CN103952798B - Glue fiber acid bath low temperature evaporation and continuous crystallization process and device thereof - Google Patents
Glue fiber acid bath low temperature evaporation and continuous crystallization process and device thereof Download PDFInfo
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- CN103952798B CN103952798B CN201410178997.XA CN201410178997A CN103952798B CN 103952798 B CN103952798 B CN 103952798B CN 201410178997 A CN201410178997 A CN 201410178997A CN 103952798 B CN103952798 B CN 103952798B
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- 239000002253 acid Substances 0.000 title claims abstract description 74
- 238000001704 evaporation Methods 0.000 title claims abstract description 54
- 238000002425 crystallisation Methods 0.000 title claims abstract description 33
- 230000005712 crystallization Effects 0.000 title claims abstract description 33
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000003292 glue Substances 0.000 title abstract description 5
- 239000000835 fiber Substances 0.000 title abstract description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 52
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 229920000297 Rayon Polymers 0.000 claims description 28
- 238000007906 compression Methods 0.000 claims description 20
- PMZURENOXWZQFD-UHFFFAOYSA-L na2so4 Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 17
- 238000002156 mixing Methods 0.000 claims description 15
- 239000012452 mother liquor Substances 0.000 claims description 13
- 238000007599 discharging Methods 0.000 claims description 10
- 238000009987 spinning Methods 0.000 claims description 9
- 238000009835 boiling Methods 0.000 claims description 4
- 239000010446 mirabilite Substances 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 239000006210 lotion Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 4
- 239000000498 cooling water Substances 0.000 description 3
- 229910052938 sodium sulfate Inorganic materials 0.000 description 3
- 235000011152 sodium sulphate Nutrition 0.000 description 3
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 229920000742 Cotton Polymers 0.000 description 1
- NWONKYPBYAMBJT-UHFFFAOYSA-L Zinc sulfate Chemical compound [Zn+2].[O-]S([O-])(=O)=O NWONKYPBYAMBJT-UHFFFAOYSA-L 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 230000001112 coagulant Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000007380 fibre production Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 238000011068 load Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000001502 supplementation Effects 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 229960001763 zinc sulfate Drugs 0.000 description 1
- 229910000368 zinc sulfate Inorganic materials 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/50—Manufacturing or production processes characterised by the final manufactured product
- Y02P70/62—Manufacturing or production processes characterised by the final manufactured product related technologies for production or treatment of textile or flexible materials or products thereof, including footwear
Abstract
The invention discloses a glue fiber acid bath low temperature evaporation and continuous crystallization process and a device of the process. The process comprises an acid bath to be evaporated, an acid bath middle bucket, a conveying pump, a preheater, a heat exchanger A, an evaporator, a steam compressor, a heat exchanger A, a heat exchanger B, a discharge pump, a crystal pulp tank and a centrifuge, wherein the output of the acid bath middle bucket to be evaporated and crystallized is connected with the steam preheater through the conveying pump the condensed water preheater; the output of the steam preheater is connected with an evaporation crystallizer and the heat exchanger B through the heat exchanger A; the evaporation crystallizer and the heat exchanger B are in serial connection; the output of the evaporation crystallizer is connected with the crystal pulp tank through the discharge pump; the output of the crystal pulp tank is connected with a separator; the output of the separator is connected with a mother liquid tank. The energy is greatly saved; moreover as the evaporation and the crystallization are integrated, stable evaporation and continuous crystallization are achieved; meanwhile the whole set of the equipment is compact and reliable, the civil engineering investment is saved, small space is occupied, the number of operators needed is small, the operation is stable and reliable, and the whole system can be under configuration control and is highly automatic.
Description
Technical field
The present invention relates to a kind of viscose acid bath low-temperature evaporation and continuous crystallisation technique and device thereof.
Background technology
Viscose is regenerated celulose fibre, it take native cellulose as raw material, spin after the process of series of physical chemical process and form, viscose is similar to natural cotton fiber, there is good hygroscopicity, gas permeability, dyeability, antistatic, comfortable and easy to wear, that synthetic fiber cannot be compared, its textiles deeply by consumers in general like that commercially there is stronger competitiveness.Viscose is since suitability for industrialized production, and along with the development, perfect of viscose technology and green technology, viscose output constantly increased with the speedup of more than 10% in recent years, and domestic viscose production capacity is more than 3,500,000 tons so far.
The production of viscose, first be stoste workshop material pulp through leaching namely, squeezing, pulverize, experienced, yellow, dissolving, filtration, make qualified viscose glue after the operation such as deaeration, viscose glue is solidification forming in acid bath, and after the drawing-off of spinning machine and scouring machine post processing, drying machine drying, viscose is made in packing.Acid station continuously supplies a certain amount of department meeting technological requirement to spinning machine specially, coagulating bath or spinning bath are named again in acid bath, acid bath is the solution with sulfuric acid, sodium sulphate, zinc sulfate preparation, the main task at acid station is formed constant acid bath, continuously flow to spinning machine at a certain temperature, to guarantee that normal operation is produced in spinning, whether the composition of acid bath and temperature stabilization and transparency have very important impact to viscose quality.A certain amount of water and sodium sulphate to be generated at fiber forming process, be back to sulfuric acid concentration in the body lotion at acid station to reduce, must be a part of by the moisture evaporation in backflow acid bath, in acid bath after evaporation, sodium sulfate concentration raises, sulfate crystal in acid bath should be separated out a part, therefore, the evaporation of acid bath and crystallization are the vital tasks at acid station.
Along with the continuous expansion of viscose production capacity, the technology of viscose and equipment equipment are also in continuous progress, production capacity as viscose staple fibre production line single line is increased to 50,000 tons/year even 100,000 tons/year by 0.5 ten thousand tons/year, acid station acid bath evaporation mode also even 14 imitates evaporation by single effect evaporation to 11 effects, evaporability also increases to 25 tons/hour by singly overlapping 10 tons/hour, evaporation efficiency improves greatly, and evaporation liquid to steam ratio reaches 1:0.27 ~ 0.33.
Viscose industry generally adopts efficient 11 effect flash distillation plant and continuous crystallizing systems at present.Evaporating principle: body lotion is injected into vaporific under vacuum conditions, utilizes self liberated heat through decompression cooling, the part moisture content in body lotion is evaporated, thus reaches concentrated body lotion and energy-conservation object.Technological process: filter qualified body lotion and enter the flash liberation of horizontal-type evaporator V10 section after flowmeter metering, enter V11 section again and continue degassed evaporation, then A8 ~ A1 preheating is delivered to by circulating pump, flash distillation is sprayed finally by entering V1V2 after A0 and H heating, enter V3 ~ V9 again to evaporate further, obtain qualified concentrated body lotion, overflow back acid bath mixing channel through liquid bath.The steam produced in V1V2 and V3 ~ V8, for pre-heater A1 ~ A8, carries out preheating to the body lotion passed through, and meanwhile, self is condensed into condensed water and gets rid of; The thermal source of A0 and H is fresh saturated vapor; The evaporation vapour produced in evaporimeter V9 ~ V11 is inhaled in mixing condenser MK1, MK2, and this cooling water of cooling water-cooled can be recycled after treatment.The exhaust of this device enters the second condenser HK through steam jet pump respectively by each blast pipe, cooled water condensation, then aspirated by water ring vacuum pump further and enter air through blast pipe or remove emission-control equipment.The advantage of 11 effect flash distillations: due to body lotion when explosive evaporation be not outer come heat source, but the damp and hot heat required when supplying evaporation utilizing self, and the process of flash heating is carried out step by step respectively in the vaporization chamber of series connection at different levels, cascade raising temperature, make full use of temperature difference, maximally utilise heat, thus save heat energy.Weak point: (1) acid bath is through 11 effect vaporising devices, and moisture is condensed into water and discharges after being inhaled into mixing condenser MK1, MK2 by the evaporated vapor produced in evaporimeter V9 ~ V11, still have certain heat energy not to be fully utilized in evaporated vapor;
(2) evaporated vapor is condensed into water also needs a large amount of cooling water, needs to consume a large amount of power; (3) higher to vacuum level requirements, generally want Water-ring vacuum to add steam-jet vacuum pump and just can reach requirement;
(4) package unit tank body is many, and volume is comparatively large, and pipeline is complicated, and floor space is larger;
(5) owing to will overcome the overboard problem of condensation that vacuum is brought, overcome acceleration of gravity, package unit is installed should higher than drain gully 9.8M, and the building cost of device is higher;
(6) pipeline is complicated, and the Controlling vertex such as valve are many, and maintenance load is larger.
