CN102219672A - Method and device for producing pure terephthalic acid by alkali decrement wastewater residues - Google Patents
Method and device for producing pure terephthalic acid by alkali decrement wastewater residues Download PDFInfo
- Publication number
- CN102219672A CN102219672A CN2011101039378A CN201110103937A CN102219672A CN 102219672 A CN102219672 A CN 102219672A CN 2011101039378 A CN2011101039378 A CN 2011101039378A CN 201110103937 A CN201110103937 A CN 201110103937A CN 102219672 A CN102219672 A CN 102219672A
- Authority
- CN
- China
- Prior art keywords
- solid
- alkali decrement
- waste water
- terephthalic acid
- equipment
- 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.)
- Pending
Links
Images
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a method for recovering pure terephthalic acid, and in particular relates to a method and device for producing pure terephthalic acid by alkali decrement wastewater residues. The method is characterized by comprising the steps of: decolorization by dissolution, distillation, second decolorization and crystallization. By improving the preparation process, residues are recovered from alkali decrement wastewater, and simultaneously, the alkali decrement wastewater residues are converted into the pure terephthalic acid product, thus the elimination rate of CODcy (Chemical Oxygen Demand cy) value in the alkali decrement wastewater reaches about 75%, the alkali decrement wastewater is modified into industrial wastewater which is easily biodegradable, and the secondary environmental pollution caused by the alkali decrement wastewater residues is well reduced, in addition, the prepared pure terephthalic acid product with the recovery rate reaching 90% and the purity reaching over 99.5% has extraordinarily high economical and environmental benefits.
Description
Technical field:
The present invention relates to a kind of pure terephthalic acid's of recovery method, be meant a kind of method and device thereof more specifically with alkali decrement waste water residue production pure terephthalic acid.
Background technology:
Alkali decrement waste water is that polyester fabric is added industrial sewage after the alkaline purification, and generally about 8000～30000, alkali decrement waste water residue main component is the para-phthalic sodium salt slurry to its COD value.At present, at the processing of dyeing waste water, be target with the COD value that reduces in the dyeing waste water, more is, by in dyeing waste water, throwing in the trivalent iron salt medicament, and use acid for adjusting pH value, thus the terephthalic acid in the alkali decrement waste water is separated out in solid-state mode, this method can make the COD value of alkali decrement waste water reduce 70-80%, but the defective of aforesaid method is: the terephthalic acid impurity of 1, separating out is very many, can't utilize once more, and be difficult to handle, cause secondary pollution easily; 2, adopt the method for acid out, cost is too high.
Have based on this, the applicant makes the present invention.
Summary of the invention:
At the problems referred to above, a first aspect of the present invention purpose is to provide a kind of method with alkali decrement waste water residue production pure terephthalic acid.
The technical scheme that the present invention takes is as follows:
A kind of method with alkali decrement waste water residue production pure terephthalic acid is characterized in that, may further comprise the steps:
1, alkali decrement waste water residue preparation:
Alkali decrement waste water is collected to water collecting basin by the alkali decrement machine in workshop, makes the alkali decrement waste water homogenizing, guarantee the acid out stable operation in step down.
Alkali decrement waste water in the water collecting basin is entered the acid out pond continuously, add acid while intaking, and constantly stir, separate out until a large amount of white depositions (terephthalic acid sodium salt residue), the preferred bases reduction waste water is with 12.5m
3The flow of/h adds the acid out pond, and pH value is controlled at 6.5 – 7, and described acid adopts 98% certified products sulfuric acid to handle, and reaching the CODcy clearance about 75% in the waste water, and general spent acid has higher CODcy, so can't reach processing requirements.
With the above-mentioned alkali decrement waste water residue that obtains, standby after filtering, dry, pulverizing.
In the alkali decrement waste water residue (being commonly called as salt slurry) of above-mentioned preparation, prime cost is the terephthalic acid sodium salt, and the terephthalic acid sodium salt content is about 95%, and the water ratio of alkali decrement waste water residue is controlled in 1%.
2, dissolving decolouring: get 1000 kilograms of aforementioned alkali decrement waste water residues that make, adding excessive DMF(dimethyl formamide) solvent, sorbing material pull an oar, the weight ratio of alkali decrement waste water residue, DMF solvent, sorbing material is 1:6-8:0.3, after making beating is finished, be heated to 80-120 ℃ at normal temperatures, stir, dissolved 1～4 hour, get lysate, lysate carries out solid-liquid separation.
Described excessive DMF solvent is to instigate so that aforementioned bases reduction waste water residue dissolves fully, and generally speaking, the alkali decrement waste water residue is controlled at 1:5～10 with DMF weight of solvent ratio, can obtain extraordinary solute effect, and excessive DMF solvent can be recycled; Described DMF solvent preferably adopts mass concentration to be not less than 99.9% DMF solvent, particularly preferably, adopts 80 ℃-120 ℃ mass concentration to be not less than 99.9% DMF solvent, and solute effect is better.Dissolution time is 1～4 hour, more preferably, dissolves and can obtain preferable solute effect in 2 hours.
Add sorbing material during making beating simultaneously, described sorbing material be preferably gac, nut-shell, potter's clay or diatomaceous one or more, main titanium dioxide, textile auxiliary and other mechanical impuritys of removing in the lysate of its effect.
More preferably: the weight ratio of alkali decrement waste water residue, DMF solvent, sorbing material is 1:6-8:0.3, can obtain solute effect preferably.
Preferably, add carbonate in described lysate, the kind and the consumption of described carbonate are not particularly limited, only otherwise goal of the invention of the present invention is produced restriction to get final product, as barium carbonate, described carbonate gets final product with the sulfate ion of removing in pure terephthalic acid's product.
Described solid-liquid separation can adopt centrifuging or gravity filtration, the preferred mode that adopts centrifuging, centrifuge speed is preferably 2900 commentaries on classics/min, the solid residue that filters out is sorbing material such as gac, nut-shell or potter's clay, diatomite, put into reuse in the pulping process, liquid phase is delivered to subsequent processing and handles;
Certainly, also can realize removing by filter the solid impurity in the lysate and finishing decolouring with dissolved solution by having the filter of absorption and decolouring function.
3, distillation: the lysate after the above-mentioned filtration is sent in the distillation tower, be heated to 150 ℃ and distill, extract the DMF solvent under the negative pressure of vacuum out, by distillation, can extract the DMF solvent 50～60% of lysate out, preferably, the DMF solvent cycle that distills out reuse to the pulping process;
4, decolouring for the second time: the concentrated solution after will distilling, adding sorbing material decolours once more, described sorbing material be preferably gac, nut-shell and potter's clay, diatomaceous one or more, carry out solid-liquid separation then, isolated solid phase is recycled to recycle in the pulping process;
Behind distillation process, before the Crystallization Procedure, carry out the bleaching process second time, promptly with sorbing material the concentrated solution after distilling is handled once more, this is owing to the rising along with distillation tower internal heating temperature, the DMF solvent turns to be yellow easily, whiteness to product exerts an influence, and therefore before carrying out crystallization, concentrated solution is decoloured once more, can effectively improve the whiteness of finished product, improve the quality of products.
5, crystallization: the concentrated solution after will carrying out decolouring is for the second time sent into cooling reactor, crystallisation by cooling under 5-10 ℃ of temperature, after separating out, crystallization carries out solid-liquid separation, wherein, isolated liquid phase (DMF solvent) is delivered to reuse in the pulping process, get pure terephthalic acid's finished product 900kg after solid phase is washed, filters, dried, the rate of recovery reaches 90%, and purity is more than 99.5%.Preferably, after the filtrate distillation after the washing, gained DMF solvent reclaiming, distilled water stores the back reuse.
A second aspect of the present invention purpose is to provide a kind of device with alkali decrement waste water residue production pure terephthalic acid, comprise the decrement machine, the acid out pond links to each other with the decrement machine, first equipment for separating liquid from solid links to each other with the acid out pond, pulverizing drying installation links to each other with first equipment for separating liquid from solid, beating apparatus links to each other with the pulverizing drying installation, dissolver links to each other with beating apparatus, second equipment for separating liquid from solid links to each other with dissolver on the one hand, link to each other with beating apparatus on the other hand, water distilling apparatus links to each other with second equipment for separating liquid from solid on the one hand, link to each other with beating apparatus on the other hand, the decolouring device links to each other with water distilling apparatus, be equipped with sorbing material in the decolouring device, the 3rd equipment for separating liquid from solid links to each other with the decolouring device on the one hand, link to each other with beating apparatus on the other hand, crystallization apparatus links to each other with the 3rd equipment for separating liquid from solid, the 4th equipment for separating liquid from solid links to each other with crystallization apparatus on the one hand, link to each other with beating apparatus on the other hand, water washing device links to each other with the 4th equipment for separating liquid from solid, the 5th equipment for separating liquid from solid links to each other with water washing device, drying unit, the after-fractionating device links to each other with the 5th equipment for separating liquid from solid respectively, and beating apparatus links to each other with the after-fractionating device.
Further:
Between described decrement machine and acid out pond, water collecting basin is set also.
Described pulverizing drying installation is the dryer that belt is pulverized function, first equipment for separating liquid from solid, second equipment for separating liquid from solid, the 3rd equipment for separating liquid from solid, the 4th equipment for separating liquid from solid, the 5th equipment for separating liquid from solid adopt any one of whizzer or filter, beating apparatus adopts the making beating still, dissolver adopts dissolution kettle, water distilling apparatus adopts distillation tower, and crystallization apparatus adopts cooling-water machine.
Beneficial effect of the present invention is as follows:
The present invention is through extensive and deep development research, by improving preparation technology, from alkali decrement waste water, reclaim residue (main component is the terephthalic acid sodium salt), saved processing step, in preparation method's process, various products are recycled, therefore, make the CODcy value clearance of alkali decrement waste water reach about 75%, and modification becomes the trade effluent of readily biodegradable, also the secondary pollution environment that the alkali decrement waste water residue is caused brings fine improvement, simultaneously the alkali decrement waste water residue is changed into pure terephthalic acid's product, turn waste into wealth, pure terephthalic acid's product of preparation, the rate of recovery reaches 90%, purity is more than 99.5%, has very high economical effectiveness and environmental benefit.
Below the invention will be further described by the drawings and specific embodiments.
Description of drawings:
Fig. 1 is the process flow sheet of embodiment of the invention production method;
Fig. 2 is the structure composition diagram of embodiment of the invention production equipment.
Embodiment:
Embodiment 1:
As shown in Figure 1, a kind of method with alkali decrement waste water residue production pure terephthalic acid of the present invention may further comprise the steps:
Alkali decrement waste water is collected to water collecting basin by the alkali decrement machine in workshop, makes the alkali decrement waste water homogenizing, guarantee the acid out stable operation in step down.
The alkali decrement waste water of homogenizing in the water collecting basin is entered the acid out pond continuously, add acid while intaking, and constantly stir, separate out until a large amount of white depositions (terephthalic acid sodium salt residue), in the present embodiment, alkali decrement waste water is with 12.5m
3The flow of/h adds the acid out pond, and pH value is controlled at 6.5 – 7, and described acid adopts 98% certified products sulfuric acid to handle, and reaching the CODcy clearance about 75% in the waste water, and general spent acid has higher CODcy, so can't reach processing requirements.
Alkali decrement waste water residue with obtaining filters, and standby after solid phase oven dry, the pulverizing, liquid phase is discharged.In the alkali decrement waste water residue after oven dry is pulverized, prime cost is the terephthalic acid sodium salt, and the terephthalic acid sodium salt content is about 95%, and the water ratio of alkali decrement waste water residue is controlled in 1%.
Get the alkali decrement waste water residue after 1000 kilograms of oven dry are pulverized, adding mass concentration and be 99.9% DMF solvent, sorbing material pulls an oar, the weight ratio of alkali decrement waste water residue, DMF solvent, sorbing material is 1:6-8:0.3, after making beating is finished, is heated to 80-120 ℃ at normal temperatures, stir, dissolved 2 hours, and got lysate, lysate carries out solid-liquid separation, the solid phase gac is recycled in the pulping process and utilizes once more, and liquid phase is then sent into distillation tower and distilled.
