CN103553172A - Coking residual ammonia water ammonia distillation process equipment and improved method - Google Patents
Coking residual ammonia water ammonia distillation process equipment and improved method Download PDFInfo
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- CN103553172A CN103553172A CN201310578282.9A CN201310578282A CN103553172A CN 103553172 A CN103553172 A CN 103553172A CN 201310578282 A CN201310578282 A CN 201310578282A CN 103553172 A CN103553172 A CN 103553172A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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Abstract
The invention provides coking residual ammonia water ammonia distillation process equipment and an improved method. The improved method is characterized in that ammonia steam containing NH3, H2S, HCN and other components, which are discharged from the top of an ammonia distillation tower, is pressurized by a first-stage heat pump, is fed into an acid pickling tower for pickling, ammonia removing and demisting so as to obtain ammonia-removed secondary steam; medium pressure steam supplemented for ammonia distillation is injected by a steam injector and is mixed with part of the secondary steam, and the mixed steam is guided to the lower part of an ammonia distillation tower and is used for ammonia water ammonia distillation; and part of secondary steam is pressurized by using a second-stage heat pump, is fed into a reboiler and exchanges heat with ammonia distillation wastewater and is used as a hot source of the reboiler for generating steam. Compared with the prior art, the improved method has the beneficial effects that the ammonia steam at the top of the ammonia distillation tower is subjected to adiabatic compression by the first-stage heat pump, so that the temperature and pressure of the ammonia steam are increased, ammonia in the pressurized ammonia steam is removed by an acid pickling method, so that the steam without ammonia can serve as secondary steam to be recycled in the ammonia distillation process, and the consumption of steam required for the residual ammonia water ammonia distillation is reduced.
Description
Technical field
The present invention relates to process the technical field of coking remained ammonia, relate in particular to a kind of coking remained ammonia ammonia distillation process equipment and improve one's methods.
Background technology
In the raw gas that process of coking produces, contain 300～450g/Nm
3water vapour.Raw gas is cooling through cyclic ammonia water spraying cooling and coal gas primary cooler, and the water vapour in raw gas enters cyclic ammonia water with coal gas cooling condensation Cheng Shui, and cyclic ammonia water amount also increases thereupon; This partial ammonia water (being referred to as remained ammonia) increasing in cyclic ammonia water is delivered to other device outward and is processed, and removes the detrimental impurity such as ammonia in remained ammonia, phenol and COD, and processed waste water is arranged outward after reaching national corresponding wastewater discharge standard.
At present, the remained ammonia ammonia distillation process of coke-oven plant generally adopts steam stripped method to remove the NH in remained ammonia
3, H
2the component such as S, HCN, ammonia still process tower top ammonia vapour drains into coal gas system, and at the bottom of ammonia still, distilled ammonia wastewater is delivered to biochemical treatment apparatus.For what make that distilled ammonia wastewater meets follow-up biochemical treatment apparatus, enter water requirement, ammoniacal liquor ammonia distillation process need to consume a large amount of steam.For improving the concentration of sending ammonia in ammonia vapour outside, at desorb tower top, be provided with ammonia vapour dephlegmator and ammonia vapour water cooler, ammonia vapour makes to send outside ammonia vapour through partial condensation backflow and reaches 15～18% containing ammonia concentration.Dephlegmator and ammonia vapour water cooler also need to consume a large amount of recirculated water when condensation ammonia vapour.Coke-oven plant urgently wishes by the improvement of ammonia distillation process and the application of new technology, realizes the steam consumption quantity that reduces ammonia distillation process, reduces remained ammonia processing cost.
Summary of the invention
The object of the present invention is to provide a kind of coking remained ammonia ammonia distillation process equipment and improve one's methods, ammonia still process tower top is discharged contains NH
3, H
2the ammonia vapour of the component such as S, HCN through one-level heat pump add force feed pickling tower acid wash-out ammonia, demist obtains deamination secondary steam; The supplementary middle pressure steam of ammonia still process mixes with part secondary steam by steam injector injection, and mixing steam causes ammonia still bottom for ammoniacal liquor ammonia still process; By secondary heat pump (mechanical vapor compressor), will after part secondary steam high pressure, deliver to reboiler and distilled ammonia wastewater heat exchange, as reboiler, produce the thermal source of steam.Incoagulability sour gas drains into coal gas system through vacuum pump.Have advantages of reduce costs, rational in infrastructure, simple to operate.
For achieving the above object, the present invention realizes by the following technical solutions:
A kind of coking remained ammonia ammonia distillation process equipment, comprise ammonia still, one-level heat pump, pickling tower, deentrainment tower, steam injector, secondary heat pump, reboiler, acid storage, acid cycle pump, washing water pump, it is characterized in that, described ammonia still top output terminal is connected with pickling tower by one-level heat pump, ammonia still bottom output terminal is connected by reboiler with input terminus pipeline, reboiler is connected with deentrainment tower pipeline at output by secondary heat pump, steam injector output terminal is connected with ammonia still, pickling top of tower output terminal is connected with deentrainment tower bottom by pipeline, pickling tower bottom output terminal is connected with acid storage, acid storage is connected with pickling tower top by acid cycle pump, deentrainment tower top output terminal is connected with steam injector by pipeline, deentrainment tower bottom is connected with washing water pump.
Described ammonia still tower top working pressure absolute pressure is between 0.05～0.15MPa, and at the bottom of ammonia still tower, working pressure is higher than more than tower top pressure 0.02MPa.
The diluted acid of described pickling tower scrubbing ammonia vapour is sulfuric acid or phosphoric acid.
Utilize the NH that contains of ammonia still process tower top discharge
3, H
2the steam of S, HCN is wherein 2～6% containing ammonia concentration.Ammonia vapour is delivered to pickling tower through one-level heat pump adiabatic compression, ammonia vapour removes the ammonia in ammonia vapour at pickling tower through weak acid scrubbing, deamination steam is discharged by tower top as secondary steam after deentrainment tower demist, part secondary steam is mixed and is delivered to ammonia still bottom by steam injector with the middle pressure steam filling into, part secondary steam again pressurizes and delivers to reboiler heating distilled ammonia wastewater through secondary heat pump, secondary steam is condensed into water and arranges outward in reboiler, incoagulability sour gas is through vacuum pumping to coal gas system, and concrete steps are as follows:
1) after remained ammonia and distilled ammonia wastewater heat exchange, enter ammonia still top, the steam that waste water reboiler produces enters at the bottom of by tower, and the middle pressure steam filling into enters ammonia still bottom with part secondary steam after steam injector mixes;
2) NH in remained ammonia
3, H
2the component such as S, HCN, is discharged by tower top through steam stripped desorb, and the distilled ammonia wastewater at the bottom of ammonia still is arranged outward through reboiler;
3) in the outer ammonia excretion vapour of tower top, contain NH
3, H
2the component such as S, HCN, ammonia vapour is delivered to pickling tower through the pressurization of one-level heat pump, and pickling tower adopts dilute sulphuric acid or dilute phosphoric acid scrubbing ammonia vapour, removes the ammonia in ammonia vapour;
4) deamination steam is flutterred the acid mist of carrying secretly in collection steam by deentrainment tower, deentrainment tower is divided into washing section and filler demist section, deamination steam enters at the bottom of by tower, after washing water pump 10 washing section circulated sprinkling washings and demist, by tower top, discharged, the deamination steam after deamination, demist is recycled in ammoniacal liquor ammonia still process as secondary steam;
5) ammoniacal liquor ammonia still process need to supplement a certain amount of middle pressure steam, middle pressure steam sprays and mixes with part secondary steam through steam injector, mixed secondary steam is delivered to ammonia still bottom, part secondary steam pressurizes again through secondary heat pump, after pressurization, deliver to reboiler and distilled ammonia wastewater indirect heat exchange, at the bottom of the steam that in reboiler, distilled ammonia wastewater produces enters ammonia still, secondary steam is condensed into water and arranges outward, and in secondary steam, incoagulability sour gas drains into coal gas system through vacuum pump;
6) vaporization of the distilled ammonia wastewater heat exchange rear section in reboiler, at the bottom of the steam of generation enters ammonia still, the distilled ammonia wastewater that reboiler is discharged is through ammoniacal liquor interchanger and remained ammonia heat exchange.
