CN104495757B - SO in sulfuric acid apparatus3absorb low-temperature heat energy recovery system - Google Patents
SO in sulfuric acid apparatus3absorb low-temperature heat energy recovery system Download PDFInfo
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- CN104495757B CN104495757B CN201510004554.3A CN201510004554A CN104495757B CN 104495757 B CN104495757 B CN 104495757B CN 201510004554 A CN201510004554 A CN 201510004554A CN 104495757 B CN104495757 B CN 104495757B
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- acid
- gas
- sulfuric acid
- tubular type
- liquid separator
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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
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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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses SO in a kind of sulfuric acid apparatus3Absorbing low-temperature heat energy recovery system, high-concentration sulfuric acid sprays from the atomizer of tubular type Jet absorber, with the SO being once converted3Process gas is fully contacted, and absorbs SO therein3Generate high-temperature concentrated sulfuric acid.Enter gas-liquid separator from tube-type jet lower part outlet process gas out, carry out gas-liquid separation, then enter two-level absorption tower after gas-liquid separator outlet demister is except mist, in tower, absorb remaining SO with concentrated sulphuric acid3After again through tower top demister except after mist, process gas returns again to conversion system and carries out twice transformation.
Description
Technical field
The present invention relates to SO in sulfuric acid apparatus3Absorption system field, SO in specifically a kind of sulfuric acid apparatus3Absorb low-temperature level
Heat reclaiming system.
Background technology
Production technology in sulfuric acid apparatus, energy-saving and emission-reduction, the level that utilizes of raising used heat are always sulfuric acid industry technology people
The target that member pursues.Gas washing in SA production technology in early days focuses on the conversion reaction heat of the combustion heat and the middle potential temperature reclaiming high-temperature position
Can, industry worker is made that contribution greatly in this regard, has promoted the flourish of sulfuric acid industry.But at SO3Absorb
Generate the energy recovery aspect that sulphuric acid produces, as receiving SO3Absorb reaction heat and the carrier of the sulphuric acid heat of dilution, high-temperature concentrated sulfuric acid
Being only used for adding hot desalinized water, its waste heat energy is all lost in vain by circulating water the most always.Along with novel corrosion resistant
The appearance of material and gradual perfection, the temperature of heat carrier concentrated sulphuric acid can greatly be promoted, and makes this part of low-temperature level heat
Being recycled in order to possible of energy.The most existing multiple different technology is applied to the recovery of this partial heat energy.
Summary of the invention it is an object of the invention to provide SO in a kind of sulfuric acid apparatus3Absorb low-temperature heat energy recovery system, with
Realize concentrated sulphuric acid atomization and SO3Process gas is fully contacted.
In order to achieve the above object, the technical solution adopted in the present invention is:
SO in sulfuric acid apparatus3Absorb low-temperature heat energy recovery system, it is characterised in that: include tubular type Jet absorber, join
There are the gas-liquid separator of spraying cycle pump, waste heat boiler, diluter, boiler water-suppling heater, desalted water preheater, two grades of absorptions
Tower, be furnished with two grades of absorption acid circulating pumps two-level absorption tower circulation acid tank, two grades of absorption cycle acid coolers,
Described tubular type Jet absorber is made up of mixing chamber and the atomizer being arranged in mixing chamber, turns from sulfuric acid apparatus
The SO that chemical industry section is once converted3Process gas enters in the mixing chamber of tubular type Jet absorber, in mixing chamber and atomizer
The sulfuric acid droplets sprayed in mixing chamber is fully contacted, major part SO in process gas3Absorbed, 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 absorber3Process gas and
High-temperature concentrated sulfuric acid enters gas-liquid separator, and after gas-liquid separator carries out gas-liquid separation, gas phase is left gas-liquid separator and entered two
Bottom level absorption tower, the high-temperature concentrated sulfuric acid separated is stored in gas-liquid separator bottom, after then being pressurizeed by spraying cycle pump
It is sent to waste heat boiler；
Described two-level absorption tower is packed tower, and concentrated sulphuric acid is evenly distributed on by the acid trap in two-level absorption tower top and fills out
In material, from the process gas packing layer in two-level absorption tower from bottom to top and the concentrated sulphuric acid counter current contacting of gas-liquid separator, work
SO remaining in skill gas3Being absorbed by concentrated sulphuric acid, the lower tower acid gravity flow of two-level absorption tower enters two-level absorption tower circulation acid tank and keeps in,
The acid trap on two-level absorption tower top is removed again after two grades of absorption cycles are pumped to two grades of absorption cycle acid cooler coolings.Go out two grades
The process gas return sulfuric acid apparatus conversion section absorbing tower top 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 concentrated sulphuric acid after cooling
Send into the atomizer delivering to tubular type Jet absorber after regulating acid concentration in diluter again, by the atomization of tubular type Jet absorber
Shower nozzle sprays to mixing chamber.Meanwhile, one concentrated acid is drawn through boiler water-suppling heater and desalted water from waste heat boiler outlet
After preheater recovery waste heat, export as product acid.
