Method and plant for processing of cellulose plant black liquor

FIELD: process engineering.

SUBSTANCE: invention relates to processing of black liquor of cellulose plant for extraction of chemicals and power contained therein. Proposed process comprises feed of black liquor into pyrolysis reactor with, in fact, no oxygen space. Sand heated in boiler with fluidised bed is fed into said reactor to gasify said black liquor so that gaseous components and soli matter are formed. Gaseous components formed in pyrolysis reactor are directed for recovery. Sand is separated from solid matter formed in pyrolysis reactor and returned back into boiler with fluidised bed. Water is added to remained solid matter to dilute soda contained in solid substance. Formed soda-water solution is returned to cellulose coking and remained solid coal to boiler with fluidised bed. This plant comprises the boiler with fluidised bed, pyrolysis, sand feeder, means to direct gaseous components, sand separator from solid matter, means to return separated sand, mixing reactor, means to return soda-water solution to cooking process and remained solid coal to boiler with fluidised bed.

EFFECT: extraction of chemicals and power in one cycle, increased volume of formed gases.

31 cl, 4 dwg

 

Background of the invention

The invention relates to a method of processing black liquor pulp mill to extract it in chemicals and energy. The invention also relates to an installation for the processing of black liquor pulp mill to extract it in chemicals and energy.

During the production of pulp wood raw material, such as wood chips, processed using heat and chemicals, by cooking in a chemical solution that contains liquor in addition to other components. This process is called cooking of cellulose. The purpose of this process is the removal of lignin, the binding fiber. Cooking chemicals used in Kraft pulping, are a mixture of sodium hydroxide (NaOH) and sodium sulfide (Na2S). In the soda cooking process for chemical pulping is a sodium hydroxide (NaOH). In the carbonate method of cooking for chemical pulping is a sodium carbonate (Na2CO3). After cooking fibrous pulp, which is separated from the wood material, is isolated from the cooking liquor, in which the various components of wood material, such as lignin and inorganic substances dissolved during digestion. This chemical compound, i.e. black liquor, which is separated after cooking, subsequently evaporated in the evaporation installation for to produce a combustible material that contains as little water as possible. This material is obtained from the final stage of evaporation, and is usually fed into the boiler for burning, can have a solids content up to 85%.

Traditionally black liquor burned in the recovery boiler, whereby produces steam and electricity for use as energy at the plant, and possibly for sale. The inorganic portion of the black liquor is removed from the recovery boiler in the form of a salt in the liquid state; the boiler produces heat, which heats and turns water into steam for energy production, and salt in a liquid state, from which reacquire cooking chemicals. This processing is disclosed, for example, in patents Finland 82494 and 91290.

Gasification of black liquor was tested as a replacement boiler, but commercially competitive solution practically not found.

Publication WO 2004/005610 discloses a solution in which the black liquor is subjected to pyrolysis, and the resulting pyrolysis coke is gasified. However, this method difficult to implement in practice and requires a separate and expensive installation of gasification.

Summary of the invention

The objective of this invention is to provide a method and installation for PE�of erebody black liquor, in which the boiler may be removed from the recycling process and which are simple and easily implementable using mostly existing equipment pulp mill.

The method of the invention differs

- flow black liquor pyrolysis reactor having essentially not containing oxygen space,

- feed in a pyrolysis reactor sand, is heated in the boiler with fluidized bed through which the black liquor is gasified and forms gaseous components and solid matter,

- direction of the gaseous components formed in the pyrolysis reactor, for recycling,

separation of sand from the solids in the pyrolysis reactor, and returning it to the boiler with fluidized bed,

- the addition of water to the remaining solid substance, which dissolves in the soda contained in the solid substance,

- the return of the formed solution soda-water in the pulping process and return the remaining solid coal into the boiler with fluidized bed.

The installation according to the invention is characterized in that it includes

- boiler with a fluidized bed,

- pyrolysis reactor, in which black liquor is served and where black liquor is subjected to pyrolysis in essentially not containing oxygen space and way�tons of gaseous components and solid matter,

- means for supplying sand obtained from the boiler with fluidized bed in the pyrolysis reactor,

- means for directing the gaseous components formed in the pyrolysis reactor, for recycling,

- a separator for separating the sand from the solids in the reactor of pyrolysis,

- a means for returning the separated sand to the boiler with fluidized bed,

- reactor mixing for mixing the separated solids with water so that the soda contained in the solid substance, soluble in water, and

- means for returning solution of soda-water in the pulping process and to return the remaining solid coal into the boiler with fluidized bed.

The basic idea of the invention consists in that the black liquor is subjected to pyrolysis, feeding black liquor and the sand is heated in the boiler with fluidized bed, in the same pyrolysis reactor, in which black liquor is heated to a suitable temperature essentially does not contain oxygen in space, so that the volatile materials contained in the black liquor is transformed into a gaseous state. Another basic idea of the invention is that the gaseous components are separated from the solids and feed on recycling, for example, to produce electricity; the sand is separated from the solids and direct� back into the boiler with fluidized bed; a solid substance is mixed with water, obtaining, thus, a solution of soda-water and the solid material is carbon, which is sent, for example, in the boiler with fluidized bed for further use. According to one embodiment of the inert gas or gas mixture is also fed into the pyrolysis reactor. According to another embodiment of the invention, the gaseous components formed in the pyrolysis reactor, is sent for further processing, such as cleaning and/or condensation. According to another embodiment of the invention, the sand is fed into the pyrolysis reactor so hot that it heats the black liquor to a temperature required for pyrolysis, whereby no additional heating in the pyrolysis reactor.

The method according to the invention provides the advantage that only a single chemical cycle is achieved by recovery of energy and chemicals. In addition, pyrolysis oil, separated from the gaseous components by condensation, can be used as a substitute for fossil fuel or, if necessary, it can be further purified to obtain a transport fuel. Another advantage is that when the pyrolysis is rapid, the formation of gas maximum. Also, postalcodenumber pyrolysis is low, to avoid problems of corrosion and contamination inherent in conventional boilers.

Brief description of the drawings

The invention will be described in more detail with reference to the accompanying drawings, among which:

Fig.1 shows a schematic view of one installation for applying the method according to the invention, and

Fig.2 shows a schematic view of a second system for applying the method according to the invention,

Fig.3 shows a schematic view of a third installation for applying the method according to the invention, and

Fig.4 shows a schematic view of the fourth installation for applying the method according to the invention.

Detailed description of the invention

Fig.1 shows a schematic view of the apparatus suitable for applying the method according to the invention. It has a boiler 1 with a fluidized bed, in which a suitable fuel burn 2, most preferably, fuel, formed in a pulp mill. It is also possible to feeding into the boiler with fluidized bed is known for solid, liquid or gaseous auxiliary fuel 3, such as oil, gas or any other suitable fuel. From the boiler with fluidized bed flue gases formed 4 channel known in itself a way to clean it and possibly heat recovery.

From the boiler with pseudois�NYM with a layer of hot sand 5, having a typical temperature of 200°C-900°C is fed into the reactor 6 pyrolysis, in which black liquor is also served 7 and fluidizing gas 8. The reactor 6 pyrolysis can be any suitable reactor, such as a furnace with a fluidized bed or the like.

Fluidizing gas 8 is an inert gas or mixture of gases. To this end it is possible to use pure inert gases, but much more preferable to use, for example, any described below neskondensirovannyh gases or gases which contain unreacted gases or gas mixtures such as carbon monoxide, carbon dioxide, nitrogen, oxides of nitrogen or water vapor. Additionally, even the flue gases are purified from solids such as flue gases from the boiler with fluidized bed, can be used as fluidizing gas.

The temperature in the reactor 6 pyrolysis is approximately 200°C-900°C, preferably 400°C-700°C. When the hot sand 5 having a temperature of 200°C-900°C, served in it, it heats the black liquor. The gaseous components 9 and the solid is 10, which contains mainly ash and particulate carbon, subsequently formed in the reactor material from black liquor.

The gaseous components 9 channel for further processing or use as such in their gotoblas�th form to obtain a transport fuel or as an auxiliary fuel in the boiler 1 of a fluidized bed. Alternatively, the gases may be directed into the condenser 11. In the condenser 11 condensed gases form the oil 12, which is directed for use as fuel to produce electricity, or it can be further purified to obtain, for example, an automotive fuel. This oil can also be used in the boiler 1 with a fluidized bed as an auxiliary fuel. Neskondensirovannyh gases 13 in turn is directed to the production of electricity or for disposal by other means, and at least some of them can be directed back into the boiler 1 with a fluidized bed as an auxiliary fuel or fluidizing gas 8.

