CN102251423A - Continuous displacement and digestion process for dissolving pulp - Google Patents
Continuous displacement and digestion process for dissolving pulp Download PDFInfo
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- CN102251423A CN102251423A CN2011102137166A CN201110213716A CN102251423A CN 102251423 A CN102251423 A CN 102251423A CN 2011102137166 A CN2011102137166 A CN 2011102137166A CN 201110213716 A CN201110213716 A CN 201110213716A CN 102251423 A CN102251423 A CN 102251423A
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- 238000006073 displacement reaction Methods 0.000 title claims abstract description 124
- 238000000034 method Methods 0.000 title claims abstract description 46
- 230000008569 process Effects 0.000 title claims abstract description 37
- 229920000875 Dissolving pulp Polymers 0.000 title claims abstract description 28
- 230000029087 digestion Effects 0.000 title abstract description 20
- 239000002253 acid Substances 0.000 claims abstract description 71
- 239000003513 alkali Substances 0.000 claims abstract description 20
- 238000006386 neutralization reaction Methods 0.000 claims abstract description 11
- 238000005516 engineering process Methods 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 110
- 238000010411 cooking Methods 0.000 claims description 93
- 238000009835 boiling Methods 0.000 claims description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 19
- 230000008676 import Effects 0.000 claims description 18
- 238000005406 washing Methods 0.000 claims description 17
- 238000006243 chemical reaction Methods 0.000 claims description 15
- 238000009413 insulation Methods 0.000 claims description 15
- 238000003860 storage Methods 0.000 claims description 15
- 239000000243 solution Substances 0.000 claims description 14
- 230000007062 hydrolysis Effects 0.000 claims description 13
- 238000006460 hydrolysis reaction Methods 0.000 claims description 13
- 239000002002 slurry Substances 0.000 claims description 11
- 239000000706 filtrate Substances 0.000 claims description 10
- 238000010438 heat treatment Methods 0.000 claims description 9
- 238000010790 dilution Methods 0.000 claims description 7
- 239000012895 dilution Substances 0.000 claims description 7
- 230000014759 maintenance of location Effects 0.000 claims description 6
- 238000010792 warming Methods 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 5
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- 238000005086 pumping Methods 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 150000003839 salts Chemical class 0.000 claims description 3
- 239000002994 raw material Substances 0.000 abstract description 11
- 239000000126 substance Substances 0.000 abstract description 6
- 239000000835 fiber Substances 0.000 abstract description 5
- 102100030386 Granzyme A Human genes 0.000 description 11
- 101001009599 Homo sapiens Granzyme A Proteins 0.000 description 11
- 238000004061 bleaching Methods 0.000 description 6
- 229920002488 Hemicellulose Polymers 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 229920005610 lignin Polymers 0.000 description 5
- 235000017166 Bambusa arundinacea Nutrition 0.000 description 4
- 235000017491 Bambusa tulda Nutrition 0.000 description 4
- 241001330002 Bambuseae Species 0.000 description 4
- 235000015334 Phyllostachys viridis Nutrition 0.000 description 4
- 239000011425 bamboo Substances 0.000 description 4
- 238000004537 pulping Methods 0.000 description 4
- 229920001131 Pulp (paper) Polymers 0.000 description 3
- 229920000297 Rayon Polymers 0.000 description 2
- 238000005903 acid hydrolysis reaction Methods 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 229920002678 cellulose Polymers 0.000 description 2
- 239000001913 cellulose Substances 0.000 description 2
- 239000012467 final product Substances 0.000 description 2
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000004321 preservation Methods 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- 230000021736 acetylation Effects 0.000 description 1
- 238000006640 acetylation reaction Methods 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 150000004676 glycans Chemical class 0.000 description 1
- 230000003301 hydrolyzing effect Effects 0.000 description 1
- 238000005580 one pot reaction Methods 0.000 description 1
- 238000011017 operating method Methods 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 230000020477 pH reduction Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000011122 softwood Substances 0.000 description 1
- 235000014347 soups Nutrition 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000010902 straw Substances 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
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Abstract
The invention relates to a continuous displacement and digestion process for dissolving pulp. By adopting the traditional vertical pot digestion equipment and combining a continuous digestion technology, a fiber raw material is prepared into the dissolving pulp (chemical fiber pulp), and the purposes of saving energy, protecting the environment, improving the yield and the quality and reducing the consumption are fulfilled. A plurality of digestion pots are adopted in the digestion process for the dissolving pulp, the digestion solution outlet of each digestion pot is directly communicated with the digestion solution displacement outlet of other each digestion pot through a pipeline, and random two or more digestion pots form closed circular connection; during working, the same process conditions are set in the digestion process of each digestion pot from filling completion to pot feeding, and three periods of displacement time of all the digestion pots are set to be the same; and by adjusting the time interval between the digestion pots, the displacement time is superposed, namely at least two pots are in the process of acid displacement, neutralization displacement or alkali reclamation displacement in the displacement time, the displacement time is superposed and continuous displacement is performed at the time superposition point.
Description
Technical field
The present invention relates to the continuous replacing and digesting technoloy of a kind of dissolving pulp, is to adopt traditional vertically digesting equipment, in conjunction with the continuously cooking technology, makes fibrous raw material make dissolving pulp (chemical fibre slurry), and reaches the purpose of energy-saving and environmental protection, raising output and quality, reduction consumption.Belong to textile industry pulping technique field.
Background technology
The main raw material(s) of producing viscose is linter pulp and dissolving pulp, in recent years because factors such as sown areas of cotton minimizings, the linter pulp increment seldom, so dissolving pulp becomes the unique raw material sources that increase viscose.Dissolving pulp is through purer wood pulp, straw pulp behind bleaching, the extraction organic solvent etc.It has removed lignin, hemicellulose through acidolysis, keeps chemical cellulose.
Domestic present dissolving pulp manufacturing enterprise more than 90% still adopts single pot of mode boiling of tradition, earlier under low temperature environment, adorn pot, be incubated when utilizing thermal source that digester is heated to 170 ℃, after the H factor (temperature and time relative reaction rate in the digestion process) reaches requirement, promptly the slurries in the digester can be discharged, finish the boiling of one pot of paper pulp.Just can carry out the production of next pot because this mode need be got rid of cooking liquor when cooking liquor reaches 170 ℃, cause the huge waste of heat energy.The steam consumption of tradition vertically digesting is (4～4.5t vapour/t slurry) approximately; The omnidistance cycle of boiling dissolving pulp long (18-20 hour/pot).