Lysate after filtering is sent in the distillation tower, be heated to 120～150 ℃ and distill, more preferably, selects 150 ℃ to obtain best effecies down, extraction DMF solvent under the negative pressure of vacuum, the reuse to the pulping process of the DMF solvent cycle of extraction;
With the concentrated solution after the distillation, add gac and decolour, carry out solid-liquid separation then, isolated solid phase is recycled to recycle in the pulping process;
Concentrated solution after will decolouring is crystallisation by cooling under 5-10 ℃ of temperature, after separating out, crystallization carries out solid-liquid separation, wherein, isolated liquid phase (DMF solvent) is delivered to reuse in the pulping process, and solid phase is washed, filtered, after the filtrate distillation after the washing, gained DMF solvent reclaiming, distilled water stores the back reuse, and solid phase is drying and packaging then, purity is pure terephthalic acid's finished product 900kg of 99.5%, the rate of recovery 90%.
Embodiment 2:
As shown in Figure 2, a kind of device with alkali decrement waste water residue production pure terephthalic acid of the present invention comprises:
Decrement machine 1: wherein said decrement machine 1 provides alkali decrement waste water;
Acid out pond 3 links to each other with decrement machine 1, the alkali decrement waste water that decrement machine 1 is collected carries out acid out in acid out pond 3, first equipment for separating liquid from solid 4 links to each other with acid out pond 3, in the present embodiment, first equipment for separating liquid from solid 4 adopts whizzer, and the alkali decrement waste water residue that produces in the acid out pond 3 is separated into liquid phase and the solid phase that contains the terephthalic acid sodium salt in first equipment for separating liquid from solid 4.Preferably, between described decrement machine 1 and acid out pond 3, water collecting basin 2 is set also; 2 pairs of alkali decrement waste waters of described water collecting basin carry out homogenizing.
Pulverizing drying installation 5 links to each other with first equipment for separating liquid from solid 4, pulverizing drying installation adopts band to pulverize the dryer of function, be used for the solid phase alkali decrement waste water residue that first equipment for separating liquid from solid 4 obtains is dried, pulverized, beating apparatus 6a links to each other with pulverizing drying installation 5, be used for the alkali decrement waste water residue after oven dry, the pulverizing is pulled an oar, beating apparatus 6a can adopt the making beating still, dissolver 6b links to each other with beating apparatus 6a, be used for the slurry that beating apparatus 6a produces is finished dissolving, decolouring, the dissolver 6a of present embodiment adopts dissolution kettle.The second equipment for separating liquid from solid 6c links to each other with dissolver 6b on the one hand, link to each other with beating apparatus 6a on the other hand, wherein the isolating solid product of the second equipment for separating liquid from solid 6c is sorbing materials such as gac, can be recycled to beating apparatus 6a through pipeline utilizes once more, liquid phase is then sent into water distilling apparatus 6d and is handled, water distilling apparatus 6d links to each other with the second equipment for separating liquid from solid 6c on the one hand, link to each other with beating apparatus 6a on the other hand, water distilling apparatus 6d adopts distillation tower, after the isolating liquid product of the second equipment for separating liquid from solid 6c distills in distillation tower, gained overhead fraction (50%DMF solvent) enters described beating apparatus 6a and carries out recycle, gained tower bottom distillate (mainly being pure terephthalic acid's mother liquor and DMF solvent) enters and carries out crystallization in the crystallization apparatus 6g behind decolouring device 6e.Decolouring device 6e links to each other with water distilling apparatus 6d, be equipped with sorbing material such as gac among the decolouring device 6e, be used for the concentrated solution that distillation tower distills out is decoloured once more, the 3rd equipment for separating liquid from solid 6f links to each other with decolouring device 6e on the one hand, link to each other with beating apparatus 6a on the other hand, crystallization apparatus 6g links to each other with the 3rd equipment for separating liquid from solid 6f, wherein the isolating solid product of the 3rd equipment for separating liquid from solid 6f is sorbing materials such as gac, can be recycled to beating apparatus 6a through pipeline utilizes once more, liquid phase is then sent into crystallization apparatus 6g and is carried out crystallization, crystallization apparatus 6g can adopt cooling reactor or cooling-water machine, the 4th equipment for separating liquid from solid 6h links to each other with crystallization apparatus 6g on the one hand, link to each other with beating apparatus 6a on the other hand, water washing device 7 links to each other with the 4th equipment for separating liquid from solid 6h, wherein: the solid product (pure terephthalic acid's product) among described the 4th equipment for separating liquid from solid 6h enters into water washing device and washes, and the liquid product among the 4th equipment for separating liquid from solid 6h (DMF solvent) enters beating apparatus 6a reuse.The 5th equipment for separating liquid from solid 8 links to each other with water washing device 7, drying unit 9, after-fractionating device 10 link to each other with the 5th equipment for separating liquid from solid 8 respectively, beating apparatus 6a links to each other with after-fractionating device 10, pure terephthalic acid's product is after washing, carry out solid-liquid separation at the 5th equipment for separating liquid from solid 8, promptly get pure terephthalic acid's finished product after wherein solid product (pure terephthalic acid's product) enters drying unit 9 dryings.After liquid product (being mainly DMF solvent and water) entered and distills in the after-fractionating device 10, gained overhead fraction water entered the storage tanks reuse, and the tower bottom distillate of gained (DMF solvent) then enters beating apparatus 6a recycle once more.
Beneficial effect of the present invention is as follows:
The present invention is by reclaiming the p-phthalic acid from alkali decrement waste water residue (terephthalic acid (TPA) sodium salt), so that the CODcy value clearance (salt slurry deals residue) of waste water reaches about 75%, and modification becomes easy biodegradable industrial wastewater, also the secondary pollution environment is brought very big improvement, simultaneously alkali decrement waste water residue (terephthalic acid (TPA) sodium salt) is changed into fine terephthalic acid products, turn waste into wealth. Have extraordinary economic benefit and environmental benefit.
Claims (10)
1. method of producing the pure terephthalic acid with the alkali decrement waste water residue, it is characterized in that, may further comprise the steps: get 1000 kilograms of alkali decrement waste water residues, add DMF solvent, sorbing material, pull an oar, the weight ratio of alkali decrement waste water residue, DMF solvent, sorbing material is 1:6-8:0.3, after making beating is finished, be heated to 80-120 ℃ at normal temperatures, stir, dissolved 1～4 hour, get lysate, lysate carries out solid-liquid separation; After distillation, crystallization, obtain pure terephthalic acid's finished product then.
2. a kind of method according to claim 1 with alkali decrement waste water residue production pure terephthalic acid, it is characterized in that: described distillation is meant: lysate is heated to 120～150 ℃ distills, extract the DMF solvent under the negative pressure of vacuum out; The DMF solvent cycle that distills out reuse to the pulping process.
3. a kind of method of producing the pure terephthalic acid with the alkali decrement waste water residue according to claim 1, it is characterized in that: described crystallization is meant: the concentrated solution after will distilling is crystallisation by cooling under 5-10 ℃ of temperature, after separating out, crystallization carries out solid-liquid separation, solid phase gets pure terephthalic acid's finished product after washing, filtration, oven dry, liquid phase is delivered to reuse in the pulping process.
4. according to claim 1 or 2 or 3 described a kind of methods with alkali decrement waste water residue production pure terephthalic acid, it is characterized in that: decolouring before the crystallization: the concentrated solution after will distilling adds sorbing material and decolours; Carry out solid-liquid separation after the decolouring, solid phase is circulated to reuse in the pulping process, and liquid phase enters Crystallization Procedure.
5. a kind of method with alkali decrement waste water residue production pure terephthalic acid according to claim 1, it is characterized in that: lysate is through solid-liquid separation, and solid phase is circulated to reuse in the pulping process, and liquid phase enters distillation process.
6. a kind of method of producing the pure terephthalic acid with the alkali decrement waste water residue according to claim 1, it is characterized in that: described alkali decrement waste water residue preparation comprises: alkali decrement waste water is collected to water collecting basin, make the alkali decrement waste water homogenizing, enter the acid out pond then continuously, add acid while intaking, and constantly stir, separate out until white precipitate, collect the alkali decrement waste water residue then, standby after filtering, dry, pulverizing.
7. according to claim 6ly a kind ofly produce pure terephthalic acid's method, it is characterized in that with the alkali decrement waste water residue: described sorbing material be selected from gac, nut-shell, potter's clay or diatomaceous one or more.
8. according to the described a kind of method with alkali decrement waste water residue production pure terephthalic acid of one of claim 1～7, it is characterized in that: described solid-liquid separation adopts centrifuging, and centrifuge speed is preferably 2900 commentaries on classics/min.
