CN111803995A - Natural evaporation crystallization system for acid bath discharge liquid reflux removal part and application - Google Patents
Natural evaporation crystallization system for acid bath discharge liquid reflux removal part and application Download PDFInfo
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- CN111803995A CN111803995A CN202010754815.4A CN202010754815A CN111803995A CN 111803995 A CN111803995 A CN 111803995A CN 202010754815 A CN202010754815 A CN 202010754815A CN 111803995 A CN111803995 A CN 111803995A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/0018—Evaporation of components of the mixture to be separated
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/16—Purification
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F13/00—Recovery of starting material, waste material or solvents during the manufacture of artificial filaments or the like
- D01F13/02—Recovery of starting material, waste material or solvents during the manufacture of artificial filaments or the like of cellulose, cellulose derivatives or proteins
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
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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 natural evaporation crystallization system for a reflux removal part of acid bath discharge liquid and application thereof. The system of the invention consists of a temporary storage pool of acid bath discharge liquid, a natural crystallization pool, a liquid preparation pool, a sodium sulfate pool, a sulfuric acid pool, a zinc sulfate pool, an additive pool, a control center, an acid bath device and a pump and a pipeline which are connected according to the process. When the viscose fiber is in vitamin production, the acid bath discharge liquid in the acid bath device is firstly pumped into the temporary storage pool of the acid bath discharge liquid by the pump after passing through the sulfur recovery device, part of the acid bath discharge liquid in the temporary storage pool of the acid bath discharge liquid is pumped into the liquid preparation pool, and the rest acid bath discharge liquid in the temporary storage pool of the acid bath discharge liquid is completely discharged into the natural crystallization pool. The natural evaporation crystallization system overcomes the defects of the prior art, and sodium sulfate in the acid bath discharge liquid which is removed and returned to the liquid preparation pool in the temporary storage pool of the acid bath discharge liquid is crystallized by adopting a natural evaporation crystallization method, so that the salt content of the wastewater entering a sewage treatment plant is reduced.
Description
Technical Field
The invention belongs to the field of viscose fiber production, and particularly relates to a system for naturally evaporating and crystallizing all residual liquid effluent after a reflux part of acid bath effluent is removed and application thereof.
Background
The carbon disulfide method is used for producing viscose staple fiber, pulp is used as a main raw material, alkali liquor is used for dipping to produce alkali cellulose, the alkali cellulose is pressed, crushed, dipped and aged, then the alkali cellulose enters a xanthating machine, the xanthating machine reacts with carbon disulfide to generate cellulose xanthate, diluted alkali is added to dissolve the cellulose xanthate to prepare viscose, and the viscose is filtered, matured and defoamed, and then functional additives are added before spinning and then the viscose is spun. In the spinning process, viscose is sprayed out from a spinneret to generate cellulose fiber in an acid bath, the cellulose fiber is drawn to obtain certain strength, and further refined after being cut, namely acid washing, water washing, desulfurization, oiling and the like, and then the cellulose fiber is dried and packaged into a finished product for delivery.
When viscose fiber is produced, a large amount of chemical reagents such as caustic soda, sulfuric acid and the like are consumed, and a large amount of high-salinity wastewater is generated. According to a first-class reference value of caustic soda consumption of each ton of viscose fibers in a clean production evaluation index system (2017) of regenerated cellulose fiber manufacturing industry (viscose method) of 470kg or less and a first-class reference value of wastewater production of 44m or less3Meanwhile, the first-level reference value of the extraction amount of the sodium sulfate is not lower than 500 kg. Even when the viscose fiber enterprises reach the first-level index of the clean production standard, the content of sodium sulfate in the viscose waste water is still 8000 mg/L.The high sodium sulfate content results in high cost of wastewater treatment, while sodium sulfate enters the treated water. Particularly, in northwest China, when sewage containing rivers and lakes are lacked, the wastewater with high sodium sulfate content influences the growth of plants, and causes salinization and desertification of land.
Generally, viscose fiber factories maintain normal production by using a method of firstly crystallizing and then refluxing crystallization mother liquor for acid bath waste liquid discharged from an acid bath device. The crystallization apparatus is generally a multi-effect evaporation apparatus, however, the current crystallization apparatus faces at least two problems: firstly, the flow of the acid bath waste liquid to be crystallized is large, so that the energy consumption of the multi-effect evaporation device during normal operation is high; secondly, when the crystallization device has different crystallization output amounts, the output amount fluctuation of the crystallization mother liquor is large, and the residual crystallization mother liquor except the backflow crystallization mother liquor can only be discharged into a sewage treatment plant. When the normal production is maintained by adopting a mode of firstly crystallizing and then refluxing the crystallization mother liquor, the content of sodium sulfate in the sewage entering a sewage treatment plant is high, and the cost of sewage treatment is increased.
