CN115253545B - Method and system for recycling dedusting water in viscose staple fiber production process - Google Patents
Method and system for recycling dedusting water in viscose staple fiber production process Download PDFInfo
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- CN115253545B CN115253545B CN202210885000.9A CN202210885000A CN115253545B CN 115253545 B CN115253545 B CN 115253545B CN 202210885000 A CN202210885000 A CN 202210885000A CN 115253545 B CN115253545 B CN 115253545B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
- B01D47/06—Spray cleaning
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D33/00—Filters with filtering elements which move during the filtering operation
- B01D33/04—Filters with filtering elements which move during the filtering operation with filtering bands or the like supported on cylinders which are impervious for filtering
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D33/00—Filters with filtering elements which move during the filtering operation
- B01D33/58—Handling the filter cake in the filter for purposes other than for regenerating the filter cake remaining on the filtering element
- B01D33/60—Handling the filter cake in the filter for purposes other than for regenerating the filter cake remaining on the filtering element for washing
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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
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- 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
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Abstract
The invention relates to a method and a system for recycling dust-removing water in the production process of viscose staple fibers, which belongs to the field of viscose fiber production. The invention can reduce water consumption and wastewater treatment capacity in production by fully utilizing water generated in viscose fiber production and recycling discharged dust-removing water, can reduce material loss caused by water washing materials and steam consumption increased by water washing materials in the operation of the rubber belt type vacuum filter, and does not increase alkali consumption.
Description
Technical Field
The invention relates to a method and a system for recycling dust-removing water in the production process of viscose staple fibers, in particular to a method and a system for cleaning an adhesive acid bath on the surface of a material filtered by a rubber belt type vacuum filter after the dust-removing water and a saturated sodium sulfate solution are mixed, and belongs to the field of viscose fiber production.
Background
At present, the following processes are adopted by part of enterprises in domestic viscose staple fiber production: separating sodium sulfate-containing solid particles by using a rubber vacuum belt filter, enabling the filtered sodium sulfate solids to fall into an S barrel (melting barrel) containing solid-liquid two phases, adding alkali liquid to adjust pH, and conveying the sodium sulfate solids into a thickener by using a centrifugal pump to carry out sedimentation and thickening. The thickened material falls into a centrifugal machine through a pipeline to be dehydrated, supernatant overflows back to the S barrel, mother liquor removed by the centrifugal machine flows back to the S barrel, and the dehydrated material of the centrifugal machine is dried to dry water.
The process has the following characteristics: firstly, as the water content of the material dehydrated by the centrifugal machine is lower than that of the material filtered by the rubber vacuum belt filter and partial alkali liquor is introduced into the S barrel, the volume of liquid phase substances in the S barrel is increased, and the supernatant liquid of the partial thickener is required to be directly discharged into an acid bath, so that the steam consumption of the previous working procedure is increased; secondly, in the process of separating sodium sulfate-containing solid particles from acid bath by using a rubber belt type vacuum filter, a small amount of acid bath is adsorbed on the surface of the separated sodium sulfate solid, a spray water method is adopted to wash materials, excessive acid bath residues on the surface of the materials are caused when the spray water quantity is low, alkali consumption is increased, part of sodium sulfate solid is dissolved when the spray water quantity is high, material loss is caused, water after washing the materials is mixed into the acid bath, and steam consumption in viscose fiber production is increased; thirdly, when the anhydrous sodium sulfate is dried, the adopted water foam dust removing method utilizes water to treat dust carried by hot air in the drying process through a water foam dust remover, and the dust removing water is directly discharged to the sewage for treatment.
As mentioned above, the existing process has such problems in operation: part of supernatant is directly discharged into the acid bath, so that the steam consumption of the previous working procedure is increased; when the spray water quantity of the belt filter is high, the steam consumption and the water consumption and the anhydrous sodium sulphate loss are increased; when the spraying water quantity is low, acid bath adhered to the materials is increased, and the consumption of sodium hydroxide is increased; the dust removal water is discharged outwards, so that the water consumption is increased, and the sewage treatment capacity is increased. Therefore, research and development of a new process for recycling the dust-removing water are required.
Disclosure of Invention
The invention aims to solve the technical problem of providing a method and a system for recycling dust-removing water in the production process of viscose staple fibers, which are characterized in that the dust-removing water generated in the production process of viscose fibers is mixed with a saturated sodium sulfate solution, and an acid bath on the surface of sodium sulfate solid particles on a rubber belt type vacuum filter is washed in a known spraying manner to reduce the acid bath adhered to the solid sodium sulfate, so that the recycling of the dust-removing water is realized.
The technical scheme for solving the technical problems is as follows: a method for reclaiming the dust-removing water in the production of viscose staple fibre includes such steps as mixing the dust-removing water generated in the production of viscose staple fibre with saturated sodium sulfate solution, and washing the acid bath on the surface of sodium sulfate solid on rubber belt-type vacuum filter.
The invention provides a process for recycling the dust-removing water, which is simple to operate and good in effect, reduces the overall process running cost, and improves the environmental protection performance of the process.
