CN101664627B - Method and equipment for purifying tail gas generated in producing sodium cyanide by cracking light oil - Google Patents
Method and equipment for purifying tail gas generated in producing sodium cyanide by cracking light oil Download PDFInfo
- Publication number
- CN101664627B CN101664627B CN2009101876248A CN200910187624A CN101664627B CN 101664627 B CN101664627 B CN 101664627B CN 2009101876248 A CN2009101876248 A CN 2009101876248A CN 200910187624 A CN200910187624 A CN 200910187624A CN 101664627 B CN101664627 B CN 101664627B
- Authority
- CN
- China
- Prior art keywords
- tower
- tail gas
- sodium cyanide
- decyanation
- equipment
- 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.)
- Expired - Fee Related
Links
Landscapes
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a method and equipment for purifying tail gas generated in producing sodium cyanide by cracking light oil and relates to a method and equipment for purifying tail gas of sodium cyanide, in particular to a method and equipment for absorbing hydrogen cyanide and ammonia in the tail gas by chemical and physical methods. The equipment comprises a decyanation tower, a deamination tower, a distillation tower, as well as a water ring vacuum pump, a feed gas cooler, a heat exchanger, and the like, wherein decyanation comprises the steps of adopting a caustic soda solution spraying method for generating the sodium cyanide and water in the decyanation tower; deamination comprises the steps of adopting a water spraying method for absorbing the ammonia in the tail gas in the deamination tower and then heating and distilling to obtain ammonia water. The tail gas of sodium cyanide can be used as available hydrogen for recovery after the decyanation and the deamination. The method and the equipment are both simple and easy to implement, not only solve the problem of pollution of the sodium cyanide on atmospheric environment, but also enhance the economic benefits of enterprises, accord with the recycling economy mode and solve the problems of complex equipment structure and heavy investment in the existing sodium cyanide tail gas processing method.
Description
Technical field
The present invention relates to the purification method of tail gas of sodium cyanide, specifically is a kind of hydrogen cyanide in chemistry and the physical method absorption tail gas and method of ammonia utilized.
Background technology
Present domestic Sodium Cyanide Production is based on light oil cracking method, produces hydrogen cyanide earlier, absorbs with soda bath and produces Cymag.And contain hydrogen cyanide gas and ammonia in the tail gas that existing production method produces, and all be discharged in the atmosphere, so not only serious environment pollution causes waste again because this part gas can not obtain utilizing.Existing enterprise adopts the method for sulfuric acid absorption in order to utilize the ammonia in the tail gas.And the enforcement of this method then needs a large amount of investments, and the equipment complexity, and operating cost is very high.
Summary of the invention
At existing situation, the purpose of this invention is to provide a kind of good purification, the purification method of the tail gas of sodium cyanide that operating cost is low is to solve pollution problem and the resource reutilization of tail gas to environment.
Technical scheme of the present invention is hydrogen cyanide gas and the ammonia that adopts in chemistry and the physical method cleaning of off-gas, obtains Cymag and ammoniacal liquor.
Structure of the present invention is as shown in drawings: be made of decyanation tower, deammoniation tower and destilling tower.One water ring vacuum pump is arranged between decyanation tower and deammoniation tower, a feed gas chiller is arranged between water ring vacuum pump and the deammoniation tower.Decyanation tower, water ring vacuum pump and feed gas chiller link to each other by pipeline, and are communicated with deammoniation tower.One heat exchanger is arranged between deammoniation tower and destilling tower.Heat exchanger exit connects a still liquid cooler.Still liquid cooler links to each other with deammoniation tower.In the destilling tower outlet one overhead condenser is arranged.One ammoniacal liquor cooler is arranged in the overhead condenser bottom.In ammoniacal liquor cooler bottom one basin is arranged.In the destilling tower bottom one reboiler is arranged.Exhaust gas treating method of the present invention is: when the tail gas of producing enters the decyanation tower, in the decyanation tower, the soda bath of employing 30% sprays processing to tail gas, generates Cymag and water.The soda bath spray flux is 15m
3/ h.The unstripped gas air inflow is 10000Nm
3/ h, wherein hydrogen 80%, ammonia 1.2%, hydrogen cyanide 0.0005%, other is nitrogen.Outlet by the tail gas process decyanation tower after the spray processing is sent to the water ring vacuum pump supercharging.The exhaust temperature that enters the decyanation tower is 65～70 ℃.Pressure is-0.03～-0.04Mpa.Through 30% soda bath spray, exhaust temperature drops to 50～55 ℃.Tail gas enters water ring vacuum pump after the decyanation, and the solubility with pressure of ammonia in water increases and increase, and therefore the pump discharge gas pressure increased to 0.06～0.07Mpa.Again tail gas is delivered to feed gas chiller, be cooled to 35～40 ℃ and enter deammoniation tower.Water sprays processing to tail gas in deammoniation tower, and the ammonia in the tail gas is absorbed by water.Absorption liquid is the weak aqua ammonia of 1.0～1.5% content.The spray water consumption is 13m
3/ h, the tail gas air inflow is about 10000Nm
3/ h.Weak aqua ammonia is sent into heat exchanger then, and sending into destilling tower after weak aqua ammonia is heated to 90 ℃ carries out concentration.Treatment temperature is 105 ℃.Pressure is 0.08～0.1Mpa.Distillation back finished product ammoniacal liquor is by the overhead condenser extraction, enters basin be cooled to room temperature in the ammoniacal liquor cooler after.Tail gas of sodium cyanide conduct behind the decyanation deamination can utilize hydrogen to reclaim.
The present invention sends out method and equipment is all simple, and is easy to implement.The equipment that adopts is conventional decyanation tower, deammoniation tower and destilling tower.By installing water ring vacuum pump additional, feed gas chiller, heat exchanger etc. constitute the tail gas of sodium cyanide purifier.Spray mode by soda bath reclaims Cymag.Adopt the spray mode of water to reclaim ammoniacal liquor.The while recover hydrogen.Both solved the pollution of tail gas of sodium cyanide,, met the recycling economy pattern again for enterprise has increased economic benefit to atmospheric environment.Solved existing device structure complexity, invested big problem the existence of tail gas of sodium cyanide processing method.
Description of drawings
Accompanying drawing is a structural representation of the present invention
1-decyanation tower 2-water ring vacuum pump 3-feed gas chiller 4-deammoniation tower 5-still liquid cooler 6-heat exchanger 7-destilling tower heat exchanger 8-overhead condenser 9-ammoniacal liquor cooler 10-reboiler 11-basin
Arrow is the flow direction such as tail gas, ammoniacal liquor, condensed water behind the tail gas clean-up among the figure
The specific embodiment
Structure of the present invention is as shown in drawings: be made of decyanation tower 1, deammoniation tower 4 and destilling tower 7.The specification of decyanation tower is E=5.36M
2, φ 2600 * 20000.The specification of deammoniation tower is φ 1400 * 16000.Destilling tower is φ 1000 * 13000.One water ring vacuum pump 2 is arranged between decyanation tower and deammoniation tower, a feed gas chiller 3 is arranged between water ring vacuum pump and the deammoniation tower.Decyanation tower, water ring vacuum pump and feed gas chiller link to each other by pipeline, and are communicated with deammoniation tower.One heat exchanger 6 is arranged between deammoniation tower and destilling tower.Heat exchanger exit connects a still liquid cooler 5.Still liquid cooler links to each other with deammoniation tower.In the destilling tower outlet one overhead condenser 8 is arranged.One ammoniacal liquor cooler 9 is arranged in the overhead condenser bottom.In ammoniacal liquor cooler bottom one basin 11 is arranged.One reboiler 10 is arranged in the destilling tower bottom.The tail gas of producing is with 10000Nm
3/ h enters the decyanation tower, and in the decyanation tower, the soda bath of employing 30% sprays processing to tail gas.The soda bath spray flux is 15m
3/ h., generate Cymag and water.Outlet by the tail gas process decyanation tower after the spray processing is sent to the water ring vacuum pump supercharging.The exhaust temperature that enters the decyanation tower is 70 ℃.Pressure is-0.03Mpa.Through the soda bath spray, exhaust temperature drops to 55 ℃.Tail gas enters water ring vacuum pump after the decyanation.The pump discharge gas pressure is 0.06Mpa.Again tail gas is delivered to feed gas chiller, be cooled to 40 ℃ and enter deammoniation tower.Water sprays processing to tail gas in deammoniation tower, and the tail gas air inflow is about 10000Nm
3/ h, the spray water consumption is 13m
3/ h.Generate the weak aqua ammonia of 1.5% content.Weak aqua ammonia is sent into heat exchanger then, and sending into destilling tower after weak aqua ammonia is heated to 90 ℃ carries out concentration.Treatment temperature is 105 ℃.Pressure is 0.08Mpa.Distillation back finished product ammoniacal liquor enters basin after being cooled to room temperature in overhead condenser enters the ammoniacal liquor cooler.By operation 24 hours every days, per hour recyclable 81% hydrogen 9880 standard cubic meters.Every day recyclable 17～18% content 5 tons of ammoniacal liquor.Reclaim 2.6 kilograms of 100% Cymags every day.
Claims (2)
1. the exhaust purifying method of a generated in producing sodium cyanide by cracking light oil, it is characterized in that: the tail gas of producing enters the decyanation tower, adopts 30% soda bath that tail gas is sprayed processing, and the soda bath spray flux is 15m
3/ h, the unstripped gas air inflow is 10000Nm
3Again through being pressurized to 0.06～0.07Mpa, being cooled to 35～40 ℃ after the supercharging again and entering deammoniation tower after/h, quilt are sprayed and handle, water sprays processing to tail gas in deammoniation tower, and the spray water consumption is 13m
3/ h, the tail gas air inflow is about 10000Nm
3/ h sends into weak aqua ammonia then and sends into destilling tower after heat exchanger is heated to 90 ℃ and carry out concentration, and treatment temperature is 105 ℃, and pressure is 0.08～0.1Mpa.
2. the exhaust gas purification equipment of a generated in producing sodium cyanide by cracking light oil, by decyanation tower (1), deammoniation tower (4) and destilling tower (7) constitute, it is characterized in that: a water ring vacuum pump (2) is arranged between decyanation tower and deammoniation tower, one feed gas chiller (3) between taking, water ring vacuum pump and deamination is arranged, the decyanation tower, water ring vacuum pump and feed gas chiller link to each other by pipeline, and connection deammoniation tower, one heat exchanger (6) is arranged between deammoniation tower and destilling tower, connect a still liquid cooler (5) on the heat exchanger exit, still liquid cooler links to each other with deammoniation tower, in destilling tower upper outlet portion one overhead condenser (8) is arranged, one ammoniacal liquor cooler (9) is arranged in the overhead condenser bottom, in ammoniacal liquor cooler bottom one basin (11) is arranged, a reboiler (10) is arranged in the destilling tower bottom.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009101876248A CN101664627B (en) | 2009-09-23 | 2009-09-23 | Method and equipment for purifying tail gas generated in producing sodium cyanide by cracking light oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009101876248A CN101664627B (en) | 2009-09-23 | 2009-09-23 | Method and equipment for purifying tail gas generated in producing sodium cyanide by cracking light oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101664627A CN101664627A (en) | 2010-03-10 |
| CN101664627B true CN101664627B (en) | 2010-09-15 |
Family
ID=41801502
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2009101876248A Expired - Fee Related CN101664627B (en) | 2009-09-23 | 2009-09-23 | Method and equipment for purifying tail gas generated in producing sodium cyanide by cracking light oil |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101664627B (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102502708B (en) * | 2011-10-21 | 2013-11-13 | 重庆紫光天化蛋氨酸有限责任公司 | Preparation method for preparing alkali metal or alkali earth metal cyanide with high purity and high yield |
| CN105645436B (en) * | 2016-03-18 | 2017-10-17 | 安徽省化工设计院 | A kind of system that ammonia is reclaimed in the waste gas produced from benzene cyanogen class device |
| CN106629878A (en) * | 2016-10-20 | 2017-05-10 | 安庆市长虹化工有限公司 | High-cyanide-content wastewater treatment system and treatment method |
| CN109621638A (en) * | 2018-12-07 | 2019-04-16 | 鲁西化工集团股份有限公司 | A kind of the deamination and desulfurization device and technique of conversion gas condensate liquid |
| CN110589852B (en) * | 2019-10-10 | 2023-04-07 | 营创三征(营口)精细化工有限公司 | Method and device for producing sodium cyanide by mixed cracking of ammonia, light oil and natural gas |
| CN110563000A (en) * | 2019-10-11 | 2019-12-13 | 营创三征(营口)精细化工有限公司 | Energy-saving tail gas deamination process and equipment for producing sodium cyanide |
| CN113082949B (en) * | 2021-05-14 | 2023-03-21 | 云南绿宝香精香料股份有限公司 | Deodorization system is retrieved in eucalyptus oil valeraldehyde separation |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1994530A (en) * | 2006-12-08 | 2007-07-11 | 昆明理工大学 | Method for removing hydrogen sulfide and hydrogen cyanide from calcium carbide furnace gas |
-
2009
- 2009-09-23 CN CN2009101876248A patent/CN101664627B/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1994530A (en) * | 2006-12-08 | 2007-07-11 | 昆明理工大学 | Method for removing hydrogen sulfide and hydrogen cyanide from calcium carbide furnace gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101664627A (en) | 2010-03-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101664627B (en) | Method and equipment for purifying tail gas generated in producing sodium cyanide by cracking light oil | |
| CN102060406B (en) | Efficient stripping and closed-loop treatment integrated process for recycling ammonia nitrogen wastewater from tail gas | |
| CN202924782U (en) | Rectification stripping device for ammonia-nitrogen wastewater treatment | |
| CN111302899B (en) | Ammonia and tertiary butanol recovery device and method in cyclohexanone ammoximation production process | |
| CN102190341B (en) | Stripping ammonia-removing method based on flash evaporation and heat pump technologies | |
| CN107758960A (en) | A kind of processing method of ammonia waste water | |
| CN110498398B (en) | Waste hydrochloric acid differential pressure regeneration treatment system and regeneration treatment method | |
| CN104860464A (en) | Energy-saving ammonia-nitrogen wastewater treatment method and device | |
| CN201410354Y (en) | Waste gas absorption device for nitrate production | |
| CN104829494A (en) | Energy-saving urea production system and production process thereof | |
| CN210786860U (en) | Tail gas absorption device for recycling carbon dioxide | |
| CN103145287A (en) | Method for recovering ammonia and synthesis gas from coking wastewater | |
| CN101857246B (en) | Process method for co-producing ammonium bicarbonate by using coking plant waste | |
| CN104370404A (en) | Melamine device wastewater treatment method and treatment system thereof | |
| CN104860465B (en) | Double-tower catalysis thermal-coupling reflux deamination method and deamination device thereof | |
| CN109432958A (en) | A kind for the treatment of device for ammonia-containing waste gas | |
| CN204337983U (en) | The recycling treatment process system of MOCVD waste gas in a kind of LED chip production process | |
| CN219399606U (en) | Be used for viscose fiber exhaust gas treatment system | |
| CN219194564U (en) | Device for concentrating waste liquid in 1, 4-butanediol production | |
| CN215249583U (en) | Waste acid concentration regeneration sulfuric acid production line | |
| CN212450617U (en) | Waste hydrochloric acid differential pressure regeneration treatment system | |
| CN204079524U (en) | A kind of high salt high ammonia-nitrogen sewage treatment system | |
| CN203128193U (en) | Purifying and recovering equipment system of sulfur tetrafluoride | |
| CN208265798U (en) | Taurine wastewater zero discharge processing unit | |
| CN202478634U (en) | Device for processing acid mist |
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 | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20100915 Termination date: 20140923 |
|
| EXPY | Termination of patent right or utility model |