9. device of producing the pure terephthalic acid with the alkali decrement waste water residue, it is characterized in that, comprise the decrement machine, the acid out pond links to each other with the decrement machine, first equipment for separating liquid from solid links to each other with the acid out pond, pulverizing drying installation links to each other with first equipment for separating liquid from solid, beating apparatus links to each other with the pulverizing drying installation, dissolver links to each other with beating apparatus, second equipment for separating liquid from solid links to each other with dissolver on the one hand, link to each other with beating apparatus on the other hand, water distilling apparatus links to each other with second equipment for separating liquid from solid on the one hand, link to each other with beating apparatus on the other hand, the decolouring device links to each other with water distilling apparatus, be equipped with sorbing material in the decolouring device, the 3rd equipment for separating liquid from solid links to each other with the decolouring device on the one hand, link to each other with beating apparatus on the other hand, crystallization apparatus links to each other with the 3rd equipment for separating liquid from solid, the 4th equipment for separating liquid from solid links to each other with crystallization apparatus on the one hand, link to each other with beating apparatus on the other hand, water washing device links to each other with the 4th equipment for separating liquid from solid, and the 5th equipment for separating liquid from solid links to each other with water washing device, drying unit, the after-fractionating device links to each other with the 5th equipment for separating liquid from solid respectively, and beating apparatus links to each other with the after-fractionating device.
10. a kind of device of producing the pure terephthalic acid with the alkali decrement waste water residue according to claim 9, it is characterized in that: described pulverizing drying installation is pulverized the dryer of function for band, first equipment for separating liquid from solid, second equipment for separating liquid from solid, the 3rd equipment for separating liquid from solid, the 4th equipment for separating liquid from solid, the 5th equipment for separating liquid from solid adopt any one of whizzer or filter, beating apparatus adopts the making beating still, dissolver adopts dissolution kettle, water distilling apparatus adopts distillation tower, and crystallization apparatus adopts cooling-water machine.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101039378A CN102219672A (en) | 2011-04-26 | 2011-04-26 | Method and device for producing pure terephthalic acid by alkali decrement wastewater residues |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2011101039378A CN102219672A (en) | 2011-04-26 | 2011-04-26 | Method and device for producing pure terephthalic acid by alkali decrement wastewater residues |
Related Child Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310677223.7A Division CN103755555A (en) | 2011-04-26 | 2011-04-26 | Apparatus for producing purified terephthalic acid by using alkali-minimization wastewater residue |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102219672A true CN102219672A (en) | 2011-10-19 |
Family
ID=44776406
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2011101039378A Pending CN102219672A (en) | 2011-04-26 | 2011-04-26 | Method and device for producing pure terephthalic acid by alkali decrement wastewater residues |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102219672A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103224450A (en) * | 2013-04-25 | 2013-07-31 | 绍兴县远程树脂科技有限公司 | Method for producing purified terephthalic acid by using alkali reduction wastewater residue, and device thereof |
| CN105001080A (en) * | 2015-09-02 | 2015-10-28 | 刘健 | Method of recycling terephthalic acid in dacron alkali peeling waste residues by using yttria |
| CN105152923A (en) * | 2015-09-02 | 2015-12-16 | 刘健 | Process-optimized method for recycling terephthalic acid |
| CN105585475A (en) * | 2015-08-06 | 2016-05-18 | 绍兴汉青环保科技有限公司 | Printing and dyeing white mud resource utilizing method |
| CN106430839A (en) * | 2016-11-17 | 2017-02-22 | 无锡明盛纺织机械有限公司 | Anaerobic-aerobic-precipitation-diatomite adsorption treatment process for alkali-minimization wastewater in printing and dyeing industry |