Summary of the invention
Its object of the present invention is just to provide a kind of viscose acid bath low-temperature evaporation and continuous crystallisation technique and device thereof, dramatically saves on the energy, and evaporation and crystallization integration, achieve steady-state evaporation and continuous crystallisation, outfit is reliably compact simultaneously, saves construction investment, floor space is little, operating personnel are few, operate more reliable and more stable, total system can make Combining soft control, increasingly automated.
Realize above-mentioned purpose and the technical scheme taked is:
A kind of viscose acid bath low-temperature evaporation and continuous crystallisation technique, the acid solution of crystallization to be evaporated in bucket in the middle of acid bath is sent into A heat exchanger by feeding engine after steam preheater, and enter crystallizing evaporator, under vacuum conditions, acid bath is evaporated with low boiling, the steam of evaporation enters the steam-water mixing body that vapour compression machine is compressed into high enthalpy, steam-water mixing body enters A heat exchanger, B heat exchanger, by the chuck of heat exchanger, acid bath is heated, acid bath is heated through circulating pump and is evaporated between A heat exchanger---crystallizing evaporator---B heat exchanger, the steam evaporated enters vapour compression machine compression again, steam-water mixing body after compression condenses into water and is collected into condensate water pot in heat exchanger chuck, now condensed water still has uniform temperature, with pump, condensed water is delivered to condensed water preheater to preheat acid bath liquid to be evaporated, part acid bath liquid in crystallizing evaporator after evaporation then pumps to magma tank by discharging, and isolate saltcake and mother liquor through seperator, mother liquor is for preparing new spinning acid bath, and saltcake then produces glauber salt further, carries out so continuously evaporating and crystallization.
The device of a kind of viscose acid bath low-temperature evaporation and continuous crystallisation technique, comprise the middle bucket of acid bath of crystallization to be evaporated, in the middle of acid bath, bucket exports and connects steam preheater through feeding engine, condensed water preheater, described steam preheater exports and connects crystallizing evaporator and B heat exchanger through A heat exchanger, crystallizing evaporator and B heat exchanger are for being connected in series, crystallizing evaporator exports and connects magma tank through discharging pump, and magma tank exports and connects seperator, and seperator exports and connects mother liquor tank; Described crystallizing evaporator vacuum port connects vavuum pump through vacuum cooler, crystallizing evaporator steam (vapor) outlet connects the steam inlet of A heat exchanger and B heat exchanger through vapour compression machine, A heat exchanger is connected condensate pump with the condensation-water drain of B heat exchanger through condensate water pot, and condensate pump output connects condensed water preheater; Circulating pump is connected in series between described A heat exchanger input and B heat exchanger output.
Compared with prior art the present invention has the following advantages.