Disclosure of Invention
Aiming at the defects in the prior art, the invention provides a system for enabling all residual discharge liquid after the acid bath discharge liquid is subjected to backflow removal to enter natural evaporation crystallization. In a system for naturally evaporating and crystallizing all the rest discharged liquid after the backflow part of the acid bath discharged liquid is removed, the acid bath discharged liquid is divided into two parts, the first part of the acid bath discharged liquid is pumped into a liquid preparation pool for liquid preparation and then returns to an acid bath device to maintain the normal production of viscose fibers, and the second part of the acid bath discharged liquid enters a natural crystallization pool. The method overcomes the defects of the prior art by discharging all the residual discharged liquid of the acid bath discharged liquid except the reflux part into a natural evaporation crystallization system, and avoids the generation of high-content sodium sulfate wastewater during the production of viscose fiber vitamin.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect of the invention, a natural evaporative crystallization system for an acid bath effluent reflux removal portion is provided, which comprises an acid bath effluent temporary storage tank, a natural crystallization tank, a sodium sulfate tank, a sulfuric acid tank, a zinc sulfate tank, an additive tank, a control center, a liquid preparation tank, a pump and a connecting pipeline.
The acid bath discharge liquid in the temporary storage pool of the acid bath discharge liquid is sent into the temporary storage pool of the acid bath discharge liquid by the pump after passing through the sulfur recovery device.
Preferably, the volume flow of the acid bath discharge liquid is determined by the volume of the viscose raw liquid entering the acid bath device.
And part of the acid bath discharge liquid in the temporary storage pool of the acid bath discharge liquid is pumped into the liquid preparation pool, and the rest acid bath discharge liquid in the temporary storage pool of the acid bath discharge liquid is completely discharged into the natural crystallization pool.
Preferably, part of the acid bath discharge liquid in the temporary acid bath discharge liquid storage pool is pumped into the liquid preparation pool, and when the liquid level of the acid bath device is kept constant, the volume flow of the acid bath which needs to flow back to the acid bath device is calculated.
Preferably, the concentration of sodium sulfate in the acid bath of said means for flowing back into the acid bath is determined in accordance with existing production data.
Preferably, the pumping flow rate of part of the acid bath discharge liquid in the acid bath discharge liquid temporary storage pool pumped into the liquid preparation pool is determined according to the total mass of the sodium sulfate in the acid bath flowing back to the acid bath device, namely the product of the pumping flow rate pumped from the acid bath discharge liquid temporary storage pool into the liquid preparation pool and the concentration of the sodium sulfate therein is equal to the product of the concentration of the sodium sulfate in the acid bath flowing back to the acid bath device and the volume flow rate of the acid bath flowing back to the acid bath device when the liquid level of the acid bath device is maintained constant.
Preferably, the acid bath discharge liquid in the natural crystallization tank naturally crystallizes and precipitates without artificial energy input.
The pumping flow of the partial acid bath discharge liquid pumped into the liquid preparation pool is realized by controlling the flow of the pump by the control center.
The sodium sulfate pool, the sulfuric acid pool, the zinc sulfate pool and the additive pool are respectively communicated with the liquid preparation pool through pipelines and pumps, and the sodium sulfate, the sulfuric acid, the zinc sulfate and the additive are respectively pumped to the liquid preparation pool.
Preferably, when the sodium sulfate is pumped from the sodium sulfate pool to the liquid preparation pool, the flow rate of the sodium sulfate in the acid bath flowing back to the acid bath device is converted into the volume flow rate of the pumped sodium sulfate when the liquid level of the acid bath device is kept constant.
Preferably, when the sulfuric acid is pumped from the sulfuric acid pool to the liquid preparation pool, the flow rate of the sulfuric acid in the acid bath flowing back to the acid bath device is converted into the volume flow rate of the pumped sulfuric acid when the liquid level of the acid bath device is kept constant.
Preferably, when zinc sulfate is pumped from the zinc sulfate pool to the liquid preparation pool, the zinc sulfate flow in the acid bath flowing back to the acid bath device is converted into the volume flow of the zinc sulfate to be pumped when the liquid level of the acid bath device is maintained to be constant.
Preferably, when the additive is pumped from the additive tank to the liquid preparation tank, the additive flow in the acid bath flowing back to the acid bath device is converted into the volume flow of the pumped additive when the liquid level of the acid bath device is kept constant.
When the sodium sulfate pool, the sulfuric acid pool, the zinc sulfate pool and the additive pool respectively pump sodium sulfate, sulfuric acid, zinc sulfate and additives to the liquid preparation pool, the respective pumping flow rates are realized by controlling the flow rates of the corresponding pumps by the control center.
The liquid preparation pool is a place for preparing acid bath liquid for production.
The liquid preparation pool pumps the acid bath liquid for production to the acid bath device through a pipeline and a pump, and the pumping flow rate of the acid bath liquid for production is realized by controlling the flow rate of the pump through a control center.
Preferably, the volume flow of the acid bath liquid for production pumped from the liquid preparation pool to the acid bath device through the pipeline and the pump is determined by the volume flow of the acid bath required to flow back to the acid bath device when the liquid level of the acid bath device is kept constant.
A second aspect of the invention provides the use of a natural evaporative crystallization system for the acid bath effluent reflux removal section in viscose fiber production.
Compared with the prior art, the invention has the following beneficial effects:
1. the acid bath discharge liquid completely enters a natural evaporation crystallization system for viscose fiber production after the reflux part is removed;
2. the cost of extracting the sodium sulfate by completely feeding the acid bath discharge liquid into a natural evaporation crystallization system after removing the reflux part is low.
Drawings
In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
FIG. 1 is a schematic diagram of a natural evaporative crystallization system for the acid bath effluent reflux section.
1-temporary storage pool of acid bath discharge liquid; 2-a natural crystallization tank; 3-a liquid preparation pool; 4-sodium sulfate pool; 5-a sulfuric acid tank; 6-zinc sulfate pool; 7-an additive tank; 8-a control center; 9-acid bath device; 10-sulfur recovery device, 11-18-pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the technical solutions of the present invention will be described in detail below. It is to be understood that the described embodiments are merely exemplary of the invention, and not restrictive of the full scope of the invention. All other embodiments, which can be derived by a person skilled in the art from the examples given herein without any inventive step, are within the scope of the present invention.
Specific example 1:
the viscose stock solution is from the existing viscose stock solution production workshop and has the following formula: the water content is 83.8 percent, the content of the alpha-cellulose is 8.7 percent, the content of the caustic soda is 5.2 percent, and the consumption quota of the viscose is 10.52 tons/ton of viscose.
According to fig. 1, in the natural evaporation crystallization system of the acid bath discharge liquid reflux part, the formulation of the acid bath pumped from the liquid preparation pool to the acid bath device: 140g/L of sulfuric acid, 280g/L of sodium sulfate, 20g/L of zinc sulfate and 2g/L of additive. The concentration of the sulfuric acid in the sulfuric acid tank is 1500 g/L; the concentration of the additive in the additive pool is 100g/L, and the concentration of the sulfuric acid is 200 g/L; the concentration of zinc sulfate in the zinc sulfate pool is 200g/L, and the concentration of sulfuric acid is 200 g/L; the concentration of sodium sulfate in the sodium sulfate pool is 400 g/L.
The pumping rate of the viscose stock solution to the acid bath device is 100kg/hr, and the pumping rate of the liquid preparation pool to the acid bath device is 45.5L/hr. The acid bath solution discharged from the acid bath device is 100.78L/hr, and is discharged to the temporary storage pool of acid bath discharge solution after passing through the sulfur recovery device. At this time, after the operation of the control center, the liquid preparation tank receives 8.25L/hr of the acid bath liquid from the acid bath discharge liquid temporary storage tank, 4.26L/hr of the zinc sulfate supplementary liquid from the zinc sulfate tank, 0.852L/hr of the additive supplementary liquid from the additive tank, 3.56L/hr of the sulfuric acid supplementary liquid from the sulfuric acid tank, and 28.344L/hr of the sodium sulfate supplementary liquid from the sodium sulfate tank. At this time, the production of the acid bath device is stable, the volume flow rate of the acid bath liquid discharged from the acid bath device and entering the natural crystallizing pond is 92.53L/hr, and the generation amount of mirabilite in the natural crystallizing pond is 35.67 kg/hr. The operating cost for crystallizing the mirabilite in the natural crystallizing pond is 0.
Specific example 2:
the viscose stock solution is from the existing viscose stock solution production workshop and has the following formula: the water content is 83.8 percent, the content of the alpha-cellulose is 8.7 percent, the content of the caustic soda is 5.2 percent, and the consumption quota of the viscose is 10.52 tons/ton of viscose.
