CN103351041A - Electrodialysis alkali recovery technology during viscose fiber production - Google Patents
Electrodialysis alkali recovery technology during viscose fiber production Download PDFInfo
- Publication number
- CN103351041A CN103351041A CN2013103117794A CN201310311779A CN103351041A CN 103351041 A CN103351041 A CN 103351041A CN 2013103117794 A CN2013103117794 A CN 2013103117794A CN 201310311779 A CN201310311779 A CN 201310311779A CN 103351041 A CN103351041 A CN 103351041A
- Authority
- CN
- China
- Prior art keywords
- electrodialysis
- viscose fiber
- alkali
- produced
- alkali recovery
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Abstract
The invention provides an electrodialysis alkali recovery technology during viscose fiber production, which is characterized by comprising the steps that pretreated waste alkali liquor and de-mineralized water at a flow ratio of (1-2):1 enter a membrane module by a pump, and are conveyed to an electrodialysis membrane module device for alkali liquor electrodialysis recovery, wherein a concentration of sodium hydroxide of the pretreated waste alkaline liquor is 50-200g/L, and the content of hemicellulose is 20-150g/L. According to the characteristic that high-concentration waste alkaline liquor containing the hemicellulose is generated during a viscose fiber production course, an optimized technological parameter is selected, so that the electrodialysis alkali recovery technology has the advantages of high alkali recovery rate, low energy consumption and stability in operation.
Description
Technical field
The present invention relates to a kind of alkali recovery process, be specifically related to the electrodialysis alkali recovery process in a kind of viscose fiber production, belong to the Waste recovery technical field in the viscose fiber production.
Background technology
Viscose fiber is the man-made fiber that utilizes process the chemistry such as the macromolecular material wood pulp contain natural cellulose, cotton pulp and mechanical means to process.Viscose fiber is the kind that approaches the most with the natural fiber clothes performance in the chemical fibre, have soft, moisture absorption is breathed freely, it is elegant to overhang, bright-coloured, the antistatic characteristics such as textile process that are easy to of dyeing, yet being to come from the sky to be better than natural regenerated cellulose fibre, is one of important materials of textile industry raw material.China has about 40 of viscose fiber enterprise at present, and except production common viscose fiber (long filament, staple fibre) and high-tenacity fibre, the viscose fiber of high wet modulus fibrid and special property also has production.
Need a large amount of industrial chemicals in the production process of viscose fiber, can produce a large amount of waste water, these waste water contain sulfuric acid, zinc sulfate, dithiocarbonic anhydride, Mierocrystalline cellulose, dissolved organic matter etc., all environment are produced very large harm, are one of primary pollution source of textile industry.
In production process of viscose fiber, need to by dipping method the hemicellulose in the raw material be dissolved out with alkaline solution, otherwise can produce extremely adverse influence to production technique and final product quality.Therefore, when producing viscose fiber, the press lye treating plant need to be set in process procedure, from the steeping lye system, separate a certain amount of hemicellulose.And can produce the high density salkali waste contain hemicellulose in the steeping process, and for reducing production costs, reducing alkaline consumption, each chemical fiber factory mainly adopts dialysis technique to separate half fibre to carry out recycle of alkali liquor at present.But dialysis technique reclaims the alkali lye inefficiency, and water consumption is large, and takies larger floor area of building, progressively eliminates.The membrane filtration alkali recovery technology that develops rapidly in recent years is expected to replace dialysis technique and carries out recycle of alkali liquor, improves the quality of products and the waste water utilization rate.
201210486339.8, name is called the application for a patent for invention of " secondary treatment method of discarded alkali lye in a kind of viscose fiber production ", this patent will be through conventional pretreated, naoh concentration is 70 ~ 90g/L, discarded alkali lye and the de-mineralized water of half fibre content, 60 ~ 70g/L are delivered to respectively the diffusion dialysis membrane stack, carry out diffusion dialysis, the throughput ratio of described pre-treatment waste lye and de-mineralized water is 1 ~ 2:1, the alkali lye that will hang down hemicellulose concentration after the diffusion dialysis separates with the alkali lye of height half fine concentration, and the alkali lye of described low hemicellulose concentration is back to production.The shortcoming of this patent is: the rate of recovery of diffusion dialysis is not high, and can not well separate with xylogen alkali.