In the eighties in last century, the Radar company of Sweden and U.S. Beloit company have developed a kind of boiling method cooperatively, with the hot black liquor collection storage in the digester, and its heat energy of reuse in next digester cycle then.
Similarly boiling mainly contains following three kinds of methods at present:
1, the quick displacement cooking method of RDH.
2, the super batch cooking method of SuperBatch.
3, DDS displacement cooking method.
The patent of RDH belongs to U.S. GLV company, and the patent of SuperBatch belongs to Finland Metso company, and the patent of DDS belongs to U.S. CPL company.The technology similar in China still is in blank.
The basic principle of these methods is identical, wherein with DDS cooking effect the best, generally be that a plurality of digesters are linked together by the pipeline circulation, the pipeline between adjacent two digesters is provided with reservoir, and the volume of 1 reservoir needs 3 times of digester capacity.The cooking liquor that reservoir inside groove storage temperature is lower, the cooking liquor that the water jacket storage temperature is higher.But be to use grooving, when the big build-up of pressure of the unbalanced or inside and outside liquid storage amount of external and internal pressure difference can cause groove to be damaged by pressure or flatten.
This technology has reduced energy consumption, contain remaining chemicals in the liquid of circulation, increased the selectivity of cooking reaction, can remove (boiling is to lower card valency) to more lignin in the raw material and increase the intensity of fiber, reduced removal amount, be easy to bleaching at the bleachery lignin.
Though this mode has effectively been saved heat energy,, big volume reservoir all is set between each digester, can cause area of mill site bigger, equipment investment is higher.
Summary of the invention
The purpose of this invention is to provide the continuous replacing and digesting technoloy of a kind of dissolving pulp, energy-conservation and can eliminate when putting pot waste gas to the pollution of environment.
Solution of the present invention is characterized in that, described method is: a plurality of digesters are in different operations respectively, during work, set the sour time swap t2 of all digesters, in to reclaim time swap t9 all identical with time swap t5 and alkali, adjust the zero-time between each digester, make each time swap overlap; When to digesting technoloy when the time, coincide point began to replace, open the cooking liquor import and the cooking liquor outlet of each pot that needs displacement simultaneously, and with the headstock gear of cooking liquor reservoir, make the digester of each displacement send into liquid that needs and the equal cooking liquor of the total amount that displaces simultaneously, reach continuous displacement; After displacement is finished, close each headstock gear simultaneously, enter subsequent handling, wait for time swap next time.
Particularly, adopt a plurality of digesters with cooking liquor import, cooking liquor outlet, each pot has and overlaps the independently cooking liquor circulatory system, each digester inputs or outputs to liquid storage by on-off structure control cooking liquor liquid storage independently and irritates, each digester is connected with the cooking liquor heater, each digester bottom is provided with the slurry outlet, it is characterized in that: the cooking liquor outlet of each digester all directly communicates by the cooking liquor displacement import of each digester of pipeline and other, and any two or more digesters all form closed circulation and connect;
Described reservoir is the hot acid liquid bath; Hot black liquor; Hot water storgae; Cold white liquid bath; White liquid bath of heat and dilution liquid bath.The volume of each reservoir is 1.5-2 a times of digester.Each digester is connected with heater, and each digester bottom is provided with the slurry outlet.Each pot has and overlaps the independently cooking liquor circulatory system, uses in normal boiling.
For energy savings consumption, described cooking liquor liquid storage (black liquor of High Temperature High Pressure) is by heat exchanger heating white liquid or running water, cooking liquor liquid storage after the heat exchange enters liquid storage and irritates, hot water is then delivered to other by hot-water line and need be used with the place of hot water, carry out the pulp washing operation in the pulp washing operation behind the digesting technoloy as it being delivered to, to make full use of the energy.
The technology of a digester cycle is as follows:
(1) pot filling: send into hot water more than 95 ℃ in the time of the dress pot, the limit charging, the limit liquor charging, until pot is filled, this moment, kettle temperature was T1;
(2) acid displacement: with hot water V
1With hot acid liquid V
2Digester bottom input from filling displaces hydrolyzate V from the top
3Deliver to reservoir; This boiling kettle temperature is warming up to T2 from T1; Time swap t2;
(3) hydrolysis heats up: feed steam and be warming up to T3, t3 consuming time heats up;
(4) hydrolysis insulation: temperature T 4=T3, temperature retention time t4;
(5) neutralization displacement: the white liquid V of heat that elder generation sends here from the white liquid bath of heat
4Rapidly and acid solution; Subsequently respectively with hot black liquor V
5The heat white liquid V additional with needs
6From the input of digester bottom, displace hot acid liquid V from the top
7, make the boiling kettle temperature reduce to T5, time swap t5;
The hot acid liquid V that displaces
7Send into another digester that needs hot acid liquid or hot acid liquid bath;
The neutralizer V that displaces
8Send evaporation section, reclaim salt;
The hot black liquor V of the pH that displaces 〉=7
9Enter the hot black liquor groove;
(6) neutralization insulation: holding temperature T6=T5, temperature retention time t6;
(7) soda boiling heats up: directly be heated to T7 through heater with steam, heat time heating time t7;
(8) soda boiling insulation: temperature T 8=T7, soda boiling time t8;
(9) alkali reclaims displacement: after cooking reaction reaches terminal point, and pulp washing filtrate V
10Send into the digester bottom, the top displaces the hot black liquor V more than 160 ℃
11, warm black liquor V
12To comprehensive groove; Replace to the end kettle temperature and reduce to T9 below 100 ℃ by T8; T9 during time swap;
(10) put pot: 80 ℃ of rare black liquor of dilution pumping are extracted out with pulp pump and are sent spraying pot to, and the temperature t 10 when putting pot is lower than 95 ℃, put to be lower than 80 ℃ after pot is finished, and can load pot, and a pot time t10 is put in the operation boiling that next time circulates;
During work, the digesting technoloy of setting each digester is accomplished to from filling and sets identical process conditions before putting pot, and it is all identical to set 3 time swaps of all digesters: t2=t5=t9; Adjust the time interval between each digester, make time swap overlap, promptly have at least two pots to be in operation 2 acid displacements, the operation 5 and displacement or operation 9 alkali recovery displacement, and time swap overlaps at time swap;
When to when the time, coincide point began to replace, open the cooking liquor import and the cooking liquor outlet of each pot that needs displacement simultaneously, and with the headstock gear of cooking liquor reservoir, make the digester of each displacement send into liquid that needs and the equal cooking liquor of the total amount that displaces simultaneously, reach continuous displacement; After displacement is finished, close each headstock gear simultaneously, enter subsequent handling, wait for time swap next time.
An embodiment of the invention are:
T1＝60℃-70℃；t1＝30-90min；
T2＝150-155℃；t2＝25-40min；
T4＝T3＝170-175℃，t3＝20-30min；t4＝120-240min；
T6＝T5＝150-160℃，t5＝20-40min，t6＝2-30min；
T8＝T7＝165℃-175℃，t7＝20-40min；t8＝30-90min；
Below T9=100 ℃, t9=20-40min;
T10 is lower than 95 ℃, t15-20min.
Further, during displacement
V
1+ V
2Remaining space=V in the-pot
3
V
4+V
5+V
6＝V
7+V
8+V
9；
V
10＝V
11+V
12。
Wherein, the V that displaces of operation 9
11Promptly as V
5Send in the pot of operation 5, rest parts is sent into the hot black liquor groove; The V that displaces in the operation 5
7Promptly as V
2Send in the pot of operation 2, rest parts is sent into the hot acid liquid bath, and each conveyance conduit is by the flowmeter autocontrol valve.
As preferably: in each digester, have 3 pots to overlap simultaneously, realize a pair of two displacements in 2,5,9 times of operation.
Such as, adopt 4 digester A, B, C, D, wherein each displacement has three pots to replace continuously, and another pot is in holding stage:
When the A pot is in the initial of operation 2 acid displacement, the B pot is in the operation 5 and displacement initial, and the C pot is in cooking reaction and reaches terminal point, and operation 9 alkali reclaim the initial of displacement, and the D pot is in other operation;
Open corresponding valve simultaneously, make the C pot bottom import pulp washing filtrate V
10, the hot black liquor V more than 160 ℃ that the top displaces
11As V
5Directly send into the B pot bottom, rest parts is sent into the hot black liquor groove, warm black liquor V
12Deliver to comprehensive groove;
160 ℃ of-170 ℃ of hot acid liquid V that B pot top displaces
6, V wherein
2From A pot bottom input A pot, the hydrolyzate V that A pot top displaces
3Enter reservoir;
After time swap reached, valve-off finished the displacement of A pot operation 2, B pot operation 5, C pot operation 9 simultaneously, and up to replace next time: the A pot reaches operation 5, and the B pot reaches operation 9, and the D pot reaches operation 2, carried out above-mentioned similarly displacement simultaneously ... the rest may be inferred.
Another embodiment of the present invention: in each digester, have 2 pots to overlap simultaneously, realize displacement one to one in operation 2,5.Such as: adopt 4 digester A, B, C, D,
When the A pot is in the initial of operation 2 acid displacement, the B pot is in the operation 5 and displacement initial, and C pot D pot is in other operation; Open corresponding valve simultaneously, the hot black liquor that makes the hot black liquor groove is sent into the operation 5 of carrying out the B pot and displacement from the B pot bottom, the hot acid liquid V that B pot top displaces
6From the operation 2 acid displacements of A pot bottom input carrying out A pot, the hydrolyzate V that A pot top displaces
3Enter reservoir; After time swap reached, valve-off finished A pot operation 2, B pot operation 5 simultaneously, up to displacement next time.
Another embodiment of the present invention: in each digester, have 2 pots to overlap simultaneously, realize displacement one to one in operation 5,9.Such as: adopt 4 digester A, B, C, D, when the A pot is in the initial of operation 5, the B pot is in the initial of operation 9, and C pot D pot is in other operation; Then open corresponding valve simultaneously, make the B pot bottom import pulp washing filtrate, the hot black liquor V that the top displaces
11Directly send into the A pot bottom, carry out in the operation 5 of A pot and displacement, the hot acid liquid V that A pot top displaces
7Enter the hot acid liquid bath; After time swap reached, valve-off reclaimed displacement with displacement, B pot operation 9 alkali in the operation 5 of end A pot, up to displacement next time simultaneously.
In the above-mentioned embodiment,, then should send into corresponding storage tank by the cooking liquor that this pot that breaks down receives in the replacing process continuously if there is a certain pot to break down.
The present invention is applicable to various timber, bamboo raw material, and raw material is not had specific (special) requirements; Can change raw material variety at any time; Can steaming mixed different raw material; Can distinguish the boiling different material simultaneously mixes behind same hardness or different hardness again.Only need to make compound above-mentioned permutizer condition get final product according to the concrete technological parameter of actual conditions adjustment.
Advantage of the present invention is:
1, effectively utilizes boiling heat energy, save steam: decoction system is a process of utilizing the contained heat energy of cooking liquor to replace heating and heat exchange, steam directly feeds in the circulation fluid to be warming up to maximum temperature, the efficient height, heating-up time is short, therefore effectively saved the consumption of steam, the ton slurry steam consumption can reach the 1.5-2 ton, saves steam more than 65% than traditional batch boiling;
2, put pot temperature below 100 ℃, do not have traditional boiling to put the foul smell and the waste gas of pot process, eliminate atmosphere pollution;
3, improve dissolving pulp yield 1-3%, increase output,, hydrolytic acidification time is shortened because the restored acid hydrolyzate has been used in hydrolysis;
4, the heat energy of digestion process generation makes full use of by continuous displacement, and reaction condition is evenly gentle, and the boiling maximum temperature only needs 160～170 ℃, therefore can keep a cellulose more, fully removes the hemicellulose lignin, makes the yield raising of dissolving pulp, and output increases;
5, reduce Kappa number, because liquid filling stage acid solution helps the stripping of hemicellulose in the acidic hydrolysis process; Excess base is used in soda boiling, does not give lignin condensation chance, and Kappa number is reduced, and improves the dissolving pulp quality:
6, the bleaching chemical consumption reduces, reduced discharge of wastewater load and wastewater flow rate: because Kappa number reduces, the required effective chlorine dose of bleaching is reduced, the consumption of bleaching medicine reduces, simultaneously also reduce bleaching effluent amount and pollutional load, saved the wastewater treatment expense;
7, the dissolving pulp quality is even: be full of liquid displacement from bottom to up, carry out big liquor ratio boiling, and alkali lye and uniformity of temperature profile, the dissolving pulp quality that boiling is come out is even;
8, continuous replacing and digesting technoloy has concurrently intermittently and the characteristics of continuously cooking, makes the flow process of continuous displacement cooking simple, and operating procedure is simplified, so the investment of grassroot project is low; Because make full use of the equipment of traditional batch boiling, newly added equipment is few, when existing chemical fibre factory was undergone technological transformation, cost of investment was lower;
9, strong to various fibrous raw material adaptability, also can be used for paper making pulps boiling and corncob hydrolysis and produce furfural.
Description of drawings
Fig. 1 is the system architecture schematic diagram.
Be labeled as among Fig. 1: cooking liquor import 1, cooking liquor outlet 2, cooking liquor dress pot inlet 3, slurry outlet 4, the white liquid bath 5 of heat, cooking liquor reservoir 6, hot cooking liquor reservoir 7, white liquid heat exchanger 8, cold white liquid pipe 9, the white liquid pipe 10 of heat, running water heat exchanger 11, running water pipe 12, hot-water line 13, gases at high pressure pipeline 14, dilution reservoir 15, pulp washing section dilution intake line 16, spraying pot 17, cold white liquid bath 18, hot water storgae 19, cooking liquor heater 20.
Fig. 2 represents the process conditions curve of 1 pot.
Fig. 3 represents a plurality of pots process conditions curve (4 pots), and many are in different time (abscissa), the curve of same process condition, (curve shape is identical, the position difference).
Fig. 4 represents a plurality of pots process conditions curve, and many are in different time (abscissa), the curve of same process condition, (curve shape is identical, the position difference).
Fig. 5 represents a plurality of pots process conditions curve, and many are in different time (abscissa), the curve of same process condition, (curve shape is identical, the position difference).
Fig. 6 represents a plurality of pots process conditions curve, and many are in different time (abscissa), the curve of same process condition, (curve shape is identical, the position difference).
Fig. 7 represents a plurality of pots process conditions curve, and many are in different time (abscissa), the curve of same process condition, (curve shape is identical, the position difference).
Fig. 8 represents the relation of the bamboo pulp digester yield and the H factor.
The specific embodiment
The inventive method comprises a plurality of cooking liquor displacement imports 1 that have, cooking liquor displacement outlet 2 is adorned pot digester of inlet 3 with cooking liquor, described each digester is connected with cooking liquor heater 20, each digester bottom is provided with slurry outlet 4, the cooking liquor displacement outlet 2 of described each digester all directly communicates by the cooking liquor displacement import 1 of each digester of pipeline and other, and the cooking liquor of each digester displacement outlet 2 all is connected with same cooking liquor reservoir 6 by pipeline, and cooking liquor reservoir 6 communicates with the cooking liquor dress pot inlet 3 of each digester by pipeline.Among Fig. 1, digester is four pots of A, B, C, D among the figure, certainly, also can be provided with more; In addition, the cooking liquor displacement outlet 2 of each digester described in the present embodiment all directly communicates by the cooking liquor displacement import 1 of each digester of pipeline and other, be meant directly connection between the digester, and the groove of liquid storage need be set between per two digesters.
During work, set identical process conditions of each digester and program.10 operations following (digester cycle):
1, pot filling:
Send into hot water more than 95 ℃ in the time of the dress pot, limit charging (bamboo chip or other are treated the boiling material), the limit liquor charging, until pot is filled, this moment, kettle temperature was T1=60 ℃-70 ℃.The present invention adorns pot and also can adopt from lower acid solution of the temperature that displaces of other pot or the warm acid solution in the reservoir, a dress pot time t1=30-90min.
2, acid displacement:
With V
1The hot acid liquid V of hot water (135 ℃) and 160 ℃-170 ℃
2Digester bottom input (for prehydrolysis provides acid condition, prehydrolysis being carried out fast) from filling displaces hydrolyzate V from the top
3Deliver to reservoir, can be used for loading other pot.This boiling kettle temperature is warming up to T2=150-155 ℃ from T1=60 ℃-70 ℃.Time swap t2=25-40min; Wherein, V
1+ V
2=V
3
In the prehydrolysis process, the acetate that is discharged by the acetylation glycan makes the pH value of hydrolyzate drop to 3～4, thereby causes the hydrolysis of hemicellulose, and hemicellulose is separated from raw material.
3, hydrolysis heats up
Follow-up temperature of continuing rising (feeding steam heats up) is finished in displacement, and to T3=170-175 ℃, t3=20-30min consuming time heats up.
4, hydrolysis (circulation) insulation: temperature T 4=T3=170-175 ℃, temperature retention time t4=120-240min;
During heating and heat preservation, circulating pump is released the pre-hydrolyzed solution in the digester, and the top and the bottom by digester after directly heating with steam through heater enter in the pot, circulate.
5, neutralization displacement:
When the prehydrolysis reaction reaches P factor control (end) point of expection, the V that elder generation sends here from the white liquid bath of heat
4The white liquid (150-155 ℃) of heat rapidly in and acid solution; Subsequently respectively with 160-170 ℃ hot black liquor V
5The heat white liquid V additional with needs
6(145 ℃-150 ℃) displace V from the input of digester bottom from the top
7160 ℃-170 ℃ of hot acid liquid make the boiling kettle temperature reduce to T5=150-160 ℃, time swap t5=20-40min,
The hot acid liquid V that displaces
7Can send into another digester that needs hot acid liquid or hot acid liquid bath.V
7Unnecessary part is sent into the hot acid liquid bath to send into another digester that needs hot acid liquid.
The neutralizer V that displaces
8(being in the critical pH=7 of soda acid) send evaporation section, reclaims salt.
The hot black liquor V of the pH that displaces 〉=7
9Enter the hot black liquor groove.
6, neutralization insulation (further neutralization reaction, and make alkali lye infiltrate through in the tablet)
Acid solution with in the alkali and displacement finish after temperature T 6=T5=150-160 ℃, temperature retention time t6=20-30min;
7, soda boiling heats up
Circulating pump is released the cooking liquor in the digester, directly heats the back through heater with steam and is entered in the pot by the top and the bottom of digester, circulates, and reaches T7=165 ℃-175 ℃, heat time heating time t7=20-40min.
8, soda boiling insulation: T8=T7=165 ℃-175 ℃, soda boiling time t8=30-90min;
Released from the cooking liquor in the digester by circulating pump, the process heater enters a pot interior circulation soda boiling with the direct hot digestion liquid of steam, heating back by the top and the bottom of digester.
The soda boiling emphasis is according to the H factor control of setting.The H factor is that boiling temperature and digestion time are combined into parameter of moral in the pulping digestion process.
A and B flavor constant in the formula, constant A=E/R, E are delignification reaction activation energy, R is a gas constant.On the basis of big quantitative determination activation energy, get E=32000 card/gram molecule, then A=16113.T is an absolute temperature, reaction rate K is 1 when supposing 100 ℃ (373K), can calculate the reaction rate constant K of different temperatures correspondence.
According to the H factor=average relative reaction rate * time interval, calculate the H factor.Utilize H factor control boiling end under certain condition, thereby stablize pulping quality and yield.
Among the present invention, the bamboo pulp H factor is controlled at 600-800; If adopt softwood pulp, the H factor is controlled at 800-1200.Because under the certain situation of alkali charge, the too high meeting of the H factor sharply descends yield, the pulping quality is affected; And the H factor is crossed low can causing and is cooked phenomenon rawly, slag rate height, and screened yield descends.
9, alkali reclaims displacement:
When cooking reaction reaches control (end) point of expection, about 80 ℃ pulp washing filtrate V from pulp washing
10Send into the digester bottom, the top displaces the hot black liquor V more than 160 ℃
11, the warm black liquor V about 135 ℃
12To comprehensive groove, a part is replenished liquid as next digester cycle, and another part carries out alkali and reclaims; Replace to the end kettle temperature and reduce to T9 (below 100 ℃), wait for and put pot by T8=165-175 ℃.
T9=20-40min during time swap.
Replacement amount is pressed the 100-110% of digester capacity.V
10＝V
11+V
12。
10, put pot:
Extract out with pulp pump through the paper pulp of pulp washing filtrate cooling and to send spraying pot to, the temperature t 10 when putting pot is lower than 95 ℃, puts to be lower than 80 ℃ after pot is finished, and can load pot, and a pot time t15-20min is put in the operation boiling that next time circulates.
During work, a plurality of digesters are in different operations respectively.Such as being example, certainly, also more digesters can be set with A, B, four digesters of C, D.The time (150min) of A, B, four pots of difference of C, D fixed interval, each pot is accomplished to from filling and puts the identical process conditions of the preceding setting of pot, as Fig. 2.Certainly, in order further to simplify the operation, the filling operation also can be identical with the process conditions of putting pot operation.
Fig. 2 represents the process conditions curve of 1 pot.
Fig. 3 represents a plurality of pots process conditions curve (4 pots, a pair of two replacing process), and 4 are in different time (abscissa), the curve of same process condition, (curve shape is identical, the position difference).
As can be seen from Figure 3, the acid of each pot displacement operation 2, neutralization displacement operation 5, alkali reclaim the identical time swap of displacement operation 9, i.e. t2=t5=t9.
There are 3 pots to be in operation 2,5,9 simultaneously.
When to the time coincide point, when needing displacement, open the cooking liquor displacement import and the cooking liquor displacement outlet of each pot that needs displacement simultaneously, and with cooking liquor reservoir (hot acid liquid bath; Hot black liquor; Hot water storgae; Cold white liquid bath; White liquid bath of heat or dilution liquid bath) headstock gear, the total amount that makes each pot send into digester equates with the total amount that displaces:
V
1+ V
2Remaining space=V in the-pot
3
V
4+V
5+V
6＝V
7+V
8+V
9；
V
10＝V
11+V
12。
Wherein, the V of operation 9
11Promptly as V
5Send in the pot of operation 5, rest parts is sent into the hot black liquor groove; V in the operation 5
7Promptly as V
2Send in the pot of operation 2, rest parts is sent into the hot acid liquid bath.Each conveyance conduit is by the flowmeter autocontrol valve.
After displacement is finished, close a headstock gear, enter subsequent handling, wait for time swap next time.
A pair of two displacements(have three pots can realize continuous displacement in four pots, a pot is replaced continuously to two other pot):
When the A pot is in the initial of operation 2, the B pot is in the initial of operation 5, and the C pot is in cooking reaction and reaches terminal point, and operation 9 initial, the D pot is in other operation (such as acid hydrolysis insulation operation).Then open corresponding valve simultaneously, make the C pot bottom import pulp washing filtrate V
10, the hot black liquor V more than 160 ℃ that the top displaces
11=V
5Directly send into the B pot bottom, carry out the operation 5 of B pot; Warm black liquor V about 135 ℃
12To comprehensive groove;
160 ℃ of-170 ℃ of hot acid liquid V that B pot top displaces
6, V wherein
2Part is carried out the operation 2 of A pot, the hydrolyzate V that A pot top displaces from A pot bottom input A pot
3Enter reservoir.
After time swap reached (t2=t5=t9), valve-off finished the displacement of A pot operation 2, B pot operation 5, C pot operation 9 simultaneously, and up to replace next time: the A pot reaches operation 5, and the B pot reaches operation 9, and the D pot reaches operation 2, carried out above-mentioned similarly displacement simultaneously.The rest may be inferred carries out a pair of two displacements.
Certainly,, can not realize continuous circulation, also can have between two pots and carry out continuous cyclic permutation if certain pot breaks down.Two pots overlapped in the time of operation 2,5,9, and being in operation 2 such as a pot, to have another pot to be in operation 5 when initial initial, or pot is in operation 5, and to have another pot to be in operation 9 when initial initial.Should send into corresponding storage tank by the cooking liquor that the pot that breaks down receives gets final product.
Displacement one to one: such as: when the A pot is in the initial of operation 2, the B pot is in the initial of operation 5, and C pot D pot is in other operation.Then open corresponding valve simultaneously, hot black liquor is sent into the B pot bottom, and the hot acid liquid that B pot top displaces carries out the operation 2 that A crosses from the input of A pot bottom, and the filling liquid that A pot top displaces enters reservoir.C pot, D pot were replaced when another time replaced continuously.Or
Displacement one to one: such as: when the A pot is in the initial of operation 5, the B pot is in the initial of operation 9, and C pot D pot is in other operation.Then open corresponding valve simultaneously, make the B pot bottom import pulp washing filtrate, the hot black liquor that the top displaces is directly sent into the A pot bottom, carries out the operation 5 of A pot, and the hot acid liquid that A pot top displaces enters the hot acid liquid bath.C pot, D pot were replaced when another time replaced continuously.
In the above-described embodiment, white liquid in the white liquid bath 5 of described heat can heat by ad hoc heater, but for energy savings consumption, the cooking liquor displacement outlet 2 of each digester and the pipeline between the cooking liquor reservoir 6 are provided with white liquid heat exchanger 8, described white liquid heat exchanger 8 also is connected with cold white liquid pipe 9 and the white liquid pipe 10 of heat, and the white liquid pipe 10 of heat is connected between white liquid heat exchanger 8 and the white liquid bath 5 of heat.Mention in the embodiment of front, when carrying out the cooking liquor displacement, one of them digester need be put cooking liquor to cooking liquor reservoir 6, at this moment, this cooking liquor white liquid heat exchanger 8 of flowing through, cold white liquid carries out heat exchange from cold white liquid bath 18 through the cold white liquid pipe 9 white liquid heat exchanger 8 of also flowing through, after the heat exchange, cooking liquor still flow in the cooking liquor reservoir 6, the white liquid of heat after the heat exchange then flow in the white liquid bath 5 of heat by the white liquid pipe 10 of heat, utilize the heat energy dialogue liquid of cooking liquor to heat well, saved the energy.
In the above-described embodiment, owing to only need use the heat of seldom a part of cooking liquor to the heat exchange of cold white liquid, and in order to make full use of this heat, also be provided with running water heat exchanger 11 on the cooking liquor displacement outlet 2 of each digester and the pipeline between the cooking liquor reservoir 6, described running water heat exchanger 11 is arranged in parallel with white liquid heat exchanger 8, and running water heat exchanger 11 also is connected with running water pipe 12 and hot-water line 13.Cold water is from running water pipe 12 running water heat exchanger 11 heat exchange of flowing through, cooking liquor after the heat exchange flow in the cooking liquor reservoir 6, hot water is then delivered to hot water storgae 19 by hot-water line 13 and is stored, delivering to other again need use with the place of hot water, carries out the pulp washing operation as it being delivered in the pulp washing operation behind the digesting technoloy.
For ease of putting the pot operation, be connected with gases at high pressure pipeline 14 at each digester top.When needs are put pot, in digester, feed gases at high pressure by gases at high pressure pipeline 14, thereby also can well the slurries in the digester be discharged.
A pair of two displacements of 1 four digesters of embodiment
Whole digester cycle has 10 operations:
Replacement amount
Concrete steps are as follows:
1, B pot dress pot
Start dress pot blower fan, the dress pot is sent into 52.5m from hot water storgae simultaneously
3Hot water (95 ℃) or acid solution (solid-liquid volume ratio 1: 2.5) are until pot is filled.Close the pot cover valve, start the soup circulating pump, begin circulation, kettle temperature is 65-70 ℃ and waits for intensification.
Illustrate: 1. over dry tablet 35t;
2. tablet moisture 50%. is with water 35m
3
3. replenish hot water 52.5m
3
The pot in remaining space 52.5m
3
2, B pot acid solution displacement
The dress pot is finished, and the B pot self is played circulation (as Fig. 1), sends into 135 ℃ of hot water 82m earlier from hot water storgae then
3, send into 82m from the hot acid liquid bath or from the hot acid liquid (160 ℃-170 ℃) of C pot then
3, displace 111.5m from the pot top simultaneously
3Hydrolyzate (mixed liquor of filling liquid, warm acid solution, the hot acid liquid) processing of anhydrating (or deliver to the A pot and load).The B pot self was played circulation after displacement was finished, and at this moment kettle temperature is 145 ℃-150 ℃.Wait for and continue to heat up.
Illustrate:
1, adds displacement hot water amount 82m
3
2, add displacement acid solution amount 82m
3
3, discharging the hydrolysis liquid measure is 82+82-52.5 (remaining space in the pot)=111.5m
3
3, B pot hydrolysis heating and heat preservation
Earlier kettle temperature is added to 170 ℃ by the digester steam heater.
4, B pot hydrolysis circulation insulation
Be incubated 240 minutes.
5, acid neutralization displacement
After hydrolysis reaches terminal point (being incubated 240 minutes), send 145 ℃-150 ℃ 20m here from the white liquid bath of heat
3The white liquid of heat rapidly in and acid solution.
Respectively from 160-165 ℃ of hot black liquor 112m from the C pot
3And 48m
3The white liquid of heat is sent into the B pot, replaces the interior 130m that takes the dish out of the pot from B pot top
3(contain 10m
3Condensed water) 160 ℃ of-170 ℃ of hot acid liquid (set amount is the boundary with PH＜7).82 (m in the hot acid liquid
3) enter the A pot and carry out acid displacement, the remaining hot acid liquid bath that automatically switches to.
Be in the critical neutralizer 34m of soda acid
3Enter comprehensive groove after evaporation section is sent in heat exchange.
The hot black liquor 26m of all the other PH 〉=7
3Enter the hot black liquor groove.Kettle temperature was 145 ℃-150 ℃ after displacement was finished.
6, neutralization insulation
Insulation 20min.
7, soda boiling heats up
In soda boiling heats up, send into 145 ℃-150 ℃ white liquid 32m of heat
3, displace 145 ℃ of-150 ℃ of hot black liquor 32m
3Send into the hot black liquor groove.
Illustrate: sending into total white liquid measure is 100m
3: in the operation 5 and when displacement add the white liquid V4 (20m of heat
3), the white liquid V6 (48m of heat
3), soda boiling heats up and adds 32 (m
3).
8, soda boiling insulation
Insulation 120min.Do recovery after waiting for the soda boiling terminal point.
9, alkali reclaims displacement
When cooking reaction reaches terminal point, send 80 ℃ of rare black liquor 180m from accumulator tank (from rare black liquor of pulp washing)
3Deliver to digester.Displace the 112m more than 160 ℃
3(contain 10m
3Condensed water) (setting value) hot black liquor is delivered to the A pot and is carried out alkali displacement or deliver to hot black liquor groove, the warm black liquor 68m below 135 ℃
3To comprehensive groove, last kettle temperature drops to below 100 ℃, waits for and puts pot.
10, put pot
By 80 ℃ of rare black liquor 116.2m of dilution pumping
3To the B pot, start and put a pot pump and take out slurry and send into spraying pot.
Rare black liquor of sending in the pot is 116.2m
3
Claims (10)
1. the continuous replacing and digesting technoloy of dissolving pulp, adopt a plurality of digesters, it is characterized in that: a plurality of digesters are in different operations respectively, during work, set the sour time swap t2 of all digesters, in to reclaim time swap t9 all identical with time swap t5 and alkali, adjust the zero-time between each digester, make each time swap overlap; When to digesting technoloy when the time, coincide point began to replace, open the cooking liquor import and the cooking liquor outlet of each pot that needs displacement simultaneously, and with the headstock gear of cooking liquor reservoir, make the digester of each displacement send into liquid that needs and the equal cooking liquor of the total amount that displaces simultaneously, reach continuous displacement; After displacement is finished, close each headstock gear simultaneously, enter subsequent handling, wait for time swap next time.
2. the continuous replacing and digesting technoloy of dissolving pulp according to claim 1, it is characterized in that: adopt a plurality of cooking liquor imports that have, the digester of cooking liquor outlet, each pot has and overlaps the independently cooking liquor circulatory system, each digester inputs or outputs to liquid storage by on-off structure control cooking liquor liquid storage independently and irritates, each digester is connected with the cooking liquor heater, each digester bottom is provided with the slurry outlet, it is characterized in that: the cooking liquor outlet of each digester all directly communicates by the cooking liquor swap-in mouth of each digester of pipeline and other, and any two or more digesters all form closed circulation and connect;
The technology of a digester cycle is as follows:
(1) pot filling: send into hot water more than 95 ℃ in the time of the dress pot, the limit charging, the limit liquor charging, until pot is filled, this moment, kettle temperature was T1;
(2) acid displacement: with hot water V
1With hot acid liquid V
2Digester bottom input from filling displaces hydrolyzate V from the top
3Deliver to reservoir; This boiling kettle temperature is warming up to T2 from T1; Time swap t2;
(3) hydrolysis heats up: feed steam and be warming up to T3, t3 consuming time heats up;
(4) hydrolysis insulation: temperature T 4=T3, temperature retention time t4;
(5) neutralization displacement: the white liquid V of heat that elder generation sends here from the white liquid bath of heat
4Rapidly and acid solution; Subsequently respectively with hot black liquor V
5The heat white liquid V additional with needs
6From the input of digester bottom, displace hot acid liquid V from the top
7, make the boiling kettle temperature reduce to T5, time swap t5;
The hot acid liquid V that displaces
7Send into another digester that needs hot acid liquid or hot acid liquid bath;
The neutralizer V that displaces
8Send evaporation section, reclaim salt;
The hot black liquor V of the pH that displaces 〉=7
9Enter the hot black liquor groove;
(6) neutralization insulation: holding temperature T6=T5, temperature retention time t6;
(7) soda boiling heats up: directly be heated to T7 through heater with steam, heat time heating time t7;
(8) soda boiling insulation: temperature T 8=T7, soda boiling time t8;
(9) alkali reclaims displacement: after cooking reaction reaches terminal point, and pulp washing filtrate V
10Send into the digester bottom, the top displaces the hot black liquor V more than 160 ℃
11, warm black liquor V
12To comprehensive groove; Replace to the end kettle temperature and reduce to T9 below 100 ℃ by T8; T9 during time swap;
(10) put pot: 80 ℃ of rare black liquor of dilution pumping are extracted out with pulp pump and are sent spraying pot to, and the temperature t 10 when putting pot is lower than 95 ℃, put to be lower than 80 ℃ after pot is finished, and can load pot, and a pot time t10 is put in the operation boiling that next time circulates;
During work, the digesting technoloy of setting each digester is accomplished to from filling and sets identical process conditions before putting pot, and it is all identical to set 3 time swaps of all digesters: t2=t5=t9; Adjust the time interval between each digester, make time swap overlap, promptly have at least two pots to be in operation 2 acid displacements, the operation 5 and displacement or operation 9 alkali recovery displacement, and time swap overlaps at time swap;
When to when the time, coincide point began to replace, open the cooking liquor import and the cooking liquor outlet of each pot that needs displacement simultaneously, and with the headstock gear of cooking liquor reservoir, make the digester of each displacement send into liquid that needs and the equal cooking liquor of the total amount that displaces simultaneously, reach continuous displacement; After displacement is finished, close each headstock gear simultaneously, enter subsequent handling, wait for time swap next time.
3. the continuous replacing and digesting technoloy of dissolving pulp according to claim 2 is characterized in that:
T1＝60℃-70℃；t1＝30-90min；
T2＝150-155℃；t2＝25-40min；
T4＝T3＝170-175℃，t3＝20-30min；t4＝120-240min；
T6＝T5＝150-160℃，t5＝20-40min，t6＝2-30min；
T8＝T7＝165℃-175℃，t7＝20-40min；t8＝30-90min；
Below T9=100 ℃, t9=20-40min;
T10 is lower than 95 ℃, t15-20min;
During displacement, replacement amount is as follows in each digester:
V
1+ V
2Remaining space=V in the-pot
3
V
4+V
5+V
6＝V
7+V
8+V
9；
V
10＝V
11+V
12；
Wherein, the V that displaces of operation 9
11Promptly as V
5Send in the pot of operation 5, rest parts is sent into the hot black liquor groove; The V that displaces in the operation 5
7Promptly as V
2Send in the pot of operation 2, rest parts is sent into the hot acid liquid bath, and each conveyance conduit is by the flowmeter autocontrol valve.
4. the continuous replacing and digesting technoloy of dissolving pulp according to claim 1 is characterized in that: in each digester, have 3 pots to overlap in 2,5,9 times of operation simultaneously, realize a pair of two displacements.
5. the continuous replacing and digesting technoloy of dissolving pulp according to claim 4 is characterized in that: adopt 4 digester A, B, C, D, wherein each displacement has three pots to replace continuously, and another pot is in holding stage:
When the A pot is in the initial of operation 2 acid displacement, the B pot is in the operation 5 and displacement initial, and the C pot is in cooking reaction and reaches terminal point, and operation 9 alkali reclaim the initial of displacement, and the D pot is in other operation;
Open corresponding valve simultaneously, make the C pot bottom import pulp washing filtrate V
10, the hot black liquor V more than 160 ℃ that the top displaces
11As V
5Directly send into the B pot bottom, rest parts is sent into the hot black liquor groove, warm black liquor V
12Deliver to comprehensive groove;
160 ℃ of-170 ℃ of hot acid liquid V that B pot top displaces
6, V wherein
2From A pot bottom input A pot, the hydrolyzate V that A pot top displaces
3Enter reservoir;
After time swap reached, valve-off finished the displacement of A pot operation 2, B pot operation 5, C pot operation 9 simultaneously, and up to replace next time: the A pot reaches operation 5, and the B pot reaches operation 9, and the D pot reaches operation 2, carried out above-mentioned similarly displacement simultaneously ... the rest may be inferred.
6. the continuous replacing and digesting technoloy of dissolving pulp according to claim 1 is characterized in that: in each digester, have 2 pots to overlap in operation 2,5 simultaneously, realize displacement one to one.
7. the continuous replacing and digesting technoloy of dissolving pulp according to claim 6 is characterized in that: adopt 4 digester A, B, C, D,
When the A pot is in the initial of operation 2 acid displacement, the B pot is in the operation 5 and displacement initial, and C pot D pot is in other operation; Open corresponding valve simultaneously, the hot black liquor that makes the hot black liquor groove is sent into the operation 5 of carrying out the B pot and displacement from the B pot bottom, the hot acid liquid V that B pot top displaces
6From the operation 2 acid displacements of A pot bottom input carrying out A pot, the hydrolyzate V that A pot top displaces
3Enter reservoir; After time swap reached, valve-off finished A pot operation 2, B pot operation 5 simultaneously, up to displacement next time.
8. the continuous replacing and digesting technoloy of dissolving pulp according to claim 1 is characterized in that: in each digester, have 2 pots to overlap in operation 5,9 simultaneously, realize displacement one to one.
9. the continuous replacing and digesting technoloy of dissolving pulp according to claim 8 is characterized in that: adopt 4 digester A, B, C, D,
When the A pot is in the initial of operation 5, the B pot is in the initial of operation 9, and C pot D pot is in other operation; Then open corresponding valve simultaneously, make the B pot bottom import pulp washing filtrate, the hot black liquor V that the top displaces
11Directly send into the A pot bottom, carry out in the operation 5 of A pot and displacement, the hot acid liquid V that A pot top displaces
7Enter the hot acid liquid bath; After time swap reached, valve-off reclaimed displacement with displacement, B pot operation 9 alkali in the operation 5 of end A pot, up to displacement next time simultaneously.
10. according to the continuous replacing and digesting technoloy of each described dissolving pulp of claim 4-9, it is characterized in that:, then should send into corresponding storage tank by the cooking liquor that this pot that breaks down receives in the replacing process continuously if there is a certain pot to break down.
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|---|---|---|---|
| CN 201110213716 CN102251423B (en) | 2011-07-28 | 2011-07-28 | Continuous displacement and digestion process for dissolving pulp |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103264037A (en) * | 2013-04-16 | 2013-08-28 | 浙江布莱蒙农业科技股份有限公司 | Treatment process of livestock died of epidemic diseases |
| CN114736176A (en) * | 2022-05-19 | 2022-07-12 | 中国科学院广州能源研究所 | A kind of method for preparing furfural from agricultural and forestry waste |
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| US4849052A (en) * | 1983-08-24 | 1989-07-18 | Beloit Corporation | Batch digester multi-stage pulping process |
| CN1094108A (en) * | 1992-12-02 | 1994-10-26 | 沃斯特-阿尔潘工业技术公司 | A kind of method of making dissolving pulp |
| WO1997038156A1 (en) * | 1996-04-04 | 1997-10-16 | Impco-Voest-Alpine Pulping Technologies Gmbh | Process for continuously supplying liquid during the boiling of cellulose in a boiler |
| CN102127877A (en) * | 2010-12-28 | 2011-07-20 | 宜宾竹海竹资源科技有限责任公司 | Production process of bamboo-dissolving pulp |
-
2011
- 2011-07-28 CN CN 201110213716 patent/CN102251423B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4849052A (en) * | 1983-08-24 | 1989-07-18 | Beloit Corporation | Batch digester multi-stage pulping process |
| CN1094108A (en) * | 1992-12-02 | 1994-10-26 | 沃斯特-阿尔潘工业技术公司 | A kind of method of making dissolving pulp |
| WO1997038156A1 (en) * | 1996-04-04 | 1997-10-16 | Impco-Voest-Alpine Pulping Technologies Gmbh | Process for continuously supplying liquid during the boiling of cellulose in a boiler |
| CN102127877A (en) * | 2010-12-28 | 2011-07-20 | 宜宾竹海竹资源科技有限责任公司 | Production process of bamboo-dissolving pulp |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103264037A (en) * | 2013-04-16 | 2013-08-28 | 浙江布莱蒙农业科技股份有限公司 | Treatment process of livestock died of epidemic diseases |
| CN103264037B (en) * | 2013-04-16 | 2015-06-17 | 浙江布莱蒙农业科技股份有限公司 | Treatment process of livestock died of epidemic diseases |
| CN114736176A (en) * | 2022-05-19 | 2022-07-12 | 中国科学院广州能源研究所 | A kind of method for preparing furfural from agricultural and forestry waste |
| CN114736176B (en) * | 2022-05-19 | 2023-06-06 | 中国科学院广州能源研究所 | A method for preparing furfural from agricultural and forestry waste |
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Owner name: SHANGHAI HAICHENG CHEMICAL TECHNOLOGY CO., LTD. Free format text: FORMER OWNER: GUANGZHOU HAISUM ENERGY TECHNOLOGY CO., LTD. Effective date: 20141218 |
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Effective date of registration: 20141218 Address after: 162650 the Inner Mongolia Autonomous Region Hulun Buir city Zhalantun voeren Paper Street alley No. 11 Zheng Patentee after: Qu Chuanwu Patentee after: SHANGHAI HAISUM CHEMICAL TECHNOLOGY CO., LTD. Address before: 162650 the Inner Mongolia Autonomous Region Hulun Buir city Zhalantun voeren Paper Street alley No. 11 Zheng Patentee before: Qu Chuanwu Patentee before: Guangzhou Haicheng Energy Technology Co., Ltd. |
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