The mixture of solids and sand fed to a separator 14, where the sand 5 was separated from the residue solids and returned to the boiler 1 with a fluidized bed. The remaining solid material 15 is fed to the reactor 16 mixing, add water 17. Soda in the solid state (TV.), Na2CO3(TV.), present in the solid 16, is dissolved in water and then can be directed back into the pulping process in the form of a solution 18 soda-water [H2O+Na2CO3(water.)]. The remaining solid material 19 is essentially solid carbon, which can be returned to the boiler with pseudodog�by the layer as such or after drying in the dryer 20.

The gaseous components and solid matter can also be sent in a separate gas separator 21, which may be, for example, a conventional cyclone separator. In the gas separator 21 solid and sand formed in the reactor 6 pyrolysis is separated from the gaseous components, which are sent for disposal, and solid and sand is directed into the separator 14 for separating them from each other. If necessary, the reactor 6 pyrolysis can be heated, also using a separate heat source 22, so that the pyrolysis reactor is not supplied oxygen-containing material. It is most preferable to use the indirect heating in which heat of the heat source used to heat the pyrolysis reactor from the outside.

Fig.2 shows a schematic view of a second system suitable for applying the method according to the invention. The same reference position used in Fig.1, used for corresponding components in the case of Fig.2, and for them it is not given a separate explanation if this is not necessary for understanding. The solution shown in Fig.2, differs from the solution shown in Fig.1, in that the pyrolysis reactor is a rotary kiln, which is heated from the outside.

In this case, the reactor 6 pyrolysis is essentially g�izontally, tubular furnace, which can also be rotated about its longitudinal axis. Black liquor 7 and sand 5 preferably serves at the upper end, i.e. the loading end located slightly inclined furnaces, and, accordingly, the solid material 10 is removed from the lower end, i.e. the discharge end of the tubular furnace, the separator 14. Inside the furnace may also be located in its longitudinal direction, the mixer or feed auger that propels the solid material through the furnace with a suitable speed. Gas components 9, formed in the reactor 6 pyrolysis are removed from the upper end of the tubular furnace and sent for disposal or recycling, as shown in Fig.1. In this embodiment, the implementation there is no need for a separate separator for separating solids and gases from each other, and the furnace, which forms the reactor 6 pyrolysis, is also a means for their separation.

Flue gas 4 from the boiler 1 fluidized bed is sent over a separate channel 22 to heat the reactor 6 pyrolysis. Around the tubular furnace was created preferably heat-insulating channel system or the space through which flue gases flow from the boiler 1 with a fluidized bed, so that the combustion gases are suitable to the discharge end of the reactor 6 pyrolysis, that is, tubular furnace, and then takuto direction to the loading end of the furnace and from there, the flue gases 4 are removed for processing as needed. Thus, in the pyrolysis reactor is a countercurrent heat whereby subjected to pyrolysis black liquor is continuously heated as it progresses through the furnace toward the discharge end. At least one discharge channel 23 for discharging solids, such as ash separated from the flue gases, preferably formed in the channel 22 of the flue gas in the pyrolysis reactor or any other suitable location.

Instead of or in addition to heating the flue gas of the boiler with fluidized bed, pyrolysis reactor may also be heated burners using liquid or gaseous fuel by feeding them hot flue gases to heat the pyrolysis reactor.

In the case of a separate external heating of the pyrolysis reactor inlet temperature of sand may be lower because the sand there is no need to heat the black liquor to a temperature of pyrolysis, as it is performed at the expense of additional heat. Thus, the temperature of the sand can only be 200°C or more.

If due to the operation of the reactor 6 pyrolysis temperature tends to rise too high or the exhaust flue gases are too hot, the flue gases can be cooled before they are served to heat the reactor 6 PIR�Lisa, using cooling solutions, known in themselves, for example, in refrigerators or on the surfaces of heat transfer 24 in which the heat of the flue gases is extracted and utilized elsewhere in the process.

Instead of heating the flue gases is also possible to apply any other method of heating in which the temperature in the reactor 6 pyrolysis becomes suitable for pyrolysis and is preferably 400°C-700°C.

In the case of using a horizontal furnace as a reactor 6 pyrolysis, it does not require a separate pseudoviruses gas.

Fig.3 and 4 illustrate additional embodiments of the invention.

Fig.3 shows the solution corresponding to the solution of Fig.1, and Fig.4 shows the solution corresponding to the solution of Fig.2, except that they also have a separate vessel 25 recausticizing, served in a solution of 18 soda-water [H2O+Na2CO3(water.)]. In addition, calcium oxide 26 (CaO) is fed in the form of solids (TV.) in the vessel 25 recausticizing, whereby you get sodium hydroxide (NaOH) and calcium carbonate (CaCO3as the reaction product. Formed by their mixture 27 is directed into the separator, which is known in itself and not shown in the drawings and from which sodium hydroxide (NaOH) are recycled in the process, and the calcium carbonate (CaCO3) send n� roasting method known by itself, after which the resulting calcium oxide (CaO) can be re-filed in a vessel recausticizing.

The method according to the invention, thus, does not require a conventional recovery boiler, and removing chemicals from the black liquor can be carried out mainly through the pyrolysis reactor, the size and investment costs which are a fraction of the cost of the boiler-utilizer. Likewise, the operating costs of the pyrolysis reactor is quite low compared to the recovery boiler. As the gas generated in the pyrolysis reactor, can also be used or further purified for use as fuel gas turbines or diesel generators, electric power and steam required in the method, can be produced much more efficiently than when using the known solutions with heat recovery boiler. Also, applying the solution according to the invention, it is possible to avoid solutions that require expensive gasifier, the application of which, at least according to the current experience, quite difficult.

Boiler fluidized bed can be any known boiler with a fluidized bed, in which the sand can be heated and from which the sand can be recycled to the pyrolysis reactor. The pyrolysis reactor may be made�perform any suitable pyrolysis reactor, but the use of a horizontal rotary cylindrical furnace is preferred because the operation and behavior is well known and controlled. The reactor mixing can, in turn, may be any suitable reactor mixing, which can be served solids from the separator and the water and from which a suitable image can be removed by solution and solid. It is also possible to use after reactor mixing separate separator, through which a solution of soda-water is separated from solids. If necessary, solid substance, which is essentially carbon, can be dried before it is fed to the boiler with fluidized bed.

The invention set forth above in the description and drawings merely by way of example and in no way limited to them, and the scope of protection defined in the enclosed claims. Thus, individual features of various existing examples can also be combined and applied as required to other options implementation.

1. A method of processing black liquor pulp mill to extract it in chemicals and energy, characterized in that it includes:
the supply of black liquor pyrolysis reactor having essentially not containing oxygen space,
feed in a pyrolysis reactor sand, heated in the boiler with fluidized bed through which the black liquor is gasified and forms gaseous components and solid matter,
the direction of the gaseous components formed in the pyrolysis reactor, for recycling,
separation of sand from the solids in the pyrolysis reactor, and return it to the boiler with fluidized bed,
adding water to the remaining solid substance, which dissolves in the soda contained in the solid substance,
return the resulting solution of soda-water in the pulping process and return the remaining solid coal into the boiler with fluidized bed.

2. A method according to claim 1, characterized in that the gaseous components and solid matter formed in the pyrolysis reactor, is sent to a separator to separate them from each other.

3. A method according to claim 1, characterized in that the pyrolysis reactor serves inert gas or mixture of gases with which the black liquor is mixed.

4. A method according to claim 2, characterized in that the pyrolysis reactor serves inert gas or mixture of gases with which the black liquor is mixed.

5. A method according to claim 3 or 4, characterized in that the gas or mixture of gases, directional(nd) in a pyrolysis reactor at least partially formed by(a) gases derived from the pyrolysis reactor, which remain neskondensirovannyh last� condensation.

6. A method according to claim 3 or 4, characterized in that the gas or mixture of gases, directional(nd) in a pyrolysis reactor at least partially formed by(a) carbon dioxide or carbon monoxide.

7. A method according to claim 3 or 4, characterized in that the gas or mixture of gases, directional(nd) in a pyrolysis reactor at least partially formed by(a) nitrogen or oxides of nitrogen.

8. A method according to claim 3 or 4, characterized in that the gas or mixture of gases, directional(nd) in a pyrolysis reactor at least partially formed by(a) flue gases.

9. A method according to any one of claims.1-4, characterized in that the temperature in the pyrolysis reactor is 200°C-900°C, preferably 400°C-700°C.

10. A method according to any one of claims.1-4, characterized in that the sand is fed into the pyrolysis reactor at a temperature of 200°C-900°C, preferably 400°C-700°C.

11. A method according to any one of claims.1-4, characterized in that the pyrolysis reactor and heated in a separate heat source.

12. A method according to claim 11, characterized in that the pyrolysis reactor is heated by external heating.

13. A method according to claim 12, characterized in that the pyrolysis reactor is heated by heat from the outside flue gases from the boiler with fluidized bed.

14. A method according to any one of claims.1-4, characterized in that the pyrolysis reactor is used essentially in a horizontal cylindrical furnace.

15. A method according to claim 14, wherein the�, that cylindrical furnace is rotated during pyrolysis.

16. A method according to any one of claims.1-4, characterized in that as a cyclone separator is used.

17. A method according to claim 14, characterized in that the separator used in a horizontal cylindrical furnace, which serves as a pyrolysis reactor.

18. A method according to any one of claims.1-4, characterized in that the gaseous components separated in the separator is condensed in the condenser, whereby oil is extracted, and neskondensirovannyh gases are sent for reuse in other processes where needed fuel.

19. Installation for processing black liquor pulp mill to extract it in chemicals and energy, characterized in that it includes
boiler fluidized bed,
pyrolysis reactor, in which black liquor is served and where black liquor is subjected to pyrolysis in essentially not containing oxygen space and forms gaseous components and solid matter,
means for supplying sand obtained from the boiler with fluidized bed in the pyrolysis reactor,
means for directing the gaseous components formed in the pyrolysis reactor, for recycling,
a separator for separating the sand from the solids in the reactor of pyrolysis,
means for returning the separated sand to the boiler � fluidized bed,
the reactor mixing for mixing the separated solids with water so that the soda contained in the solid substance, soluble in water,
the means for returning solution of soda-water in the pulping process and to return the remaining solid coal into the boiler with fluidized bed.

20. Apparatus according to claim 19, characterized in that it includes means of an inert gas or mixture of gases in the pyrolysis reactor.

21. Apparatus according to claim 20, characterized in that it has a separate heat source for heating the pyrolysis reactor.

22. Apparatus according to claim 21, characterized in that it has a separate heat source mounted to heat the pyrolysis reactor from the outside.

23. Apparatus according to claim 22, characterized in that the flue gases of the boiler with fluidized bed used as a separate heat source.

24. Apparatus according to any one of claims.19-23, characterized in that the pyrolysis reactor is used essentially in a horizontal cylindrical furnace.

25. Apparatus according to claim 24, characterized in that the cylindrical furnace is installed so that it rotates around its longitudinal axis.

26. Apparatus according to any one of claims.19-23, characterized in that the furnace serves as a pyrolysis reactor, used as a means of separation from each other gaseous components and solid matter, clicks�Savasana in the pyrolysis reactor.

27. Apparatus according to any one of claims.19-23, characterized in that the separator is used as a means of separation from each other gaseous components and solid matter formed in the pyrolysis reactor.

28. Apparatus according to claim 27, characterized in that the separator is a cyclone.

29. Apparatus according to any one of claims.19-23, characterized in that it comprises a condenser, which condenses the gaseous components separated in the separator, whereby oil and neskondensirovannyh gases; and a means for their areas for reuse in other processes where needed fuel.

30. Apparatus according to any one of claims.19-23, characterized in that the temperature in the pyrolysis reactor is 200°C-900°C, preferably 400°C-700°C.

31. Apparatus according to any one of claims.18-23, characterized in that it includes means for supplying sand to the pyrolysis reactor at a temperature of 200°C-900°C, preferably 400°C-700°C.



 

Same patents:

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1 tbl, 8 ex

FIELD: textile fabrics, paper.

SUBSTANCE: it is intended for usage in pulp and paper industry. Invention contains processing unit for treatment of fibrous cellulose basic material, containing treatment tool for discharge of inclusion from basic material, grinding tool for basic material crushing for destruction in it nodes and decompose tool for decomposition lengthway of crushed basic material. It is used conveyor with pair of rotated in the same direction screws for treatment of crushed material into paper pulp, at that conveyor is devided into multitude of sections, facility for feeding of materials to be treated at least in one area and facility for temperature control and/or pressure at least in one of areas. Black liquor, formed during the process of paper pulp output, is treated in facility, containing evaporator for concentration of black liquor till containing of solid substance 30-70%, instrument for treatment of concentrated black liquor at temperature 300-650°C and encapsulated conveyor for transportation of concentrated black liquor from evaporator to instrument at temperature higher than 90°C. Invention also includes method, consisting in usage of described above facility.

EFFECT: creation of treatment advantageous process of fibrous cellulose basic material and treatment of black liquor.

39 cl, 5 dwg, 1 tbl

FIELD: textiles, paper.

SUBSTANCE: method refers to cellulose washing method and can be used in pulp and paper industry to obtain sulfite cellulose when producing paper and cardboard and chemical processing. Cellulose is rinsed with cold water in the presence of organic additive agent SAA of weakly anionic type - compound UMS-1. The present additive is water-based mixture of biodegradable ethoxylated fatty alcohols and non-chlorinated solvents. Additive consumption makes 0.005-0.02% of completely dry pulp weight.

EFFECT: enhancement of cellulose washing efficiency and pulldown of common and hazardous resin content in cellulose.

3 tbl, 15 ex

FIELD: paper industry.

SUBSTANCE: device comprises hollow cylindrical body with tightly attached bottom and cover. Body contains at least two porous elements, which are equipped with facilities for fixation to body, cover plug, facilities of tangential supply of liquid phase inside body, facilities of gas supply inside body, facilities for withdrawal of products of gas dissolution in water medium. All porous elements are equipped with facilities of tight fixation of them to each other by lateral sides and by end sides to bottom of body and cover-plug, and altogether they create tight regular volumetrical body, which creates longitudinal external and internal cavities in its internal space together with body walls, being communicated to each other only through pores of elements for separate supply of water medium and gas accordingly. Axis of internal cavity matches axis of body.

EFFECT: simplified manufacturing of device elements, unification of porous elements, simplified assembly of device and its maintenance.

4 cl, 3 dwg

FIELD: woodworking industry.

SUBSTANCE: water medium, which comprises cooking base, is treated with gas mixture that contains sulfur dioxide. For this purpose device is used with tangential supply of water medium, which is equipped with porous element that separates it internal space into two longitudinal cavities. Gas mixture is supplied along one side of element and further to water medium through its pores under pressure of 0.6-1.2 MPa, and water medium is supplied along another side of element under pressure that is 0.04-0.06 MPa lower than pressure of gas mixture. Water medium is supplied in the form of main and additional flows. Water medium after its treatment with gas mixture is exposed to floatation cleaning with application of inertial gaseous part of processing products as flotator. Blower products from cooking boilers are supplied into water medium in process of its floatation cleaning.

EFFECT: increased efficiency of process and simplified process.

4 cl, 1 dwg, 3 ex

FIELD: chemistry.

SUBSTANCE: water suspension of crushed aspen wood is put into a flow reactor and ozonised. Ozonation is carried out with concentration of ozone in the ozone-oxygen mixture equal to 90 mg/l, gas flow rate equal to 2-4 l/h and temperature of 20°C and hydromodulus between 0.1:1.0 and 1.6:1.0.

EFFECT: high quality of the cellulose intermediate product, low consumption of reagents, high ecological cleanness of the process.

5 ex, 2 tbl

FIELD: oil and gas industry.

SUBSTANCE: synthesis method of multi-purpose self-adjusting catalyst for liquid-phase low-temperature oxidation cracking of organic raw material, including natural biomass, is described, and it consists in the fact that iron salt FeCl3 x 6H2O is dissolved in water containing lower alcohol in concentrations required for formation of colloid system capable of peptisation, at heating up to the temperature not exceeding 100°C and constant mixing so that suspension of colloid solid particles of iron oxides containing organic impurities is obtained. The above suspension can change its activity depending on type of organic raw material and oxidiser, and at cracking of natural biomass and in case the latter represents lignine or lignine-containing biomass it has properties of ferments in relation to lignine. Method of liquid-phase low-temperature oxidising cracking of organic raw material, including natural biomass, in presence of catalyst at atmospheric pressure is described. At that, air oxygen and/or hydrogen peroxide is used as oxidiser and the above catalyst is used as catalyst.

EFFECT: high-activity catalyst of liquid-phase oxidising cracking.

8 cl, 7 dwg, 11 ex

FIELD: chemistry.

SUBSTANCE: raw material undergoes steam treatment before the cooking step. Cellulose obtained by cooking, undergoes cold caustic extraction (CCE) during subsequent treatment.

EFFECT: invention enables to obtain cellulose with high output and purity of the product, and avoid accumulation of hemicellulose in the bleaching filtrate.

21 cl, 7 ex, 9 tbl, 13 dwg

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