CN1403381A - Method for recovering organic acid from waste alkali liquor - Google Patents
Method for recovering organic acid from waste alkali liquor Download PDFInfo
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- CN1403381A CN1403381A CN 01131453 CN01131453A CN1403381A CN 1403381 A CN1403381 A CN 1403381A CN 01131453 CN01131453 CN 01131453 CN 01131453 A CN01131453 A CN 01131453A CN 1403381 A CN1403381 A CN 1403381A
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- Prior art keywords
- extraction
- organic acid
- waste
- reclaims
- waste lye
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- 239000002699 waste material Substances 0.000 title claims abstract description 32
- 238000000034 method Methods 0.000 title claims abstract description 25
- 150000007524 organic acids Chemical class 0.000 title claims abstract description 18
- 239000003513 alkali Substances 0.000 title claims abstract description 10
- 238000000605 extraction Methods 0.000 claims abstract description 85
- 239000002351 wastewater Substances 0.000 claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000002253 acid Substances 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims abstract description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 48
- 239000003795 chemical substances by application Substances 0.000 claims description 25
- 150000004648 butanoic acid derivatives Chemical class 0.000 claims description 23
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 claims description 12
- -1 organic acid salt Chemical class 0.000 claims description 6
- 239000010865 sewage Substances 0.000 claims description 6
- 238000006386 neutralization reaction Methods 0.000 claims description 5
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims description 4
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 4
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 4
- 238000003889 chemical engineering Methods 0.000 claims description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 2
- 229910017604 nitric acid Inorganic materials 0.000 claims description 2
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims 3
- 239000004215 Carbon black (E152) Substances 0.000 claims 1
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims 1
- 239000000920 calcium hydroxide Substances 0.000 claims 1
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims 1
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 claims 1
- 239000000292 calcium oxide Substances 0.000 claims 1
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 claims 1
- 229930195733 hydrocarbon Natural products 0.000 claims 1
- 150000002430 hydrocarbons Chemical class 0.000 claims 1
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims 1
- 239000000347 magnesium hydroxide Substances 0.000 claims 1
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims 1
- 229920000642 polymer Polymers 0.000 claims 1
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 abstract description 83
- 238000005516 engineering process Methods 0.000 abstract description 7
- 238000006482 condensation reaction Methods 0.000 abstract description 3
- FERIUCNNQQJTOY-UHFFFAOYSA-M Butyrate Chemical compound CCCC([O-])=O FERIUCNNQQJTOY-UHFFFAOYSA-M 0.000 abstract 1
- 238000006243 chemical reaction Methods 0.000 abstract 1
- 230000007613 environmental effect Effects 0.000 abstract 1
- 238000005352 clarification Methods 0.000 description 14
- 238000003756 stirring Methods 0.000 description 14
- 230000008929 regeneration Effects 0.000 description 7
- 238000011069 regeneration method Methods 0.000 description 7
- 230000001172 regenerating effect Effects 0.000 description 6
- 238000001035 drying Methods 0.000 description 5
- 238000011084 recovery Methods 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- YIWUKEYIRIRTPP-UHFFFAOYSA-N 2-ethylhexan-1-ol Chemical compound CCCCC(CC)CO YIWUKEYIRIRTPP-UHFFFAOYSA-N 0.000 description 2
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N Butyraldehyde Chemical compound CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000008267 milk Substances 0.000 description 2
- 210000004080 milk Anatomy 0.000 description 2
- 235000013336 milk Nutrition 0.000 description 2
- 238000004381 surface treatment Methods 0.000 description 2
- 241001448862 Croton Species 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000007037 hydroformylation reaction Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 150000007522 mineralic acids Chemical class 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- HGBOYTHUEUWSSQ-UHFFFAOYSA-N valeric aldehyde Natural products CCCCC=O HGBOYTHUEUWSSQ-UHFFFAOYSA-N 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Physical Water Treatments (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
A method for recovering organic acid from waste alkali liquor discharged by octenal condensation reaction, in particular to a technology for recovering butyric acid from waste acid water discharged by a system after oil removal of waste alkali liquor discharged by an aldolization reaction to generate octenal. The content of butyric acid in the waste water after the waste alkali liquid is acidified, demulsified and deoiled is still up to 1.5-2.0% (by weight). The invention adopts the acidification-extraction-back extraction technology to recover the butyric acid (or butyrate) in the wastewater, and the technology can recycle more than 80 percent of the butyric acid in the wastewater and simultaneously ensure that the COD in the wastewater is CODcrAlso reduces the concentration of water from about 35000mg/L to about 6000mg/L, greatly improves the quality of externally discharged water, and has environmental benefitsThe economic benefit is particularly remarkable.
Description
Affiliated field:
The present invention relates to from a kind of waste liquid that contains high density butyric acid (or butyrates), reclaim butyro-novel process, especially relate to the waste lye that the octenal condensation reaction is discharged, butyro-recovery method in the useless sour water after the acidifying oil removing.
The waste lye that the octenal condensation reaction is discharged is behind the acidifying breaking milk and removing oil, the butyric acid that still contains 1.5-2.0% (weight) in its waste water, and butyric acid (or butyrates) is a kind of important chemical material, can from waste water, reclaim butyric acid and can create very high economic benefit, can significantly reduce organic quantity discharged in the waste water simultaneously again.
Prior art:
Because the waste water that contains high density butyric acid (or butyrates) in producing seldom, so reclaim domestic and international report also few especially of the method for butyric acid (or butyrates) from this waste water, existent method to be adopted with alkali neutralization, evaporation drying then, use the inorganic acid acidifying again, organic acid dissociates.For example, general universal decimal classification 661,725,66.03, introduced among the 628:33 and reclaimed butyro-report in the production 2-ethylhexanol waste liquid, this waste liquid is the sewage that is produced with the crotons hydroformylation butyraldehyde stage, wherein contain butyrates 40-100g/L, adopt recovery method for contain butyric acid waste water-sewage neutralization-evaporation-in and butyrates-butyro-rectifying-product butyric acid, but in evaporation drying technology for the low waste water of organic acid content owing to the energy consumption height, unreasonable economically, another kind method then is to adopt extraction, distil process is because the butyric acid boiling point is higher, also high to the requirement of separation operation condition, and investment, the energy consumption height, operational difficulty.
Goal of the invention
The purpose of this invention is to provide a kind of novel method that effectively from contain high density butyric acid (or butyrates) waste water, reclaims butyric acid (or butyrates), promptly adopt acidifying, extraction, reextraction, new drying technique to reclaim butyrates (or butyric acid), make it feasible on technology, can realize industrialization.
Summary of the invention:
In order to achieve the above object, the present invention has at first considered acidifying oil removing condition, it is the necessary acidified oil removing of octenal condensation waste lye, and the acidulated condition of processed waste water, by the organic acid rerum natura as can be known, organic acid its solubleness in water under the neutral condition less than C-5 is very big, and in next its solubleness in water that can reduce greatly of acidic conditions, reclaim with extraction process again, acidifying can be selected mineral acid, as inorganic middle strong acid such as sulfuric acid, hydrochloric acid, nitric acid, phosphoric acid, preferentially select the vitriol oil.Making the acidifying pH value is that 2.0-4.0 is advisable, and preferentially selecting pH value is 2.5～3.0.Next is the selection of extraction agent and strippant, and extraction agent is preferentially selected two-ethylhexanol based on the single alcohol more than the C-7, and strippant is preferentially selected NaOH based on highly basic.And with extraction, the relevant optimum operation condition of the stripping, (extraction agent: waste water), preferentially select 1: 2 that wherein is in a ratio of 1: 4; The unit surface treatment capacity is 50～150L/m
2.h, preferentially select 70L/m
2.h; Agitator motor rotating speed 100～600r/min; Churning time 5～10min and settling time are 30～180min.Waste water is through the discharging of extraction agent (1-3 level) extraction post neutralization, its extraction phase recycles after the strippant back extraction, stripping obtains the product butyrates mutually after drying, and butyrates gets butyric acid after the strong acid acidifying, so far finished the purpose that reclaims butyrates (or butyric acid) from waste water.The invention effect:
Octanol waste lye is behind the acidifying breaking milk and removing oil, still contain 1.5-2.0% (weight) butyric acid in the waste water, the method report that reclaims butyric acid (or butyrates) at present from this waste water is few especially, existing as: contain butyric acid waste water-sewage neutralization-evaporation-in and butyrates-butyro-rectifying-product butyric acid technology, for the low waste water of organic acid content because the energy consumption height, unreasonable economically, acidifying-extraction of the present invention-reextraction-dry new technology reclaims the butyric acid (butyrates) that contains in the useless sour water of butyric acid, and butyric acid (butyrates) rate of recovery in this waste water is reached more than 80%.Institute's effluent enters biochemical treatment apparatus and can not cause any impact to wastewater treatment field after reclaiming.The present invention with in compare with evaporation drying technology, have save energy and treating water and can directly carry out characteristics such as biochemical treatment
Accompanying drawing and brief description:
As accompanying drawing the technical process of the present invention with the two-stage countercurrent extraction described, wherein:
(1)-the spent acid tank
(2)-the alkali groove
(3)-the one-level extraction tank
(4)-the secondary extraction tank
(5)-the reextraction groove
(6)-organic acid salt receipts groove
Accompanying drawings specific implementation process of the present invention:
Useless sour water after the acidified oil removing of octanol waste lye after regulating, PH is entered waste acid water groove (1), enter one-level extraction tank (3) after metering, carry out extraction process with backspace extraction phase from secondary extraction tank (4), after the extracting and separating, extracting phase enters in the secondary extraction tank (4) and extraction agent generation extraction process from the reextraction groove, its extracting phase enters chemical engineering sewage processing field and carries out biochemical treatment after neutralization, extraction phase enters one-level extraction tank (3) recycle.The extraction phase of separating from one-level extraction tank (3) enters reextraction groove (5) and strips from the alkali lye of alkali groove (2), extracting phase enters secondary extraction tank (4) and recycles, the back extraction of getting off from the reextraction groove enters organic acid salt receipts groove (6) mutually, carries out the dried recovered organic acid salt.
Hereto, the present invention has finished and reclaimed organic acid salt (or organic acid) purpose from the useless sour water of octanol waste lye after oil removing.Processed waste water can directly enter chemical engineering sewage processing field and carry out biochemical treatment after neutralization.
Embodiment:
From octanol waste lye, reclaim butyric acid (butyrates) and install little trial run, be illustrated with specific embodiment:
With the mixer-settler is extraction equipment, adopts the two-stage countercurrent extraction, and (the COD value is 32068～37092mg/L), and acidifying PH is under the 2.5-3.5 condition, is in a ratio of 1～6: 6 (extraction agent: waste water), the unit surface treatment capacity is 50～150L/m after oil removing at waste water
2.h under the condition, agitator motor rotating speed 300～600r/min; Churning time 5～10min and settling time are under 30～180min condition useless sour water to be carried out cycling extraction regeneration tests (experiment flow is seen accompanying drawing).
Experimental example 1 operational condition is:
The butyric acid waste water 600ml that after the acidifying oil removing, contains high density, pH value is 2.6, extraction agent 230ml after just extracting, motor speed is 420r/min, stirs 5min, clarification 60min, extracting phase carries out the extraction second time with the extraction agent 230min after regenerate (extraction phase behind the reextraction reclaims butyrates with strippant regeneration) again and stirs 7min, motor speed is 380r/min, clarification 60min, and the butyric acid total yield is 88.9.
Experimental example 2 operational conditions are:
The butyric acid waste water 600ml that after the acidifying oil removing, contains high density, pH value is 2.9, extraction agent 250ml after just extracting, motor speed is 420r/min, stirs 7min, clarification 60min, extracting phase carries out the extraction second time with the extraction agent 230min of (extraction phase behind the reextraction is regenerated with strippant and reclaimed butyrates) after regenerating again and stirs 7min, motor speed is 390r/min, clarification 60min, and the butyric acid total yield is 87.6.
Experimental example 3 operational conditions are:
The butyric acid waste water 600ml that after the acidifying oil removing, contains high density, pH value is 2.5, extraction agent 270ml after just extracting, motor speed is 450r/min, stirs 6min, clarification 60min, extracting phase carries out the extraction second time with the back of regenerating (extraction phase behind the reextraction reclaims butyrates with strippant regeneration) extraction agent 250min again, stirs 8min, and motor speed is 340r/min, clarification 60min, the butyric acid total yield is 92.3.
Experimental example 4 operational conditions are:
The butyric acid waste water 600ml that after the acidifying oil removing, contains high density, pH value is 2.7, extraction agent 270ml after just extracting, motor speed is 400r/min, stirs 8min, clarification 60min, extracting phase carries out the extraction second time with the extraction agent 240min of the back of regenerating (extraction phase behind the reextraction reclaims butyrates with strippant regeneration) again, stirs 6min, and motor speed is 350r/min, clarification 60min, the butyric acid total yield is 92.1.
Experimental example 5 operational conditions are:
The butyric acid waste water 600ml that after the acidifying oil removing, contains high density, pH value is 3.0, extraction agent 220ml after just extracting, motor speed is 490r/min, stirs 8min, clarification 60min, extracting phase carries out the extraction second time with the extraction agent 200min of the back of regenerating (extraction phase behind the reextraction reclaims butyrates with strippant regeneration) again, stirs 6min, and motor speed is 330r/min, clarification 60min, the butyric acid total yield is 86.0.
Experimental example 6 operational conditions are:
The butyric acid waste water 600ml that after the acidifying oil removing, contains high density, pH value is 2.9, extraction agent 240ml after just extracting, motor speed is 500r/min, stirs 8min, clarification 60min, extracting phase carries out the extraction second time with the extraction agent 220min of the back of regenerating (extraction phase behind the reextraction reclaims butyrates with strippant regeneration) again, stirs 6min, and motor speed is 340r/min, clarification 60min, the butyric acid total yield is 86.9.
Experimental example 7 operational conditions are:
The butyric acid waste water 600ml that after the acidifying oil removing, contains high density, pH value is 2.6, extraction agent 250ml after just extracting, motor speed is 430r/min, stirs 8min, clarification 60min, extracting phase carries out the extraction second time with the extraction agent 230min of the back of regenerating (extraction phase behind the reextraction reclaims butyrates with strippant regeneration) again, stirs 6min, and motor speed is 300r/min, clarification 60min, the butyric acid total yield is 87.1.Secondary extraction, the recovery butyric acid treatment effect of stripping are listed in table 1.
Table 1:
Claims (10)
1, a kind of organic acid method that from waste lye, reclaims, it is characterized in that: the useless sour water after the acidified oil removing of octanol waste lye is entered waste acid water groove (1) after PH regulates, enter one-level extraction tank (3) after metering, carry out extraction process with the extraction phase that returns from secondary extraction tank (4), after the extracting and separating, extracting phase enters in the secondary extraction tank (4) and extraction agent generation extraction process from the reextraction groove, its extracting phase enters chemical engineering sewage processing field and carries out biochemical treatment after neutralization, extraction phase enters one-level extraction tank (3) recycle.The extraction phase of separating from one-level extraction tank (3) enters reextraction groove (5) and strips from the alkali lye of alkali groove (2), extracting phase enters secondary extraction tank (4) and recycles, the back extraction of getting off from the reextraction groove enters organic acid salt receipts groove (6) mutually, carries out the dried recovered organic acid salt.
2, a kind of organic acid method that reclaims from waste lye according to claim 1 is characterized in that: octanol waste lye through from extract or be the extraction agent oil removing with other hydrocarbon polymer after the acidulated condition of waste liquid be: PH is less than 4.0.
3, a kind of organic acid method that reclaims from waste lye according to claim 1 is characterized in that: select strong acid in sulfuric acid, hydrochloric acid, nitric acid, the phosphoric acid etc. during acidifying.
4, a kind of organic acid method that reclaims from waste lye according to claim 1, it is characterized in that: extraction agent selects to contain C
7And above alcohol.
5, a kind of organic acid method that reclaims from waste lye according to claim 1, it is characterized in that: 1～12: 6 (extraction agents: waste water) are selected in comparing of extraction agent.
6, a kind of organic acid method that reclaims from waste lye according to claim 1, it is characterized in that: extraction can be selected 1 grade for use to the extraction of 4 stage countercurrents, preferentially selects the extraction of 2 stage countercurrents.
7, a kind of organic acid method that reclaims from waste lye according to claim 1, it is characterized in that: getting disengaging time is less than 3 hours.
8, a kind of organic acid method that reclaims from waste lye according to claim 1, it is characterized in that: strippant is selected highly basic or basic oxide such as sodium hydroxide, potassium hydroxide, calcium hydroxide, magnesium hydroxide, calcium oxide for use.
9, a kind of organic acid method that reclaims from waste lye according to claim 1, it is characterized in that: the concentration of strippant is little by 40%.
The treatment process of 10, extraction according to claim 1, reextraction dried recovered butyrates is characterized in that: one-level extraction tank (3), secondary extraction tank (4), reextraction groove (5), organic acid salt are received groove (6)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011314532A CN1162335C (en) | 2001-09-11 | 2001-09-11 | Method for recovering organic acid from waste alkali liquor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB011314532A CN1162335C (en) | 2001-09-11 | 2001-09-11 | Method for recovering organic acid from waste alkali liquor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1403381A true CN1403381A (en) | 2003-03-19 |
| CN1162335C CN1162335C (en) | 2004-08-18 |
Family
ID=4670590
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB011314532A Expired - Fee Related CN1162335C (en) | 2001-09-11 | 2001-09-11 | Method for recovering organic acid from waste alkali liquor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1162335C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101353213B (en) * | 2007-07-25 | 2010-06-09 | 中国石油天然气股份有限公司 | Method for treating octanol waste alkali liquid by using alcohol acidification extraction method |
| CN103012104A (en) * | 2011-09-26 | 2013-04-03 | 中国石油天然气股份有限公司 | Method for treating butanol-octanol waste alkali liquor and recycling butyric acid |
| CN106186147A (en) * | 2016-07-26 | 2016-12-07 | 北京惠宇乐邦环保科技有限公司 | A kind of recovery and treatment method of high concentration waste organic acid |
| CN106927596A (en) * | 2015-12-30 | 2017-07-07 | 中国石油天然气股份有限公司 | Method for treating octanol waste alkali liquor |
| CN111978202A (en) * | 2020-08-12 | 2020-11-24 | 浙江理工大学上虞工业技术研究院有限公司 | Recovery method of alkaline washable disperse dye hydrolysate |
-
2001
- 2001-09-11 CN CNB011314532A patent/CN1162335C/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101353213B (en) * | 2007-07-25 | 2010-06-09 | 中国石油天然气股份有限公司 | Method for treating octanol waste alkali liquid by using alcohol acidification extraction method |
| CN103012104A (en) * | 2011-09-26 | 2013-04-03 | 中国石油天然气股份有限公司 | Method for treating butanol-octanol waste alkali liquor and recycling butyric acid |
| CN103012104B (en) * | 2011-09-26 | 2014-12-24 | 中国石油天然气股份有限公司 | Method for treating butanol-octanol waste alkali liquor and recycling butyric acid |
| CN106927596A (en) * | 2015-12-30 | 2017-07-07 | 中国石油天然气股份有限公司 | Method for treating octanol waste alkali liquor |
| CN106186147A (en) * | 2016-07-26 | 2016-12-07 | 北京惠宇乐邦环保科技有限公司 | A kind of recovery and treatment method of high concentration waste organic acid |
| CN106186147B (en) * | 2016-07-26 | 2020-05-19 | 北京惠宇乐邦环保科技有限公司 | Recovery treatment method of high-concentration organic acid wastewater |
| CN111978202A (en) * | 2020-08-12 | 2020-11-24 | 浙江理工大学上虞工业技术研究院有限公司 | Recovery method of alkaline washable disperse dye hydrolysate |
| CN111978202B (en) * | 2020-08-12 | 2022-08-05 | 浙江理工大学上虞工业技术研究院有限公司 | Recovery method of alkaline washable disperse dye hydrolysate |
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| Publication number | Publication date |
|---|---|
| CN1162335C (en) | 2004-08-18 |
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