CN103446865A - Nitrophosphate tail gas deamination device and nitrophosphate tail gas deamination process - Google Patents
Nitrophosphate tail gas deamination device and nitrophosphate tail gas deamination process Download PDFInfo
- Publication number
- CN103446865A CN103446865A CN2013102749621A CN201310274962A CN103446865A CN 103446865 A CN103446865 A CN 103446865A CN 2013102749621 A CN2013102749621 A CN 2013102749621A CN 201310274962 A CN201310274962 A CN 201310274962A CN 103446865 A CN103446865 A CN 103446865A
- Authority
- CN
- China
- Prior art keywords
- absorption liquid
- phosphorus
- nitre
- ammonia
- tail gas
- 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
Images
Abstract
The invention discloses a nitrophosphate tail gas deamination device and a nitrophosphate tail gas deamination process. The device mainly comprises a spray tower, an absorption liquid circulation pump, a nitric (phosphoric) acid solution storage tank, a nitric (phosphoric) acid solution charge pump, a static mixer, an absorption liquid cooler, a multi-gear demister and an induced draft fan, wherein the bottom of the spray tower is an absorption liquid pool, and a spray layer is arranged on the upper part of the spray tower; the absorption liquid pool is connected with the spray layer via the circulation pump, the mixer and the cooler; the mixer is connected with the nitric (phosphoric) acid solution storage tank; the demister and the induced draft fan are arranged at the outlet of the tower; and the absorption liquid pool is connected with a main production line for nitrophosphate. The process disclosed by the invention is as follows: tail gas enters from the lower part of the tower, and flows through spray sections from bottom to top to be absorbed, a gas leaving from the top of the tower is demisted by the demister, and emptied by the induced draft fan; an absorption liquid is conveyed by the circulation pump and conveyed to the spray layer after through the cooler; fresh nitric (phosphoric) acid solution is pumped in the mixer from a storage groove by a pump, and mixed in the absorption liquid; the generated ammonium nitrate (phosphate) is absorbed, and conveyed to the main production line to produce nitrophosphate.
Description
Technical field
The present invention relates to chemical field, specifically, is about the sour phosphate tail gas deamination apparatus of a kind of nitre (phosphorus) and technique.
Background technology
Nitrophosphate fertilizer is the efficient compound fertilizer that is rich in nitrogen and phosphorus.In the Phosphate Fertilizer Production process, in and workshop section produce containing in ammonia and tail gas, produce containing ammonia and transform tail gas at conversion section, these two strands of ammonia-containing exhausts enter engine manifold and enter atmosphere after ammonia absorber is processed.At present, the ammonia absorber that factory is used is packed tower, take process waste liquor as absorbent, and ammonia-containing exhaust is washed.Form silica gel due to the hydrogen fluoride gas in tail gas after dissolving in absorption liquid, often stop up packed tower, reduced the absorption efficiency of packed tower, cause ammonia content in tail gas to exceed standard, not only cause the loss of ammonia, and contaminated environment.In addition, absorption liquid enters plant chimney stalk and processes and the circulatory system, and the ammonia of recovery fails to be used, and causes the wasting of resources.Nitrophosphate fertilizer tail gas has the characteristics of " two high is low ", that is: temperature is high, exhaust temperature 71-75 ℃; Moisture content is high, and dew-point temperature is 62 ℃, and the tail gas moisture content, up to 25%, approaches saturation state; Concentration is low, and tail gas ammonia content is less than 1%.These character of nitrophosphate fertilizer tail gas make deamination have very large difficulty.Must open up new deamination technology and equipment, to improving the absorption efficiency of ammonia.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, a kind of new deamination apparatus is provided.Another object of the present invention, be to provide a kind of new deamination technique.
Technical scheme of the present invention: factory's nitre (phosphorus) acid solution of take is absorbent, adopt spray column to carry out spray washing to ammonia-containing exhaust, in liquid phase, ammonia and nitre (phosphorus) acid solution generation chemical reaction, generate nitre (phosphorus) acid ammonium solution, return to main production procedure, for the production of the nitrophosphate fertilizer product, realize the recycling of resource.