SO in described sulfuric acid apparatus3Absorb low-temperature heat energy recovery system, it is characterised in that: tubular type Jet absorber mixes
Close indoor and 1～3 layer of atomizer is set, atomizer concentrated sulphuric acid out and SO3Process gas is fully contacted, and atomizer sprays
Density is 100～200 t/(m2H), tubular type Jet absorber mixing indoor air velocity is 8～15 m/s.
SO in described sulfuric acid apparatus3Absorb low-temperature heat energy recovery system, it is characterised in that: gas-liquid separator gas phase goes out
Mouth arranges demister and removes acid mist further.
SO in described sulfuric acid apparatus3Absorb low-temperature heat energy recovery system, it is characterised in that: air-flow in two-level absorption tower
Speed is 1.6～2.0m/s, liquid spraying density 20～25m3/ (m2H), packed height 3～4 meters.
The invention have the advantage that
(1) using the process units that the present invention builds, its process equipment is simple, and operation and maintenance costs is low, once invests
Save.
(2) use tubular type injection to absorb flow process, reduce the resistance drop of process gas system, sulfate system blower fan can be reduced
Load output.
(3) gas-liquid separator is set and demister reduces entrainment, alleviate the tail gas impact on two-level absorption tower.
Accompanying drawing explanation
Fig. 1 is the process flow diagram of the present invention.
Detailed description of the invention
Shown in Figure 1, SO in sulfuric acid apparatus3Absorb low-temperature heat energy recovery system, including tubular type Jet absorber 1,
It is furnished with the gas-liquid separator 2 of spraying cycle pump 7, waste heat boiler 8, diluter 9, boiler water-suppling heater 10, desalted water preheater
11, two-level absorption tower 3, be furnished with two grades of absorption acid circulating pumps 5 two-level absorption tower circulation 4, two grades of absorption cycle acid coolers of acid tank
6；
Tubular type Jet absorber 1 is made up of mixing chamber and the atomizer being arranged in mixing chamber, converts from sulfuric acid apparatus
The SO that workshop section is once converted3Process gas enter tubular type Jet absorber 1 mixing chamber in, in mixing chamber with atomizer to
The sulfuric acid droplets sprayed in mixing chamber is fully contacted, major part SO in process gas3Absorbed, 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 13Process gas and height
Temperature concentrated sulphuric acid enters gas-liquid separator 2, and after gas-liquid separator 2 carries out gas-liquid separation, process gas is gone out by gas-liquid separator 2 gas phase
Mouth enters bottom two-level absorption tower 3, and the high-temperature concentrated sulfuric acid separated is stored in gas-liquid separator 2 bottom, is then followed by injection
It is sent to waste heat boiler 8 after ring pump 7 pressurization；
Two-level absorption tower 3 is packed tower, and concentrated sulphuric acid is evenly distributed on filler by the acid trap in two-level absorption tower 3 top
In, from the process gas packing layer in two-level absorption tower 3 from bottom to top and the concentrated sulphuric acid counter current contacting of gas-liquid separator 2, work
SO remaining in skill gas3Being absorbed by concentrated sulphuric acid, it is temporary that the lower tower acid gravity flow of two-level absorption tower 3 enters two-level absorption tower circulation acid tank 4
Deposit, then remove two-level absorption tower 3 top acid trap after two grades of absorbent recirculation pumps 5 deliver to two grades of absorption cycle acid cooler 6 coolings.Go out
The process gas of two-level absorption tower 3 tower top returns again to sulfuric acid apparatus conversion section 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, and the concentrated sulphuric acid after cooling send
Enter the atomizer delivering to tubular type Jet absorber 1 after regulating concentration in diluter 9 again, by the atomization of tubular type Jet absorber 1
Shower nozzle sprays to mixing chamber.Meanwhile, one concentrated acid is drawn through boiler water-suppling heater 10 and desalination from waste heat boiler 8 outlet
After water preheater 11 recovery waste heat, export as product acid.