According to fig. 1, in the natural evaporative crystallization system for the acid bath discharge liquid reflux portion, the formulation of the acid bath pumped from the solution preparation tank to the acid bath device: 140g/L of sulfuric acid, 280g/L of sodium sulfate, 20g/L of zinc sulfate and 2g/L of additive. The concentration of the sulfuric acid in the sulfuric acid tank is 1840 g/L; the concentration of the additive in the additive pool is 100g/L, and the concentration of the sulfuric acid is 200 g/L; the concentration of zinc sulfate in the zinc sulfate pool is 200g/L, and the concentration of sulfuric acid is 200 g/L; the concentration of sodium sulfate in the sodium sulfate pool is 400 g/L.
The pumping rate of the viscose stock solution to the acid bath device is 100kg/hr, and the pumping rate of the liquid preparation pool to the acid bath device is 45.5L/hr. The acid bath solution discharged from the acid bath device is 100.78L/hr, and is discharged to the temporary storage tank of the acid bath discharge solution after passing through the sulfur recovery device. At this time, after the operation of the control center, the liquid preparation tank receives 9.5615L/hr of the acid bath liquid from the acid bath discharge liquid temporary storage tank, 4.21L/hr of the zinc sulfate supplementary liquid from the zinc sulfate tank, 0.843L/hr of the additive supplementary liquid from the additive tank, 2.91L/hr of the sulfuric acid supplementary liquid from the sulfuric acid tank, and 27.786L/hr of the sodium sulfate supplementary liquid from the sodium sulfate tank. At the moment, the production of the acid bath device is stable, the volume flow of the acid bath liquid discharged from the acid bath device into the natural crystallizing pond is 91.22L/hr, and the generation amount of mirabilite in the natural crystallizing pond is 35164 kg/hr. The operating cost for crystallizing the mirabilite in the natural crystallizing pond is 0.
Specific example 3:
the viscose stock solution is from the existing viscose stock solution production workshop and has the following formula: the water content is 83.8 percent, the content of the alpha-cellulose is 8.7 percent, the content of the caustic soda is 5.2 percent, and the consumption quota of the viscose is 10.52 tons/ton of viscose.
According to fig. 1, in the natural evaporative crystallization system for the acid bath discharge liquid reflux portion, the formulation of the acid bath pumped from the solution preparation tank to the acid bath device: 140g/L of sulfuric acid, 280g/L of sodium sulfate, 20g/L of zinc sulfate and 2g/L of additive. The concentration of the sulfuric acid in the sulfuric acid tank is 1500 g/L; the concentration of the additive in the additive pool is 100g/L, and the concentration of the sulfuric acid is 200 g/L; the concentration of zinc sulfate in the zinc sulfate pool is 200g/L, and the concentration of sulfuric acid is 200 g/L; the sodium sulfate pool is powder of sodium sulfate decahydrate.
The pumping rate of the viscose stock solution to the acid bath device is 100kg/hr, and the pumping rate of the liquid preparation pool to the acid bath device is 45.5L/hr. The acid bath solution discharged from the acid bath device is 100.78L/hr, and is discharged to the temporary storage pool of acid bath discharge solution after passing through the sulfur recovery device. At this time, after the operation of the control center, the liquid preparation pool receives 37.98L/hr of acid bath liquid from the acid bath discharge liquid temporary storage pool, 3.21L/hr of zinc sulfate supplementary liquid from the zinc sulfate pool, 0.644L/hr of additive supplementary liquid from the additive pool, 3.732L/hr of sulfuric acid supplementary liquid from the sulfuric acid pool, and 14.248kg/hr of sodium sulfate decahydrate from the sodium sulfate pool. At this time, the production of the acid bath device is stable, the volume flow rate of the acid bath liquid discharged from the acid bath device and entering the natural crystallizing pond is 62.8L/hr, and the generation amount of mirabilite in the natural crystallizing pond is 24.21 kg/hr. The operating cost for crystallizing the mirabilite in the natural crystallizing pond is 0.
Specific example 4:
the viscose stock solution is from the existing viscose stock solution production workshop and has the following formula: the water content is 83.8 percent, the content of the alpha-cellulose is 8.7 percent, the content of the caustic soda is 5.2 percent, and the consumption quota of the viscose is 10.52 tons/ton of viscose.
