CN102674489B - high-concentration ammonia-containing wastewater treatment method based on vapour compression - Google Patents
high-concentration ammonia-containing wastewater treatment method based on vapour compression Download PDFInfo
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- CN102674489B CN102674489B CN201210153670.8A CN201210153670A CN102674489B CN 102674489 B CN102674489 B CN 102674489B CN 201210153670 A CN201210153670 A CN 201210153670A CN 102674489 B CN102674489 B CN 102674489B
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- tower
- vapour
- ammonia
- temperature
- deammoniation
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- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 229910021529 ammonia Inorganic materials 0.000 title claims abstract description 37
- 230000006835 compression Effects 0.000 title claims description 6
- 238000007906 compression Methods 0.000 title claims description 6
- 238000004065 wastewater treatment Methods 0.000 title abstract description 3
- 239000002351 wastewater Substances 0.000 claims abstract description 21
- 230000009615 deamination Effects 0.000 claims abstract description 11
- 238000006481 deamination reaction Methods 0.000 claims abstract description 11
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 15
- 238000000034 method Methods 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 238000009833 condensation Methods 0.000 claims description 11
- 230000005494 condensation Effects 0.000 claims description 11
- 238000000605 extraction Methods 0.000 claims description 6
- 239000012141 concentrate Substances 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 5
- 230000002045 lasting effect Effects 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 239000010808 liquid waste Substances 0.000 claims description 5
- 238000002156 mixing Methods 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 3
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 238000011084 recovery Methods 0.000 abstract 1
- 238000005204 segregation Methods 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 8
- 239000003245 coal Substances 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000004134 energy conservation Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 230000008016 vaporization Effects 0.000 description 2
- 241000282326 Felis catus Species 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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Abstract
The invention relates to a high-concentration ammonia-containing wastewater treatment method based on vapour compressio, comprising the following steps: to-be-treated high-concentration ammonia-containing wastewater is pumped in a deamination tower after heat exchange, ammonia vapour is stripped from the top or the middle-upper part of the deamination tower, and then enters a vapour compressor tobe pressurized and heated, and then enters a reboiler at the bottom of the deamination tower to serve as a heat source of the deamination tower to exchange heat with a part of kettle solution of a tower kettle, the temperature of the ammonia vapour is decreased, and the ammonia vapour is partially condensed, and enters a subsequent segregation device to be concentrated and purified and then directly used, wherein the total ammonia content in the wastewater can be lower than 100 mg/L. Compared with the prior art, the recovery efficiency of ammonia is high, equipment investment is low, and onlya small amount of electric energy is needed, that is, the latent heat of the vapour generated on the top of the tower can be much adequately utilized, thus greatly saving energy consumption.
Description
Technical field
The present invention relates to a kind of method of handling strong ammonia wastewater, relate in particular to a kind for the treatment of process of the strong ammonia wastewater based on vapour compression.The invention belongs to wastewater treatment and energy-saving field.
Background technology
Strong ammonia wastewater is a class generation and the bigger waste water system of harm, extensively results from the commercial runs such as oil refining, gasification, coal tarization, pharmacy.For such waste water, generally must earlier will be just carrying out biochemical treatment or reuse behind the ammonia removal.
The steam stripped method is the common method that removes ammonia in the current industrial process, according to waste water composition and subsequent technique requirement, the technical matters such as single tower stripping of single tower stripping, double tower stripping and band side line is arranged generally.The ammonia that stripping goes out is generally produced liquefied ammonia or weak ammonia through fractional condensation, purification, refining back.Above-mentioned these stripping process all are to adopt live steam to make thermal source at the bottom of the tower, and power consumption is all than higher: if will remove sour gas and ammonia simultaneously the time, the consumption of ton water vapor is about the 190-330 kilogram; If be deamination, the steam consumption of ton water also will be more than 130 kilograms.
Develop more energy-conservation strong ammonia wastewater and handle new technology, have the dual value of economy and environmental protection.
Summary of the invention:
The objective of the invention is to develop more energy-conservation treatment process, propose a kind for the treatment of process of the strong ammonia wastewater based on vapour compression.This method adopts maturing appts of the prior art by utilizing the vapour compression technology, has realized the recycling of low-grade steam latent heat, can satisfy under the prerequisite for the treatment of effect, and system energy consumption is further reduced.
To achieve these goals, processing step of the present invention is:
Earlier after heat exchange, pump into pending strong ammonia wastewater in the deammoniation tower, the tower top pressure of controlling deammoniation tower respectively is 0～0.5MPa, tower top temperature is 90-150 ℃, tower bottom pressure is 0.02～0.52Mpa, column bottom temperature is 100～165 ℃, the mixing steam of ammonia and part water (hereinafter to be referred as ammoniacal liquor vapour) enters vapour compressor after being come out by stripping from the top of deammoniation tower or middle and upper part one side.After ammoniacal liquor vapour is forced into 0.2-1.5 MPa, temperature and is increased to 115-220 ℃ by vapour compressor, enter the reboiler at the bottom of the deamination Tata, thermal source as deammoniation tower, carry out heat exchange with the part still liquid of tower reactor, the ammoniacal liquor stripping temperature is reduced to 105-190 ℃, by partial condensation, enter follow-up fractional condensation device and concentrate and purify directly utilization of back.Simultaneously, by pipeline or pump extraction still liquid waste water, after the heat exchange cooling, enter lasting biochemical treatment apparatus or reuse from the deammoniation tower bottom.Feed live steam in the other reboiler of deammoniation tower, supply the part of shortage of heat.
The tower top pressure of more excellent deammoniation tower is controlled to be 0.1～0.20MPa in the present invention, and tower top temperature is 110-130 ℃.
Preferred tower bottom pressure is 0.12～0.22Mpa in the present invention, and column bottom temperature is 120～135 ℃.
After preferred ammoniacal liquor vapour is forced into 0.2-0.6 MPa, temperature and is increased to 133-165 ℃ by vapour compressor in the present invention, enter the reboiler at the bottom of the deamination Tata, as the thermal source of deammoniation tower.
After adopting this method to handle, total ammonia can be low to moderate below the 100mg/L in the waste water, can satisfy the biochemical treatment requirement fully.
The present invention compared with prior art only needs small amount of electrical energy, can more take full advantage of the latent heat of cat head extraction steam, has saved energy consumption significantly.The ammonia organic efficiency is higher, and facility investment economizes, and the equipment configuration technology maturation of using, and processing condition control is simple, can be widely used in the processing occasion of various ammonia-containing waters more.
Description of drawings:
Fig. 1 is process flow diagram of the present invention.
Embodiment:
Also be described further by reference to the accompanying drawings below by embodiment, but be not limitation of the invention further.
Embodiment 1:
Present embodiment is chosen the Coal Chemical Industry ammonia-containing water, and treatment capacity is 2 tons/hour, contains ammonia concentration 12000 mg/L.This waste water removes sour gas with vaporizing extract process earlier, pumps into after heat exchange then in the deammoniation tower, and the tower top pressure of controlling deammoniation tower respectively is 0.15MPa, and tower top temperature is 123 ℃, and tower bottom pressure is 0.16MPa, and column bottom temperature is 129 ℃.Ammoniacal liquor vapour enters vapour compressor after coming out from the top stripping of deammoniation tower.After ammoniacal liquor vapour is forced into 0.35MPa, temperature and is increased to 148 ℃ by vapour compressor, enter the reboiler at the bottom of the deamination Tata, thermal source as deammoniation tower, carry out heat exchange with the part still liquid of tower reactor, the ammoniacal liquor stripping temperature is reduced to 115 ℃, by partial condensation, enter follow-up fractional condensation device and concentrate and purify directly utilization of back.Simultaneously, by pump extraction still liquid waste water, after the heat exchange cooling, enter lasting biochemical treatment apparatus from the deammoniation tower bottom.Feed live steam in the other reboiler of deammoniation tower, supply the part of shortage of heat.
Adopt as above technology, its processed waste water total ammonia 15 mg/L meet the requirements.
Processing ton water is reduced to by 190 kilograms of 1.0MPa steam of original needs and only needs 95 kilograms of 0.4MPa steam, about 16 degree of power consumption.