Compared with prior art, the invention has the beneficial effects as follows:
Ammonia still process tower top ammonia vapour improves the temperature and pressure of ammonia vapour through one-level heat pump adiabatic compression, the ammonia vapour after pressurization removes ammonia in ammonia vapour through acid wash, makes deamination steam can be used as secondary steam and recycles in ammonia distillation process.Reduce the consumption of the required steam of remained ammonia ammonia still process.
Accompanying drawing explanation
Fig. 1 is structure iron of the present invention.
1-ammonia still 2-one-level heat pump 3-pickling tower 4-deentrainment tower 5-steam injector 6-secondary heat pump 7-reboiler 8-acid storage 9-acid cycle pump 10-washing water pump
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is further illustrated:
As shown in Figure 1, a kind of coking remained ammonia ammonia distillation process equipment, by ammonia still 1, one-level heat pump 2, pickling tower 3, deentrainment tower 4, steam injector 5, secondary heat pump 6, reboiler 7, acid storage 8, acid cycle pump 9 and washing water pump 10 form, ammonia still 1 top output terminal is connected with pickling tower 3 by one-level heat pump 2, ammonia still 1 bottom output terminal is connected by reboiler 7 with input terminus pipeline, reboiler 7 by secondary heat pump 6 with go out deentrainment tower 4 pipeline at outputs and be connected, steam injector 5 output terminals are connected with ammonia still 1, pickling tower 3 top output terminals are connected with deentrainment tower 4 bottoms by pipeline, pickling tower 3 bottom output terminals are connected with acid storage 8, acid storage 8 is connected with pickling tower 3 tops by acid cycle pump 9, deentrainment tower 4 top output terminals are connected with steam injector 5 by pipeline, deentrainment tower 4 bottoms are connected with washing water pump 10.Ammonia still 1 tower top working pressure absolute pressure is between 0.05～0.15MPa, at the bottom of ammonia still 1 tower, working pressure is higher than more than tower top pressure 0.02MPa, the diluted acid of pickling tower 3 scrubbing ammonia vapour is sulfuric acid or phosphoric acid, the technical process of two kinds of weak acid scrubbing deaminations is identical, and following technical process narration be take sulfuric acid as example.
Utilize the NH that contains of ammonia still process tower top discharge
3, H
2the ammonia vapour of S, HCN is wherein 2～6% containing ammonia concentration.Ammonia vapour is delivered to pickling tower through one-level heat pump (vapour compressor) adiabatic compression.Ammonia vapour removes the ammonia in ammonia vapour at pickling tower through weak acid scrubbing, deamination steam is discharged by tower top as secondary steam after deentrainment tower demist, part secondary steam is mixed and is delivered to ammonia still bottom by steam injector with the middle pressure steam filling into, and part secondary steam again pressurizes and delivers to reboiler heating distilled ammonia wastewater through secondary heat pump.Secondary steam is condensed into water and arranges outward in reboiler, incoagulability sour gas through vacuum pumping to coal gas system.Its specific operation process is described below:
1) after remained ammonia and distilled ammonia wastewater heat exchange, enter ammonia still 1 top, the steam that waste water reboiler 7 produces enters at the bottom of by tower, and the middle pressure steam filling into enters ammonia still 1 bottom after steam injector 5 mixes with part secondary steam; ;
2) NH in remained ammonia
3, H
2the component such as S, HCN, is discharged by tower top through steam stripped desorb, and the distilled ammonia wastewater at 1 end of ammonia still is arranged outward through reboiler;
3) in the ammonia still 1 outer ammonia excretion vapour in top, contain NH
3, H
2the component such as S, HCN, ammonia vapour is delivered to pickling tower 3 through 2 pressurizations of one-level heat pump, and pickling tower 3 adopts dilute sulphuric acid washing ammonia vapour, removes the ammonia in ammonia vapour;
4) deamination steam is flutterred the acid mist of carrying secretly in collection steam by deentrainment tower 4, dilution heat of sulfuric acid in acid storage 8 is delivered to pickling tower top spray through acid cycle pump 9, ammonia in dilution heat of sulfuric acid absorbing ammonia vapour generates ammonium sulfate, ammonium sulfate liquor drains into acid storage 8 at the bottom of by tower, part ammonium sulfate liquor is delivered to ammonium sulfate device, and sulfuric acid and water add to acid storage 8.Deentrainment tower is divided into washing section and filler demist section, and deamination steam enters at the bottom of by tower, after the washing of washing section circulated sprinkling and demist, by tower top, is discharged, and the secondary steam part of discharge is mixed into ammonia still 1 bottom through steam injector 5 and the middle pressure steam that fills into.Deamination steam after deamination, demist is recycled in ammoniacal liquor ammonia still process as secondary steam;
5) ammoniacal liquor ammonia still process need to supplement a certain amount of middle pressure steam, middle pressure steam sprays and mixes with part secondary steam through steam injector, mixed secondary steam is delivered to ammonia still bottom, part secondary steam pressurizes again through secondary heat pump 6, after pressurization, deliver to reboiler 7 and distilled ammonia wastewater indirect heat exchange, at the bottom of the steam that in reboiler 7, distilled ammonia wastewater produces enters ammonia still, secondary steam is condensed into water and arranges outward, and in secondary steam, incoagulability sour gas drains into coal gas system through vacuum pump; The steam that the required steam of ammonia still 1 ammonia still process also can all be produced by reboiler 7 is supplied with at the bottom of tower;
6) vaporization of the distilled ammonia wastewater heat exchange rear section in reboiler, at the bottom of the steam of generation enters ammonia still, the distilled ammonia wastewater that reboiler is discharged is through ammoniacal liquor interchanger and remained ammonia heat exchange.
Ammonia vapour ammonia steam pressure after the pressurization of one-level heat pump is elevated between 1.2～1.5 times of scopes of original pressure; Deamination secondary steam is after steam injector, and vapor pressure is higher than more than ammonia still bottom pressure 0.02MPa; Deamination secondary steam after secondary heat pump pressurization, secondary steam temperature of saturation higher than ammonia still at the bottom of more than service temperature 10 ゜ C; When reboiler working pressure is during higher than coal gas system pressure, can cancel vacuum pump system, the non-condensable gases in reboiler directly drains into coal gas system.
In dilute sulphuric acid liquid absorbing ammonia vapour, ammonia generates ammonium sulfate, and the dilution heat of sulfuric acid of part sulfur-bearing ammonium is delivered to ammonium sulfate device and extracted sulphur ammonium.In dilute phosphoric acid liquid-absorbent ammonia vapour, ammonia generates phosphorus ammonium, and the dilute phosphoric acid solution of the phosphorous ammonium of part is delivered to phosphorus ammonium desorption apparatus and processed.
Claims (4)
1. a coking remained ammonia ammonia distillation process equipment, comprise ammonia still, one-level heat pump, pickling tower, deentrainment tower, steam injector, secondary heat pump, reboiler, acid storage, acid cycle pump, washing water pump, it is characterized in that, described ammonia still top output terminal is connected with pickling tower by one-level heat pump, ammonia still bottom output terminal is connected by reboiler with input terminus pipeline, reboiler is connected with deentrainment tower pipeline at output by secondary heat pump, steam injector output terminal is connected with ammonia still, pickling top of tower output terminal is connected with deentrainment tower bottom by pipeline, pickling tower bottom output terminal is connected with acid storage, acid storage is connected with pickling tower top by acid cycle pump, deentrainment tower top output terminal is connected with steam injector by pipeline, deentrainment tower bottom is connected with washing water pump.
2. a kind of coking remained ammonia ammonia distillation process equipment according to claim 1, is characterized in that, described ammonia still tower top working pressure absolute pressure is between 0.05～0.15MPa, and at the bottom of ammonia still tower, working pressure is higher than more than tower top pressure 0.02MPa.
3. a kind of coking remained ammonia ammonia distillation process equipment according to claim 1, is characterized in that, the diluted acid of described pickling tower scrubbing ammonia vapour is sulfuric acid or phosphoric acid.
4. adopting processing unit claimed in claim 1 to be used for improving the method for coking remained ammonia ammonia distillation process, is the NH that contains that utilizes the discharge of ammonia still process tower top
3, H
2the ammonia vapour of S, HCN is wherein 2～6% containing ammonia concentration.Ammonia vapour is delivered to pickling tower through one-level heat pump adiabatic compression, ammonia vapour removes the ammonia in ammonia vapour at pickling tower through weak acid scrubbing, deamination steam is discharged by tower top as secondary steam after deentrainment tower demist, part secondary steam is mixed and is delivered to ammonia still bottom by steam injector with the middle pressure steam filling into, part secondary steam again pressurizes and delivers to reboiler heating distilled ammonia wastewater through secondary heat pump, secondary steam is condensed into water and arranges outward in reboiler, incoagulability sour gas through vacuum pumping to coal gas system, it is characterized in that, concrete steps are as follows:
1) after remained ammonia and distilled ammonia wastewater heat exchange, enter ammonia still top, the steam that waste water reboiler produces enters at the bottom of by tower, and the middle pressure steam filling into enters ammonia still bottom with part secondary steam after steam injector mixes;
2) NH in remained ammonia
3, H
2the component such as S, HCN, is discharged by tower top through steam stripped desorb, and the distilled ammonia wastewater at the bottom of ammonia still is arranged outward through reboiler;
3) in the outer ammonia excretion vapour of ammonia still process tower top, contain NH
3, H
2the component such as S, HCN, ammonia vapour is delivered to pickling tower through the pressurization of one-level heat pump, and pickling tower adopts dilute sulphuric acid or dilute phosphoric acid scrubbing ammonia vapour, removes the ammonia in ammonia vapour;
4) deamination steam is flutterred the acid mist of carrying secretly in collection steam by deentrainment tower, deentrainment tower is divided into washing section and filler demist section, deamination steam enters at the bottom of by tower, after the washing of washing water pump washing section circulated sprinkling and demist, by tower top, discharged, the deamination steam after deamination, demist is recycled in ammoniacal liquor ammonia still process as secondary steam;
5) ammoniacal liquor ammonia still process need to supplement a certain amount of middle pressure steam, and middle pressure steam sprays and mixes with part secondary steam through steam injector, and mixed secondary steam is delivered to ammonia still bottom, and part contains H
2the secondary steam of S, HCN gas pressurizes again through secondary heat pump, after pressurization, deliver to reboiler and distilled ammonia wastewater indirect heat exchange, at the bottom of the steam that in reboiler, distilled ammonia wastewater produces enters ammonia still, secondary steam is condensed into water and arranges outward, and in secondary steam, incoagulability sour gas drains into coal gas system through vacuum pump;
6) vaporization of the distilled ammonia wastewater heat exchange rear section in reboiler, at the bottom of the steam of generation enters ammonia still, the distilled ammonia wastewater that reboiler is discharged is through ammoniacal liquor interchanger and remained ammonia heat exchange.
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Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104355321A (en) * | 2014-10-23 | 2015-02-18 | 中冶焦耐工程技术有限公司 | Technology and device for producing stronger ammonia water with controllable concentration by scrubbing ammonia through ammonium phosphate |
| CN104445476A (en) * | 2014-11-25 | 2015-03-25 | 徐翔 | Ethyl alcohol biogas slurry deamination technology and equipment |
| CN104743728A (en) * | 2015-03-27 | 2015-07-01 | 王文领 | Energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water |
| CN104860464A (en) * | 2015-05-22 | 2015-08-26 | 江西明兴环境工程有限公司 | Energy-saving ammonia-nitrogen wastewater treatment method and device |
| CN105417813A (en) * | 2015-11-09 | 2016-03-23 | 宁波科新化工工程技术有限公司 | Technique for treating desulfurization waste solution of carbonate under vacuum |
| CN105481036A (en) * | 2015-11-06 | 2016-04-13 | 王文领 | Energy-saving type negative-pressure deamination method of coked residual ammonia water |
| CN106219571A (en) * | 2016-09-14 | 2016-12-14 | 南京高捷轻工设备有限公司 | Evaporation deamination realizes degree of depth recovery system and the recovery method of ammonia near-zero release |
| CN106673014A (en) * | 2016-12-29 | 2017-05-17 | 天津市创举科技有限公司 | Process of removing sulfur and ammonia from coke gas to prepare ammonia water |
| CN108404639A (en) * | 2018-04-28 | 2018-08-17 | 中冶焦耐(大连)工程技术有限公司 | A kind of relieving haperacidity exhaust gas cleaner and technique |
| CN109647160A (en) * | 2017-10-12 | 2019-04-19 | 宝武炭材料科技有限公司 | Method for treating tail gas of ammonium sulfate mother liquor circulation tank |
| CN110575744A (en) * | 2019-10-09 | 2019-12-17 | 江苏沃德凯环保科技有限公司 | Special fabric ammonia-containing waste gas circulating purification and recovery process |
| CN114212850A (en) * | 2021-12-27 | 2022-03-22 | 中冶焦耐(大连)工程技术有限公司 | High-efficiency energy-saving thermal coupling ammonia distillation process |
| CN114229939A (en) * | 2021-12-27 | 2022-03-25 | 中冶焦耐(大连)工程技术有限公司 | High-efficiency energy-saving ammonia distillation process |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU656976A1 (en) * | 1976-10-25 | 1979-04-15 | Украинский научно-исследовательский углехимический институт | Method of reprocessing ammonia liquor of byproduct coke industry |
| CN100496660C (en) * | 2003-12-22 | 2009-06-10 | 济南钢铁集团总公司 | Process for treating residual ammonia water of coking |
| CN102527212A (en) * | 2011-12-07 | 2012-07-04 | 南京钢铁股份有限公司 | Comprehensive treating method and system for tail gas in ammoniac tank of coke-oven plant |
| CN103041679A (en) * | 2013-01-15 | 2013-04-17 | 美景（北京）环保科技有限公司 | Waste gas treatment system of acid gas containing ammonia |
| CN203625075U (en) * | 2013-11-15 | 2014-06-04 | 张卫东 | Ammonia still process equipment for coking remained ammonium hydroxide |
-
2013
- 2013-11-15 CN CN201310578282.9A patent/CN103553172B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| SU656976A1 (en) * | 1976-10-25 | 1979-04-15 | Украинский научно-исследовательский углехимический институт | Method of reprocessing ammonia liquor of byproduct coke industry |
| CN100496660C (en) * | 2003-12-22 | 2009-06-10 | 济南钢铁集团总公司 | Process for treating residual ammonia water of coking |
| CN102527212A (en) * | 2011-12-07 | 2012-07-04 | 南京钢铁股份有限公司 | Comprehensive treating method and system for tail gas in ammoniac tank of coke-oven plant |
| CN103041679A (en) * | 2013-01-15 | 2013-04-17 | 美景（北京）环保科技有限公司 | Waste gas treatment system of acid gas containing ammonia |
| CN203625075U (en) * | 2013-11-15 | 2014-06-04 | 张卫东 | Ammonia still process equipment for coking remained ammonium hydroxide |
Cited By (19)
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| CN104355321A (en) * | 2014-10-23 | 2015-02-18 | 中冶焦耐工程技术有限公司 | Technology and device for producing stronger ammonia water with controllable concentration by scrubbing ammonia through ammonium phosphate |
| CN104445476A (en) * | 2014-11-25 | 2015-03-25 | 徐翔 | Ethyl alcohol biogas slurry deamination technology and equipment |
| CN104743728A (en) * | 2015-03-27 | 2015-07-01 | 王文领 | Energy-saving type deaminizing method for realizing negative pressure deamination by coking surplus ammonia water |
| CN104860464A (en) * | 2015-05-22 | 2015-08-26 | 江西明兴环境工程有限公司 | Energy-saving ammonia-nitrogen wastewater treatment method and device |
| CN104860464B (en) * | 2015-05-22 | 2017-05-03 | 江西耐可化工设备填料有限公司 | Energy-saving ammonia-nitrogen wastewater treatment method and device |
| CN105481036A (en) * | 2015-11-06 | 2016-04-13 | 王文领 | Energy-saving type negative-pressure deamination method of coked residual ammonia water |
| CN105417813A (en) * | 2015-11-09 | 2016-03-23 | 宁波科新化工工程技术有限公司 | Technique for treating desulfurization waste solution of carbonate under vacuum |
| CN105417813B (en) * | 2015-11-09 | 2018-01-26 | 宁波科新化工工程技术有限公司 | A kind of vacuum carbonate desulfuration waste liquid treatment process method |
| CN106219571B (en) * | 2016-09-14 | 2018-08-21 | 南京高捷轻工设备有限公司 | Evaporate depth recovery system and recovery method that deamination realizes ammonia near-zero release |
| CN106219571A (en) * | 2016-09-14 | 2016-12-14 | 南京高捷轻工设备有限公司 | Evaporation deamination realizes degree of depth recovery system and the recovery method of ammonia near-zero release |
| CN106673014A (en) * | 2016-12-29 | 2017-05-17 | 天津市创举科技有限公司 | Process of removing sulfur and ammonia from coke gas to prepare ammonia water |
| CN106673014B (en) * | 2016-12-29 | 2018-11-23 | 天津市创举科技股份有限公司 | Process for preparing ammonia water by desulfurization and deamination of coke oven gas |
| CN109647160A (en) * | 2017-10-12 | 2019-04-19 | 宝武炭材料科技有限公司 | Method for treating tail gas of ammonium sulfate mother liquor circulation tank |
| CN108404639A (en) * | 2018-04-28 | 2018-08-17 | 中冶焦耐(大连)工程技术有限公司 | A kind of relieving haperacidity exhaust gas cleaner and technique |
| CN110575744A (en) * | 2019-10-09 | 2019-12-17 | 江苏沃德凯环保科技有限公司 | Special fabric ammonia-containing waste gas circulating purification and recovery process |
| CN114212850A (en) * | 2021-12-27 | 2022-03-22 | 中冶焦耐(大连)工程技术有限公司 | High-efficiency energy-saving thermal coupling ammonia distillation process |
| CN114229939A (en) * | 2021-12-27 | 2022-03-25 | 中冶焦耐(大连)工程技术有限公司 | High-efficiency energy-saving ammonia distillation process |
| CN114229939B (en) * | 2021-12-27 | 2024-04-26 | 中冶焦耐(大连)工程技术有限公司 | Efficient energy-saving ammonia distillation process |
| CN114212850B (en) * | 2021-12-27 | 2024-04-26 | 中冶焦耐(大连)工程技术有限公司 | Efficient energy-saving type thermal coupling ammonia distillation process |
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