Summary of the invention
The present invention is directed to the problem that salkali waste reclaims in the viscose fiber production, proposed a kind of electrodialysis alkali recovery process that is applicable in the viscose fiber production.According to the characteristic that produces the high density salkali waste contain hemicellulose in the production process of viscose fiber, select the processing parameter optimized, make it to have the alkali recovery height, low, the stable advantage of energy consumption.
For achieving the above object, the present invention adopts following technical scheme:
Electrodialysis alkali recovery process during a kind of viscose fiber is produced, it is characterized in that: waste lye after pretreatment and de-mineralized water are entered membrane module by the throughput ratio of 1 ~ 2:1 by pump be delivered to the electrodialysis film group device, carry out electrodialysis and reclaim alkali lye, described waste lye naoh concentration after pretreatment is 50 ~ 200g/L, and half fibre content is 20 ~ 150g/L.
Described waste lye and de-mineralized water enter the electrodialysis film group device in the mode of cross-flow.
Described electrodialytic temperature is 15 ~ 45 ℃.
The gauge pressure of described pump is 0.03 ~ 0.08Mpa, and pressure is excessive, and significantly shorten the work-ing life of film, and cost raises.
The flow control flux of alkaline liquor guarantees the concentration difference of film front and back solution greater than the de-mineralized water flow.Flux of alkaline liquor is 200 ~ 800L/h, and the de-mineralized water flow is 160 ~ 600L/h.
Described electrodialysis impressed DC voltage, magnitude of voltage are 40V, and current value is 92A, and interelectrode distance is 10cm, is conducive to promote dialysis efficiency.
The present invention recycles the enrichment alkali that the electrodialysis cathode compartment obtains, and the anolyte compartment contains the waste liquid acid neutralization of hemicellulose, and the Precipitation hemicellulose filters, and obtains hemicellulose as fermentation raw material.
Acid neutralization to pH value is 2 ~ 5.
Described acid is that concentration is the sulfuric acid of 0.1 ~ 2.5mol/L.
In the described electrodialysis process, the concentration of lye of holding anode chamber waste liquid is 8 ~ 15g/L.In electrodialysis process, with the Ph value reduction of waste liquid, anolyte compartment's xylogen gradates as the colloidal lignin and separates out, and causes easily stifled groove, and system resistance is increased.
Describedly separate out filtrate behind the hemicellulose through reverse osmosis, obtain de-mineralized water and recycle.
Described film group device uses is many to anion and cation exchange membrane pair, and the distance between the anion and cation exchange membrane is 0.1 ~ 0.2mm.Selecting this distance is in order to increase Reynolds number, to increase spread coefficient, improving velocity of diffusion.
Recovery concentration of lye after electrodialysis is 40 ~ 420g/L, contains partly fine in 10g/L.
Recycle of alkali liquor rate of the present invention is 60% ~ 85%.
Power consumption of the present invention is 800 ~ 2000 degree electricity/ton alkali.
Beneficial effect of the present invention is:
1, the present invention adopts the electrodialysis alkali recovery process to process the waste lye of viscose fiber in producing, and the equipment cost of technique is low, and technical process is simple, and production efficiency is high, and not only the rate of recovery of alkali is high, can also be simultaneously half in the waste liquid be finely separated well with alkali.
2, owing to can produce the high density salkali waste that contains hemicellulose in the production process of viscose fiber, according to this characteristic, the present invention has selected the special process parameter system of optimizing, and is conducive to promote electrodialytic efficient, thereby effectively guarantees the rate of recovery of alkali.
3, the present invention controls flux of alkaline liquor greater than the de-mineralized water flow, and flux of alkaline liquor is 200 ~ 800L/h, and the de-mineralized water flow is 160 ~ 600L/h, guarantees the concentration difference of film front and back solution, thereby has guaranteed electrodialytic infiltration efficient.
