process equipment through recycling. Pump Creditable a centrifugal pump, which delivers the CIP solution and the liquid for flushing the users of the system CIP. The heater heats the CIP CIP solution to the required temperature. The stream can be recycled through the heater CIP and any of the two CIP tanks to establish the desired value of temperature.

b. Solution and a liquid for rinsing CIP

The CIP solution is a solution of caustic soda heated to the desired temperature. A solution prepared by diluting with plenty of water. The liquid for rinsing CIP refers to clean water, heated to a setpoint.

c. Flow and return CIP

Users of the System CIP include the following: the mixing vessel is mashed, the juice Container #1, fine cleaning Centrifuge, a holding tank for the broth, Centrifuge for protein broth, ventilation broth, Washing centrifuge, Chiller juice, Cooling coil juice, Refrigerated juice container and the Reservoir for the protein.

Example 24 - the Purity of the protein, the yield of the protein product and the output biosyrya

Dry protein concentrate and dry biological raw materials produced according to the flowchart of the method shown in Fig.38 and described in this application.

Table 6 shows the purity of the protein, the yield of the protein product and the output biosyrya. Used in the present application and is described elsewhere in n�standing description, the purity of the protein is calculated as the percentage of total final dry product, protein yield calculated as a percentage of the total mass of the original dry matter and yield biosyrya calculated as a percentage of the total mass of the original dry matter.

Table 6
The product yield
The day IDay IIDay III
Purity protein67,7%69,9%69,1%
Protein yield23,2%20,3%21,6%
The output biosyrya43,7%47,6%37,6%

Dry protein concentrate and dry biological raw materials analysed further.

Example 25 the process yields

Table 7 summarizes the typical ranges of the protein yield, biosyrya and flour from duckweed.

Product
Table 7
The product yield of the process
The yields of products of the process
Typical range output
Protein15-28%
Biological raw materials30-52%
Flour of duckweed32-55%

Various methods and techniques described above provide a number of ways to implement the order. Of course, it should be understood that not necessarily all the described objectives or advantages may be achieved in accordance with any specific variant of the implementation described in this application. Thus, for example, professionals, skilled in the art will understand that the methods can be implemented in a manner that provides or optimizes one advantage or group of advantages as described in the present application, without necessarily achieving other objectives or advantages described or proposed in this application. In this application there are many alternatives. It should be understood that certain preferred embodiments of the expressly include one, the other or few symptoms, while others explicitly exclude one, the other or few symptoms, while others reduce the trait inclusion of one, two or several�x favorable characteristics.

In addition, a qualified specialist will be obvious applicability of various features from different embodiments. Similarly, the various elements, features and steps described above, as well as other known equivalents for each such element, feature or step, can be used in various combinations to the average expert in the art when implementing the methods in accordance with the principles described in this application. Among the various elements of the signs and stages, some will be included in the direct form, while others are expressly excluded in various embodiments of the implementation.

Although the present application has been disclosed in the context of certain embodiments and examples, qualified specialists in this field technicians will be understood that embodiments of the application extend beyond the specifically disclosed embodiments to other alternative embodiments of the and/or their use and modification, and equivalents.

In some embodiments, the number expressing quantities of ingredients, properties such as molecular weight, reaction conditions, etc. used to describe and statements of some embodiments of the application, should be seen as supplemented in some cases by the term "�roughly". Thus, in some embodiments, the numerical parameters given in the text of the description and the attached claims are approximations that may vary depending on the desired properties, which are believed to be provided with the specific variant implementation. In some embodiments, the numerical parameters should be considered with the given number of significant digits and by applying standard rounding techniques. Notwithstanding that the numerical ranges and parameters reflecting the wide scope of some embodiments of the application are approximations, the numerical values presented in some examples, listed with the highest possible practical accuracy.

In some embodiments, the articles "a", "an" and "the" in the original text of the application, and similar references used in the context of describing a particular embodiment of the application (in particular in the framework of certain items the following formula of the invention) can be considered to encompass both the singular and the plural. An enumeration of the ranges of values in this application is intended only to facilitate the individual instructions of each individual value within the range. If not otherwise indicated, each individual�e value included in the description, as if it were individually listed in this application. All the methods described in the present application, can be performed in any suitable order, if not otherwise stated or otherwise apparent from the context. The use of any and all examples, or exemplary language (e.g. "such as") provided in some embodiments in the present application is intended just for better clarification of the application and is not meant to limit the scope of the application, otherwise stated. None of the expressions in the description should not be construed as indicating any not claimed element necessary for the practical implementation of the application.

Preferred embodiments of the present invention described in this application, including the best option known to the inventors for implementing the present application. Changes in such preferred embodiments will be apparent to the average skilled in the art after reading the preceding description. It is assumed that skilled professionals will be able to apply such changes in appropriate cases, the application may be practiced otherwise than specifically described in this application. Thus, many embodiments of the present W�turnout includes all modifications and equivalents of the objects listed in the claims appended to this description in accordance with applicable law. In addition, any combination of the above-described elements in all possible variations covered by the present application, unless otherwise stated or otherwise apparent from the context.

All patents, patent applications, publications of patent applications, and other materials, such as articles, books, specifications, publications, documents, things and/or the like provided in the present application, is incorporated by reference in full in all respects, except for the conduct of any proceedings on the application associated with listed, by any of the above, which are inconsistent or in conflict with this document, or any of the above, which can produce bounding activity against the widest scope of the claims, now or in the future associated with this document. As an example, in the case of any inconsistency or conflict between the description, definition and/or application of the term associated with any included material and material related to this document, the description, definition and/or the use of the term in this document shall prevail.

In conclusion, it should be understood that embodiments of the invention disclosed in us�Mr sage application illustrate the principles of embodiments of the invention. Other modifications that may apply, can be in the context of the present application. Thus, as an example, but not limitation, alternative configurations of the embodiments of the invention may be used in accordance with the present description. Accordingly, embodiments of the present invention is not limited to exactly what is shown and described.

PRESENTATION of EXAMPLES of carrying out the INVENTION

Some embodiments of the invention are disclosed in the following paragraphs.

Points

1. A method of producing multiple products from biomass of aquatic organism, including:

obtaining biomass;

the destruction of biomass with getting destroyed biomass;

the separation of the destroyed biomass with getting juice and the first solid phase;

forming a wet protein concentrate using the juice;

drying the wet protein concentrate to produce dry protein concentrate;

production of wet biosyrya by using the first solid phase,

drying wet biosyrya obtaining at least one product selected from a dry biosyrya and carbohydrate-rich flour,

where many products includes products selected from dry protein concentration�ATA dry biosyrya and carbohydrate-rich flour, and

where at least 50% of the protein in the multiple products is present in a concentration of protein powder.

2. The method of claim 1, where the step of obtaining includes:

biomass production of aquatic organism on an industrial scale; and

the collection of biomass.

3. The method of claim 1, where the separation step includes pressing the destroyed biomass.

4. The method of claim 1, further comprising:

filtration of the juice with obtaining the filtered juice and the second solid phase;

clarification of filtered juice with obtaining a clarified juice and a third solid phase;

coagulating protein from the clarified juice with obtaining broth comprising a wet protein concentrate; and

the office of the wet protein concentrate from the broth.

5. The method of claim 4, where at least one of: the first solid phase, the second solid phase, a third solid phase and the broth is used to obtain biosyrya and carbohydrate-rich flour.

6. A method according to claim 1 wherein the body includes a water species ofLemna.

7. The method of claim 1, where the fracture involves the application of at least one of: a ball mill, colloid mill, cutter mill, hammer mill, crusher, puree the machine and filter press.

8. The method of claim 3, wherein the compaction includes the application of at least one�of belt press, lobed press, rotary press, screw press, filter press and press finish.

9. The method of claim 1, wherein the juice comprises a soluble protein.

10. The method of claim 4, comprising pressing at least one of the first hard phase, the second solid phase or a third solid phase, since the juice and biosyrya.

11. The method of claim 10, wherein the second juice combine with the juice.

12. The method of claim 10, where additional compression is performed with the use of a screw press.

13. The method of claim 10, further comprising drying biosyrya.

14. The method of claim 13, wherein the drying is performed using at least one of: a turbulent dryers, spray dryer, drum dryer, flash dryer, fluidized bed dryer, double-drum dryers and rotary dryers.

15. The method of claim 4, wherein the filtering is performed using at least one of: vibration separator, vibrating screen filter, vibrating separator, circular steps, linear vibrating screens/inclined movement, decanter centrifuges and filter press.

16. The method of claim 15, where the vibratory separator includes at least one vibrating mesh filter.

17. The method of claim 4, which includes clarification centrifugation and/or additional filtering filter�ƈ juice.

18. The method of claim 17, where the lightening involves the application of at least one high-speed multi-disc centrifuge, microfiltration and ultrafiltration.

19. The method of claim 4, wherein the clarified juice is stored in refrigerated storage tanks.

20. The method of claim 4, wherein the coagulating includes lowering the pH of the clarified juice.

21. The method of claim 20, wherein the pH is reduced to pH below about 6.

22. The method of claim 20, wherein the pH is reduced to pH below about 5.

23. The method of claim 20, wherein the pH is reduced to pH about 4.5.

24. The method of claim 20, wherein lowering the pH comprises applying at least one acid selected from hydrochloric acid, nitric acid and sulfuric acid.

25. The method of claim 4, wherein the coagulating performed using precipitator comprising at least one heat exchanger.

26. The method of claim 25, where at least one heat exchanger includes at least one plate or tube heat exchanger or a heat exchanger with steam injection.

27. The method of claim 4, wherein the coagulating comprises heating the clarified juice to a first temperature with obtaining broth; and cooling the broth to a second temperature.

28. The method of claim 27, wherein the first temperature is from about 40°C to about 100°C.

29. The method according to item 27, where �which temperature is lower than about 40°C.

30. The method according to item 27, where the second temperature is lower than approximately 30°C.

31. The method of claim 1, wherein the separation includes the use of high-speed multi-disc centrifuge.

32. The method of claim 1, wherein the wet protein concentrate is stored in refrigerated storage tanks.

33. The method of claim 1, further comprising drying the wet protein concentrate to produce dry protein concentrate.

34. The method of claim 33, where the drying is performed using a spray dryer, drum dryer, turbulent dryers, flash dryers, fluidized bed dryer, double-drum dryers and rotary dryers.

35. The method of claim 1, further comprising a contact material selected from the group consisting of a third solid phase and a clarified juice, at least one of: alcohol, solvent or water, and acid catalyst, with the formation of a mixture separation of a mixture of liquid and solid phase, resulting in lipids and ash forming components in the material is separated with liquid.

36. The method of claim 1, further comprising, before or immediately after the destruction, the washing of the biomass with an aqueous solvent.

37. System to generate multiple products from biomass of aquatic organism, including:

block destroyed�Oia for the destruction of biomass with getting destroyed biomass;

a separation unit for separating the destroyed biomass with getting juice and a solid phase;

unit for forming a wet protein concentrate using the juice;

the drying unit of protein for drying the wet protein concentrate to produce dry protein concentrate; and

unit for drying wet biosyrya obtaining at least one product selected from a dry biosyrya and carbohydrate-rich flour, where wet biological raw materials includes a solid phase;

where many products includes products selected from the dry protein concentrate, dry biosyrya and carbohydrate-rich flour, and

where at least 50% of the protein in the multiple products is present in a concentration of protein powder.

38. A system according to paragraph 37, where the unit of destruction includes at least one device selected from a colloid mill, cutter mill, ball mill, hammer mill, crusher, puree the machine and filter press.

39. A system according to paragraph 37, where the separation unit includes at least one device selected from a belt press, decanter centrifuge, lobed press, rotary press, screw press, filter press and press finish.

40. A system according to paragraph 37, where the unit for forming a wet protein concentrate using the juice includes at least one unit selected and� of the filtration unit, block lightening, block protein coagulation and collection unit of a protein.

41. A system according to paragraph 40, where the filtration unit comprises at least one device selected from the vibratory separator, vibrating screen filter, vibrating separator, circular steps, linear vibrating screens/inclined movement, decanter centrifuge, filter press.

42. A system according to paragraph 40, where the unit clarification includes at least one device selected from the high-speed disc centrifuge, microfiltration, ultrafiltration.

43. A system according to paragraph 40, where the unit of coagulation of the protein includes at least one device selected from thermostates and device for the deposition of acid.

44. A system according to paragraph 40, where the protein includes at least one device selected from a high-speed multi-disc centrifuge, settling tank, clarifier and decanter centrifuges.

45. A system according to paragraph 37, where the unit of drying the protein includes at least one device selected from a spray dryer, double-drum dryers and flash dryers.

46. A system according to paragraph 37, where the unit for drying biosyrya includes at least one device selected from the dryer fluidized bed, turbulent dryers, flash dryers, drum dryers and rotary dryers.

47. System punctu, further comprising a unit for sanitary treatment.

1. A method of producing multiple products from biomass of aquatic plants, including:
obtaining biomass;
the destruction of biomass with getting destroyed biomass;
the separation of the destroyed biomass with getting juice and the first solid phase;
filtration of the juice with obtaining the filtered juice and the second solid phase;
clarification of filtered juice with obtaining a clarified juice and a third solid phase;
coagulating protein from the clarified juice with obtaining broth comprising a wet protein concentrate; and
the office of the wet protein concentrate from the broth,
drying the wet protein concentrate to produce dry protein concentrate;
production of wet biosyrya by using the first solid phase,
drying wet biosyrya obtaining at least one product selected from a dry biosyrya and carbohydrate-rich flour,
where many products includes products selected from the dry protein concentrate, dry biosyrya and carbohydrate-rich flour, and
where at least 50% of the protein in the multiple products is present in a concentration of protein powder.

2. A method according to claim 1, wherein the step of obtaining includes:
biomass production of aquatic plants on an industrial scale; and
the collection of biomass.

3. SPO�about by p. 1, where the separation step includes pressing the destroyed biomass.

4. A method according to claim 3, pressing involves the application of at least one of the belt press, lobed press, rotary press, screw press, filter press and press finish.

5. A method according to claim 1, where at least one of: the first solid phase, the second solid phase, a third solid phase and the broth is used to obtain biosyrya and carbohydrate-rich flour.

6. A method according to claim 1, where the types of aquatic plants includes species Lemna.

7. A method according to claim 1, where the fracture involves the application of at least one of: a ball mill, colloid mill, cutter mill, hammer mill, crusher, puree the machine and filter press.

8. A method according to claim 1, wherein the juice comprises a soluble protein.

9. A method according to claim 1, comprising pressing at least one of the first hard phase, the second solid phase or a third solid phase, since the juice and biosyrya.

10. A method according to claim 9, wherein the second juice combine with the juice.

11. A method according to claim 9, where additional compression is performed with the use of a screw press.

12. A method according to claim 9, further comprising drying biosyrya.

13. A method according to claim 12, wherein the drying is performed using at least one of: a turbulent dryers, spray dryer, drum dryer, flash sushi�Ki, the fluidized bed dryer, double-drum dryers and rotary dryers.

14. A method according to claim 1, wherein the filtering is performed using at least one of: vibration separator, vibrating screen filter, vibrating separator, circular steps, linear vibrating screens/inclined movement, decanter centrifuges and filter press.

15. A method according to claim 14, where the vibratory separator includes at least one vibrating mesh filter.

16. A method according to claim 1, wherein the bleaching involves centrifugation and/or additional filtering of the filtered juice.

17. A method according to claim 16, where the lightening involves the application of at least one high-speed multi-disc centrifuge, microfiltration and ultrafiltration.