Embodiment 2:
Present embodiment is chosen the Coal Chemical Industry ammonia-containing water, and treatment capacity is 2 tons/hour, contains ammonia concentration 12000 mg/L.This waste water removes sour gas with vaporizing extract process earlier, pumps into after heat exchange then in the deammoniation tower, and the tower top pressure of controlling deammoniation tower respectively is 0.25MPa, and tower top temperature is 135 ℃, and tower bottom pressure is 0.27Mpa, and column bottom temperature is 140.5 ℃.After the top stripping of ammoniacal liquor vapour deammoniation tower comes out, enter vapour compressor.After ammoniacal liquor vapour is forced into 0.6 MPa, temperature and is increased to 180 ℃ by vapour compressor, enter the reboiler at the bottom of the deamination Tata, thermal source as deammoniation tower, carry out heat exchange with the part still liquid of tower reactor, the ammoniacal liquor stripping temperature is reduced to 155 ℃, by partial condensation, enter follow-up fractional condensation device and concentrate and purify directly utilization of back.Simultaneously, by pump extraction still liquid waste water, after the heat exchange cooling, enter lasting biochemical treatment apparatus from the deammoniation tower bottom.Feed live steam in the other reboiler of deammoniation tower, supply the part of shortage of heat.
Adopt as above technology, its processed waste water total ammonia 45 mg/L meet the requirements.
Processing ton water is reduced to by 190 kilograms of 1.0MPa steam of original needs and only needs 90 kilograms of 0.6MPa steam, about 12 degree of power consumption.
Embodiment 3:
Present embodiment is chosen the Coal Chemical Industry ammonia-containing water, and treatment capacity is 2 tons/hour, contains ammonia concentration 12000 mg/L.This waste water pumps into after heat exchange in the deammoniation tower, and the tower top pressure of controlling deammoniation tower respectively is 0.02MPa, and tower top temperature is 98 ℃, and tower bottom pressure is 0.05MPa, and column bottom temperature is 102 ℃.After the top stripping of ammoniacal liquor vapour deammoniation tower comes out, enter vapour compressor.After ammoniacal liquor vapour is forced into 0.3MPa, temperature and is increased to 145 ℃ by vapour compressor, enter the reboiler at the bottom of the deamination Tata, thermal source as deammoniation tower, carry out heat exchange with the part still liquid of tower reactor, the ammoniacal liquor stripping temperature is reduced to 138 ℃, by partial condensation, enter follow-up fractional condensation device and concentrate and purify directly utilization of back.Simultaneously, by pump extraction still liquid waste water, after the heat exchange cooling, enter lasting biochemical treatment apparatus from the deammoniation tower bottom.Feed live steam in the other reboiler of deammoniation tower, supply the part of shortage of heat.
Adopt as above technology, its processed waste water total ammonia 32 mg/L meet the requirements.
The consumption of processing ton water vapor is reduced to 98 kilograms of 0.6MPa steam by 190 kilograms of 1.0MPa steam of former technology, about 14 degree of power consumption.
Claims (1)
1. treatment process based on the strong ammonia wastewater of vapour compression, earlier with pending strong ammonia wastewater, after heat exchange, pump in the deammoniation tower, the tower top pressure of controlling deammoniation tower respectively is 0.15MPa, tower top temperature is 123 ℃, tower bottom pressure is 0.16Mpa, column bottom temperature is 129 ℃, after the mixing steam of ammonia and part water forms ammoniacal liquor vapour and is come out by stripping from the top of deammoniation tower or middle and upper part one side, enter vapour compressor, be forced into 0.35 MPa, after temperature is increased to 148 ℃, enter the reboiler at the bottom of the deamination Tata, as the thermal source of deammoniation tower, carry out heat exchange with the part still liquid of tower reactor, the ammoniacal liquor stripping temperature is reduced to 115 ℃, by partial condensation, enters follow-up fractional condensation device and concentrates and purify directly utilization of back; Simultaneously, by pipeline or pump extraction still liquid waste water, after the heat exchange cooling, enter lasting biochemical treatment apparatus or reuse from the deammoniation tower bottom; Feed live steam in the other reboiler of deammoniation tower, supply the part of shortage of heat.
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| CN201210153670.8A CN102674489B (en) | 2012-05-17 | 2012-05-17 | high-concentration ammonia-containing wastewater treatment method based on vapour compression |
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| CN201210153670.8A CN102674489B (en) | 2012-05-17 | 2012-05-17 | high-concentration ammonia-containing wastewater treatment method based on vapour compression |
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| CN102674489B true CN102674489B (en) | 2013-09-18 |
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Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103408086A (en) * | 2013-08-02 | 2013-11-27 | 天华化工机械及自动化研究设计院有限公司 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
| CN103395841B (en) * | 2013-08-08 | 2015-08-05 | 北京赛科康仑环保科技有限公司 | The comprehensive utilization of resources technique of a kind of tungstenic crystalline mother solution and wash water |
| CN104058475B (en) * | 2014-07-11 | 2015-08-05 | 成都华西堂投资有限公司 | A kind of heat pump distillation deamination new energy-saving process |
| CN104083885B (en) * | 2014-07-11 | 2015-11-11 | 成都华西堂投资有限公司 | The heat pump distillation new energy-saving process of desulfurization solvent in renewable flue gas desulfurization |
| CN104843813A (en) * | 2014-12-30 | 2015-08-19 | 中国天辰工程有限公司 | Coal gasification high ammonia nitrogen wastewater treatment process |
| CN106379952A (en) * | 2015-08-07 | 2017-02-08 | 王树岩 | Apparatus and process for treating ammonia nitrogen wastewater and recycling ammonia |
| CN106015064B (en) * | 2016-06-06 | 2019-04-26 | 贵州赤天化股份有限公司 | The operating method of motor-driven compressor substitution steam driven compressor |
| CN106698785B (en) * | 2016-12-19 | 2020-04-10 | 青岛科技大学 | Coal gasification wastewater phenol-ammonia recovery process |
| CN107158734A (en) * | 2017-06-21 | 2017-09-15 | 河北乐恒化工设备制造有限公司 | The device and its energy-efficient concentrating method of N ethyl piperazidines of energy-efficient concentrate |
| CN109987669A (en) * | 2019-05-15 | 2019-07-09 | 济南冶金化工设备有限公司 | Ammonia steaming system and ammonia distillation process |
| CN111908697A (en) * | 2020-09-07 | 2020-11-10 | 查都（上海）科技有限公司 | Energy-saving phenol ammonia recovery unit |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB768830A (en) * | 1951-09-18 | 1957-02-20 | Metallgesellschaft Ag | Method of working up aqueous liquors containing ammonia |
| CN101264948A (en) * | 2008-04-25 | 2008-09-17 | 北京化工大学 | Ammonia nitrogen waste water discharge-reducing and ammonia nitrogen resource utilizing device and method |
| CN102190341A (en) * | 2010-03-09 | 2011-09-21 | 天华化工机械及自动化研究设计院 | Stripping ammonia-removing method based on flash evaporation and heat pump technologies |
| CN102320671A (en) * | 2011-06-17 | 2012-01-18 | 青岛科技大学 | Method for treating waste water containing acid and ammonia |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5335257A (en) * | 1976-09-14 | 1978-04-01 | Hitachi Zosen Corp | Method for treating drainage containing ammonia by steam stripping |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB768830A (en) * | 1951-09-18 | 1957-02-20 | Metallgesellschaft Ag | Method of working up aqueous liquors containing ammonia |
| CN101264948A (en) * | 2008-04-25 | 2008-09-17 | 北京化工大学 | Ammonia nitrogen waste water discharge-reducing and ammonia nitrogen resource utilizing device and method |
| CN102190341A (en) * | 2010-03-09 | 2011-09-21 | 天华化工机械及自动化研究设计院 | Stripping ammonia-removing method based on flash evaporation and heat pump technologies |
| CN102320671A (en) * | 2011-06-17 | 2012-01-18 | 青岛科技大学 | Method for treating waste water containing acid and ammonia |
Non-Patent Citations (1)
| Title |
|---|
| JP昭53-35257A 1978.04.01 |
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