CN111870991B - Heating evaporation crystallization system for reflux removal part of spinning bath discharge liquid and application - Google Patents
Heating evaporation crystallization system for reflux removal part of spinning bath discharge liquid and application Download PDFInfo
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- CN111870991B CN111870991B CN202010757306.7A CN202010757306A CN111870991B CN 111870991 B CN111870991 B CN 111870991B CN 202010757306 A CN202010757306 A CN 202010757306A CN 111870991 B CN111870991 B CN 111870991B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D9/02—Crystallisation from solutions
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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
- B01D9/0031—Evaporation of components of the mixture to be separated by heating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D9/00—Crystallisation
- B01D2009/0086—Processes or apparatus therefor
Abstract
The invention discloses a heating evaporation crystallization system for a reflux removal part of spinning bath discharge liquid and application thereof. The system of the invention consists of a temporary storage pool of spinning bath discharge liquid, a heating evaporation device, a liquid preparation pool, a sodium sulfate pool, a sulfuric acid pool, a zinc sulfate pool, an additive pool, a control center, a spinning bath device and pumps and pipelines which are connected according to the process. When the viscose fiber is in production, the spinning bath discharge liquid in the spinning bath device firstly passes through the sulfur recovery device and then is pumped into the temporary storage pool of the spinning bath discharge liquid, part of the spinning bath discharge liquid in the temporary storage pool of the spinning bath discharge liquid is pumped into the liquid preparation pool, and the rest of the spinning bath discharge liquid in the temporary storage pool of the spinning bath discharge liquid is completely discharged into the heating evaporation device. The invention overcomes the defects of the prior art, and adopts a heating evaporation crystallization method to crystallize the sodium sulfate in the spinning bath discharge liquid which is removed from the temporary storage pool of the spinning bath discharge liquid and flows back to the liquid preparation pool, thereby reducing the salt content of the wastewater entering a sewage treatment plant.
Description
Technical Field
The invention belongs to the field of viscose fiber production, and particularly relates to a heating evaporation crystallization system for all residual discharge liquid after a reflux part of discharge liquid of a spinning bath is removed and an application of the system.
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 fibers in a spinning bath, the cellulose fibers are drawn to obtain certain strength, and the cellulose fibers are further refined after being cut, namely acid washing, water washing, desulfurization, oiling and the like, and then are dried and packaged to obtain finished products 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 spinning bath waste liquid discharged from a spinning 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 spinning 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 heating evaporation crystallization system for a reflux removal part of spinning bath discharge liquid. In a heating evaporation crystallization system for a reflux-removing part of spinning bath discharge liquid, the spinning bath discharge liquid is divided into two parts, the first part of the spinning bath discharge liquid is pumped into a liquid preparation pool for liquid preparation and then returns to a spinning bath device to maintain the normal production of viscose fibers, and the second part of the spinning bath discharge liquid enters a heating evaporation device. The heating evaporation crystallization system for the reflux removal part of the spinning bath discharge liquid overcomes the defects of the prior art, and avoids the generation of high-content sodium sulfate wastewater during the production of viscose fibers.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect of the invention, a heating evaporation crystallization system for a backflow removing part of spinning bath discharge liquid comprises a spinning bath discharge liquid temporary storage pool, a heating evaporation device, 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.
The spinning bath discharge liquid in the temporary spinning bath discharge liquid storage pool is conveyed into the temporary spinning bath discharge liquid storage pool by a pump after passing through a sulfur recovery device from the spinning bath discharge liquid in the spinning bath device.
Preferably, the volume flow of the spinning bath discharge is determined by the volume of the viscose dope entering the spinning bath apparatus.
And part of the spinning bath discharge liquid in the temporary spinning bath discharge liquid storage pool is pumped into the liquid preparation pool, and the rest of the spinning bath discharge liquid in the temporary spinning bath discharge liquid storage pool is completely discharged into the heating and evaporating device.
Preferably, part of the spinning bath discharge liquid in the spinning bath discharge liquid temporary storage pool is pumped into the liquid preparation pool, and when the liquid level of the spinning bath device is kept constant, the volume flow of the spinning bath which needs to flow back to the spinning bath device is calculated.
Preferably, the concentration of sodium sulfate in the spinning bath flowing back to the spinning bath apparatus is determined in accordance with the existing production data.
Preferably, the pumping flow rate of part of the spinning bath discharge from the spinning bath discharge buffer is determined by the total mass of the sodium sulfate in the spinning bath flowing back to the spinning bath device, i.e. the product of the pumping flow rate from the spinning bath discharge buffer into the mixing tank and the concentration of sodium sulfate therein is equal to the product of the concentration of sodium sulfate in the spinning bath flowing back to the spinning bath device and the volume flow rate of the spinning bath flowing back to the spinning bath device while the liquid level of the spinning bath device is maintained constant.
Preferably, the spinning bath discharge liquid in the heating and evaporating device is heated and crystallized, and the existing evaporating and crystallizing device is adopted, and the existing multi-effect evaporating device is further preferably adopted.
The pumping flow of part of the spinning 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 solution preparation pool, the flow rate of the sodium sulfate in the spinning bath flowing back to the spinning bath device is converted into the volume flow rate of the pumped sodium sulfate when the liquid level of the spinning bath device is kept constant.
Preferably, when the sulfuric acid is pumped from the sulfuric acid pool to the solution preparation pool, the flow rate of the sulfuric acid in the spinning bath flowing back to the spinning bath device is converted into the volume flow rate of the pumped sulfuric acid when the liquid level of the spinning bath device is kept constant.
Preferably, when zinc sulfate is pumped from the zinc sulfate pool to the solution preparation pool, the zinc sulfate flow in the spinning bath flowing back to the spinning bath device is converted into the volume flow of the zinc sulfate to be pumped when the liquid level of the spinning bath device is kept constant.
Preferably, when the additive is pumped from the additive pool to the solution preparation pool, the additive flow in the spinning bath flowing back to the spinning bath device is converted into the volume flow of the pumped additive by maintaining the liquid level of the spinning bath device to be 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 spinning bath solution for production.
The liquid preparation pool pumps the spinning bath liquid for production to the spinning bath device through a pipeline by a pump, and the pumping flow of the spinning bath liquid for production is realized by controlling the flow of the pump by a control center.
Preferably, the volume flow of the spinning bath liquid for production pumped from the liquid preparation pool to the spinning bath device through the pipeline and the pump is determined by the volume flow of the spinning bath liquid required to flow back to the spinning bath device when the liquid level of the spinning bath device is kept constant.
A second aspect of the invention provides the use of a heated evaporative crystallization system for the defluxed portion of the spin bath effluent in viscose fiber production.
Compared with the prior art, the invention has the following beneficial effects:
1. the heating evaporation crystallization system for the reflux removal part of the spinning bath discharge liquid is used for viscose fiber production;
2. the method has the advantage that the cost of extracting the sodium sulfate by completely feeding the spinning bath discharge liquid into the heating 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 heated evaporative crystallization system for the defluxed portion of the spin bath effluent.
1-temporary storage pool of spinning bath discharge liquid; 2-heating the evaporation plant; 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-spinning bath device; 10-sulfur recovery device, 11-19-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 heating evaporation crystallization system for the reflux portion of the spinning bath discharge, the formulation of the spinning bath pumped by the solution preparation tank to the spinning 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 spinning bath device is 100kg/hr, and the pumping rate of the liquid preparation pool to the spinning bath device is 45.5L/hr. The spinning bath liquid discharged from the spinning bath device is 100.78L/hr, and is discharged to a temporary storage pool of spinning bath discharge liquid after passing through a sulfur recovery device. At this time, after the operation of the control center, the liquid preparation tank receives 8.25L/hr of the spinning bath liquid from the temporary storage tank of the spinning bath discharge liquid, 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 spinning bath device is stable, the volume flow of the spinning bath liquid discharged from the spinning bath device and entering the heating evaporation device is 92.53L/hr, and the generation amount of mirabilite in the heating evaporation device is 35.67 kg/hr.
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 heating evaporation crystallization system for the reflux portion of the spinning bath discharge, the formulation of the spinning bath pumped by the solution preparation tank to the spinning 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 spinning bath device is 100kg/hr, and the pumping rate of the liquid preparation pool to the spinning bath device is 45.5L/hr. The spinning bath liquid discharged from the spinning bath device is 100.78L/hr, and is discharged to a temporary storage pool of spinning bath discharge liquid after passing through a sulfur recovery device. At this time, after the operation of the control center, the liquid preparation tank receives 9.5615L/hr of spinning bath liquid from the temporary storage tank of the spinning bath discharge liquid, 4.21L/hr of zinc sulfate supplementary liquid from the zinc sulfate tank, 0.843L/hr of additive supplementary liquid from the additive tank, 2.91L/hr of sulfuric acid supplementary liquid from the sulfuric acid tank, and 27.786L/h of sodium sulfate supplementary liquid from the sodium sulfate tank. At the moment, the production of the spinning bath device is stable, the volume flow of the spinning bath liquid discharged from the spinning bath device and entering the heating evaporation device is 91.22L/hr, and the generation amount of mirabilite in the heating evaporation device is 35164 kg/hr.
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 heating evaporation crystallization system for the reflux portion of the spinning bath discharge, the formulation of the spinning bath pumped by the solution preparation tank to the spinning 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 spinning bath device is 100kg/hr, and the pumping rate of the liquid preparation pool to the spinning bath device is 45.5L/hr. The spinning bath liquid discharged from the spinning bath device is 100.78L/hr, and is discharged to a temporary storage pool of spinning bath discharge liquid after passing through a sulfur recovery device. At this time, after the operation of the control center, the liquid preparation pool receives 37.98L/hr of spinning bath liquid from the temporary storage pool of spinning bath discharge liquid, 3.21L/hr of zinc sulfate supplementary liquid from a zinc sulfate pool, 0.644L/hr of additive supplementary liquid from an additive pool, 3.732L/hr of sulfuric acid supplementary liquid from a sulfuric acid pool, and 14.248kg/hr of sodium sulfate decahydrate from a sodium sulfate pool. At this time, the production of the spinning bath device is stable, the volume flow of the spinning bath liquid discharged from the spinning bath device and entering the heating evaporation device is 62.8L/hr, and the generation amount of mirabilite in the heating evaporation device is 24.21 kg/hr.
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 heating evaporation crystallization system for the reflux portion of the spinning bath discharge, the formulation of the spinning bath pumped by the solution preparation tank to the spinning 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 spinning bath device is 100kg/hr, and the pumping rate of the liquid preparation pool to the spinning bath device is 45.5L/hr. The spinning bath liquid discharged from the spinning bath device is 100.78L/hr, and is discharged to a temporary storage pool of spinning bath discharge liquid after passing through a sulfur recovery device. At this time, after the operation of the control center, the liquid preparation pool receives 38.685L/hr of spinning bath liquid from the temporary storage pool of spinning bath discharge liquid, 3.188L/hr of zinc sulfate supplementary liquid from a zinc sulfate pool, 0.639L/hr of additive supplementary liquid from an additive pool, 3.046L/hr of sulfuric acid supplementary liquid from a sulfuric acid pool, and 13.976kg/hr of sodium sulfate decahydrate from a sodium sulfate pool. At this time, the production of the spinning bath device is stable, the volume flow of the spinning bath liquid discharged from the spinning bath device and entering the heating evaporation device is 62.1L/hr, and the generation amount of mirabilite in the heating evaporation device is 23.94 kg/hr.
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 (4)
1. The application of the heating evaporation crystallization system for the reflux removal part of the spinning bath discharge liquid in viscose fiber production is characterized in that the heating evaporation crystallization system comprises a temporary storage pool of the spinning bath discharge liquid, a heating evaporation device, 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; wherein:
part of spinning bath discharge liquid in the spinning bath discharge liquid temporary storage pool is pumped into a liquid preparation pool, and the rest of spinning bath discharge liquid in the spinning bath discharge liquid temporary storage pool is completely discharged into a heating evaporation device;
the pump delivery of partial spinning bath discharge liquid into the liquid preparation pool through a pump is realized by controlling the flow of the pump by a control center, the pump delivery of sodium sulfate, sulfuric acid, zinc sulfate and additives to the liquid preparation pool is realized by controlling the flow of the corresponding pump by the control center, the spinning bath liquid for production is pumped to the spinning bath device through a pipeline by the liquid preparation pool through the pump, and the pump delivery of the spinning bath liquid for production is realized by controlling the flow of the pump by the control center.
2. The application of 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.
3. The use according to claim 1, wherein the liquid distribution tank is the location where the spinning bath solution for production is prepared.
4. The use according to claim 1, characterized in that the spinning bath effluent from the spinning bath effluent buffer is pumped from the spinning bath effluent from the spinning bath apparatus to the spinning bath effluent buffer after passing through a sulfur recovery unit.
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