18. A method according to claim 1, wherein the clarified juice is stored in refrigerated storage tanks.

19. A method according to claim 1, wherein the coagulating includes lowering the pH of the clarified juice.

20. A method according to claim 19, where the pH is reduced to pH below about 6.

21. A method according to claim 19, where the pH is reduced to pH below about 5.

22. A method according to claim 19, where the pH is reduced to pH of approximately 4.5.

23. A method according to claim 19, where the lowering of pH involves the use of at least one acid selected from hydrochloric acid, nitric acid and sulfuric acid.

24. A method according to claim 1, wherein the coagulating perform CT using precipitator, comprising at least one heat exchanger.

25. A method according to claim 24, where the at least one heat exchanger includes at least one plate or tube heat exchanger or a heat exchanger with steam injection.

26. A method according to claim 1, wherein the coagulating comprises heating the clarified juice to a first temperature with obtaining broth; and cooling the broth to a second temperature.

27. A method according to claim 26, wherein the first temperature is from about 40°C to about 100°C.

28. A method according to claim 26, where the second temperature is lower than about 40°C.

29. A method according to claim 26, where the second temperature is lower than approximately 30°C.

30. A method according to claim 1, wherein the separation includes the use of high-speed multi-disc centrifuge.

31. A method according to claim 1, wherein the wet protein concentrate is stored in refrigerated storage tanks.

32. A method according to claim 1, further comprising drying the wet protein concentrate to produce dry protein concentrate.

33. A method according to claim 32, where the drying is performed using a spray dryer, drum dryer, turbulent dryers, flash dryers, fluidized bed dryer, double-drum dryers and rotary dryers.

34. A method according to claim 1, further comprising a contact material selected from the group consisting of a third solid phase and a clarified juice, �about least with one of the following: alcohol, solvent or water, and acid catalyst to form a mixture, separating the mixture of liquid and solid phase, resulting in lipids and ash forming components in the material is separated with liquid.

35. A method according to claim 1, further comprising, before or immediately after the destruction, the washing of the biomass with an aqueous solvent.



 

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15 cl, 3 dwg

FIELD: chemistry.

SUBSTANCE: invention relates to biotechnology of obtaining haemostatic medications. Claimed is method of separating purified fibrinogen concentrate, free of viruses and ballast proteins. Solubilisation of cryoprecipitate of fresh frozen human plasma is realised. Fibrinogen is precipitated with 20-30% PEG solution. Separated sediment is dissolved in buffer with sodium citrate and sodium chloride. Virus inactivation of solution by solvent-detergent method is carried out in presence of 1-3% Tween-80 and 0.1-1.5% of tri-n-butylphoshate. Obtained concentrate is purified from products of virus inactivation and solvent-detergents by triple extraction with liquid paraffin. After that, obtained fibrinogen concentrate is re-precipitated with 1.0-2.5 M glycine solution. Sterile filtration and lyophilic drying with further corking of lyophilisate under vacuum and thermal inactivation are performed.

EFFECT: invention makes it possible to obtained lyophilised form of fibrinogen concentrate with approximately 55% output.

FIELD: biotechnology.

SUBSTANCE: method comprises the steps of destroying the bodies of inclusion, renaturation and purification of protein. Before renaturation, the preliminary purification of protein is carried out using chromatography on Q-Sepharose and SP-Sepharose using the combined columns with Q- and SP-Sepharose. After renaturation chelate and ion-exchange chromatography of recombinant prourokinase M5 is carried out without intermediate elution of the target protein with use of metal-chelate sorbent activated with ions Co2+ or Zn2+.

EFFECT: invention enables to select prourokinase M5 from inclusion bodies, comprising the present prourokinase, with high yield.

4 cl, 2 tbl, 4 ex

FIELD: chemistry.

SUBSTANCE: invention relates to the field of obtaining and separation of single-domain molecules (SDAB). Described is a method of the separation or purification of the SDAB molecule, which represents a trivalent molecule of a ATN-103 nanobody, targeting TNFα and HAS, from a mixture, containing the said SDAB molecule and one or more polluting substances. The mixture is brought in contact with a cation-exchange carrier under conditions, which make it possible for the SDAB molecule to bind with the carrier or be absorbed on the carrier. One or more polluting substances are removed and SDAB is selectively eluted from the carrier. The conductivity of a conditioning medium (CM), used for the carrier loading, constitutes from approximately 12 to 9 mS/cm and pH under conditions of loading is corrected to a value from 4.0 to 4.3. The buffer for elution corresponds to approximately 50 mM of sodium chloride or less and has pH from approximately 5.5 to 7.2. Disclosed is a method or a process of obtaining recombinant SDAB of ATN-103. A host-cell is supported in the conditions at which recombinant ATN-103 SDAB is expressed. The mixture of molecule SDAB and one or more polluting substances is obtained. ATN-103 SDAB is purified or separated with the application of cation-exchange chromatography, as said above.

EFFECT: application of the invention provides new methods of the separation or purification of the nanobody, which can be applied in obtaining the ATN-103 nanobody.

19 cl, 4 dwg, 6 ex

FIELD: biotechnologies.

SUBSTANCE: method of obtaining of a complex of antimicrobic peptides of an insect includes infecting of adipose body of an insect at a larval instar with Micrococcus luteus A270 and Escherichia coli D31 bacteria with the subsequent extraction of adipose body of an insect at a larval instar. The adipose body of an insect is placed into a nutrient medium containing water solution of sugars, inorganic salts and the antibiotic meropenem in pre-set ratio and incubated during a day with the subsequent elution of the complex of antimicrobic peptides of an insect from cultural liquid by the method of reverse-phase chromatography on the column Vydac C18 at the linear gradient of acetonitrile from 0% up to 50%.

EFFECT: invention allows to simplify a method of obtaining antimicrobic peptides.

5 dwg, 4 ex

FIELD: chemistry.

SUBSTANCE: invention refers to peptide chemistry and concerns producing tripeptide diacetate H-β-Ala-Pro-DabNHBzl referred to a biologically active compound used in cosmetic industry as an active component for cosmetic products, particularly for stimulating skin rejuvenation, tightening and prevention. The method is based on the 6-staged synthesis and is free from the stages of setting and releasing the protective groups. The method involves proline β-chlorpionyl chloride acylation followed by producing N-(3-chlorpropionyl)proline pentafluorphenyl ester in the presence of N,N'-dicyclohexyl carbodiimide. The above pentafluorphenyl ester is condensed thereafter with glumatic acid monomethyl ester to produce N-(β-chlorpropionyl)-Pro-Glu(δ-OMe)OH. That is followed by benzylamine amidation in a combination with ammonolysis and chlorine substitution by an amino group. That enables producing the tripeptide β-Ala-Pro-Glu(δ-NH2)NHBzl; Hofmann rearrangement is conducted with the use of iodo-benzene diacetate to produce a target product.

EFFECT: method is characterised by simplicity, effectiveness; it is cost-effective and uses more accessible and cheap agents.

6 ex

FIELD: biotechnology.

SUBSTANCE: method of obtaining SSI comprises the following steps. The strain Yersinis pestis KM 1279 is grown on 1.5% agar LB, the bacteria are washed three times with cold buffered normal saline. The bacteria are pelleted by centrifugation, suspended in a solution of 5 mM NaOH, kept at 37°C for two hours and the cells are pelleted by centrifugation. The supernatant is selected and the procedure as repeated three times, three supernatants are combined and filtered through the nitrocellulose membrane. The filtrate is extracted three times with the mixture of chloroform-methanol-water in a ratio of 5:2:1. The chloroform fractions are separated by centrifugation, combined and freed from water-soluble impurities. The aqueous fraction is separated by centrifugation and removed, and the chloroform fraction is dried in a vacuum rotary evaporator and the dry preparation SSI is obtained. The proposed SSI is characterised with brown colouring of dry crystals, hydrophobic properties, fluorescence in ultraviolet, lipopeptide nature, the presence of iron ions, the molecular weight of 380.6 Da.

EFFECT: inventions enable to obtain the natural regulator of virulence of plague agent.

2 cl, 6 dwg, 6 ex

FIELD: medicine, pharmaceutics.

SUBSTANCE: invention refers to biotechnology. What is presented is a method for preparing a recombinant protein of type III interferon-like factor (ILF III) of the producing strain E. coli. The inclusion bodies E. coli are washed and dissolved with using 2% aqueous γ-cyclodextrin. That is followed by the sequential Ni-Sepharose, Q-Sepharose and SP-Sepharose chromatographic procedures. Refolding of a target protein is performed with using a mixture of cysteamine and cystamine at pH 10.5. The Amberchrome Profile XT20, Amberchrome Profile HPR10 and Kromasil 300-5C18 chromatographic procedures are sequentially performed.

EFFECT: invention enables optimising the ILF III purification environment at the stage of washing and dissolving the inclusion bodies Ecoli and provides 12% target protein yield.

3 dwg, 4 ex

FIELD: chemistry.

SUBSTANCE: invention relates to biotechnology, specifically to immunostimulating compounds and may be used in medicine. An immunostimulating peptide of an amino acid sequence XLYDKGYTSKEQKDCVGI, where N-terminal X is N-acetylalanine, and may be covalently linked to fatty acids, selected from C2-C25, to form PDAG (peptidyl-2,3-diacylglycerides). The resulted compound may be included in pharmaceutical formulations for stimulating an immune response.

EFFECT: invention provides efficient stimulation of an immune response in subjects and may enhance the immunogenicity of the antigenic peptide when administered with PDAG.

29 cl, 10 dwg, 9 ex

FIELD: biotechnology.

SUBSTANCE: method of production of peptides is proposed. Yeast autolysis is carried out. The cell membranes are separated by centrifugation. The autolysate is purified on the gel sulphocationite in the hydrogen form, containing 12-16% divinylbenzene. The resulting peptide aqueous solution is passed sequentially through the gel anion-exchange material to obtain the solution at pH 2.0-2.6, and then through the gel cation-exchange material with the divinylbenzene content of 1-2% or macroporous cation-exchange material.

EFFECT: obtaining highly purified peptides that have biological activity.

11 ex

FIELD: chemistry.

SUBSTANCE: invention relates to purification of various gamma-carboxylated olypeptide forms with application of ion-exchange chromatography. In particular, in accordance with invention, claimed is method of purification of polypeptide, which has desirable content of gamma-carboxyglutaminic acid, from sample, containing mixture of said polypeptide versions, which have different content of gamma-carboxyglutaminic acid, with the claimed method including stages: (a) loading said sample on anion-exchange chromatographic material; (b) elution of said polypeptide with application of solution with pH lower than 9.0, containing at least one salt, selected from ammonium acetate, ammonium chloride and sodium acetate; and (c) selection of fraction, obtained after said elution, with polypeptides in said fraction having desired content of gamma-carboxyglutaminic acids.

EFFECT: claimed is method of purifying polypeptide, which has desirable content of carboxyglutaminic acid.

8 cl, 13 dwg, 6 tbl, 7 ex

FIELD: agriculture.

SUBSTANCE: invention relates to agriculture, namely to devices for mixing feed. The unit comprises a working chamber mounted resiliently on a base and equipped with an actuator. The chamber is made hollow with a curvilinear helical surface. The chamber is assembled from four circular sections rigidly connected in a circle to each other and four straight sections. Each circular section is assembled from interconnected sub-sections in the form of strips to form helical lines on their surfaces and the helical surfaces in the form of triangular pockets. The rectangular sections are made of a strip folded along straight lines to form parallelograms. The strip is folded into cylindrical coils connected to each other along the longitudinal edges to form helical polygonal pockets of triangular shape on the inner surface, and on the outer surface - unidirectional helical polygonal lines.

EFFECT: use of the invention enables to improve the quality of the feed obtained.

14 dwg

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