CN1042124C - Continuous production of liquid SO by using waste heat of converted gas3And 65% SO3System of oleum - Google Patents
Continuous production of liquid SO by using waste heat of converted gas3And 65% SO3System of oleum Download PDFInfo
- 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
- Authority
- CN
- China
- Prior art keywords
- absorption tower
- oleum
- circulation groove
- liquid
- film evaporator
- 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
- 239000007788 liquid Substances 0.000 title claims abstract description 20
- 239000002918 waste heat Substances 0.000 title claims abstract description 6
- 238000010924 continuous production Methods 0.000 title claims description 7
- 238000010521 absorption reaction Methods 0.000 claims abstract description 36
- 239000007789 gas Substances 0.000 claims abstract description 33
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 24
- 239000002253 acid Substances 0.000 claims abstract description 18
- 239000010409 thin film Substances 0.000 claims abstract description 18
- 238000002407 reforming Methods 0.000 claims abstract description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 10
- 230000008676 import Effects 0.000 claims description 8
- 239000007921 spray Substances 0.000 claims description 6
- 238000001704 evaporation Methods 0.000 claims description 5
- 230000008020 evaporation Effects 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- PVNIIMVLHYAWGP-UHFFFAOYSA-N Niacin Chemical compound OC(=O)C1=CC=CN=C1 PVNIIMVLHYAWGP-UHFFFAOYSA-N 0.000 abstract 1
- 239000010408 film Substances 0.000 abstract 1
- 239000011664 nicotinic acid Substances 0.000 abstract 1
- 239000003245 coal Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000005580 one pot reaction Methods 0.000 description 2
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
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- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
- Drying Of Gases (AREA)
Abstract
The invention relates to a method for producing liquid SO3And 65% SO3A system of fuming acid, which uses 20 percent SO of the existing sulfuric acid equipment3Fuming acid absorption tower, 98% sulfuric acid absorption tower and SO3Thin film evaporator and 65% SO3Fuming acid absorption tower and SO3The condenser is connected with an integral device through a spiral condenser and a circulating tank, and SO3The gas inlet of the film evaporator is connected with the reforming gas with a certain temperature sent by the reformer, SO that the liquid SO is continuously produced by utilizing the waste heat of the reforming gas3And 65% SO3Nicotinic acid.
Description
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).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96116845A CN1042124C (en) | 1996-02-14 | 1996-02-14 | Continuous production of liquid SO by using waste heat of converted gas3And 65% SO3System of oleum |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96116845A CN1042124C (en) | 1996-02-14 | 1996-02-14 | Continuous production of liquid SO by using waste heat of converted gas3And 65% SO3System of oleum |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1147477A CN1147477A (en) | 1997-04-16 |
| CN1042124C true CN1042124C (en) | 1999-02-17 |
Family
ID=5123801
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96116845A Expired - Fee Related CN1042124C (en) | 1996-02-14 | 1996-02-14 | Continuous production of liquid SO by using waste heat of converted gas3And 65% SO3System of oleum |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1042124C (en) |
Families Citing this family (4)
| 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)
| 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 |
-
1996
- 1996-02-14 CN CN96116845A patent/CN1042124C/en not_active Expired - Fee Related
Patent Citations (1)
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1147477A (en) | 1997-04-16 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C06 | Publication | ||
| PB01 | Publication | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C53 | Correction of patent of invention or patent application | ||
| COR | Change of bibliographic data |
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 |