Method for complex processing natural gas for obtaining fresh water and fuel and device for its realization

FIELD: petroleum chemistry, chemical technology.

SUBSTANCE: method involves carrying out the preparing synthesis gas by the gaseous oxidative conversion of natural gas with air oxygen, catalytic conversion of synthesis gas to a catalyzate followed by its cooling and separating and feeding a liquid phase into reactor for synthesis of gasoline. For aim reducing the cost of manufacturing catalytic preparing methanol is carried out in the synthesis reactor wherein methanol is fed into reactor for preparing high-octane components of gasoline that are stabilized and separated for liquid components and fatty gas that is fed into reactor for preparing oligomer-gasoline. Then liquid components from reactors wherein high-octane components of gasoline and oligomer-gasoline are prepared and then combined, and the mixture is stabilized. Water formed in all synthesis reactions after separating is removed separately, combined and fed to the fresh water preparing block and formed nitrogen is fed for storage with partial using in technological cycle and in storage of synthetic fuel. The unreacted depleted synthesis gas from block wherein methanol is prepared is used for feeding methanol into reactor sprayers for preparing high-octane component of gasoline, and unreacted gases from reactor for preparing oligomer-gasoline are fed into generator for synthesis gas. Also, invention claims the device for realization of the method. The device consists of blocks for preparing synthesis gas, catalytic conversion of synthesis gas to catalyzate and preparing gasoline and made of two separate reactors for preparing high-octane additive of gasoline and oligomer-gasoline. The device is fitted additionally by block for preparing fresh water and nitrogen collector. The reactor sprayers are connected with intermediate capacity for collection of methanol and with reactor for synthesis of methanol and block for preparing methanol, and reactor for preparing oligomer-gasoline is connected pneumatically with block for preparing synthesis gas. Invention provides the development of method for the combined preparing the fuel and fresh water.

EFFECT: improved preparing method.

2 cl, 6 dwg, 2 ex

 

The invention relates to a method for integrated processing of natural gas and air with simultaneous production of water for drinking and agricultural purposes, high-octane components of gasoline and gases.

The known method for complex processing of sea water to obtain fresh water and valuable mineral components. The method includes the successive stages of mechanical filtration, separation elements and salts present in sea water and brines and fresh water [1].

The main disadvantages of the method according to the patent of Russian Federation №2089511 are cumbersome equipment, low production efficiency, high energy costs, high cost of produced fresh water.

Known technology for processing natural gas into synthetic diesel and jet fuel for small installations of low pressure [2].

Known technology includes two main stages: the production of synthesis gas by methane reforming and Fischer-Tropsch synthesis, allowing a single-pass process to obtain high outputs fraction With7-C20. Optionally, the technology can be included and standard stage fractionation.

The main disadvantages of the technology are low productivity, a narrow range obtained cont the work (including up to 30% of low-octane gasoline plus fraction, requiring additional processing), the high cost of the whole process with the utilization of water as the waste of the primary production.

Also known a method of producing motor fuels from carbon-containing raw material with sequential final product from the feedstock, the synthesis gas. The gas flow after the first stage reactor is cooled and separated into a liquid fraction and a gas phase containing neprevyshenie components of synthesis gas and dimethyl ether (DME), while the liquid fraction is further isolated DME, and the gas phase is divided into 2 streams - one is mixed with the synthesis gas and is fed into the same reactor of the first stage. The second gas stream is fed to the second stage, where upon contact with a catalyst comprising zeolite ZSM-5 and metaloxides component is the conversion of DME and components of synthesis gas into gasoline fraction, gaseous hydrocarbons and water fraction (EN 2143417) [3].

The main disadvantages of this method of producing motor fuels from carbonaceous raw materials by RF patent No. 2143417 are: the need to use oxygen for the production of synthesis gas, which in turn requires the creation of oxygen equipment with significant capital investment and high operating costs, low yield of DME, and therefore, a gasoline fraction, a high cost is the cost of the process, a high degree of pollution of the water fraction with subsequent disposal together with gaseous hydrocarbons.

The known method of producing motor fuels, which receive the synthesis gas non-catalytic gas-phase oxidative conversion of natural gas with oxygen at a temperature of 800-1500°and a pressure of 1-10 MPa. This is followed by catalytic conversion of synthesis gas in the synthesis reactor, dimethyl ether, followed by cooling the product gas mixture, and the division into liquid and gas phase. Thus from the liquid phase produce dimethyl ether, which is sent to the catalytic reactor synthesis gas, and a gas phase containing neprevyshenie components of synthesis gas, is directed to re-catalytic conversion in an additional reactor for the synthesis of dimethyl ether without mixing with the original synthesis gas (EN 2226524) [4].

The method allows to increase the yield of dimethyl ether and accordingly gasoline fraction and reduce the cost of the process due to the use of oxygen, however, does not solve the problem of complex processing of natural gas, disposing of waste, including of course a valuable commodity product - water, also remains high overall cost of production.

The technical objective of the claimed group of inventions is to improve water quality, reduce their cost, improving the environment, improving the efficiency of the process.

The goal of the project is achieved by the method of complex processing of natural gas, providing for receiving fresh water and fuel, including the production of synthesis gas of gas-phase oxidative conversion of natural gas with oxygen, kompremirovannyj synthesis gas, the purification from residual oxygen and moisture, the subsequent catalytic conversion of synthesis gas to produce cooling and separation catalyzate with the direction of the liquid phase catalyzate in reactor production of gasoline and water separation in the receiver-separator, characterized in that, to improve water quality, reduce cost, improve the environment and increase the efficiency of the process, from the reactor synthesis catalyzate the formed methanol is sent to the reactor high octane components of gasoline, where in the presence of a zeolite catalyst at a pressure of 0.7-1.0 MPa and a given temperature produces high-octane components of gasoline, which is divided into a liquid condensate and rich gas directed into the reactor to obtain the oligomer-gasoline, and liquid condensate is separated into an aqueous layer and an organic liquid products, combining with the previously obtained oligomer-gasoline and served in the hundred block the waste utilization technologies gasoline, while the water generated during the execution of all stages of the synthesis products, after separative separately output, are combined and fed into the preparation unit of fresh water, where it is distilled residues of methanol and fatty hydrocarbons, is subjected to bioremediation and salinity, and sedimentation method, the nitrogen supplied to the storage and partial use in the production cycle, while the unreacted gases from the reactor to obtain the oligomer-gasoline is sent to the generator synthesis gas and depleted synthesis gas reactor high octane components of gasoline fed to the spray of methanol injectors these reactors.

The goal of the project is also achieved by the plant for complex processing of natural gas with obtaining fresh water and fuel containing unit for production of synthesis gas containing nodes purification and compression of air and natural gas, synthetic gas generator, the site of compression of the synthesis gas, the unit production of methanol, including reactors purification of synthesis gas, a reactor for methanol synthesis, filled with a catalyst and mounted in series, a heat exchanger, an intermediate tank for collecting methanol, block high octane components of gasoline, including filled zeolite catalyst reactors, nozzles which newmagic aulacese associated with intermediate capacity gathering of methanol and reactors for methanol synthesis, refrigerator, three phase separator, a unit for production of oligomer-gasoline, including the reactor obtain the oligomer-gasoline, pneumatically connected to the block synthesis gas, gasoline stabilizer, including stabilization column, the capacity to collect petrol, the preparation unit of fresh water, including site distillation of the residual methanol and hydrocarbons, the nodes of bioremediation and water salinity, tanks for water harvesting, the collection of nitrogen.

In the basis of the method for integrated processing of natural gas with obtaining fresh water and fuel on the development of highly efficient technologies for production of synthesis gas, methanol and high-octane components of gasoline (wok), allowing clean with preservation of the environment to solve the problem of obtaining an additional source of water for drinking and agricultural purposes. The way the original surpasses international standards of cost, depth and complexity of processing of raw materials with a high degree of use of the end products and energozapchast to the overall process.

The material flows of the process of obtaining water and hydrocarbons from natural gas
1. The production of synthesis gas from natural gas:
Taken:Received:
Natural gas1427 kg/hWater660 kg/h
The air10502 kg/hCabalistically synthesis gas11269 kg/h
Total:11929 kg/h11929 kg/h
2. The methanol synthesis

Taken:Received:
CabalisticallyWet methanol, including
synthesis gas11269 kg/hMethanol1323,6 kg/h
Water41 kg/h
Inert gas9904,4
Total:11269 kg/hKg/h
3. Obtaining water and hydrocarbons
Taken:Received:
Wet methanol, includingWater784,0 kg/h
Methanol1323,6 kg/hHydrocarbons
Water41 kg/h(liquid and gaseous)578,6 kg/h
Methanol narora.2.0 kg/h
Total:1364,6 kg/h1364,6 kg/h
Consumption per 1 ton of produced water and 0,4T hydrocarbon per hour:
1. Natural gas988,23 kg/h
2. The air7272,85 kg/h

Principle the Lok diagram, installation of complex processing of natural gas, including get fresh (potable) water are presented in figure 1 figure 2-7 shows circuit blocks installation of complex processing of natural gas.

The installation integrated natural gas processing block contains (1) a synthesis gas (BS-Y), block (7) the production of methanol (BM), block (25) high octane components of gasoline (BVCB), block (30) of receipt of the oligomer-gasoline from fatty gases formed after the block (7) BVCB (BO-B), block (37) stabilization of gasoline (BSB), block (42) preparation of fresh water (BPV), collection (48) nitrogen generated in the process of implementation of the method.

Unit (1) for production of synthesis gas (BS-D) includes the node (2) purification and compression of air, the node (3) cleaning, preparation and compression of natural gas, the node (4) mixing of air and natural gas generator (5) synthesis gas, the node (6) the compression of the synthesis gas (see figure 2).

Block (7) the production of methanol BM (see figure 1 and 3) includes a reactor (8) and (9) purification of synthesis gas (SG) from residual oxygen and moisture, refrigerators (10-12), receivers, separators (13-15), reactors (16-18) synthesis of methanol, mounted in series, a heat exchanger (19) heating of the gas, the intermediate tank (20) for collecting methanol.

Block (25) high octane components of gasoline (BVCB) (see figure 1 and 4) includes a pump (21) feeding methanol, recupera the passive heat exchanger (22), reactors (23-24) high octane components of gasoline (PSC), water cooler (26), three phase separator (27), oven (28) for heating the regeneration gas, the compressor (29) gas regeneration.

Block (30) of receipt of the oligomer-gasoline from fatty gases (BO-B) includes a compressor (31) liquid gas, refrigerator (32), separator (33), furnace (34) for heating the regeneration gas, the reactor (35) oligomerization of petrol, compressor (36) for feeding gas regeneration (figure 1 and 5).

Block (37) stabilization of gasoline (BSB) (figure 1 and 6) includes a casing (38) stabilization, air cooler (39), reflux tank (40), a receptacle (41) for the collection of commercial gasoline.

Block (42) preparation of fresh (potable) water (BPV) has a node (43) distillation residues of methanol and fatty hydrocarbons, the node (44) of bioremediation, the node (45) mineralization and improve taste of water, the intermediate tank (46) for water collection, storage capacity (47) for water. (figure 1 and 7).

Below is a description of work installation and method for integrated processing of natural gas. Natural gas after passing through the node (3) cleaning, preparation and compression are mixed in node (4) mixing with air, passed through the node (2) purification and compression of the air unit (1) for production of synthesis gas in a ratio of 1:5 or 1:6, and then enters the generator (5) synthesis gas, where at a temperature of 850-900 (2000° (C) the formation of synthesis gas (a ratio of N2:WITH=2,1:1 or 1.8:1, respectively). Then the obtained synthesis gas at 260°C, a pressure of 4.5-5.0 MPa and a flow rate of 5000 h-1-4000 h-1comes from a node (6) the compression of the synthesis gas unit (1) for production of synthesis gas at a pressure of 5.0 MPa in the reactor (8) purification of synthesis gas from residual oxygen (0.5%), if the oxygen concentration in the synthesis gas exceeds 0.5% vol. The reactor (8) purification of synthesis gas from residual oxygen tube, loaded Ecumenical-copper (or alumapalooza) catalyst. Loading capacity 3.0 m3(3.6 t) at a space velocity of the gas 8000 h-1. Operating temperature 200-240°C. After the reactor (8-9), (16-18) there are water coolers (10-12) and the receiver - separator (13-15) to capture water generated during cleaning.

Thus purged of residual oxygen synthesis gas is fed into the intermediate reactor (9) for its purification from residual moisture (required for purification of soot when available). The reactor (9) is a vertical cylindrical apparatus, the loaded adsorbent is silica gel. Loading capacity is determined by the performance of the installation. The operating temperature of the reactor 40-50°C. Apply two parallel switchable reacto is a, one of which is open, and the other is in the stage of regeneration of the adsorbent as a loss in adsorption capacity. Regeneration is carried out in a stream of nitrogen 200-300 h-1at a temperature of 140-160°C.

Next, the synthesis gas is sent to the first of the three reactors (16-18) methanol synthesis BM, passing heated to 160-180°With the built-in reactor heater.

The shell-and-tube reactor, loaded alûmocink-copper catalyst. The working temperature of 240-250°C.

The catalyst for methanol synthesis is activated once for the entire service life, so the hydrogen economy is only necessary during the period of preparation for the installation to work. Reactors (16-18), mounted on a "cascade", without preheating the syngas. After each reactor there are water coolers (10-12) and the receiver-separator (13-15) to collect the formed methanol.

The production of methanol is accompanied by release of heat energy (110,8 kJ per mol when using pure methanol or 3090000 kJ per tonne methanol), which can cause excessive temperature rise, which leads to irreversible reduction of the activity of the catalyst. The maximum allowable temperature is 270 C. For partial removal of heat of reaction and to feed the system with synthesis gas in the annular space of the reactor is served cold (60-80°synthesis gas after cleaning and drying.

Block (7) the production of methanol also contains a heat exchanger (19) of the heated gas (synthesis gas) and the intermediate tank (20) for collecting methanol. Receiver-separator (13-15) all reactor unit (7) methanol is fed into the intermediate tank (20) for collecting methanol. Next, the methanol from the intermediate vessel (20) of the block (7) is served by a pump (21) feeding methanol after heating in a recuperative heat exchanger (22) to 180-220°in the reactors (23-24) high octane components of gasoline (BVCB) block (25) receiving BVCB. Depleted synthesis gas thus fed to the spray of methanol in the nozzle reactor of high octane components of gasoline (PSC). Reactors (23-24) high octane components of gasoline unit (25) to obtain the WKB operate alternately with meregenerasikan pre-owned no less than 500 hours, filled with zeolite catalyst containing zeolite type pentasil. Catalytic conversion is carried out at a pressure of 0.7-1.0 MPa. The total amount of catalyst in each reactor (23-24) obtain the WKB is not less than 3.3 m3.

Temperature reactors (23-24) is regulated to maintain a certain conversion of raw materials throughout the conversion cycle. Removing the exothermic heat of reaction occurs through the inner surface of the reaction space. The heat flux then use the : as a source of heat for heating gas recycle, supply of heat exchangers and heating cube column stabilization (38) of the block (37) stabilization of gasoline.

Regeneration of the catalyst is carried out at a pressure of 0.7-1.0 MPa nitrogen-air mixture circulating through the compressor.

For heating gases regeneration of catalysts are heat exchangers and furnace (figure 1 conventionally not shown) for heating the regeneration gas. Regeneration time 100-120 hours, the service life of the zeolite catalyst is not less than 2 years.

The reaction products (produce) temperature 420-430°from reactors (23-24) are heat recovery heat exchanger (22) heating of the substrate, then after cooling in a water-refrigerator (26) of the block (25) receiving BVCB catalysate is divided in three-phase separator (27) of the block (25) receiving BVCB. Fatty gases enter the reactor (35) oligomerization unit (30) to obtain the oligomer-gasoline (BO-B)containing the compressor (31) liquid gas, refrigerator (32), separator (33), furnace (34) for heating the regeneration gas and the compressor (36) for feeding gas regeneration. Liquid condensate is stratified and settled in the separator (33), the aqueous layer was separated, and the liquid organic products pump going on pre-heated in heat exchangers and in column (38) stabilization unit (37) stabilization of gasoline, operating at a pressure of 1.2-1.4 MPa. In the reactor (35) of the block (30) bio-B at a pressure of 2 MPa going on the t turn Alifanov with the formation of oligomer-gasoline. In the reactor (35) may use the same zeolite catalyst. Unreacted gases from the top of the reactor (35) receiving the oligomer petrol unit (30) of receipt of bio-B are sent to the generator (5) synthesis gas unit (1) for production of synthesis gas, and the resulting liquid organic products combined with unstable gasoline from a three-phase separator (27) of the block (25) receiving BVCB and sent to the column (36) stabilization unit (37) stabilization of gasoline. Operating temperature reactor (35) of the block (30) bio-B 340-380°C, the volumetric rate of supply of liquefied gases 2-4 h-1.

The filtration element of the purification unit and the compression of air BS-G provides purification from oil and particles.

The generator (5) synthesis gas BS-G is getting gas of the following composition:

H2=25 - 28%CO=12-14%
CO2=3-4%CH4≤1,5%
O2=0%S≤0.1 ppm
the water droplet phaseno
nitric oxideno

The generator works (5) synthesis gas at pressures up to 1 MPa, working temperature is not more than 1000° (in the case of catalytic conversion of methane into synthesis gas). The temperature of the synthesis gas at the outlet of heat is obmennik no more than 30-50° C.

Depending on the objectives and performance requirements in BS-G can connect several generators, including different types of reactors.

From the bottom of the column (38) stabilization unit (37) stabilization of gasoline is withdrawn stable gasoline and after cooling is eliminated with the installation as a commercial product in a container (41) for the collection of commercial gasoline.

Top zipper columns (38) stabilization is cooled in air cooler (39) of the block (37) stabilization of gasoline and collected in the reflux tank (40) block (37) stabilization of gasoline (BSB). Liquid organic condensate is partially served by a pump (not specified conditionally) for irrigation columns (38) of the block (37), BSB, and a specified number circulates in the reactor (23-24) obtain PSC block (25) receiving BVCB. The use of two parallel blocks (25) receiving BVCB and (30) to obtain the oligomer-gasoline bio-B increases the water outlet.

Water is supplied to the node (43) distillation residues of methanol and fatty hydrocarbon block (42) preparation of fresh water BPV and then enters the node (44) bioremediation, where it completes its cleanup.

Node (45) mineralization and taste of the water block (42) BPV completes the process of obtaining water for drinking and agricultural purposes. Block (42) contains intermediate and cumulative capacity (46-47) is water.

Ustanovochnaja automatic control system, ensure trouble-free automatic shut-off when the malfunction of individual items.

Below are specific examples of the implementation of the inventive method, in accordance with the above process scheme and the operation of the unit indicating the specific examples of the modes of implementation of individual stages of the method, which accordingly do not limit it.

Example 1.

Feedstock natural gas is mixed with air in the ratio of 1:5-6, after which the mixture is fed to the Converter gas-phase oxidative reforming of natural gas with oxygen in the air, where the temperature 850-2000°With the formation of synthesis gas with a ratio of N2:WITH=a 1.8-to 2.1:1. The resulting synthesis gas after the site of compression at a pressure of 5.0 MPa is fed into the reactor for purification of residual oxygen, if the oxygen concentration in the synthesis gas exceeds 0.4% when the feeding speed of the gas 8000 h-1and the working temperature of 200-240°C. After the reactor purification of the synthesis gas is cooled and fed into the receiver-separator to trap water generated during cleaning.

Then the obtained sites gas at 260°C, a pressure of 4.5 to 5 MPa and a flow rate 4000-5000 h-1is directed to catalytic conversion to methanol synthesis reactor. The resulting produce is cooled. After that section is Aut liquid (methanol-raw) and the gas phase. Methanol raw enters the catalytic conversion reactor, where 380-430°C, a pressure of 0.6-1.0 MPa in contact with a catalyst containing a zeolite of type pentasil and metal oxide component, resulting in water and hydrocarbons (liquid and gaseous) in a ratio of 1:0.5 on feedstock is natural gas. Gaseous hydrocarbons are reactor obtain the oligomer-gasoline. Water generated at all stages of the synthesis are combined and fed into the preparation unit of fresh water.

Example 2.

Natural gas is mixed with air in the ratio of 1:6 and fed into the Converter, where at a temperature of 2000°With the formation of synthesis gas in a ratio of N2:WITH=a 1.8:1. Then the obtained synthesis gas at 260°C, a pressure of 4.5 MPa and a flow rate of 4000 h-1supplied to the methanol synthesis reactor. The formed methanol into the reactor conversion, where at 430°C, pressure of 1.0 MPa is in contact with a catalyst containing a zeolite of type pentasil, resulting in water and hydrocarbons in a ratio of 1:0.4 natural gas.

The principal block diagram of the installation of fresh water complex processing of natural gas is shown in Fig 1.

The estimated capacity of the plant in the example, up to 16 TT/year of water and up to 6.3 TT/year WKB (or up to 10 TT/year of gasoline).

The site clear and natural gas BS-G provides a sulfur content of 0.1 ppm in the form of H 2S, chlorine is missing

Sources of information

1. RF patent №2089511, C 02 F 1/42, publ. 10.09.97. Bulletin No. 25.

2. Kagan D.N., A.L. Lapidus, Krylov, A. Development melastatin technologies for processing natural gas into synthetic diesel and jet fuel for small installations of low pressure. - Gas chemistry in the twenty-first century. Problems and prospects (proceedings of the Moscow seminar on gas chemistry 2000-2002). M., 2003, p.131-170.

3. RF patent №2143417, C 07 C 1/04, 41/06, publ. 1999. Bulletin No. 12.

4. RF patent №2226524, C 07 C 1/04, 41/06, 43/04, C 10 G 3/00, publ. 10.04.2004. Bulletin No. 10.

1. Method for integrated processing of natural gas, providing for receiving fresh water and fuel, including the production of synthesis gas of gas-phase oxidative conversion of natural gas with oxygen, kompremirovannyj synthesis gas, the purification from residual oxygen and moisture, the subsequent catalytic conversion of synthesis gas to produce cooling and separation catalyzate with the direction of the liquid phase catalyzate in reactor production of gasoline and water separation in the receiver-separator, the synthesis reactor catalyzate the formed methanol is sent to the reactor high octane components of gasoline, where in the presence of a zeolite catalyst at a pressure of 0.7-1.0 MPa and a given temperature get high-octane components of gasoline, which is divided into a liquid condensate and rich gas, directed into the reactor to obtain the oligomer-gasoline, and liquid condensate is separated into an aqueous layer and an organic liquid products, combining with the previously obtained oligomer-gasoline and served in a gasoline stabilizer, while the water generated during the execution of all stages of the synthesis products, after separative separately output, are combined and fed into the preparation unit of fresh water, where it is distilled residues of methanol and fatty hydrocarbons, is subjected to bioremediation and salinity, and sedimentation method, the nitrogen supplied to the storage and partial use in the production cycle, while the unreacted gases from the reactor to obtain the oligomer-gasoline is sent to the generator synthesis gas and depleted synthesis gas reactor high octane components of gasoline fed to the spray of methanol injectors these reactors.

2. Plant for complex processing of natural gas by the method according to claim 1 with obtaining fresh water and fuel containing unit for production of synthesis gas containing nodes purification and compression of air and natural gas, synthetic gas generator, the site of compression of the synthesis gas, the unit production of methanol, including reactors purification of synthesis gas, a reactor for methanol synthesis, filled with a catalyst and mounted in series, the heat transfer is IR, the intermediate tank to collect methanol, block high octane components of gasoline, including filled zeolite catalyst reactors, nozzles which pneumohydraulic associated with intermediate capacity gathering of methanol and reactors for methanol synthesis, refrigerator, three phase separator, a unit for production of oligomer-gasoline, including the reactor obtain the oligomer-gasoline, pneumatically connected to the block synthesis gas, gasoline stabilizer, including stabilization column, the capacity to collect petrol, the preparation unit of fresh water, including site distillation of the residual methanol and hydrocarbons, the nodes of bioremediation and water salinity, tanks for water harvesting, the collection of nitrogen.



 

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4 dwg

FIELD: chemical industry; petrochemical industry; bio-engineering; methods of purification of the concentrated waste waters.

SUBSTANCE: the invention is pertaining to bio-engineering, in particular, to purification of the concentrated waste waters and may be used in chemical and petrochemical industries. The method of purification of the concentrated waste water containing aromatic hydrocarbons and their derivatives, peroxides and aldehydes, includes an aerobic treatment with strains of bacteria Pseudomonas sp. VCPV-3893 and Rhodococcus sp. VCLMV-3892. At that before the stage of the aerobic treatment carry out a preliminary purification of the waste waters by a consecutive stages of treatment of the waste waters with an alkaline solution up to the pH value of no less than 9.5. Then conduct the further distillation of the treated flow at the temperature of the bottom distillation residue of the column of no less than 98°C and the duration of presence of no less than 0.2 hour. At that the bottom distillation residue of the column is directed to the stage of the aerobic treatment and the upper product of the column is directed to utilization. The method allows to purify effectively the concentrated waste waters containing aromatic hydrocarbons and their derivatives, and also peroxides and aldehydes.

EFFECT: the invention ensures effective purification of the concentrated waste waters containing aromatic hydrocarbons, their derivatives, peroxides and aldehydes.

4 ex

The invention relates to a device for biological wastewater treatment

The invention relates to techniques for filtering microbial reagent-free water treatment for drinking water from the storage conditions on the surface and submarine vessels of the long voyage, the crew of spacecraft and orbital stations

The invention relates to methods of treatment of polluted groundwater anthropogenic pollutants, and after the ISL

The invention relates to the field of water purification, namely the reagentless field of water treatment, and can be used to supply drinking water to consumers located in places of temporary stay of people, or small urban, or when disconnecting consumers from the mains water supply
The invention relates to the field of purification of water in hydrolysis, pulp and paper, machinery and other industries, forming wastewater contaminated with petroleum products, organic and suspended solids

The invention relates to methods of wastewater treatment and can be used on small enterprises processing meat and meat products

The invention relates to the field of deep biological treatment of water from difficultly oxidizable organic compounds

FIELD: chemical industry; petrochemical industry; bio-engineering; methods of purification of the concentrated waste waters.

SUBSTANCE: the invention is pertaining to bio-engineering, in particular, to purification of the concentrated waste waters and may be used in chemical and petrochemical industries. The method of purification of the concentrated waste water containing aromatic hydrocarbons and their derivatives, peroxides and aldehydes, includes an aerobic treatment with strains of bacteria Pseudomonas sp. VCPV-3893 and Rhodococcus sp. VCLMV-3892. At that before the stage of the aerobic treatment carry out a preliminary purification of the waste waters by a consecutive stages of treatment of the waste waters with an alkaline solution up to the pH value of no less than 9.5. Then conduct the further distillation of the treated flow at the temperature of the bottom distillation residue of the column of no less than 98°C and the duration of presence of no less than 0.2 hour. At that the bottom distillation residue of the column is directed to the stage of the aerobic treatment and the upper product of the column is directed to utilization. The method allows to purify effectively the concentrated waste waters containing aromatic hydrocarbons and their derivatives, and also peroxides and aldehydes.

EFFECT: the invention ensures effective purification of the concentrated waste waters containing aromatic hydrocarbons, their derivatives, peroxides and aldehydes.

4 ex

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