CN103408086A - MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof - Google Patents
MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof Download PDFInfo
- Publication number
- CN103408086A CN103408086A CN2013103333897A CN201310333389A CN103408086A CN 103408086 A CN103408086 A CN 103408086A CN 2013103333897 A CN2013103333897 A CN 2013103333897A CN 201310333389 A CN201310333389 A CN 201310333389A CN 103408086 A CN103408086 A CN 103408086A
- Authority
- CN
- China
- Prior art keywords
- ammonia
- steam
- deamination
- stripping
- ammoniacal liquor
- 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
Landscapes
- Physical Water Treatments (AREA)
Abstract
The invention relates to an MVR vapor-stripping deamination system. The MVR (Mechanical Vapor Recompression) vapor-stripping deamination system comprises a vapor-stripping deamination tower, an ammonia water rectification tower and a condenser, wherein a high-ammonia-nitrogen sewage input pipe, a vapor input pipe I, a post-deamination waste water discharge port and an ammonia-containing vapor discharge port I are arranged on the vapor-stripping deamination tower; the vapor-stripping deamination tower is connected with a reboiler; the high-ammonia-nitrogen sewage input pipe is connected with waste water feed preheaters (II and I); the post-deamination waste water discharge port is connected with the waste water feed preheater I and an axial flow pump respectively; the ammonia-containing vapor discharge port I is connected with the reboiler through a mechanical vapor compressor; the reboiler is connected with a dilute ammonia water storage tank connected with the ammonia water rectification tower; a discharge port, an ammonia-containing vapor discharge port II and a vapor input pipe are arranged on the ammonia water rectification tower; the discharge port is connected with a rectification tower kettle discharge pump and the waste water feed preheater II; the ammonia-containing vapor discharge port II is connected with the condenser; a strong ammonia water discharge port is connected with a strong ammonia water storage tank connected with the ammonia water rectification tower. Meanwhile, the invention further discloses an application method of the MVR vapor-stripping deamination system. The MVR vapor-stripping deamination system has the advantages of less investment, high feasibility and high comprehensive utilization ration.
Description
Technical field
The present invention relates to ammonia-containing water deamination processing technology field, relate in particular to a kind of MVR stripping deamination system and method thereof.
Background technology
The industries such as petrochemical industry, metallurgy, food usually can produce the waste water of a large amount of ammonia nitrogens.Because the cost compare of processing ammonia nitrogen waste water is high, wherein the consumption of steam usually more than 180kg/t waste water, installs not energy-conservationly, and working cost is high, and enterprise is difficult to bear.
Ammonia-containing water removes technology biochemical process, blow-off method, vaporizing extract process, break point chlorination, ion exchange method, chemical precipitation method, membrane separation process etc. usually.At present, the ammonia-nitrogen content produced in processing industry adopts comparative maturity and the technology that extensively adopts is by the method for steam stripped rectifying deamination usually at the high-concentration ammonia nitrogenous wastewater of 500 ~ 10000ppm, high ammonia-nitrogen wastewater, after the stripping stage stripping of steam stripping ammonia-removing tower, then is produced to certain density ammoniacal liquor after rectifying section rectifying.Owing in stripping process, consuming a large amount of steam, and steam is produced ammoniacal liquor by the condensation of rectifying section overhead condenser, so steam consumption is higher.Although the research that reduces energy consumption by economic benefits and social benefits stripping deamination technique is arranged domestic, by economic benefits and social benefits stripping deamination technique, can make steam consumption reduce by 40 ~ 45%, yet concerning high ammonia-nitrogen wastewater was processed, energy consumption was still higher.
Function of mechanical steam recompression (Mechanical Vapor Recompression) technology, be called for short the MVR technology, in the evaporation operation unit, latent heat due to its 100% circulation secondary steam, system itself can reach thermal equilibrium substantially, live steam only starts to start preheating for system, thereby significantly reduce the consumption of vaporizer to external live steam, with respect to multiple-effect evaporation, it is a kind of novel high-efficiency and energy-saving device, now be widely used in trade effluent, the concentrated decrement treatment of black liquid, dairy products, sugaring, the distillation and concentrations such as starch are processed, and sea water desaltination, a lot of production fields such as salt manufacturing.But for high ammonia-nitrogen wastewater, due to the common more complicated of waste water quality, therefore only with the MVR technology carry out evaporative crystallization not only steam output greatly and also the product obtained impure, can't industrial reuse.
Summary of the invention
Technical problem to be solved by this invention is to provide a kind of MVR stripping deamination system little, easy to implement of investing.
Another technical problem to be solved by this invention is to provide a kind of application method of energy-efficient this MVR stripping deamination system.
For addressing the above problem, a kind of MVR stripping deamination system of the present invention, comprise steam stripping ammonia-removing tower, ammoniacal liquor rectifying tower, condenser, it is characterized in that: a upper lateral part of described steam stripping ammonia-removing tower is provided with the high-ammonia-nitrogen sewage input tube, the one side lower part is provided with the steam input pipe I, its opposite side bottom is connected with reboiler by the pipeline I, and its bottom is provided with the discharge of wastewater mouth after deamination, and its top is provided with and contains ammonia steam outlet I; Described high-ammonia-nitrogen sewage input tube is connected with wastewater feed preheater II, wastewater feed preheater I successively, and this wastewater feed preheater II, wastewater feed preheater I are equipped with the deamination effluent outfall; Discharge of wastewater mouth after described deamination is connected with respectively described wastewater feed preheater I, propeller pump by the pipeline II, and this propeller pump is connected with described reboiler; The described ammonia steam outlet I that contains is connected with described reboiler by the mechanical vapour compressor; One side of described reboiler is provided with the weak ammonia discharge outlet, and is connected with the weak ammonia storage tank by this weak ammonia discharge outlet; Described weak ammonia storage tank is connected with described ammoniacal liquor rectifying tower through rectifying fresh feed pump, interchanger successively; The bottom of described ammoniacal liquor rectifying tower is provided with discharge port, and its top is provided with and contains ammonia steam outlet II, and the one side is provided with the steam input pipe II; Described discharge port is connected with rectifying tower reactor discharging pump by the pipeline III, and with described wastewater feed preheater II, is connected through described interchanger by rectifying tower reactor discharging pump; The described ammonia steam outlet II that contains is connected with described condenser by the pipeline IV, and this condenser is respectively equipped with recirculated water backwater discharge outlet, circulating water intake, strong aqua discharge outlet; Described strong aqua discharge outlet is connected with the strong aqua storage tank by the pipeline V, and this strong aqua storage tank is connected with described ammoniacal liquor rectifying tower, strong aqua output tube respectively through the ammoniacal liquor reflux pump.
Described mechanical vapour compressor refers to positive-displacement compressor or radial compressor, and compressor boost is 20 ~ 80kPa.
Described reboiler refers to a kind of in vertical thermosyphon reboiler, the vertical reboiler of forced cyclic type, horizontal reboiler.
On described mechanical vapour compressor, propeller pump, rectifying fresh feed pump, rectifying tower reactor discharging pump, ammoniacal liquor reflux pump, be equipped with under meter.
The application method of a kind of MVR stripping deamination system as above comprises the following steps:
(1) will through wastewater feed preheater I, wastewater feed preheater II, enter steam stripping ammonia-removing tower successively through pretreated high-ammonia-nitrogen sewage, simultaneously, steam is inputed to described steam stripping ammonia-removing tower and carry out the stripping deamination, obtaining respectively temperature and be 95 ~ 110 ℃ and pressure is the steam that contains ammonia 3 ~ 8% of 0.085 ~ 0.15MPa and the waste water after deamination;
(2) the described steam that contains ammonia 3 ~ 8% enters reboiler through containing after ammonia steam outlet I is heated by the mechanical vapour compressor pressurizes; Simultaneously, a waste water part after described deamination is discharged by the deamination effluent outfall through wastewater feed preheater I, all the other bottom lease making propeller pump enter described reboiler, the described steam that contains ammonia 3 ~ 8% evaporates the waste water after described deamination in described reboiler, the steam after being evaporated respectively and condensed mass concentration are 3 ~ 8% ammoniacal liquor; Steam after described evaporation enters in described steam stripping ammonia-removing tower as stripping deamination steam;
(3) described condensed mass concentration is that 3 ~ 8% ammoniacal liquor enters the weak ammonia storage tank through the weak ammonia discharge outlet, and through rectifying fresh feed pump, interchanger, enters in the ammoniacal liquor rectifying tower successively; Simultaneously, steam is inputed in described ammoniacal liquor rectifying tower and carries out steam stripped rectifying, obtain respectively the deamination waste water after up to standard and contain the steam of ammonia 15 ~ 30%; Described deamination waste water after up to standard is discharged by the deamination effluent outfall through wastewater feed preheater II by rectifying tower reactor discharging pump, described interchanger successively;
(4) the described steam that contains ammonia 15 ~ 30% enters condenser condenses through containing ammonia steam outlet II, obtain mass concentration and be 15 ~ 30% ammoniacal liquor, this mass concentration is that 15 ~ 30% ammoniacal liquor is divided into two portions through the strong aqua discharge outlet by the ammoniacal liquor reflux pump, wherein a part is through the output of strong aqua output tube, and rest part enters described ammoniacal liquor rectifying tower and carries out rectifying.
The pretreated high-ammonia-nitrogen sewage of described step in (1) refers to that ammonia-nitrogen content is that the pH value of 500 ~ 10000ppm is adjusted to 11.5 ~ 12.0 ammonia-containing water.
(1) the steam in (3) all refers to saturation steam or superheated vapour to described step with described step.
The present invention compared with prior art has the following advantages:
1, the present invention utilizes the function of mechanical steam recompression technology, steam after the stripping deamination is improved to the pressure and temperature of steam by mechanically compress, heat source as the steam stripping ammonia-removing tower tower bottom reboiler is used, make in stripping deamination process only to consume a small amount of compressor start power of motor, only in start-up course, consume a small amount of steam, in course of normal operation without extra consumption stripped vapor, reduced the consumption of stripping steam, effectively solved traditional process for treating high ammonia nitrogen waste water steam consumption quantity run into high, the problem that running cost is high, accomplished energy-saving, innoxious, minimizing, the processing of stabilization.
2, the ammonia concn comparison low pass that produces after by MVR stripping deamination of the present invention 3 ~ 5% left and right of being everlasting, need further by rectifying tower, to carry out the rectifying concentrate, only need to consume a small amount of steam, concentrate by the preliminary of MVR, need the weak ammonia of rectifying only to be 1/20 ~ 1/100 of original wastewater flow rate.
3, with China Petrochemical Industry's catalyst plant 40m3/h high ammonia-nitrogen wastewater, be treated to example, due to ammonia-nitrogen content in waste water usually in about 6000mg/l, waste water after processing reaches national grade one discharge standard, the ammonia concn obtained after treatment is 25%, apply respectively single tower stripping distillation technology, economic benefits and social benefits stripping deamination technology and MVR stripping deamination method wastewater treatment is calculated, calculation result sees the following form 1
Table 1
Remarks: the steam price is according to 200 yuan/t, and industrial electro is calculated according to 0.8 yuan/kWh.
As can be seen from Table 1, adopt MVR stripping deamination method running cost be about the stripping distillation technology and 33%, be 58% of economic benefits and social benefits steam stripping technique; In addition, the use of MVR stripping deamination method, minimizing due to the rectifying amount, requirement for recirculated cooling water also reduces greatly, by above analysis, can be drawn, MVR stripping deamination method has reduced the running cost of wastewater treatment significantly, and ammonia nitrogen waste water is processed and had very important realistic meaning.
4, the present invention invests littlely, easy to implement, can be widely used in the inorganic ammonia nitrogen wastewater treatment industry such as petrochemical industry, metallurgy, food.
The accompanying drawing explanation
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described in further detail.
Fig. 1 is the process flow sheet of invention.
In figure: 1-wastewater feed preheater I, 2-wastewater feed preheater II, 3-steam stripping ammonia-removing tower, 4-mechanical vapour compressor, 5-reboiler, 6-propeller pump, 7-weak ammonia storage tank, 8-interchanger, 9-ammoniacal liquor rectifying tower, 10-rectifying fresh feed pump, 11-rectifying tower reactor discharging pump, 12-condenser, 13-strong aqua storage tank, 14-ammoniacal liquor reflux pump.
Embodiment
As shown in Figure 1, a kind of MVR stripping deamination system, comprise steam stripping ammonia-removing tower 3, ammoniacal liquor rectifying tower 9, condenser 12.
One upper lateral part of steam stripping ammonia-removing tower 3 is provided with the high-ammonia-nitrogen sewage input tube, the one side lower part is provided with the steam input pipe I, its opposite side bottom is connected with reboiler 5 by the pipeline I, and its bottom is provided with the discharge of wastewater mouth after deamination, and its top is provided with and contains ammonia steam outlet I; The high-ammonia-nitrogen sewage input tube is connected with wastewater feed preheater II 2, wastewater feed preheater I 1 successively, and this wastewater feed preheater II 2, wastewater feed preheater I 1 are equipped with the deamination effluent outfall; Discharge of wastewater mouth after deamination is connected with respectively wastewater feed preheater I 1, propeller pump 6 by the pipeline II, and this propeller pump 6 is connected with reboiler 5; Containing ammonia steam outlet I is connected with reboiler 5 by mechanical vapour compressor 4; One side of reboiler 5 is provided with the weak ammonia discharge outlet, and is connected with weak ammonia storage tank 7 by this weak ammonia discharge outlet; Weak ammonia storage tank 7 is connected with ammoniacal liquor rectifying tower 9 through rectifying fresh feed pump 10, interchanger 8 successively; The bottom of ammoniacal liquor rectifying tower 9 is provided with discharge port, and its top is provided with and contains ammonia steam outlet II, and the one side is provided with the steam input pipe II; Discharge port is connected with rectifying tower reactor discharging pump 11 by the pipeline III, and with wastewater feed preheater II 2, is connected through interchanger 8 by rectifying tower reactor discharging pump 11; Contain ammonia steam outlet II and be connected with condenser 12 by the pipeline IV, this condenser 12 is respectively equipped with recirculated water backwater discharge outlet, circulating water intake, strong aqua discharge outlet; The strong aqua discharge outlet is connected with strong aqua storage tank 13 by the pipeline V, and this strong aqua storage tank 13 is connected with ammoniacal liquor rectifying tower 9, strong aqua output tube respectively through ammoniacal liquor reflux pump 14.
Wherein:
Mechanical vapour compressor 4 refers to positive-displacement compressor or radial compressor, and compressor boost is 20 ~ 80kPa.
Reboiler 5 refers to a kind of in vertical thermosyphon reboiler, the vertical reboiler of forced cyclic type, horizontal reboiler.
On mechanical vapour compressor 4, propeller pump 6, rectifying fresh feed pump 10, rectifying tower reactor discharging pump 11, ammoniacal liquor reflux pump 14, be equipped with under meter.
The application method of this MVR stripping deamination system comprises the following steps:
(1) will through wastewater feed preheater I 1, wastewater feed preheater II 2, enter steam stripping ammonia-removing tower 3 successively through pretreated high-ammonia-nitrogen sewage, simultaneously, saturation steam or superheated vapour are inputed to steam stripping ammonia-removing tower 3 and carry out the stripping deamination, obtaining respectively temperature and be 95 ~ 110 ℃ and pressure is the steam that contains ammonia 3 ~ 8% of 0.085 ~ 0.15MPa and the waste water after deamination.
Pretreated high-ammonia-nitrogen sewage refers to that ammonia-nitrogen content is that the pH value of 500 ~ 10000ppm is adjusted to 11.5 ~ 12.0 ammonia-containing water.
(2) the steam that contains ammonia 3 ~ 8% enters reboiler 5 through containing after ammonia steam outlet I is heated by 4 pressurizations of mechanical vapour compressor; Simultaneously, a waste water part after deamination is discharged by the deamination effluent outfall through wastewater feed preheater I 1, all the other bottom lease making propeller pump 6 enter reboiler 5, the steam that contains ammonia 3 ~ 8% evaporates the waste water after deamination in described reboiler (5), the steam after being evaporated respectively and condensed mass concentration are 3 ~ 8% ammoniacal liquor; Steam after evaporation enters in steam stripping ammonia-removing tower 3 as stripping deamination steam.
(3) condensed mass concentration is that 3 ~ 8% ammoniacal liquor enters weak ammonia storage tank 7 through the weak ammonia discharge outlet, and through rectifying fresh feed pump 10, interchanger 8, enters in ammoniacal liquor rectifying tower 9 successively; Simultaneously, saturation steam or superheated vapour are inputed in ammoniacal liquor rectifying tower 9 and carry out steam stripped rectifying, obtain respectively the deamination waste water after up to standard and contain the steam of ammonia 15 ~ 30%; Deamination waste water after up to standard is discharged by the deamination effluent outfall through wastewater feed preheater II 2 by rectifying tower reactor discharging pump 11, interchanger 8 successively.
(4) the steam that contains ammonia 15 ~ 30% enters condenser 12 condensations through containing ammonia steam outlet II, obtain mass concentration and be 15 ~ 30% ammoniacal liquor, this mass concentration is that 15 ~ 30% ammoniacal liquor is divided into two portions through the strong aqua discharge outlet by ammoniacal liquor reflux pump 14, wherein a part is through the output of strong aqua output tube, and rest part enters ammoniacal liquor rectifying tower 9 and carries out rectifying.
Claims (7)
1. MVR stripping deamination system, comprise steam stripping ammonia-removing tower (3), ammoniacal liquor rectifying tower (9), condenser (12), it is characterized in that: a upper lateral part of described steam stripping ammonia-removing tower (3) is provided with the high-ammonia-nitrogen sewage input tube, the one side lower part is provided with the steam input pipe I, its opposite side bottom is connected with reboiler (5) by the pipeline I, its bottom is provided with the discharge of wastewater mouth after deamination, and its top is provided with and contains ammonia steam outlet I; Described high-ammonia-nitrogen sewage input tube is connected with wastewater feed preheater II (2), wastewater feed preheater I (1) successively, and this wastewater feed preheater II (2), wastewater feed preheater I (1) are equipped with the deamination effluent outfall; Discharge of wastewater mouth after described deamination is connected with respectively described wastewater feed preheater I (1), propeller pump (6) by the pipeline II, and this propeller pump (6) is connected with described reboiler (5); The described ammonia steam outlet I that contains is connected with described reboiler (5) by mechanical vapour compressor (4); One side of described reboiler (5) is provided with the weak ammonia discharge outlet, and is connected with weak ammonia storage tank (7) by this weak ammonia discharge outlet; Described weak ammonia storage tank (7) is connected with described ammoniacal liquor rectifying tower (9) through rectifying fresh feed pump (10), interchanger (8) successively; The bottom of described ammoniacal liquor rectifying tower (9) is provided with discharge port, and its top is provided with and contains ammonia steam outlet II, and the one side is provided with the steam input pipe II; Described discharge port is connected with rectifying tower reactor discharging pump (11) by the pipeline III, and with described wastewater feed preheater II (2), is connected through described interchanger (8) by rectifying tower reactor discharging pump (11); The described ammonia steam outlet II that contains is connected with described condenser (12) by the pipeline IV, and this condenser (12) is respectively equipped with recirculated water backwater discharge outlet, circulating water intake, strong aqua discharge outlet; Described strong aqua discharge outlet is connected with strong aqua storage tank (13) by the pipeline V, and this strong aqua storage tank (13) is connected with described ammoniacal liquor rectifying tower (9), strong aqua output tube respectively through ammoniacal liquor reflux pump (14).
2. a kind of MVR stripping deamination system as claimed in claim 1, it is characterized in that: described mechanical vapour compressor (4) refers to positive-displacement compressor or radial compressor, compressor boost is 20 ~ 80kPa.
3. a kind of MVR stripping deamination system as claimed in claim 1 is characterized in that: described reboiler (5) refers to a kind of in vertical thermosyphon reboiler, the vertical reboiler of forced cyclic type, horizontal reboiler.
4. a kind of MVR stripping deamination system as claimed in claim 1, it is characterized in that: described mechanical vapour compressor (4), propeller pump (6), rectifying fresh feed pump (10), rectifying tower reactor discharging pump (11), ammoniacal liquor reflux pump are equipped with under meter on (14).
5. the application method of a kind of MVR stripping deamination system as claimed in claim 1 comprises the following steps:
(1) will through wastewater feed preheater I (1), wastewater feed preheater II (2), enter steam stripping ammonia-removing tower (3) successively through pretreated high-ammonia-nitrogen sewage, simultaneously, steam is inputed to described steam stripping ammonia-removing tower (3) and carry out the stripping deamination, obtaining respectively temperature and be 95 ~ 110 ℃ and pressure is the steam that contains ammonia 3 ~ 8% of 0.085 ~ 0.15MPa and the waste water after deamination;
(2) the described steam that contains ammonia 3 ~ 8% enters reboiler (5) through containing after ammonia steam outlet I is heated by mechanical vapour compressor (4) pressurization; Simultaneously, a waste water part after described deamination is discharged by the deamination effluent outfall through wastewater feed preheater I (1), all the other bottom lease making propeller pump (6) enter described reboiler (5), the described steam that contains ammonia 3 ~ 8% evaporates the waste water after described deamination in described reboiler (5), the steam after being evaporated respectively and condensed mass concentration are 3 ~ 8% ammoniacal liquor; Steam after described evaporation enters in described steam stripping ammonia-removing tower (3) as stripping deamination steam;
(3) described condensed mass concentration is that 3 ~ 8% ammoniacal liquor enters weak ammonia storage tank (7) through the weak ammonia discharge outlet, and through rectifying fresh feed pump (10), interchanger (8), enters in ammoniacal liquor rectifying tower (9) successively; Simultaneously, steam is inputed in described ammoniacal liquor rectifying tower (9) and carries out steam stripped rectifying, obtain respectively the deamination waste water after up to standard and contain the steam of ammonia 15 ~ 30%; Described deamination waste water after up to standard is discharged by the deamination effluent outfall through wastewater feed preheater II (2) by rectifying tower reactor discharging pump (11), described interchanger (8) successively;
(4) the described steam that contains ammonia 15 ~ 30% enters condenser (12) condensation through containing ammonia steam outlet II, obtain mass concentration and be 15 ~ 30% ammoniacal liquor, this mass concentration is that 15 ~ 30% ammoniacal liquor is divided into two portions through the strong aqua discharge outlet by ammoniacal liquor reflux pump (14), wherein a part is through the output of strong aqua output tube, and rest part enters described ammoniacal liquor rectifying tower (9) and carries out rectifying.
6. the application method of a kind of MVR stripping deamination system as claimed in claim 5 is characterized in that: the pretreated high-ammonia-nitrogen sewage of described step in (1) refers to that ammonia-nitrogen content is that the pH value of 500 ~ 10000ppm is adjusted to 11.5 ~ 12.0 ammonia-containing water.
7. the application method of a kind of MVR stripping deamination system as claimed in claim 5 is characterized in that: (1) the steam in (3) all refers to saturation steam or superheated vapour to described step with described step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013103333897A CN103408086A (en) | 2013-08-02 | 2013-08-02 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013103333897A CN103408086A (en) | 2013-08-02 | 2013-08-02 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103408086A true CN103408086A (en) | 2013-11-27 |
Family
ID=49601146
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013103333897A Pending CN103408086A (en) | 2013-08-02 | 2013-08-02 | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103408086A (en) |
Cited By (38)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445476A (en) * | 2014-11-25 | 2015-03-25 | 徐翔 | Ethyl alcohol biogas slurry deamination technology and equipment |
| CN105174346A (en) * | 2015-09-21 | 2015-12-23 | 中国成达工程有限公司 | Mother liquor deamination process and equipment for soda production through thermal method |
| CN106015064A (en) * | 2016-06-06 | 2016-10-12 | 贵州赤天化股份有限公司 | Structure and operation method for driving compressor with motors instead of steam |
| CN106186501A (en) * | 2016-09-19 | 2016-12-07 | 江苏泫槿环境科技有限公司 | A kind of high concentration ammonia nitrogen wastewater treatment system and processing method |
| CN106379952A (en) * | 2015-08-07 | 2017-02-08 | 王树岩 | Apparatus and process for treating ammonia nitrogen wastewater and recycling ammonia |
| CN106395858A (en) * | 2016-10-15 | 2017-02-15 | 上海国际化建工程咨询有限公司 | Device and method for preparing pure liquid ammonia from ammonia-containing conversion condensate wastewater |
| CN107298448A (en) * | 2017-07-19 | 2017-10-27 | 北京中科康仑环境科技研究院有限公司 | A kind of method that ammonia is reclaimed from ammonia nitrogen waste water |
| CN107487802A (en) * | 2017-09-07 | 2017-12-19 | 北京赛科康仑环保科技有限公司 | A kind of recycling processing method of high ammonia nitrogen and high salt waste water |
| CN107635912A (en) * | 2015-05-21 | 2018-01-26 | 卡萨尔公司 | For the method for the production capacity for improving ammonia-preparing device |
| CN108203130A (en) * | 2016-12-20 | 2018-06-26 | 中国石油化工股份有限公司 | A kind of method of ammonium salt-containing wastewater treatment |
| CN108203132A (en) * | 2016-12-20 | 2018-06-26 | 中国石油化工股份有限公司 | A kind of method of ammonium salt-containing wastewater treatment |
| CN108726758A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726766A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726756A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN108726606A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726763A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726761A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726611A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726608A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726607A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726760A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726765A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726612A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN108726610A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN108726613A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726762A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726767A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726759A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN109850972A (en) * | 2019-01-17 | 2019-06-07 | 杉杉能源（宁夏）有限公司 | A kind of processing system improving ammonia recovery in ternary precursor production waste water |
| 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 |
| JP2019141820A (en) * | 2018-02-23 | 2019-08-29 | 木村化工機株式会社 | Mvr type distillation apparatus of ammonia aqueous solution |
| CN110540331A (en) * | 2019-09-23 | 2019-12-06 | 南京蓝胜环保科技有限公司 | process method for removing oil and reducing COD (chemical oxygen demand) of wastewater by using hexamethyl silazane |
| CN111170389A (en) * | 2020-01-09 | 2020-05-19 | 长沙矿冶研究院有限责任公司 | Ammonia stripping and distilling system and method for ammonia nitrogen wastewater |
| CN111825145A (en) * | 2020-08-07 | 2020-10-27 | 吴嘉 | Method and device for treating ammonia nitrogen wastewater and recovering ammonia |
| US10815132B2 (en) | 2017-04-21 | 2020-10-27 | China Petroleum & Chemical Corporation | Apparatus and method for treating waste water containing ammonium salts |
| CN112875783A (en) * | 2021-04-14 | 2021-06-01 | 北京中科康仑环境科技研究院有限公司 | System and method for treating wastewater containing volatile substances |
| CN114593615A (en) * | 2022-03-23 | 2022-06-07 | 上海谋基实业有限公司 | Energy recycling method for acrylic acid purification process |
| CN115253350A (en) * | 2022-08-05 | 2022-11-01 | 淄博万华机械设备有限公司 | Double-tower MVR continuous distillation recovery system and method |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07116650A (en) * | 1993-10-20 | 1995-05-09 | Nitto Kikai Kk | Separation and treatment of gaseous ammonia from high concentrated ammonia-containing water |
| 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 |
| CN101962242A (en) * | 2009-07-23 | 2011-02-02 | 江苏新河农用化工有限公司 | High-efficiency deamination method for industrial waste water containing ammonia |
| CN202246318U (en) * | 2011-09-06 | 2012-05-30 | 天华化工机械及自动化研究设计院 | Composite steam stripping ammonia-removing tower |
| CN102674489A (en) * | 2012-05-17 | 2012-09-19 | 青岛科技大学 | high-concentration ammonia-containing wastewater treatment method based on vapour compression |
-
2013
- 2013-08-02 CN CN2013103333897A patent/CN103408086A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH07116650A (en) * | 1993-10-20 | 1995-05-09 | Nitto Kikai Kk | Separation and treatment of gaseous ammonia from high concentrated ammonia-containing water |
| 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 |
| CN101962242A (en) * | 2009-07-23 | 2011-02-02 | 江苏新河农用化工有限公司 | High-efficiency deamination method for industrial waste water containing ammonia |
| CN202246318U (en) * | 2011-09-06 | 2012-05-30 | 天华化工机械及自动化研究设计院 | Composite steam stripping ammonia-removing tower |
| CN102674489A (en) * | 2012-05-17 | 2012-09-19 | 青岛科技大学 | high-concentration ammonia-containing wastewater treatment method based on vapour compression |
Cited By (58)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104445476A (en) * | 2014-11-25 | 2015-03-25 | 徐翔 | Ethyl alcohol biogas slurry deamination technology and equipment |
| CN107635912B (en) * | 2015-05-21 | 2020-10-20 | 卡萨尔公司 | Method for treating process condensate in an ammonia plant |
| CN107635912A (en) * | 2015-05-21 | 2018-01-26 | 卡萨尔公司 | For the method for the production capacity for improving ammonia-preparing device |
| CN106379952A (en) * | 2015-08-07 | 2017-02-08 | 王树岩 | Apparatus and process for treating ammonia nitrogen wastewater and recycling ammonia |
| CN105174346A (en) * | 2015-09-21 | 2015-12-23 | 中国成达工程有限公司 | Mother liquor deamination process and equipment for soda production through thermal method |
| CN106015064A (en) * | 2016-06-06 | 2016-10-12 | 贵州赤天化股份有限公司 | Structure and operation method for driving compressor with motors instead of steam |
| 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 |
| CN106186501A (en) * | 2016-09-19 | 2016-12-07 | 江苏泫槿环境科技有限公司 | A kind of high concentration ammonia nitrogen wastewater treatment system and processing method |
| CN106395858A (en) * | 2016-10-15 | 2017-02-15 | 上海国际化建工程咨询有限公司 | Device and method for preparing pure liquid ammonia from ammonia-containing conversion condensate wastewater |
| CN106395858B (en) * | 2016-10-15 | 2018-09-28 | 上海国际化建工程咨询有限公司 | A kind of method and device converting lime set waste water making pure liquefied ammonia containing ammonia |
| CN108203130A (en) * | 2016-12-20 | 2018-06-26 | 中国石油化工股份有限公司 | A kind of method of ammonium salt-containing wastewater treatment |
| CN108203132A (en) * | 2016-12-20 | 2018-06-26 | 中国石油化工股份有限公司 | A kind of method of ammonium salt-containing wastewater treatment |
| CN108726767A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726756B (en) * | 2017-04-21 | 2022-12-27 | 中国石油化工股份有限公司 | Method for treating ammonium salt-containing wastewater |
| CN108726756A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN108726606A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726763A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726761A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726611A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726608A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726607A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726760A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726765A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726612A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN108726610A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN108726613A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726762A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726758A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726759A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | The processing method of ammonium salt-containing waste water |
| CN108726761B (en) * | 2017-04-21 | 2023-04-07 | 中国石油化工股份有限公司 | Treatment method of catalyst production wastewater |
| CN108726608B (en) * | 2017-04-21 | 2023-03-31 | 中国石油化工股份有限公司 | Treatment method of catalyst production wastewater |
| CN108726607B (en) * | 2017-04-21 | 2023-03-14 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| CN108726758B (en) * | 2017-04-21 | 2023-02-24 | 中国石油化工股份有限公司 | Treatment method of catalyst production wastewater |
| CN108726613B (en) * | 2017-04-21 | 2023-02-07 | 中国石油化工股份有限公司 | Treatment method of catalyst production wastewater |
| US11572289B2 (en) | 2017-04-21 | 2023-02-07 | China Petroleum & Chemical Corporation | Apparatus and method for treating waste water containing ammonium salts |
| CN108726767B (en) * | 2017-04-21 | 2023-02-07 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| CN108726759B (en) * | 2017-04-21 | 2023-01-06 | 中国石油化工股份有限公司 | Method for treating ammonium salt-containing wastewater |
| US10815132B2 (en) | 2017-04-21 | 2020-10-27 | China Petroleum & Chemical Corporation | Apparatus and method for treating waste water containing ammonium salts |
| CN108726611B (en) * | 2017-04-21 | 2023-01-03 | 中国石油化工股份有限公司 | Treatment method of catalyst production wastewater |
| CN108726610B (en) * | 2017-04-21 | 2022-12-27 | 中国石油化工股份有限公司 | Method for treating waste water containing ammonium salt |
| CN108726763B (en) * | 2017-04-21 | 2021-08-27 | 中国石油化工股份有限公司 | Treatment method of catalyst production wastewater |
| CN108726762B (en) * | 2017-04-21 | 2021-08-27 | 中国石油化工股份有限公司 | Treatment method of catalyst production wastewater |
| CN108726612B (en) * | 2017-04-21 | 2022-12-27 | 中国石油化工股份有限公司 | Method for treating waste water containing ammonium salt |
| CN108726766A (en) * | 2017-04-21 | 2018-11-02 | 中国石油化工股份有限公司 | A kind of processing method of catalyst production waste water |
| CN108726760B (en) * | 2017-04-21 | 2022-11-25 | 中国石油化工股份有限公司 | Treatment method of catalyst production wastewater |
| CN108726766B (en) * | 2017-04-21 | 2022-11-25 | 中国石油化工股份有限公司 | Method for treating catalyst production wastewater |
| CN107298448A (en) * | 2017-07-19 | 2017-10-27 | 北京中科康仑环境科技研究院有限公司 | A kind of method that ammonia is reclaimed from ammonia nitrogen waste water |
| CN107487802B (en) * | 2017-09-07 | 2021-04-02 | 北京赛科康仑环保科技有限公司 | Resourceful treatment method for high-ammonia-nitrogen high-salt wastewater |
| CN107487802A (en) * | 2017-09-07 | 2017-12-19 | 北京赛科康仑环保科技有限公司 | A kind of recycling processing method of high ammonia nitrogen and high salt waste water |
| JP2019141820A (en) * | 2018-02-23 | 2019-08-29 | 木村化工機株式会社 | Mvr type distillation apparatus of ammonia aqueous solution |
| CN109850972A (en) * | 2019-01-17 | 2019-06-07 | 杉杉能源（宁夏）有限公司 | A kind of processing system improving ammonia recovery in ternary precursor production waste water |
| 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 |
| CN110540331A (en) * | 2019-09-23 | 2019-12-06 | 南京蓝胜环保科技有限公司 | process method for removing oil and reducing COD (chemical oxygen demand) of wastewater by using hexamethyl silazane |
| CN111170389A (en) * | 2020-01-09 | 2020-05-19 | 长沙矿冶研究院有限责任公司 | Ammonia stripping and distilling system and method for ammonia nitrogen wastewater |
| CN111825145A (en) * | 2020-08-07 | 2020-10-27 | 吴嘉 | Method and device for treating ammonia nitrogen wastewater and recovering ammonia |
| CN112875783A (en) * | 2021-04-14 | 2021-06-01 | 北京中科康仑环境科技研究院有限公司 | System and method for treating wastewater containing volatile substances |
| CN114593615A (en) * | 2022-03-23 | 2022-06-07 | 上海谋基实业有限公司 | Energy recycling method for acrylic acid purification process |
| CN115253350A (en) * | 2022-08-05 | 2022-11-01 | 淄博万华机械设备有限公司 | Double-tower MVR continuous distillation recovery system and method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103408086A (en) | MVR (Mechanical Vapor Recompression) vapor-stripping deamination system and application method thereof | |
| CN110606470B (en) | Device for concentrating, resolving and producing hydrogen chloride from hydrochloric acid | |
| CN107619078B (en) | Device for treating acidic wastewater by adopting concentration stripping method | |
| CN106746110A (en) | A kind of device and processing method for processing high ammonia nitrogen and high salt waste water | |
| CN106830010A (en) | Methyl alcohol and ammonium chloride extraction equipment and extraction process in a kind of glycine production | |
| CN110407173A (en) | A kind of waste acid treatment system and the method using system processing spent acid | |
| CN104843816B (en) | A kind of heat pump flash distillation stripping deamination coproduction of ammonia sulfate and the method for ammonia | |
| CN103819041A (en) | Method for concentrating high-salinity wastewater at low temperature | |
| CN203483884U (en) | Device for concentrating caprolactam solution with combination of mechanical vapor recompression and multiple-effect evaporation | |
| CN106379952A (en) | Apparatus and process for treating ammonia nitrogen wastewater and recycling ammonia | |
| CN106967114B (en) | Recycling comprehensive treatment method and system for fosetyl-aluminum wastewater | |
| CN104860465A (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN210214856U (en) | Energy-efficient surplus aqueous ammonia distillation plant | |
| CN107792904A (en) | A kind of technique and device of continuous removal of ammonia and nitrogen light component organic matter and salt | |
| CN204644041U (en) | A kind of ammonia nitrogen waste water treatment system | |
| CN102774816B (en) | Method and device for concentrating waste acid in titanium dioxide production by sulfuric acid process | |
| CN202193615U (en) | Dilute sulfuric acid concentration processing equipment | |
| CN110054342A (en) | A method of product salt is obtained to high organic wastewater processing with high salt | |
| CN104829032A (en) | Ammonia-nitrogen wastewater treatment system | |
| CN102838180B (en) | Rare metal wastewater zero discharge process | |
| CN1161316C (en) | Lactic acid refining short range distillation process with drum evaporator | |
| CN206654738U (en) | Methanol and ammonium chloride extraction equipment in a kind of glycine production | |
| CN207451656U (en) | A kind of continuous removal of ammonia and nitrogen light component organic matter and salt system | |
| CN208839075U (en) | A kind of vacuum crystallization system | |
| CN111635348A (en) | Application and system of screw vacuum pump in caprolactam refining process production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20131127 |