The beneficial effects of the invention are as follows: the invention can reduce water consumption and wastewater treatment capacity in production by fully utilizing water generated in viscose fiber production and recycling discharged dust-removing water, can reduce material loss caused by water washing materials and steam consumption increased by water washing materials in the operation of the rubber belt type vacuum filter, and does not increase alkali consumption.
On the basis of the technical scheme, the invention can be improved as follows.
Further, the dust removing water is obtained by mixing water generated in the production process of the viscose staple fibers with anhydrous sodium sulfate materials, the water generated in the production process of the viscose staple fibers is condensed water generated after flash evaporation, heat exchange and condensation, pH neutral water recovered in the production or water containing sodium sulfate or zinc sulfate and having pH neutral, the anhydrous sodium sulfate materials are anhydrous sodium sulfate blocks or dust in hot air generated by drying the anhydrous sodium sulfate, the saturated sodium sulfate solution is mother liquor or thickener supernatant generated after dehydration of a centrifugal machine, and the cleaning mode is spraying or overflow.
The water with neutral pH recovered in the production can be the cooling water of a recovered centrifugal machine, the sealing water of a centrifugal pump and the water of a flash evaporation mixing condenser, or can be replaced by the common water used in the production or the desulfurization and the deacidification in the production of viscose fiber. The water with neutral pH value containing sodium sulfate or zinc sulfate can be the reclaimed sealing water of a belt filter, the water of a flash evaporation water station and the water neutralized after alkali addition, and besides sodium sulfate or zinc sulfate, the water does not contain other inorganic matters, and can be used as a water source for the process of the invention by dissolving sodium sulfate dust.
Further, the method comprises the following steps: 1) Dedusting by using condensate water generated in production: the condensed water generated after flash evaporation, heat exchange and condensation in the viscose fiber production process is mixed with dust in hot air generated by drying anhydrous sodium sulfate in a spraying mode to obtain dust removal water; 2) Mixing dust removal water with supernatant: adding alkali into the material filtered by the rubber belt type vacuum filter to adjust the pH value, conveying the material into a thickener for thickening, and mixing part of overflowed supernatant with dust removal water; 3) And (3) cleaning materials: spraying the sodium sulfate solution formed after mixing on the surface of sodium sulfate solid on a rubber belt type vacuum filter, and cleaning acid bath adhered on the sodium sulfate solid.
The mixed solution of the dust removal water and the supernatant of the thickener is used as the spray water of the rubber belt type vacuum filter, so that the acid content of materials of the rubber belt type vacuum filter can be reduced, the dissolution of the materials by direct water spray can be reduced, and the steam consumption increased by directly discharging the spray water and part of supernatant into an acid bath can be further reduced.
By adopting the technical scheme, compared with the prior art, the supernatant of the thickener of the prior art directly overflows into the acid bath, dust removal water is discharged to the sewage treatment station, sodium sulfate solid particles on the rubber belt type vacuum filter are washed by water, and the steam consumption and the water consumption are high. After the technical scheme is adopted: 1. the supernatant fluid of the thickener is mixed with dust removal water to replace water for washing sodium sulfate solids in the prior art, the dust removal water is recycled and is not discharged to sewage, the loss of anhydrous sodium sulfate caused by dust removal outside the dust removal water in the prior art is reduced, and the yield of anhydrous sodium sulfate is increased; 2. the dissolution of sodium sulfate is reduced, and the yield is increased from 52% to 53%;3. the acid bath amount of sodium sulfate adhesion is the same as that of the prior art, and the water consumption and the wastewater treatment amount are reduced by recycling the dust removal water; 4. the supernatant liquid is mixed with dust removal water to wash the materials and then is discharged into an acid bath, and the supernatant liquid replaces part of spray water, so that a large amount of water introducing systems (the part of water introduced from the outside in the prior art for cleaning the materials is not required to be introduced in the invention) can be reduced, and the steam consumption is reduced.
Further, in the step 1), the temperature of the condensed water is 60-90 ℃, and the output quantity of the condensed water is 1-3.5 m/h when the condensed water is mixed with dust in hot air 3 The dust in the hot air is treated by a water pump to be 20-100kg/h per hour.
Further, in the step 2), the temperature of the supernatant is 40-50 ℃, and the flow rate of the supernatant is 0.5-1 m/h when the supernatant is mixed with the dedusting water 3 The mixing volume ratio of the supernatant to the dedusting water is 1:7-1:1.
the beneficial effect of adopting above-mentioned further scheme is that the sodium sulfate solid that rubber vacuum belt filter filtered falls into and contains solid-liquid two-phase S bucket, adds alkaline solution and adjusts pH, and then carries in the thickener through centrifugal pump and subsides thickening, and the material of thickening falls into the centrifuge through the pipeline and dewaters, and supernatant overflows back to S bucket, and the material after the centrifuge dewaters is through drying stoving moisture, and the mother liquor that the centrifuge got rid of flows back to in the S bucket. Because the water content of the material dehydrated by the centrifugal machine is lower than that of rubberThe water content of the filtered material and the introduction of part of alkali liquor into the S barrel of the vacuum belt filter can cause the volume increase of liquid phase substances in the S barrel. Therefore, the supernatant liquid can be used as the water for spraying the filtering material of the rubber vacuum belt filter together with dust removal water, and the flow is controlled to be 0.5-1m per hour 3 The volume of the liquid phase in the S-tub can be stabilized.
