CN102924956A - Recovery, balance adjustment and comprehensive utilization technology for mixing alkali in indigo blue production - Google Patents
Recovery, balance adjustment and comprehensive utilization technology for mixing alkali in indigo blue production Download PDFInfo
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Abstract
A purpose of the invention is to achieve sodium reduction, potassium retention, and no use or less use of potassium hydroxide based on recovery utilization of mixing alkali and potassium-sodium balance adjustment in an indigo blue production process. According to the present invention, waste alkali residue, washing alkali water and surplus sodium hydroxide in oxidation alkali in the existing production are utilized, bicarbonate or carbon dioxide, and a plurality of ways are applied and introduced to the concentrate, and difference between dissolubility of sodium carbonate and potassium carbonate and a common ion effect are delicately utilized to generate sodium carbonate precipitate and separate, such that removal of surplus sodium hydroxide in the liquid alkali is achieved without introduction of new impurities, the sodium carbonate product is co-produced, about 0.5 ton of the potassium hydroxide is saved and about 1 ton of the sodium carbonate is by-produced when per ton of the indigo blue product is produced, and a new process route with characteristics of alkali resource comprehensive utilization and delicate potassium and sodium balance is developed. With the present invention, characteristics of low investment, resource saving, cleaning, environmental protection, economy, novelty, strong practicality and wide generalization application value are provided, significant theory and application values are provided for the circular economy and sustainable development strategy, and wide social benefits, economic benefits and ecological benefits are provided.
Description
Technical field
The invention belongs to dye chemical industry raw material production field, wait cleaning of vat dyes to produce and the comprehensive utilization of resources technology for indigo.
Background technology
Indigo is a kind of environmental protection, time-honored primary colour dye, is widely used in the fabric colorings such as cotton, fiber crops and viscose glue, and especially consumption is very large aspect the warp dyeing of indigo jean.
Present industrial production all is to prepare indigo via the oxidation of 3-indoles phenates, wherein reaction process comprises the mixed base reaction under 220～250 ℃ with a certain amount of anilino-acetate, sodium amide and sodium hydroxide and potassium hydroxide, obtain the alkali fusion thing of 20～30% 3-indoles phenates, this alkali fusion thing is dissolved in the large water gaging, after the blowing air oxidation, obtain indigo through press filtration, washing, granulation again.
The mol ratio of KOH and NaOH is about 0.6: 1 in the oxidation sig water, about 1: 1 ratio far below production requirement, potassium sodium compares serious unbalance, for this reason, existing indigo production technique all is to adopt the method for adding potassium hydroxide in the mixed base, regulate potassium sodium ratio, because indigo 440～450kg metal sodium production sodium amide that needs to add per ton, finally be converted into sodium hydroxide, cause sodium hydroxide excessive, the potassium hydroxide of simultaneously having to again add about 500kg is adjusted potassium sodium ratio, causes alkali number more more than needed.The part of alkali more than needed is by in the airborne carbonic acid gas and form alkaline residue, a part is washed after indigo the carrying secretly forms diluted alkaline water in the water, at last by in the sulfuric acid and rear discharging, oxidation diluted alkaline more than needed there is no good outlet, alkali is arbitrarily processed or is sold at a bargain, and wherein valuable potassium is failed fine utilization.Present mixed base Cycling And Utilizing Patterns has not only caused the huge waste of potassium resource, and does not have the fine potassium that utilizes shortage of resources, and per ton indigoly have mixed base about 6000 yuan to be worth to fail to realize, greatly to have increased indigo production cost.
As seen, existing indigo production technique is also undesirable aspect the recycling of mixed base, particularly potassium hydroxide consumption is high starting material, alkaline residue, buck, mixed base more than needed are failed the problems such as fine utilization, production cost height, not only can cause impact, the waste of resource and increasing of processing costs on environment, and it's a pity a large amount of consumption and wasted the potassium resource of rare preciousness most, the profit of enterprise self is not high yet.
Because indigo the grade in the vat dyes production process, the capital usually utilizes mixed base as the solvent in the alkali fusion condensation reaction, in the recovery process, exist " the few potassium of rich sodium ", need to add potassium hydroxide, with balance potassium sodium ratio, cause mixed base more than needed, the Universal Problems that exists simultaneously diluted alkaline water and alkaline residue to fail to recycle.
Reducing the charging capacity of potassium hydroxide, the comprehensive utilization mixed base, rationally regulate potassium-sodium balance in the mixed base, is for many years emphasis and the difficult problem of tackling key problem in the product line such as indigotin, does not have so far good solution.
Compare serious unbalance for potassium sodium in existing the production, potassium resource is not fully used, this situation of serious waste of resources, therefore, excessive sodium hydroxide in the mixed base separated by the mode of salify precipitation be used, reclaim as far as possible the mixed base in washing water and the alkaline residue, allowing valuable potassium hydroxide preserve as far as possible and to get back in the alkali systems is our main direction.
The present invention is directed to the problems referred to above, we have adopted the opposition thinking of " fall sodium and stay potassium ", guarantee as far as possible the recycling of diluted alkaline water and alkaline residue by technique and engineering, utilized cleverly the significant difference of yellow soda ash and salt of wormwood solubleness, by making the way of yellow soda ash Precipitation, reach easy, the low-cost potassium-sodium balance of regulating, realized recycling alkali more than needed, used no or little the purpose of potassium hydroxide.
Summary of the invention
The inventor passes through the comparative analysis to the dissolubility data of each potassium, sodium salt, finds Na
2CO
3Solubleness compare K
2CO
3Much smaller, when 0 degree～30 is spent, Na
2CO
3The K that only has of solubleness
2CO
31/15～1/5, by further test, find that also the common-ion effcet of sodium can also further reduce Na
2CO
3Solubleness, temperature is little on its impact.If pass into CO in shortage toward mixing in the buck
2Or stack gas should be preferentially with mix buck in NaOH form the lower Na of solubleness
2CO
3, by temperature regulation and common-ion effcet, can be easily early stage direct crystallization separate out yellow soda ash, a small amount of carbonate can further be separated out in later stage concentrated.Can form the mixed base that meets production requirement fully by existing processing requirement acquisition potassium, sodium, realize the easy adjusting of potassium sodium ratio.
Based on above-mentioned thinking, the inventor gropes repeatedly through lab scale, has finished a separate part NaOH from the mixed alkali liquor that is rich in NaOH and KOH, thereby reaches the invention of regulating the simple and easy to do method of potassium sodium ratio in the alkali lye.Its flow process is to add supercarbonate (such as bicarbonate of ammonia, sodium bicarbonate), CO in alkali lye
2Perhaps stack gas is utilized Na
2CO
3With K
2CO
3The remarkable difference of solubleness and common-ion effcet and salt effect make Na in water
2CO
3Preferential precipitation separates, thereby reaches the purpose of regulating potassium sodium ratio.
The inventor passes through experimental exploring and condition optimizing repeatedly, has proved economy, novelty, the practicality of this method.This method can be well be combined with filter progress except alkaline residue, washing with existing, and not increase, does not introduce new impurity, is the new technology route of the adjusting potassium sodium ratio an of the best.
The inventive method can adopt following specific embodiments:
1. short-cut method of regulating potassium sodium ratio in the mixed alkali liquor, it comprises the steps:
In the certain density mixed base aqueous solution, add bicarbonate of ammonia, the sodium bicarbonate of proportional quantity or pass into an amount of CO
2Or stack gas reacts, and NaOH is changed into Na
2CO
3, the limit coronite stirs, and temperature of reaction is preferably reacted (about 70 ℃) at 15～100 ℃ under the temperature of factory's two effect evaporated liquors, cooling after reaction is finished, stirring, crystallization, then filtered while hot obtains Na
2CO
3Crude product and process after mother liquor, mother liquor is got back to the original vapo(u)rization system of factory and directly is condensed into mixed base and applies mechanically Na
2CO
3Crude product prepares NaOH through the saturated aqueous sodium carbonate washing through causticization and reclaims alkali, also can be directly as commodity Na
2CO
3Take out; Saturated sodium carbonate solution after the washing mainly contains potassium hydroxide and sodium hydroxide and salt of wormwood, can time usefulness wash, and can concentrate separately or be inserted in the mixed base until the yellow soda ash non-conformity of quality closes when requiring, and carries out potassium-sodium balance and regulates.
In preferred specific embodiments, technique of the present invention comprises the steps:
In the certain density mixed base aqueous solution, add bicarbonate of ammonia or the sodium bicarbonate of proportional quantity or pass into an amount of CO
2Or stack gas reacts, and the limit coronite stirs, and temperature of reaction is at 15～100 ℃, preferably reaction (about 70 ℃) under the temperature of factory's two effect evaporated liquors, stirred crystallization after reaction is finished, Tc is 0～80 ℃, preferably at 0～10 ℃, then filtered while hot obtains Na
2CO
3Crude product and process after mother liquor, mother liquor is got back to the original vapo(u)rization system of factory and directly is condensed into mixed base and applies mechanically Na
2CO
3Crude product prepares NaOH through causticization and reclaims alkali through the saturated aqueous sodium carbonate washing, also can be directly as commodity Na
2CO
3Take out.Saturated sodium carbonate solution after the washing can concentrate separately or be inserted in the mixed base, carries out potassium-sodium balance and regulates.
Adopt the Na in the inventive method separation alkali lye
2CO
3, the potassium sodium ratio in the regulator solution, it is very little to have an investment, substantially can utilize existing most facilities, control the characteristics of " giving up ", Benefit with " giving up ", not only can make potassium substantially realize complete recovery, and can also be formed with the sodium product of value.Can realize substantially not consuming potassium hydroxide, can also the coproduction huge market demand, the good yellow soda ash of profit or the target of sodium hydroxide product.
Technique of the present invention has the characteristics of less investment, instant effect, energy-efficient, clean environment firendly, economy, novelty, practical, this method can be well be combined with filter progress except alkaline residue, washing with existing, and not increasing, do not introduce new impurity, is the new technology route of the adjustment potassium sodium ratio an of the best.Have extensively huge application value, be yellow soda ash or the sodium hydroxide of rationally the applying mechanically of mixed base in indigo and other vat production, coproduction high added value, few with or founded new method without potassium hydroxide.
Embodiment
The present invention can be further described with indefiniteness embodiment hereinafter.
1 70 ℃ of crystallization experiments of embodiment
Take by weighing triple effect concentrated solution (mixed base) 200.00g (K/Na=0.62: 1, CO
3 2-=15.54g/L, basicity (mixed base)=692.41g/L) passes into 15.00g CO in mixed base
2, the Na of adularescent at once
2CO
3Generate, and heat release is obvious, along with CO
2constantly pass into, crystallization increases, when being reacted to CO
2After the amount of the appointment that passes into, temperature of reaction has reached about 62 ℃, stops CO
2Pass into, 70 ℃ of insulations continue to be stirred 2 hours, after sufficient crystallising and the cooling, heat filtering obtains mother liquor 154.00g (K/Na=1.08, CO
3 2-=41.45g/L, basicity (mixed base)=446.99g/L, potassium content 3.82%) and crude product Na
2CO
338.79g (K/Na=0, CO
3 2-=51.03g/L, basicity (mixed base)=7.53%).
(20 ℃) crystallization experiment under embodiment 2 room temperatures
Take by weighing triple effect concentrated solution 200.00g (K/Na=0.62: 1, CO
3 2-=15.54g/L, basicity (mixed base)=692.41g/L) passes into 15.00g CO in mixed base
2, the Na of adularescent at once
2CO
3Generate, and heat release is obvious, along with CO
2constantly pass into, crystallization increases, when being reacted to CO
2After the amount of the appointment that passes into, temperature of reaction has reached about 62 ℃, stops CO
2Pass into, be cooled to room temperature, stir 2 hours sufficient crystallisings, filter, obtain mother liquor 155.00g (K/Na=1.08: 1, CO
3 2-=41.93g/L, basicity (mixed base)=442.59g/L, potassium content 3.82%) and crude product Na
2CO
336.40g (K/Na=0, CO
3 2-=51.63g/L, basicity (mixed base)=6.51%).
(0 ℃) crystallization experiment under embodiment 3 room temperatures
Take by weighing triple effect concentrated solution 200.00g (K/Na=0.62: 1, CO
3 2-=15.54g/L, basicity (mixed base)=692.41g/L) passes into 15.00g CO in mixed base
2, the Na of adularescent at once
2CO
3Generate, and heat release is obvious, along with CO
2constantly pass into, crystallization increases, when being reacted to CO
2After the amount of the appointment that passes into, temperature of reaction has reached about 62 ℃, stops CO
2Pass into, place in the frozen water and cool off, stirs 2 hours sufficient crystallisings, filtration obtains mother liquor 154.00g (K/Na=1.08: 1, CO
3 2-=43.22g/L, basicity (mixed base)=444.76g/L, potassium content 3.81%) and crude product Na
2CO
335.40g (K/Na=0, CO
3 2-=50.76g/L, basicity (mixed base)=49.50%).
Implementation column 4
Take by weighing triple effect concentrated solution 200.00g (K/Na=0.62: 1, CO
3 2-=15.54g/L, basicity (mixed base)=692.41g/L) passes into 11.25g CO in mixed base
2, the Na of adularescent at once
2CO
3Generate, and heat release is obvious, along with CO
2constantly pass into, crystallization increases, when being reacted to CO
2After the amount of the appointment that passes into, temperature of reaction has reached about 62 ℃, stops CO
2Pass into, 70 ℃ of insulations continue to be stirred 2 hours, after sufficient crystallising and the cooling, heat filtering obtains mother liquor 162.00g (K/Na=0.96: 1, CO
3 2-=23.96g/L, basicity (mixed base)=511.75g/L, potassium content 4.37%) and crude product Na
2CO
329.49g (K/Na=0, CO
3 2-=50.42g/L, basicity (mixed base)=6.51%).
Embodiment 5
Take by weighing triple effect concentrated solution 400.00g (K/Na=0.62: 1, CO
3 2-=15.54g/L, basicity (mixed base)=692.41g/L) passes into 70.00g CO in mixed base
2, the Na of adularescent at once
2CO
3Generate, and heat release is obvious, along with CO
2constantly pass into, crystallization increases, when being reacted to CO
2After the amount of the appointment that passes into, temperature of reaction has reached about 64 ℃, stops CO
2Pass into, filtered while hot obtains mother liquor 255.00g (K/Na=1.22: 1, CO
3 2-=154.21g/L, basicity (mixed base)=209.15g/L) and crude product Na
2CO
392.58g (K/Na=0, CO
3 2-=52.91g/L, basicity (mixed base)=6.72%).
Embodiment 6
It is unwashed indigo behind the filter press in producing to get 100g, adds the washing of pulling an oar of 500g water, obtains 510g washing water (K/Na=0.85, CO
3 2-=0.22%, basicity (mixed base)=4.36%).Get the above-mentioned wash water of 150g, in wash water, add 210g alkaline residue (K/Na=0.68, CO
3 2-=13.29%, basicity (mixed base)=33.65%), be stirred to alkaline residue and dissolve fully, allow solution naturally be down to room temperature and filter, obtain 305g filtrate (K/Na=0.71, CO
3 2-=6.52%L, basicity (mixed base)=22.00%) and 60g solid (K/Na=0.42, CO
3 2-=18.81%, basicity (mixed base)=11.38%), solid and filtrate are washed respectively and are concentrated.The a saturated Na of 100ml
2CO
3The step solid obtains 8.59g over dry Na in the washing
2CO
3The g solid is analyzed Na
2CO
3Content is 99.07%.
B is concentrated with upper step filtrate heating, is condensed into 52% alkali (K/Na=0.97, CO
3 2-=0.83%, basicity (mixed base)=52.35%), the solid that the obtains saturated Na of 100ml
2CO
3Washing obtains 18.9g content and is 99.20% Na
2CO
3Finished product.
Embodiment 7
Toward triple effect concentrated solution 5T (K/Na=0.97: 1, CO is housed
3 2-=30g/L passes into stack gas CO in the still of basicity (mixed base)=562.41g/L)
2, the Na of adularescent at once
2CO
3Generate, and heat release is obvious, along with CO
2constantly pass into, crystallization increases, when potassium sodium stops to pass into of stack gas than after reaching required standard, filter press, K/Na=1.06 in the filtrate: 1, CO
3 2-=35.23g/L, basicity (mixed base)=555.37g/L obtains crude product Na
2CO
3(K/Na=0.83, CO
3 2-=9.31%, basicity (mixed base)=33.66%), the filtrate heating being concentrated into over dry becoming dehydration alkali, (zero pour is 199 ℃ to this dehydration alkali, K/Na=1.09: 1, CO
3 2-=2.76%, basicity (mixed base)=96.21%) with plant produced dehydration alkali (zero pour=197 ℃, K/Na=1.12: 1, CO
3 2-=2.07%, basicity (mixed base)=96.21%) every analytical data all approaches, and indigo quality is not affected after applying mechanically back indigo production system.
Embodiment 8
Toward triple effect concentrated solution 5T (K/Na=0.97: 1, CO is housed
3 2-=30g/L, basicity (adds NH in the still of mixed base=562.41g/L)
4HCO
3, the Na of adularescent at once
2CO
3Generate, and emit a large amount of ammonias, along with NH
4HCO
3Continuous adding, crystallization increases, and stops to add NH after potassium sodium ratio reaches required standard
4HCO
3, filter press, K/Na=1.08 in the filtrate: 1, CO
3 2-=33.23g/L, basicity (mixed base)=560.22g/L obtains crude product Na
2CO
3(K/Na=0.46, CO
3 2-=31.71%, basicity (OH
-)=5.25%, moisture=20.77%), the filtrate heating being concentrated into over dry becoming dehydration alkali, this dehydration alkali zero pour is 197 ℃, K/Na=1.12: 1, CO
3 2-=2.10%, basicity (mixed base)=96.21%.
Embodiment 9
With black ash solid 68.50 gram (K/Na=0.46, CO obtained above
3 2-=31.71%, basicity (OH
-)=5.25%, moisture=20.77%), with the saturated Na of 100g
2CO
3Washing (CO
3 2-=16.08%) filters, obtain 54.46g yellow soda ash solid (K/Na=0, CO
3 2-=40.65%, basicity (OH
-)=0, moisture=27.68%) and 114g washings (K/Na=0.53, CO
3 2-=16.10%, basicity (OH
-)=2.73%), can fully wash out potassium hydroxide and sodium hydroxide and the salt of wormwood carried secretly, the Na that the yellow soda ash drying obtains afterwards
2CO
3Finished product content is 99.72%.
Claims (6)
1. the present invention relates to one and from the mixed alkali liquor that is rich in NaOH and KOH, adjust and reduce NaOH content and separate out yellow soda ash, thereby reach the simple and easy method of heightening potassium sodium ratio in the alkali lye; Its flow process be add in the certain density alkali oxide aqueous solution proportional quantity bicarbonate of ammonia or/and sodium bicarbonate or/and pass into the CO of proportional quantity
2Or a kind of or its combination in the stack gas, with NaOH on demand Partial Conversion become Na
2CO
3Reach the purpose of regulating potassium sodium ratio thereby separate out.
2. method according to claim 1, the concentration of alkali oxide can be between 10%～50%, but consider from effect, the material concentration about 45% after concentrated with triple effect.
3. method according to claim 1, certain density alkali oxide can be through the concentrated mixed base of triple effect, also can be the washings of the mixing diluted alkaline water that extracts from washing buck, alkaline residue or washing yellow soda ash crude product, separately or mix and be concentrated to certain density material, namely mixed alkali liquor be NaOH, KOH, Na
2CO
3, K
2CO
3The mixing solutions of arbitrary composition.
4. method according to claim 1, supercarbonate or CO
2Or stack gas passes into to need in the process to stir or beat with pump and loops absorption.
5. method according to claim 1, its reaction and Tc can be carried out in wider scope, and 30 ℃～90 ℃ industrial more economical.
6. mother liquor is got back to the original vapo(u)rization system of factory and directly is condensed into mixed base and applies mechanically Na after processing
2CO
3Crude product can be directly as commodity Na through the saturated aqueous sodium carbonate washing
2CO
3Take out, also can produce NaOH through causticizing process.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103556420A (en) * | 2013-10-30 | 2014-02-05 | 江苏泰丰化工有限公司 | Method for recycling mixed alkali liquor from after-treatment washing process of indigo |
| CN103554995A (en) * | 2013-10-30 | 2014-02-05 | 江苏泰丰化工有限公司 | Method for recycling mixed alkali liquor in indigo production |
| CN104151859A (en) * | 2013-11-06 | 2014-11-19 | 江苏泰丰化工有限公司 | Indigo blue product mixed alkali recovery device |
| CN104624616A (en) * | 2015-02-13 | 2015-05-20 | 内蒙古泰兴泰丰化工有限公司 | Device and method for treating mixed alkaline residue in indigotin production |
| CN104624615A (en) * | 2015-02-13 | 2015-05-20 | 内蒙古泰兴泰丰化工有限公司 | Treatment device for mixed alkaline residue in indigo blue production |
| CN104624617A (en) * | 2015-02-13 | 2015-05-20 | 内蒙古泰兴泰丰化工有限公司 | Method for treating mixed alkali residues in production of indigo |
| CN104692422A (en) * | 2015-02-13 | 2015-06-10 | 内蒙古泰兴泰丰化工有限公司 | Mixed alkaline residue treatment device and method in indigo blue production |
| CN104761483A (en) * | 2015-02-13 | 2015-07-08 | 内蒙古泰兴泰丰化工有限公司 | Mixed alkaline residue treatment method during indigo production |
| CN104876247A (en) * | 2015-04-30 | 2015-09-02 | 浙江奇彩环境科技有限公司 | Method for resource recycling processing of indigo alkaline residue |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5429337A (en) * | 1977-08-08 | 1979-03-05 | Kurashiki Boseki Kk | Recovery of indigo dyestuff |
| DE2740855C2 (en) * | 1977-09-10 | 1987-03-12 | Schumacher'sche Fabrik Gmbh & Co Kg, 7120 Bietigheim-Bissingen, De | |
| CN101774654A (en) * | 2009-01-08 | 2010-07-14 | 重庆宁寰再生资源开发有限责任公司 | Treatment device of waste liquid/slag |
| CN101323577B (en) * | 2007-06-14 | 2011-04-13 | 重庆达华砼外加剂科技发展有限公司 | Method for extracting aniline and sodium carbonate and potassium carbonate from mixed alkaline residue in bipseudoindoxyl production |
| CN102127307A (en) * | 2010-12-29 | 2011-07-20 | 梅剑平 | Recovered mixed alkali solution from production of indigo, and recovering method and use thereof |
-
2011
- 2011-08-09 CN CN201110226829.XA patent/CN102924956B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5429337A (en) * | 1977-08-08 | 1979-03-05 | Kurashiki Boseki Kk | Recovery of indigo dyestuff |
| DE2740855C2 (en) * | 1977-09-10 | 1987-03-12 | Schumacher'sche Fabrik Gmbh & Co Kg, 7120 Bietigheim-Bissingen, De | |
| CN101323577B (en) * | 2007-06-14 | 2011-04-13 | 重庆达华砼外加剂科技发展有限公司 | Method for extracting aniline and sodium carbonate and potassium carbonate from mixed alkaline residue in bipseudoindoxyl production |
| CN101774654A (en) * | 2009-01-08 | 2010-07-14 | 重庆宁寰再生资源开发有限责任公司 | Treatment device of waste liquid/slag |
| CN102127307A (en) * | 2010-12-29 | 2011-07-20 | 梅剑平 | Recovered mixed alkali solution from production of indigo, and recovering method and use thereof |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103556420A (en) * | 2013-10-30 | 2014-02-05 | 江苏泰丰化工有限公司 | Method for recycling mixed alkali liquor from after-treatment washing process of indigo |
| CN103554995A (en) * | 2013-10-30 | 2014-02-05 | 江苏泰丰化工有限公司 | Method for recycling mixed alkali liquor in indigo production |
| CN103556420B (en) * | 2013-10-30 | 2015-11-18 | 江苏泰丰化工有限公司 | A kind of method reclaiming mixed alkali liquor from indigo aftertreatment washing process |
| CN104151859A (en) * | 2013-11-06 | 2014-11-19 | 江苏泰丰化工有限公司 | Indigo blue product mixed alkali recovery device |
| CN104151859B (en) * | 2013-11-06 | 2016-01-13 | 江苏泰丰化工有限公司 | A kind of device of indigo Product recycling mixed base |
| CN104624616A (en) * | 2015-02-13 | 2015-05-20 | 内蒙古泰兴泰丰化工有限公司 | Device and method for treating mixed alkaline residue in indigotin production |
| CN104624615A (en) * | 2015-02-13 | 2015-05-20 | 内蒙古泰兴泰丰化工有限公司 | Treatment device for mixed alkaline residue in indigo blue production |
| CN104624617A (en) * | 2015-02-13 | 2015-05-20 | 内蒙古泰兴泰丰化工有限公司 | Method for treating mixed alkali residues in production of indigo |
| CN104692422A (en) * | 2015-02-13 | 2015-06-10 | 内蒙古泰兴泰丰化工有限公司 | Mixed alkaline residue treatment device and method in indigo blue production |
| CN104761483A (en) * | 2015-02-13 | 2015-07-08 | 内蒙古泰兴泰丰化工有限公司 | Mixed alkaline residue treatment method during indigo production |
| CN104692422B (en) * | 2015-02-13 | 2016-03-30 | 内蒙古泰兴泰丰化工有限公司 | Its Future about Alkaline Residue Treatment Unit and treatment process is mixed in indigo production |
| CN104876247A (en) * | 2015-04-30 | 2015-09-02 | 浙江奇彩环境科技有限公司 | Method for resource recycling processing of indigo alkaline residue |
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