4, will to control the concentration of lye of anolyte compartment's waste liquid be in the scope of 8 ~ 15g/L in the present invention, and avoiding anolyte compartment's lignin conversion is that the colloidal lignin is separated out, and causes stifled groove, and system resistance is increased, and helps to reduce energy consumption, saves cost.
5, the present invention recycles the enrichment alkali that the electrodialysis cathode compartment obtains, the anolyte compartment contains the waste liquid acid neutralization of hemicellulose, the Precipitation hemicellulose, filter, obtain hemicellulose and can be used as fermentation raw material, simultaneously, filtrate is reclaimed de-mineralized water through reverse osmosis, to the recycling of resource, effectively saved the energy, have very large environment protection significance.
Embodiment
Below in conjunction with embodiment essentiality content of the present invention is described in further detail.
Embodiment 1
Electrodialysis alkali recovery process during a kind of viscose fiber is produced, waste lye after pretreatment and de-mineralized water are entered membrane module by the throughput ratio of 1:1 by pump be delivered to the electrodialysis film group device, carry out electrodialysis and reclaim alkali lye, described waste lye naoh concentration after pretreatment is 50 g/L, and half fibre content is 30 g/L.
Embodiment 2
Electrodialysis alkali recovery process during a kind of viscose fiber is produced, waste lye after pretreatment and de-mineralized water are entered membrane module by the throughput ratio of 2:1 by pump be delivered to the electrodialysis film group device, carry out electrodialysis and reclaim alkali lye, described waste lye naoh concentration after pretreatment is 90 g/L, and half fibre content is 20 g/L.
Described waste lye and de-mineralized water enter the electrodialysis film group device in the mode of cross-flow.
Embodiment 3
Electrodialysis alkali recovery process during a kind of viscose fiber is produced, waste lye after pretreatment and de-mineralized water are entered membrane module by the throughput ratio of 1.5:1 by pump be delivered to the electrodialysis film group device, carry out electrodialysis and reclaim alkali lye, described waste lye naoh concentration after pretreatment is 200g/L, and half fibre content is 150 g/L.
Described waste lye and de-mineralized water enter the electrodialysis film group device in the mode of cross-flow.
Embodiment 4
Electrodialysis alkali recovery process during viscose fiber is produced, waste lye after pretreatment and de-mineralized water are entered membrane module by the throughput ratio of 1.2:1 by pump be delivered to the electrodialysis film group device, carry out electrodialysis and reclaim alkali lye, described waste lye naoh concentration after pretreatment is 150g/L, and half fibre content is 100 g/L.
Described waste lye and de-mineralized water enter the electrodialysis film group device in the mode of cross-flow.
Embodiment 5
Present embodiment is substantially the same manner as Example 4, on this basis:
Described electrodialytic temperature is 30 ℃.
The gauge pressure of described pump is 0.05Mpa.
Embodiment 6
Present embodiment is substantially the same manner as Example 4, on this basis:
Described electrodialytic temperature is 15 ℃.
The gauge pressure of described pump is 0.03Mpa.
Flux of alkaline liquor is 500L/h, and the de-mineralized water flow is 400L/h.
Embodiment 7
Present embodiment is substantially the same manner as Example 4, on this basis:
Described electrodialytic temperature is 45 ℃.
The gauge pressure of described pump is 0.08Mpa.
Flux of alkaline liquor is 200L/h, and the de-mineralized water flow is 160L/h.
Described electrodialysis impressed DC voltage, magnitude of voltage are 40V, and current value is 92A, and interelectrode distance is 10cm.
Embodiment 8
Present embodiment is substantially the same manner as Example 4, on this basis:
Described electrodialytic temperature is 25 ℃.
The gauge pressure of described pump is 0.06Mpa.
Flux of alkaline liquor is 800L/h, and the de-mineralized water flow is 600L/h.
Described electrodialysis impressed DC voltage, magnitude of voltage are 40V, and current value is 92A, and interelectrode distance is 10cm.
Embodiment 9
Present embodiment is substantially the same manner as Example 8, on this basis:
The enrichment alkali that the electrodialysis cathode compartment obtains is recycled, and the anolyte compartment contains the waste liquid acid neutralization of hemicellulose, and the Precipitation hemicellulose filters, and obtains hemicellulose as fermentation raw material.