The supernatant overflowed by the thickener is saturated sodium sulfate solution with the temperature of 40-50 ℃ or solution with the temperature of 40-50 ℃ and a small amount of sodium sulfate solid, the concentration of sodium sulfate in the obtained solution is still at a higher level after the saturated sodium sulfate solution is mixed with dust removal water, and the sodium sulfate solid on the rubber belt type vacuum filter is cleaned by the saturated sodium sulfate solution, so that the acid bath adhered on the upper surface can be washed away, the filtered sodium sulfate solid can not be dissolved too much, and the material loss can not be caused.
Further, in the step 3), the spraying flow rate of the sodium sulfate solution formed after mixing is 1.5-4.5 m/hr 3 . By spraying means conventional in the art, such as spray heads, nozzles, etc. The sodium sulfate solution formed after mixing is sprayed and washed to wash sodium sulfate solids filtered by the rubber vacuum belt filter, and then the sodium sulfate solids are mixed with mother liquor of the rubber vacuum belt filter and discharged into an acid bath.
The other technical scheme for solving the technical problems is as follows: the utility model provides a dust removal water recycle's system in viscose staple fiber production process, its characterized in that, including dust remover, dust removal circulating pump, enrichment vessel, blender and washing spray set, the lower part intercommunication of dust remover has the outlet pipe, the middle part intercommunication of dust remover has inlet tube and intake pipe, the upper portion intercommunication of dust remover has the outlet duct, the outlet pipe with the import intercommunication of dust removal circulating pump, the export of dust removal circulating pump and the one end intercommunication of dust removal circulating spray pipeline, the other end of dust removal circulating spray pipeline stretch into to in the dust remover and be equipped with circulating spray set, circulating spray set is located the top of intake pipe, dust removal circulating spray pipeline still communicates with the one end of dust removal pump branch pipeline, the other end of dust removal pump branch pipeline with the blender intercommunication, the upper portion of enrichment vessel through enrichment vessel overflow pipeline with the blender intercommunication, the blender through spray pipeline with the belt cleaning spray set intercommunication.
The system uses condensed water produced after evaporation and condensation in the production process of viscose fiber as water of a water foam dust remover when anhydrous sodium sulphate is dried, and the condensed water is mixed with dust in hot air in a known spraying mode; filtering the materials by a rubber belt type vacuum filter, adding alkali into an S barrel, adjusting pH, conveying the materials into a thickener by a centrifugal pump for thickening, and mixing part of overflow supernatant with dust removal water; finally, the mixed sodium sulfate solution is sprayed on the surface of sodium sulfate solid on the rubber belt type vacuum filter in a known spraying mode, so as to reduce the acid bath amount adhered on the sodium sulfate solid.
Further, the dust remover is a foam dust remover, a liquid level meter is arranged on the dust remover, an automatic control valve is arranged on the water inlet pipe, and valves are arranged on the water outlet pipe, the dust removal circulating spray pipeline, the dust removal pump branch pipeline, the thickener overflow pipeline and the spray pipeline. The water inlet pipe can be further provided with a water pump for conveying condensed water.
The beneficial effect of adopting the further scheme is that the dust remover can be a well-known water foam dust remover, and the dust wrapped by hot air for drying sodium sulfate in the dust remover is mixed with condensed water in a well-known spraying mode. The invention also controls the liquid level in the dust remover through the liquid level meter and the self-control valve.
Further, the mixer is a preparation tank, a ball float valve for controlling the liquid level in the preparation tank is arranged on a dust removal pump branch pipeline, and a spray water pump is arranged on a spray water pipeline.
Further, the mixer is a venturi liquid-liquid mixer.
The beneficial effect of adopting the further scheme is that the supernatant liquid of the thickener and the dust-removing water are directly mixed, the dust-removing water is conveyed to the preparation tank or the Venturi liquid-liquid mixer by the dust-removing circulating pump to be mixed with the supernatant liquid of the thickener, and the mixture is conveyed to the cleaning spraying device, such as a belt filter spray pipe, etc., through a known spraying mode, the filtered material is cleaned.
Drawings
FIG. 1 is a schematic diagram of a mixer of the present invention as a compounding tank;
FIG. 2 is a schematic diagram of the structure of the venturi liquid-liquid mixer of the present invention.
In the drawings, the list of components represented by the various numbers is as follows:
1. the device comprises a water inlet pipe, 2, an automatic control valve, 3, a dust remover, 4, a liquid level meter, 5, a dust removal circulating pump, 6, a dust removal circulating spray pipeline, 7, a dust removal pump branch pipeline, 8, a ball float valve, 9, a preparation tank, 10, a thickener, 11, a valve, 12, a thickener overflow pipeline, 13, a spray water pump, 14, a spray water pipeline, 15, a cleaning spray device, 16, a venturi liquid-liquid mixer and 17, and a rubber belt type vacuum filter.
Detailed Description
The principles and features of the present invention are described below with examples given for the purpose of illustration only and are not intended to limit the scope of the invention.
The invention relates to a method for recycling dust-removing water in the production process of viscose staple fibers, which is characterized in that the dust-removing water generated in the production process of the viscose staple fibers is mixed with saturated sodium sulfate solution, and the acid bath on the surface of sodium sulfate solid on a rubber belt type vacuum filter 17 is cleaned by the dust-removing water.
The dust removing water is obtained by mixing water generated in the production process of the viscose staple fibers with anhydrous sodium sulphate materials, the water generated in the production process of the viscose staple fibers is condensed water generated after flash evaporation, heat exchange and condensation, pH neutral water recovered in the production or water containing sodium sulfate or zinc sulfate and having neutral pH, preferably the condensed water generated after flash evaporation, heat exchange and condensation, and the temperature is preferably 60-90 ℃. Flash evaporation is a process of an acid bath workshop, and in the operation process, steam in a flash evaporation heater is subjected to heat exchange and condensation to generate condensed water, and part of the water is collected and used for dust removal of anhydrous sodium sulfate. The anhydrous sodium sulfate material is anhydrous sodium sulfate material or dust in hot air generated by drying anhydrous sodium sulfate, preferably dust in hot air generated by drying anhydrous sodium sulfate. The saturated sodium sulfate solution is produced in the production of viscose fiber, and can be mother solution produced after dehydration of a centrifugal machine or supernatant liquid of the thickener 10, preferably supernatant liquid of the thickener 10. The cleaning mode is spraying or overflowing, preferably spraying.
When the invention adopts the preferable scheme, the following three conditions are required to be satisfied in the production of viscose fiber: 1. filtering solid sodium sulfate particles in the acid bath by adopting a rubber belt type vacuum filter 17; 2. treating sodium sulfate dust by adopting a water dust remover; 3. the concentration of sodium sulfate is increased by adopting a sedimentation and thickening method.
The invention meets the three conditions: the condensed water produced in the production of viscose is used for dust removal of a water foam dust remover, and then the supernatant liquid overflowed by the thickener 10 is mixed with dust removal water, and finally the mixture is used for washing sodium sulfate solid particles separated from acid bath by the rubber belt type vacuum filter 17, so that the consumption of water and steam is reduced, and the wastewater is discharged outwards.
The invention aims at realizing the invention by circulating the steps.
The method comprises the following specific steps:
(1) Dedusting by using condensate water generated in production: the condensed water at 60-90 ℃ generated after flash evaporation and condensation in the viscose fiber production process is used for 1-3.5 m/h 3 The amount of the sodium sulfate powder is conveyed into the dust remover 3 through conveying equipment (such as a water pump) and is mixed with dust in hot air generated by drying the sodium sulfate powder in a spraying mode, and the treatment amount of the dust (namely sodium sulfate) in the hot air is 20-100kg/h per hour.
(2) Mixing dust removal water with supernatant: mixing the dust-removing water generated after dust removal with part of supernatant overflowed from the thickener 10 by a conveying device (a dust-removing circulating pump 5), wherein the overflow amount of the supernatant of the thickener 10 is 0.5-1m 3 In the range of/h, the mixing volume ratio of the supernatant to the dedusting water is 1:7-1:1. the filtered material falls into an S barrel, alkali is added, the pH is adjusted, the filtered material is conveyed into a thickener 10 through a centrifugal pump to be thickened, and the supernatant overflows and reaches the temperature of 40-50 ℃.
(3) And (3) cleaning materials: spraying the mixed sodium sulfate solution on the surface of the material (i.e. sodium sulfate solid particles) filtered from the acid bath by a rubber belt type vacuum filter 17, and vacuum filtering according to the rubber belt typeThe acid bath content of the treated material of the machine 17 is controlled to control the water flow rate of spraying water to be 1.5-4.5m 3 In the range, the amount of acid bath adhered to the material is reduced.
The invention also relates to a system for recycling dust-removing water in the production process of viscose staple fibers, which comprises a dust remover 3, a dust-removing circulating pump 5, a thickener 10, a mixer and a cleaning spray device 15, wherein the lower part of the dust remover 3 is communicated with a water outlet pipe, the middle part of the dust remover 3 is communicated with a water inlet pipe 1 and an air inlet pipe, the upper part of the dust remover 3 is communicated with an air outlet pipe, the water outlet pipe is communicated with the inlet of the dust-removing circulating pump 5, the outlet of the dust-removing circulating pump 5 is communicated with one end of a dust-removing circulating spray pipe 6, the other end of the dust-removing circulating spray pipe 6 extends into the dust remover 3 and is provided with the circulating spray device, the circulating spray device is positioned above the air inlet pipe, the dust-removing circulating spray pipe 6 is also communicated with one end of a dust-removing pump branch pipe 7, the other end of the dust-removing pump branch pipe 7 is communicated with the mixer, the upper part of the thickener 10 is communicated with the mixer through a thickener overflow pipe 12, and the mixer is communicated with the cleaning spray device 15 through a spray pipe 14.
The system uses condensed water produced after evaporation and condensation in the production process of viscose fiber as water of a water foam dust remover when anhydrous sodium sulphate is dried, and the condensed water is mixed with dust in hot air in a known spraying mode; filtering the materials by a rubber belt type vacuum filter 17, adding alkali into an S barrel, adjusting the pH value, conveying the materials into a thickener 10 by a centrifugal pump for thickening, and mixing part of overflow supernatant with dust removal water; finally, the mixed sodium sulfate solution is sprayed on the surface of sodium sulfate solid on the rubber belt type vacuum filter 17 in a known spraying mode, so as to reduce the acid bath amount adhered on the sodium sulfate solid.
Preferably, the dust remover 3 is a foam dust remover, a liquid level meter 4 is arranged on the foam dust remover, an automatic control valve 2 is arranged on the water inlet pipe 1, and valves 11 are arranged on the water outlet pipe, the dust removal circulating spray pipeline 6, the dust removal pump branch pipeline 7, the thickener overflow pipeline 12 and the spray pipeline 14. The water inlet pipe 1 can be also provided with a water pump for conveying condensed water.
The dust remover 3 can be a well-known water foam dust remover, and dust wrapped by hot air for drying sodium sulfate in the dust remover 3 is mixed with condensed water in a well-known spraying mode. The invention also controls the liquid level in the dust remover 3 through the liquid level meter 4 and the automatic control valve 2, for example, an existing control system is adopted and is respectively connected with the liquid level meter 4 and the automatic control valve 2 in a communication way, and the control system controls the opening and closing and the opening of the automatic control valve 2 according to the liquid level information in the dust remover 3 monitored by the liquid level meter 4.
Preferably, the mixer is a preparation tank 9, a ball float valve 8 for controlling the liquid level in the preparation tank 9 is arranged on the dust removal pump branch pipeline 7, the liquid level in the preparation tank 9 is controlled through the ball float valve 8, and a spray water pump 13 is arranged on the spray water pipeline 14 and used for conveying sodium sulfate solution formed after mixing; alternatively, the mixer is a venturi liquid-liquid mixer 16.
The technical scheme and technical effects of the present invention are described below with examples and comparative examples:
example 1
This embodiment 1 is further described below with reference to fig. 1:
(1) Dedusting by using condensate water generated in production: about 3.5 m/hr is fed to the dust separator 3 via the water inlet pipe 1 3 The condensed water with the temperature of 90 ℃ is detected by a liquid level meter 4, the liquid level is maintained at about 60% by controlling the amount of the added condensed water by an automatic control valve 2, hot air generated by drying anhydrous sodium sulphate contacts with dust removing water in the dust remover 3, and the air volume of the hot air discharged into the dust remover 3 is 23000m 3 In the range of/h, the amount of dust carried by hot air is 100kg/h (i.e., the maximum dust handling capacity of the dust collector 3).
(2) Mixing of the liquids: when the liquid level of the liquid level meter 4 shows 60%, a valve 11 at the inlet of the dust removal circulating pump 5 is opened, the dust removal circulating pump 5 is started, the valve 11 of the dust removal circulating spray pipeline 6 is opened, and the valve 11 is kept normally open in operation. Opening a valve 11 of a dust removal pump branch pipeline 7, controlling the water inflow and the liquid level of a configuration tank 9 through a float valve 8, opening the valve 11 of a thickener overflow pipeline 12 of a thickener 10 when the liquid level is close to 50%, adjusting the flow according to the liquid level of an S barrel, and controlling the overflow amount to be 1m 3 In the range of/h, the water inflow is controlled through the float valve 8 to ensure that the liquid level is about 50%; the overflowed supernatant liquid temperature is 50 ℃, and the mixing volume ratio of the overflowed supernatant liquid to the dedusting water is 1:3.5.
(3) And (3) flushing materials: opening the valve 11 at the outlet of the preparation tank 9, starting the spray water pump 13, and adjusting the water quantity of the spray water pipeline 14 to be 4.5m by adjusting the valve 11 on the spray water pipeline 14 3 And/or so.
Example 2
Example 2 is further described below with reference to fig. 1:
(1) Dedusting by using condensate water generated in production: about 3.5 m/hr is fed to the dust separator 3 via the water inlet pipe 1 3 The condensed water with the temperature of 90 ℃ is detected by a liquid level meter 4, the liquid level is maintained at about 60% by controlling the amount of the added condensed water by an automatic control valve 2, hot air generated by drying anhydrous sodium sulphate contacts with dust removing water in the dust remover 3, and the air volume of the hot air discharged into the dust remover 3 is 23000m 3 In the range of/h, the amount of dust carried by hot air is 100kg/h (i.e., the maximum dust handling capacity of the dust collector 3).
(2) Mixing of the liquids: when the liquid level of the liquid level meter 4 shows 60%, a valve 11 at the inlet of the dust removal circulating pump 5 is opened, the dust removal circulating pump 5 is started, the valve 11 of the dust removal circulating spray pipeline 6 is opened, and the valve 11 is kept normally open in operation. Opening a valve 11 of a dust removal pump branch pipeline 7, controlling the water inflow and the liquid level of a configuration tank 9 through a float valve 8, opening the valve 11 of a thickener overflow pipeline 12 of a thickener 10 when the liquid level is close to 50%, adjusting the flow according to the liquid level of an S barrel, and controlling the overflow amount to be 0.5m 3 In the range of/h, the water inflow is controlled through the float valve 8 to ensure that the liquid level is about 50%; the overflowed supernatant liquid temperature is 50 ℃, and the mixing volume ratio of the overflowed supernatant liquid to the dedusting water is 1:7.
(3) And (3) flushing materials: opening the valve 11 at the outlet of the preparation tank 9, starting the spray water pump 13, and adjusting the water quantity of the spray water pipeline 14 to be 4m by adjusting the valve 11 on the spray water pipeline 14 3 And/or so.
Example 3
Example 3 is further described below with reference to fig. 2:
(1) Dedusting by using condensate water generated in production: about 1 m/hour of the feed to the dust collector 3 via the F3 water line 1 3 The condensed water with the temperature of 60 ℃ is detected by a liquid level meter 4, the liquid level is maintained at about 60% by controlling the amount of the added condensed water by an automatic control valve 2, hot air generated by drying anhydrous sodium sulphate contacts with dust removing water in the dust remover 3, and the air quantity of the hot air discharged into the dust remover 3 is 4000m 3 In the range of/h, the amount of dust carried by hot air is 20kg/h.
(2) Mixing of the liquids: when the liquid level of the liquid level meter 4 shows 60%, a valve 11 at the inlet of the dust removal circulating pump 5 is opened, the dust removal circulating pump 5 is started, the valve 11 of the dust removal circulating spray pipeline 6 is opened, and the valve 11 is kept normally open in operation. Opening the valve 11 of the dust removing pump branch pipeline 7, opening the valve 11 of the thickener overflow pipeline 12, and controlling the overflow amount to be 0.5m per hour 3 The dust-removing water and the supernatant liquid of the thickener 10 are gathered together into a Venturi liquid-liquid mixer 16; the overflowed supernatant liquid temperature is 40 ℃, and the mixing volume ratio of the overflowed supernatant liquid to the dedusting water is 1:2.
(3) And (3) flushing materials: opening a valve 11 on a spray water pipeline 14, and controlling the flow of the dedusting pump branch pipeline 7 to be 1.5m through the valve 11 on the dedusting pump branch pipeline 7 3 And/or so.
Example 4
Example 4 is further described below with reference to fig. 2:
(1) Dedusting by using condensate water generated in production: about 1 m/hour of the feed to the dust collector 3 via the F3 water line 1 3 The condensed water with the temperature of 60 ℃ is detected by a liquid level meter 4, the liquid level is maintained at about 60% by controlling the amount of the added condensed water by an automatic control valve 2, hot air generated by drying anhydrous sodium sulphate contacts with dust removing water in the dust remover 3, and the air quantity of the hot air discharged into the dust remover 3 is 4000m 3 In the range of/h, the amount of dust carried by hot air is 20kg/h.
(2) Mixing of the liquids: when the liquid level of the liquid level meter 4 shows 60%, a valve 11 at the inlet of the dedusting circulating pump 5 is opened, the dedusting circulating pump 5 is started, a valve 11 of the dedusting circulating spray pipeline 6 is opened, and the valve 11 is arranged at the position ofThe operation is kept normally open. Opening the valve 11 of the dust removing pump branch pipeline 7, opening the valve 11 of the thickener overflow pipeline 12, and controlling the overflow amount to be 1m per hour 3 The dust-removing water and the supernatant liquid of the thickener 10 are gathered together into a Venturi liquid-liquid mixer 16; the overflowed supernatant liquid temperature is 40 ℃, and the mixing volume ratio of the overflowed supernatant liquid to the dedusting water is 1:1.
(3) And (3) flushing materials: opening a valve 11 on a spray water pipeline 14, and controlling the flow of the dedusting pump branch pipeline 7 to be 2m through the valve 11 on the dedusting pump branch pipeline 7 3 And/or so.
Example 5
Example 5 is further described below with reference to fig. 1:
(1) Dedusting by using condensate water generated in production: about 2.5 m/hr is fed to the dust separator 3 via the water inlet pipe 1 3 The recovered centrifuge cooling water with the temperature of 75 ℃ is detected by a liquid level meter 4, the amount and the liquid level of the added centrifuge cooling water are controlled by an automatic control valve 2, hot air generated by drying anhydrous sodium sulphate contacts with production water in the dust remover 3, and the air volume of the hot air discharged into the dust remover 3 is 12000m 3 In the range of/h, the amount of dust carried by hot air is 60kg/h.
(2) Mixing of the liquids: when the liquid level of the liquid level meter 4 shows 60%, a valve 11 at the inlet of the dust removal circulating pump 5 is opened, the dust removal circulating pump 5 is started, the valve 11 of the dust removal circulating spray pipeline 6 is opened, and the valve 11 is kept normally open in operation. Opening a valve 11 of a dust removal pump branch pipeline 7, controlling the water inflow and the liquid level of a configuration tank 9 through a float valve 8, opening the valve 11 of a thickener overflow pipeline 12 of a thickener 10 when the liquid level is close to 50%, adjusting the flow according to the liquid level of an S barrel, and controlling the overflow amount to be 0.8m 3 In the range of/h, the water inflow is controlled through the float valve 8 to ensure that the liquid level is about 50%; the overflow supernatant liquid temperature is 45 ℃, and the mixing volume ratio of the overflow supernatant liquid and the dedusting water is 0.8:2.5.
(3) And (3) flushing materials: opening the valve 11 at the outlet of the preparation tank 9, starting the spray water pump 13, and adjusting the water quantity of the spray water pipeline 14 to be 3.3m by adjusting the valve 11 on the spray water pipeline 14 3 And/or so.
Example 6
This embodiment 6 is further described below with reference to fig. 1:
(1) Dedusting by using condensate water generated in production: about 3.5 m/hr is fed to the dust separator 3 via the water inlet pipe 1 3 The liquid level in the dust remover 3 is detected by a liquid level meter 4, the quantity and the liquid level of the recovered centrifugal pump sealing water are controlled by an automatic control valve 2, hot air generated by drying anhydrous sodium sulphate contacts with production water in the dust remover 3, and the air quantity of the hot air discharged into the dust remover 3 is 12000m 3 In the range of/h, the amount of dust carried by hot air is 20kg/h.
(2) Mixing of the liquids: when the liquid level of the liquid level meter 4 shows 60%, a valve 11 at the inlet of the dust removal circulating pump 5 is opened, the dust removal circulating pump 5 is started, the valve 11 of the dust removal circulating spray pipeline 6 is opened, and the valve 11 is kept normally open in operation. Opening a valve 11 of a dust removal pump branch pipeline 7, controlling the water inflow and the liquid level of a configuration tank 9 through a float valve 8, opening the valve 11 of a thickener overflow pipeline 12 of a thickener 10 when the liquid level is close to 50%, adjusting the flow according to the liquid level of an S barrel, and controlling the overflow amount to be 0.8m 3 In the range of/h, the water inflow is controlled through the float valve 8 to ensure that the liquid level is about 50%; the overflow supernatant liquid temperature is 45 ℃, and the mixing volume ratio of the overflow supernatant liquid and the dedusting water is 0.8:3.5.
(3) And (3) flushing materials: opening the valve 11 at the outlet of the preparation tank 9, starting the spray water pump 13, and adjusting the water quantity of the spray water pipeline 14 to be 4.3m by adjusting the valve 11 on the spray water pipeline 14 3 And/or so.
Comparative example 1
This comparative example uses prior art, spraying on a rubber belt vacuum filter directly uses process water that would dissolve sodium sulfate solids in use. And the dust-removing water produced by drying is directly discharged, and supernatant fluid of the thickener directly overflows into an acid bath.
And (3) result comparison:
the original technology directly sprays production water to a rubber belt type vacuum filter, dust-removing water is directly discharged, and supernatant liquid of a thickener directly overflows into an acid bath. The rubber is prepared by the original process per hourSpraying 4.5m for belt type vacuum filter 3 The produced water of (2) needs to be directly evaporated after being discharged into a system, 0.33 ton of steam is needed for evaporating 1 ton of water by the system, 4.5 multiplied by 0.33 ton/hour of steam consumption is needed, 3.5 cubic meters of dust-removing water is discharged, 3.5 multiplied by 1 ton/hour of wastewater treatment is increased, and corresponding steam consumption is also needed to be increased when supernatant liquor of a thickener overflows into an acid bath. Because the production water is used for spraying, the production water can dissolve the anhydrous sodium sulphate, and the dissolved anhydrous sodium sulphate is separated out from the system again to cause steam consumption.
With the process of the invention, the system only needs to evaporate 3.5 tons of water per hour and add 1m 3 Compared with the prior art, the method reduces the evaporation capacity of 1 ton of water, reduces the steam consumption by 1 multiplied by 0.33 ton/hour, reduces the water consumption of 3.5 cubic meters/hour and 3.5 cubic meters/hour of discharged sewage, reduces the loss of 100kg of sodium sulfate along with dust removal water per hour, increases the yield of the anhydrous sodium sulfate by 100 kg/hour, and reduces the 0.04 ton steam consumption increased by dissolving the anhydrous sodium sulfate because of reducing the dissolution of the anhydrous sodium sulfate by using the sodium sulfate-containing solution.
While embodiments of the present invention have been shown and described above, it will be understood that the above embodiments are illustrative and not to be construed as limiting the invention, and that variations, modifications, alternatives and variations may be made to the above embodiments by one of ordinary skill in the art within the scope of the invention.
The above examples merely represent one embodiment of the present invention and are not to be construed as limiting the scope of the present invention. It should be noted that it will be apparent to those skilled in the art that several variations and modifications can be made without departing from the spirit of the invention, which are all within the scope of the invention.
Claims (8)
1. The method for recycling the dust removal water in the production process of the viscose staple fibers is characterized by comprising the following steps of: 1) Dedusting by using condensate water generated in production: the condensed water generated after flash evaporation, heat exchange and condensation in the viscose fiber production process is mixed with dust in hot air generated by drying anhydrous sodium sulfate in a spraying mode to obtain dust removal water; 2) Mixing dust removal water with supernatant: adding alkali into the material filtered by the rubber belt type vacuum filter to adjust the pH value, conveying the material into a thickener for thickening, and mixing part of overflowed supernatant with dust removal water; 3) And (3) cleaning materials: spraying the sodium sulfate solution formed after mixing on the surface of sodium sulfate solid on a rubber belt type vacuum filter, and cleaning acid bath adhered on the sodium sulfate solid.
2. The method for recycling dedusting water in a viscose staple fiber production process according to claim 1, wherein in the step 1), the temperature of the condensed water is 60-90 ℃, and the output of the condensed water is 1-3.5 m/h when the condensed water is mixed with dust in hot air 3 The dust in the hot air is treated with 20-100kg/h per hour.
3. The method for recycling dedusting water in the production process of viscose staple fiber according to claim 1, wherein in the step 2), the temperature of the supernatant is 40-50 ℃, and the flow rate of the supernatant is 0.5-1 m/h when the supernatant is mixed with dedusting water 3 The mixing volume ratio of the supernatant to the dedusting water is 1:7-1:1.
4. the method for recycling dedusting water in the production process of viscose staple fiber according to claim 1, wherein in the step 3), the spraying flow rate of the sodium sulfate solution formed after mixing is 1.5-4.5 m/hr 3 。
5. A system for realizing the method of dust removal water recycle in viscose staple fiber production process according to any one of claims 1 to 4, characterized in that the system comprises a dust remover (3), a dust removal circulating pump (5), a thickener (10), a mixer and a cleaning spray device (15), wherein a water outlet pipe is communicated with the lower part of the dust remover (3), a water inlet pipe (1) and an air inlet pipe are communicated with the middle part of the dust remover (3), an air outlet pipe is communicated with the upper part of the dust remover (3), the water outlet pipe is communicated with the inlet of the dust removal circulating pump (5), the outlet of the dust removal circulating pump (5) is communicated with one end of a dust removal circulating spray pipeline (6), the other end of the dust removal circulating spray pipeline (6) extends into the dust remover (3) and is provided with a circulating spray device, the circulating spray device is positioned above the air inlet pipe, the dust removal circulating spray pipeline (6) is also communicated with one end of a dust removal pump branch pipeline (7), the other end of the dust removal pump pipeline (7) is communicated with the mixer, the upper part of the dust removal circulating pump (5) is communicated with the mixer through the thickener (12) and the thickener (14) through the thickener (14).
6. The system for recycling the dust-removing water in the viscose staple fiber production process according to claim 5, wherein the dust remover (3) is a foam dust remover, a liquid level meter (4) is arranged on the dust remover, an automatic control valve (2) is arranged on the water inlet pipe (1), and valves (11) are arranged on the water outlet pipe, the dust-removing circulating spray pipeline (6), the dust-removing pump branch pipeline (7), the thickener overflow pipeline (12) and the spray water pipeline (14).
7. The system for recycling dedusting water in the viscose staple fiber production process according to claim 5 or 6, wherein the mixer is a preparation tank (9), a ball float valve (8) for controlling the liquid level in the preparation tank (9) is arranged on the dedusting pump branch pipeline (7), and a spray water pump (13) is arranged on the spray water pipeline (14).
8. A system for recycling of dust-removing water in a viscose staple fiber production process according to claim 5 or 6, characterized in that said mixer is a venturi liquid-liquid mixer (16).
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| CN113955773A (en) * | 2021-11-05 | 2022-01-21 | 唐山三友集团兴达化纤有限公司 | Separation system and method for sodium sulfate in modal fiber acid bath |
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| CN1070129A (en) * | 1992-07-15 | 1993-03-24 | 江西省纺织工业科研设计院 | Exhaust gas treatment method and device during viscose rayon is produced |
| CN202220084U (en) * | 2011-08-19 | 2012-05-16 | 邵明福 | Production equipment directly extracting sodium sulphate by acid bath |
| CN202576677U (en) * | 2012-02-17 | 2012-12-05 | 杭州奥通科技有限公司 | Silicon nitrogen serial flame-retardant viscose staple fiber production line |
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