According to fig. 1, in the natural evaporative crystallization system for the acid bath discharge liquid reflux portion, the formulation of the acid bath pumped from the solution preparation tank to the acid bath device: 140g/L of sulfuric acid, 280g/L of sodium sulfate, 20g/L of zinc sulfate and 2g/L of additive. The concentration of the sulfuric acid in the sulfuric acid tank is 1840 g/L; the concentration of the additive in the additive pool is 100g/L, and the concentration of the sulfuric acid is 200 g/L; the concentration of zinc sulfate in the zinc sulfate pool is 200g/L, and the concentration of sulfuric acid is 200 g/L; the sodium sulfate pool is powder of sodium sulfate decahydrate.
The pumping rate of the viscose stock solution to the acid bath device is 100kg/hr, and the pumping rate of the liquid preparation pool to the acid bath device is 45.5L/hr. The acid bath solution discharged from the acid bath device is 100.78L/hr, and is discharged to the temporary storage pool of acid bath discharge solution after passing through the sulfur recovery device. At this time, after the operation of the control center, the liquid preparation pool receives 38.685L/hr of acid bath liquid from the acid bath discharge liquid temporary storage pool, 3.188L/hr of zinc sulfate supplementary liquid from the zinc sulfate pool, 0.639L/hr of additive supplementary liquid from the additive pool, 3.046L/hr of sulfuric acid supplementary liquid from the sulfuric acid pool, and 13.976kg/hr of sodium sulfate decahydrate from the sodium sulfate pool. At this time, the production of the acid bath device is stable, the volume flow rate of the acid bath liquid discharged from the acid bath device and entering the natural crystallizing pond is 62.1L/hr, and the generation amount of mirabilite in the natural crystallizing pond is 23.94 kg/hr. The operating cost for crystallizing the mirabilite in the natural crystallizing pond is 0.
The applicant states that the present invention is illustrated by the above examples to show the process features and methods of use of the present invention, but the present invention is not limited to the above detailed process features, i.e. it is not meant to imply that the present invention must rely on the above detailed apparatus features to be practiced. It will be apparent to those skilled in the art that any modifications to the invention, equivalent substitutions of selected devices of the invention, additions of auxiliary components, selection of specific forms and the like, are within the scope and disclosure of the invention.
The embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the invention is not described in any way for the possible combinations in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.
Claims (9)
1. A natural evaporation crystallization system for a reflux removal part of acid bath discharge liquid is characterized by comprising a temporary storage pool of the acid bath discharge liquid, a natural crystallization pool, a sodium sulfate pool, a sulfuric acid pool, a zinc sulfate pool, an additive pool, a control center, a liquid preparation pool, a pump and a connecting pipeline.
2. The natural evaporation crystallization system for the acid bath drain back-flow removal part according to claim 1, wherein the acid bath drain in the acid bath drain temporary storage tank is pumped into the acid bath drain temporary storage tank from the acid bath drain in the acid bath device after passing through a sulfur recovery device.
3. The natural evaporative crystallization system for the acid bath effluent deflux section as recited in claim 1, wherein a portion of the acid bath effluent from the temporary acid bath effluent storage tank is pumped into the solution preparation tank, and the remaining acid bath effluent from the temporary acid bath effluent storage tank is discharged into the natural crystallization tank.
4. The natural evaporation crystallization system for the acid bath discharge liquid reflux portion as claimed in claim 3, wherein the pumping amount of a part of the acid bath discharge liquid pumped into the liquid preparation tank is realized by controlling the flow rate of the pump through the control center.
5. The natural evaporation crystallization system for the acid bath effluent backflow removal section as claimed in claim 1, wherein the sodium sulfate tank, the sulfuric acid tank, the zinc sulfate tank and the additive tank are respectively communicated with the solution preparation tank through pipes via pumps, and the sodium sulfate, the sulfuric acid, the zinc sulfate and the additives are respectively pumped to the solution preparation tank.
6. The natural evaporation crystallization system for the acid bath effluent backflow removal portion as claimed in claim 1, wherein the sodium sulfate tank, the sulfuric acid tank, the zinc sulfate tank, the additive tank are respectively pumped to the liquid preparation tank by the sodium sulfate tank, the sulfuric acid tank, the zinc sulfate tank, and the additive tank by controlling the flow rates of the respective pumps through the control center.
7. The natural evaporative crystallization system for acid bath effluent deflux section as recited in claim 1 wherein the liquor dosing tank is the site where the process acid bath is dosed.
8. The natural evaporation crystallization system for the acid bath discharge liquid reflux removal part as claimed in claim 1, wherein the liquid preparation pool pumps the production acid bath liquid to the acid bath device through a pipeline by a pump, and the pumping flow rate of the production acid bath liquid is realized by controlling the flow rate of the pump by a control center.
9. Use of a system for natural evaporative crystallization of an acid bath effluent deflux section according to any one of claims 1-8 in viscose fiber production.
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Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DD265390A5 (en) * | 1986-11-19 | 1989-03-01 | Politechnika Szczecinska,Pl | METHOD OF ILLUSTRATING THE WATER-FREE SODIUM SULFATE OF AROMATIC BATH IN THE PRODUCTION OF VISCOSE FIBERS |
| CN1043535A (en) * | 1988-12-24 | 1990-07-04 | 由正明 | Sulfuric acid pickling waste liquid regenerated processing method |
| CN2670340Y (en) * | 2003-12-11 | 2005-01-12 | 宜兴市新东化工有限公司 | Recovering and utilizing treater for waste sulfuric acid liquid |
| US20060163164A1 (en) * | 2004-10-25 | 2006-07-27 | Matthew Pratt | Process for making high purity sodium sulfate |
| CN103510166A (en) * | 2012-06-20 | 2014-01-15 | 杭州奥通科技有限公司 | High wet modulus viscose fiber coagulating bath processing assembly line |
| CN204307566U (en) * | 2014-12-09 | 2015-05-06 | 山东银鹰化纤有限公司 | A kind of acid bath blending equipment |
| CN105369689A (en) * | 2015-11-17 | 2016-03-02 | 成都丽雅纤维股份有限公司 | Acid bath process for glass paper production |
| CN109231603A (en) * | 2018-11-21 | 2019-01-18 | 江苏南大环保科技有限公司 | The method and device of cooperative disposal acid waste liquid in cellulose viscose manufacturing technique |
| CN109457325A (en) * | 2018-11-21 | 2019-03-12 | 江苏南大环保科技有限公司 | The method and apparatus of the recycling of viscose rayon spinning acid waste liquid sublevel and recycled |
| CN209322625U (en) * | 2018-11-06 | 2019-08-30 | 宜宾海丝特纤维有限责任公司 | A kind of environment-friendly cycle processing system of viscose glue waste liquid |
-
2020
- 2020-07-31 CN CN202010754815.4A patent/CN111803995A/en active Pending
Patent Citations (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DD265390A5 (en) * | 1986-11-19 | 1989-03-01 | Politechnika Szczecinska,Pl | METHOD OF ILLUSTRATING THE WATER-FREE SODIUM SULFATE OF AROMATIC BATH IN THE PRODUCTION OF VISCOSE FIBERS |
| CN1043535A (en) * | 1988-12-24 | 1990-07-04 | 由正明 | Sulfuric acid pickling waste liquid regenerated processing method |
| CN2670340Y (en) * | 2003-12-11 | 2005-01-12 | 宜兴市新东化工有限公司 | Recovering and utilizing treater for waste sulfuric acid liquid |
| US20060163164A1 (en) * | 2004-10-25 | 2006-07-27 | Matthew Pratt | Process for making high purity sodium sulfate |
| CN103510166A (en) * | 2012-06-20 | 2014-01-15 | 杭州奥通科技有限公司 | High wet modulus viscose fiber coagulating bath processing assembly line |
| CN204307566U (en) * | 2014-12-09 | 2015-05-06 | 山东银鹰化纤有限公司 | A kind of acid bath blending equipment |
| CN105369689A (en) * | 2015-11-17 | 2016-03-02 | 成都丽雅纤维股份有限公司 | Acid bath process for glass paper production |
| CN209322625U (en) * | 2018-11-06 | 2019-08-30 | 宜宾海丝特纤维有限责任公司 | A kind of environment-friendly cycle processing system of viscose glue waste liquid |
| CN109231603A (en) * | 2018-11-21 | 2019-01-18 | 江苏南大环保科技有限公司 | The method and device of cooperative disposal acid waste liquid in cellulose viscose manufacturing technique |
| CN109457325A (en) * | 2018-11-21 | 2019-03-12 | 江苏南大环保科技有限公司 | The method and apparatus of the recycling of viscose rayon spinning acid waste liquid sublevel and recycled |
Non-Patent Citations (2)
| Title |
|---|
| 于捍江: "黏胶短纤维酸浴调配系统的节能优化设计", 《化工进展》 * |
| 张弓: "《中等职业教育教材 化工原理 下 2000年版》", 30 June 2000, 化学工业出版社 * |
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