Recovery concentration of lye after electrodialysis is 250g/L, contains half fine 8g/L.
The recycle of alkali liquor rate is 82%.
Power consumption is 1200 degree electricity/ton alkali.
Embodiment 10
Present embodiment is substantially the same manner as Example 9, on this basis:
Acid neutralization to pH value is 2.
Described acid is that concentration is the sulfuric acid of 0.1mol/L.
In the described electrodialysis process, the concentration of lye of anolyte compartment's waste liquid is 8g/L.
Recovery concentration of lye after electrodialysis is 100g/L, contains half fine 8g/L.
The recycle of alkali liquor rate is 80%.
Power consumption is 1800 degree electricity/ton alkali.
Embodiment 11
Present embodiment is substantially the same manner as Example 9, on this basis:
Acid neutralization to pH value is 5.
Described acid is that concentration is the sulfuric acid of 2.5mol/L.
In the described electrodialysis process, the concentration of lye of anolyte compartment's waste liquid is 15g/L.
Describedly separate out filtrate behind the hemicellulose through reverse osmosis, obtain de-mineralized water and recycle.
Recovery concentration of lye after electrodialysis is 40g/L, contains half fine 8g/L.
The recycle of alkali liquor rate is 75%.
Power consumption is 1000 degree electricity/ton alkali.
Embodiment 12
Present embodiment is substantially the same manner as Example 9, on this basis:
Acid neutralization to pH value is 4.
Described acid is that concentration is the sulfuric acid of 1.5mol/L.
In the described electrodialysis process, the concentration of lye of anolyte compartment's waste liquid is 10g/L.
Describedly separate out filtrate behind the hemicellulose through reverse osmosis, obtain de-mineralized water and recycle.
Recovery concentration of lye after electrodialysis is 420 g/L, contains half fine 9g/L.
The recycle of alkali liquor rate is 60%.
Power consumption is 2000 degree electricity/ton alkali.
Embodiment 13
Present embodiment is substantially the same manner as Example 9, on this basis:
Acid neutralization to pH value is 3.
Described acid is that concentration is the sulfuric acid of 0.8 mol/L.
In the described electrodialysis process, the concentration of lye of anolyte compartment's waste liquid is 12g/L.
Describedly separate out filtrate behind the hemicellulose through reverse osmosis, obtain de-mineralized water and recycle.
Recovery concentration of lye after electrodialysis is 250 g/L, contains half fine 8.5g/L.
The recycle of alkali liquor rate is 85%.
Power consumption is 800 degree electricity/ton alkali.
Embodiment 14
Present embodiment is substantially the same manner as Example 13, on this basis:
Described film group device uses is many to anion and cation exchange membrane pair, and the distance between the anion and cation exchange membrane is 0.1mm.
Recovery concentration of lye after electrodialysis is 280g/L, contains half fine 7.5g/L.
The recycle of alkali liquor rate is 78%.
Power consumption is 800 degree electricity/ton alkali.
Embodiment 15
Present embodiment is substantially the same manner as Example 13, on this basis:
Described film group device uses is many to anion and cation exchange membrane pair, and the distance between the anion and cation exchange membrane is 0.2mm.
Recovery concentration of lye after electrodialysis is 320 g/L, contains half fine 7g/L.
The recycle of alkali liquor rate is 82%.
Power consumption is 1000 degree electricity/ton alkali.
Embodiment 16
Present embodiment is substantially the same manner as Example 13, on this basis:
Described film group device uses is many to anion and cation exchange membrane pair, and the distance between the anion and cation exchange membrane is 0.15mm.
Recovery concentration of lye after electrodialysis is 360g/L, contains half fine 8.2g/L.
The recycle of alkali liquor rate is 80%.
Power consumption is 900 degree electricity/ton alkali.
Embodiment 17
Present embodiment is substantially the same manner as Example 16, on this basis:
Described pre-treatment is the pretreatment technology that pressed liquor electrodialysis alkali reclaimed during viscose fiber was produced: NaOH content is that the pressed liquor of 150g/L is removed oarse-grained material by the method for electricity flocculation first, then enter millipore filter by pump, filtrate pumps into the diffusion dialysis film separating system again, the gained dialyzate is alkali lye, reclaim alkali lye, concentrated solution is that pretreated pressed liquor is used for follow-up electrodialysis process.
The electrode of described electricity flocculation is iron-carbon dioxide process carbon electrode.
The polar plate spacing of described electricity flocculation is 0.8m, and voltage is 260V.
The pressed liquor flow of described electricity flocculation is 90L/h.
The stirring velocity of described electricity flocculation is 150r/min, time 15min.
The membrane pore size of described millipore filter is 20 μ m.
Described diffusion dialysis refers to, pressed liquor after will filtering respectively and de-mineralized water enter membrane module by pump and are delivered to the diffusion dialysis membrane stack, pressed liquor and de-mineralized water are that convection current is passed through, and obtain sig water after diffusion dialysis, and the pressed liquor after the described filtration and the throughput ratio of de-mineralized water are 1:1.
The film that described diffusion dialysis is used is many cationic exchange membranes, and the distance between the cationic exchange membrane is 0.9mm.
The gauge pressure of described pump is 0.03Mpa.
Described pressed liquor flow is 70 ~ 90L/h, and the flow of water is 50 ~ 70L/h.
Embodiment 18
Present embodiment is substantially the same manner as Example 16, on this basis:
Described pre-treatment is the pretreatment technology that pressed liquor electrodialysis alkali reclaimed during viscose fiber was produced: NaOH content is that the pressed liquor of 162g/L is removed oarse-grained material by prefilter first, then enter millipore filter by pump, filtrate is reclaimed xylogen and is held back the pollutent of macromolecule through ultrafiltration again, obtains sig water and is used for follow-up electrodialysis process.
The aperture of described prefilter is 20 μ m.
Filtrate in the described prefilter is fibrous nodules, and the raw material of fibrous nodules is high hydroformylation dimension synthetic fibre and set polyester fibre.
The sphere diameter 30mm of described fibrous nodules, ball density 1.3kg/m
3, pack density is 80kg/m.
The flow velocity of described prefilter is 10m/h.
Described prefilter, when the Pressure Drop of pressed liquor by filter core greater than 0.08Mpa, namely filter core is cleaned.
The service temperature of described millipore filter is 20 ℃, and pressure is 0.1Mpa.
The membrane pore size of described millipore filter is 0.1 μ m.
What described ultra-filtration membrane separation system was used is tubular fibre formula membrane module.
The service temperature of described ultrafiltration is that temperature is 20 ℃, and pressure is 0.05Mpa.
Described ultrafiltration, the flow of pressed liquor are 90 L/h.
The membrane pore size of described ultra-filtration membrane is 0.001 μ m.
Embodiment 19
Present embodiment is substantially the same manner as Example 16, on this basis:
Described pre-treatment is the pretreatment technology that pressed liquor electrodialysis alkali reclaimed during viscose fiber was produced, NaOH content is that the pressed liquor of 182g/L filters out oarse-grained impurity by flame filter press first, enter membrane module by pump again and be delivered to the diffusion dialysis membrane stack, obtain sig water and be used for follow-up electrodialysis process.
The density of filter cloth is 1150g/m in the described flame filter press
2
The working pressure of described flame filter press is 0.2Mpa, and flow is 20m
3/ (h*m
2).
The filter cloth surface of described flame filter press scribbles diatomite.
Diatomaceous thickness is 2mm.
Described diffusion dialysis refers to, pressed liquor after will filtering respectively and de-mineralized water enter membrane module by pump and are delivered to the diffusion dialysis membrane stack, pressed liquor and de-mineralized water are that convection current is passed through, and obtain sig water after diffusion dialysis, and the pressed liquor after the described filtration and the throughput ratio of de-mineralized water are 2:1.
The film that described diffusion dialysis is used is many cationic exchange membranes, and the distance between the cationic exchange membrane is 0.9mm.