1～3 layer of atomizer is set in tubular type Jet absorber 1 mixing chamber, atomizer concentrated sulphuric acid out and SO3Work
Skill gas is fully contacted, and atomizer sprinkle density is 100～200 t/(m2H), tubular type Jet absorber mixing indoor air flow
Speed is 8～15 m/s.
Gas-liquid separator 2 gaseous phase outlet arranges demister and removes acid mist further.
In two-level absorption tower 3, air velocity is 1.6～2.0m/s, liquid spraying density 20～25m3/ (m2H), filler is high
Spend 3～4 meters.
Embodiment 1: use 200,000 tons/year of sulphur-burning sulphuric acid plants of the present invention
From conversion section containing 6～10%SO3Process gas, enters tubular type injection and inhales from the top of tubular type Jet absorber
In receipts device, contact with the concentrated sulphuric acid of the atomizer ejection being arranged on Jet absorber top, the SO in process gas3Absorbed.
Ejector a diameter of φ 1800mm, effective depth is 4000mm.Enter the acid of tubular type Jet absorber dense control 99.1%～
99.3%, acid temperature control is at 170 DEG C～185 DEG C.Going out the Jet absorber dense control 99.5～99.6% of acid, acid temperature control is at 195 DEG C
～210 DEG C.Enter after gas-liquid separator carries out gas-liquid separation from the bottom of tube-type jet process gas out, process gas warp
Gas-liquid separator gaseous phase outlet demister is except entering two-level absorption tower after mist.Two-level absorption tower is packed tower, tower diameter phi
4000mm, effective tower height 13000mm.Process gas connects with the adverse current in packing layer of 98% sulphuric acid under from tower top from bottom to top
Touch, the remaining SO in process gas3Absorbed, then carry out secondary through tower top demister and turn except returning conversion section from tower top after mist
Change.
The high-temperature concentrated sulfuric acid being stored in gas-liquid separator bottom is sent to more than waste heat boiler recovery after spraying cycle pump pressurizes
Heat, produces the low-pressure saturated steam of 0.5～1.0MPa.Go out waste heat boiler temperature～180 DEG C of concentrated sulphuric acids enter dilute device and add
Water dilute acid is dense send tubular type Jet absorber atomizer again to 99.1%～99.3%.Absorb SO3The unnecessary concentrated sulphuric acid of rear generation
Draw from heat boiler outlet and deliver to final absorption tower circulation acid tank or air drying cycle acid tank for producing 98% sulphuric acid.
Embodiment 2: use 600,000 tons/year of sulphur-burning sulphuric acid plants of the present invention
From conversion section containing 6～10%SO3Process gas, enters tubular type absorber from the top of tubular type Jet absorber
In, contact with the concentrated sulphuric acid of the atomizer ejection being arranged in Jet absorber, the SO in process gas3Absorbed.Ejector
A diameter of φ 3000mm, effective depth is 6000mm.Entrance tubular type Jet absorber acid is dense to be controlled 99.1%～99.3%, acid temperature
Control at 170 DEG C～185 DEG C.Going out the Jet absorber dense control 99.5～99.6% of acid, acid temperature control is at 195 DEG C～210 DEG C.From
The bottom of tube-type jet process gas out enters in gas-liquid separator after gas-liquid separation, and process gas is through gas-liquid separator gas phase
Outlet demister is except entering two-level absorption tower after mist.Two-level absorption tower is packed tower, tower diameter phi 6600mm, effective tower height
13000mm.Process gas from bottom to top with the 98% sulphuric acid counter current contacting in packing layer under from tower top, residual in process gas
Remaining SO3Absorbed, then carried out twice transformation from tower top return conversion section after tower top demister is except mist.
The high-temperature concentrated sulfuric acid being stored in gas-liquid separator bottom is sent to more than waste heat boiler recovery after spraying cycle pump pressurizes
Heat, produces the low-pressure saturated steam of 0.5～1.0MPa.Go out waste heat boiler temperature～180 DEG C of concentrated sulphuric acids enter dilute device and add
Water dilute acid is dense send tubular type Jet absorber atomizer to 99.1%～99.3%, continues to absorb SO3.Absorb SO3Rear generation
Unnecessary concentrated sulphuric acid is drawn from heat boiler outlet and is delivered to final absorption tower circulation acid tank or air drying cycle acid tank for producing
98% sulphuric acid.
Claims (4)
1. SO in sulfuric acid apparatus3Absorb low-temperature heat energy recovery system, it is characterised in that: include tubular type Jet absorber, be furnished with spray
Penetrate the gas-liquid separator of circulating pump, waste heat boiler, diluter, boiler water-suppling heater, desalted water preheater, two-level absorption tower,
It are furnished with two-level absorption tower circulation acid tank, two grades of absorption cycle acid coolers of two grades of absorption acid circulating pumps；The injection of described tubular type absorbs
Device is made up of mixing chamber and the atomizer being arranged in mixing chamber, the SO being once converted from sulfuric acid apparatus conversion section3Work
Skill gas enters in the mixing chamber of tubular type Jet absorber, the sulfuric acid droplets sprayed in mixing chamber with atomizer in mixing chamber
It is fully contacted, by major part SO in sulfuric acid droplets absorption technique gas3, produce high-temperature concentrated sulfuric acid；Described gas-liquid separator sets
Put below tubular type Jet absorber, go out the SO of tubular type Jet absorber3Process gas and high-temperature concentrated sulfuric acid enter gas-liquid separator,
After gas-liquid separator carries out gas-liquid separation, gas phase is left gas-liquid separator and is entered bottom two-level absorption tower, the height separated
Temperature concentrated sulphuric acid is stored in gas-liquid separator bottom, is sent to waste heat boiler after then being pressurizeed by spraying cycle pump；Described two grades of absorptions
Tower is packed tower, and concentrated sulphuric acid is evenly distributed in filler by the acid trap in two-level absorption tower top, from gas-liquid separator
The process gas packing layer in two-level absorption tower from bottom to top and concentrated sulphuric acid counter current contacting, SO remaining in process gas3Dense
Sulfuric acid absorption, the lower tower acid gravity flow of two-level absorption tower enters two-level absorption tower circulation acid tank and keeps in, then through two grades of absorbent recirculation pumps
The acid trap on two-level absorption tower top is removed after delivering to two grades of absorption cycle acid cooler coolings；Go out the process gas on two-level absorption tower top
Return sulfuric acid apparatus conversion section and carry 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 concentrated sulphuric acid after cooling sends into the atomization delivering to tubular type Jet absorber after regulating acid concentration in diluter again
Shower nozzle, is sprayed to mixing chamber by the atomizer of tubular type Jet absorber；Meanwhile, one is drawn from waste heat boiler outlet
Concentrated acid, after boiler water-suppling heater and desalted water preheater recovery waste heat, exports as product acid.
SO in sulfuric acid apparatus the most according to claim 13Absorb low-temperature heat energy recovery system, it is characterised in that: tubular type is sprayed
1～3 layer of atomizer is set in penetrating absorber mixing chamber, atomizer concentrated sulphuric acid out and SO3Process gas is fully contacted, mist
Changing shower nozzle sprinkle density is 100～200 t/m2H, tubular type Jet absorber mixing indoor air velocity is 8～15 m/s.
SO in sulfuric acid apparatus the most according to claim 13Absorb low-temperature heat energy recovery system, it is characterised in that: gas-liquid is divided
Demister is set from device gaseous phase outlet and removes acid mist further.
SO in sulfuric acid apparatus the most according to claim 13Absorb low-temperature heat energy recovery system, it is characterised in that: two grades of suctions
In receipts tower, air velocity is 1.6～2.0m/s, liquid spraying density 20～25m3/m2H, packed height 3～4 meters.
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| Application Number | Priority Date | Filing Date | Title |
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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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| CN104495757A CN104495757A (en) | 2015-04-08 |
| CN104495757B true CN104495757B (en) | 2016-09-28 |
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Families Citing this family (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 |
| US10640376B2 (en) * | 2016-07-21 | 2020-05-05 | Haldor Topsoe A/S | Process for the production of sulfur trioxide |
| 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 |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN102070128A (en) * | 2010-11-07 | 2011-05-25 | 湖南新恒光科技有限公司 | Process for efficiently recovering afterheat generated in the process of producing sulfuric acid from pyritic |
| 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 |
-
2015
- 2015-01-06 CN CN201510004554.3A patent/CN104495757B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
| CN102958829A (en) * | 2010-01-20 | 2013-03-06 | 梅克斯公司 | Energy recovery in manufacture of sulfuric acid |
| CN102070128A (en) * | 2010-11-07 | 2011-05-25 | 湖南新恒光科技有限公司 | Process for efficiently recovering afterheat generated in the process of producing sulfuric acid from pyritic |
| 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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