Deamination apparatus of the present invention mainly comprises: spray column, absorption liquid circulating pump, nitre (phosphorus) acid solution charge pump, the sour storage tank of nitre (phosphorus), static mixer, absorption liquid cooler, multiple shelves demister, air-introduced machine.Spray column is designed by counter current contacting, tower reactor is for absorbing liquid pool, and two-layer spraying layer is equipped with on spray column top, and tower reactor is connected with spraying layer with the absorption liquid cooler by circulating pump, static mixer is arranged on the absorption liquid circulation line, with tower reactor, with nitre (phosphorus) acid storage tank, is connected respectively.Be further characterized in that, the absorption tower tower reactor is connected with the nitrophosphate fertilizer main line by pipeline, for reclaiming the ammonium nitrate of generation, produce nitrophosphate fertilizer.
According to above device, spray column deamination technique of the present invention is as follows: ammonia-containing exhaust enters in tower from the tower bottom, and the spray section of flowing through is from bottom to top discharged from tower top after the washing deamination of absorption liquid, enter multiple shelves demister and isolate the drop of carrying secretly, and extract emptying out by air-introduced machine.The tower reactor absorption liquid is carried by circulating pump, after the absorption liquid cooler cools, sends into spraying layer, and ammonia-containing exhaust is carried out to spray-absorption.In order to regulate the pH value of absorption liquid, nitre (phosphorus) acid solution is squeezed into static mixer with centrifugal pump from nitre (phosphorus) acid solution storage tank, evenly is mixed in circulating absorption solution and goes.The sour ammonium of the nitre generated in absorption process (phosphorus), draw and deliver to main line production nitrophosphate fertilizer from tower reactor, realizes the recycling of ammonia.Be further characterized in that, on the absorption liquid circulation line, cooler is set, by the control to the absorption liquid temperature, in the situation that do not make condensation vapor, the temperature of reduce absorption process, to improve the absorptivity of ammonia, utilize the temperature difference of gas-liquid two-phase simultaneously, by the evaporation of the moisture in an absorption liquid part, obtain denseer nitre (phosphorus) ammonium salt solution, to alleviate the thermic load of main flow solution evaporation link.
The present invention has following beneficial effect:
(1) there is dead band in packed tower, easily stops up, and misoperation also can liquid flooding, reduces absorption efficiency; Spray column is void tower, without dead band, exists, and never stops up, can liquid flooding, and stable operation is reliable, and the gas flow resistance is little, and the blower fan power consumption is low.(2) to adopt nitre (phosphorus) acid solution be absorbent in the present invention, generate the sour ammonium of nitre (phosphorus) after absorbing the ammonia in tail gas, by chemical reaction process, ammonia is fixed in liquid phase, the volatilization loss of ammonia in liquid phase under minimizing high temperature, overcome the adverse effect of hot conditions to absorption process, can obtain higher absorption efficiency.(3) regulate the temperature of absorption liquid near the dew-point temperature of gas by cooler, absorption process is controlled at lower temperature carries out, be beneficial to the absorption of ammonia, simultaneously, absorb temperature by control moisture is fixed in gas phase, avoid condensation vapor to reduce the concentration of absorption liquid, also can utilize the sensible heat of gas to evaporate portion of water, obtain denseer nitre (phosphorus) acid ammonium solution and return to main flow, alleviate the load of evaporimeter on main flow.
The accompanying drawing explanation
Fig. 1 is the system flow chart of deamination apparatus of the present invention and technique.In figure, the 1-absorption tower, 2-absorbs liquid pool, 3-circulated sprinkling layer, the multiple shelves of 4-demister, 5-air-introduced machine, 6-absorption liquid circulating pump, 7-nitre (phosphorus) acid solution storage tank, 8-charge pump, 9-static mixer, 10-absorption liquid cooler.
The specific embodiment
Below in conjunction with accompanying drawing, flow process, method and the technological means of spray deamination of the present invention is described further.
As shown in Figure 1, tail gas ammonia retracting device of the present invention mainly comprises a spray column 1, an absorption liquid circulating pump 6, a nitre (phosphorus) acid solution storage tank 7, a nitre (phosphorus) acid solution charge pump 8, a static mixer 9, absorption liquid cooler 10, one multiple grade demister 4 and an air-introduced machine 5.Spray column 1 is designed by counter current contacting, bottom is for absorbing liquid pool 2, top is furnished with two-layer circulated sprinkling layer 3, absorbing liquid pool 2 is connected with circulated sprinkling layer 3 with absorption liquid cooler 10 by absorption liquid circulating pump 6, static mixer 9 is arranged on the absorption liquid circulation line, be connected with nitre (phosphorus) acid solution storage tank 7 with absorption liquid pool 2 respectively, multiple shelves demister 4 and air-introduced machine 5 are set outside the spray column outlet.Be further characterized in that, will absorb liquid pool 2 and be connected with the nitrophosphate fertilizer main line by pipeline, for the sour ammonium of nitre (phosphorus) that reclaims generation, produce nitrophosphate fertilizer.
Ammonia-containing exhaust enters in tower from spray column 1 bottom, the spray section of flowing through from bottom to top, and the gas-liquid two-phase contact, heat and mass, this process key reaction formula are:
NH
3+H
2O≒NH
3+H
2O≒NH
4 ++OH
-
H
++?OH
-≒H
2O
NH
4 ++NO
3 -(H
2PO
4 -)≒NH
4NO
3(NH
4H
2PO
4)
Increase nitre (phosphorus) acid concentration, can impel the chemical absorbing reaction forward to carry out, the ammonium salt of generation is the energy stable existence in solution, reduces the volatilization loss of liquid phase ammonia.Gas phase is discharged from tower top after the washing deamination of absorption liquid, enters multiple shelves demister 4 and isolates the drop of carrying secretly, and extract emptying out by air-introduced machine 5.The tower reactor absorption liquid is carried by circulating pump 6, sends into spraying layer 3 after absorption liquid cooler 10 cools, and ammonia-containing exhaust is carried out to spray-absorption.Pass into cooling water in cooler 10, remove the part heat from absorption liquid, to reduce the temperature of absorption process, simultaneously, lower than gas, utilize the sensible heat evaporation portion of water of gas due to the absorption liquid temperature, play the effect of concentrated absorption liquid, obtain dense ammonium nitrate solution and return to the nitrophosphate fertilizer main flow, alleviate the load of evaporimeter on main flow.Control the temperature of cooler, make more than absorption process is controlled at the gas dew point temperature, to avoid condensation vapor to reduce the concentration of absorption liquid.In order to regulate the pH value of absorption liquid, nitre (phosphorus) acid solution is squeezed into static mixer 9 with centrifugal charge pump 8 from nitre (phosphorus) acid solution storage tank 7, evenly is mixed in absorption liquid and goes.Regulate the flow of charge pump 8, the pH=1 of control absorption liquid ~ 5, make absorptivity remain on a higher level.The sour ammonium of the nitre generated in absorption process (phosphorus), draw and deliver to main line production nitrophosphate fertilizer from tower reactor, realizes the recycling of ammonia.
In sum, innovation characteristic of the present invention has three: one, adopts spray column to substitute packed tower, has not only solved the blockage problem of equipment, and has reduced the resistance of gas, has reduced the power consumption of air-introduced machine.The 2nd, adopt nitre (phosphorus) acid solution as absorbent, by chemical absorbing, ammonia is fixed on to liquid phase, effectively prevent the volatilization of ammonia from liquid phase, absorption process generates the sour ammonium of nitre (phosphorus) and directly recycles and produce the nitrophosphate fertilizer product.The 3rd, absorb temperature by appropriate control, the moisture that tail gas is carried is fixed on gas phase, prevents from that it from condensing to enter liquid phase, and utilizes the sensible heat of gas to evaporate the moisture of a part of absorption liquid, obtains denseer ammonium nitrate solution, with the raising value.By technological means of the present invention, overcome the nitrophosphate fertilizer neutralization and transformed tail gas high-temperature, high-moisture percentage, the low ammonia concentration adverse effect that recovery produces to ammonia, recovery process is simple and cost is low, has promotional value.
According to the described flow process of Fig. 1 and technique; built the model test device in laboratory; tower diameter 100mm, spray section tower height 1.6m, spray equipment is a multihole distributor; aperture 1.5mm; pitch of holes 7mm, test the mist that analog gas used is air and ammonia, and mist can be heated to by preheater temperature required; absorption liquid used is formed by nitric acid and distilled water configuration, and the method that in tail gas, ammonia concentration adopts environmental protection ministerial standard (HJ533-2009) to introduce is detected.Analog reslt is as follows:
Embodiment 1
Under normal temperature condition, salpeter solution is absorbent, regulates absorption liquid pH=3, and absorption liquid is played circulation with pump, sees through the tower top spray equipment and is dispersed into drop, records the about 2.8mm of liquid-drop diameter, with the ammonia-containing exhaust entered at the bottom of tower, carries out counter current contacting, and the control sprinkle density is 89m
3/ (m
2﹒ h), empty tower gas velocity is 1.95m/s, the NH in tail gas
3carry out chemical reaction and remove with the nitric acid in absorption liquid, the tail gas of purification is through demister except after the fine drop of deentrainment, and emptying by air-introduced machine, absorption liquid is discharged from tower reactor.Absorption tower entrance NH
3content is 3000mg/m
3, outlet content is 419mg/m
3, deamination efficiency 86%.
Embodiment 2
Under normal temperature, salpeter solution is absorbent, regulates absorption liquid pH=3, and absorption liquid is beaten to spray equipment with circulating pump, is dispersed into diameter 2.8mm drop, with the ammonia-containing exhaust entered at the bottom of tower, carries out counter current contacting, and the control sprinkle density is 140m
3/ (m
2﹒ h), empty tower gas velocity is 1.95m/s, the NH in tail gas
3carry out chemical reaction, NH with nitric acid
3be removed.Tail gas after deamination is removed entrained drip through demister, by air-introduced machine, extracts emptying out, and still liquid is discharged absorption system.Absorption tower entrance NH
3content is 3000mg/m
3, recording the outlet ammonia content is 187 mg/m
3, deamination efficiency 93.8%.
Control entrance ammonia-containing exhaust temperature 70 C, the absorption liquid temperature 45 C, take salpeter solution as absorbent, regulate absorption liquid pH=3, circulating pump carries absorption liquid to spray equipment to be disperseed, the about 2.8mm of liquid-drop diameter, carry out counter current contacting with the ammonia-containing exhaust entered at the bottom of tower, the control sprinkle density is 140m
3/ (m
2﹒ h), empty tower gas velocity is 1.95m/s, the NH in tail gas
3carry out chemical reaction and be removed with nitric acid.Cleaning of off-gas, after the demister demist, is discharged by air-introduced machine, and the tower reactor absorption liquid is drawn absorption system.Absorption tower entrance NH
3content is 3000mg/m
3, outlet content is 232 mg/m
3, deamination efficiency 92.3%.
Embodiment 4
Under normal temperature condition, take phosphoric acid solution as absorbent, regulate absorption liquid pH=1.3, absorption liquid is played circulation with pump, sees through the tower top spray equipment and is dispersed into drop, records the about 2.8mm of liquid-drop diameter, carry out counter current contacting with the ammonia-containing exhaust entered at the bottom of tower, the control sprinkle density is 140m
3/ (m
2﹒ h), empty tower gas velocity is 2.32m/s, the NH in tail gas
3carry out chemical reaction and remove with the phosphoric acid in absorption liquid, the tail gas of purification is through demister except after the fine drop of deentrainment, and emptying by air-introduced machine, absorption liquid is discharged from tower reactor.Absorption tower entrance NH
3content is 3000mg/m
3, outlet content is 373mg/m
3, deamination efficiency 87.6%.
Claims (10)
1. a nitrophosphate fertilizer neutralizes and the device that transforms the tail gas ammonia recovery, comprise a spray column, one absorption liquid circulating pump, one nitre (phosphorus) acid solution charge pump, one nitre (phosphorus) acid solution storage tank, one static mixer, one absorption liquid cooler, one multiple grade demister and an air-introduced machine, spray column is designed by counter current contacting, bottom is for absorbing liquid pool, top is furnished with two-layer circulated sprinkling layer, absorbing liquid pool is connected with the circulated sprinkling layer with the absorption liquid cooler by the absorption liquid circulating pump, static mixer is arranged on the absorption liquid circulation line, with the absorption liquid pool, with nitre (phosphorus) acid solution storage tank, be connected respectively, multiple shelves demister and air-introduced machine are set outside the spray column outlet, be further characterized in that, to absorb liquid pool is connected with the nitrophosphate fertilizer main line, for reclaiming the sour ammonium of nitre (phosphorus) of generation, produce nitrophosphate fertilizer.
2. ammonia recovery unit according to claim 1, is characterized in that, described spraying layer has two-stage.
3. ammonia recovery unit according to claim 1, is characterized in that, described absorbent is nitre (phosphorus) acid solution.
4. ammonia recovery unit according to claim 1, is characterized in that, described cooler carries out cooling to absorption liquid to absorption liquid.
5. ammonia recovery unit according to claim 1, is characterized in that, described static mixer evenly is mixed into nitre (phosphorus) acid solution in circulating absorption solution.
6. ammonia recovery unit according to claim 1, is characterized in that, after the drop that described multiple shelves demister is carried secretly tail gas separates recovery, by air-introduced machine, extracts emptying out.
7. a nitrophosphate fertilizer neutralizes and transforms the tail gas ammonia recovery process, comprise the following steps: the nitrophosphate fertilizer ammonia-containing exhaust enters from the tower bottom, flow through the circulated sprinkling layer from bottom to top, after the washing deamination of absorption liquid, from tower top, discharge, enter multiple shelves demister and isolate the drop of carrying secretly, and extract emptying out by air-introduced machine, absorption liquid is carried by circulating pump, after cooling, cooler sends into spraying layer, by static mixer, nitre (phosphorus) acid solution evenly is mixed in circulating absorption solution and goes, to regulate the acid-base value of absorption liquid.
8. ammonia reclaiming process according to claim 7, is characterized in that, also comprises the blend step of circulating absorption solution and nitre (phosphorus) acid solution.
9. ammonia reclaiming process according to claim 7, is characterized in that, also comprises the cooling step of absorption liquid, absorption liquid cools in cooler, improve acceptance condition, by control, absorb temperature, make in tail gas steam noncondensing, utilize the tail gas sensible heat to make absorption liquid concentrated simultaneously.
10. ammonia reclaiming process according to claim 7, it is characterized in that, also comprise the recycling step of the sour ammonium of nitre (phosphorus), dense nitre (phosphorus) acid ammonium solution of spray column tower reactor by liquid pump be delivered to the Phosphate Fertilizer Production line in and workshop section, for Phosphate Fertilizer Production, realize the recycling of ammonia.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013102749621A CN103446865A (en) | 2013-07-03 | 2013-07-03 | Nitrophosphate tail gas deamination device and nitrophosphate tail gas deamination process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2013102749621A CN103446865A (en) | 2013-07-03 | 2013-07-03 | Nitrophosphate tail gas deamination device and nitrophosphate tail gas deamination process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103446865A true CN103446865A (en) | 2013-12-18 |
Family
ID=49729946
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2013102749621A Pending CN103446865A (en) | 2013-07-03 | 2013-07-03 | Nitrophosphate tail gas deamination device and nitrophosphate tail gas deamination process |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103446865A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104941380A (en) * | 2014-03-31 | 2015-09-30 | 英尼奥斯欧洲股份公司 | Improved smog eliminator operation for quenching effluent |
| CN105983317A (en) * | 2015-01-31 | 2016-10-05 | 中国石油化工股份有限公司 | Ammonia neutralization device |
| CN106345235A (en) * | 2016-11-02 | 2017-01-25 | 中国天辰工程有限公司 | Process for removing ammonia from reaction gas in preparation of hydrocyanic acid |
| CN108926962A (en) * | 2018-08-10 | 2018-12-04 | 重庆天原化工有限公司 | Ammonia-containing exhaust recovery and treatment method |
| CN109485461A (en) * | 2018-10-17 | 2019-03-19 | 贵州芭田生态工程有限公司 | Phosphorus ore acid hydrolysis waste gas absorption and utilization method neutralize mother liquor and phosphate fertilizer preparation method |
| CN110133186A (en) * | 2019-04-18 | 2019-08-16 | 贵州开磷集团矿肥有限责任公司 | A kind of diammonium phosphate exhaust washer pH measuring device |
| CN112058058A (en) * | 2020-09-02 | 2020-12-11 | 北京金隅琉水环保科技有限公司 | Recovery and circulation system for escaped ammonia in cement kiln ammonia process denitration tail gas and control method thereof |
| CN113952814A (en) * | 2021-11-29 | 2022-01-21 | 唐县冀东水泥有限责任公司 | Deamination tower for preventing ammonia from escaping |
| CN114314928A (en) * | 2022-01-04 | 2022-04-12 | 湖南烯富环保科技有限公司 | Integrated production line and method for removing chloride ions and regenerating dechlorination agent from dechlorination slag |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1040153A (en) * | 1988-07-19 | 1990-03-07 | Basf公司 | The method of from the waste gas of producing fertilizer, removing nitrogen oxide |
| US5928413A (en) * | 1996-10-25 | 1999-07-27 | Mitsubishi Heavy Industries, Ltd. | Flue gas treating system and process |
| JP2002143639A (en) * | 2000-11-10 | 2002-05-21 | Kurita Water Ind Ltd | Method for treating ammonia gas |
| CN101164662A (en) * | 2007-08-24 | 2008-04-23 | 中北大学 | Deaminizing denitrifying dehumidification technology and device in nitrophosphate fertilizer tail gas |
| CN201380041Y (en) * | 2009-03-17 | 2010-01-13 | 杨暑燕 | Spray absorption tower |
-
2013
- 2013-07-03 CN CN2013102749621A patent/CN103446865A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1040153A (en) * | 1988-07-19 | 1990-03-07 | Basf公司 | The method of from the waste gas of producing fertilizer, removing nitrogen oxide |
| US5928413A (en) * | 1996-10-25 | 1999-07-27 | Mitsubishi Heavy Industries, Ltd. | Flue gas treating system and process |
| JP2002143639A (en) * | 2000-11-10 | 2002-05-21 | Kurita Water Ind Ltd | Method for treating ammonia gas |
| CN101164662A (en) * | 2007-08-24 | 2008-04-23 | 中北大学 | Deaminizing denitrifying dehumidification technology and device in nitrophosphate fertilizer tail gas |
| CN201380041Y (en) * | 2009-03-17 | 2010-01-13 | 杨暑燕 | Spray absorption tower |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104941380A (en) * | 2014-03-31 | 2015-09-30 | 英尼奥斯欧洲股份公司 | Improved smog eliminator operation for quenching effluent |
| CN105983317A (en) * | 2015-01-31 | 2016-10-05 | 中国石油化工股份有限公司 | Ammonia neutralization device |
| CN106345235A (en) * | 2016-11-02 | 2017-01-25 | 中国天辰工程有限公司 | Process for removing ammonia from reaction gas in preparation of hydrocyanic acid |
| CN108926962A (en) * | 2018-08-10 | 2018-12-04 | 重庆天原化工有限公司 | Ammonia-containing exhaust recovery and treatment method |
| CN109485461A (en) * | 2018-10-17 | 2019-03-19 | 贵州芭田生态工程有限公司 | Phosphorus ore acid hydrolysis waste gas absorption and utilization method neutralize mother liquor and phosphate fertilizer preparation method |
| CN110133186A (en) * | 2019-04-18 | 2019-08-16 | 贵州开磷集团矿肥有限责任公司 | A kind of diammonium phosphate exhaust washer pH measuring device |
| CN112058058A (en) * | 2020-09-02 | 2020-12-11 | 北京金隅琉水环保科技有限公司 | Recovery and circulation system for escaped ammonia in cement kiln ammonia process denitration tail gas and control method thereof |
| CN113952814A (en) * | 2021-11-29 | 2022-01-21 | 唐县冀东水泥有限责任公司 | Deamination tower for preventing ammonia from escaping |
| CN114314928A (en) * | 2022-01-04 | 2022-04-12 | 湖南烯富环保科技有限公司 | Integrated production line and method for removing chloride ions and regenerating dechlorination agent from dechlorination slag |
| CN114314928B (en) * | 2022-01-04 | 2023-09-08 | 湖南烯富环保科技有限公司 | Integrated production line and method for chloride ion removal and chlorine removal slag regeneration chlorine removal agent |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103446865A (en) | Nitrophosphate tail gas deamination device and nitrophosphate tail gas deamination process | |
| CN102294159B (en) | Integrated processor for dirty, damp and hot tail gas and technology thereof | |
| CN109045976A (en) | A kind of ammonia process of desulfurization flue gas disappears white waste heat depth recovery system and application | |
| CN201333374Y (en) | Device capable of collecting carbon dioxide contained in flue gases of power plant through ammonia by utilizing void tower | |
| CN102218261B (en) | Method and equipment for collecting carbon dioxide from fuel gas by using ammonia water fine spraying | |
| CN101601964A (en) | A kind of high-efficiency ammonia flue gas desulfurization technique and device | |
| CN101708414A (en) | System and method for desulphurizing waste gas by cyclic absorption and application thereof | |
| CN201578973U (en) | Flue gas carbon dioxide capturing equipment and absorption tower thereof | |
| CN103307904A (en) | Fog-dissipation and water-recycling type cooling tower | |
| CN201026440Y (en) | Absorption, oxidation, concentration combined desulfurizing tower | |
| CN101428196A (en) | In-hollow column intercrystalline ammonia process of desulfurization, recovery system and method thereof | |
| CN2899917Y (en) | Smoke desulfurizing and denitrifying device by ammonia method | |
| CN108426264A (en) | The device of coloured plume is eliminated in a kind of Mist heat recovering collaboration dedusting | |
| CN107166416A (en) | A kind of gas industry boiler energy-saving and flue gas deep purifying integrated processing system and method | |
| CN104495757A (en) | System for removing low-temperature thermal energy generated during adsorption of SO3 from sulfuric acid production device | |
| CN214693383U (en) | Chemical production ammonia-containing wastewater treatment device | |
| CN206492366U (en) | The compact ammonia process carbon trapping system of ammoniacal liquor second-kind absorption-type heat pump driving | |
| CN205360984U (en) | Waste discharge production line of ammonia preparation ammonium sulfate crystallization of utilization | |
| CN208742284U (en) | A kind of single column washing Wet fume sweetening dust remover of no stock tank secondary cycle | |
| CN206334531U (en) | A kind of water saving in ammonia desulfurizing process and the device for controlling aerosol phenomenon | |
| CN201609626U (en) | Device applied in ammonia flue gas desulfurization by using technology of hydrochloric acid production through flue gas dechlorination | |
| CN209348375U (en) | Flue gas takes off white plumage system | |
| CN207042170U (en) | Condensation method water saving wet desulfurizer | |
| CN106693614A (en) | Ammonia-water second-kind absorption type heat pump driven compact type ammonia-process carbon capture system | |
| CN209034090U (en) | A kind of ammonia process of desulfurization flue gas disappears white waste heat depth recovery system |
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: 20131218 |