| CN107032554A (en) * | 2016-11-22 | 2017-08-11 | 浙江丰林亚麻染整有限公司 | A kind of alkali decrement waste water dual treatment method and apparatus |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101130494A (en) * | 2007-08-28 | 2008-02-27 | 浙江华联三鑫石化有限公司 | Method for recycling p-benzene dicarboxylic acid from coloured p-benzene dicarboxylic acid |
| CN101244857A (en) * | 2007-02-12 | 2008-08-20 | 陈定良 | Alkali deweighting wastewater processing method and device |
-
2011
- 2011-04-26 CN CN2011101039378A patent/CN102219672A/en active Pending
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101244857A (en) * | 2007-02-12 | 2008-08-20 | 陈定良 | Alkali deweighting wastewater processing method and device |
| CN101130494A (en) * | 2007-08-28 | 2008-02-27 | 浙江华联三鑫石化有限公司 | Method for recycling p-benzene dicarboxylic acid from coloured p-benzene dicarboxylic acid |
Non-Patent Citations (1)
| Title |
|---|
| 邢其毅等: "《基础有机化学》", 30 June 2005, 高等教育出版社 * |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103224450A (en) * | 2013-04-25 | 2013-07-31 | 绍兴县远程树脂科技有限公司 | Method for producing purified terephthalic acid by using alkali reduction wastewater residue, and device thereof |
| CN105585475A (en) * | 2015-08-06 | 2016-05-18 | 绍兴汉青环保科技有限公司 | Printing and dyeing white mud resource utilizing method |
| CN105585475B (en) * | 2015-08-06 | 2017-09-22 | 绍兴汉青环保科技有限公司 | Printing and dyeing white clay resource utilization method |
| CN105001080A (en) * | 2015-09-02 | 2015-10-28 | 刘健 | Method of recycling terephthalic acid in dacron alkali peeling waste residues by using yttria |
| CN105152923A (en) * | 2015-09-02 | 2015-12-16 | 刘健 | Process-optimized method for recycling terephthalic acid |
| CN106430839A (en) * | 2016-11-17 | 2017-02-22 | 无锡明盛纺织机械有限公司 | Anaerobic-aerobic-precipitation-diatomite adsorption treatment process for alkali-minimization wastewater in printing and dyeing industry |
| CN107032554A (en) * | 2016-11-22 | 2017-08-11 | 浙江丰林亚麻染整有限公司 | A kind of alkali decrement waste water dual treatment method and apparatus |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102219672A (en) | Method and device for producing pure terephthalic acid by alkali decrement wastewater residues | |
| CN101503353B (en) | Technique for purifying crude terephthalic acid from alkali deweighting wastewater | |
| CN104649300B (en) | The method of recovery and refining sodium bromide from dipropyl cyanoacetate mixture | |
| CN101314609B (en) | Process for preparing D-glucosamine hydrochlorate | |
| CN100503546C (en) | Method for purifying terephthalic acid from waste material | |
| CN113979987B (en) | Purification device and method for high-purity ethylene carbonate | |
| CN103981032A (en) | Method for decolorizing rice bran wax | |
| CN104086017A (en) | Treatment method of H acid separation waste water | |
| CN101244857B (en) | Alkali deweighting wastewater processing method and device | |
| CN101492399B (en) | Method for preparing methylpropene sodium sulfonate | |
| CN102234226A (en) | Method for recovering and purifying terephthalic acid in alkali-minimization waste liquor | |
| CN104086398A (en) | Method for separating and recovering oxalic acid from waste oxalic acid liquor | |
| CN104003910B (en) | The method extracting 5-sodium sulfo isophthalate waste water is produced from three monomers | |
| CN106928172A (en) | A kind of process for refining of dibenzofuran | |
| CN101284775B (en) | Process for reclaiming 2-keto-L-gulonate by salting out method | |
| CN114477250B (en) | Method for preparing magnesium sulfate by utilizing anthraquinone waste acid | |
| CN102731263B (en) | Recovery technology for disperse red 3B condensation mother liquor | |
| CN101525287B (en) | Method for refining sebacic acid | |
| CN103755555A (en) | Apparatus for producing purified terephthalic acid by using alkali-minimization wastewater residue | |
| CN106831390A (en) | A kind of method of utilization waste PET film preparation monomer PTA | |
| CN108569961A (en) | A kind of device producing p-phthalic acid | |
| RU2315715C1 (en) | Method of production of aluminum sulfate | |
| CN104529937A (en) | Method for continuously purifying rubber vulcanization accelerator M by using solvent | |
| CN104744238A (en) | Method for recovering glycolic acid in phenoxyacetic acid pesticide waste water | |
| CN105111077B (en) | A kind of method for reclaiming solvent in trimethylolpropane light component |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C12 | Rejection of a patent application after its publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20111019 |