This technique and device thereof can utilize steam completely, do not lose steam thermal energy, need a small amount of coming into being except steam except device starts, and are in operation without the need to supplementing nascent steam again; Evaporating temperature is low to moderate 50 ~ 60 DEG C, and evaporation efficiency is 30 times of tradition evaporation; Do not need cooling water, therefore greatly saved energy consumption, evaporating one ton of water only needs power consumption 50KWH.Generally use with existing viscose glue factory 11 imitate compared with flash evaporation technology, greatly save the energy; And evaporation and crystallization can integrations, realize steady-state evaporation and continuous crystallisation, simultaneously outfit is reliably compact, saving construction investment.Floor space is little, operating personnel are few; Supporting public work project is few; Operate more reliable and more stable, total system can make Combining soft control, increasingly automated.
Accompanying drawing explanation
Below in conjunction with accompanying drawing, the invention will be further described.
Fig. 1 is this technique and apparatus structure principle schematic thereof.
Detailed description of the invention
Viscose acid bath low-temperature evaporation and continuous crystallisation technique, as shown in Figure 1, the acid solution of crystallization to be evaporated in bucket 1 in the middle of acid bath is sent into A heat exchanger 6 by feeding engine 2 after steam preheater 20, and enter crystallizing evaporator 11, under vacuum conditions, acid bath is evaporated with low boiling, the steam of evaporation enters the steam-water mixing body that vapour compression machine 12 is compressed into high enthalpy, steam-water mixing body enters A heat exchanger 6, B heat exchanger 5, by the chuck of heat exchanger, acid bath is heated, acid bath is heated through circulating pump 7 and is evaporated between A heat exchanger 6---crystallizing evaporator 11---B heat exchanger 5, the steam evaporated again enters vapour compression machine 12 and compresses, steam-water mixing body after compression condenses into water and is collected into condensate water pot 8 in heat exchanger chuck, now condensed water still has uniform temperature, with pump, condensed water is delivered to condensed water preheater 3 to preheat acid bath liquid to be evaporated, part acid bath liquid in crystallizing evaporator 11 after evaporation then goes out to magma tank 17 by discharging pump 16, and isolate saltcake and mother liquor through seperator 18, mother liquor is for preparing new spinning acid bath, and saltcake then produces glauber salt further, carries out so continuously evaporating and crystallization.
The device of viscose acid bath low-temperature evaporation and continuous crystallisation technique, comprise the middle bucket 1 of acid bath of crystallization to be evaporated, in the middle of acid bath, bucket 1 exports and connects steam preheater 20 through feeding engine 2, condensed water preheater 3, as shown in Figure 1, described steam preheater 20 exports and connects crystallizing evaporator 11 and B heat exchanger 5 through A heat exchanger 6, crystallizing evaporator 11 and B heat exchanger 5 are for being connected in series, crystallizing evaporator 11 exports and connects magma tank 17 through discharging pump 16, magma tank 17 exports and connects seperator 18, and seperator 18 exports and connects mother liquor tank; Described crystallizing evaporator 11 vacuum port a connects vavuum pump 15 through vacuum cooler 14, crystallizing evaporator 11 steam (vapor) outlet b connects the steam inlet c of A heat exchanger 6 and B heat exchanger 5 through vapour compression machine 12, A heat exchanger 6 is connected condensate pump 9 with the condensation-water drain d of B heat exchanger 5 through condensate water pot 8, and condensate pump 9 output connects condensed water preheater 3; Circulating pump 7 is connected in series between described A heat exchanger 6 input and B heat exchanger 5 output.
Described condensate pump 9 output connects vapour compression machine 12 through spray pump 10, spray cooler 13.
Be provided with overflow launder 19 between described seperator 18 output and mother liquor tank, described magma tank overfall e connects overflow launder 19.
The pipeline rake ratio that described discharging pump 16 connects magma tank 17 is 10%.
Operation principle
This technique and device thereof comprise evaporation and crystallization two processes, as shown in Figure 1, its path is acid bath---acid bath middle bucket---feeding engine---pre-heater---heat exchanger A---evaporimeter---vapour compression machine---A heat exchanger, B heat exchanger---discharging pump---magma tank---centrifuge to be evaporated.
The acid solution of crystallization to be evaporated in bucket 1 in the middle of acid bath is sent into A heat exchanger 6 by feeding engine 2 after steam preheater 20, and enter crystallizing evaporator 11, under vacuum conditions, acid bath is evaporated with low boiling, the steam of evaporation enters the steam-water mixing body that vapour compression machine 12 is compressed into high enthalpy, steam-water mixing body enters A heat exchanger 6, B heat exchanger 5, by the chuck of heat exchanger, acid bath is heated, acid bath is heated through circulating pump 7 and is evaporated between A heat exchanger 6---crystallizing evaporator 11---B heat exchanger 5, the steam evaporated again enters vapour compression machine 12 and compresses, steam-water mixing body after compression condenses into water and is collected into condensate water pot 8 in heat exchanger chuck, now condensed water still has uniform temperature, with pump, condensed water is delivered to condensed water preheater 3 to preheat acid bath liquid to be evaporated, part acid bath liquid in crystallizing evaporator 11 after evaporation then goes out to magma tank 17 by discharging pump 16, and isolate saltcake and mother liquor through seperator 18, mother liquor is for preparing new spinning acid bath, and saltcake then produces glauber salt further, so carry out continuously evaporating and crystallization.
Claims (5)
1. a viscose acid bath low-temperature evaporation and continuous crystallisation technique, it is characterized in that, the acid solution of crystallization to be evaporated in bucket (1) in the middle of acid bath is sent into A heat exchanger (6) by feeding engine (2) after steam preheater (20), and enter crystallizing evaporator (11), under vacuum conditions, acid bath is evaporated with low boiling, the steam of evaporation enters the steam-water mixing body that vapour compression machine (12) is compressed into high enthalpy, steam-water mixing body enters A heat exchanger (6), B heat exchanger (5), by the chuck of heat exchanger, acid bath is heated, acid bath is heated through circulating pump (7) and is evaporated between A heat exchanger (6)---crystallizing evaporator (11)---B heat exchanger (5), the steam evaporated enters vapour compression machine (12) compression again, steam-water mixing body after compression condenses into water and is collected into condensate water pot (8) in heat exchanger chuck, now condensed water still has uniform temperature, with pump, condensed water is delivered to condensed water preheater (3) to preheat acid bath liquid to be evaporated, part acid bath liquid in crystallizing evaporator (11) after evaporation then goes out to magma tank (17) by discharging pump (16), saltcake and mother liquor is isolated through seperator (18), mother liquor is for preparing new spinning acid bath, and saltcake then produces glauber salt further, carries out so continuously evaporating and crystallization.
2. the device of a kind of viscose acid bath low-temperature evaporation according to claim 1 and continuous crystallisation technique, comprise the middle bucket (1) of acid bath of crystallization to be evaporated, in the middle of acid bath, bucket (1) exports through feeding engine (2), condensed water preheater (3) connects steam preheater (20), it is characterized in that, described steam preheater (20) exports and connects crystallizing evaporator (11) and B heat exchanger (5) through A heat exchanger (6), crystallizing evaporator (11) and B heat exchanger (5) are for being connected in series, crystallizing evaporator (11) exports and connects magma tank (17) through discharging pump (16), magma tank (17) exports and connects seperator (18), seperator (18) exports and connects mother liquor tank, described crystallizing evaporator (11) vacuum port (a) connects vavuum pump (15) through vacuum cooler (14), crystallizing evaporator (11) steam (vapor) outlet (b) connects the steam inlet (c) of A heat exchanger (6) and B heat exchanger (5) through vapour compression machine (12), A heat exchanger (6) is connected condensate pump (9) with the condensation-water drain (d) of B heat exchanger (5) through condensate water pot (8), and condensate pump (9) output connects condensed water preheater (3), circulating pump (7) is connected in series between described A heat exchanger (6) input and B heat exchanger (5) output.
3. the device of a kind of viscose acid bath low-temperature evaporation according to claim 2 and continuous crystallisation technique, is characterized in that, described condensate pump (9) output connects vapour compression machine (12) through spray pump (10), spray cooler (13).
4. the device of a kind of viscose acid bath low-temperature evaporation according to claim 2 and continuous crystallisation technique, it is characterized in that, described seperator (18) is provided with overflow launder (19) between output and mother liquor tank, described magma tank overfall (e) connects overflow launder (19).
5. the device of a kind of viscose acid bath low-temperature evaporation according to claim 2 and continuous crystallisation technique, is characterized in that, the pipeline rake ratio that described discharging pump (16) connects magma tank (17) is 10%.
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| CN201410178997.XA CN103952798B (en) | 2014-04-30 | 2014-04-30 | Glue fiber acid bath low temperature evaporation and continuous crystallization process and device thereof |
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| CN201410178997.XA CN103952798B (en) | 2014-04-30 | 2014-04-30 | Glue fiber acid bath low temperature evaporation and continuous crystallization process and device thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104499067B (en) * | 2014-12-16 | 2017-01-18 | 许达人 | Plate type preheater for acid bath, flash evaporation device of plate type preheater for acid bath and alkaline cleaning process |
| CN111921221B (en) * | 2020-07-31 | 2022-06-21 | 北京神州瑞霖环境技术研究院有限公司 | System for removing reflux part and double-evaporation crystallization of acid bath discharge liquid and application |
| CN111870991B (en) * | 2020-07-31 | 2022-02-25 | 北京神州瑞霖环境技术研究院有限公司 | Heating evaporation crystallization system for reflux removal part of spinning bath discharge liquid and application |
| CN113233478A (en) * | 2021-04-20 | 2021-08-10 | 潍坊金鑫化工化纤设备技术开发中心 | Method for extracting high-purity sodium sulfate crystals from high-wet-modulus fiber coagulation bath |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1070961A (en) * | 1992-09-28 | 1993-04-14 | 潍坊化学纤维厂 | Utilize the technology of acid bath evaporation indirect steam manufactured goods acid |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| JPH0134083B2 (en) * | 1985-03-13 | 1989-07-18 | Kimura Kakoki Co Ltd | |
| CN102168326B (en) * | 2011-03-24 | 2012-08-22 | 南通三圣石墨设备科技股份有限公司 | Efficient and energy-saving flash evaporation method for viscose acid bath system and special device |
| CN102641607A (en) * | 2012-03-11 | 2012-08-22 | 甘肃蓝科石化高新装备股份有限公司 | Vaporization crystallizer device with mechanical vapor compressor |
| CN203425552U (en) * | 2013-07-24 | 2014-02-12 | 深圳市捷晶能源科技有限公司 | Concentration and crystallization equipment for sodium sulfite |
| CN203807618U (en) * | 2014-04-30 | 2014-09-03 | 九江恒生化纤有限公司 | Device for acid bath low-temperature evaporation and continuous crystallization of viscose |
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2014
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1070961A (en) * | 1992-09-28 | 1993-04-14 | 潍坊化学纤维厂 | Utilize the technology of acid bath evaporation indirect steam manufactured goods acid |
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Address after: 332017, Hang Seng Chemical Fiber Co., Ltd., 18 Bailu Avenue, Gushan Town, Mount Lu District, Jiangxi, Jiujiang Applicant after: JIUJIANG HENGSHENG CHEMICAL FIBER CO., LTD. Address before: 332017, Hang Seng Chemical Fiber Co., Ltd., 18 Bailu Avenue, Gushan Town, Mount Lu District, Jiangxi, Jiujiang Applicant before: JIUJIANG HENGSHENG CHEMICAL FIBER CO., LTD. |
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Free format text: CORRECT: APPLICANT; FROM: JIUJIANG HENGSHENG CHEMICAL FIBER LTD. TO: JIUJIANG HENGSHENG CHEMICAL FIBER CO., LTD. |
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