CN1042124C - Continuous prodn equipment for liquid SO3 and 65% SO3 fuming sulfuric acid utilizing afterheat in converted gas - Google Patents

Continuous prodn equipment for liquid SO3 and 65% SO3 fuming sulfuric acid utilizing afterheat in converted gas Download PDF

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Publication number
CN1042124C
CN1042124C CN96116845A CN96116845A CN1042124C CN 1042124 C CN1042124 C CN 1042124C CN 96116845 A CN96116845 A CN 96116845A CN 96116845 A CN96116845 A CN 96116845A CN 1042124 C CN1042124 C CN 1042124C
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China
Prior art keywords
absorption tower
circulation groove
oleum
liquid
outlet
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Expired - Fee Related
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CN96116845A
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CN1147477A (en
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刘少武
方本中
吴家本
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  • Treating Waste Gases (AREA)
  • Gas Separation By Absorption (AREA)
  • Drying Of Gases (AREA)

Abstract

The present invention relates to equipment for producing liquid SO3 and 65% of SO3 fuming acid. In the existing sulfuric acid equipment, a 20% of SO3 fuming acid absorption tower and a 98% of sulfuric acid absorption tower are connected with an SO3 membrane evaporator, a 65% of SO3 fuming acid absorption tower and an SO3 condenser through a spiral condenser and a circulating tank; in addition, the gas inlet of the SO3 membrane evaporator is connected with reformed gas which has a certain temperature and is conveyed by a reformer; thereby, the liquid SO3 and the 65% of SO3 fuming acid can be continuously produced by the residual heat of the reformed gas.

Description

Utilize reforming gas waste heat continuous production liquid SO 3And 65%SO 3The system of oleum
The present invention relates to a kind of production sulfan (SO 3) and 65% sulphur trioxide (SO 3) system of oleum.
At present, industrial production liquid SO 3And 65%SO 3(dissociating) oleum all adopts 20%SO 3(dissociating) common oleum is a raw material, and through 2-3 placed in-line still pot, with the coal heating, one pot one pot discontinuously SO 3Steam, make liquid SO through condensation 3Or 65%SO 3Sulfuric acid behind the fuming acid, every pot of steaming is put back to system again.Again in pot, add 20%SO later on 3Fuming acid continues to produce.The poor product quality that this method is produced, the device structure complexity, investment is big, and is intermittent operation, and it was both dangerous to need to consume a large amount of bunker coals, and output is low again.In addition, producing in the vitriolic technology with reforming gas, adopting the processing unit of double conversion and double absorption usually, promptly it has two absorption towers, carries out twice absorption with twice reforming gas and produces sulfuric acid.Though this equipment need not consume coal, can't produce pure SO 3And 65%SO 3Fuming acid can't satisfy people's needs.
Purpose of the present invention is exactly to provide a kind of device structure simple in order to address the above problem, invest little, the safe and reliable reforming gas waste heat continuous production liquid SO that utilizes 3And 65%SO 3The system of oleum.
Technical solution of the present invention:
A kind of reforming gas waste heat continuous production liquid SO that utilizes 3And 65%SO 3The system of oleum, it includes 20%SO 3Oleum absorption tower 1 and 98% sulfuric acid absorption tower 2, wherein the outlet on absorption tower 1 links to each other with circulation groove 6-2, the outlet on absorption tower 2 with circulation groove 6-3, link to each other, circulation groove 6-2 and 6-3 are connected by pump (9), comb water cooler 7 connects the spray acid import of 98% sulfuric acid absorption tower 2, and spiral water cooler 8 meets 20%SO 3The spray acid import on oleum absorption tower 1, another outlet that it is characterized in that circulation groove 6-2 links to each other with the liquid-inlet of thin-film evaporator 3 by pump 10, the gas feed of thin-film evaporator 3 connects the reforming gas of being sent here by convertor with certain temperature, and reforming gas is communicated with the pneumatic outlet of thin-film evaporator 3 by valve 11 simultaneously and together meets 20%SO 3The gas feed on oleum absorption tower 1, the liquid exit of thin-film evaporator 3 connects the import of circulation groove 6-2, form the recycle system of thin-film evaporator 3, the evaporation outlet of thin-film evaporator 3 links to each other with the gas feed of condenser 4, the entery and delivery port of condenser 4 connects water coolant, can obtain neat liquid SO at its condensate outlet 3, the pneumatic outlet of condenser 4 meets 65%SO 3The gas feed on oleum absorption tower 5,65%SO 3The pneumatic outlet on oleum absorption tower 5 connects the gas feed of 98% sulfuric acid absorption tower 2 by valve 12, and its liquid exit meets the circulation groove 6-1 of self, and circulation groove 6-1 meets 65%SO by pump 13 and spiral water cooler 14 3The spray acid import on oleum absorption tower 5, circulation groove 6-2 also is communicated with circulation groove 6-1,6-3 by pump 15.
System of the present invention is rationally advanced, and is simple in structure, invests for a short time, both can produce liquid SO separately 3Or 65%SO 3Fuming acid also can while continuous production liquid SO 3And 65%SO 3Fuming acid.Present device utilizes reforming gas used heat to come work, so equipment is durable in use, need not to expend bunker coal, the production cost product low 100% more than than produced in conventional processes per ton, and entire equipment production is being carried out under the air tight condition continuously, and the concentration of medium that is contacted is a scope stably, and equipment is subjected to the corrosion situation very faint, the quality product height is wanted much superior at aspects such as outward appearance and dregginess.
Fig. 1 is the structure principle chart of system of the present invention.
Dotted portion is the part of original sulfuric acid typical production flow process among Fig. 1, and the solid line among Fig. 1 is partly made liquid SO for the present invention 3With 65% free SO 3The environment division that oleum increased.
As Fig. 1, temperature is that (this reformed gas is by SO for 200~290 ℃ reforming gas 3Convertor is sent, and it is about 8% SO 3Gas) at first send into thin-film evaporator 3, this moment is by 200%SO 3The 20% free SO that carry to thin-film evaporator 3 by circulation groove 6-2 and pump 10 on oleum absorption tower 1 3Just by the heat heating evaporation of reforming gas itself, the reforming gas after the heat exchange is sent into 20%SO to oleum 31 relieving haperacidity of oleum absorption tower, SO 3Thin-film evaporator 3 evaporation back liquid are got back to circulation groove 6-2, with 20%SO 3The concentration that oleum absorption tower 1 is sent is higher than 20% free SO 3Oleum is sent into SO after mixing again 3Thin-film evaporator 3 forms circulation.Evaporation at thin-film evaporator 3 exports the SO that obtains 3Vaporised gas is delivered to SO 3Condenser 4 condensations just obtain condensed neat liquid SO from the condensate outlet of condenser 4 3, the SO that does not have condensation to get off 3Gas is delivered to 65%SO again 3Oleum absorption tower 5 absorbs, and sends into circulation acid tank 6-1 after the absorption, and circulation acid tank 6-1 sends into 14 coolings of spiral water cooler by pump 13, and the liquid-inlet of sending absorption tower 5 after the cooling back to is by absorbing SO 3Gas increases concentration, can obtain 65%SO from the outlet of spiral water cooler 14 simultaneously 3The oleum finished product.For guaranteeing that circulation acid tank 6-2 goes here and there acid and regulates, when promptly concentration is high, deliver to circulation groove 6-2, if amount is after a little while, be returned to circulation groove 6-1 from circulation groove 6-2 outlet by pump 15 again, guarantee continuous production.65%SO 3The gas that not having in the oleum absorption tower 5 absorbs is delivered to 98% sulfuric acid absorption tower 2 from its outlet and is absorbed once more and be used for relieving haperacidity.

Claims (1)

1. one kind is utilized reforming gas waste heat continuous production liquid SO 3And 65%SO 3The system of oleum, it includes 20%SO 3Oleum absorption tower (1) and 98% sulfuric acid absorption tower (2), wherein the outlet of absorption tower (1) links to each other with circulation groove (6-2), the outlet on absorption tower (2) links to each other with circulation groove (6-3), circulation groove (6-2) and (6-3) be connected by pump (9), comb water cooler (7) connects the spray acid import of 98% sulfuric acid absorption tower (2), and spiral water cooler (8) meets 20%SO 3The spray acid import on oleum absorption tower (1), another outlet that it is characterized in that circulation groove (6-2) links to each other with the liquid-inlet of thin-film evaporator (3) by pump (10), the gas feed of thin-film evaporator (3) connects the reforming gas of being sent here by convertor with certain temperature, and reforming gas is communicated with the pneumatic outlet of thin-film evaporator (3) by valve (11) simultaneously and together meets 20%SO 3The gas feed on oleum absorption tower (1), the liquid exit of thin-film evaporator (3) connects the import of circulation groove (6-2), form the recycle system of thin-film evaporator (3), the evaporation outlet of thin-film evaporator (3) links to each other with the gas feed of condenser (4), the entery and delivery port of condenser (4) connects water coolant, can obtain neat liquid SO at its condensate outlet 3, the pneumatic outlet of condenser (4) meets 65%SO 3The gas feed on oleum absorption tower (5), 65%SO 3The pneumatic outlet on oleum absorption tower (5) connects the gas feed of 98% sulfuric acid absorption tower (2) by valve (12), and its liquid exit connects the circulation groove (6-1) of self, and circulation groove (6-1) meets 65%SO by pump (13) and spiral water cooler (14) 3The spray acid import on oleum absorption tower (5), circulation groove (6-2) also is communicated with circulation groove (6-1), (6-3) by pump (15).
CN96116845A 1996-02-14 1996-02-14 Continuous prodn equipment for liquid SO3 and 65% SO3 fuming sulfuric acid utilizing afterheat in converted gas Expired - Fee Related CN1042124C (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN96116845A CN1042124C (en) 1996-02-14 1996-02-14 Continuous prodn equipment for liquid SO3 and 65% SO3 fuming sulfuric acid utilizing afterheat in converted gas

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Application Number Priority Date Filing Date Title
CN96116845A CN1042124C (en) 1996-02-14 1996-02-14 Continuous prodn equipment for liquid SO3 and 65% SO3 fuming sulfuric acid utilizing afterheat in converted gas

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CN1147477A CN1147477A (en) 1997-04-16
CN1042124C true CN1042124C (en) 1999-02-17

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Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100425528C (en) * 2005-03-09 2008-10-15 上海华谊集团上硫化工有限公司 Preparation of high concentration fuming sulfuric acid using residual heat distillation method
CN105366650B (en) * 2014-08-31 2018-10-02 天津渤大硫酸工业有限公司 A kind of oleum production equipment
CN110155955B (en) * 2019-04-01 2021-07-23 岷山环能高科股份公司 Production method for preparing electronic-grade sulfuric acid by using non-ferrous smelting flue gas
CN116101982B (en) * 2023-01-09 2024-06-14 江苏吉华化工有限公司 Sulfur acid making system and method

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1013267B (en) * 1987-10-12 1991-07-24 美克德株式会社 Container lid

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1013267B (en) * 1987-10-12 1991-07-24 美克德株式会社 Container lid

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Free format text: CORRECT: PATENTEE; FROM: TAN XIANFENG; ZHANG JINGJIANG; LIU SHAOWU TO: JURONG CHANGJIANG CHEMICAL INDUSTRY CO.,JIANGSU PROVINCE

CP03 Change of name, title or address

Address after: 212411 Shu Town, Jiangsu City, Jurong Province

Patentee after: Jurong Jiangsu Changjiang chemical industry company

Address before: 212411 Jurong sulphuric acid factory of Shu Town, Jurong County, Jiangsu Province

Patentee before: Tan Xianfeng

Patentee before: Zhang Jingjiang

Patentee before: Liu Shaowu

C19 Lapse of patent right due to non-payment of the annual fee
CF01 Termination of patent right due to non-payment of annual fee