CN105016309A - SWSR-2 sulfur recovery device and process - Google Patents
SWSR-2 sulfur recovery device and process Download PDFInfo
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- CN105016309A CN105016309A CN201510401950.XA CN201510401950A CN105016309A CN 105016309 A CN105016309 A CN 105016309A CN 201510401950 A CN201510401950 A CN 201510401950A CN 105016309 A CN105016309 A CN 105016309A
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- flue gas
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 76
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 75
- 239000011593 sulfur Substances 0.000 title claims abstract description 75
- 238000011084 recovery Methods 0.000 title claims abstract description 36
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000003546 flue gas Substances 0.000 claims abstract description 73
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 70
- 239000007789 gas Substances 0.000 claims abstract description 65
- 230000002745 absorbent Effects 0.000 claims abstract description 40
- 239000002250 absorbent Substances 0.000 claims abstract description 40
- 238000006477 desulfuration reaction Methods 0.000 claims abstract description 36
- 230000023556 desulfurization Effects 0.000 claims abstract description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 claims abstract description 15
- 238000002360 preparation method Methods 0.000 claims abstract description 12
- 238000002485 combustion reaction Methods 0.000 claims abstract description 11
- 239000007788 liquid Substances 0.000 claims description 28
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 17
- 239000002253 acid Substances 0.000 claims description 13
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- 238000010521 absorption reaction Methods 0.000 claims description 12
- 238000001914 filtration Methods 0.000 claims description 12
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 11
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 11
- 239000000395 magnesium oxide Substances 0.000 claims description 6
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 6
- 238000005507 spraying Methods 0.000 claims description 6
- 238000003860 storage Methods 0.000 claims description 6
- 238000010791 quenching Methods 0.000 claims description 5
- 239000011777 magnesium Substances 0.000 claims description 4
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 230000000171 quenching effect Effects 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 230000032683 aging Effects 0.000 claims description 2
- 230000018044 dehydration Effects 0.000 claims description 2
- 238000006297 dehydration reaction Methods 0.000 claims description 2
- 150000002978 peroxides Chemical class 0.000 claims description 2
- 230000002378 acidificating effect Effects 0.000 abstract description 3
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 3
- 239000001257 hydrogen Substances 0.000 abstract description 3
- 239000000463 material Substances 0.000 abstract description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 abstract 2
- 238000004064 recycling Methods 0.000 abstract 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 54
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 description 8
- 239000000347 magnesium hydroxide Substances 0.000 description 8
- 229910001862 magnesium hydroxide Inorganic materials 0.000 description 8
- 230000003009 desulfurizing effect Effects 0.000 description 7
- 238000005516 engineering process Methods 0.000 description 7
- 239000003513 alkali Substances 0.000 description 6
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 description 4
- 238000005984 hydrogenation reaction Methods 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 230000001502 supplementing effect Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- NEMFQSKAPLGFIP-UHFFFAOYSA-N magnesiosodium Chemical compound [Na].[Mg] NEMFQSKAPLGFIP-UHFFFAOYSA-N 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 239000007832 Na2SO4 Substances 0.000 description 2
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 2
- -1 alcohol amine Chemical class 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 229910052943 magnesium sulfate Inorganic materials 0.000 description 2
- 229920006395 saturated elastomer Polymers 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 description 1
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical compound OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 229910052749 magnesium Inorganic materials 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 230000009469 supplementation Effects 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention relates to a SWSR-2 sulfur recovery device and process. The SWSR-2 sulfur recovery device comprises a sulfur-manufacturing combustion furnace, a Claus reaction system, a tail gas burning system, a flue gas desulfurization tower and an absorbent preparation and transportation system. The process comprises the following steps: step 1, subjecting hydrogen sulfide-contained acidic gas to Claus reaction and recycling sulfur and heat energy of the hydrogen sulfide-contained acidic gas; step 2, introducing sulfur tail gas into the tail gas burning system; and step 3, allowing the SO2-contained flue gas to pass through the flue gas desulfurization tower so as to remove SO2. According to the invention, equipment investment is low; material safety is high; process flow is short; processing process is safe and reliable; recovery rate of SO2 is high; SO2 content in discharged gas can be reduced to below 50 mg/Nm3, so requirements of national standards are met.
Description
Technical Field
The invention relates to a novel process suitable for sulfur recovery and tail gas treatment, in particular to a novel process for sulfur recovery and tail gas treatment, which is formed by optimally combining a conventional Claus process and a sodium-magnesium wet-process sulfur flue gas desulfurization technology.
Background
Energy conservation and emission reduction are advocated in China all the time, the emission amount of atmospheric sulfur dioxide is strictly controlled, and the emission concentration of sulfur dioxide specified by national standards is not higher than 960mg/g before 2012. At present, relevant national departments are planning and revising the comprehensive emission standard of atmospheric pollutants, and the newly-built sulfur device is required to have the sulfur dioxide emission concentration less than 400mg/Nm3(the emission concentration of the specific area is less than 200mg/Nm3). China petrochemical actively implements the green low-carbon development strategy, and the reduction of the sulfur dioxide emission concentration of the flue gas of a sulfur device is taken as one of important indexes for the oil refining plate to create world first-class competition, so that the sulfur dioxide emission concentration reaches the world advanced level (400 mg/Nm) in 20153) Part of enterprises reach the world leading level (200 mg/Nm)3)。
At present, the domestic sulfur recovery and tail gas treatment process technology adopts a Claus sulfur recovery process of high-temperature thermal reaction and two-stage catalytic reaction, and the sulfur-making tail gas contains a small amount of H2S、SO2、COS、SxAnd the emission of the harmful substances after direct incineration can not meet the environmental protection requirements specified by the state. The sulfur recovery tail gas treatment method mainly comprises a low-temperature Claus method, a selective oxidation method and a reduction absorption method. Wherein, the low-temperature Claus method is also called sub-dew point sulfur recovery technology, which is one of the widely applied sulfur recovery and tail gas treatment technology types, but the independent low-temperature Claus method needs higher investment and operation cost; the selective oxidation being selective catalytic oxidation of H2S is elemental sulfur and SO2The method has the defects of high requirements on equipment and the like; the hydrogenation reduction absorption process is to recover element S, SO in the tail gas of sulfur recovery2COS, CS, etc. under very low hydrogen partial pressure and very low operation pressure (about 0.01 MPa-0.06 MPa), special tail gas treating special hydrogenation catalyst is used to reduce or hydrolyze the catalyst into H2S is absorbed by alcohol amine solution, and the regenerated alcohol amine solution is recycled. Absorb H2The rich solution of S is regenerated to be rich in H2The S gas returns to the upstream unit, and the total sulfur in the purified gas after the absorption treatment is less than 300 ppm. The process has long flow, needs hydrogenation technology, has higher safety control requirement of the device, and can not meet the requirement of further improving the environmental protection requirement on the sulfur recovery effect.
Disclosure of Invention
The invention aims to provide a process of an SWSR-2(SWSR-Sun way Sulfur Recovery) Sulfur Recovery device, which is a new process for Sulfur Recovery and tail gas treatment formed by optimized combination of a Claus process and a sodium-magnesium wet-process Sulfur flue gas desulfurization technology, and aims to reduce equipment investment, shorten process flow, reduce energy consumption, save land occupation, improve material safety and reduce the Sulfur dioxide content in the treated flue gas to 50mg/Nm3The following.
The object of the invention can be achieved by the following measures:
the SWSR-2 sulfur recovery device comprises a sulfur production combustion furnace, a Claus reaction system, a tail gas incineration system, a flue gas desulfurization tower and an absorbent preparation and conveying system, and the connection mode is as follows: the sulfur-making combustion furnace is sequentially connected with a Claus reaction system, a tail gas incineration system, a flue gas desulfurization tower and an absorbent preparation and conveying system.
The flue gas desulfurization tower is a core unit of a flue gas desulfurization system and mainly comprises a flue gas quenching zone, an absorption zone, a filtering module, a gas-liquid separator, a chimney and the like; the absorbent preparation and delivery system comprises 1 storage bin, 2 feeding units, 2 curing tanks, a magnesium hydroxide storage tank and other auxiliary devices.
A SWSR-2 sulfur recovery process comprises the following specific steps:
firstly, the acid gas containing hydrogen sulfide is subjected to Claus reaction and the sulfur and heat energy in the acid gas are recovered
After being combusted by a sulfur production combustion furnace, the acid gas containing hydrogen sulfide enters a Claus reaction system to generate sulfur and a sulfur production tail gas, wherein the sulfur is recovered and sent to a liquid sulfur storage facility;
② the tail gas for sulfur production is sent into a tail gas incineration system
Mixing the sulfur-making tail gas with air, feeding the mixture into a tail gas incineration system for incineration, and converting the sulfur-containing medium into SO2Form an SO-containing2The flue gas enters a flue gas desulfurization tower after heat energy is recovered;
③ containing SO2Removing SO from flue gas by a flue gas desulfurization tower2
Containing SO2The flue gas contacts with the absorbent entering the flue gas desulfurization tower through the absorbent preparation and conveying system, wherein SO is contained in the flue gas2Absorbed by absorbent, the circulating absorbent enters the tower bottom to remove SO2The purified flue gas is sent into a flue to be discharged.
Wherein the absorbent is Mg (OH)2A slurry made by curing magnesium oxide; and the absorbent may also comprise a sodium hydroxide solution.
And the incineration in the tail gas incineration system is a peroxide combustion process.
The operation temperature of the flue gas desulfurization tower is 40-270 ℃.
Said SO-containing2Removing SO from flue gas by a flue gas desulfurization tower2The specific process flow comprises the following steps: (1) the flue gas entering the flue gas desulfurization tower horizontally enters a quenching zone of the tower and is fully contacted with a circulating absorbent sprayed by a nozzle; (2) the flue gas rises to an absorption area provided with 4 layers of nozzles, a circulating absorbent is sent to the nozzles through a circulating pump for spraying, and spraying liquid and the flue gas are fully mixed; (3) the desulfurized flue gas rises to enter the filtering module part, venturi tubes are arranged in the filtering module, and a nozzle for spraying water to the diverging section of each venturi tube is arranged at the outlet of each venturi tube; (4) the flue gas passing through the filtering module rises to enter a gas-liquid separation zone, the separated water falls into the filtering module zone from the bottom of the gas-liquid separator after the flue gas is subjected to gas-liquid separation, and the purified flue gas after dehydration passes through an upper chimneyAnd is discharged to the atmosphere.
Wherein, the circulating liquid in the step (1) forms a high-density water curtain vertical to the entering direction of the flue gas, the high-density water curtain and the high-density water curtain are fully contacted, the temperature of the flue gas is greatly reduced and saturated to about 60 ℃, and most of dust can be washed in the area; absorbing sulfur dioxide, particulate matters and other acidic gases in the flue gas in the step (2), and purifying the flue gas; and (3) further collecting dust particles and acid mist contained in the flue gas.
The absorbent preparation and conveying system comprises supplement and circulation of absorbent, namely the liquid level at the bottom of the desulfurizing tower is kept by supplementing water, the pH value of the circulating absorbent is controlled to be 6-7 by supplementing alkali liquor, and the circulating absorbent and a discharged liquid treatment system are adopted to treat discharged liquid. Wherein,
a) make-up water
And the liquid level of the circulating liquid at the bottom of the desulfurizing tower is maintained by controlling an adjusting valve on a water supplementing pipeline through a liquid level meter.
b) Alkali liquor
And continuously supplementing the magnesium hydroxide into the absorption liquid at the bottom of the desulfurization tower and the washing liquid of the filtering module. The circulating pump pipeline at the bottom of the tower is provided with a pH meter, and the amount of the alkali liquor entering the desulfurizing tower is adjusted by an adjusting valve on an alkali liquor pipeline, so that the pH value is controlled to be about 6-7.
NaOH with the mass concentration of 30% is sent into an alkali liquor tank from an upstream device through a system pipeline, then is pressurized by the alkali liquor pump and then is divided into two paths, wherein one path is sent to the bottom of the desulfurization tower, and the other path is sent to a filtering module in the desulfurization tower.
c) Absorbent circulation
Circulating liquid at the bottom of the tower is circulated by three circulating pumps, circulating absorbent is stored at the bottom of the desulfurizing tower and is respectively sent to a cooling nozzle of a quenching zone of the desulfurizing tower and an absorption nozzle at the middle part of the desulfurizing tower by the circulating pump at the bottom of the desulfurizing tower.
d) Absorption tower liquor drainage
The discharged liquid is sent to a discharged liquid treatment system for treatment through a tower bottom circulating pump.
In addition, Mg (OH)2The desulfurization mechanism of NaOH is that alkaline substances and sulfurous acid solution generated by dissolving sulfur dioxide in water carry out acid-base neutralization reaction, and the pH value of circulating liquid is adjusted by adjusting the adding amount of magnesium hydroxide solution. The selection of the water to gas ratio and the number of nozzles required for sulfur dioxide absorption is determined by the inlet concentration of sulfur dioxide, the emission requirements, and the temperature of the saturated gas.
The reaction chemical formula is as follows:
magnesium oxide pulping:
MgO+H2O→Mg(OH)2
and (3) desulfurization reaction:
Mg(OH)2+SO2→MgSO3+H2O
Mg(OH)2+SO3→MgSO4+H2O
2NaOH+SO2→Na2SO3+H2O
2NaOH+SO3→Na2SO4+H2O
and (3) oxidation reaction:
MgSO3+0.5O2→MgSO4
Na2SO3+0.5O2→Na2SO4
compared with the prior art, the invention has the following advantages:
(1) the Claus sulfur recovery process and the sodium-magnesium wet flue gas desulfurization technology are combined for the first time, the sulfur recovery and tail gas treatment process is used, the sulfur dioxide content in the exhaust gas can be reduced to the minimum, and the achieved effect is far better than the effect of the two in the respective working processes.
(2) The method has the advantages of low equipment investment, high material safety, short process flow, low energy consumption, small occupied area, no need of complicated and difficult-to-control hydrogenation process, safe and reliable process and no process and equipment with high risk.
(3) The main raw material MgO powder of the desulfurizer has rich magnesium ore resources in China, low price and low operation cost.
(4) The recovery rate of sulfur dioxide in tail gas treatment is high, and the content of sulfur dioxide in the exhaust gas can be reduced to 50mg/Nm3The amount of sulfur dioxide discharged to the atmosphere by the sulfur recovery and tail gas treatment device is reduced, and the national standard requirement is met.
Drawings
FIG. 1 is a schematic of a SWSR-2 sulfur recovery process scheme of the present invention.
Detailed Description
The present invention will be further described with reference to the following examples.
Example 1
A SWSR-2 sulfur recovery process comprises the following specific steps:
firstly, the acid gas containing hydrogen sulfide is subjected to Claus reaction and the sulfur and heat energy in the acid gas are recovered
After being combusted by a sulfur production combustion furnace, the acid gas containing hydrogen sulfide enters a Claus reaction system to generate sulfur and a sulfur production tail gas, wherein the sulfur is recovered and sent to a liquid sulfur storage facility;
② the tail gas for sulfur production is sent into a tail gas incineration system
Mixing the sulfur-making tail gas with air, feeding the mixture into a tail gas incineration system for incineration, and converting sulfur-containing mediumIs SO2Form an SO-containing2The flue gas enters a flue gas desulfurization tower after heat energy is recovered;
③ containing SO2Removing SO from flue gas by a flue gas desulfurization tower2
Containing SO2The flue gas contacts with absorbent (magnesium hydroxide slurry with mass concentration of 20% prepared by aging magnesium oxide) entering flue gas desulfurization tower through absorbent preparation and conveying system, wherein SO2Absorbed by absorbent, the circulating absorbent enters the tower bottom to remove SO2The purified flue gas is sent into a flue to be discharged.
Detecting the content of sulfur dioxide in the exhaust gas to be 39mg/Nm3。
Example 2
A SWSR-2 sulfur recovery process comprises the following specific steps:
firstly, the acid gas containing hydrogen sulfide is subjected to Claus reaction and the sulfur and heat energy in the acid gas are recovered
After being combusted by a sulfur production combustion furnace, the acid gas containing hydrogen sulfide enters a Claus reaction system to generate sulfur and a sulfur production tail gas, wherein the sulfur is recovered and sent to a liquid sulfur storage facility;
② the tail gas for sulfur production is sent into a tail gas incineration system
Mixing the sulfur-making tail gas with air, feeding the mixture into a tail gas incineration system for incineration, and converting the sulfur-containing medium into SO2Form an SO-containing2The temperature of the flue gas is 270 ℃, and the content of sulfur dioxide is 18000mg/Nm3. Then the recovered heat energy enters a flue gas desulfurization tower;
③ containing SO2Removing SO from flue gas by a flue gas desulfurization tower2
Containing SO2Flue gas and absorbent (magnesium hydroxide slurry with mass concentration of 20% and sodium hydroxide with mass concentration of 30%) entering the flue gas desulfurization tower through absorbent preparation and conveying systemSolution) of SO in the solution2Absorbed by absorbent, the circulating absorbent enters the tower bottom to remove SO2The purified flue gas is sent into a flue to be discharged.
Detecting the content of the sulfur dioxide in the exhaust gas to be 31mg/Nm3。
Claims (10)
1. The SWSR-2 sulfur recovery device is characterized by comprising a sulfur production combustion furnace, a Claus reaction system, a tail gas incineration system, a flue gas desulfurization tower and an absorbent preparation and conveying system, wherein the connection mode is as follows: the sulfur-making combustion furnace is sequentially connected with a Claus reaction system, a tail gas incineration system, a flue gas desulfurization tower and an absorbent preparation and conveying system.
2. The SWSR-2 sulfur recovery device of claim 1, wherein said flue gas desulfurization tower essentially comprises a flue gas quench section, an absorption section, a filtration module, a gas-liquid separator and a chimney.
3. The SWSR-2 sulfur recovery process is characterized by comprising the following specific steps of:
firstly, the acid gas containing hydrogen sulfide is subjected to Claus reaction and the sulfur and heat energy in the acid gas are recovered
After being combusted by a sulfur production combustion furnace, the acid gas containing hydrogen sulfide enters a Claus reaction system to generate sulfur and a sulfur production tail gas, wherein the sulfur is recovered and sent to a liquid sulfur storage facility;
② the tail gas for sulfur production is sent into a tail gas incineration system
Mixing the sulfur-making tail gas with air, feeding the mixture into a tail gas incineration system for incineration, and converting the sulfur-containing medium into SO2Form an SO-containing2The flue gas enters a flue gas desulfurization tower after heat energy is recovered;
③ containing SO2Removing SO from flue gas by a flue gas desulfurization tower2
Containing SO2The flue gas contacts with the absorbent entering the flue gas desulfurization tower through the absorbent preparation and conveying system, wherein SO is contained in the flue gas2Absorbed by absorbent, the circulating absorbent enters the tower bottom to remove SO2The purified flue gas is sent into a flue to be discharged.
4. The SWSR-2 sulfur recovery process of claim 3, wherein said absorbent is Mg (OH)2A slurry made by aging magnesium oxide.
5. The SWSR-2 sulfur recovery process of claim 4, wherein said absorbent further comprises a sodium hydroxide solution.
6. The SWSR-2 sulfur recovery process of claim 3, wherein incineration in said tail gas incineration system is a peroxide combustion process.
7. The SWSR-2 sulfur recovery process of claim 6, wherein the operating temperature of said flue gas desulfurization tower is 40-270 ℃.
8. The SWSR-2 sulfur recovery process of claim 3, wherein SO is contained2Removing SO from flue gas by a flue gas desulfurization tower2The specific process flow comprises the following steps: (1) the flue gas entering the flue gas desulfurization tower horizontally enters a quenching zone of the tower and is fully contacted with a circulating absorbent sprayed by a nozzle; (2) the flue gas rises to an absorption area provided with 4 layers of nozzles, a circulating absorbent is sent to the nozzles through a circulating pump for spraying, and spraying liquid and the flue gas are fully mixed; (3) the desulfurized flue gas rises to enter the filtering module part, venturi tubes are arranged in the filtering module, and a nozzle for spraying water to the diverging section of each venturi tube is arranged at the outlet of each venturi tube; (4) the flue gas after passing through the filtering module rises to enter a gas-liquid separation zone, the separated water falls into the filtering module zone from the bottom of the gas-liquid separator after the gas-liquid separation, and the purified flue gas after dehydration is discharged into the atmosphere through an upper chimney.
9. The SWSR-2 sulfur recovery process of claim 8, wherein the pH of the recycled absorbent is controlled to be in the range of 6 to 7.
10. The SWSR-2 sulfur recovery process of claim 3, wherein said absorbent preparation and delivery system comprises make-up and recycle of the absorption liquid by maintaining the desulfurization tower bottoms level with make-up water, make-up lye to control the pH of the recycled absorbent to 6-7, and circulating the absorbent with a circulating pump, a blowdown treatment system to treat the effluent.
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
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CN105692563A (en) * | 2016-01-27 | 2016-06-22 | 山东三维石化工程股份有限公司 | SWSR (Sunway Sulfur Recovery)-7 technology and SWSR-7 device |
CN108910829A (en) * | 2018-07-26 | 2018-11-30 | 国家能源投资集团有限责任公司 | The sulfur recovery method of sour gas sulfur recovery system and sour gas |
CN109019524A (en) * | 2018-08-30 | 2018-12-18 | 山东迅达化工集团有限公司 | A kind of recovery technology of sulfur of middle low concentration sour gas |
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2015
- 2015-07-09 CN CN201510401950.XA patent/CN105016309A/en active Pending
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Cited By (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN105692563A (en) * | 2016-01-27 | 2016-06-22 | 山东三维石化工程股份有限公司 | SWSR (Sunway Sulfur Recovery)-7 technology and SWSR-7 device |
CN105692563B (en) * | 2016-01-27 | 2018-11-13 | 山东三维石化工程股份有限公司 | SWSR-7 sulfur recovery technologies and device |
CN108910829A (en) * | 2018-07-26 | 2018-11-30 | 国家能源投资集团有限责任公司 | The sulfur recovery method of sour gas sulfur recovery system and sour gas |
CN109019524A (en) * | 2018-08-30 | 2018-12-18 | 山东迅达化工集团有限公司 | A kind of recovery technology of sulfur of middle low concentration sour gas |
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