CN105480953A - Alkylated waste acid cracking technology adopting sulphur as fuel - Google Patents
Alkylated waste acid cracking technology adopting sulphur as fuel Download PDFInfo
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- CN105480953A CN105480953A CN201410526789.4A CN201410526789A CN105480953A CN 105480953 A CN105480953 A CN 105480953A CN 201410526789 A CN201410526789 A CN 201410526789A CN 105480953 A CN105480953 A CN 105480953A
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- acid
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses an alkylated waste acid cracking technology adopting sulphur as fuel and especially a production technology of sulfuric acid by alkylated waste acid cracking in high-temperature environment generated by sulphur combustion. The technology comprises the following steps: cracking the waste sulfuric acid in high-temperature environment, recovering the heat from an exhaust-heat boiler, performing closed acid scrubbing and purifying, transforming for two times, absorbing for two times, absorbing the tail gas and so on, so that qualified sulfuric acid product is produced. Compared with commonly used gaseous fuels, such as the natural gas, the liquefied gas and the like, the fuel sulphur can be transformed into the product in the alkylated cracking technology, so that the device operation cost is greatly reduced; dilute acid efflux caused by H2O generated by gaseous fuel combustion is avoided, so that new waste discharge is thereby avoided; moreover, the alkylated waste acid cracking technology also reduces CO2 discharge generated by gaseous fuel combustion.
Description
Technical field
The present invention relates to a kind of sulphur that uses as the alkylation spent acid cracking technology of fuel.
Background technology
Along with the upgrading of China's gasoline quality, the demand of high-grade gasoline continues to increase, and the alkyl plant producing high-grade gasoline can produce Waste Sulfuric Acid.For a long time, waste sulfuric acid from alkylation discharge and process be a difficult problem of environmental protection always.At present, domestic several main spent acid treatment process comprises: production White Carbon black and oil rust-preventive agent technique, produces ammonium sulfate and rust-preventive agent technique, burns cracking industrial sulphuric acid, activated carbon decolorizing system 25% (W) dilute sulphuric acid.Spent acid White Carbon black not only complex process, sodium silicate raw material seldom arrives, and product White Carbon black does not have market; Spent acid thiamine process ammoniacal liquor consumption is large, major product sulphur ammonium sales difficulty, by-product rust-preventive agent there is no market; Spent acid dilute sulphuric acid technology remains in four not enough, is difficult to realize suitability for industrialized production.Burn the method existing industrial applications at present of cracking industrial sulphuric acid, generally use the geseous fuel such as Sweet natural gas, liquefied gas, the heat energy required for Waste Sulfuric Acid cracking is provided.These gas fuel combustions produce a large amount of CO
2and H
2o, adds the load of follow-up acid making system, and the moisture in flue gas cannot balance and form the outer row of diluted acid needs, causes new waste discharge.
Summary of the invention
The present invention is that a kind of sulphur that uses is as the alkylation spent acid cracking technology of fuel.
Main technical schemes of the present invention: use sulphur as the alkylation spent acid cracking technology of fuel, it is characterized in that using sulphur to make fuel, there is provided the heat energy required for the cracking of alkylation spent acid, namely under the hot environment that produces in sulfur burning of alkylation spent acid, the technique of sulfuric acid is produced in cracking.
Described alkylation spent acid cracking technology, in comprising Waste Sulfuric Acid at high temperature cracking, waste heat boiler heat recuperation, closing acid-scrubbing cleaning, twice conversion, twice absorption and tail gas absorption operation etc., produces qualified sulfuric acid product.
Concrete steps: the Waste Sulfuric Acid carrying out alkylation unit enters spent acid sloptank, send into atomizing lance through vertical pump, spray into pyrolyzer after compressed air atomizing.Molten sulphur in molten sulfur sloptank sends into sulphur spray gun through liquid sulfur pump, after the atomization of sulphur spray gun, send into pyrolyzer, contact with the air after preheating, Thorough combustion produces a large amount of heat energy, make Waste Sulfuric Acid complete cracking under the high temperature of 1000-1100 DEG C, generate SO
2and H
2o.Containing SO
2flue gas, through waste heat boiler, air preheater, enters the cooling of dynamic wave scrubber adiabatic humidification after cooling, then through stuffing washing tower, temperature is down to less than 40 DEG C, through two-stage electrostatic precipitator removing acid mist, after supplementing a certain amount of air, enter drying tower, the moisture in removing flue gas, through SO
2convertor sent into by gas blower, enters a suction tower and once absorbs, then enter convertor and carry out twice transformation after once transforming, then enters two suction towers and carry out double absorption.Absorb SO
3after the vitriol oil add water and regulate acid dense to 98%, send into finished acid basin.Go out the SO of two suction tower tail gas more than the further absorption of residual of tail gas absorber
2, guarantee tail gas qualified discharge.
Compared with the geseous fuel such as the Sweet natural gas generally used, liquefied gas, converting fuel is product by the alkylation spent acid cracking technology that sulphur makes fuel, greatly reduces plant running cost; Avoid the H because gas fuel combustion produces
2o and the outer row's diluted acid formed, avoid new waste discharge; In addition, the CO because gas fuel combustion produces is also reduced
2discharge.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the embodiment of the present invention.
In figure, 1-pyrolyzer, 2-waste heat boiler, 3-air preheater, 4-dynamic wave scrubber, 5-header tank, 6-packing tower, 7-one-level electrostatic precipitator, 8-secondary electrostatic precipitator, 9-molten sulfur sloptank, 10-spent acid sloptank, 11-air blower, 12-dynamic wave diluted acid recycle pump, 13-tail inhales tower, 14-tail inhales tower recycle pump, 15-second absorption tower, 16-packing tower diluted acid recycle pump, 17-first absorption tower, 18-drying tower, 19-main blower, 20-the IIIth interchanger, 21-the Ith interchanger, 22-mono-section of electric furnace, 23-convertor, 24-tetra-sections of electric furnaces, 25-the IIth interchanger, 26-the IVth interchanger, 27-the Vth interchanger, 28-lye vat, 29-finished acid tank, 30-finished acid sloptank, 31-bis-inhales circulation groove, 32-mono-inhales circulation groove, 33-dry recycle groove.
Embodiment
Below in conjunction with embodiment and accompanying drawing, the invention will be further described.
Embodiment: as shown in Figure 1, the present embodiment uses sulphur to comprise as the alkylation spent acid cracking technology flow process of fuel:
Liquid-state sulfur in molten sulfur sloptank (9) sprays into pyrolyzer (1) and burns together with the air (~ 220 DEG C) after air preheater (3) preheating, and in-furnace temperature controls at about 1000-1100 DEG C.The Waste Sulfuric Acid come from spent acid sloptank (10) sprays into Pintsch process spent acid pyrolyzer (1).From pyrolyzer (1) SO of 1000-1100 DEG C out
2furnace gas, after moving heat by waste heat boiler (2), temperature drops to about about 450 DEG C, then enters air preheater (3), and after furnace gas temperature is reduced to about 300 DEG C by 450 DEG C, furnace gas enters purification section dynamic wave scrubber (4).Simultaneously with enter air that stove liquid-state sulfur react after air preheater (3) preheating, temperature rises to about 220 DEG C, enters stove and reacts, get up to reduce the consumption of liquid-state sulfur like this by the Energy harvesting in system together with liquid-state sulfur.
Go out the furnace gas of cracking workshop section, temperature about 300 DEG C, first enters dynamic wave scrubber (4), contacted with the diluted acid of spray by reverse jet tube, moisture in diluted acid is rapidly evaporated, and simultaneously furnace gas temperature also decreases (adiabatic humidification process), and in furnace gas, the impurity such as most dust is removed.Furnace gas after adiabatic humidification enters packing tower (6) to carry out washing, cooling, moisture in further removing furnace gas, furnace gas temperature is down to less than 38 DEG C, enter one-level electrostatic precipitator (7), secondary electrostatic precipitator (8) acid mist that removing is remaining further successively, make acid mist <0.005g/m in furnace gas
3, deliver to drying tower (18).
Furnace gas after purification with 93% sour sprinkle, makes moisture in furnace gas be down to 0.1 gram/mark rice in drying tower (18)
3below, then acid mist is removed by fiber mist eliminator, through main blower (19) pressurization after enter interchanger III (20), interchanger I(21 successively) shell side, respectively with the pyrolytic conversion gas heat exchange that exports from convertor (23) three sections and one section of catalyst layer in pipe, making interchanger I(21) shell-side outlet furnace temperature reaches about 420 DEG C, enter convertor (23) sections, under vanadium catalyst effect, SO
2be oxidized to SO
3and after releasing a large amount of heat, enter interchanger I(21) tube side heat exchange to 470 DEG C about, enter convertor (23) two sections of catalyst layers and proceed reaction, about reacted pyrolytic conversion gas enters the intraductal heat exchange to 440 DEG C of heat exchanger II (25), enter three sections of catalyst layers and continue reaction, three sections of conversion rate at tube exits reach more than 95%, and reforming gas enters interchanger III (20) tube side, below heat exchange to 170 DEG C, enter the first absorption tower (17) and carry out first time absorption, absorbed SO
3gas enter interchanger V (27) successively, the shell side of heat exchanger II (25), interior from five sections and the heat exchange of two sections of catalyst layer pyrolytic conversion gas with pipe respectively, heat exchanger II (25) shell-side outlet temperature is made to reach about 420 DEG C, enter convertor (23) four sections of catalyst layers and carry out second time conversion, about reacted pyrolytic conversion gas enters the intraductal heat exchange to 410 DEG C of interchanger IV (26), enter five stage catalyst layer and continue reaction, five sections of outlet total conversion rates reach more than 99.7%, reforming gas is through about the tube side heat exchange to 140 DEG C of interchanger V (27), enter second absorption tower (15) carry out second time absorb after, enter in tail gas absorber (13) with 10% sodium hydroxide solution absorption SO wherein
2and SO
3, the tail gas after absorbing passes through smoke stack emission.
In order to keep the balance of each tower recycle acid concentration, the 93% acid string that drying tower (18) generates is to the first absorption tower (17), simultaneously go here and there back corresponding 98% acid by absorption tower (17,15) to drying tower (18), make drying tower (18) recycle system keep balance that is sour dense and water.Corresponding 98% acid of absorption tower (17,15) output, sends into finished acid sloptank (30), then is pumped into finished acid tank (29) by sloptank acid.
Claims (3)
1. use sulphur as an alkylation spent acid cracking technology for fuel, it is characterized in that using sulphur to make fuel, the heat energy required for the cracking of alkylation spent acid is provided, be i.e. the technique of cracking production sulfuric acid under the hot environment that produces in sulfur burning of alkylation spent acid.
2. alkylation spent acid cracking technology according to claim 1, is characterized in that comprising Waste Sulfuric Acid at high temperature cracking, waste heat boiler heat recuperation, closing acid-scrubbing cleaning, twice conversion, twice absorption and tail gas absorption operation.
3. alkylation spent acid cracking technology according to claim 1, it is characterized in that: the Waste Sulfuric Acid carrying out alkylation unit enters spent acid sloptank, atomizing lance is sent into through vertical pump, spray into pyrolyzer after compressed air atomizing, the Molten sulphur in molten sulfur sloptank sends into sulphur spray gun through liquid sulfur pump, after the atomization of sulphur spray gun, send into pyrolyzer, contact with the air after preheating, Thorough combustion produces a large amount of heat energy, makes Waste Sulfuric Acid complete cracking under the high temperature of 1000-1100 DEG C, generates SO
2and H
2o, containing SO
2flue gas, through waste heat boiler, air preheater, enters the cooling of dynamic wave scrubber adiabatic humidification after cooling, then through stuffing washing tower, temperature is down to less than 40 DEG C, through two-stage electrostatic precipitator removing acid mist, after supplementing air, enter drying tower, the moisture in removing flue gas, through SO
2convertor sent into by gas blower, enters a suction tower and once absorbs, then enter convertor and carry out twice transformation after once transforming, then enters two suction towers and carry out double absorption; Absorb SO
3after the vitriol oil add water and regulate acid dense to 98%, send into finished acid basin, go out the SO of two suction tower tail gas more than the further absorption of residual of tail gas absorber
2, tail gas qualified discharge.
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|---|---|---|---|
| CN201410526789.4A CN105480953A (en) | 2014-10-09 | 2014-10-09 | Alkylated waste acid cracking technology adopting sulphur as fuel |
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| CN201410526789.4A CN105480953A (en) | 2014-10-09 | 2014-10-09 | Alkylated waste acid cracking technology adopting sulphur as fuel |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106379868A (en) * | 2016-08-30 | 2017-02-08 | 南京海陆化工科技有限公司 | Method for preparing sulfuric acid by burning sulfur-containing waste liquid |
| CN106744722A (en) * | 2016-12-27 | 2017-05-31 | 江苏科瑞工程设计有限公司 | A kind of regeneration technology of acetylene cleaning Waste Sulfuric Acid |
| CN106927432A (en) * | 2017-03-23 | 2017-07-07 | 贵州诺威施生物工程有限公司 | Heating system and its application in gas washing in SA production |
| CN107311117A (en) * | 2017-06-20 | 2017-11-03 | 中国石油集团东北炼化工程有限公司葫芦岛设计院 | Sulphur recovery and alkylation spent acid Combined Treatment process for cleanly preparing and device |
| CN107934920A (en) * | 2017-11-29 | 2018-04-20 | 中石化南京工程有限公司 | A kind of device of Waste Sulfuric Acid and hydrogen sulfide waste gas integrated treatment |
| CN107954403A (en) * | 2018-01-08 | 2018-04-24 | 上海乐谦工程科技有限公司 | A kind of resource-conserving spent acid treatment process and device |
| CN109882864A (en) * | 2019-03-26 | 2019-06-14 | 刘兵 | A kind of technique and system of the coproduction relieving haperacidity of dangerous waste incineration disposal |
| CN110240123A (en) * | 2019-06-27 | 2019-09-17 | 山东鲁北企业集团总公司 | A method of utilizing rotary kiln incineration sulfur waste sulphur and sulphur-bearing waste solution Sulphuric acid |
| CN110683520A (en) * | 2018-07-06 | 2020-01-14 | 中国石油化工股份有限公司 | Process for preparing sulfuric acid by regenerating low-concentration dilute waste sulfuric acid |
| CN111747382A (en) * | 2020-05-25 | 2020-10-09 | 惠州宇新化工有限责任公司 | Method and system for concentrating and recycling dilute acid by using alkylation waste acid recycling device |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61251502A (en) * | 1985-04-30 | 1986-11-08 | Jgc Corp | Treatment of waste sulfuric acid |
| CN1751984A (en) * | 2004-09-20 | 2006-03-29 | 中国石油天然气股份有限公司 | Treatment technology of producing sulfuric acid from alkylated spent sulfuric acid through high temperature decomposition |
| US20100254889A1 (en) * | 2007-11-07 | 2010-10-07 | Basf Se | Method for producing sulfuric acid |
| CN203382501U (en) * | 2013-06-19 | 2014-01-08 | 中国石油化工股份有限公司 | Spray gun applied to waste-sulfuric-acid-pyrolysis sulfuric acid preparation |
-
2014
- 2014-10-09 CN CN201410526789.4A patent/CN105480953A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS61251502A (en) * | 1985-04-30 | 1986-11-08 | Jgc Corp | Treatment of waste sulfuric acid |
| CN1751984A (en) * | 2004-09-20 | 2006-03-29 | 中国石油天然气股份有限公司 | Treatment technology of producing sulfuric acid from alkylated spent sulfuric acid through high temperature decomposition |
| US20100254889A1 (en) * | 2007-11-07 | 2010-10-07 | Basf Se | Method for producing sulfuric acid |
| CN203382501U (en) * | 2013-06-19 | 2014-01-08 | 中国石油化工股份有限公司 | Spray gun applied to waste-sulfuric-acid-pyrolysis sulfuric acid preparation |
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106379868A (en) * | 2016-08-30 | 2017-02-08 | 南京海陆化工科技有限公司 | Method for preparing sulfuric acid by burning sulfur-containing waste liquid |
| CN106744722B (en) * | 2016-12-27 | 2019-03-29 | 江苏科瑞工程设计有限公司 | A kind of regeneration technology of acetylene cleaning Waste Sulfuric Acid |
| CN106744722A (en) * | 2016-12-27 | 2017-05-31 | 江苏科瑞工程设计有限公司 | A kind of regeneration technology of acetylene cleaning Waste Sulfuric Acid |
| CN106927432A (en) * | 2017-03-23 | 2017-07-07 | 贵州诺威施生物工程有限公司 | Heating system and its application in gas washing in SA production |
| CN107311117A (en) * | 2017-06-20 | 2017-11-03 | 中国石油集团东北炼化工程有限公司葫芦岛设计院 | Sulphur recovery and alkylation spent acid Combined Treatment process for cleanly preparing and device |
| CN107311117B (en) * | 2017-06-20 | 2024-01-12 | 中国石油集团东北炼化工程有限公司葫芦岛设计院 | Clean production process and device for combined treatment of sulfur recovery and alkylated waste acid |
| CN107934920A (en) * | 2017-11-29 | 2018-04-20 | 中石化南京工程有限公司 | A kind of device of Waste Sulfuric Acid and hydrogen sulfide waste gas integrated treatment |
| CN107954403A (en) * | 2018-01-08 | 2018-04-24 | 上海乐谦工程科技有限公司 | A kind of resource-conserving spent acid treatment process and device |
| CN107954403B (en) * | 2018-01-08 | 2024-03-12 | 上海乐谦工程科技有限公司 | Resource-saving waste acid treatment process and device |
| CN110683520A (en) * | 2018-07-06 | 2020-01-14 | 中国石油化工股份有限公司 | Process for preparing sulfuric acid by regenerating low-concentration dilute waste sulfuric acid |
| CN109882864A (en) * | 2019-03-26 | 2019-06-14 | 刘兵 | A kind of technique and system of the coproduction relieving haperacidity of dangerous waste incineration disposal |
| CN110240123A (en) * | 2019-06-27 | 2019-09-17 | 山东鲁北企业集团总公司 | A method of utilizing rotary kiln incineration sulfur waste sulphur and sulphur-bearing waste solution Sulphuric acid |
| CN110240123B (en) * | 2019-06-27 | 2021-06-22 | 山东鲁北企业集团总公司 | Method for preparing sulfuric acid by using rotary kiln incineration waste sulfur and sulfur-containing waste liquid |
| CN111747382A (en) * | 2020-05-25 | 2020-10-09 | 惠州宇新化工有限责任公司 | Method and system for concentrating and recycling dilute acid by using alkylation waste acid recycling device |
| CN111747382B (en) * | 2020-05-25 | 2022-04-15 | 惠州宇新化工有限责任公司 | Method and system for concentrating and recycling dilute acid by using alkylation waste acid recycling device |
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