CN104495757A - System for removing low-temperature thermal energy generated during adsorption of SO3 from sulfuric acid production device - Google Patents
System for removing low-temperature thermal energy generated during adsorption of SO3 from sulfuric acid production device Download PDFInfo
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- CN104495757A CN104495757A CN201510004554.3A CN201510004554A CN104495757A CN 104495757 A CN104495757 A CN 104495757A CN 201510004554 A CN201510004554 A CN 201510004554A CN 104495757 A CN104495757 A CN 104495757A
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- Prior art keywords
- gas
- sulfuric acid
- acid
- absorption tower
- process gas
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Classifications
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
- C01B17/76—Preparation by contact processes
- C01B17/775—Liquid phase contacting processes or wet catalysis processes
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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
-
- 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 a system for removing low-temperature thermal energy generated during adsorption of SO3 from a sulfuric acid production device. High-concentration sulfuric acid is sprayed out of a spraying head of a tubular spraying absorber to fully contact a SO3 containing process gas obtained by converting once and absorb SO3 in the SO3 containing process gas to generate high-temperature concentrated sulfuric acid. The process gas coming out of an outlet on the lower part of the tubular spraying absorber is made to enter a gas-liquid separator, then the process gas is separated from the liquid and demisted by a demister which is arranged on the outlet of the gas-liquid separator, and the demisted process gas is made to enter a secondary absorption tower. After the residual SO3 in the process gas is absorbed by concentrated sulfuric acid in the secondary absorption tower and is demisted by a demister which is arranged on the top of the secondary absorption tower, the process gas is made to return to a conversion system and is converted for the second time.
Description
Technical field
The present invention relates to SO in sulfuric acid apparatus
3absorption system field, specifically SO in a kind of sulfuric acid apparatus
3absorb low-temperature heat energy recovery system.
Background technology
Production technology in sulfuric acid apparatus, the level that utilizes of energy-saving and emission-reduction, raising used heat is the target that sulfuric acid industry technician pursues always.Early stage gas washing in SA production technology focuses on and reclaims the combustion heat of high-temperature position and the conversion reaction heat energy of middle potential temperature, and industry worker has made great contribution in this regard, has promoted the flourish of sulfuric acid industry.But at SO
3absorb the energy recovery aspect generating sulfuric acid and produce, as reception SO
3the carrier of absorption reaction heat and the sulfuric acid heat of dilution, high-temperature concentrated sulfuric acid is for a long time always only for adding hot desalinized water, and its waste heat energy is all recycled water cooling and loses in vain.Along with appearance and the gradual perfection of Novel corrosion-resistant corrosion material, the temperature of the thermal barrier vitriol oil can be promoted greatly, makes being recycled in order to possibility of this part of low-temperature heat energy.Existing multiple different technology is applied to the recovery of this part heat energy at present.
summary of the inventionthe object of this invention is to provide SO in a kind of sulfuric acid apparatus
3absorb low-temperature heat energy recovery system, to realize vitriol oil atomization and and SO
3process gas fully contacts.
In order to achieve the above object, the technical solution adopted in the present invention is:
SO in sulfuric acid apparatus
3absorb low-temperature heat energy recovery system, it is characterized in that: comprise tubular type Jet absorber, be furnished with the gas-liquid separator of spraying cycle pump, waste heat boiler, diluter, boiler water-suppling heater, de-salted water preheater, two-level absorption tower, be furnished with secondary and absorb two-level absorption tower circulation acid tank, the secondary absorption cycle acid cooler of acid circulating pump
Described tubular type Jet absorber is made up of, from the SO that sulfuric acid apparatus conversion section is once converted mixing section and the atomizer be arranged in mixing section
3process gas enters in the mixing section of tubular type Jet absorber, and the sulfuric acid droplets sprayed in mixing section with atomizer in mixing section fully contacts, most of SO in process gas
3absorbed, produced high-temperature concentrated sulfuric acid;
Described gas-liquid separator is arranged on below tubular type Jet absorber, goes out the SO of tubular type Jet absorber
3process gas and high-temperature concentrated sulfuric acid enter gas-liquid separator, carry out after gas-liquid separation through gas-liquid separator, gas phase is left gas-liquid separator and is entered bottom two-level absorption tower, and the high-temperature concentrated sulfuric acid separated is stored in gas-liquid separator bottom, is sent to waste heat boiler after then being pressurizeed by spraying cycle pump;
Described two-level absorption tower is packing tower, and the vitriol oil is evenly distributed in filler by the acid trap in two-level absorption tower top, from packing layer from bottom to top in two-level absorption tower of the process gas of gas-liquid separator and vitriol oil counter current contact, and SO remaining in process gas
3absorbed by the vitriol oil, the lower tower acid gravity flow of two-level absorption tower enters two-level absorption tower circulation acid tank and keeps in, then is pumped to through secondary absorption cycle the acid trap going to two-level absorption tower top after the cooling of secondary absorption cycle acid cooler.The process gas going out two-level absorption tower top returns sulfuric acid apparatus conversion section and carries out twice transformation;
Described waste heat boiler reclaims low-temperature level waste heat in high-temperature concentrated sulfuric acid and produces low-pressure saturated steam, the vitriol oil after cooling delivers to the atomizer of tubular type Jet absorber again after sending into and regulating acid concentration in diluter, sprayed to mixing section by the atomizer of tubular type Jet absorber.Meanwhile, draw one concentrated acid after boiler water-suppling heater and de-salted water preheater recovery waste heat from waste heat boiler outlet, export as product acid.
SO in described sulfuric acid apparatus
3absorb low-temperature heat energy recovery system, it is characterized in that: 1 ~ 3 layer of atomizer is set in tubular type Jet absorber mixing section, the atomizer vitriol oil out and SO
3process gas fully contacts, and atomizer specific liquid rate is 100 ~ 200 t/(m
2h), tubular type Jet absorber mixing indoor air velocity is
8 ~ 15m/s.
SO in described sulfuric acid apparatus
3absorb low-temperature heat energy recovery system, it is characterized in that: gas-liquid separator gaseous phase outlet arranges mist eliminator and removes acid mist further.
SO in described sulfuric acid apparatus
3absorb low-temperature heat energy recovery system, it is characterized in that: in two-level absorption tower, gas velocity is 1.6 ~ 2.0m/s, liquid spraying density 20 ~ 25m
3/ (m
2h), packed height 3 ~ 4 meters.
Advantage of the present invention is:
(1) production equipment adopting the present invention to build, its processing unit is simple, and operation and maintenance costs is low, a reduced investment.
(2) adopt tubular type to spray and absorb flow process, reduce the resistance drop of process gas system, the load that can reduce sulfate system blower fan exports.
(3) gas-liquid separator and mist eliminator minimizing entrainment are set, alleviate the impact of tail gas on two-level absorption tower.
Accompanying drawing explanation
Fig. 1 is process flow diagram of the present invention.
Embodiment
Shown in Figure 1, SO in sulfuric acid apparatus
3absorb low-temperature heat energy recovery system, comprise tubular type Jet absorber 1, be furnished with the gas-liquid separator 2 of spraying cycle pump 7, waste heat boiler 8, diluter 9, boiler water-suppling heater 10, de-salted water preheater 11, two-level absorption tower 3, be furnished with two-level absorption tower circulation acid tank 4, secondary absorption cycle acid cooler 6 that secondary absorbs acid circulating pump 5;
Tubular type Jet absorber 1 is made up of, from the SO that sulfuric acid apparatus conversion section is once converted mixing section and the atomizer be arranged in mixing section
3process gas enters in the mixing section of tubular type Jet absorber 1, and the sulfuric acid droplets sprayed in mixing section with atomizer in mixing section fully contacts, most of SO in process gas
3absorbed, produced high-temperature concentrated sulfuric acid;
Gas-liquid separator 2 is arranged on below tubular type Jet absorber 1, goes out the SO of tubular type Jet absorber 1
3process gas and high-temperature concentrated sulfuric acid enter gas-liquid separator 2, after gas-liquid separator 2 carries out gas-liquid separation, process gas enters bottom two-level absorption tower 3 by gas-liquid separator 2 gaseous phase outlet, the high-temperature concentrated sulfuric acid separated is stored in gas-liquid separator 2 bottom, is sent to waste heat boiler 8 after then being pressurizeed by spraying cycle pump 7;
Two-level absorption tower 3 is packing tower, and the vitriol oil is evenly distributed in filler by the acid trap in two-level absorption tower 3 top, from packing layer from bottom to top in two-level absorption tower 3 of the process gas of gas-liquid separator 2 and vitriol oil counter current contact, and SO remaining in process gas
3absorbed by the vitriol oil, the lower tower acid gravity flow of two-level absorption tower 3 enters two-level absorption tower circulation acid tank 4 and keeps in, then delivers to after the cooling of secondary absorption cycle acid cooler 6 through secondary absorbent recirculation pump 5 and remove two-level absorption tower 3 top acid trap.The process gas going out two-level absorption tower 3 tower top returns sulfuric acid apparatus conversion section again and carries out twice transformation;
Waste heat boiler 8 reclaims low-temperature level waste heat in high-temperature concentrated sulfuric acid and produces low-pressure saturated steam, the vitriol oil after cooling delivers to the atomizer of tubular type Jet absorber 1 again after sending into and regulating concentration in diluter 9, sprayed to mixing section by the atomizer of tubular type Jet absorber 1.Meanwhile, export from waste heat boiler 8 and draw one concentrated acid after boiler water-suppling heater 10 and de-salted water preheater 11 recovery waste heat, export as product acid.
1 ~ 3 layer of atomizer is set in tubular type Jet absorber 1 mixing section, the atomizer vitriol oil out and SO
3process gas fully contacts, and atomizer specific liquid rate is 100 ~ 200 t/(m
2h), tubular type Jet absorber mixing indoor air velocity is
8 ~ 15m/s.
Gas-liquid separator 2 gaseous phase outlet arranges mist eliminator and removes acid mist further.
In two-level absorption tower 3, gas velocity is 1.6 ~ 2.0m/s, liquid spraying density 20 ~ 25m
3/ (m
2h), packed height 3 ~ 4 meters.
Embodiment 1: adopt 200,000 tons/year of sulphur-burning sulphuric acid plants of the present invention
From conversion section containing 6 ~ 10%SO
3process gas, enters from the top of tubular type Jet absorber in tubular type Jet absorber, and the vitriol oil sprayed with the atomizer being arranged on Jet absorber top contacts, the SO in process gas
3absorbed.Injector diameter is φ 1800mm, and virtual height is 4000mm.Entering the acid of tubular type Jet absorber densely controls 99.1% ~ 99.3%, and sour temperature control is at 170 DEG C ~ 185 DEG C.Go out the dense control 99.5 ~ 99.6% of Jet absorber acid, sour temperature control is at 195 DEG C ~ 210 DEG C.After the bottom process gas out of tube-type jet enters and carries out gas-liquid separation gas-liquid separator, process gas enters two-level absorption tower after the demist of gas-liquid separator gaseous phase outlet mist eliminator.Two-level absorption tower is packing tower, tower diameter phi 4000mm, effective tower height 13000mm.Process gas from bottom to top with from the 98% sulfuric acid counter current contact in packing layer under from tower top, the remaining SO in process gas
3absorbed, then after the demist of tower top mist eliminator, return conversion section from tower top carry out twice transformation.
The high-temperature concentrated sulfuric acid being stored in gas-liquid separator bottom is sent to waste heat boiler recovery waste heat after the pressurization of spraying cycle pump, produces the low-pressure saturated steam of 0.5 ~ 1.0MPa.Go out a waste heat boiler temperature ~ 180 DEG C vitriol oil and enter that the acid of thin up device thin up is dense send tubular type Jet absorber atomizer again to 99.1% ~ 99.3%.Absorb SO
3the unnecessary vitriol oil of rear generation is drawn from heat boiler outlet and is delivered to final absorption tower circulation acid tank or air drying cycle acid tank for the production of 98% sulfuric acid.
Embodiment 2: adopt 600,000 tons/year of sulphur-burning sulphuric acid plants of the present invention
From conversion section containing 6 ~ 10%SO
3process gas, enter from the top of tubular type Jet absorber in tubular type resorber, the vitriol oil sprayed with the atomizer be arranged in Jet absorber contacts, the SO in process gas
3absorbed.Injector diameter is φ 3000mm, and virtual height is 6000mm.Entering the acid of tubular type Jet absorber densely controls 99.1% ~ 99.3%, and sour temperature control is at 170 DEG C ~ 185 DEG C.Go out the dense control 99.5 ~ 99.6% of Jet absorber acid, sour temperature control is at 195 DEG C ~ 210 DEG C.Enter gas-liquid separator after gas-liquid separation from the bottom process gas out of tube-type jet, process gas enters two-level absorption tower after the demist of gas-liquid separator gaseous phase outlet mist eliminator.Two-level absorption tower is packing tower, tower diameter phi 6600mm, effective tower height 13000mm.Process gas from bottom to top with from the 98% sulfuric acid counter current contact in packing layer under from tower top, the remaining SO in process gas
3absorbed, then after the demist of tower top mist eliminator, return conversion section from tower top carry out twice transformation.
The high-temperature concentrated sulfuric acid being stored in gas-liquid separator bottom is sent to waste heat boiler recovery waste heat after the pressurization of spraying cycle pump, produces the low-pressure saturated steam of 0.5 ~ 1.0MPa.Go out a waste heat boiler temperature ~ 180 DEG C vitriol oil to enter the acid of thin up device thin up and densely after 99.1% ~ 99.3%, send tubular type Jet absorber atomizer, continue to absorb SO
3.Absorb SO
3the unnecessary vitriol oil of rear generation is drawn from heat boiler outlet and is delivered to final absorption tower circulation acid tank or air drying cycle acid tank for the production of 98% sulfuric acid.
Claims (4)
1. SO in sulfuric acid apparatus
3absorb low-temperature heat energy recovery system, it is characterized in that: comprise tubular type Jet absorber, be furnished with the gas-liquid separator of spraying cycle pump, waste heat boiler, diluter, boiler water-suppling heater, de-salted water preheater, two-level absorption tower, be furnished with two-level absorption tower circulation acid tank, secondary absorption cycle acid cooler that secondary absorbs acid circulating pump;
Described tubular type Jet absorber is made up of, from the SO that sulfuric acid apparatus conversion section is once converted mixing section and the atomizer be arranged in mixing section
3process gas enters in the mixing section of tubular type Jet absorber, and the sulfuric acid droplets sprayed in mixing section with atomizer in mixing section fully contacts, by most of SO in sulfuric acid droplets absorption technique gas
3, produce high-temperature concentrated sulfuric acid;
Described gas-liquid separator is arranged on below tubular type Jet absorber, goes out the SO of tubular type Jet absorber
3process gas and high-temperature concentrated sulfuric acid enter gas-liquid separator, carry out after gas-liquid separation through gas-liquid separator, gas phase is left gas-liquid separator and is entered bottom two-level absorption tower, and the high-temperature concentrated sulfuric acid separated is stored in gas-liquid separator bottom, is sent to waste heat boiler after then being pressurizeed by spraying cycle pump;
Described two-level absorption tower is packing tower, and the vitriol oil is evenly distributed in filler by the acid trap in two-level absorption tower top, from packing layer from bottom to top in two-level absorption tower of the process gas of gas-liquid separator and vitriol oil counter current contact, and SO remaining in process gas
3absorbed by the vitriol oil, the lower tower acid gravity flow of two-level absorption tower enters two-level absorption tower circulation acid tank and keeps in, then is pumped to through secondary absorption cycle the acid trap going to two-level absorption tower top after the cooling of secondary absorption cycle acid cooler;
The process gas going out two-level absorption tower top returns sulfuric acid apparatus conversion section and carries out twice transformation;
Described waste heat boiler reclaims low-temperature level waste heat in high-temperature concentrated sulfuric acid and produces low-pressure saturated steam, the vitriol oil after cooling delivers to the atomizer of tubular type Jet absorber again after sending into and regulating acid concentration in diluter, sprayed to mixing section by the atomizer of tubular type Jet absorber;
Meanwhile, draw one concentrated acid after boiler water-suppling heater and de-salted water preheater recovery waste heat from waste heat boiler outlet, export as product acid.
2. SO in sulfuric acid apparatus according to claim 1
3absorb low-temperature heat energy recovery system, it is characterized in that: 1 ~ 3 layer of atomizer is set in tubular type Jet absorber mixing section, the atomizer vitriol oil out and SO
3process gas fully contacts, and atomizer specific liquid rate is 100 ~ 200 t/(m
2h), tubular type Jet absorber mixing indoor air velocity is
8 ~ 15m/s.
3. SO in sulfuric acid apparatus according to claim 1
3absorb low-temperature heat energy recovery system, it is characterized in that: gas-liquid separator gaseous phase outlet arranges mist eliminator and removes acid mist further.
4. SO in sulfuric acid apparatus according to claim 1
3absorb low-temperature heat energy recovery system, it is characterized in that: in two-level absorption tower, gas velocity is 1.6 ~ 2.0m/s, liquid spraying density 20 ~ 25m
3/ (m
2h), packed height 3 ~ 4 meters.
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|---|---|---|---|
| CN201510004554.3A CN104495757B (en) | 2015-01-06 | 2015-01-06 | SO in sulfuric acid apparatus3absorb low-temperature heat energy recovery system |
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| CN201510004554.3A CN104495757B (en) | 2015-01-06 | 2015-01-06 | SO in sulfuric acid apparatus3absorb low-temperature heat energy recovery system |
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| CN104495757B CN104495757B (en) | 2016-09-28 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104229756A (en) * | 2013-06-18 | 2014-12-24 | 天津渤大硫酸工业有限公司 | High-yield system for 105 acid |
| CN109562939A (en) * | 2016-07-21 | 2019-04-02 | 托普索公司 | Method for producing sulfur trioxide |
| CN111252742A (en) * | 2020-04-01 | 2020-06-09 | 中化重庆涪陵化工有限公司 | Flue gas acid making system for recovering low-level heat of secondary absorption process |
| CN111252743A (en) * | 2020-04-01 | 2020-06-09 | 中化重庆涪陵化工有限公司 | Sulfur acid making system for recovering low-level heat of secondary absorption process |
| CN114408871A (en) * | 2022-01-28 | 2022-04-29 | 山东明大化学科技股份有限公司 | Heat recovery device for sulfur acid production |
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| CN102958829A (en) * | 2010-01-20 | 2013-03-06 | 梅克斯公司 | Energy recovery in manufacture of sulfuric acid |
| CN103588179A (en) * | 2013-11-13 | 2014-02-19 | 俞向东 | Device and method for improving steam generating rate of low-temperature waste heat recovery system for sulfuric acid |
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| CN101124157A (en) * | 2005-02-21 | 2008-02-13 | 奥图泰有限公司 | Method and device for producing sulfuric acid |
| CN101481095A (en) * | 2009-02-05 | 2009-07-15 | 中国石化集团南京设计院 | Process for recovering and utilizing sulfuric acid manufacture energy |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104229756A (en) * | 2013-06-18 | 2014-12-24 | 天津渤大硫酸工业有限公司 | High-yield system for 105 acid |
| CN109562939A (en) * | 2016-07-21 | 2019-04-02 | 托普索公司 | Method for producing sulfur trioxide |
| CN109562939B (en) * | 2016-07-21 | 2022-12-06 | 托普索公司 | Process for producing sulfur trioxide |
| CN111252742A (en) * | 2020-04-01 | 2020-06-09 | 中化重庆涪陵化工有限公司 | Flue gas acid making system for recovering low-level heat of secondary absorption process |
| CN111252743A (en) * | 2020-04-01 | 2020-06-09 | 中化重庆涪陵化工有限公司 | Sulfur acid making system for recovering low-level heat of secondary absorption process |
| CN111252743B (en) * | 2020-04-01 | 2021-05-28 | 中化重庆涪陵化工有限公司 | Sulfur acid making system for recovering low-level heat of secondary absorption process |
| CN111252742B (en) * | 2020-04-01 | 2021-05-28 | 中化重庆涪陵化工有限公司 | Flue gas acid making system for recovering low-level heat of secondary absorption process |
| CN114408871A (en) * | 2022-01-28 | 2022-04-29 | 山东明大化学科技股份有限公司 | Heat recovery device for sulfur acid production |
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| Publication number | Publication date |
|---|---|
| CN104495757B (en) | 2016-09-28 |
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Address after: 230088 in the high tech Industrial Development Zone, No. 669, Changjiang West Road, Hefei City, Anhui Province Patentee after: EAST CHINA ENGINEERING SCIENCE AND TECHNOLOGY Co.,Ltd. Address before: 230024 No. 70 Wangjiang East Road, Anhui, Hefei Patentee before: EAST CHINA ENGINEERING SCIENCE AND TECHNOLOGY Co.,Ltd. |