Paper products from straw of cereals of natural colour and their fabrication technique

FIELD: textiles, paper.

SUBSTANCE: whiteness of paper products of natural colour is 35-60% ISO, and for their production unbleached straw cellulose is used with a tensile strength of 230-280 mN, fracture strength with multiple bends of 40-90 times and permanganate index of 16-28. The composition of natural-coloured paper products includes sanitary and hygienic natural-coloured paper, paper towel of natural colour, paper for wipe of natural colour, paper for photocopies of natural colour, paper box for food of natural colour, natural-coloured wrapping paper for food products, and printing paper of natural colour.

EFFECT: strength of the above mentioned paper products is high, and when control over the content of harmful substances dioxin and adsorbable organic halides are not detected.

24 cl, 20 ex

 

The technical field

This invention relates to paper products made of straw cereals natural color and method of manufacture, specifically, the use of unbleached pulp from straw of cereals as main raw material for the manufacture of paper products natural colors and themselves made paper products.

The level of technology

Household paper is one of the objects of consumption, taking into account the psychological requirements for the degree of whiteness, and some physical characteristics of paper pulp is made mainly from bleached wood pulp. Below are a few existing technological solutions manufacturing household paper.

CN 94105089 relates to sanitary-hygienic paper with a highly effective drug for recovery from wheat straw, manufacturing techniques presented paper in this literature, including included the manufacture of paper sheets.

In CN 200410026132 disclosed method of manufacture of household paper of collagen fibers and vegetable fibers, which is to prepare the cellulose solution bleached pulp from coniferous (broadleaf) species of wood and pulp from wheat straw with a mass concentration of from 1% to 4%, the Otomi mix this solution with the cellulose of collagen fibers add the softener in the pool cellulose, then the obtained cellulose material is delivered to the filter paper machine for the extrusion, drying, twisting to get the products.

Pollutants from the pulp and paper industry are mainly generated in the processing and production of black liquor after cooking and bleaching of cellulose, especially in later. In traditional chlorine-containing waste bleaching solutions are not only common factors causing pollution of the water environment, such as COD and BOD, and other specific pollutants. For example, chloroform, formed in the bleaching process the chloride and hypochlorite. Its content in the exhaust after bleaching solutions of one ton of pulp hypochlorite from pressing sugar cane is about 150-250 g, waste solutions after bleaching of wood pulp, about 700, And in waste solutions whitening chloride, in addition to chloroform, it also contains more than 40 species of organic chlorides, such as 2-chlorophenol, 3-chlorophenol, dioxins and chlorofuran, many of which are highly toxic. Oh threatened by conversion to the deformity, cancer and abrupt change.

In Western Europe, Hong Kong, Taiwan, Japan, South Korea set a strict limit to the EXT is VCE harmful substances in the production process office paper the prohibition of the use of chlorine-containing bleaching tools and Breitner and mandatory requirements for the content of harmful substances in the production process. In Japan is limited to white (70%), to avoid the application of brainer not in moderation. Rate this: in waste water COD≤20 kg/t of paper; AOX≤0.3 kg/t of paper. Water pollution will cost businesses and society in high price.

In the above map documents used wheat straw or plant fiber as raw materials manufacturing sanitary paper or household paper. Due to the backwardness of the existing methods in the manufacture of cellulose from straw of cereals usually cook the cereal raw materials to its low hardness. For example, to get permanganate calcium 11-14 requires a large amount of the applied solution of reagents for cooking and long term heating and holding temperature, which will inevitably lead to grinding and damage to the cellulose and hemicellulose in the cereal raw materials. Resulting strength of the prepared straw pulp is relatively low, and the quality of the produced tissue paper and household paper is not satisfactory. In addition, in the process of making sanitary paper and domestic boom is GI existing technology necessary step bleaching, which will lead to environmental pollution and the products. Educated dioxins and adsorbed organic halides are substances that cause cancer; however, in the process of making paper from wood pulp current technology requires the addition of Breitner and other harmful substances, the balance of which to a certain extent, threatening the health of the user.

Therefore, the relative lack of current technology pulp and paper industry and the manufacturing of higher-quality paper pulp from straw of cereals represent the invention.

The content of the inventions

The main purpose of this invention is in the manufacture of paper articles of straw cereals natural colors, which include sanitary paper natural color, paper towel, natural color, paper for drying natural color, paper photocopies natural color paper box for food, natural colors, wrapping paper for food products natural color and printing paper natural color. The strength of the above paper products is high, and when control over the content of harmful substances in them is not detected dioxin and adsorbed organic halides.

To implement vishey the marks, use the following technological solutions.

Manufactured paper products natural color of raw unbleached pulp from straw of cereals. White presented paper products natural color 25-60% ISO, preferably white-mentioned items - 35-45% ISO.

The breaking length of the unbleached straw pulp described in this invention, is 5.0-7.5 km, tear resistance - 230-280 mn, tensile fracture with multiple kinks - 40-90 times, white - 25-45% ISO, the degree of grinding cellulose - 32-38°SR; preferably the breaking length of the specified unbleached straw pulp is 6.5-7.5 km, tear resistance - 250-280 mn, tensile fracture - 65-90 time, the degree of grinding cellulose - 32-36°SR, white - 35-45% ISO.

Part of paper products natural color, set forth in this invention, includes sanitary paper natural color, paper towel, natural color, paper for drying natural color, paper photocopies natural color paper box for food, natural colors, wrapping paper for food products natural color and printing paper natural color.

Paper products natural color, set forth in this invention are sanitary paper natural color, which contains 70-100% of the unbleached straw pulp and 0-30% notbale the Noah wood pulp. The height of capillary rise of a liquid in the transverse direction of its products 30-100 mm/100, preferably the height of capillary rise of a liquid in the transverse direction - 40-100 mm/100, more preferably product - 50-80 mm/100 C.

Index tensile strength tissue paper natural color, set forth in this invention is 4 to 12 N·m/g, preferably paper - 8-12 N·m/g; softness described paper - 120-180 mn, preferably paper - 120-150 mn; density described paper - 10,0-18,0 g/m2preferably paper - 11,0-13,0 g/m2.

Paper products natural color, set forth in this invention, paper towel, which contains 70-100% of the unbleached straw pulp and 0-30% of unbleached wood pulp. Its tensile strength in the wet state in the longitudinal direction is 22-55 N/m, preferably 30-45 N/m

The height of capillary rise of a liquid in the transverse direction of the paper towels natural color, set forth in this invention, 30-100 mm/100, preferably 40-100 mm/100, more preferably 50-80 mm/100 C.

The softness and density of paper towels natural color, set forth in this invention, respectively 120-180 mn and 23.0-45,0 g/m2, preferably 120-150 mn and 3.0-40,0 g/m 2.

Paper products natural color, set forth in this invention are paper box for food, natural color, which is made from 70-100% of the unbleached straw pulp and 0-30% of unbleached wood pulp, the characteristics of which conform to the requirements of the paper box for food on GB 18006.1-1999 A.

Paper products natural color, set forth in this invention, are photocopy paper natural color, which contains 50-80% of the unbleached straw pulp and 20-50% of unbleached wood pulp. Average breaking length presented paper in the longitudinal and transverse direction is 3.2-7.5 km, and preferably 4.5 to 7.5 km, more preferably - 6,0-7,5 km

Tensile fracture during repeated bending in the transverse direction of the paper photocopies natural color, set forth in this invention, is 60-200 times, preferably 80-185 time.

The density of paper photocopies natural color, set forth in this invention, are 60,0-75,0 g/m2preferably - 65,0-72,0 g/m2more preferably 69,0-72,0 g/m2; opacity paper photocopies natural color, set forth in this invention, is 82,0-98,0%, preferably 90-98%.

Paper products natural color, set forth in this invention, ablauts the wrapping paper for food, which contains 50-70% of the unbleached straw pulp and 30-50% of unbleached wood pulp. Its breaking length is 3.2-7.6 km, preferably 4,5-7,6 km

The density and tensile fracture during repeated bending in the transverse direction of wrapping paper natural colors for the food products described in this invention, respectively 45-65 g/m2and 90-200 times; preferably 50-60 g/m2and 120-200 time.

Tear resistance in the transverse direction of wrapping paper natural colors for the food products described in this invention, are 300-600 mn, preferably 400-600 mn.

White offset paper natural color, set forth in this invention, is 30-60% ISO, its pulp contains 65-85% of the unbleached straw pulp and 15-35% of unbleached wood pulp.

Breaking length offset paper natural color, set forth in this invention, is 2.5-5.5 km, and for the selected offset paper - 3,5-5,5 km

Opacity, offset paper, natural color, set forth in this invention, is 82-98%, and for the selected offset paper - 85-98%, for more than the selected offset paper - 92-98%.

Tensile fracture during repeated bending in the transverse direction offset paper natural color, set forth in this breath is reenie, is 10-35 times, preferably 15-35 times.

Paper products natural color, set forth in this invention are paper to wipe that contains 70-100% of the unbleached straw pulp and 0-30% of unbleached wood pulp. Its tensile strength in the wet state in the longitudinal direction is 22-55 N/m, preferably 30-45 N/m

The height of capillary rise of a liquid in the transverse direction is presented paper for drying natural color 30-100 mm/100, preferably 40-100 mm/100, more preferably 50-80 mm/100 C.

The softness and density of the presented paper for drying natural colors respectively 120-200 mn and 14.0-36,0 g/m2, preferably 120-180 mn and 18-28 g/m2.

In steps of receiving unbleached straw pulp described in this invention, includes cooking and washing, in particular, to obtain the highly rigid straw pulp permanganate number of 16-28 and the degree of grinding of 10-24°SR after cooking raw materials from cereals; preferably with permanganate number 16-23 and the degree of grinding of 10-24°SR.

The preparation described unbleached straw pulp is in the order of cooking, washing and oxygen delignification. Oxygen delignification includes: pumping pulp hardness permanganate is the number of 16-28 after cooking with the addition of alkali and oxygen in the reactor column oxygen delignification; in the reaction of delignification is formed pulp hardness permanganate number 10-14.

Selected oxygen delignification - one-step, this reaction is carried out in the reactor column oxygen delignification; temperature and pressure set forth the highly rigid pulp at the inlet and at the outlet of this reactor columns, respectively 95-100°C, 0.9 To 1.2 MPa and 100-105°C, 0.2-0.6 MPa; during oxygen delignification the consumption of alkali (NaOH) is 2-4% of the total absolute dry pulp, the flow of oxygen - 20-40 kg/t (absolute dry pulp); the response time is 60-90 minutes

This invention straw cellulose from plants cereals obtained by cooking, washing and oxygen delignification and so on; in raw materials from cereals include one or some of the materials from rice straw, wheat straw, cotton stalk, Marc sugar cane, cane or reed toetoe.

For this invention, paper products natural color of straw pulp obtained by grinding and dressing, if you want to add some unbleached wood pulp and other pulp for paper production. Due to the fact that outlined straw cellulose is a high-quality unbleached pulp having high so the awn and resistance to fracture, data and paper products are unbleached, strength and coefficient of receiving fibers respectively increase by 30-50% and 10%, and also increases the strength of paper products, for example, breaking length, etc. Presented paper products natural color can significantly reduce the degree of environmental pollution and avoid harmful substances.

When control over the content of harmful substances in paper products natural color no dioxin and adsorbed organic halide.

Another purpose of this invention is to provide method of producing paper products natural color.

To accomplish the above objectives are technological solutions.

The method of obtaining the above-mentioned paper products natural color is as follows:

(1) to obtain the unbleached straw pulp sequentially through the cooking, extrusion of a solution, rinsing and splitting and oxygen delignification;

(2), respectively mix the above unbleached straw pulp;

(3) uniformly mix the unbleached straw pulp unbleached wood pulp or other cellulose for paper production phase (2), as applicable, of the mass fraction of cellulose for paper products;

(4) provide the substance of the pulp after refining and set out to get paper products natural color.

Step (3) of the method further includes: when mixing or before mixing add the required auxiliary reagents for other paper products except Breitner. This method is a common method of obtaining paper products existing equipment.

Get the highly rigid cellulose with hardness 16-28 and the degree of grinding of 10-24°SR after cooking raw materials from cereals in accordance with step (1).

The method of cooking the cellulose contained in this invention includes one of the sulfite-ammonia method, antrahinonovye sodium method, sulfate method or sulfite-sodium method:

when cooking cellulose sulfite-ammonia method, the flow rate of the ammonium sulfite is 9-13% of the flow rate of absolutely dry raw materials;

when cooked pulp antrahinonovye soda way the consumption of alkali (NaOH) is 9-15% of the flow rate of absolutely dry raw materials;

when cooking cellulose sulfate way the consumption of alkali (NaOH) is 8-11% of the flow rate of absolutely dry raw materials;

when cooking cellulose sulfite-sodium way costs NaOH and sodium sulfite are 11-15% and 2-6% of the weight of absolutely dry raw material.

The method of cooking the cellulose contained in this invention includes one of the sulfite-ammonia method, antrahinonovye sodium method, sulfates the way or sulfite-sodium method:

1) when cooked pulp in a spherical digester periodic action or digester continuous steps:

outlined sulfite-ammonia method includes:

(1) add the reagent solution for pulping in cereal plant material, including the consumption of ammonium sulfite is 9-13% of the flow rate of absolutely dry raw materials, module 1 bath:2-4;

(2) heating the mixture of steam to a temperature 165-173°C, duration of fever, minor Gazipasa and warming is 160-210 min;

outlined antrahinonovye soda method includes:

(1) add the reagent solution for pulping in cereal plant material, including the consumption of alkali (NaOH) is 9-15% of the flow rate of absolutely dry raw materials, module 1 bath:2-4, and consumption of anthraquinone - 0,5-0,8% of the expense of absolutely dry raw materials;

(2) heating the mixture of steam to a temperature of 160-165°C, duration of fever, minor Gazipasa and warming is 140-190 min;

outlined sulfate method includes:

(1) addition of a solution of the cooking reagent in cereal vegetable raw materials with the consumption of alkali (NaOH) 8-11% of the flow rate of absolutely dry raw materials, module 1 bath:2-4 and sulfinate 5-8%;

(2) heating the mixture of steam to a temperature 165-173°C, temperature rise, a slight gaseous and heat retention prodoljaute is only 150-200 min;

outlined sulfite-sodium method includes:

(1) addition of a solution of the cooking reagent in cereal vegetable raw materials with the consumption of alkali (NaOH) 11-15%, preferably 9-15% by weight of absolutely dry raw material, sodium sulfite 2-6% and anthraquinone 0,02-0,08%, module 1 bath:3-4;

(2) heating the mixture of steam to a temperature of 160-165°C, temperature rise, a slight gaseous and heat retention continue just 140-190 min;

2) when cooking in a vertical digester:

outlined sulfite-ammonia method:

(1) add a solution of the cooking reagent in cereal vegetable raw materials with a flow rate of ammonium sulfite 9-15% of the flow rate of absolutely dry raw materials, module 1 bath:6-10;

(2) cereal plant material with hot black liquor enters the digester through the casting machine. After filling, close the pot with a lid, pour in the cooking reagent temperature 130-145°C, simultaneously deflate the air from the boiler and increase the pressure up to 0.6-0.75 MPa, the temperature of the cooking reagent to 156-173°C. temperature Rise, heat preservation and replacement continue a total of 220 minutes After that to pump pulp pump to purge the boiler;

outlined antrahinonovye soda method:

(1) add a solution of the cooking reagent in cereal vegetable raw materials with the consumption of alkali in NaOH 9-17% of the flow rate of absolutely dry raw material, adul bath 1:6-9, consumption of anthraquinone 0,5-0,8%;

(2) cereal plant material with hot black liquor enters the digester through the casting machine. After filling, close the pot with a lid, pour in the cooking reagent temperature 130-145°C, simultaneously deflate the air from the boiler and increase the pressure up to 0.4-0.6 MPa, the temperature of the cooking liquid to 147-165°C. temperature Rise, heat preservation and replacement continue only 170-200 minutes After that to pump pulp pump to purge the boiler;

outlined sulfate method:

(1) add a solution of the cooking reagent in cereal vegetable raw materials with the consumption of alkali in NaOH 8-13% of the flow rate of absolutely dry raw materials, module 1 bath:6-10 and sulfinate 5-9%;

(2) cereal plant material with hot black liquor enters the digester through the casting machine. After filling, close the pot with a lid, pour in the cooking reagent temperature 130-145°C, simultaneously deflate the air from the boiler and increase the pressure up to 0,5-0,65 MPa, the temperature of the cooking liquid to 155-168°C. temperature Rise, heat preservation and replacement continue just 180-220 minutes After that to pump pulp pump to purge the boiler;

outlined sulfite-sodium method includes:

(1) addition of a solution of the cooking reagent in cereal vegetable raw materials with the consumption of the m alkali 9-17% by weight of absolutely dry raw material, sodium sulfite 4-8%, anthraquinone 0.04 to 0.08%, the module baths 1:6-10;

(2) cereal plant material with hot black liquor is introduced into the digester through the casting machine. After filling, close the pot with a lid, pour in the cooking reagent temperature 145°C, simultaneously deflate the air from the boiler and increase the pressure to 0.45-0.6 MPa, the temperature of the cooking liquid to 152-165°C. temperature Rise, heat preservation and replacement continue just 180-220 minutes After that to pump pulp pump to purge the boiler;

outlined oxygen delignification in this invention includes:

(1) the transfer of the formed pulp hardness permanganate number of 16-28 after cooking the pump in the reactor column oxygen delignification and Supplement it alkali and oxygen; and

(2) this highly rigid cellulose is subjected to delignification reaction in the reactor column oxygen delignification and turns into pulp hardness permanganate number 10-14.

Selected oxygen delignification is the one for her reaction used reactor-column oxygen delignification; temperature and pressure set forth the highly rigid cellulose at the entrance of this reactor columns are 90-100°C and 0.9-1.2 MPa, exit at 95-105°C and 0.2-0.4 MPa. In the process oxygen delignification the consumption of alkali in NaOH is 2-4% of the expense of absolutely dry pulp, the flow of oxygen - 20-40 kg to 1 ton of absolutely dry pulp; duration of response - 60-90 minutes

The use of a single unbleached straw pulp in the manufacture of paper products natural color, set out in items 1-3 formula.

The breaking length of the unbleached straw pulp described in this invention, is 5.0-7.5 km, tear resistance - 230-280 mn, white - 25-45% ISO, tensile fracture is 40-90 times, the degree of grinding cellulose - 32-38°SR; preferably breaking length 6.5-7.5 km, tear resistance - 250-280 mn, tensile fracture is 65-90 time, the degree of grinding cellulose - 32-36°SR, whiteness - 35-45% ISO.

The preparation described unbleached straw pulp is in the order of cooking, washing and oxygen delignification, including cooking affects the transformation of cereals of plant raw materials in pulp hardness permanganate number of 16-28 and degree of grinding cellulose 10-24°SR, and the transformation of cereals of plant raw materials in pulp hardness permanganate number 16-23 and degree of grinding cellulose 10-24°SR to prepare selected unbleached straw pulp.

Preferably the preparation is set forth unbleached straw pulp is in the order of cooking, washing and oxygen delignification. Sour is odna delignification includes: pumping pulp hardness permanganate number of 16-28 after cooking with the addition of alkali and oxygen in the reactor column oxygen delignification; in the reaction of delignification is formed pulp hardness permanganate number 10-14.

Preferably the oxygen delignification is a single-stage, her reaction is carried out in the reactor column oxygen delignification; temperature and pressure set forth the highly rigid cellulose at the entrance of this reactor columns are 95-100°C and 0.9-1.2 MPa, exit at 100-105°C and 0.2-0.6 MPa. During oxygen delignification liquor consumption in NaOH is 2-4% of the expense of absolutely dry cellulose, the flow of oxygen - 20-40 kg to 1 ton of absolutely dry pulp; duration of response - 60-90 minutes

Outlined cooking is one way sulfite-ammonia, anthraquinone-sodium, sulfate and sulfite-sodium.

When cooking method sulfite-ammonia flow rate of the ammonium sulfite is 9-13% of the flow rate of absolutely dry raw material.

When cooking method anthraquinone sodium consumption of alkali in NaOH is 9-15% of the flow rate of absolutely dry raw material.

When cooking method sulfate liquor consumption in NaOH is 8-11% of the flow rate of absolutely dry raw material.

When cooking method sulfite is sodium, the alkali consumption is 11-15% by weight of absolutely dry raw materials, the consumption of sodium sulfite is 2-6% by weight of absolutely dry raw material.

Set out the washing:

(1) to pump the highly rigid pulp to what concentrations of 8-15% in the press, squeeze black liquor from the pulp and to obtain products with a concentration of 18-25%; selected press is a transitional press, single-screw, twin-screw or dvuhventsovye;

(2) for washing the pulp after the juice, which is held in the vacuum scrubber, scrubber, pressure, or horizontal belt scrubber, used black liquor with a concentration of 3-6 .2°Ve' and pH 8-8 .3 at a temperature of 70-80°C and water temperature of 70-80°C, or both together.

With the purpose of clear explanation of this invention and its technical options adopted the terms in this invention give the following definitions, which have the advantage when there is a mismatch in any other documents.

Unbleached straw pulp described in this invention, refers to straw pulp, which is made from annual plants, including, but not limited to, wheat and rice straw, cotton stalks, the juice of sugar cane, toetoe reed, cane, or combinations thereof, and not subjected to any bleaching or straw pulp, which is made from cereal plants and subjected to oxygen delignification without any bleaching.

Paper products natural colors in this invention are produced using traditional methods of straw pulp is C plants cereals as raw material without processes otbelivanie or oxygen delignification without other otbelivanie.

In the manufacture of unbleached straw pulp specified in this invention, firstly, the raw material of cereal crops using existing technology, i.e. accepted normal "dry" and "wet" method to hide the leaves, ears of corn, grains, fibre, wheat, etc. so you can reduce the pressure in the following technologies and improve the quality of straw pulp. When the workpiece by the method of "dry" and "wet" you can use existing equipment such as straw, noise, dust collector, santalka with flushing method is "wet", the inclined roller dehydrator, etc. Raw materials from cereals remove water after harvesting can be used as pure materials, raw materials from cereals remove water - absolute dry culture total length of straw 15-30 mm. technology Adopted procurement of raw materials known techniques of this industry.

In this invention can be used hammer crusher for procurement of raw materials by the method of "dry", including the following.

(1) Cutting and twisting raw materials from cereals using a hammer mill.

Hammer crusher in this activity includes the supply of raw materials, part of the crushing and twisting, part of the separation and ejection. Raw materials with a round cross-section of cereals under the force of the compression tapered, resulting in time is the bookmark sheet, barb, grain, core, etc. with straw, and released from the output of the hammer mill. The length of the released materials from cereals is 20-50 mm

Available hammer crusher the present invention used for the preparation of raw materials. His speed is 500-800 rpm, the speed of entry of raw materials from cereals in a hammer mill is 0.5-1.3 m/s Low speed or fast boot speed will result in the inability to complete twist of raw materials, the impact of the penetration of the reagent solution to boiling and then the influence of pulp quality.

On the outer surface of the raw material of cereals have a layer of wax inside the straw - layer core, when applying the conventional method for preparing a layer of wax can be easily removed under the influence of soaking solution reagents for cooking, but the core layer is difficult to remove because of the air inside the straw that leads to the difficulty of penetration of the reagent solution for cooking. Cutting and twisting raw materials from cereals using hammer crusher promotes complete digestion of a reagent solution for cooking and after cooking to get high quality pulp.

(2) vacuum cleaning of the raw material after cutting and crushing.

Refining of the raw material after cutting and grinding dust is adopted to remove most of the impurities such as dust, pesos is, leaf and spike grass, which can lead to reduced consumption of chemicals in the cooking process and reduce cooking time.

The dust collector in the present invention can be applied for the preparation of raw materials from cereals, includes roller dust collector (optimization), dvuhkonechnaya the dust collector or cyclone. Air flow cyclone for dust removal is 30000-38000 m3/h, air pressure is 210 mm vods you can remove the majority of dust in raw materials from cereals for the convenience of subsequent cooking.

(3) Sifting raw materials after extraction.

In raw materials from cereals after extraction often contain large leaves of grass, debris and other impurities in the process of cooking or formed undissolved items in connection with the difficult penetration of some impurities solution of reagents for cooking, or caused by the increased viscosity of the black liquor after the reaction of other impurities with marasim the reagent solution and the influence of circulation Varadero of a reagent solution. All these factors will lead to uneven cooking and difficulties of the operation, the influence of the number of extracted black liquor and purification of cellulose. And sifting materials can avoid these issues, therefore, the operation of prosea very important for the preparation of raw materials from cereals by the method of "dry".

The cylindrical sieve in Yes the Mr. the invention adopted for the preparation of raw materials from cereals by the method of "dry", his speed is 18-29 rpm, the angle of inclination is 6-12°. The cylindrical sieve has a two-layer construction, the side length of the square mesh sieves the inner layer is 30-40 mm, the diameter of the sieve mesh of the outer layer is 4-6 mm In the process of prosea cylindrical sieve can sift through large leaves of grass, debris, etc., providing the degree of purification of cellulose.

The effectiveness of removing impurities of raw materials from cereals by the method of "dry"described in this invention, more than 90%, while the conventional method is 70%. The method of "dry"described in this invention can reduce the amount of dust in cellulose, can increase the odds of obtaining cellulose to 3-6% in comparison with the conventional method, to reduce production costs by 2-5%.

According to this invention can soak raw soak-off solution before cooking, so that the module baths reached up to 1:2-4. At atmospheric pressure and at a temperature of 85°C is mixed for 10 min and more, better mixed at a temperature of 85-95°C. for 10-40 minutes It provides full contact soak-off solution from the raw material of wheat Saul for uniform and complete soaking of raw materials. As a soak-off solution, you can apply the alkaline solution with a certain concentration average (NaOH) 4% absolute dry is on raw materials; you can also apply a mixture of the above alkaline solution with a black solution with a concentration of 11-14°Ve' (at 20°C). Soaking raw materials you provide coolant temperature and the rest of black alkali solution, to reduce energy needs and resources and to promote the production of black liquor headed outside cells, hemicelluloses and lignins allocated under heating, to prepare for subsequent cooking. The above soaking raw materials refers to the pre-treatment process, the purpose of soaking is to contribute to the further delignification in cooking.

Preparation of cellulose from raw materials cereals is the process of removing lignin from the raw materials, as far as possible, leaving the cellulose and hemicellulose to produce paper. Due to the fact that lignin, cellulose, hemicellulose and other compositions of raw materials there are some chemical changes, degradation and damage under the influence of high temperature in the cooking process, it is necessary to study the law of changes of raw materials in the cooking process, to develop the optimum cooking conditions. The method of preparation of cellulose in the present invention can reduce manufacturing cost and to save energy consumption and to increase the yield of pulp through systematic research is of ashada and concentration of the cooking solution, cooking time and aging temperature cooking, conducting cooking, as far as possible, reducing damage to the cellulose and hemicellulose.

According to the method of the present invention is obtained the highly rigid pulp after cooking, its hardness is equal permanganate number of 16-28 (i.e. the number of Kappa 24-50), the degree of grinding of 10-24°SR; hardness selected the highly rigid cellulose equal permanganate number 18-27 (i.e. the number of Kappa 29-48); preferably the hardness of the highly rigid cellulose equal permanganate number 20-25 (i.e. the number of Kappa 34-42).

The highly rigid cellulose prepared by the method of cooking in this invention, a raw material for producing unbleached pulp. With the application of modern technologies, the cooking time and long exposure, the cooking temperature is high, the consumption of a reagent solution for cooking large. And according to this invention method, the solution flow rate of reagents for cooking reduced the cooking time and extracts significantly reduced. According to this invention the method of cooking can how to reduce production costs and save energy consumption and to increase the yield of pulp through the systematic study of the flow and concentration of the cooking solution, cooking time and aging temperature cooking, conducting cooking, as far as possible, reducing damage to cellulo and hemicellulose. The release of the highly rigid cellulose according to the described method of cooking is 58-68%.

According to this invention after cooking the resulting pulp with a high hardness is diluted at a certain pressure of 0.75 MPa and sprayed into the purge boiler. Diluted solution may be above the black liquor for steeping. The concentration of the highly rigid cellulose in the blowdown boiler 8-15%, hardness (permanganate number of 16-28) equal to the number of Kappa 26-50, purge the boiler and screw press connect transfer pump, which is transported by the highly rigid cellulose from the blowdown of the boiler to the input screw press, where does the highly rigid cellulose, after extrusion of this highly rigid pulp comes out of the screw press, the concentration output of the pulp is increased to 20-28% vs. 8-15%, which is highly concentrated and highly rigid cellulose temperature of 70-80°C. during the extrusion of cellulose the most part black pulp is pushed into the chute for storage. Selected press is used for extraction of black liquor in the current technology, the predominant single-screw, twin-screw or dvuhventsovye press with variable radius and step.

When squeezing pulp to purge the press there is a big pressure, temperature increases rapidly, h is about decoupling the atrial, division, atrial fibrillation, fracture, fracture of the primary wall, when the cellulose absorbs enough energy, resulting in a large voltage and a much increased reactivity of the highly rigid cellulose. At the same time, the fibrosis occurs, surface organic matter and impurities between the fibers dissolve in wyarno-boiled black liquor and stand out from the gutter, with the purity of the cellulose, it is much more. Part evils and impurities are highlighted together with the black liquor. In this invention the preferred screw press with variable diameter, due to the variable diameter is uniform dewatering of the pulp inside and outside in slowly diminishing space. In this invention the selected single-screw press with a variable diameter after extrusion of the highly rigid cellulose degree of grinding of the cellulose does not change.

During extrusion of the cellulose can be applied dvuhventsovye press, which, as a single-screw press, can minimize the violation of fiber, meanwhile, a high degree of extraction of black liquor in the application of this dokvantovogo press can significantly reduce further water consumption when washing compared to single-screw press, after extrusion, the concentration of the highly rigid cellulose is revised 20%, maximum up to 25%.

According to this invention when washing the highly rigid cellulose must first dilute the highly rigid pulp black liquor with a concentration of 11-14 Ve' (20°C), obtained by cooking or extrusion, to a concentration of 2.5-3.5%, then sift with current technology, such as vibrating screen, loss of cellulose in this process is 0.2%to 0.5%. Then rinse vacuum scrubber or scrubber pressure in the existing technology. In order to apply vacuum scrubber is the occurrence of differential pressure inside and outside the cells of the pulp in the washing process, which allows to obtain a higher degree of purification in the washing process. To achieve a high degree of cleaning, the washing can be carried out 1 or 2 times or 3 times.

According to this invention after washing, the concentration of cellulose varies between 9-11%, the pulp enters the dismissed machine through the auger, the degree of grinding the treated pulp in the range 26 to 28°SR and wet weight of 1.5-1.7 g, temperature of 65-70°C. dismissed This machine is available with the installation, for example high-frequency dismissed machine, torsion machine, disc grinder, disc refiner, delantera to loosen the fibrous structure or cage cellulose. Due to the blooming can races is acivate cellulose and expose the lignin between the cellulose, which is convenient for further oxygen delignification.

The highly rigid cellulose obtained after cooking, or cellulose obtained after dissolution or leaching, subject to oxygen delignification: whitening for 60-90 min at a flow rate of alkali (NaOH) 2-4% of absolutely dry pulp and the consumption of oxygen 20-40 kg/t pulp. At this time, the hardness of the pulp To (permanganate number) is reduced to 11-13 equal to the number of Kappa 12,5-17, the degree of grinding cellulose 32-36°SR. In this invention preferably oxygen delignification is a single stage, using a single reactor column, the temperature of the highly rigid cellulose to the inlet of the reactor 90-100°C, a pressure of 0.9-1.2 MPa and at the temperature of 95-105°C. and a pressure of 0.2-0.4 MPa. Apply single-stage oxygen delignification to ensure the strength of cellulose, relative to the multi-stage oxygen delignification, single-stage oxygen delignification has the smallest value for the degradation of cellulose. Among the process parameters selected in this invention single-stage oxygen delignification characterized by low temperature and a relatively long time to spent mild reaction delignification and most avoided degradation of cellulose. In this invention the concentration of selected highly rigid pulp prior to oxygen is Noah delignification is within 8-18%. Oxygen delignification is carried out at an average concentration advantages: small investment, due to mixing with the average concentrations and technology pump pumping the treatment of pulp is much easier than processing at high concentration; less corrosion of the equipment at low concentrations and there is no danger of combustion in oxygen.

Obtained according to the above operations unbleached pulp has a breaking length of 5.0-7.5 km, tear resistance 230-280 mn, whiteness of 25-45% ISO, tensile fracture during repeated bending 40-90 times, the degree of grinding cellulose 32-38°SR.

The advantage of this invention

(1) Unbleached pulp can avoid causing harm to the person from chemicals used in the bleaching process, resulting paper products natural colors do not contain dioxin and carcinogenic substances that absorb organic halides. Therefore, it does not harm the person.

(2) Unbleached pulp can reduce the impact on breaking length, tear resistance and tensile fracture in the bleaching process, due to different manufacturing techniques derived straw pulp has excellent characteristics, can significantly improve the quality of paper products natural color.

(3) According to this invention, when manufacturing the AI paper products natural color of straw pulp not add Breitner, in the resulting paper products are not subject to secondary contamination of that substance, and paper products retain their original characteristics and not hurting the person.

(4) due to the improved method of manufacture unbleached pulp in this invention the strength and characteristics of the unbleached pulp is much higher, so you can apply the pulp together with a small amount of wood pulp and other pulp for making paper products, as well as directly apply straw pulp for high quality paper products.

Specific steps of manufacturing

Example 1

Wheat straw is processed hammer crusher, then loaded into the digester, where solutions are added to the cooking reagent with ammonium sulfite in 9% of the consumption of absolutely dry raw materials, module 1 bath:3. The mixture is heated to 110°C with a holding time of 30 minutes, and then subjected to minor gatusso for 25 minutes and heated for 60 minutes to a temperature of 168°C with a holding time of 90 minutes. The hardness of the pulp after cooking 22 is equal to the number of Kappa 35,5, the degree of grinding and 11.6°SR. The pulp is diluted black liquor to a concentration of 2.5% and sifted using existing equipment, such as vibrating screen. Loss of cellulose in that the process is 0.5%. Rinse the pulp vacuum scrubber. After washing the obtained highly rigid cellulose concentration of 10%, which is sent to the pipe cellulose average concentration is pumped into the reactor-column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and a liquor containing alkali (NaOH) flow 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent for magnesium sulphate in 1% to completely dry the pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 100°C and a pressure of 0.3 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length 5,0 km, tensile fracture with multiple bends 40 times the tear resistance of 220 mn, whiteness 40% ISO and degree of grinding cellulose 34°SR. Unbleached straw pulp is subjected to grinding, the degree of grinding of 33°SR and wet weight 2.1, to Prepare unbleached wood pulp by the degree of grinding of 20°SR and wet weight of 12,

Unbleached straw pulp mass fraction of 65% and unbleached wood pulp mass fraction of 35% are grinded, the received mixture is subjected to mixing and dressing, after that, it turns out offset paper natural color. Parameters such offset paper, natural color: the density of 69.0 g/m2the opacity of 85%breaking length - 3.9 km, whiteness - 49% ISO, tensile fracture during repeated bending in the transverse direction 19 times and tear resistance 258 mn.

Example 2

After preparation of raw materials from rice straw dry method using a hammer mill, to fill it to the spherical digester periodic action where to add the sulfite ammonium 13% cost of absolutely dry raw material, the module of the bath is 1:4. The mixture is heated to 120°C with a holding time of 40 min, subjected to minor gatusso 25 min and heated for 60 minutes to 168°C with a holding time of 90 minutes, the Hardness and the degree of grinding of the highly rigid cellulose obtained after cooking, respectively 16 (i.e., the Kappa number 23) and 23.4°SR, the concentration of the pulp, diluted black liquor, to 2.5%; the loss factor in the process of sifting the existing technique, as a vibrating screen, is 0.2%. Rinse the pulp vacuum scrubber. Afterwards, screw the highly rigid cellulose with a concentration of 10% is heated to 70°C and transported in the pipe cellulose average concentration. After thermal improvement of this pulp in the pipe it is passed through a centrifugal pump pulp medium is nd concentration in the reactor column oxygen delignification. Before entry into the reactor column pulp is mixed with an alkaline solution containing oxygen (20 kg/t of pulp) and 3.5% of absolutely dry pulp consumption of alkali (NaOH) in the pipeline, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent for magnesium sulphate in 1% to completely dry the pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 100°C and a pressure of 0.4 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 6.8 km tensile fracture with multiple kinks 50 times the tear resistance of 250 mn, whiteness 41% ISO and degree of grinding cellulose 36°SR.

Outlined unbleached straw pulp mass fraction of 70% and unbleached wood pulp mass fraction of 30% grinded separately in the double-disc refiner at a concentration of 3.0% and 4.5%, respectively. The standard quality of the prepared cellulose: straw - degree of grinding of 34°SR and wet weight of 1.8 g for wood 22°SR and 10 g, respectively. Presented wood pulp prepared using existing equipment, breaking length is 6.5 km, tear resistance - 1000 mn, whiteness of 18% ISO, p is echnosti fracture with multiple kinks - 1000 times.

Offset paper natural colors obtained by the method of manufacture milled homogeneous pulp on clinocerinae mnogoelektronnoe paper machine.

The density of the described offset paper natural color is 70,0 g/m2opacity - 84%, breaking length - 4.9 km, whiteness - 52% ISO, tensile fracture during repeated bending in the transverse direction 22 times, tear resistance - 229 mn.

Example 3

Raw materials from sugar cane bagasse harvested the conventional dry method, after removal of the core is filled in a spherical digester, where solutions are added to the cooking reagent with ammonium sulfite in 11% to absolutely dry raw materials, module 1 bath:2,5. The mixture is heated to a temperature of 130°C with a holding time of 20 minutes, subjected to minor gatusso for 20 minutes. The mixture is heated for 50 minutes to a temperature of 165°C with a holding time of 70 minutes. The hardness of the pulp after cooking 21 is equal to the number of Kappa 32, the degree of grinding - 14,2°SR. The highly rigid cellulose is processed by twin-screw press designed for the extraction of black liquor, in order to achieve concentrations of up to 25%, then diluted to a concentration of 2.5% and is subjected to washing vacuum scrubber. After this, the pulp concentration of from 10 to 13% is heated by means of the screw until the temperature is s 70°C and transported in the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (30 kg/t of pulp) and a liquor containing alkali in NaOH by weight 3% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 98°C and a pressure of 1.05 MPa with a protective reagent magnesium sulfate by weight 0,8% of absolutely dry pulp is subjected to the reaction of delignification on 85 minutes when the temperature at the top of 102°C. and a pressure of 0.4 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp rupture length 6,0 km, tensile fracture with multiple bends 70 times the tear resistance of 230 mn, whiteness 40% ISO and degree of grinding cellulose 35°SR.

Preferably unbleached straw pulp mass fraction of 85% and unbleached wood pulp mass fraction of 15% grinded separately in dvuhserijnom refiner at a concentration of 3.2% and 4.0%, respectively. The standard quality of the prepared cellulose: straw - concentration of 3.2%, the degree of grinding of 33°SR and wet weight 2.0 g, wood - 4,0%, 18°SR and 11 g of COO is responsible. Offset paper natural colors obtained by the method of manufacture milled homogeneous pulp on short-clinocerinae mnogoelektronnoe paper machine.

The density of the described offset paper natural color is 65.0 g/m2the opacity of 85%, a breaking length of 5.5 km, whiteness - 48% ISO, tensile fracture during repeated bending in the transverse direction of the - 28 times, tear resistance - 230 mn.

Example 4

Raw cane toetoe harvested hammer crusher and filled in a spherical digester, where solutions are added to the cooking reagent with ammonium sulfite in 11% to absolutely dry raw materials, module 1 bath:3. The mixture is heated to a temperature of 140°C with a holding time of 40 minutes, subjected to minor gatusso for 20 minutes and heated for 60 minutes to a temperature of 175°C with a holding time of 90 minutes. The hardness of the pulp after cooking 19 is equal to the number of Kappa 28,5, the degree of grinding is 15.6°SR. The highly rigid cellulose is processed transitional single screw press designed for the extraction of black liquor, in order to achieve concentrations of up to 26%, then diluted to a concentration of from 2.5 to 3.0% of the black liquor, screened by vibrating screen (loss of cellulose and 0.2%) and cleaned from impurities sorting (loss of 0.1%). Purified cellulose input concentration of 2.0% under argueta flushing horizontal belt scrubber at a temperature of 70°C, whilst the output concentration does not reach up to 9%. Thereafter, the cellulose is dissolved dismissed on the machine, in this process the degree of grinding is transformed from 24°SR 27°SR. Then adjust the concentration of the cellulose to 10%, heat it to 70°C and transported in the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (30 kg/t of pulp) and a liquor containing alkali in NaOH consumption 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 102°C. and a pressure of 1.2 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to delignification reaction for 90 minutes at a temperature on the top of 105°C and a pressure of 0.5 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 7.5 km, tensile fracture with multiple kinks 80 times the tear resistance of 280 mn, whiteness 37% ISO and degree of grinding cellulose 33°SR.

Outlined unbleached straw pulp mass fraction of 50% and not Talena wood pulp mass fraction 50% first grinded separately in the cylindrical refiner at a concentration of 3.8%, the pressure of 0.20 MPa and the current A, then double-disc refiner until conditions are that the concentration of 3.4%, the degree of grinding of 35°SR and wet weight 2.2 g for straw pulp and 4.5%, 19°SR and 12 g, respectively, for wood. Presented wood pulp prepared using existing technology.

Wrapping paper natural colors for food products obtained by the method of manufacture milled prepared cellulose on odnogrupnitsu odnotrahniki machine for making sanitary paper with one of woolen cloth. The density of wrapping paper natural colors for food is 60,0 g/m2thick 79,0 μm, the smoothness on the front and the back - 47S and 39S, whiteness - 20% ISO, the opacity is 97.6%, breaking length - 6.8 km tensile fracture during repeated bending in the transverse direction is 150 times the tear resistance in the transverse direction is 600 mn, humidity - 5,2%.

Example 5

Reed toetoe and cane on the mass ratio of 1:4 are handled hammer crusher, then use the hot black liquor temperature of 135°C digester via the filling hole, and the module of the bath is achieved up to 1:7. Close the lid of the boiler during filling, add in boiler solution of the cooking reagent temperature of 145°C with a flow rate of the school of the eyes in NaOH in 13% to absolutely dry raw materials, anthraquinone - 0,5%. To take the black liquor and the air and increase the pressure up to 0.6 MPa. Then turn on the recirculation pump of the boiler and the tubular heater to raise the temperature of the solution of the cooking reagent to 155°C. the temperature Increase and the exposure continues with a total of 160 minutes. Hot black liquor is replaced diluted and transported in a tank of hot black liquor. Pulp after cooking hardness 20, equal to the number of Kappa 30, and the degree of grinding of 15°SR is adjusted to a concentration of 18% and is transported in a disk refiner to blossom, then the trumpet pulp average concentration after washing the conventional method and subsequent heating to a temperature of 70°C by means of the screw. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (35 kg/t of pulp) and an alkaline solution containing alkali in NaOH by weight 2,5% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 100°C and a pressure of 1.2 MPa with a protective reagent magnesium sulfate by weight 1% of absolutely dry pulp is subjected to delignification reaction at 80 minutes at a temperature on the top of 105°C and a pressure of 0.4 MPa in re store column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length 7,0 km, tensile fracture with multiple kinks 60 times the tear resistance of 240 mn, whiteness 37% ISO and degree of grinding cellulose 37°SR.

Outlined unbleached straw pulp mass fraction of 60% and unbleached wood pulp mass fraction of 40% above grinded separately in the cylindrical refiner at a concentration of 3.8%, the pressure of 0.20 MPa and the current 65 A, then in the double-disc refiner at a concentration of 3.3%, a pressure of 0.15 MPa and the current 45 And until the conditions are that the degree of grinding cellulose 48°SR and wet weight of 2.8, Stated wood pulp prepared using existing equipment, breaking length is 7 km, tear resistance - 100 mn, whiteness - 20% ISO, strength fracture with multiple bends - over 1000 times. The degree of grinding of the unbleached straw pulp is 36°SR and wet weight of 2.3 g, wood - 20°SR and 12 g, respectively.

Wrapping paper natural colors for food products obtained by the method of manufacture milled homogeneous pulp.

The density of wrapping paper natural colors for food is 45 g/m2thick 79,0 μm, the depth is bone on the front and reverse side 45S and 36S, whiteness - 45% ISO, the opacity is 97.6%, breaking length - 5.8 km, tensile fracture during repeated bending in the transverse direction is 170 times the tear resistance in the transverse direction - 550 mn, humidity - 5,3%.

Example 6

Cane after processing hammer crusher is injected into the spherical digester, where solutions are added to the cooking reagent with the consumption of alkali (NaOH) in 9% and anthraquinone 0.8% to absolutely dry raw materials, module 1 bath:4. The mixture is heated to a temperature of 110° C, holding for 40 minutes, subjected to minor gatusso for 30 minutes and heated for 50 minutes to a temperature of 173°C with a holding time of 60 minutes. The hardness of the pulp after cooking is 20 equal to the number of Kappa 30,7, the degree of grinding is 12.5°SR. The highly rigid cellulose is processed transitional single screw press designed for the extraction of black liquor, in order to achieve concentrations of up to 20%, and then subjected to conventional washing method, such as a scrubber, working under pressure. Thereafter, the cellulose is dissolved dismissed on the machine, heated to 70°C and transported in the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulosebased in the pipeline to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution, containing alkali NaOH by weight 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to delignification reaction at 70 minutes at a temperature on the top of 100°C and a pressure of 0.3 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 5.8 km, tensile fracture with multiple kinks 55 times the tear resistance of 260 mn, whiteness 40% ISO and degree of grinding cellulose 38°SR.

Outlined unbleached straw pulp mass fraction of 55% and unbleached wood pulp mass fraction 45% grinded separately in the double-disc refiner at a concentration of 3.5% and 4.5%, respectively. The standard quality of the prepared cellulose: straw - degree of grinding of 35°SR and wet weight 2.0 g, wood - 20°SR and 12 g, respectively. Presented wood pulp is coniferous sulphate pulp, prepared with the use of existing equipment, breaking length is 5.0 km, tear resistance - 1100 mn, whiteness of 18% ISO, tensile fracture with multiple bends - over 1000 times, the degree razmo needs what and 39°SR.

Fabricate milled cellulose to obtain a wrapping paper natural colors for food, density of 51.5 g/m2thick 75,0 μm, the smoothness on the front and the back - 48S and 36S, whiteness - 40% ISO, opacity - 96.8 per cent, breaking length is 3.2 km, tensile fracture during repeated bending in the transverse direction is 140 times the tear resistance in the transverse direction - 380 mn, humidity and 5.8%.

Example 7

Raw materials from cotton stalks harvested hammer crusher and filled in a spherical digester, where solutions are added to the cooking reagent with the consumption of alkali in NaOH 8% to absolutely dry raw materials, sulfinate 8% and module baths 1:2. The mixture is heated to a temperature of 110°C with a holding time of 40 minutes, subjected to minor gatusso for 25 minutes and heated for 45 minutes to a temperature of 166°C with a holding time of 75 minutes. The hardness of the pulp after cooking 22 is equal to the number of Kappa 35, the degree of grinding and 11.6°SR. This highly rigid cellulose is dissolved in a high-frequency dismissed machine and processed duhallow press, designed for the extraction of black liquor, in order to achieve concentrations of up to 32%. The pulp is diluted diluted black liquor to a concentration of 2.5%, is subjected to conventional washing method after purification from impurities. After that, the concentration in the initial pulp reaches up to 15%. In the next step, the pulp is heated to 70°C by means of the screw and is transported in the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution containing alkali in NaOH by weight 3% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to delignification reaction for 90 minutes at a temperature on the top of 100°C and a pressure of 0.4 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached stem cellulose breaking length of 4.3 km, tensile fracture with multiple bends 70 times the tear resistance of 275 mn, whiteness 42% ISO and degree of grinding cellulose 34°SR.

Outlined unbleached stem pulp mass fraction 80% and unbleached wood pulp mass fraction of 20% grinded separately in the double-disc refiner at a concentration of 3.5% and 4.5%, respectively. Standard quality is VA prepared cellulose: for stem - the degree of grinding of 55°SR and wet weight 2.0 g, wood - 48°SR and 2.6 g, respectively. Presented wood pulp is coniferous sulphate pulp, prepared with the use of existing equipment, breaking length is 5.0 km, tear resistance - 1100 mn, whiteness of 18% ISO, tensile fracture with multiple bends - over 1000 times, the degree of grinding 39°SR.

Fabricate milled cellulose to obtain photocopy paper natural color, density - 60,0-80,0 g/m2average breaking length in the longitudinal and transverse directions is 4.5 km stiffness in longitudinal bending - 112 mn, lateral bending - 72 mn, whiteness of 44.7% ISO.

Example 8

Rice and wheat straw on the mass ratio of 1:3 handled hammer crusher dry method, then digester, where solutions are added to the cooking reagent with the consumption of alkali in NaOH in 11% to absolutely dry raw materials, solidnest 5% and module baths, 1:4. The mixture is heated to a temperature of 110°C with a holding time of 20 minutes, subjected to minor gatusso for 30 minutes and heated for 40 minutes to a temperature of 168°C with a holding time of 90 minutes. The hardness of the pulp after cooking 19 is equal to the number of Kappa 29, the degree of grinding - 14,3°SR. The highly rigid cellulose is processed in the conventional transitional single screw press designed the La extraction of black liquor. Output the pulp is diluted to a concentration of 3.0% diluted black mortar and sieved by vibrating screen (loss of cellulose and 0.2%) and cleaned from impurities sorting (loss of 0.1%). Purified cellulose is subjected to leaching horizontal belt scrubber at a concentration of 3.0% and a temperature of 70°C. After that, the output concentration reaches up to 9%. In the next step, the cellulose is dissolved in a high-frequency dismissed machine, fluidities in pipe cellulose average concentration method for removal of air and pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution containing alkali in NaOH by weight 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 100°C and a pressure of 0.3 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 7.2 km, tensile fracture with multiple bends 45 times, the fight is receiving gap 250 mn, degree of whiteness 42% ISO and degree of grinding cellulose 33°SR.

Outlined unbleached straw pulp mass fraction of 50% and unbleached wood pulp mass fraction 50% first grinded separately in the cylindrical refiner at a concentration of 3.8%, the pressure of 0.20 MPa and the current 62 A, then in the double-disc refiner at a concentration of 3.4%, the pressure of 0.20 MPa and the electric current of 60 A. the Standard quality of the prepared cellulose - degree of grinding of 48°SR and wet weight of 3.2, using existing technology podgotovlyena outlined unbleached wood pulp breaking length 6.5 km, tear resistance 1000 mn, whiteness 20% ISO, tensile fracture with multiple bends over 1000 times and the degree of grinding of 38°SR. This cellulose includes unbleached coniferous sulphate pulp unbleached coniferous sulphite pulp, etc.

Fabricate milled cellulose to obtain photocopy paper natural color, density - 65.0 g/m2average breaking length in the longitudinal and transverse directions - 7.5 km, stiffness in longitudinal bending - 82 mn, lateral bending - 55 mn, whiteness of 41.8% ISO.

Example 9

Rice straw after treatment dry method hammer crusher is poured into the spherical digester, where solutions are added to the cooking reagent with the consumption of alkali is NaOH 15% and anthraquinone 0.6% to absolutely dry raw materials, module 1 bath:3. The mixture is heated to a temperature of 120°C with a holding time of 20 minutes, subjected to minor gatusso for 20-30 minutes and heated for 40 minutes to a temperature of 168°C with a holding time of 90 minutes. The hardness of the pulp after cooking is 18 equal to the number of Kappa 27, the degree of grinding - 17°SR. The highly rigid cellulose is processed in the conventional transitional single screw press designed for the extraction of black liquor. Output the pulp is diluted to a concentration of 2.5% diluted black mortar and sieved by vibrating screen (loss of cellulose and 0.2%) and cleaned from impurities sorting (loss of 0.1%). Purified cellulose is subjected to leaching horizontal belt scrubber at a concentration of 3.0% and a temperature of 68-70°C. After that, the output concentration reaches up to 9%. In the next step, the cellulose is dissolved in a high-frequency dismissed machine, heated to 70°C by means of the screw after concentration and pumped into the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution containing alkali in NaOH by weight 4% absolutely dry CE is lulzy, then heated by the steam. After complete mixing the pulp inlet temperature of 102°C. and a pressure of 1.12 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to delignification reaction at 70 minutes at a temperature on the top of 104°C. and a pressure of 0.5 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 4.4 km, tensile fracture with multiple bends 65 times the tear resistance 245 mn, whiteness 37% ISO and degree of grinding cellulose 34°SR.

Outlined unbleached stem pulp mass fraction of 70% and unbleached wood pulp mass fraction of 30% grinded separately in the double-disc refiner at a concentration of 3.2% and 4.5%, respectively. The standard quality of the prepared cellulose: to stem the degree of grinding of 55°SR and wet weight 2.0 g, wood - 48°SR and 2.0 g, respectively. Set out of wood cellulose sulfate is broad-leaved wood pulp prepared using existing technology.

Fabricate milled cellulose to obtain photocopy paper natural color.

Parameters photocopy paper natural colour: density 72,0 g/m2average razryvnaya in transverse and longitudinal directions, 6.2 km, torsional rigidity bending 90 mn, stiffness in lateral bending 56 mn, whiteness 35,0% ISO.

Example 10

Rice and wheat straw on the mass ratio of 1:3 handled hammer crusher dry method, then digester, where solutions are added to the cooking reagent with the consumption of alkali in NaOH in 11% to absolutely dry raw materials, sulfinate 5% and module baths, 1:4. The mixture is heated to a temperature of 110°C with a holding time of 20 minutes, subjected to minor gatusso for 30 minutes and heated for 40 minutes to a temperature of 168°C with a holding time of 90 minutes. The hardness of the pulp after cooking 19 is equal to the number of Kappa 29, the degree of grinding - 14,3°SR. The highly rigid cellulose is processed in the conventional transitional single screw press designed for the extraction of black liquor. Output the pulp is diluted to a concentration of 3.0% diluted black mortar and sieved by vibrating screen (loss of cellulose and 0.2%) and cleaned from impurities sorting (loss of 0.1%). Purified cellulose is subjected to leaching horizontal belt scrubber at a concentration of 3.0% and a temperature of 70°C. After that, the output concentration reaches up to 9%. In the next step, the cellulose is dissolved in a high-frequency dismissed machine, fluidities in pipe cellulose average concentration by the method of air removal and perekaziv the tsya centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution containing alkali in NaOH by weight 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 100°C and a pressure of 0.3 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 7.2 km, tensile fracture with multiple bends 45 times the tear resistance of 250 mn, whiteness 42% ISO and degree of grinding cellulose 33°SR.

Unbleached straw pulp is subjected to grinding, the degree of grinding of 30°SR and wet weight 2.3,

Paper box for food, natural colors obtained by the method of processing after mixing milled homogeneous pulp. Processing is applied splash tool capacity of 1.1%; water resistance agent of 3.3%, anionic solomyanska of 0.15%, while the vacuum to 0.055 MPa temperature drying 180°C, the drying time of 75 C. the Obtained paper box for food, fully complies with the standard of GB 18006.1-1999 class A.

Example 11

Rice straw p is after the dry processing method hammer crusher is poured into the spherical digester, where is added a solution of the cooking reagent with the consumption of alkali in NaOH 15% and anthraquinone 0.6% to absolutely dry raw materials, module 1 bath:3. The mixture is heated to a temperature of 120°C with a holding time of 20 minutes, and then subjected to minor gatusso for 20-30 minutes and heated for 40 minutes to a temperature of 168°C with a holding time of 90 minutes. The hardness of the pulp after cooking is 18 equal to the number of Kappa 27, the degree of grinding - 17°SR. The highly rigid cellulose is processed in the conventional transitional single screw press designed for the extraction of black liquor. Output the pulp is diluted to a concentration of 2.5% diluted black mortar and sieved by vibrating screen (loss of cellulose and 0.2%) and cleaned from impurities sorting (loss of 0.1%). Purified cellulose is subjected to leaching horizontal belt scrubber at a concentration of 3.0% and a temperature of 68-70°C. After that, the output concentration reaches up to 9%. In the next step, the cellulose is dissolved in a high-frequency dismissed machine, heated to 70°C by means of the screw after concentration and pumped into the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe D. the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution, containing alkali NaOH by weight 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 102°C. and a pressure of 1.12 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to delignification reaction at 70 minutes at a temperature on the top of 104°C. and a pressure of 0.5 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 4.4 km, tensile fracture with multiple bends 65 times the tear resistance 245 mn, whiteness 37% ISO and degree of grinding cellulose 34°SR.

Outlined unbleached straw pulp mass fraction of 70% and unbleached wood pulp mass fraction of 30% grinded separately, the degree of grinding of the unbleached straw pulp is 31°SR and wet weight of 2.2 g, wood: 20°SR and wet weight - 10,

Paper box for food, natural colors obtained by the method of processing after mixing milled homogeneous pulp. Processing is applied splash tool capacity of 1.1%; water resistance agent 3.3%, anionic solomyanska 0.15%under a vacuum of 0.05 MPa temperature drying 178°C, the drying time of 78 C. the Obtained paper box for food is fully compliant with B 18006.1-1999 class A.

Example 12

Reed toetoe after the dry processing method is filled in a spherical digester, where solutions are added to the cooking reagent with the consumption of alkali (NaOH) in 11% of absolutely dry raw materials and consumption of anthraquinone of 0.8%, module 1 bath:4. The mixture is heated to a temperature of 130°C with a holding time of 40 minutes, and then subjected to minor gatusso for 30 minutes and heated for 60 minutes to a temperature of 173°C with a holding time of 60 minutes. The hardness of the pulp after cooking is 25 equal to the number of Kappa 45, the degree of grinding - 12°SR. The highly rigid cellulose is processed modern transitional single screw press designed for the extraction of black liquor, is then obtained cellulose concentration of 20%, sieved by vibrating screen (loss of cellulose and 0.2%) and cleaned from impurities sorting (loss of 0.1%). Purified cellulose is subjected to leaching horizontal belt scrubber at a concentration of 2.0% and a temperature of 68-70°C. After that, the output concentration reaches up to 9%. After this, the pulp is heated to 70°C by means of the screw after concentration and pumped into the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose smesi what is in the pipeline to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution, containing alkali (NaOH) flow 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 102°C. and a pressure of 1.12 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 104°C. and a pressure of 0.5 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length 5.0 km, tensile fracture with multiple bends 69 times the tear resistance 255 mn, whiteness 42% ISO and degree of grinding cellulose 33°SR.

Outlined unbleached straw pulp mass fraction of 70% and unbleached wood pulp mass fraction of 30% above grinded separately, the degree of grinding of the unbleached straw pulp is 32°SR and wet weight of 2.3 g, of wood: - 20°SR and wet weight - 12,

Paper box for food, natural colors obtained by the method of processing after mixing milled homogeneous pulp. Processing is applied splash the product with a volume of 1.2%; water resistance agent 3%, anionic solomyanska 0.15%under vacuum to 0.055 MPa temperature drying 175°C, the drying time 80 C.

Received paper box for food, completely matched what was the standard of GB 18006.1-1999 class A.

Example 13

Wheat straw is processed hammer crusher, then loaded into the digester, where solutions are added to the cooking reagent with ammonium sulfite in 9% of the consumption of absolutely dry raw materials, module 1 bath:3. The mixture is heated to 110°C with a holding time of 30 minutes, and then subjected to minor gatusso for 25 minutes and heated for 60 minutes to a temperature of 168°C with a holding time of 90 minutes. The hardness of the pulp after cooking 22 is equal to the number of Kappa 35,5, the degree of grinding and 11.6°SR. The pulp is diluted black liquor to a concentration of 2.5% and sifted using existing equipment, such as vibrating screen. Loss of cellulose in this process is 0.5%. Rinse the pulp vacuum scrubber. After washing the obtained highly rigid cellulose concentration of 10%, which is sent to the pipe cellulose average concentration is pumped into the reactor-column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution containing alkali (NaOH) flow 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent for magnesium sulphate in 1% to completely dry the pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 100°C and a pressure of 0.3 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length 5,0 km, tensile fracture with multiple bends 40 times the tear resistance of 220 mn, whiteness 40% ISO and degree of grinding cellulose 34°SR. Unbleached straw pulp is subjected to grinding, the criterion obtained cellulose: the degree of grinding of 45°SR and wet weight of 2.8 g

Fabricate milled cellulose to obtain paper towels natural color on clinocerinae odnotrahniki paper machine.

The density of paper towels natural color is 23.0 g/m2the height of capillary rise of a liquid in the transverse direction - 66 mm/100, a tensile strength in the wet state in the longitudinal direction 36 N/m, the degree of white - 41.5% ISO.

Example 14

After preparation of raw materials from rice straw dry method using a hammer mill, to fill it to the spherical digester periodic action where to add the sulfite ammonium 13% cost of absolutely dry raw material, the module of the bath is 1:4. The mixture is heated to 120°C with a holding time of 40 min, then subjected to minor gatusso 25 min and heated for 60 minutes to 168°C with a holding time of 90 minutes the hardness of the pulp after cooking is 16 equal to the number of Kappa 23, the degree of grinding - 23,4°SR. The pulp is diluted black liquor to a concentration of 2.5% and sifted using existing equipment, such as vibrating screen. Loss of cellulose in this process is 0.2%. Rinse the pulp vacuum scrubber. Afterwards, screw the highly rigid cellulose with a concentration of 10% is heated to 70°C and transported in the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution containing alkali in NaOH consumption 3.5% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent for magnesium sulphate in 1% to completely dry the pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 100°C and a pressure of 0.4 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 6.8 km tensile fracture with multiple kinks 50 times the tear resistance of 250 mn, whiteness 4% ISO and degree of grinding cellulose 36°SR.

Outlined unbleached straw pulp mass fraction of 70% and unbleached wood pulp mass fraction of 30% grinded separately in the double-disc refiner at a concentration of 3.0% and 4.5%, respectively. The standard quality of the prepared cellulose: straw - degree of grinding 50°SR and wet weight 1.8 g, wood - 46°SR and 1.2 g, respectively. Breaking length unbleached broad-leaved wood pulp - 6.5 km, tear resistance - 1000 mn, whiteness of 18% ISO, tensile fracture - 1000 times and the degree of milling of cellulose - 38°SR.

Fabricate milled cellulose after complete mixing to obtain paper towels natural color. Dressing is performed on clinocerinae dvukhlineinoi paper machine. The density of paper towels natural color is 38.2 g/m2the height of capillary rise of a liquid in the transverse direction is 60 mm/100, a tensile strength in the wet state in the longitudinal direction of 30 N/m, the degree of whiteness 38% ISO.

Example 15

Raw materials from vyjimkou sugar cane harvested the conventional dry method, after removal of the core is filled in a spherical digester, where solutions are added to the cooking reagent with ammonium sulfite in 11% to absolutely dry raw material, the ratio of liquid to raw materials 1:2,5. The mixture is heated to pace the atmospheric temperature 130°C with a holding time of 20 minutes, subject minor gatusso for 20 minutes and heated for 50 minutes to a temperature of 165°C with a holding time of 70 minutes. The hardness of the pulp after cooking 21 is equal to the number of Kappa 32, the degree of grinding - 14,2°SR. The highly rigid cellulose is processed by twin-screw press designed for the extraction of black liquor, in order to increase the concentration to 25%, then diluted to a concentration of 2.5% and is subjected to washing vacuum scrubber. After this, the pulp concentration of from 10 to 13% is heated by means of the screw to a temperature of 70°C and transported in the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (30 kg/t of pulp) and an alkaline solution containing alkali in NaOH by weight 3% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 98°C and a pressure of 1.05 MPa with a protective reagent magnesium sulfate by weight 0,8% of absolutely dry pulp is subjected to the reaction of delignification on 85 minutes when the temperature at the top of 102°C. and a pressure of 0.4 MPa in the reactor column. In the next step, the pulp is injected into the pool and podvergaet the liquefaction, thus, there is unbleached straw pulp rupture length 6,0 km, tensile fracture with multiple bends 70 times the tear resistance of 230 mn, whiteness 40% ISO and degree of grinding cellulose 35°SR.

Outlined unbleached straw pulp mass fraction 80% and unbleached wood pulp mass fraction of 20% grinded separately at a concentration of 3.2% and 4.0%, respectively, rasmala are carried out sequentially in dvuhserijnom refiner and the double-disc refiner. The standard quality of the prepared cellulose: straw - degree of grinding 50°SR and wet weight 1.8 g, for deciduous wood - 41°SR and 1.5 g, respectively. Using existing technology podgotovlyena outlined unbleached wood pulp breaking length of 4.5 km, tear resistance 500 mn, whiteness 18% ISO, tensile fracture with multiple bends over 1000 times and the degree of grinding of 38°SR. This cellulose includes unbleached coniferous sulphate pulp unbleached coniferous sulphite pulp, etc.

Fabricate milled cellulose after complete mixing to obtain paper towels natural color. Dressing is performed on moosetache odnotrahniki paper machine. The parameters specified paper towels natural color: tight is here - 45,0 g/m2the height of capillary rise of a liquid in the transverse direction - 55 mm/100, a tensile strength in the wet state in the longitudinal direction 28 N/m, the degree of white - 41% ISO.

Example 16

Rice straw after treatment dry method hammer crusher is poured into the spherical digester, where solutions are added to the cooking reagent with the consumption of alkali (NaOH) in 15% and anthraquinone 0.6% to absolutely dry raw materials, module 1 bath:3. The mixture is heated to a temperature of 120°C with a holding time of 20 minutes, subjected to minor gatusso for 20-30 minutes and heated for 40 minutes to a temperature of 168°C with a holding time of 90 minutes. The hardness of the pulp after cooking is 18 equal to the number of Kappa 27, the degree of grinding - 17°SR. The highly rigid cellulose is processed in the conventional transitional single screw press designed for the extraction of black liquor. Output the pulp is diluted to a concentration of 2.5% diluted black mortar and sieved by vibrating screen (loss of cellulose and 0.2%) and cleaned from impurities sorting (loss of 0.1%). Purified cellulose is subjected to leaching horizontal belt scrubber at a concentration of 3.0% and a temperature of 68-70°C. After that, the output concentration reaches up to 9%. In the next step, the cellulose is dissolved in a high-frequency dismissed machine, heated to 70°C with OSU auger after concentration and pumped into the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution containing alkali in NaOH by weight 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 102°C. and a pressure of 1.12 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to delignification reaction at 70 minutes at a temperature on the top of 104°C. and a pressure of 0.5 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 4.4 km, tensile fracture with multiple bends 65 times the tear resistance 245 mn, whiteness 37% ISO and degree of grinding cellulose 34°SR.

Outlined unbleached stem pulp mass fraction of 95% and unbleached wood pulp mass fraction of 5% grinded separately in the double-disc refiner at a concentration of 3.2% and 4.5%, respectively. The standard quality of the prepared cellulose: to stem the degree of grinding of 55°SR and wet weight 2.0 g, wood - 48°SR and 2.0 g, respectively. slojena wood cellulose sulfate is broad-leaved wood pulp, prepared using existing technology.

Fabricate milled cellulose after complete mixing to obtain a tissue paper natural color.

The parameters specified tissue paper natural colour: density : 18.0 g/m2the height of capillary rise of a liquid in the transverse direction 60 mm/100, tensile strength - to 7.0 N·m/g, soft - 130 mn, whiteness of 50% ISO.

Example 17

Reed toetoe after the dry processing method is filled in a spherical digester, where solutions are added to the cooking reagent with the consumption of alkali (NaOH) in 11% of absolutely dry raw materials and consumption of anthraquinone of 0.8%, module 1 bath:4. The mixture is heated to a temperature of 130°C with a holding time of 40 minutes, and then subjected to minor gatusso for 30 minutes and heated for 60 minutes to a temperature of 173°C with a holding time of 60 minutes. The hardness of the pulp after cooking is 25 equal to the number of Kappa 45, the degree of grinding - 12°SR. The highly rigid cellulose is processed modern transitional single screw press designed for the extraction of black liquor, is then obtained cellulose concentration of 20%, sieved by vibrating screen (loss of cellulose and 0.2%) and cleaned from impurities sorting (loss of 0.1%). Purified cellulose is subjected to leaching horizontal band scrub the rum at a concentration of 2.0% and a temperature of 68-70°C. After that, the output concentration reaches up to 9%. After this, the pulp is heated to 70°C by means of the screw after concentration and pumped into the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution containing alkali (NaOH) flow 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 102°C. and a pressure of 1.12 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 104°C. and a pressure of 0.5 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length 5,0 km, tensile fracture with multiple bends 69 times the tear resistance 255 mn, whiteness 42% ISO and degree of grinding cellulose 33°SR.

Outlined unbleached straw pulp mass fraction of 70% and unbleached wood pulp mass fraction of 30% above grinded separately in Jindrisska refiner at a concentration of 3.8%, the pressure of 0,15-0,20 MPa and the current 65 A, then in the double-disc refiner at a concentration of 3.3%, the pressure of 0.20 MPa and the current 60 And until the conditions are that the degree of grinding cellulose 48°SR and wet weight of 2.8, using existing technology podgotovlyena outlined unbleached wood pulp breaking length of 6 km, the tear resistance of 1000 mn, whiteness 18% ISO, tensile fracture with multiple bends over 1000 times and the degree of grinding of 40°SR. This cellulose includes unbleached sulphate broadleaf pulp unbleached coniferous sulphite pulp, etc.

Fabricate milled cellulose to obtain a tissue paper natural color.

The parameters specified tissue paper, natural color: the density of 11.0 g/m2the height of capillary rise of a liquid in the transverse direction is 80 mm/100, tensile strength 10.0 N·m/g, soft - 120 mn, whiteness - 38% ISO.

Example 18

Rice straw, wheat straw and reeds on the mass ratio of 1:3:1 are processed by the dry method, hammer crusher and loaded into the digester, then use the hot black liquor temperature of 135°C digester via the filling hole, and the module of the bath is achieved up to 1:8. Close the lid of the boiler during the filling, add the boiler solution of the cooking reagent temperature of 145°C with a flow rate of alkali NaOH in 11% to absolutely dry raw materials, anthraquinone is 0.8%. To take the black liquor and the air and increase the pressure up to 0.6 MPa. Then turn on the recirculation pump of the boiler and the tubular heater to raise the temperature of the solution of the cooking reagent to 160°C. the temperature Increase and the exposure continued for a total of 180 minutes. Hot black liquor is replaced diluted and transported in a tank of hot black liquor. The hardness of the obtained pulp after cooking 19 is equal to the number of Kappa 29, the degree of grinding - 16°SR. The highly rigid cellulose is processed in the conventional transitional single screw press designed for the extraction of black liquor. Output the pulp is diluted to a concentration of 3.0% diluted black mortar and sieved by vibrating screen (loss of cellulose and 0.2%) and cleaned from impurities sorting (loss of 0.1%). Purified cellulose is subjected to leaching horizontal belt scrubber at a concentration of 3.0% and a temperature of 70°C. After that, the output concentration reaches up to 9%. In the next step, the cellulose is dissolved in a high-frequency dismissed machine, fluidities in pipe cellulose average concentration method for removal of air and pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and the school is full-time solution, containing alkali NaOH by weight 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent magnesium sulfate consumption by weight 1% of absolutely dry pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 100°C and a pressure of 0.4 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length 6.5 km, tensile fracture with multiple bends 45 times the tear resistance of 250 mn, whiteness of 42% ISO and the degree of milling of cellulose - 33°SR.

Outlined unbleached straw pulp mass fraction of 95% and unbleached wood pulp mass fraction of 5% grinded separately in the double-disc refiner at a concentration of 3.4%. The standard quality of the prepared cellulose: the degree of grinding of 48°SR and wet weight of 2.9, using existing technology podgotovlyena outlined unbleached wood pulp breaking length of 6 km, the tear resistance of 1000 mn, whiteness 20% ISO, tensile fracture with multiple bends over 1000 times and the degree of grinding of 38°SR. This cellulose includes unbleached sulphate broadleaf pulp, unbleached sulfite the Yu coniferous pulp, etc.

Fabricate milled cellulose to obtain a tissue paper natural color.

The parameters specified tissue paper natural colour: density - 13,0 g/m2the height of capillary rise of a liquid in the transverse direction is 30 mm/100, a tensile strength in the wet state in the longitudinal direction 22 N/m, soft - 140 mn, whiteness of 50% ISO.

Example 19

Wheat straw is processed hammer crusher, then loaded into the digester, where solutions are added to the cooking reagent with ammonium sulfite in 9% of the consumption of absolutely dry raw materials, module 1 bath:3. The mixture is heated to 110°C with a holding time of 30 minutes, and then subjected to minor gatusso for 25 minutes and heated for 60 minutes to a temperature of 168°C with a holding time of 90 minutes. The hardness of the pulp after cooking 22 is equal to the number of Kappa 35,5, the degree of grinding and 11.6°SR. The pulp is diluted black liquor to a concentration of 2.5% and sifted using existing equipment, such as vibrating screen. Loss of cellulose in this process is 0.5%. Rinse the pulp vacuum scrubber. After washing the obtained highly rigid cellulose concentration of 10%, which is sent to the pipe cellulose average concentration is pumped into the reactor-column oxygen delignification. CE is lulose mixed in the piping to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution, containing alkali (NaOH) flow 4% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent for magnesium sulphate in 1% to completely dry the pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 100°C and a pressure of 0.3 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length 5,0 km, tensile fracture with multiple bends 40 times the tear resistance of 220 mn, whiteness 40% ISO and degree of grinding cellulose 34°SR. Unbleached straw pulp is subjected to grinding, the criterion obtained cellulose: the degree of grinding of 45°SR and wet weight of 2.8 g

Fabricate milled cellulose to obtain household paper natural color. Dressing is performed on a long-lineynoye odnotrahniki paper machine.

The parameters specified household natural paper color: density of 14.0 g/m2the height of capillary rise of a liquid in the transverse direction is 100 mm/100, a tensile strength in the wet state in the longitudinal direction - 55 N/m, the degree of white - 45% ISO.

Example 20

After preparation of raw materials from rice solo is s dry method, using a hammer mill, to fill it to the spherical digester periodic action where to add the sulfite ammonium 13% cost of absolutely dry raw material, the module of the bath is 1:4. The mixture is heated to 120°C with a holding time of 40 min, then subjected to minor gatusso 25 min and heated for 60 minutes to 168°C with a holding time of 90 minutes the hardness of the pulp after cooking is 16 equal to the number of Kappa 23, the degree of grinding - 23,4°SR. The pulp is diluted black liquor to a concentration of 2.5% and sifted using existing equipment, such as vibrating screen. Loss of cellulose in this process is 0.2%. Rinse the pulp vacuum scrubber. Afterwards, screw the highly rigid cellulose with a concentration of 10% is heated to 70°C and transported in the pipe cellulose average concentration. This cellulose fluidities by the method of thermal improvements (removal of air in the pipe and is pumped by the centrifugal pump in the reactor column oxygen delignification. Cellulose is mixed in the pipe to the reactor column with oxygen (20 kg/t of pulp) and an alkaline solution containing alkali in NaOH consumption 3.5% of absolutely dry pulp, then heated by the steam. After complete mixing the pulp inlet temperature of 95°C and a pressure of 0.9 MPa with a protective reagent for magnesium sulphate in 1% to absolute the dry pulp is subjected to the reaction of delignification on 75 minutes when the temperature at the top of 100°C and a pressure of 0.4 MPa in the reactor column. In the next step, the pulp is injected into the pool and is subject to liquefaction, thus, there is unbleached straw pulp breaking length of 6.8 km tensile fracture with multiple kinks 50 times the tear resistance of 250 mn, whiteness - 45% ISO and the degree of milling of cellulose - 36°SR.

Outlined unbleached straw pulp mass fraction of 70% and unbleached wood pulp mass fraction of 30% grinded separately in the double-disc refiner at a concentration of 3.0% and 4.5%, respectively. The standard quality of the prepared cellulose: straw - degree of grinding 50°SR and wet weight 1.8 g, wood - 46°SR and 1.2 g, respectively. Breaking length unbleached broad-leaved wood pulp - 6.5 km, tear resistance - 1000 mn, whiteness of 18% ISO, tensile fracture - 1000 times and the degree of milling of cellulose - 38°SR.

Fabricate milled cellulose after complete mixing to obtain household paper natural color. Dressing is performed on clinocerinae dvukhlineinoi paper machine. The parameters specified household natural paper color: density 36,0 g/m2the height of capillary rise of a liquid in the transverse direction 60 mm/100, a tensile strength in the wet state in the longitudinal direction of 40 N/m, with Epen white - 45% ISO.

1. Paper product natural color of raw unbleached pulp from straw of cereals, white is 35-60% ISO, characterized in that for manufacturing use unbleached straw pulp with a tear resistance of 230-280 mn, tensile fracture during repeated bending 40-90 times and permanganate number of 16-28.

2. The product according to claim 1, in which the breaking length of the specified unbleached straw pulp is 5.0 - 7.5 km, white - 25-45% ISO, the degree of grinding cellulose - 32-38°SR, preferably breaking length specified unbleached straw pulp - 6,5-7,5 km, white - 35-45% ISO, the degree of grinding cellulose - 32-36°SR, tear resistance - 250-280 mn.

3. The product according to claim 1, which includes sanitary paper natural color, paper towel, natural color, paper for drying natural color, paper for photocopies natural color paper box for food, natural colors, wrapping paper for food products natural color and printing paper natural color.

4. Product according to any one of claims 1 to 3, which is sanitary paper natural colours containing 70 to 100% of the unbleached straw pulp and 0-30% of unbleached wood pulp or paper towel natural color provided is 70-100% of the unbleached straw pulp and 0-30% of unbleached wood pulp, or is the paper box for food, natural color, is made of 70-100% of the unbleached straw pulp and 0-30% of unbleached wood pulp, or paper photocopies of natural colours, containing 50-80% of the unbleached straw pulp and 20-50% of unbleached wood pulp, or is wrapping paper for food products containing 50-70% of the unbleached straw pulp and 30-50% of unbleached wood pulp, or is offset paper natural color that contains 65-85% of the unbleached straw pulp and 15-35% of unbleached wood pulp, or paper for drying, which contains 70-100% of the unbleached straw pulp and 0-30% of unbleached wood pulp.

5. The product according to claim 4, in which the height of capillary rise of a liquid in the transverse direction of the sanitary-hygienic paper natural color, 30-100 mm/100, preferably 40-100 mm/100, more preferably 50-80 mm/100, a tensile strength in the wet state in the longitudinal direction of the paper towels natural color is 22-55 N/m, preferably 30-45 N/m, or an average breaking length in the longitudinal and transverse directions paper for photocopies natural color is 3.2-7.5 km, preferably 4.5 to 7.5 km, more preferably 6,0-7,5 km or breaking the Lin wrapping paper for food products natural color is 3.2-7.6 km, preferably 4.5 to 7.6 km, or breaking length offset paper natural color, set forth in this invention is 2,5-5,5 km, preferably 3.5 to 5.5 km, or tensile strength in the wet state in the longitudinal direction of the paper for drying natural color, set forth in this invention is 22-55 N/m, preferably 30-45 N/m

6. The product according to claim 4, in which the rate of tensile strength tissue paper natural color is 4-12 N·m/g, preferably 8-12 N·m/g, or the height of capillary rise of a liquid in the transverse direction of the paper towels natural color 30-100 mm/100, preferably 40-100 mm/100, more preferably 50-80 mm/100; or tensile fracture during repeated bending in the transverse direction of the paper for photocopies natural color is 60-200 times, preferably 80-185 time; or opacity of paper for photocopies natural colors are 82,0-98,0%, preferably 90-98%, or tensile fracture during repeated bending in the transverse direction of wrapping paper natural colors for the food products are 90-200 times, preferably 120-200 time, or opaque offset paper natural color is 82-98%, preferably 85-98%, more preferably 92-98%, or height of capillary fluid is STI in the transverse direction of the paper for drying natural color 30-100 mm/100, preferably 40-100 mm/100, more preferably 50-80 mm/100 C.

7. The product according to claim 5 or 6, in which the softness outlined sanitary paper natural colors 120-180 mn, preferably 120-150 mn, or the softness of the presented paper towels natural color is 120-180 mn, preferably 120-150 mn, or tear resistance in the transverse direction outlined wrapping paper natural colors for food is 300-600 mn, preferably 400-600 nm or tensile fracture during repeated bending in the transverse direction outlined offset paper natural color is 10-35 times, preferably 15-35 times.

8. The product according to claim 5 or 6, in which the density of the contained paper is 10.0-18.0 g/m2preferably 11,0-13,0 g/m2or density presented paper towels natural color is 23,0-45,0 g/m2preferably 30,0-40,0 g/m2or the density of the contained paper for photocopies natural color is 60,0-80,0 g/m2preferably 70,0-80,0 g/m2more preferably 69,0-72,0 g/m2or the density set forth wrapping paper natural colors for food is 45-65 g/m2preferably 50-60 g/m2or density set out for drying paper natural color is 14,0-36,0 g/m2preferably 18-28 g/m 2or the density of the described offset paper natural color is 50-70 g/m2preferably 60,0-70,0 g/m2.

9. The product according to claim 5 or 6, in which the softness of the presented paper for drying natural color is 120-200 mn, preferably 120-180 mn.

10. Product according to any one of claims 1 to 3, in which the receiving set forth unbleached straw pulp includes cooking and washing, including obtaining the highly rigid straw pulp permanganate number 16-23 and the degree of grinding of 10-24°SR.

11. Product according to any one of claims 1 to 3, wherein the step of obtaining the unbleached straw pulp includes cooking and oxygen delignification, including pumping the highly rigid cellulose with permanganate number of 16-28 in the reactor column oxygen delignification with the addition of alkali and oxygen and getting after the reaction of cellulose with permanganate number 10-14, with selected oxygen delignification is a single-stage, her reaction is carried out in the reactor column oxygen delignification, the temperature and pressure set forth the highly rigid cellulose at the entrance of this reactor columns are 95-100°C and 0.9-1.2 MPa, exit at 100-105°C and 0.2-0.6 MPa, and during oxygen delignification liquor consumption in NaOH is 2-4% of the consumption of absolutely dry pulp, oxygen flow rate of 20-40 kg to 1 t absolutely su is th cellulose, duration of response 60-90 minutes

12. Product of claim 10 in which the method of cooking the cellulose includes one of the following methods: sulfite-ammonia method, entragian-soda method, the sulphate process or sulfite-sodium way, when cooking sulfite-ammonia method, the flow rate of the ammonium sulfite is 9-13% of the consumption of absolutely dry raw material, cooking the anthraquinone-sodium way the consumption of alkali NaOH is 9-15% of the consumption of absolutely dry raw material, cooking sulfate way the consumption of alkali NaOH is 8-11% of the consumption of absolutely dry raw material, cooking sulfite-sodium way the consumption of caustic soda is 11-15% of the weight of absolutely dry raw materials, the consumption of sodium sulfite is 2-6% by weight of absolutely dry raw material.

13. The product is indicated in paragraph 12, in which the method of cooking the cellulose includes one of the following methods: sulfite-ammonia method, entragian-soda method, the sulphate process or sulfite-sodium way, during cooking of cellulose in a spherical digester batch and continuous digester actions sulfite-ammonia method includes: adding a reagent solution for pulping in cereal plant material, including the consumption of ammonium sulfite is 9-13% of the consumption of absolutely dry raw materials, consumption of caustic soda is 0-8% of the races is an ode to absolutely dry raw material module 1 bath:2-4, heating the mixture of steam to a temperature 165-173°C with increasing temperature, a minor Gazipasa and conservation of heat within 160-210 min, entragian-soda method includes: adding a reagent solution for pulping in cereal plant material, including the consumption of alkali in NaOH is 9-15% of the consumption of absolutely dry raw materials, module 1 bath:2-4, and consumption of anthraquinone 0.5 to 0.8% of consumption of absolutely dry raw material, heating the mixture of steam to a temperature of 160-165°C, temperature rise, a slight gaseous and heat retention continue just 140-190 min outlined sulphate method includes: adding a reagent solution for pulping in cereal plant material, including the consumption of alkali in NaOH is 8-11% of the consumption of absolutely dry raw materials, module 1 bath:2-4, sulfinate 5-8%; heating the mixture of steam to a temperature 165-173°C, temperature rise, a slight gaseous and heat retention continue only 150-200 min; stated sulfite-sodium method includes: adding a reagent solution for pulping in cereal plant material, including the consumption of NaOH is 9-15% by weight of absolutely dry raw materials, the consumption of sodium sulfite is 2-6% by weight of absolutely dry raw materials, consumption of anthraquinone 0.04 to 0.08% of the consumption of absolutely dry raw materials, module 1 bath:3-4, heating the mixture of steam to a temperature 160-65°C, fever, slight gaseous and heat retention continue just 140-190 min, when cooking in a vertical digester: when sulfite-ammonia method, the cereal plant material using a hot-black alkaline solution temperature of 120-140°C is introduced into the digester via the filling hole after filling, close the boiler cap, pour it boiling reagent temperature of 130-160°C, at the same time suck the air from the boiler and increase the pressure up to 0.6-0.75 MPa, and the temperature of the cooking reagent to 156-173°C using a heating circulation pump and a tubular heater, temperature rise, heat preservation and replacement last 180-220 min followed by lead pump pulp pump blowdown boiler, set forth in the reagent solution for pulping consumption of ammonium sulfite is 9-15% of the consumption of absolutely dry raw materials, consumption of caustic soda is 0-8% of usage of absolutely dry raw materials, module 1 bath:6-10, when entragian-soda method, the cereal plant material using a hot-black alkaline solution temperature of 120-140°C is introduced into the digester via the filling hole after filling, close the boiler cap, pour it boiling reagent temperature of 130-160°C, at the same time suck the air from the boiler and increase pressure 0.4-0.6 MPa, and the temperature is round the cooking reagent to 147-165°C using a heating circulation pump and a tubular heater, the increase of temperature, heat preservation and replacement continue 180 min followed by lead pump pulp pump blowdown boiler, set forth in the reagent solution for pulping liquor consumption NaOH is 9-17% of the consumption of absolutely dry raw materials, module 1 bath:6-9, consumption of anthraquinone 0,5-0,8%, while the sulphate method, the cereal plant material using a hot-black alkaline solution temperature of 120-140°C is introduced into the digester via the filling hole after filling, close the boiler cap, pour it boiling reagent temperature of 130-160°C, at the same time suck the air from the boiler and increase the pressure up to 0,5-0,65 MPa, and the temperature of the cooking reagent to 155-168°C using a heating circulation pump and a tubular heater, temperature rise, heat preservation and replacement continue 200-250 min followed by pulp is pumped by the pump to purge the boiler, in the reagent solution for pulping liquor consumption NaOH is 8-13% of the consumption of absolutely dry raw materials, module 1 bath:6-10, sulfinate 5-9%, sulfite-sodium way cereal plant material using a hot-black alkaline solution temperature of 120-140°C is introduced into the digester via the filling hole, after filling, close the boiler cap, pour it boiling reagent temperature is Roy 130-160°C, at the same time suck the air from the boiler and increase the pressure to 0.45-0.6 MPa, and the temperature of the cooking reagent to 152-165°C using a heating circulation pump and a tubular heater., the increase of temperature, heat preservation and replacement continue 180-230 min followed by pulp is pumped by the pump to purge the boiler, set forth in the reagent solution for pulping consumption of NaOH is 9-17% by weight of absolutely dry raw materials, the consumption of sodium sulfite is 4-8% by weight of absolutely dry raw materials, consumption of anthraquinone 0.04 to 0.08% of the consumption of absolutely dry raw materials, module 1 bath:6-10.

14. The product according to claim 11 in which to prepare the specified unbleached straw pulp before cooking and oxygen delignification lead leaching, including:
(1) pumping the highly rigid cellulose concentration of 8-15% in the press, the pulp black liquor from pulp and obtaining products with a concentration of 18-25%, at the same time as the press use transitional press, single-screw, twin-screw or dvuhventsovye,
(2) for washing the pulp after the juice in a vacuum scrubber, scrubber, pressure, or horizontal belt scrubber used black liquor with a concentration of 3-6 .2° Be' and value pH 8-8 .3 at a temperature of 70-80°C, or water at a temperature of 70-80°C, or black liquor and water.

15. Product on any the mu one of claims 1 to 3 in which raw materials from cereals includes one or more of the following materials: rice straw, wheat straw, cotton stalks, sugar cane bagasse, common reed or cane around.

16. A method of manufacturing paper products natural colors according to any one of claims 1 to 15, including:
(1) obtaining the specified unbleached straw pulp sequentially by cooking, washing, breaking and oxygen delignification raw materials from cereals,
(2) further mixing the above unbleached straw pulp, wood pulp,
(3) uniform mixing of the unbleached straw pulp unbleached wood pulp in step (2) according to the required mass fraction of cellulose for paper products,
(4) the production of pulp produced these paper products natural color, at this stage of cooking is to obtain the highly rigid straw pulp permanganate number of 16-28 and the degree of grinding of 10-24°SR after cooking raw materials from cereals, preferably receiving the said highly rigid straw pulp permanganate number 16-23 and the degree of grinding of 10-24°SR, stage oxygen delignification includes pumping the highly rigid cellulose with permanganate number of 16-28 in the reactor column oxygen delignification, the addition of alkali and oxygen and after this reaction, the cellulose pulping with permanganate chislom-14.

17. The method according to item 16, wherein the oxygen delignification is mainly one-step, is carried out in the reactor column oxygen delignification, the temperature and pressure specified the highly rigid pulp at the inlet and at the outlet of this reactor columns, respectively 95-100°C, 0.9 To 1.2 MPa and 100-105°C, 0.2-0.6 MPa, during oxygen delignification liquor consumption NaOH is 2-4% of the consumption of absolute dry pulp, the flow of oxygen - 20-40 kg/t absolute dry pulp, the reaction time is 60-90 minutes

18. The method according to item 16, further comprising the step of splitting, which consists in the treatment of pulp after washing frequency dismissed machine, torsion machine, disk mill, disk refiner or delantera for loosening of the fibrous structure.

19. Use one unbleached straw pulp for the manufacture of paper products natural colors according to any one of claims 1 to 3, characterized in that use unbleached straw pulp with a tear resistance of 230-280 mn, tensile fracture during repeated bending 40-90 times and permanganate number of 16-28.

20. The application of claim 19, in which the breaking length of the specified unbleached straw pulp is 5.0-7.5 km, white - 25-45% ISO, the degree of grinding cellulose - 32-38°SR, mainly breaking length C is Anna stated unbleached straw pulp 6,5-7,5 km, white - 35-45% ISO, the degree of grinding cellulose - 32-36°SR, white - 35-45% ISO, tear resistance - 250-280 mn, tensile fracture with multiple kinks - 65-90 time.

21. The application of claim 19 in which the step of obtaining the specified unbleached straw pulp include cooking, washing and oxygen delignification, preferably including obtaining the highly rigid straw pulp permanganate number 16-23 and the degree of grinding of 10-24°SR after cooking raw materials from cereals.

22. The application of claim 19, wherein said steps of receiving unbleached straw pulp include cooking, washing and oxygen delignification specified oxygen delignification is pumping the highly rigid cellulose with permanganate number of 16-28 after cooking with the addition of alkali and oxygen in the reactor column oxygen delignification, in the reaction of delignification is formed pulp hardness permanganate number 10-14, preferably an oxygen delignification are single-stage, the reaction is carried out in the reactor column oxygen delignification, the temperature and pressure specified the highly rigid pulp at the inlet and at the outlet of this reactor columns, respectively 95-100°C, 0.9 To 1.2 MPa and 100-105°C, 0.2-0.6 MPa, during oxygen delignification liquor consumption NaOH is 2-4% from rashodovatsy dry pulp, the flow of oxygen - 20-40 kg/t absolute dry pulp, the response time is 60-90 minutes

23. The application of item 21 or 22, in which way pulping involves one of the sulfite-ammonia method, antrahinonove sodium method, sulfate method or sulfite-sodium way, when cooking sulfite-ammonia method, the flow rate of the ammonium sulfite is 9-13% of the consumption of absolutely dry raw material, cooking the anthraquinone-sodium way the consumption of alkali NaOH is 9-15% of the consumption of absolutely dry raw material, cooking sulfate way the consumption of alkali NaOH is 8-11% of the consumption of absolutely dry raw material, cooking sulfite-sodium way the consumption of caustic soda is 11-15% by weight absolutely dry raw material consumption of sodium sulfite is 2-6% by weight of absolutely dry raw material.

24. The application of item 21 or 22, in which rinsing is:
(1) pumping the highly rigid cellulose concentration of 8-15% in the press, the juice of black alkali cellulose and obtaining products with a concentration of 18-25%selected set forth by the press serves as a transitional press, single-screw, twin-screw or dvuhventsovye,
(2) for washing the pulp after the juice, which lead to the vacuum scrubber, the scrubber pressure or horizontal belt scrubber, apply black liquor with a concentration of 3-6 .2° Be' and C is achenium pH 8-8 .3 at a temperature of 70-80°C, or water at a temperature of 70-80°C, or black liquor and water.



 

Same patents:

FIELD: paper industry.

SUBSTANCE: one side of paper-based substrate is coated with the first dyeing composition to provide the degree of whiteness L* with the value of L1. The second dyeing composition is applied to the opposite side of the substrate having the degree of whiteness L* with the value of L2. A colored product is obtained, characterised by the degree of whiteness L* with a value of L3 for the first coated side. The second coated side of the product has a degree of whiteness L* with a value of L4. Thus L1 is not more than 8 points higher than L3, and L2 is at least 30 points higher than L4. The degree of whiteness L* is determined using the colour characteristics CIE L* a* b*, a clarifier D 65, and at the observation angle of 10°C. In this method, the penetration of dyeing substances of the dyeing composition is adjusted so that the minimal impact is achieved on the degree of whiteness of the coating of white or light colour on the opposite side of coloured paper.

EFFECT: obtaining high-quality colored paper, which has a high contrast ratio to ensure high-level package, simplification of method, reducing of cash expenses, time expenditures and labor.

15 cl, 1 dwg, 2 tbl

FIELD: textile, paper.

SUBSTANCE: article is made with at least partial use of short-fibre cellulose. To form at least two fractions of fibrous material comprising fibres having various composition, short-fibre mass is sifted through a sieve. Besides, fine fibres are separated from cellulose, which pass through the sieve with holes of diameter of 0.2-1.5 mm and which are caught and included into composition of various layers of the fibrous article.

EFFECT: improved tensile strength limit and rigidity during tensioning of long-fibre mass, and also dehydration and porosity.

19 cl, 10 dwg, 1 ex

FIELD: textile, paper.

SUBSTANCE: cellulose product comprises thermoplastic microspheres and a charged aromatic acrylamide polymer. The method to produce a cellulose product includes provision of an aqueous solution of suspension that contains cellulose fibres. Addition of thermoplastic microspheres and the charged aromatic acrylamide polymer into the suspension, and dehydration of the produced suspension. Thus made cellulose product may be used as a cardboard for liquid packing.

EFFECT: reduced porosity of a cellulose product as its volume increases and improved resistance of a wick edge to penetration of aqueous liquids for cellulose products.

25 cl, 3 tbl, 4 ex

FIELD: textile, paper.

SUBSTANCE: structure is intended for secured and/or valuable documents. It contains at least one substrate of fibre material, optionally, at least one surface layer applied onto one surface of substrate. At the same time the specified surface layer comprises coating or surface pigments and at least one binder. It also contains multiple various elements of substrate and/or optionally of a surface layer, distributed in a random manner inside the substrate and/or optionally the surface layer, and at least one portion of authenticating and/or identifying information is related to at least one spatial and/or physical criterion of at least part of specified various elements. Also a document, a packing facility and a sheet material are proposed with application of the above-specified structure. A method to make such a structure, its versions and a method to authenticate and/or identify the structure are also proposed.

EFFECT: improved extent of protection.

31 cl, 12 dwg

FIELD: textile, paper.

SUBSTANCE: method represents reduction of transition metals content in a milled mass to a level unfavorable for sporulation. Preferably, bacterial cells present in the milling system of cardboard or paper machine in fact are not destroyed in the process of technological operations used to reduce the content of transition metals. The method also refers to obtaining packing board or packing paper characterised with a low content of bacterial spores, when to obtain packing board or packing paper a milled mass is used in which the content of transition metals is reduced to a level unfavorable for sporulation.

EFFECT: reduction of bacterial spores in the milling system of a cardboard machine.

20 cl, 9 dwg, 7 ex

FIELD: paper industry.

SUBSTANCE: cardboard contains at least two layers: the first layer made of raw materials having high density and high module of elasticity; and the second layer to provide voluminousness for cardboard, in which the second layer contains chemical-thermomechanical pulp (CTMP) of broadleaf wood, cellulose and/or CTMP of coniferous wood at the specified ratio of components. At the same time coherence by Scott is achieved, making at least 80 J/m2; index of bending resistance making at least 5 Nm6/kg3 and strength in direction z, making at least 200 kPa. Invention also relates to products made of cardboard.

EFFECT: expansion of multilayer cardboard range and improvement of its quality.

15 cl, 8 tbl

FIELD: process engineering.

SUBSTANCE: this invention relates to method of processing initial sheet material containing natural organic fibers or reclaimed fibers. In compliance with proposed method, one side of said material is first processed by liquid containing said antimicrobial agent and binder and initial stock is dried. Second step comprises applying wax-containing layer on processed side of initial material for it to be impregnated at 100-145°C.

EFFECT: higher resistance to ozone and UV radiation.

18 cl, 2 dwg

FIELD: textiles, paper.

SUBSTANCE: method refers to pulp-and-paper industry, specifically to method for making bag paper, as well as to bag paper with improved service properties. Method for making bag paper involves pulp beating stage at fibre concentration 28-40% and thereafter at fibre concentration 3-6%. It is followed by two-staged addition of reinforcing and at once flocculating agent to pulp. Then paper web is casted and dried. Further beating stage at fibre concentration 3-6% requires power consumption within 20-60 kWt/h per paper ton. The second stage of addition is followed with the third stage of addition implying flocculating agent preceding headbox. Herewith at the first stage, reinforcing and at once flocculating agent is cationic starch of fractional substitutionality 0.040-0.150 in amount 0.1-1.2% of absolutely dry fibre weight, or polyacrylamide in amount 0.1-0.5% of absolutely dry fibre weight. Specified agent is added to pulp, 5-120 minutes prior to paper web casting. At the second stage reinforcing and at once flocculating agent is added in amount 0.005-0.400% of absolutely dry fibre weight. Specified agent is added to pulp, 20-120 seconds prior to paper web casting. At the third stage flocculating agent is anionic montmorillonite microparticle dispersion. Specified agent is added to pulp in amount 0.05-0.50 % of absolutely dry fibre weight. Bag paper is made under the offered method.

EFFECT: lower consumption of reinforcing and flocculating polymers, improved pulp water yield on papermaking machine grid and enhanced consumer paper properties including paper air permeability.

4 cl, 1 tbl, 3 ex

FIELD: textile industry, paper industry.

SUBSTANCE: method (version) relates to production of paper base meant for vulcanising and parchmentising and can be used in paper-pulp industry. The method includes the following stages. Energy radiation of cellulose fiber in dry condition. Grinding and refining of irradiate fiber in aqueous media till homogeneous fiber solution is prepared. Formation of web from prepared fibrous suspension, which is dewatered and dried to prepare paper base. According to another version, after paper web forming paper base is exposed to radiation to decrease polymerisation degree of fiber.

EFFECT: development of clean and economically effective process of paper base production for vulcanising and parchmentising as well as decrease of environmental pollution.

26 cl, 4 tbl, 3 ex

FIELD: pulp-and-paper industry, in particular, paper sheet having surface feeling hash to the finger, and method for applying coating onto paper sheet.

SUBSTANCE: paper sheet of such structure may be used for manufacture of paper or plastic medium for carrying of printed information, paper or plastic package, cover used in stitching and binding processes, or cardboard or plastic carton having surface feeling hash to the finger. At least one side of paper sheet is coated with layer containing non-compressible microscopic particles of non-gelatinized starch grains, or said particles are produced by grinding of plastic material. Method involves treating at least one side of paper sheet with water-based composition containing non-compressible microscopic particles which are made three-dimensional and rounded, binder, and filler; drying paper sheet after treatment. Particles are non-gelatinized starch grains, or particles are produced by grinding of plastic material. Method allows paper sheet to be produced, which has roughness coefficient Kd below 0.5.

EFFECT: simplified method and improved quality of paper sheet.

17 cl, 16 dwg, 1 tbl, 3 ex

FIELD: textiles, paper.

SUBSTANCE: invention relates to the production of hydrophilic fibrous composite materials for medical purposes, having bactericidal, hemostatic and anesthetic effect. Biologically active fiber sheeting is made in the form of fibrous base that contains cellulose, viscose fiber and a binder; the base is coated with a material containing additives in the immobilised form. The material has a weight of 75-90 g/m2, the weight of the coating is 35-50% relative to the weight of the fibrous weight. As a binder in the base a polyamine-poliamidepichlorohydrin resin is used. The coating is made on the basis of a cationic polysaccharide of natural origin. At that the additive is a blood-coagulation factor IV, antifibrinolytics, anesthetic, antimicrobial and plastifying agents.

EFFECT: reduction of quantity of fibrous materials in manufacture of the basics, and also it has new favourable features, namely, antimicrobial, hemostatic and analgesic effects.

3 cl, 1 tbl, 3 ex

FIELD: paper industry.

SUBSTANCE: one side of paper-based substrate is coated with the first dyeing composition to provide the degree of whiteness L* with the value of L1. The second dyeing composition is applied to the opposite side of the substrate having the degree of whiteness L* with the value of L2. A colored product is obtained, characterised by the degree of whiteness L* with a value of L3 for the first coated side. The second coated side of the product has a degree of whiteness L* with a value of L4. Thus L1 is not more than 8 points higher than L3, and L2 is at least 30 points higher than L4. The degree of whiteness L* is determined using the colour characteristics CIE L* a* b*, a clarifier D 65, and at the observation angle of 10°C. In this method, the penetration of dyeing substances of the dyeing composition is adjusted so that the minimal impact is achieved on the degree of whiteness of the coating of white or light colour on the opposite side of coloured paper.

EFFECT: obtaining high-quality colored paper, which has a high contrast ratio to ensure high-level package, simplification of method, reducing of cash expenses, time expenditures and labor.

15 cl, 1 dwg, 2 tbl

FIELD: textile, paper.

SUBSTANCE: article is perceived as dry to the touch and contains a foaming surfactant substance, in the form suitable to make soap foam in case of contact with water. The article is produced by application of a water solution of a foaming surfactant or a water composition comprising a foaming surfactant at one or more layers of a dry cloth of thin paper. The foaming surfactant is present in amount from 0.01 g/m2 to 6.00 g/m2. If a water composition is applied, then total amount of nonvolatile components of the specified composition does not exceed 20 wt % of dry mass of the specified one or more layers of thin paper. The method to clean hard surface consists in moistening of an article of thin paper with water and rubbing the hard surface.

EFFECT: article ensures efficient cleaning of hard surfaces, has voluminousness and thickness, even if a cleaning composition was applied on it, good persistence and mechanical strength, the article does not require moistureproof packaging or packaging materials.

32 cl, 3 dwg, 1 tbl, 4 ex

FIELD: textile, paper.

SUBSTANCE: article is made with at least partial use of short-fibre cellulose. To form at least two fractions of fibrous material comprising fibres having various composition, short-fibre mass is sifted through a sieve. Besides, fine fibres are separated from cellulose, which pass through the sieve with holes of diameter of 0.2-1.5 mm and which are caught and included into composition of various layers of the fibrous article.

EFFECT: improved tensile strength limit and rigidity during tensioning of long-fibre mass, and also dehydration and porosity.

19 cl, 10 dwg, 1 ex

FIELD: textile, paper.

SUBSTANCE: article is made with at least partial use of short-fibre cellulose. To form at least two fractions of fibrous material comprising fibres having various composition, short-fibre mass is sifted through a sieve. Besides, fine fibres are separated from cellulose, which pass through the sieve with holes of diameter of 0.2-1.5 mm and which are caught and included into composition of various layers of the fibrous article.

EFFECT: improved tensile strength limit and rigidity during tensioning of long-fibre mass, and also dehydration and porosity.

19 cl, 10 dwg, 1 ex

FIELD: textile, paper.

SUBSTANCE: article is made with at least partial use of short-fibre cellulose. To form at least two fractions of fibrous material comprising fibres having various composition, short-fibre mass is sifted through a sieve. Besides, fine fibres are separated from cellulose, which pass through the sieve with holes of diameter of 0.2-1.5 mm and which are caught and included into composition of various layers of the fibrous article.

EFFECT: improved tensile strength limit and rigidity during tensioning of long-fibre mass, and also dehydration and porosity.

19 cl, 10 dwg, 1 ex

FIELD: textile, paper.

SUBSTANCE: wallpaper substrate consists of a multilayer paper web with lower and upper sides. The lower side of the web faces a wall when applied. The upper side faces a room. Between the sides there is a lower layer and a fibrous upper layer arranged in direction from the lower side to the upper side. The fibrous lower layer is made of a mixture of fibrous materials based on cellulose and synthetic fibres. The fibrous upper layer is made of a mixture of fibrous materials based on cellulose. At the same time the upper and lower layers are interwoven with each other by means of moist pressing in a couch press. The upper side is satined and is arranged as sealed for direct printing. In particular, for deep printing with a maximum of 1 gap per 1 cm2.

EFFECT: improved quality of wallpapers.

24 cl, 1 dwg, 1 ex

FIELD: textile, paper.

SUBSTANCE: wallpaper substrate consists of a multilayer paper web with lower and upper sides. The lower side of the web faces a wall when applied. The upper side faces a room. Between the sides there is a lower layer and a fibrous upper layer arranged in direction from the lower side to the upper side. The fibrous lower layer is made of a mixture of fibrous materials based on cellulose and synthetic fibres. The fibrous upper layer is made of a mixture of fibrous materials based on cellulose. At the same time the upper and lower layers are interwoven with each other by means of moist pressing in a couch press. The upper side is satined and is arranged as sealed for direct printing. In particular, for deep printing with a maximum of 1 gap per 1 cm2.

EFFECT: improved quality of wallpapers.

24 cl, 1 dwg, 1 ex

FIELD: textile, paper.

SUBSTANCE: wallpaper substrate consists of a multilayer paper web with lower and upper sides. The lower side of the web faces a wall when applied. The upper side faces a room. Between the sides there is a lower layer and a fibrous upper layer arranged in direction from the lower side to the upper side. The fibrous lower layer is made of a mixture of fibrous materials based on cellulose and synthetic fibres. The fibrous upper layer is made of a mixture of fibrous materials based on cellulose. At the same time the upper and lower layers are interwoven with each other by means of moist pressing in a couch press. The upper side is satined and is arranged as sealed for direct printing. In particular, for deep printing with a maximum of 1 gap per 1 cm2.

EFFECT: improved quality of wallpapers.

24 cl, 1 dwg, 1 ex

FIELD: textile, paper.

SUBSTANCE: wallpaper substrate consists of a multilayer paper web with lower and upper sides. The lower side of the web faces a wall when applied. The upper side faces a room. Between the sides there is a lower layer and a fibrous upper layer arranged in direction from the lower side to the upper side. The fibrous lower layer is made of a mixture of fibrous materials based on cellulose and synthetic fibres. The fibrous upper layer is made of a mixture of fibrous materials based on cellulose. At the same time the upper and lower layers are interwoven with each other by means of moist pressing in a couch press. The upper side is satined and is arranged as sealed for direct printing. In particular, for deep printing with a maximum of 1 gap per 1 cm2.

EFFECT: improved quality of wallpapers.

24 cl, 1 dwg, 1 ex

FIELD: textile; paper.

SUBSTANCE: composition contains a fibrous mixture from chemical and thermomechanical mass and cellulose. The fibrous mixture contains birch leached chemical and thermomechanical mass with extent of grinding 60-125 ml (CSF) and cellulose with grinding extent of 350-500 ml (CSF) at the specified ratio of components. The cellulose in the fibrous mixture is a leached pine sulfate cellulose and/or pine sulphite cellulose, or pine cellulose, and/or leaf cellulose.

EFFECT: expansion of leaf-bearing soft woods due to using birch leached chemical and thermomechanical mass to prepare a fibrous semi-finished product to produce paper with high physical mechanical indices to ensure extent of whiteness.

3 cl, 1 tbl

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