CN104058538A - Technology method for steam stripping deacidification and deamination of waste water - Google Patents
Technology method for steam stripping deacidification and deamination of waste water Download PDFInfo
- Publication number
- CN104058538A CN104058538A CN201410310223.8A CN201410310223A CN104058538A CN 104058538 A CN104058538 A CN 104058538A CN 201410310223 A CN201410310223 A CN 201410310223A CN 104058538 A CN104058538 A CN 104058538A
- Authority
- CN
- China
- Prior art keywords
- tower
- ammonia
- stripping
- steam
- outlet
- 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.)
- Granted
Links
Abstract
The invention relates to a technology method for emission reducing and resource utilization of industrial waste water, in particular to a method for processing waste water containing ammonia and acid through the efficient steam stripping deamination technology and the steam stripping deacidification technology and conducting resource utilization on ammonia nitrogen and hydrogen sulfide in the waste water. The waste water with the content of ammonia nitrogen being 500-50000 mg/L and the content of hydrogen sulfide being 100-10000 mg/L can reach the national-level ammonia nitrogen discharging standard after being treated through the technologies, and the content of sulfide is reduced to be below 20 mg/L. Meanwhile, ammonia in the waste water is recycled in a high-purity ammonium sulfate mode, and hydrogen sulfide removed from the waste water can be used for preparing sulfur.
Description
Technical field
The present invention relates to a kind of method of trade effluent reduction of discharging and recycling, specifically relate to a kind of employing energy-efficient stripping deamination technique and stripping deacidifying process combination treatment containing ammonia acid-bearing wastewater, and the ammonia nitrogen in waste water and hydrogen sulfide are carried out to the method for recycling.
Background technology
In the industry production processes such as Coal Chemical Industry and petrochemical complex, can produce the ammonia nitrogen waste water of the acid gas components such as a large amount of sulfide hydrogens and carbonic acid gas, if it is not carried out to processing meeting, environment be caused to very big harm.External processing high density adopts vaporizing extract process containing the sewage of ammonia more at present, as US Patent No. 3335071 and US3404072, and domestic have adopt single tower stripping lateral line withdrawal function technical finesse sulfur-bearing containing ammonia sewage, as ZL97115113.X, its common feature be consume energy higher, process waste water per ton and need 140～180 kilograms of left and right of steam, and ammonia nitrogen process range is narrower, water outlet ammonia nitrogen concentration does not reach national grade one discharge standard (GB8978-1996 < < integrated wastewater discharge standard > > regulation primary standard ammonia nitrogen is less than 15mg/L).For containing ammonia containing sour waste water, stripping deacidifying process and stripping deamination technique that this patent adopts, good energy-conserving effect, can reach good depickling deamination effect, and recyclable highly purified ammonium sulfate is used as nitrogenous fertilizer, and isolates hydrogen sulfide for sulphur processed.
This patent is based on efficient energy-saving coupling stripping deamination technology ZL201010507488.9, further improve on its basis for the treatment of in Coal Chemical Industry and oil refining industry, produce containing ammonia acid-bearing wastewater, reach the object of energy-saving and emission-reduction and recycling.
Summary of the invention
The present invention relates to a kind of method of trade effluent reduction of discharging and recycling, specifically relate to a kind of employing High efficiency stripping deamination technique and stripping deacidifying process combination treatment containing ammonia acid-bearing wastewater, and the ammonia nitrogen in waste water and hydrogen sulfide are carried out to the method for recycling.The processing method that the present invention adopts comprises device combination mode and implementation method two aspects.
Processing unit combination explanation
The invention provides a kind of processing containing the processing unit array mode of ammonia acid-bearing wastewater, it is characterized in that at least containing in processing unit the major equipment unit such as inlet outlet heat exchanger, stripping extracting tower, steam stripping ammonia-removing tower, ammonia absorption tower, condenser, ammoniumsulphate soln storage tank and evaporative crystallizer; Its array mode is as follows:
The pending ammonia acid-bearing wastewater liquid storage tank that contains is connected with stripping extracting tower waterwater entrance through the tube side of inlet outlet heat exchanger; The shell side of inlet outlet heat exchanger is connected with steam stripping ammonia-removing tower still bottom outlet and processed waste water outlet.
Stripping extracting tower tower reactor bottom delivery conduit is connected with the pipeline of input sodium hydroxide solution by triplate line, and the delivery port of triplate line is connected with the liquid distributor of steam stripping ammonia-removing tower stripping deamination section upper end by pump; Between stripping extracting tower tower reactor and stripping depickling section, gas phase entrance is connected with steam stripping ammonia-removing tower top gaseous phase outlet by pipeline; Between stripping extracting tower stripping depickling Duan Yuqi tower top, have liquid distributor, the intake line of liquid distributor is connected with the condenser refluxing opening on top, ammonia absorption tower; Stripping extracting tower tower top outlet is connected with the gas phase input aperture between ammonia absorption tower absorber portion and tower reactor by pipeline.
Tower reactor bottom, ammonia absorption tower is connected with ammoniumsulphate soln storage tank by pipeline, the outlet of ammoniumsulphate soln storage tank is exported solid ammonium sulfate by evaporative crystallizer, and the steam of input evaporative crystallizer is delivered between steam stripping ammonia-removing tower stripping deamination section and steam stripping ammonia-removing tower tower reactor through pipeline at the secondary steam producing after evaporative crystallizer; Ammonia absorption tower absorber portion is connected with the storage tank of input dilute sulphuric acid by pipeline with the liquid distributor between its tower top, the top gaseous phase outlet of ammonia absorption tower is divided into two-way after condenser is cooling, concentrated acid Qi Zhi subsequent disposal workshop section is discharged on one tunnel, and another road phlegma is back between stripping extracting tower stripping stage and tower top.
The outlet of steam stripping ammonia-removing tower top gaseous phase is connected with the gas phase entrance between tower reactor with stripping extracting tower stripping stage; Steam stripping ammonia-removing tower tower top is connected with the outlet of stripping extracting tower tower reactor and the pipeline of sodium hydroxide solution entrance through pump with the liquid distributor between stripping stage; Gas phase entrance between steam stripping ammonia-removing tower stripping deamination section and tower reactor thereof is connected with the secondary steam output channel of steam input pipe road and ammoniumsulphate soln evaporative crystallizer; Through inlet outlet heat exchanger shell side, the wastewater outlet after processing is connected the outlet of steam stripping ammonia-removing tower tower reactor.
Process implementing method
The present invention adopts the combination unit of above-mentioned processing unit to carrying out deamination depickling processing containing ammonia acid-bearing wastewater, and the ammonia removing and hydrogen sulfide are reclaimed, and the process implementing method for this reason adopting comprises:
That need to process inputs in stripping extracting tower after stripping depickling Duan Shangjing liquid distributor disperses containing ammonia acid-bearing wastewater after waste water pump heats up by inlet outlet heat exchanger, and the ammonia steam that contains that exports stripping extracting tower at stripping depickling section and steam stripping ammonia-removing tower gaseous phase outlet to carries out the transmission of refluent heat/matter; Hydrogen sulfide in waste water and carbonic acid gas, and small part ammonia enters vapor phase, ammonia-containing water after depickling is discharged after sodium hydroxide solution is adjusted pH value from tower reactor, by pump delivery to steam stripping ammonia-removing tower stripping deamination section upper end, sprayed, the secondary steam that ammonia-containing water feeds back at stripping deamination section and the live steam of sending into and evaporative crystallizer meets and carries out the transmission of refluent heat/matter, in this process, ammonia enters vapor phase, realizes the object of deamination.After waste water deaminizing, from tower reactor output, through inlet outlet heat exchanger, discharge after containing sour ammonia-containing water heat exchange with untreated.Containing ammonia steam, by steam stripping ammonia-removing tower tower top, input to stripping extracting tower stripping depickling section for stripping depickling; That from stripping extracting tower tower top, discharges is transported to ammonia absorption tower containing ammonia containing acid vapour, dilute sulphuric acid counter current contact under ammonia absorption tower ammonia absorber portion and spray, ammonia is absorbed generation ammoniumsulphate soln by dilute sulphuric acid and collects in tower reactor, liquid storage in tower reactor is delivered to the circulation of sulfuric acid sparger by sulfuric acid pump and absorbs ammonia, by self-con-tained unit, regularly discharge saturated ammonium sulphate solution to storage tank, and further in vapo(u)rization system, reclaiming solid ammonium sulfate and secondary steam, secondary steam is transported to steam stripping ammonia-removing tower and again utilizes; Remove absorbing tower top containing acid vapour from ammonia and be delivered to condenser condensation except water vapour after ammonia, what condensation obtained is back to stripping extracting tower stripping depickling section spray containing acid condensation liquid, carbonic acid gas and hydrogen sulfide mixed gas that the gas phase of discharging from condenser is high density, can carry out aftertreatment for recovery sulphur.
Significant improvement of the present invention comprises:
According to sour gas and the ammonia difference of volatility at high temperature, by stripping extracting tower and steam stripping ammonia-removing tower serial operation, take full advantage of system thermal;
Change conventional depickling tower top cold feed into hot feed, reduced system steam mono-consumption;
Before deacidification process makes deamination operation prior to deamination operation, waste water alkalescence improves, and has reduced the consumption that regulates the sodium hydroxide of waste water potential of hydrogen;
By above-mentioned improvement, significantly reduce system operation cost, reached energy-conservation effect.
Accessible beneficial effect after the invention process:
(1) per hour accessible containing ammonia acid-bearing wastewater amount: 1t and more than;
(2) can process ammonia-nitrogen content in waste water: 500～50000mg/L;
(3) after processing, in waste discharge, ammonia-nitrogen content is low: 1～10mg/L (lower than national grade one discharge standard 15mg/L);
(4) can process the hydrogen sulfide content in waste water: 100～10000mg/L;
(5) process the hydrogen sulfide content in rear waste discharge: be less than 20mg/L;
(6) the required steam consumption quantity of waste water per ton: be less than 150kg;
(7) reclaim product: high-purity sulfuric acid ammonium and hydrogen sulfide are used for sulphur processed.
Accompanying drawing explanation
Fig. 1 is the schematic flow sheet of wastewater stripping depickling deamination technique.
concrete case study on implementation
Below enumerating embodiment further illustrates embodiment of the present invention.But the present invention is not limited to following embodiment.
Embodiment 1
Adopt the present invention to process containing ammonia acid-bearing wastewater import ammonia nitrogen concentration 1800mg/L, sulfide concentration 780mg/L, treatment capacity is 1m
3/ h.Adopt the analyses of nessler reagent colorimetry (GB7479-87) and methylene blue spectrophotometry (GB/T16489-1996), the ammonia nitrogen concentration in processed waste water is 2.7mg/L, and hydrogen sulfide content is 5mg/L, and steam consumption is 132kg/ ton waste water.
Embodiment 2
Adopt the present invention to process containing ammonia acid-bearing wastewater import ammonia nitrogen concentration 10100mg/L, sulfide concentration 6400mg/L, treatment capacity is 120m
3/ h.Adopt the analyses of nessler reagent colorimetry (GB7479-87) and methylene blue spectrophotometry (GB/T16489-1996), the ammonia nitrogen concentration in processed waste water is 8.0mg/L, and hydrogen sulfide content is 14mg/L, and steam consumption is 120kg/ ton waste water.
Embodiment 3
Adopt the present invention to process containing ammonia acid-bearing wastewater import ammonia nitrogen concentration 38300mg/L, sulfide concentration 1500mg/L, treatment capacity is 30m
3/ h.Adopt the analyses of nessler reagent colorimetry (GB7479-87) and methylene blue spectrophotometry (GB/T16489-1996), the ammonia nitrogen concentration in processed waste water is 6.5mg/L, and hydrogen sulfide content is 13mg/L, and steam consumption is 126kg/ ton waste water.
Claims (2)
1. processing is containing a processing method for ammonia acid-bearing wastewater, and its feature is to adopt following equipment and array mode:
A. major equipment comprises: inlet outlet heat exchanger, stripping extracting tower, steam stripping ammonia-removing tower, ammonia absorption tower, condenser, ammoniumsulphate soln storage tank and evaporative crystallizer;
B. the array mode that equipment adopts:
The pending ammonia acid-bearing wastewater liquid storage tank that contains is connected with stripping extracting tower waterwater entrance through the tube side of inlet outlet heat exchanger; The shell side of inlet outlet heat exchanger is connected with steam stripping ammonia-removing tower still bottom outlet and processed waste water outlet;
Stripping extracting tower tower reactor bottom delivery conduit is connected with the pipeline of input sodium hydroxide solution by triplate line, and the delivery port of triplate line is connected with the liquid distributor of steam stripping ammonia-removing tower stripping deamination section upper end by pump; Between stripping extracting tower tower reactor and stripping depickling section, gas phase entrance is connected with steam stripping ammonia-removing tower top gaseous phase outlet by pipeline; Between stripping extracting tower stripping depickling Duan Yuqi tower top, have liquid distributor, the intake line of liquid distributor is connected with the condenser refluxing opening on top, ammonia absorption tower; Stripping extracting tower tower top outlet is connected with the gas phase input aperture between ammonia absorption tower absorber portion and tower reactor by pipeline;
Tower reactor bottom, ammonia absorption tower is connected with ammoniumsulphate soln storage tank by pipeline, the outlet of ammoniumsulphate soln storage tank is exported solid ammonium sulfate by evaporative crystallizer, and the steam of input evaporative crystallizer is delivered between steam stripping ammonia-removing tower stripping deamination section and steam stripping ammonia-removing tower tower reactor through pipeline at the secondary steam producing after evaporative crystallizer; Ammonia absorption tower absorber portion is connected with the storage tank of input dilute sulphuric acid by pipeline with the liquid distributor between its tower top, the top gaseous phase outlet of ammonia absorption tower is divided into two-way after condenser is cooling, concentrated acid Qi Zhi subsequent disposal workshop section is discharged on one tunnel, and another road phlegma is back between stripping extracting tower stripping stage and tower top;
The outlet of steam stripping ammonia-removing tower top gaseous phase is connected with the gas phase entrance between tower reactor with stripping extracting tower stripping stage; Steam stripping ammonia-removing tower tower top is connected with the outlet of stripping extracting tower tower reactor and the pipeline of sodium hydroxide solution entrance through pump with the liquid distributor between stripping stage; Gas phase entrance between steam stripping ammonia-removing tower stripping deamination section and tower reactor thereof is connected with the secondary steam output channel of steam input pipe road and ammoniumsulphate soln evaporative crystallizer; Through inlet outlet heat exchanger shell side, the wastewater outlet after processing is connected the outlet of steam stripping ammonia-removing tower tower reactor.
2. processing contains a processing method for ammonia acid-bearing wastewater,, it is characterized in that adopting equipment and array mode thereof in claim 1, and adopt following processing step:
That need to process inputs in stripping extracting tower after stripping depickling Duan Shangjing liquid distributor disperses containing ammonia acid-bearing wastewater after waste water pump heats up by inlet outlet heat exchanger, and the ammonia steam that contains that exports stripping extracting tower at stripping depickling section and steam stripping ammonia-removing tower gaseous phase outlet to carries out the transmission of refluent heat/matter; Hydrogen sulfide in waste water and carbonic acid gas, and small part ammonia enters vapor phase, ammonia-containing water after depickling is discharged after sodium hydroxide solution is adjusted pH value from tower reactor, by pump delivery to steam stripping ammonia-removing tower stripping deamination section upper end, sprayed, the secondary steam that ammonia-containing water feeds back at stripping deamination section and the live steam of sending into and evaporative crystallizer meets and carries out the transmission of refluent heat/matter, in this process, ammonia enters vapor phase, realizes the object of deamination; After waste water deaminizing, from tower reactor output, through inlet outlet heat exchanger, discharge after containing sour ammonia-containing water heat exchange with untreated; Containing ammonia steam, by steam stripping ammonia-removing tower tower top, input to stripping extracting tower stripping depickling section for stripping depickling; That from stripping extracting tower tower top, discharges is transported to ammonia absorption tower containing ammonia containing acid vapour, dilute sulphuric acid counter current contact under ammonia absorption tower ammonia absorber portion and spray, ammonia is absorbed generation ammoniumsulphate soln by dilute sulphuric acid and collects in tower reactor, liquid storage in tower reactor is delivered to the circulation of sulfuric acid sparger by sulfuric acid pump and absorbs ammonia, by self-con-tained unit, regularly discharge saturated ammonium sulphate solution to storage tank, and further in vapo(u)rization system, reclaiming solid ammonium sulfate and secondary steam, secondary steam is transported to steam stripping ammonia-removing tower and again utilizes; Remove absorbing tower top containing acid vapour from ammonia and be delivered to condenser condensation except water vapour after ammonia, what condensation obtained is back to stripping extracting tower stripping depickling section spray containing acid condensation liquid, carbonic acid gas and hydrogen sulfide mixed gas that the gas phase of discharging from condenser is high density, can carry out aftertreatment for recovery sulphur.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410310223.8A CN104058538B (en) | 2014-06-30 | 2014-06-30 | A kind of processing method of wastewater stripping depickling deamination |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410310223.8A CN104058538B (en) | 2014-06-30 | 2014-06-30 | A kind of processing method of wastewater stripping depickling deamination |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104058538A true CN104058538A (en) | 2014-09-24 |
| CN104058538B CN104058538B (en) | 2016-03-16 |
Family
ID=51546516
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201410310223.8A Active CN104058538B (en) | 2014-06-30 | 2014-06-30 | A kind of processing method of wastewater stripping depickling deamination |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104058538B (en) |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478026A (en) * | 2014-12-12 | 2015-04-01 | 北京阳光欣禾科技有限公司 | Inner-coupling energy-saving stripping deamination process method |
| CN105384291A (en) * | 2015-09-23 | 2016-03-09 | 北方稀土生一伦高科技有限公司 | Method for treating ammonium chloride wastewater |
| CN105948153A (en) * | 2016-05-25 | 2016-09-21 | 北京中科瑞奥能源科技股份有限公司 | System and process for treating and utilizing phenol-ammonia wastewater |
| CN105948306A (en) * | 2016-05-12 | 2016-09-21 | 华陆工程科技有限责任公司 | Pretreatment and comprehensive utilization method of wastewater and waste gas produced during coal gasification |
| CN106315726A (en) * | 2016-10-12 | 2017-01-11 | 江苏金茂源生物化工有限责任公司 | Biogas slurry decarbonization and deamination combined system |
| CN107129087A (en) * | 2017-05-04 | 2017-09-05 | 北京阳光欣禾科技有限公司 | A kind of refuse leachate deamination removes chromium process method |
| CN107324284A (en) * | 2017-07-07 | 2017-11-07 | 天津市职业大学 | A kind of system of recycling treatment iron-contained industrial waste hydrochloric acid |
| CN109704366A (en) * | 2019-02-11 | 2019-05-03 | 中冶焦耐(大连)工程技术有限公司 | A kind of technique and system of the coupling of pressurization deacidifion heat |
| CN110104712A (en) * | 2019-04-19 | 2019-08-09 | 中石化宁波工程有限公司 | A kind of Treatment Method of Ammonia-contained Waste Water |
| US10815132B2 (en) | 2017-04-21 | 2020-10-27 | China Petroleum & Chemical Corporation | Apparatus and method for treating waste water containing ammonium salts |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11114552A (en) * | 1997-10-20 | 1999-04-27 | Kurita Water Ind Ltd | Method for recovering valuable materials from organic waste liquid |
| CN102030386A (en) * | 2010-10-15 | 2011-04-27 | 北京化工大学 | Efficient energy-saving coupling stripping deamination equipment 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 |
| CN102863112A (en) * | 2012-10-19 | 2013-01-09 | 天津市昊永化工科技有限公司 | Phenol and ammonia wastewater recycling treatment method by using single tower for performing de-acidification and de-amination simultaneously |
-
2014
- 2014-06-30 CN CN201410310223.8A patent/CN104058538B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH11114552A (en) * | 1997-10-20 | 1999-04-27 | Kurita Water Ind Ltd | Method for recovering valuable materials from organic waste liquid |
| 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 |
| CN102030386A (en) * | 2010-10-15 | 2011-04-27 | 北京化工大学 | Efficient energy-saving coupling stripping deamination equipment and method |
| CN102320671A (en) * | 2011-06-17 | 2012-01-18 | 青岛科技大学 | Method for treating waste water containing acid and ammonia |
| CN102863112A (en) * | 2012-10-19 | 2013-01-09 | 天津市昊永化工科技有限公司 | Phenol and ammonia wastewater recycling treatment method by using single tower for performing de-acidification and de-amination simultaneously |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104478026A (en) * | 2014-12-12 | 2015-04-01 | 北京阳光欣禾科技有限公司 | Inner-coupling energy-saving stripping deamination process method |
| CN104478026B (en) * | 2014-12-12 | 2016-08-24 | 北京阳光欣禾科技有限公司 | Coupling energy-saving stripping deamination process in a kind of |
| CN105384291A (en) * | 2015-09-23 | 2016-03-09 | 北方稀土生一伦高科技有限公司 | Method for treating ammonium chloride wastewater |
| CN105948306B (en) * | 2016-05-12 | 2018-09-21 | 华陆工程科技有限责任公司 | A kind of pretreatment of coal gasification waste water exhaust gas and method of comprehensive utilization |
| CN105948306A (en) * | 2016-05-12 | 2016-09-21 | 华陆工程科技有限责任公司 | Pretreatment and comprehensive utilization method of wastewater and waste gas produced during coal gasification |
| CN105948153A (en) * | 2016-05-25 | 2016-09-21 | 北京中科瑞奥能源科技股份有限公司 | System and process for treating and utilizing phenol-ammonia wastewater |
| CN106315726A (en) * | 2016-10-12 | 2017-01-11 | 江苏金茂源生物化工有限责任公司 | Biogas slurry decarbonization and deamination combined system |
| CN106315726B (en) * | 2016-10-12 | 2019-05-03 | 江苏金茂源生物化工有限责任公司 | A kind of biogas slurry decarburization combining deamination system |
| US10815132B2 (en) | 2017-04-21 | 2020-10-27 | China Petroleum & Chemical Corporation | Apparatus and method for treating waste water containing ammonium salts |
| US11572289B2 (en) | 2017-04-21 | 2023-02-07 | China Petroleum & Chemical Corporation | Apparatus and method for treating waste water containing ammonium salts |
| CN107129087A (en) * | 2017-05-04 | 2017-09-05 | 北京阳光欣禾科技有限公司 | A kind of refuse leachate deamination removes chromium process method |
| CN107129087B (en) * | 2017-05-04 | 2020-11-10 | 北京阳光欣禾科技有限公司 | Process method for removing ammonia and chromium from garbage penetrating fluid |
| CN107324284A (en) * | 2017-07-07 | 2017-11-07 | 天津市职业大学 | A kind of system of recycling treatment iron-contained industrial waste hydrochloric acid |
| CN109704366A (en) * | 2019-02-11 | 2019-05-03 | 中冶焦耐(大连)工程技术有限公司 | A kind of technique and system of the coupling of pressurization deacidifion heat |
| WO2020164341A1 (en) * | 2019-02-11 | 2020-08-20 | 中冶焦耐(大连)工程技术有限公司 | Process and system for thermal coupling of pressurized deacidification and ammonia distillation |
| CN110104712A (en) * | 2019-04-19 | 2019-08-09 | 中石化宁波工程有限公司 | A kind of Treatment Method of Ammonia-contained Waste Water |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104058538B (en) | 2016-03-16 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104058538B (en) | A kind of processing method of wastewater stripping depickling deamination | |
| CN101264948B (en) | Ammonia nitrogen waste water discharge-reducing and ammonia nitrogen resource utilizing device and method | |
| CN104030514B (en) | A kind of processing method of dual-effect energy-saving wastewater stripping depickling deamination | |
| CN104341019B (en) | A kind of energy-efficient coupling stripping rectifying deamination and desulfurization new technology | |
| CN102190341B (en) | Stripping ammonia-removing method based on flash evaporation and heat pump technologies | |
| CN102030386B (en) | Efficient energy-saving coupling stripping deamination equipment and method | |
| CN103964528B (en) | A kind of heat pump distillation stripping deamination method | |
| CN104860464A (en) | Energy-saving ammonia-nitrogen wastewater treatment method and device | |
| CN104926012A (en) | Treatment process for high-concentration ammonium-nitrogen waste water | |
| CN104843813A (en) | Coal gasification high ammonia nitrogen wastewater treatment process | |
| CN104843816B (en) | A kind of heat pump flash distillation stripping deamination coproduction of ammonia sulfate and the method for ammonia | |
| CN103588329A (en) | Condensation mother liquid waste water pretreatment and resource system and method in compound neutralization reactor in disperse blue 56 production process | |
| CN106315726B (en) | A kind of biogas slurry decarburization combining deamination system | |
| CN103318918B (en) | A kind of method of purifying and recovering ammonia gas | |
| CN104788577B (en) | Method for recycling secondary steam generated in corn starch wet milling production process | |
| CN104860465B (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN205061821U (en) | P hydroxybenzoic acid waste water processing system | |
| CN101734813B (en) | Technology for recovering ammonium sulfate by waste acid pickle generated in process of producing cyanuric acid and equipment therefor | |
| CN203307083U (en) | Negative pressure ammonia distiller by using raw gas waste heat as heat source | |
| CN202046962U (en) | Device for recovering ammonia in ammonia-nitrogen wastewater | |
| CN102923896A (en) | Deaminizing method and device for high-concentration ammonia-containing waste water | |
| CN104591458A (en) | Titanium dioxide high-concentration ammonia nitrogen industrial wastewater treatment process | |
| WO2023207098A1 (en) | Distillation-oxidation treatment system and method for waste liquid from organic acid chemical cleaning of power station boiler | |
| CN1935677A (en) | Ammonium nitrate waste water treatment method | |
| CN203402928U (en) | Resourceful treatment process system for ammonia-containing waste gas/steam in production process of ammonium paratungstate |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |