CN1021810C - Coal gas sewage extraction dephenolization and ammonia distillation treatment method - Google Patents
Coal gas sewage extraction dephenolization and ammonia distillation treatment method Download PDFInfo
- Publication number
- CN1021810C CN1021810C CN 91104418 CN91104418A CN1021810C CN 1021810 C CN1021810 C CN 1021810C CN 91104418 CN91104418 CN 91104418 CN 91104418 A CN91104418 A CN 91104418A CN 1021810 C CN1021810 C CN 1021810C
- Authority
- CN
- China
- Prior art keywords
- ammonia
- tower
- sewage
- extraction agent
- extraction
- 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.)
- Expired - Fee Related
Links
Landscapes
- Physical Water Treatments (AREA)
- Gas Separation By Absorption (AREA)
Abstract
A coal gas sewage extraction dephenolization and ammonia distillation treatment method comprises the following steps: 1. pumping the coal gas sewage into a washing tower; 2. pumping into an extraction tower for phenol removal; 3. the phenol-containing extractant enters a distillation tower, and the recovered extractant can be recycled; 4. the extracted sewage directly enters an ammonia still, and ammonia and a dissolved extracting agent are blown off by steam; 5. selectively absorbing ammonia by using ammonium phosphate barren solution in an absorption tower, and absorbing the extracting agent by the original sewage in a washing tower after cooling; 6. the rich ammonium phosphate solution is resolved in a desorption tower and cooled into concentrated ammonia water. The process has the advantage of saving equipment cost and running cost. Is suitable for the sewage treatment of coal gas or coal coking.
Description
The invention belongs to a kind of sewage water treatment method.
Widespread use gas maked coal technology in preparation town gas and material gas, but these technologies produce the sewage that contains phenol, ammonia and other objectionable impurities in a large number in the feed coal gasification, these sewage toxicities are big, the directly discharging as not handled, contaminate environment not only, and waste a large amount of industrial chemicals.This has become a major issue of restriction gas maked coal technological development.
At home, producer gas plant mostly adopts solvent dephenolize and chemical regeneration technology.This method equipment complexity, quality of sewage disposal are poor.And abroad extensively adopt extracting and dephenolizing and rectifying regeneration ammonia distillation process, wherein extracting and dephenolizing process application existing history for many years in gas sewage phenol reclaims is a kind of new ammonia reclaiming process that external developed recently gets up and select to absorb ammonia distillation process with ammonium phosphate solution.This technology is compared with chemical regeneration technology with the domestic solvent dephenolize of adopting in the past, have flow process short, do not need advantages such as soda acid, power consumption are low.But external producer uses this two simple combination that technology only is two technologies.In extracting and dephenolizing technology, the technology that adopts extracting and dephenolizing and rectifying regeneration to reclaim.Gas sewage is behind extracting and dephenolizing, generally contain 1～2% dissolved extraction agent, in order to reclaim this part extraction agent, existing extracting and dephenolizing technology is provided with and reclaims the operation that is dissolved in extraction agent in the sewage, the general sewage that adopts is through nitrogen or coal gas vaporizing extract process, therefore, need be provided with a cover coal gas stripping tower, crude phenols washing tower and coal gas supercharging system specially, to reclaim this dissolution extraction agent of 1～2%.
The objective of the invention is this technical process is simplified, save and reclaim coal gas stripping tower, crude phenols washing tower and the coal gas supercharging system that is dissolved in extraction agent in the sewage, reduce investment outlay and working cost, and can reach identical water treatment effect.
Gas sewage extracting and dephenolizing ammonia still process treatment process of the present invention is made up of extracting and dephenolizing technology and ammonia distillation process, it is characterized in that: reclaim the extraction agent that is dissolved in the sewage and finished by ammonia distillation process, the steps include:
(1) gas sewage is pumped into washing tower, steam the extraction agent that is dissolved in the sewage by ammonia still to reclaim;
(2) pump into extraction tower,, reclaim phenolic compound in the sewage with the extraction agent counter current contact;
(3) contain the phenol extraction agent and enter distillation tower and carry out rectifying separation, the extraction agent of recovery enters extraction tower and recycles;
(4) gas sewage after the extraction directly enters ammonia still, with steam ammonia, dissolution extraction agent and sour gas stripping in the water is come out;
(5) water vapour that contains ammonia, extraction agent selects to absorb ammonia with phosphorus ammonium barren liquor in the absorption tower, and residue extraction agent cooling back is absorbed by raw waste water in washing tower, and control scrubber overhead temperature can be emitted sour gas;
(6) phosphorus ammonium pregnant liquor of inhaling behind the ammonia parses ammonia in desorption tower, and becomes strong aqua after the cat head cooling, and the phosphorus ammonium barren liquor after resolving returns the absorption tower and recycles.
Advantage of the present invention is: cancelled the stripping and the stripping equipment of dissolution extraction agent in the special recycle-water, and itself and ammonia still are merged into a stripping tower, technical process is shortened, facility investment saves about 1/5; Running expense reduces by 1/10; More domestic solvent dephenolize and the chemical regeneration technology that generally adopts reduces cost over half.
Adopt present method to handle gas sewage and adopt other method effect identical, the volatile phenol rate of recovery＞99% wherein, ammonia recovery＞95% volatilizees.
The purity that reclaims crude phenols and strong aqua is higher, and impurity is few, helps further processing and utilization.Phenol content reaches 83% in the crude phenols, and ammonia content can reach 25% in the ammoniacal liquor.
The present invention handles applicable to lurgi pressure gasification sewage, coal gasification of coking sewage and other various extracting and dephenolizing, ammonia still processs that contain phenol, ammonia gas sewage.
Accompanying drawing is a process flow diagram of the present invention.
Embodiment:
The gas sewage that contains phenol and ammonia at first enters extraction tower through behind the washing tower, in extraction tower and extraction agent (isopropyl ether) counter current contact, phenol is proposed by isopropyl ether in the water, contain the phenol isopropyl ether and enter distillation tower and utilize the difference of isopropyl ether boiling point (68 ℃) and phenolic compound boiling point (＞160 ℃) to carry out rectifying separation, reclaim the back isopropyl ether and enter extraction tower and recycle.
Sewage after the extraction directly enters ammonia still, with steam ammonia, isopropyl ether and sour gas in the water stripping are together come out, sewage can go the hypomere art breading, the water vapour that contains ammonia, isopropyl ether selects to absorb ammonia with phosphorus ammonium barren liquor in the absorption tower, residue isopropyl ether cooling back is absorbed by raw wastewater in washing tower, and control washing column bottom temperature (～40 ℃) can be with sour gas (H
2SCO
2) wait and emit, remove recycle section.Inhale phosphorus ammonium pregnant liquor resolved ammonia that goes out to be absorbed in desorption tower behind the ammonia, ammonia becomes further processing and utilization of strong aqua after the cat head cooling, and phosphorus ammonium barren liquor returns the absorption tower and recycles after the cat head desorb.
Washing tower tower top temperature of the present invention is 35-40 ℃, about 25 ℃ of inflow temperature, and leaving water temperature(LWT) is 28-30 ℃, the extraction temperature of extraction tower is 28-32 ℃; Distillation Tata still temperature is 185-190 ℃, 64 ℃ of tower top temperatures; 85～90 ℃ of the inflow temperatures of ammonia still, tower still pressure is 0.01～0.02MP, 103-104 ℃ of tower still temperature, 98 ± 1 ℃ of tower top temperatures; The tower top temperature on absorption tower is 96 ± 1 ℃; The feeding temperature of desorption tower is 150 ℃, and tower still pressure is 1.15-1.20MP, and tower still temperature is 167 ± 3 ℃, and reflux ratio is about 1.Extraction agent of the present invention can use high ester, ether, ketone compounds or its mixtures of partition ratio such as isopropyl ether, hexone, N-BUTYL ACETATE.
Claims (1)
1, a kind of gas sewage extracting and dephenolizing, ammonia still process treatment process are made up of extracting and dephenolizing technology and ammonia distillation process, reclaim the dissolution extraction agent and are finished by ammonia distillation process, the steps include:
(1) gas sewage is pumped into washing tower, steam the extraction agent that is dissolved in the sewage by ammonia still to reclaim;
(2) pump into extraction tower,, reclaim phenolic compound in the sewage with the extraction agent counter current contact;
(3) contain the phenol extraction agent and enter distillation tower and carry out rectifying separation, the extraction agent of recovery enters extraction tower and recycles; It is characterized in that:
(4) gas sewage after the extraction directly enters ammonia still.With steam ammonia, dissolution extraction agent and sour gas stripping in the water are come out;
(5) water vapour that contains ammonia, extraction agent selects to absorb ammonia with phosphorus ammonium barren liquor in the absorption tower, and residue extraction agent cooling back is absorbed by raw waste water in washing tower, and control scrubber overhead temperature can be emitted sour gas;
(6) the phosphorus ammonia rich solution of inhaling behind the ammonia parses ammonia in desorption tower, and becomes strong aqua after the cat head cooling, and the phosphorus ammonia lean solution of cat head after resolving returned the absorption tower and recycled.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 91104418 CN1021810C (en) | 1991-07-04 | 1991-07-04 | Coal gas sewage extraction dephenolization and ammonia distillation treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 91104418 CN1021810C (en) | 1991-07-04 | 1991-07-04 | Coal gas sewage extraction dephenolization and ammonia distillation treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1056893A CN1056893A (en) | 1991-12-11 |
| CN1021810C true CN1021810C (en) | 1993-08-18 |
Family
ID=4906607
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 91104418 Expired - Fee Related CN1021810C (en) | 1991-07-04 | 1991-07-04 | Coal gas sewage extraction dephenolization and ammonia distillation treatment method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1021810C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1102483C (en) * | 1996-08-16 | 2003-03-05 | 布劳恩股份有限公司 | Dry shaving apparatus with guard member |
| CN102241453A (en) * | 2010-09-25 | 2011-11-16 | 仲恺农业工程学院 | Method for treating coal gasification wastewater containing phenol and ammonia |
| CN105174577A (en) * | 2015-08-06 | 2015-12-23 | 中钢集团鞍山热能研究院有限公司 | Coal chemical wastewater pretreatment process and device |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1332891C (en) * | 2004-07-21 | 2007-08-22 | 清华大学 | Hydrogen peroxide catalytic decomposing method of phenol compound |
| CN1298629C (en) * | 2005-02-17 | 2007-02-07 | 昆明理工大学 | Method for recoverying and utilization of pulluted ammonia water of brown coal pressurized gasification |
| CN102485851A (en) * | 2010-12-01 | 2012-06-06 | 鞍钢集团工程技术有限公司 | Method and apparatus for removing acid-containing droplet in gas from soda acid neutralization deamination |
| CN102060407A (en) * | 2010-12-05 | 2011-05-18 | 天津市华瑞奕博化工科技有限公司 | System and method for treating butyl acetate waste water |
| CN102259943B (en) * | 2011-07-21 | 2012-08-22 | 天津市昊永化工科技有限公司 | Energy-saving method for recycling wastewater containing phenol and ammonia |
| CN103496757A (en) * | 2013-09-29 | 2014-01-08 | 河南龙成煤高效技术应用有限公司 | Method for extraction dephenolization of high-concentration chemical wastewater containing phenol ammonia coals |
| CN103496812A (en) * | 2013-09-29 | 2014-01-08 | 河南龙成煤高效技术应用有限公司 | Method for treating high-concentration phenol-ammonia wastewater |
| CN103964543B (en) * | 2014-05-06 | 2016-01-27 | 河南龙成煤高效技术应用有限公司 | A kind of method of coal chemical technology waste water oil removing dephenolize |
| CN105418382B (en) * | 2014-09-22 | 2018-05-04 | 上海宝钢化工有限公司 | Purification method of sodium phenolate containing neutral oil |
-
1991
- 1991-07-04 CN CN 91104418 patent/CN1021810C/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1102483C (en) * | 1996-08-16 | 2003-03-05 | 布劳恩股份有限公司 | Dry shaving apparatus with guard member |
| CN102241453A (en) * | 2010-09-25 | 2011-11-16 | 仲恺农业工程学院 | Method for treating coal gasification wastewater containing phenol and ammonia |
| CN105174577A (en) * | 2015-08-06 | 2015-12-23 | 中钢集团鞍山热能研究院有限公司 | Coal chemical wastewater pretreatment process and device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1056893A (en) | 1991-12-11 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101665309B (en) | Method for treating gasified waste water containing high-concentration phenol and ammonia | |
| CN1021810C (en) | Coal gas sewage extraction dephenolization and ammonia distillation treatment method | |
| WO1991016288A1 (en) | Process for separating impurities from aqueous solution of crude ethanol | |
| CN109081767B (en) | Synthetic rectification process method and equipment for methane chloride | |
| CN109206291A (en) | A kind of separation method of chloromethanes-dimethyl ether | |
| CN106145426A (en) | In a kind of coal chemical industrial waste water, carbolic oil is combined removing system and processes technique | |
| CN102432453A (en) | Process and equipment for purifying dilute acetic acid solution | |
| CN111574478B (en) | Process for preparing epoxypropane by oxidizing propylene with hydrogen peroxide | |
| CN100447120C (en) | Technological process for refining trimethylolpropane | |
| CN103466873B (en) | A kind of process is containing the method for high-concentration phenol, ammonia sewage | |
| US4342731A (en) | Method for removing hydrogen sulfide from coke oven gas | |
| JP4535543B2 (en) | Isolation of glycol | |
| CN113735354A (en) | Method and device for treating alcohol-containing wastewater in coal-to-ethylene glycol technology | |
| KR102756942B1 (en) | Continuous multi-stage treatment apparatus for separating and recovering phosphoric acid from mixed waste acid and as the same method | |
| US4622104A (en) | Process for the recovery of ethylene glycol in concentrated form | |
| CN205223068U (en) | System for retrieve dimethyl sulfoxide , ethanolamine among useless organic solvent of follow | |
| JP3516168B2 (en) | Phenol recovery method | |
| CN105585212A (en) | Comprehensive treating and recycling method for PTA (purified terephthalic acid) production wastewater | |
| CN214299725U (en) | Purification device for PTA (purified terephthalic acid) refining mother liquor | |
| US4049782A (en) | Process for producing pure concentrated ammonia | |
| CN106946651A (en) | A kind of method of extracting rectifying and reaction side line rectification process ethanol, isopropanol and formaldehyde composite waste | |
| CN1151123C (en) | Acetonitrile refining and recovering process | |
| CN112520931A (en) | Purification method and device for PTA (purified terephthalic acid) refining mother liquor | |
| CN222266660U (en) | System for recovering methyl nitrite gas and purifying dimethyl oxalate | |
| CN105237441B (en) | Device and method for recovering methane sulfonic acid |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |