CN101481095A - Process for recovering and utilizing sulfuric acid manufacture energy - Google Patents
Process for recovering and utilizing sulfuric acid manufacture energy Download PDFInfo
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- CN101481095A CN101481095A CNA200910028269XA CN200910028269A CN101481095A CN 101481095 A CN101481095 A CN 101481095A CN A200910028269X A CNA200910028269X A CN A200910028269XA CN 200910028269 A CN200910028269 A CN 200910028269A CN 101481095 A CN101481095 A CN 101481095A
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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
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- 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
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Abstract
The invention discloses a process for recycling energy in the sulfuric acid manufacture. The invention adopts the process gas containing SO2 generated by burning sulfur in the sulfuric acid manufacture and the heat released by oxidizing SO2 in the process gas to SO3 as a heat source to produce high pressure superheated steam at a pressure between 4.9 and 10MPa, and adopts the heat generated by SO3 absorbed by the sulfuric acid as the heat source to produce low pressure saturated steam less than or equal to 1.6MPa. The produced high pressure superheated steam and the produced low pressure saturated steam are sent to a turbo unit to generate electricity or for supply. The steam producing ability by producing every ton of sulfuric acid is increased to about 1.7t from the traditional 1.2t by adopting the process. If all the steam is completely applied to generate electricity, the electricity generating ability for producing every ton of acid is increased to about 380kW*h from traditional 260kW*h, and the electricity generating ability is improved by about 46 percent.
Description
Technical field
The invention belongs to chemical field, relate to the technology of a kind of gas washing in SA production energy recovery and utilization.
Background technology
The traditional method of China's gas washing in SA production energy recovery is the SO that utilizes sulfur burning to produce
2And SO
2Be oxidized to SO
3The heat that is discharged produces middle pressure steam, rather than produces high pressure steam, and the high pressure steam of same tonnage is higher by about 10% than the generated energy of middle pressure steam; SO
3Substantially do not had to reclaim by sulfuric acid absorption institute liberated heat.1 ton of sulfuric acid by-product of every production middle pressure steam is about 1.2 tons.If these steam are used for generating electricity, 1 ton of sulfuric acid of every production can generate electricity about 260kWh.And utilizing the present invention, 1 ton of sulfuric acid of every production can about 1.2 tons of by-product high-pressure steams and about 0.5 ton of low-pressure steam.If these steam all are used for generating, 1 ton of sulfuric acid of every production can generate electricity about 380kWh.
Summary of the invention
The purpose of this invention is to provide a kind of sulfuric acid energy recycle technology, utilize the chemical reaction heat of gas washing in SA production produce high pressure superheated steam and low-pressure saturated steam outer for or be used for generating, generating capacity is compared with traditional method, and one ton of sulfuric acid generating capacity of every production improves 46% (about about 120kWh).
A kind ofly utilize sulfur burning to generate for gas washing in SA production to contain SO
2SO in (sulfur dioxide) process gas and this process gas
2Be oxidized to SO
3The heat that (sulfur trioxide) discharges is produced the high pressure superheated steam of 4.9～10MPa as thermal source; And utilize SO
3The heat that is produced when being generated higher concentration sulfuric acid by sulfuric acid absorption as thermal source production smaller or equal to the 1.6MPa low-pressure saturated steam; And the high pressure superheated steam of gained and low-pressure saturated steam sent into Turbo-generator Set generating or outer the confession.
The heat that is discharged with the burning of high-duty boiler recovery sulphur produces high-pressure saturated steam, reclaims SO with cryogenic high pressure superheater and/or high temperature and high pressure steam superheater
2Be oxidized to SO
3The heat heating high-pressure saturation steam that is discharged becomes high pressure superheated steam and reclaims SO with economizer
2Be oxidized to SO
3The heat heating high-pressure oiler feed that is discharged becomes high pressure superheated steam.Contain SO
2SO in the process gas
2Be oxidized to SO
3Rear generation contains SO
3Process gas, the SO in this process gas
3By release heat after the sulfuric acid absorption sulfuric acid temperature is raise; Reclaim SO with low-pressure boiler again
3Generated the heat generation low-pressure saturated steam that higher concentration sulfuric acid is discharged by sulfuric acid absorption.But thereby make 1.2 tons of left and right sides high pressure superheated steam of 1 ton of sulfuric acid by-product of the every generation of acid production with sulphur process system and 0.5 ton of left and right sides low-pressure saturated steam, as with these high pressure superheated steam and low-pressure saturated steam all for generating, then the generating capacity of 1 ton of acid of every production can be brought up to about 380kWh about the 260kWh by conventional method.Its typical flow synoptic diagram is seen Fig. 1 and Fig. 2.
With (high temperature (800 ℃～1200 ℃) that the burning of 4.9～10.0MPa) high-duty boiler recovery sulphur produces contains SO
2The heat of process gas produces high-pressure saturated steam, reclaims SO with one or more economizer
2Be oxidized to SO
3The heat heating boiler feedwater that is discharged is used the cryogenic high pressure superheater or/and the high temperature and high pressure steam superheater reclaims SO
2Be oxidized to SO
3The heat heating high-pressure saturation steam that is discharged becomes high pressure superheated steam, makes 1.2 tons of left and right sides high pressure superheated steam of 1 ton of sulfuric acid by-product of every generation.
To contain SO
3Process gas from bottom to top by first absorber, can establish one deck or two-layer filler or multi-layer sheet in first absorber, gas is that 98%～99.5% the concentrated sulfuric acid fully contacts SO with the concentration that sprays into from above in first absorber
3Absorbed simultaneously release heat by the concentrated sulfuric acid, absorb SO
3The concentration of rear sulfuric acid and temperature all can raise, its concentration increases by 0.4%～1%, temperature increases by 10 ℃～30 ℃, the concentrated sulfuric acid that again concentration and temperature is all raise is sent into the low-pressure boiler heated feed water and is produced low-pressure saturated steam smaller or equal to 1.6MPa, concentration descended and enters absorber after 0.4%～1% and recycle after the concentrated sulfuric acid part of coming out from low-pressure boiler and water mixed, and another part concentrated sulfuric acid is sent after boiler feedwater is cooled off.But 1 ton of sulfuric acid by-product of every production is smaller or equal to about 0.5 ton of 1.6MPa low-pressure saturated steam in this way.
The high pressure superheated steam that system produces and low-pressure saturated steam can all for generating, also can partly be used for power generation part steam and supply outward according to actual needs.Specifically be to realize by condensing, filling condensing, the condensing that draws gas, draw gas back pressure type or back pressure type steam turbine generating set.The vapor pressure of outer confession can be decided as required.
General SO
2Be oxidized to SO
3It is V that employed catalyst can adopt active ingredient
2O
5The conventional catalyst of (vanadic anhydride), percentage composition of the present invention is weight percentage.
With the technical process of " 3+1 " double conversion and double absorption acid production with sulphur is example, establishes high-duty boiler (4.9MPa～10.0MPa), will contain SO in the sulfur furnace outlet
2High-temperature technology gas drop to about 400 ℃～460 ℃ from 800 ℃～1200 ℃, boiler heat absorption back produces high-pressure saturated steam; Establish the high temperature and high pressure steam superheater with 600 ℃ ± 30 ℃ the SO that contains in convertor I section outlet
3The technology reformed gas be cooled to 440 ℃ ± 30 ℃; Before first resorber, establish economizer 2, will be from the SO that contains of hot and cold heat exchanger
3Process gas be cooled to enter first resorber about 130 ℃～210 ℃; Before second resorber, establish cryogenic high pressure vapor superheater and economizer 1, will contain a small amount of SO
3Process gas enter second resorber again after being cooled to 120 ℃～200 ℃ by 450 ℃ ± 20 ℃.
Utilize aforesaid device can be with heat and the SO that sulfur burning discharged
2Be oxidized to SO
3The heat recuperation that is discharged produces high pressure superheated steam, and then high pressure superheated steam is sent into steam turbine power generation.And through the economizer 2 cooled SO that contain
3Process gas be admitted to the first resorber bottom, the vitriol oil with 98%～99.5% sprays into from the first resorber top.The concentrated sulfuric acid fully contacts with process gas and absorbs SO
3Release heat, sulfuric acid concentration and temperature further improve, and absorb SO
3Sulfuric acid concentration usually be controlled at below 99.9%, temperature is controlled at below 225 ℃.First resorber can be one deck or two-layer filler or multi-ply wood, absorbs SO
3After high-temperature concentrated sulfuric acid be admitted to low pressure boiler again, the heat of concentrated acid is passed to oiler feed produce low-pressure saturated steam, the concentrated acid temperature reduces, and the acid after the sulfuric acid that adds water or low concentration then in the vitriol oil reduces concentration sprays into first resorber again and recycles.Make in this way and can reclaim SO
3Absorb the heat that is discharged and produce low-pressure steam, 1 ton of sulfuric acid of every production can be produced about 0.5 ton of low-pressure saturated steam.Low-pressure steam can fill into steam turbine power generation directly outward after also can directly filling into or heat.See Fig. 1 and Fig. 2.
So-called " 3+1 " refers to SO with double-absorption
2Process gas enters first absorber after through 3 catalyzed conversions (namely passing through first three section of converter) and carries out absorption first time (namely turns to a suction); Then carry out again entering again behind 1 catalyzed conversion (being the 4th section of converter) second absorber and carry out absorbing the second time (being double conversion double absorption).
Beneficial effect of the present invention compared with the prior art: by on the sulfuric acid production process circuit, heat recovery equipments such as high and low pressure boiler, HP steam superheater, high-pressure economizer, feedwater heating apparatus being set (wherein, it is 200620125513.6 disclosed vapour generators that low pressure boiler can adopt application number, miscellaneous equipment all can adopt conventional equipment), and these equipment waste heat that reclaim(ed) sulfuric acid produces that is organically combined produced high pressure and low-pressure steam, utilize 1 ton of vitriolic of the every production of this technology ability of steaming to bring up to about 1.7t from traditional 1.2t.As with these steam all for the generating, then the generating capacity of 1 ton of acid of every production is from bringing up to about 380kWh by traditional 260kWh, generating capacity improves about 46%.
Description of drawings
Fig. 1, gas washing in SA production energy recovery and utilize technical process 1 synoptic diagram.
Among the figure, 1 is sulfur furnace, and 2 is high-pressure boiler, 3 is converter, and 4 is the high temperature and high pressure steam superheater, and 5 is hot heat exchanger, 6 is hot and cold heat exchanger, and 7 is first absorber, and 8-1 is economizer, 8-2 is economizer, 9 is second absorber, and 10 is the cryogenic high pressure superheater, and 11 is low-pressure boiler, 12 is steam turbine, 13 is generator, and 14 is condenser, and 15 is oxygen-eliminating device, 16 is acid circulating pump, 17 is the low pressure feed water pump, and 18 is high pressure water pump, and 19-1 is feed-water heater 1,19-2 is that feed- water heater 2,20 is blender; F1 is Molten sulphur, and F2 is dry air, and F3-1 is high-temperature furnace gas, F3-2 is I section outlet process gas, and F3-3 is II section outlet process gas, and F3-4 is III section outlet process gas, F3-5 is first absorber outlet process gas, and F3-6 is IV section outlet process gas, and F4 is dilution water or diluted acid, F5 is low-pressure steam, F6 is desalted water, and F7-1 is first absorber outlet sulfuric acid, and F7-2 is recycle sulfuric acid, F7-3 is outer for sulfuric acid, and F8 is cooling water.
Fig. 2, gas washing in SA production energy recovery and utilize technical process 2 synoptic diagram.
Among the figure, 1 is sulfur furnace, and 2 is high-pressure boiler, 3 is converter, and 4 is the high temperature and high pressure steam superheater, and 5 is hot heat exchanger, 6 is hot and cold heat exchanger, and 7 is first absorber, and 8-1 is economizer, 8-2 is economizer, 9 is second absorber, and 10 is the cryogenic high pressure superheater, and 11 is low-pressure boiler, 12 is steam turbine, 13 is generator, and 14 is condenser, and 15 is oxygen-eliminating device, 16 is acid circulating pump, 17 is the low pressure feed water pump, and 18 is high pressure water pump, and 19-1 is feed-water heater 1,19-2 is that feed- water heater 2,20 is blender; F1 is Molten sulphur, and F2 is dry air, and F3-1 is high-temperature furnace gas, F3-2 is I section outlet process gas, and F3-3 is II section outlet process gas, and F3-4 is III section outlet process gas, F3-5 is first absorber outlet process gas, and F3-6 is IV section outlet process gas, and F4 is dilution water or diluted acid, F5 is low-pressure steam, F6 is desalted water, and F7-1 is first absorber outlet sulfuric acid, and F7-2 is recycle sulfuric acid, F7-3 is outer for sulfuric acid, and F8 is cooling water.
Embodiment
The present invention is applicable to newly-built or modernizes and expands the existing factory sulphur-burning sulphuric acid plant energy recycle.Produce 800000 tons of sulphur-burning sulphuric acid plants per year as example take " 3+1 " double-absorption, in conjunction with Fig. 1 the specific embodiment of the present invention done following explanation:
The technological process of process gas at first is described, Molten sulphur F1 and dry air F2 burn to produce in sulfur furnace 1 and contain SO
2High-temperature technology gas F3-1 (800 ℃～1200 ℃ of temperature), temperature dropped to about 430 ℃ ± 30 ℃ after process gas F3-1 entered high-pressure boiler 2 heating furnace water generates high-pressure saturated steams; Process gas F3-1 after the cooling enters the I section entrance of converter 3, and process gas is in I section catalyst V
2O
5Effect under part SO
2Be oxidized into SO
3And the release amount of heat, temperature is increased to 600 ℃ ± 30 ℃ the SO that contains
3Process gas F3-2 enter high temperature and high pressure steam superheater 4, heating contains SO from the high steam of cryogenic high pressure superheater 10
3Process gas F3-2 temperature be down to the II section entrance that enters converter 3 after 440 ℃ ± 30 ℃, SO in the process gas
2Catalyst V in the II section
2O
5Effect under to continue partial oxidation be SO
3And release heat, temperature is increased to 500 ℃ ± 30 ℃ to be become process gas F3-3 and enters in the hot heat exchanger 5, heating is through the process gas F3-5 of first absorber 7 outlet of hot and cold heat exchanger 6 preheatings, enters the III section entrance of converter 3 behind the drop in temperature to 440 ℃ ± 40 ℃, the SO in the process gas
2Catalyst V in the III section
2O
5Effect under to continue partial oxidation be SO
3And release heat, temperature is increased to 450 ℃ ± 40 ℃ to be become process gas F3-4 enter successively hot and cold heat exchanger 6 and the economizer 8-2 after process gas F3-5 that heating comes out from first absorber 7 and the boiler feedwater drop in temperature to 170 ℃ ± 40 ℃ after the III section is come out, enter first absorber, 7 bottoms, will contain SO
3Process gas F3-4 from bottom to top with 98%～99.5% concentrated sulfuric acid counter current contacting from first absorber, 7 tops, the SO in the process gas
3Absorbed by the concentrated sulfuric acid, temperature is down to about 80 ℃ to be become process gas F3-5 and comes out from first absorber, 7 tops, is increased to the IV section that 420 ℃ ± 20 ℃ process gas F3-5 enters converter 3 through hot and cold heat exchanger 6 and hot heat exchanger 5 temperature after heating; SO in the process gas
2Catalyst V in the IV of converter 3 section
2O
5Effect under continue to be oxidized to SO
3Release heat, temperature is increased to 450 ℃ ± 20 ℃ process gas F3-6 and enters successively respectively heating high-pressure saturated vapor and heating boiler feedwater low temperature superheater 10 and the economizer 8-1 after the IV section is come out, after being reduced to 160 ℃ ± 40 ℃, the process gas temperature enters second absorber, 9 bottoms, make from bottom to top and 98%～98.5% concentrated sulfuric acid counter current contacting from second absorber, 9 tops the SO in the process gas
3Absorbed by the concentrated sulfuric acid, temperature is down to about 70 ℃ and is entered atmosphere by chimney.
Next illustrates the vitriolic technical process, and 98%～99.5% sulfuric acid is sprayed into by first resorber, 7 tops, establishes multi-ply wood in first resorber 7, sulfuric acid in tower from top to bottom with from the process gas counter current contact at the bottom of the tower, the SO in the absorption technique gas
3After, concentration raises 0.4%～1.0%, and temperature raises 10 ℃～30 ℃, according to SO
3Concentration is controlled the concentration of first resorber, 7 outlet vitriol oil F7-1 below 99.9%, and temperature is below 225 ℃; Vitriol oil F7-1 sour temperature drop after acid circulating pump 16 is sent into the feedwater of low pressure boiler 11 heating boilers is low, the vitriol oil after the cooling is divided into two portions, wherein most of vitriol oil F7-2 enters and adds water or dilute sulphuric acid F4 in the mixing tank 20 to regulate concentration be to enter that circulation absorbs in first resorber 7 after 98～99.5%, temperature is reduced to about 70 ℃ sub-fraction vitriol oil F7-3 heats de-salted water in feedwater heating apparatus 19-2 heating low pressure boiler feedwater and feedwater heating apparatus 19-1 after, and the vitriol oil F7-3 after the cooling supplies outward as product.
The technical process of steam and water is described once more, de-salted water F6 carries out deoxygenation by entering deoxygenator 15 after the vitriol oil F7-3 heating in feedwater heating apparatus 19-1, deaerated water is sent into the low-temperature zone of economizer 8-1 successively after high pressure water feeding pump for boiler 18 pressurizations, heat with process gas F3-4 and F3-6 respectively in economizer 8-2 and the economizer 8-1 high temperature section, oiler feed after the intensification is sent into the heat that absorbs high-temperature technology gas F3-1 in the high-duty boiler 2 and is gasified, produce high pressure 4.9MPa～10MPa saturation steam, high-pressure saturated steam produces 120t/h left and right sides high pressure superheated steam with process gas F3-6 and the overheated back of F3-2 respectively through cryogenic high pressure superheater 10 and High Temperature High Pressure superheater 4, and high pressure superheated steam enters and drives turbine driven set in the steam turbine 12 and generate electricity; Another part deaerated water in the deoxygenator 15 is sent into feedwater heating apparatus 19-2 earlier through low pressure boiler service pump 17 and is heated with the vitriol oil, then enter in the low pressure boiler 11 heat that absorbs high-temperature concentrated sulfuric acid F7-1 and gasify, produce low-pressure saturated steam (1.0MPa) approximately to about the 50t/h, low-pressure saturated steam enters the generating of counter pressure turbine filling mouth driving steam turbine generating set; The high pressure superheated steam and the low-pressure saturated steam that enter steam turbine 12 can generate electricity about 38000kW altogether, and the exhaust steam of steam turbine outlet enters in the deoxygenator 15 after condenser 14 is condensed into condensed water and recycles.
It is example that gas washing in SA production adopts " 3+1 " double conversion and double absorption to produce 800000 tons of sulphur-burning sulphuric acid plants per year, and as shown in Figure 2, processing method that its high pressure superheated steam and low-pressure saturated steam are produced and principle are with embodiment 1.1.2 tons of left and right sides high pressure superheated steam of 1 ton of sulfuric acid by-product of every generation can be generated electricity about 30000kW by the condensing Turbo-generator Set, and 0.5 ton of left and right sides low-pressure saturated steam of by-product supplies outward.
Claims (6)
1. a gas washing in SA production energy recovery and utilize technology is characterized in that utilizing in gas washing in SA production sulfur burning to generate and contains SO
2SO in process gas and this process gas
2Be oxidized to SO
3The heat that is discharged is produced the high pressure superheated steam of 4.9～10MPa as thermal source; Utilize SO
3By heat that sulfuric acid absorption produced as the low-pressure saturated steam of thermal source production smaller or equal to 1.6MPa; The high pressure superheated steam and the low-pressure saturated steam of gained are sent into turbine driven set generating or outer the confession.
2. gas washing in SA production energy recovery according to claim 1 and utilize technology is characterized in that it being that heat with the burning of high-duty boiler recovery sulphur is discharged produces high-pressure saturated steam, reclaims SO with cryogenic high pressure superheater and/or high temperature and high pressure steam superheater
2Be oxidized to SO
3The heat heating high-pressure saturation steam that is discharged becomes high pressure superheated steam, and reclaims SO with economizer
2Be oxidized to SO
3The heat heating high-pressure oiler feed that is discharged.
3. sulfuric acid manufacture energy recycle technology according to claim 1 is characterized in that containing SO
2SO in the process gas
2Be oxidized to SO
3Rear generation contains SO
3Process gas, the SO in this process gas
3By release heat after the sulfuric acid absorption, reclaim SO with low-pressure boiler again
3By the heat generation low-pressure saturated steam that sulfuric acid absorption discharged.
4. gas washing in SA production energy recovery according to claim 2 and utilize technology is characterized in that 800 ℃～1200 ℃ that high-duty boiler recovery sulphur burning with 4.9～10.0MPa generates contain SO
2The heat of process gas produces high-pressure saturated steam, reclaims SO with one or more economizer
2Be oxidized to SO
3The heat heating boiler feedwater that is discharged is used the cryogenic high pressure superheater or/and the high temperature and high pressure steam superheater reclaims SO
2Be oxidized to SO
3The heat heating high-pressure saturation steam that is discharged becomes high pressure superheated steam.
5. sulfuric acid manufacture energy recycle technology according to claim 3 is characterized in that and will contain SO
3Process gas from bottom to top by first absorber, establish one deck or two-layer filler or multi-layer sheet in first absorber, gas is that 98%～99.5% the concentrated sulfuric acid fully contacts SO with the concentration that sprays into from above in first absorber
3Absorbed simultaneously release heat by the concentrated sulfuric acid, absorb SO
3The concentration of rear sulfuric acid and temperature all can raise, and its concentration increases by 0.4%～1%, and temperature increases by 10 ℃～30 ℃, and the concentrated sulfuric acid that again concentration and temperature is all raise is sent into the low-pressure boiler heated feed water and produced low-pressure saturated steam smaller or equal to 1.6MPa.
6. sulfuric acid manufacture energy recycle technology according to claim 1 is characterized in that the high pressure superheated steam and the low-pressure saturated steam that produce all are used for generating for generating or part, and part is outer to be supplied; Wherein, generating is to realize by condensing, filling condensing, the condensing that draws gas, draw gas back pressure type or back pressure type steam turbine generating set.
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Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101706095B (en) * | 2009-09-02 | 2011-07-20 | 陈祥明 | Method for recovering acid making waste heat |
| CN102344348A (en) * | 2011-06-13 | 2012-02-08 | 苏州浩波科技股份有限公司 | Device for utilizing waste heat from production of liquid sulfur trioxide |
| CN102556982A (en) * | 2011-12-30 | 2012-07-11 | 江苏新宏大集团有限公司 | Low-temperature exhaust heat system for sulfuric acid recovering device and application of low-temperature exhaust heat system |
| CN103063039A (en) * | 2012-12-24 | 2013-04-24 | 刘立文 | Device and process of thermal cycling for producing sulfuric acid by using calcium sulfate |
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| CN104495757A (en) * | 2015-01-06 | 2015-04-08 | 东华工程科技股份有限公司 | System for removing low-temperature thermal energy generated during adsorption of SO3 from sulfuric acid production device |
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| US10272380B2 (en) | 2010-10-29 | 2019-04-30 | E I Du Pont De Nemours And Company | Regenerative recovery of sulfur dioxide from effluent gases |
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| CN101706095B (en) * | 2009-09-02 | 2011-07-20 | 陈祥明 | Method for recovering acid making waste heat |
| CN109019529B (en) * | 2010-01-20 | 2022-06-14 | 梅克斯公司 | Energy recovery in sulfuric acid production |
| CN109019529A (en) * | 2010-01-20 | 2018-12-18 | 梅克斯公司 | Energy regenerating in sulfuric acid preparation |
| US11185812B2 (en) | 2010-10-29 | 2021-11-30 | Mecs, Inc. | Regenerative recovery of sulfur dioxide from effluent gases |
| US10272380B2 (en) | 2010-10-29 | 2019-04-30 | E I Du Pont De Nemours And Company | Regenerative recovery of sulfur dioxide from effluent gases |
| CN102344348A (en) * | 2011-06-13 | 2012-02-08 | 苏州浩波科技股份有限公司 | Device for utilizing waste heat from production of liquid sulfur trioxide |
| CN102556982A (en) * | 2011-12-30 | 2012-07-11 | 江苏新宏大集团有限公司 | Low-temperature exhaust heat system for sulfuric acid recovering device and application of low-temperature exhaust heat system |
| CN102556982B (en) * | 2011-12-30 | 2015-04-22 | 凯密迪公司 | Low-temperature exhaust heat system for sulfuric acid recovering device and application of low-temperature exhaust heat system |
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