The gauge pressure of described pump is 0.03Mpa.
Described pressed liquor flow is 75L/h, and the flow of water is 60L/h.
Embodiment 20
Present embodiment is substantially the same manner as Example 16, on this basis:
Described pre-treatment is the pretreatment technology that pressed liquor electrodialysis alkali reclaimed during viscose fiber was produced, NaOH content is that the pressed liquor of 173g/L filters out oarse-grained impurity by flame filter press first, enter millipore filter by pump again, obtain sig water and be used for follow-up electrodialysis process.
The density of filter cloth is 1150g/m in the described flame filter press
2
The working pressure of described flame filter press is 0.2Mpa, and flow is 20m
3/ (h*m
2).
The filter cloth surface of described flame filter press scribbles diatomite.
Diatomaceous thickness is 2mm.
The service temperature of described millipore filter is 30 ℃, and pressure is 0.2Mpa.
The membrane pore size of described millipore filter is 0.15 μ m.
Described millipore filter, when the Pressure Drop of pressed liquor by filter core greater than 0.08Mpa, namely filter core is cleaned.
Embodiment 21
Present embodiment is substantially the same manner as Example 16, on this basis:
Described pre-treatment is the pretreatment technology that pressed liquor electrodialysis alkali reclaimed during viscose fiber was produced, NaOH content is that the pressed liquor of 186g/L filters out oarse-grained impurity by prefilter first, reclaim xylogen and hold back the pollutent of macromolecule through ultrafiltration again, the liquid that sees through that gained contains NaOH is used for follow-up electrodialysis process.
The aperture of described prefilter is 20 μ m.
Filtrate in the described prefilter is fibrous nodules, and the raw material of fibrous nodules is high hydroformylation dimension synthetic fibre and set polyester fibre.
The sphere diameter 28mm of described fibrous nodules, ball density 1.26kg/m
3, pack density is 78kg/m.
The flow velocity of described prefilter is 9m/h.
Described prefilter, when the Pressure Drop of pressed liquor by filter core greater than 0.08Mpa, namely filter core is cleaned.
What described ultra-filtration membrane separation system was used is tubular fibre formula membrane module.
The service temperature of described ultrafiltration is that temperature is 20 ℃, and pressure is 0.05Mpa.
Described ultrafiltration, the flow of pressed liquor are 80L/h.
The membrane pore size of described ultra-filtration membrane is 0.02 μ m.
Claims (10)
1. the electrodialysis alkali recovery process during a viscose fiber is produced, it is characterized in that: waste lye after pretreatment and de-mineralized water are entered membrane module by the throughput ratio of 1 ~ 2:1 by pump be delivered to the electrodialysis film group device, carry out electrodialysis and reclaim alkali lye, described waste lye naoh concentration after pretreatment is 50 ~ 200g/L, and half fibre content is 20 ~ 150g/L.
2. the electrodialysis alkali recovery process during a kind of viscose fiber according to claim 1 is produced, it is characterized in that: described waste lye and de-mineralized water enter the electrodialysis film group device in the mode of cross-flow.
3. the electrodialysis alkali recovery process during a kind of viscose fiber according to claim 1 is produced, it is characterized in that: described electrodialytic temperature is 15 ~ 45 ℃, the gauge pressure of pump is 0.03 ~ 0.08Mpa.
4. the electrodialysis alkali recovery process during a kind of viscose fiber according to claim 1 is produced, it is characterized in that: described waste lye flow is greater than the de-mineralized water flow, and flux of alkaline liquor is 200 ~ 800L/h, and the de-mineralized water flow is 160 ~ 600L/h.
5. the electrodialysis alkali recovery process during a kind of viscose fiber according to claim 1 is produced, it is characterized in that: described electrodialysis impressed DC voltage, magnitude of voltage are 40V, and current value is 92A, and interelectrode distance is 10cm.
6. the electrodialysis alkali recovery process during a kind of viscose fiber according to claim 1 is produced, it is characterized in that: the enrichment alkali that described electrodialysis cathode compartment obtains is recycled, the raffinate acid neutralization of anolyte compartment, Precipitation hemicellulose, filter, obtain hemicellulose.
7. the electrodialysis alkali recovery process during a kind of viscose fiber according to claim 1 is produced, it is characterized in that: in the described electrodialysis process, the concentration of lye of anolyte compartment's waste liquid is 8 ~ 15g/L.
8. the electrodialysis alkali recovery process during a kind of viscose fiber according to claim 6 is produced, it is characterized in that: acid neutralization to pH value is 2 ~ 5.
9. the electrodialysis alkali recovery process during a kind of viscose fiber according to claim 6 is produced is characterized in that: describedly separate out filtrate behind the hemicellulose through reverse osmosis, obtain de-mineralized water and recycle.
10. the electrodialysis alkali recovery process during a kind of viscose fiber according to claim 1 is produced is characterized in that: described film group device uses is many to anion and cation exchange membrane pair, and the distance between the anion and cation exchange membrane is 0.1 ~ 0.2mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310311779.4A CN103351041B (en) | 2013-07-24 | 2013-07-24 | Electrodialysis alkali recovery process in a kind of viscose fiber production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310311779.4A CN103351041B (en) | 2013-07-24 | 2013-07-24 | Electrodialysis alkali recovery process in a kind of viscose fiber production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103351041A true CN103351041A (en) | 2013-10-16 |
| CN103351041B CN103351041B (en) | 2015-08-19 |
Family
ID=49307484
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310311779.4A Active CN103351041B (en) | 2013-07-24 | 2013-07-24 | Electrodialysis alkali recovery process in a kind of viscose fiber production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103351041B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104311706A (en) * | 2014-11-07 | 2015-01-28 | 宜宾雅泰生物科技有限公司 | Electrodialysis technology for exacting semi fibers by using viscose fiber pressed alkali liquor as raw materials |
| CN105668862A (en) * | 2016-04-15 | 2016-06-15 | 林淑录 | Method for recycling sodium hydroxide containing waste water in silicon wafer production process |
| CN106119431A (en) * | 2016-07-07 | 2016-11-16 | 焦作市华康糖醇科技有限公司 | A kind of xylose production process with solid acid as catalyst |
| CN106865832A (en) * | 2015-12-10 | 2017-06-20 | 宜宾丝丽雅集团有限公司 | A kind of Bipolar Membrane alkali recovery process in viscose rayon production |
| CN107999508A (en) * | 2017-11-07 | 2018-05-08 | 宜宾丝丽雅股份有限公司 | A kind of viscose glue waste slag treatment method |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60216884A (en) * | 1984-04-10 | 1985-10-30 | Teijin Eng Kk | Method for recovering available component from waste liquid generated in processing polyester fiber with alkali |
| CN102643935A (en) * | 2012-04-11 | 2012-08-22 | 宜宾丝丽雅股份有限公司 | Method for preparing xylose by using squeezed waste alkali in viscose fiber production process |
| CN102941017A (en) * | 2012-11-26 | 2013-02-27 | 宜宾海丝特纤维有限责任公司 | Process for secondary treating of waste alkali liquid during production of viscose fibers |
| CN102963994A (en) * | 2012-11-26 | 2013-03-13 | 宜宾海丝特纤维有限责任公司 | Treatment method of waste alkali liquor in production of viscose fibers |
-
2013
- 2013-07-24 CN CN201310311779.4A patent/CN103351041B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60216884A (en) * | 1984-04-10 | 1985-10-30 | Teijin Eng Kk | Method for recovering available component from waste liquid generated in processing polyester fiber with alkali |
| CN102643935A (en) * | 2012-04-11 | 2012-08-22 | 宜宾丝丽雅股份有限公司 | Method for preparing xylose by using squeezed waste alkali in viscose fiber production process |
| CN102941017A (en) * | 2012-11-26 | 2013-02-27 | 宜宾海丝特纤维有限责任公司 | Process for secondary treating of waste alkali liquid during production of viscose fibers |
| CN102963994A (en) * | 2012-11-26 | 2013-03-13 | 宜宾海丝特纤维有限责任公司 | Treatment method of waste alkali liquor in production of viscose fibers |
Non-Patent Citations (1)
| Title |
|---|
| 黄成杰等: ""电渗析法精制回收粘胶纤维压榨碱液"", 《氯碱工业》 * |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104311706A (en) * | 2014-11-07 | 2015-01-28 | 宜宾雅泰生物科技有限公司 | Electrodialysis technology for exacting semi fibers by using viscose fiber pressed alkali liquor as raw materials |
| CN106865832A (en) * | 2015-12-10 | 2017-06-20 | 宜宾丝丽雅集团有限公司 | A kind of Bipolar Membrane alkali recovery process in viscose rayon production |
| CN105668862A (en) * | 2016-04-15 | 2016-06-15 | 林淑录 | Method for recycling sodium hydroxide containing waste water in silicon wafer production process |
| CN106119431A (en) * | 2016-07-07 | 2016-11-16 | 焦作市华康糖醇科技有限公司 | A kind of xylose production process with solid acid as catalyst |
| CN107999508A (en) * | 2017-11-07 | 2018-05-08 | 宜宾丝丽雅股份有限公司 | A kind of viscose glue waste slag treatment method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103351041B (en) | 2015-08-19 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103351041B (en) | Electrodialysis alkali recovery process in a kind of viscose fiber production | |
| CN1197784C (en) | Method for recovering alkali and hemicellulose from chemical fibre waste liquid | |
| CN106242101B (en) | The processing recovery process of alkali pressed liquor in production process of viscose fiber | |
| CN109133448B (en) | Circulating environment-friendly treatment process and system for viscose waste liquid | |
| CN103351068B (en) | The ultrafiltration pretreatment technique of Black Liquor by Electrodialysis alkali collection during pulp manufactures | |
| CN103397407B (en) | The ultrafiltration pretreatment technique of pressed liquor electrodialysis alkali collection in viscose production | |
| CN101549912A (en) | Mercerized waste alkali recovery process and system thereof | |
| CN103388275B (en) | The pretreating process of Black Liquor by Electrodialysis alkali collection during a kind of pulp manufactures | |
| CN106237859B (en) | The alkali recovery process of alkali pressed liquor in production process of viscose fiber | |
| CN103349909B (en) | Post-processing method for squeezed alkali liquid in diffusion dialysis recycling viscose manufacture | |
| CN103397405B (en) | Pretreatment technique for recovering pressed liquor electrodialysis alkali in viscose fiber production | |
| CN103349913B (en) | Novel alkali recovery technology during viscose fiber production | |
| CN103349911B (en) | Diffusion dialysis pretreatment technology for recovery of electrodialysis alkali from pressed liquor in production of viscose fiber | |
| CN107938345B (en) | Preparation method of hydrolyzed silk peptide modified viscose fibers | |
| CN105525389A (en) | Chemical pulp cellulose alkali squeezing liquid zero-discharge recovery technology | |
| CN103349908A (en) | Method for squeezing alkali liquid in diffusion dialysis recycling viscose manufacture | |
| CN103362010B (en) | The diffusion dialysis pretreating process of Black Liquor by Electrodialysis alkali collection during pulp manufactures | |
| CN103351064B (en) | The millipore filtration pretreatment technology of pressed liquor electrodialysis alkali collection produced by viscose fiber | |
| CN103131019A (en) | Method extracting lignin from paper making pulp and conducting chemical modification | |
| CN106368032B (en) | Method that is a kind of while preparing cellulose fiber peacekeeping hemicellulose solution | |
| CN103349912B (en) | The pretreating process of electrodialysis alkali collection in a kind of viscose rayon production | |
| CN111661967A (en) | System and method for recovering alkali in viscose fiber production squeezing waste liquid by using double-membrane method | |
| CN104311706A (en) | Electrodialysis technology for exacting semi fibers by using viscose fiber pressed alkali liquor as raw materials | |
| CN111018213A (en) | Non-wood plant papermaking black liquor recycling treatment system and treatment process | |
| CN103349910A (en) | Pre-treatment method for pressed alkali liquor in manufacturing of recycling viscose by diffusion dialysis |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |