CN109403115B - Method for producing acetified-grade dissolving pulp by using poplar slabs - Google Patents

Method for producing acetified-grade dissolving pulp by using poplar slabs Download PDF

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CN109403115B
CN109403115B CN201811228170.XA CN201811228170A CN109403115B CN 109403115 B CN109403115 B CN 109403115B CN 201811228170 A CN201811228170 A CN 201811228170A CN 109403115 B CN109403115 B CN 109403115B
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mass
pulp
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CN109403115A (en
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吴朝军
于冬梅
李荣刚
王东
李书平
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Qilu University of Technology
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Qilu University of Technology
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Priority to PCT/CN2018/114525 priority patent/WO2020082427A1/en
Priority to US16/314,319 priority patent/US20200173103A1/en
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    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/22—Other features of pulping processes
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C5/00—Other processes for obtaining cellulose, e.g. cooking cotton linters ; Processes characterised by the choice of cellulose-containing starting materials
    • D21C5/005—Treatment of cellulose-containing material with microorganisms or enzymes
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/02—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes
    • D21C3/022—Pulping cellulose-containing materials with inorganic bases or alkaline reacting compounds, e.g. sulfate processes in presence of S-containing compounds
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C1/00—Pretreatment of the finely-divided materials before digesting
    • D21C1/02—Pretreatment of the finely-divided materials before digesting with water or steam
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/003—Pulping cellulose-containing materials with organic compounds
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C3/00—Pulping cellulose-containing materials
    • D21C3/006—Pulping cellulose-containing materials with compounds not otherwise provided for
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
    • D21C9/10—Bleaching ; Apparatus therefor
    • D21C9/1005—Pretreatment of the pulp, e.g. degassing the pulp

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  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Biochemistry (AREA)
  • Microbiology (AREA)
  • Engineering & Computer Science (AREA)
  • Wood Science & Technology (AREA)
  • Inorganic Chemistry (AREA)
  • Paper (AREA)

Abstract

The invention relates to the technical field of dissolving pulp preparation, in particular to a method for producing acetified dissolving pulp by using poplar slabs, which comprises the following steps: adding auxiliary agent for prehydrolysis(ii) a Cooking by Soda/AQ for the first stage; Soda/AQ cooking II stage; o isPDQEPP bleaching; and (4) carrying out enzyme synergistic treatment. Preparing high-purity and high-reaction-activity poplar board skin acetification grade dissolving pulp; the used chemicals are clean and environment-friendly, and the production process is clean.

Description

Method for producing acetified-grade dissolving pulp by using poplar slabs
Technical Field
The invention relates to the technical field of dissolving pulp preparation, in particular to a method for producing acetified dissolving pulp by using poplar slabs.
Background
Figure DEST_PATH_IMAGE002
At present, the yield of cellulose acetate in the world is nearly 100 ten thousand tons, while the annual production of cellulose acetate in China is nearly 40 ten thousand tons, the annual consumption of acetified wood dissolving pulp is about 30 ten thousand tons, the acetified wood dissolving pulp is mainly used for preparing cellulose triacetate and cellulose diacetate, hydroxyl groups on three positions 2, 3 and 6 on cellulose glucose units in the dissolving pulp are almost completely acetylated to obtain the cellulose triacetate (the substitution degree is more than 2.7), the cellulose triacetate is hydrolyzed to obtain the cellulose diacetate (the substitution degree is 2.4-2.6), and the reaction process is shown as the following formula.
Cellulose triacetate is widely used for films, liquid crystal display polarizing films, reverse osmosis membranes, etc., while cellulose diacetate is widely used for cigarette filters, plastic products, etc. Cellulose acetate has higher requirements on raw material, namely acetified-grade dissolving pulp, namely high purity and high reaction activity, at present, only acetified-grade cotton pulp can be prepared in China, and the acetified-grade wood dissolving pulp with high purity and high reaction activity mainly depends on import.
The process for preparing acetified dissolving pulp by using wood as a raw material at home and abroad usually adopts a prehydrolysis process, a sulfate cooking process, an ECF bleaching process or an acid sulfite cooking process, an ECF bleaching process and a cold alkali extraction process, and in order to improve the removal rate of prehydrolysis hemicellulose, inorganic acid or organic acid is usually added, so that the corrosivity of equipment is increased. In order to improve the delignification rate, some researchers adopt KP cooking technology with high vulcanization degree, but the high vulcanization degree is easy to generate odor such as methyl mercaptan, dimethyl sulfide and the like; in order to reduce ash content of dissolving pulp, dissolving pulp manufacturers need to perform acid treatment after paper pulp bleaching, but a low pH value is easy to cause part of cellulose in the dissolving pulp to be subjected to acid hydrolysis and depolymerization; in order to improve the alpha-cellulose content of the acetified dissolving pulp, some scholars adopt cold alkali extraction, but the reaction activity capacity of the acetified dissolving pulp and acetic anhydride is seriously reduced, and Egyptian scholars treat the acetified dissolving pulp by microwave radiation and high-concentration zinc chloride to improve the reaction activity, but the technology is not mature; U.S. patent reports that treatment of acetified grade dissolving pulp with strong acid increases its purity, but this technique has high pollution level and high cost. The research and development of the technology are carried out in several institutes in China, and mainly units such as southern China university, Beijing forestry university and Tokyo university make some progress in the research and development of the technology, and mainly focus on preparing acetified dissolving pulp from eucalyptus, acacia and pine.
The poplar board skin is used as the wood processing residue, the price is low, the raw materials are sufficient, the annual production amount of the wood processing residue in China is about 5000 ten thousand tons, the poplar board skin is used as one of the wood processing residues, the comprehensive cellulose content is about 82 percent, the alpha-cellulose content is about 44 percent, and if the poplar board skin is used as the raw material to produce the high-reaction-activity acetification grade dissolving pulp, the method is greatly beneficial to the development of the raw material of the acetification grade dissolving pulp. However, no record is available at home and abroad for preparing acetified-grade dissolving pulp by using poplar slabs.
Disclosure of Invention
In order to solve the technical blank that no poplar board skin is used for preparing acetified-grade dissolving pulp in the prior art, the application discloses a method for producing acetified-grade dissolving pulp by using poplar board skins.
Removing hemicellulose from poplar bark, selectively protecting cellulose, swelling fiber cells, cooking in different stages, selectively removing lignin and hemicellulose, controlling cellulose polymerization, and hydrogen peroxide-reinforced oxygen delignification of pulp/chlorine dioxide bleaching with chelating agentHot alkaline extraction with hydrogen peroxide addition/hydrogen peroxide bleaching (O)PDQEPP) removing residual lignin and hemicellulose, improving the whiteness of the pulp and adjusting the polymerization degree of the dissolved pulp, and performing biological enzyme synergistic treatment on the bleached pulp to further improve the acetification reaction value (PV value) of the bleached pulp and reduce the content of ash and Dichloromethane (DCM) extracts. After the process is adopted for treatment, the purity and the reaction activity of the acetified dissolving pulp are improved.
The invention is obtained by the following steps:
a method for producing acetified-grade dissolving pulp by using poplar slabs comprises the following steps:
(1) adding an auxiliary agent for prehydrolysis: the liquid ratio is 1 (4-10), the addition amount of a hydrolysis auxiliary agent is 0.1-2.0% of the mass of dry substances of the poplar board skin, the hydrolysis temperature is 80-170 ℃, the heat preservation time is 10-180 minutes, and the hydrolysis auxiliary agent is a mixture obtained by mixing sodium borate, magnesium sulfate, nonylphenol polyoxyethylene ether phosphate and tetrasodium iminodisuccinate according to the mass ratio of 1:1:1: 1;
(2) cooking by Soda/AQ for the first stage;
(3) Soda/AQ cooking II stage;
（4）OPDQEPp bleaching;
(5) enzyme synergistic treatment: the pulp concentration is 2-10%, the temperature is 30-50 ℃, the treatment time is 60min, the pH is = 4.0-7.0, the dosage of polyaspartic acid is 0.01-1.0% of the mass of the oven-dried pulp, the dosage of OP-13 is 0.001-0.01% of the mass of the oven-dried pulp, the dosage of OP-15 is 0.001-0.01% of the mass of the oven-dried pulp, the dosage of cellulose incision enzyme is 0.1-0.6 IU/gpulp, the dosage of xylanase is 2-4 XU/gpulp, and the dosage of pectinase is 0.1-10 IU/gpulp.
The preferred technological conditions of the first stage of Soda/AQ cooking are as follows: with Na2The alkali consumption is 5-15% of the mass of the oven dry pulp in terms of O, the liquid ratio is 1 (3-8), the consumption of magnesium hydroxide is 0.5% of the mass of the oven dry pulp, the consumption of sodium sulfite is 1.0-10.0% of the mass of the oven dry pulp, the consumption of AQ is 0.05% of the mass of the oven dry pulp, the temperature is 80-120 ℃, and the heat preservation time is 10-180 minutes.
The preferred Soda/AQ cooking II stage process conditions are as follows: with Na2The alkali consumption is absolutely dry when measured by O5-25% of pulp mass, 0.5% of magnesium hydroxide, 1.0-10.0% of sodium sulfite and 1 (3-10) of liquid ratio, wherein the amount of AQ is 0.05% of oven-dried pulp mass, the temperature is 140-180 ℃, and the heat preservation time is 10-240 minutes.
Preferably OPDQEPThe bleaching process conditions are as follows: o isPThe oxygen pressure of bleaching is 0.4-0.6 Mpa, the pulp concentration is 10 percent, and MgSO4The dosage of the sodium hydroxide is 0.6 percent of the mass of the oven-dry pulp, the dosage of the NaOH is 1.0-3.0 percent of the mass of the oven-dry pulp, and the H2O2The using amount is 0.5-3.0% of the mass of the oven-dried pulp, the temperature is 70-110 ℃, and the temperature is kept for 60min.
Preferably OPDQEPThe bleaching process conditions are as follows: qDThe bleaching process has the reaction time of 10-120 minutes, T =30 +/-2 ℃, pulp concentration of 2-8%, pH = 1-3, the use amount of sodium chlorite is 0.2-6.0% of the mass of the oven-dried pulp, and the use amount of IDS is 0.01-1.0% of the mass of the oven-dried pulp.
Preferably OPDQEPThe bleaching process conditions are as follows: the reaction time of the Ep extraction process is 30-180 min, MgSO4The dosage of the sodium hydroxide is 0.5 percent of the mass of the oven-dry pulp, the dosage of the NaOH is 0.5 to 5.0 percent of the mass of the oven-dry pulp, and the H2O2The dosage of the pulp is 1.0-5.0% of the mass of the oven-dried pulp, the dosage of IDS is 0.01-1.0% of the mass of the oven-dried pulp, the pulp concentration is 8%, and the temperature is 70-95 ℃.
Preferably OPDQEPThe bleaching process conditions are as follows: the reaction time of the P bleaching is 60-180 min, MgSO4The dosage of the sodium hydroxide is 0.5 percent of the mass of the oven-dry pulp, the dosage of the NaOH is 0.4 percent of the mass of the oven-dry pulp, the dosage of the NaAC is 0.4 percent of the mass of the oven-dry pulp, and the H content is2O2The dosage of the pulp is 1.0-5.0% of the mass of the oven-dried pulp, the pulp concentration is 10%, and the temperature is 80-95 ℃.
In conclusion, the auxiliary agent is added during prehydrolysis of the poplar board skin to selectively remove hemicellulose in the poplar board skin, then the auxiliary agent-added Soda/AQ is adopted for segmented cooking to remove lignin as much as possible and protect cellulose, and the pulp after cooking is subjected to O treatmentPDQEPP bleaching to further remove lignin and regulate the polymerization degree of dissolving pulp, and finally, using enzyme synergistic process to further raise the purity of dissolving pulpThe reaction activity of the dissolving pulp is high and adjusted, and the poplar board skin acetification grade dissolving pulp with high purity and high reaction activity is obtained.
The invention has the beneficial effects that:
(1) firstly, the hemicellulose in the poplar board skin is dissolved out in a large scale and selectivity manner by means of prehydrolysis with the addition of an auxiliary agent, finally, the purity and acetification reaction value of the poplar board skin pulp are further improved by adopting enzyme synergistic treatment, and then the Soda/AQ segmented cooking and O-steaming are combinedPDQEPP bleaching, preparing high-purity and high-reaction-activity poplar board skin acetification grade dissolving pulp;
(2) the poplar veneer is treated by adopting the process, the used chemicals are clean and environment-friendly, and the production process is clean.
Drawings
FIG. 1 is a process flow chart of the production of acetified-grade dissolving pulp by using poplar slabs.
Detailed Description
For a better understanding of the present invention, reference is made to the following examples which are set forth to illustrate, but are not to be construed to limit the present invention.
In the following examples, the hydrolysis assistant is a mixture obtained by mixing sodium borate, magnesium sulfate, nonylphenol polyoxyethylene ether phosphate and tetrasodium iminodisuccinate in a mass ratio of 1:1:1: 1.
The percentage of the materials used in each process stage is the percentage of the materials in the oven dry pulp.
Example 1:
pre-hydrolysis with addition of auxiliary agent-Soda/AQ staged cooking with addition of auxiliary agent-OPQDEpP-processing poplar board skin raw material by enzyme synergistic process: 500g of poplar bark pieces of a certain factory, which are 10-30mm long, are taken, the pentosan content of the poplar bark pieces is 24.3 percent, and the alpha-cellulose content of the poplar bark pieces is 43.0 percent.
The prehydrolysis process conditions for controlling the addition of the auxiliary agent are as follows: the liquid ratio is 1:6, the additive is 0.4%, the maximum temperature is 160 ℃, the heat preservation time is 60 minutes, the content of pentosan after hydrolysis is 8.6%, and the hydrolysis yield is 80%;
the process conditions of the first stage of Soda/AQ cooking are as follows: 5 percent of alkali, 1: 4 of liquid ratio, 0.5 percent of magnesium hydroxide, 5.0 percent of sodium sulfite, 0.05 percent of AQ, 100 +/-2 ℃ of Tmax and 60 minutes of heat preservation time;
the Soda/AQ cooking II stage process conditions are as follows: the alkali consumption is 18%, the magnesium hydroxide is 0.5%, the sodium sulfite is 3.0%, the liquid ratio is 1:7, the AQ consumption is 0.05%, the maximum temperature is 160 ℃, and the heat preservation time is 120 minutes;
OPthe oxygen pressure of the bleaching is 0.5Mpa, the pulp concentration is 10 percent, and MgSO40.6%，NaOH 2.0%，H2O21.0 percent, keeping the temperature at 95 ℃ for 60 min;
QDthe bleaching process has the reaction time of 60 minutes, T =30 +/-2 ℃, the pulp concentration is 4.0%, the pH =1.5, the sodium chlorite dosage is 3.0%, and the IDS dosage is 0.05%;
reaction time of Ep extraction process is 90min, MgSO4 0.5%，NaOH 3.0% ，H2O22.0 percent of IDS, 0.05 percent of IDS, 8 percent of pulp concentration and 85 ℃ of temperature;
reaction time of P bleaching 120min, MgSO4 0.5%，NaOH 0.4% ，NaAC 0.4%，H2O23.0 percent of pulp concentration and 90 ℃ of temperature;
the enzyme synergistic treatment conditions are as follows: the pulp concentration is 5%, the temperature is 40 ℃, the treatment time is 60min, the pH is =5.0, the dosage of polyaspartic acid (polyaspartic acid) is 0.05%, the dosage of OP-13 is 0.005%, the dosage of OP-15 is 0.005%, the dosage of cellulose endoenzyme is 0.2IU/gpulp, the dosage of xylanase is 3XU/gpulp, and the dosage of pectinase is 3 IU/gpulp.
The content of alpha-cellulose in the obtained poplar board skin acetified-grade dissolving pulp is 97%, the content of pentosan is 2.6%, the polymerization degree is 1250, the whiteness is 89% ISO, the ash content is 0.01%, the content of DCM extract is 0.03%, and the acetification reaction value (PV value) is 800.
The poplar board skin acetification grade dissolving pulp has good detection indexes and can be used for producing high-grade cellulose acetate products.
Example 2:
pre-hydrolysis with addition of auxiliary agent-Soda/AQ staged cooking with addition of auxiliary agent-OPQDEpP-enzyme synergistic process for treating poplar board skin raw material, the pentosan content of the poplar board skin is 22.3%, the alpha-cellulose content is 45.0%, and the process conditions are the same as those in example 1. The content of alpha-cellulose in the obtained poplar board skin acetification grade dissolving pulp is 97 percent, the pentosan content is 2.2 percent,1280 for polymerization degree, 90% ISO for whiteness degree, 0.01% for ash content, 0.02% for DCM extract and 820 for acetification reaction value (PV value).
The poplar board skin acetification grade dissolving pulp has good detection indexes and can be used for producing high-grade cellulose acetate products.
Example 3:
pre-hydrolysis with addition of auxiliary agent-Soda/AQ staged cooking with addition of auxiliary agent-OPQDEpP-enzyme synergistic process for treating poplar board skin raw material, the collected poplar board skin is the same as example 1. Only the prehydrolysis heat preservation time is changed to 120 minutes, the content of pentosan after hydrolysis is 8.5 percent, the hydrolysis yield is 79 percent, and other processes are not changed. The content of alpha-cellulose in the obtained poplar board skin acetified-grade dissolving pulp is 97%, the content of pentosan is 2.2%, the polymerization degree is 1200, the whiteness is 89% ISO, the ash content is 0.01%, the content of DCM extract is 0.02%, and the acetification reaction value (PV value) is 780.
Example 4:
pre-hydrolysis with addition of auxiliary agent-Soda/AQ staged cooking with addition of auxiliary agent-OPQDEpP-enzyme synergistic process for treating poplar board skin raw material, the collected poplar board skin is the same as example 1. Only changing the cooking liquor ratio of the Soda/AQ cooking stage II to be 1: 4, other processes are unchanged. The content of alpha-cellulose in the obtained poplar board skin acetified-grade dissolving pulp is 97%, the content of pentosan is 2.5%, the polymerization degree is 1060, the whiteness is 90% ISO, the ash content is 0.01%, the content of DCM extract is 0.02%, and the acetification reaction value (PV value) is 730.
The poplar board skin acetification grade dissolving pulp has good detection indexes and can be used for producing high-grade cellulose acetate products.
Example 5:
Soda/AQ staged cooking-O added with auxiliary agentPQDEpP-enzyme synergistic process for treating poplar board skin raw material, the collected poplar board skin is the same as example 1. The addition of the auxiliary agent in the step is removed by prehydrolysis, the liquid ratio is 1:6, and other processes are the same as those in the example 1. The content of alpha-cellulose in the obtained poplar board skin acetified-grade dissolving pulp is 95%, the content of pentosan is 3.6%, the polymerization degree is 1200, the whiteness is 88% ISO, the ash content is 0.015%, the content of DCM extract is 0.025%, and the acetification reaction value (PV value) is 680.
Example 6:
pre-hydrolysis with addition of auxiliary agent-Soda/AQ staged cooking with addition of auxiliary agent-OPQDEpP-enzyme synergistic process for treating poplar board skin raw material, the collected poplar board skin is the same as example 1. Combining the two-stage cooking in the steps (2) and (3) into one-stage cooking, and adding alkali, magnesium hydroxide, sodium sulfite and AQ into the two-stage cooking at one time, wherein the liquid ratio is 1:6, the Tmax is =100 +/-2 ℃, and the heat preservation time is 60 minutes; then, the temperature was maintained at 160 ℃ for 120 minutes, and the other processes were the same as in example 1. The content of alpha-cellulose in the obtained poplar board skin acetified-grade dissolving pulp is 96%, the content of pentosan is 2.7%, the polymerization degree is 1000, the whiteness is 89% ISO, the ash content is 0.01%, the content of DCM extract is 0.02%, and the acetification reaction value (PV value) is 700.
The above embodiments are preferred embodiments of the present invention, but the present invention is not limited to the embodiments, and any other changes, modifications, combinations, substitutions and simplifications which do not depart from the spirit and principle of the present invention should be construed as equivalents and are included in the scope of the present invention.

Claims (2)

1. A method for producing acetified-grade dissolving pulp by using poplar slabs is characterized by comprising the following steps:
(1) adding an auxiliary agent for prehydrolysis: the liquid ratio is 1:6, the addition amount of a hydrolysis auxiliary agent is 0.4 percent of the mass of the dry substance of the poplar board skin, the hydrolysis temperature is 160 ℃, the heat preservation time is 60 minutes, and the hydrolysis auxiliary agent is a mixture obtained by mixing sodium borate, magnesium sulfate, nonylphenol polyoxyethylene ether phosphate and tetrasodium iminodisuccinate according to the mass ratio of 1:1:1: 1;
(2) in the first stage of Soda/AQ cooking, the alkali consumption is 5 percent of the mass of the oven dry pulp, the liquid ratio is 1: 4, the magnesium hydroxide consumption is 0.5 percent of the mass of the oven dry pulp, the sodium sulfite consumption is 5.0 percent of the mass of the oven dry pulp, the AQ consumption is 0.05 percent of the mass of the oven dry pulp, the Tmax =100 +/-2 ℃, and the heat preservation time is 60 minutes;
(3) Soda/AQ cooking II stage: the alkali consumption is 18 percent of the mass of the oven-dried pulp, the magnesium hydroxide consumption is 0.5 percent of the mass of the oven-dried pulp, the sodium sulfite consumption is 3.0 percent of the mass of the oven-dried pulp, the liquid ratio is 1:7, the AQ consumption is 0.05 percent of the mass of the oven-dried pulp, the highest temperature is 160 ℃, and the heat preservation time is 120 minutes;
（4）OPDQEPp bleaching of OPThe oxygen pressure of bleaching is 0.5MPa, the pulp concentration is 10 percent, and MgSO4The dosage of the sodium hydroxide is 0.6 percent of the mass of the oven-dry pulp, the dosage of the NaOH is 2.0 percent of the mass of the oven-dry pulp, and the dosage of the sodium hydroxide is H2O2The dosage is 1.0 percent of the mass of the oven-dried pulp, the temperature is 95 ℃, and the temperature is kept for 60 min; qDThe bleaching process has the reaction time of 60 minutes, T =30 +/-2 ℃, the pulp concentration is 4.0 percent, the pH =1.5, the using amount of sodium chlorite is 3.0 percent of the mass of the oven-dried pulp, and the using amount of IDS is 0.05 percent of the mass of the oven-dried pulp; reaction time of Ep extraction process is 90min, MgSO4The dosage of the sodium hydroxide is 0.5 percent of the mass of the oven-dry pulp, the dosage of the NaOH is 3.0 percent of the mass of the oven-dry pulp, and the dosage of the sodium hydroxide is H2O2The dosage is 2.0 percent of the mass of the oven-dried pulp, the dosage of IDS is 0.05 percent of the mass of the oven-dried pulp, the pulp concentration is 8 percent, and the temperature is 85 ℃; reaction time of P bleaching 120min, MgSO4The dosage of the sodium hydroxide is 0.5 percent of the mass of the oven-dry pulp, the dosage of the NaOH is 0.4 percent of the mass of the oven-dry pulp, the dosage of the NaAC is 0.4 percent of the mass of the oven-dry pulp, and the H content is2O2The dosage is 3.0 percent of the mass of the oven-dried pulp, the pulp concentration is 10 percent, and the temperature is 90 ℃;
(5) enzyme synergistic treatment: the pulp concentration is 5%, the temperature is 40 ℃, the treatment time is 60min, the pH is =5.0, the dosage of polyaspartic acid is 0.05% of the mass of the oven-dry pulp, the dosage of OP-13 is 0.005% of the mass of the oven-dry pulp, the dosage of OP-15 is 0.005% of the mass of the oven-dry pulp, the dosage of cellulose incision enzyme is 0.2IU/gpulp, the dosage of xylanase is 3XU/gpulp, and the dosage of pectinase is 3 IU/gpulp.
2. The method according to claim 1, wherein the poplar board used in the step (1) has a length of 10 to 30mm, a pentosan content of 22.3 to 24.3%, and an α -cellulose content of 43.0 to 45.0%.
CN201811228170.XA 2018-10-22 2018-10-22 Method for producing acetified-grade dissolving pulp by using poplar slabs Expired - Fee Related CN109403115B (en)

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Application Number Priority Date Filing Date Title
CN201811228170.XA CN109403115B (en) 2018-10-22 2018-10-22 Method for producing acetified-grade dissolving pulp by using poplar slabs
PCT/CN2018/114525 WO2020082427A1 (en) 2018-10-22 2018-11-08 Method for using poplar bark to produce acetylation-grade dissolving pulp
US16/314,319 US20200173103A1 (en) 2018-10-22 2018-11-08 Method for producing acetate grade dissolving pulp from poplar residual slabs
BE20195709A BE1026675B1 (en) 2018-10-22 2019-10-17 PROCESS FOR THE PRODUCTION OF ACETATE QUALITY DISSOLVING PASTE FROM RESIDUAL POPLAR SLABS

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CN109403115B true CN109403115B (en) 2020-12-29

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