CN103482583A - SWSR (SunWay Sulfur recovery)-1 device and technique - Google Patents
SWSR (SunWay Sulfur recovery)-1 device and technique Download PDFInfo
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- CN103482583A CN103482583A CN201310409906.4A CN201310409906A CN103482583A CN 103482583 A CN103482583 A CN 103482583A CN 201310409906 A CN201310409906 A CN 201310409906A CN 103482583 A CN103482583 A CN 103482583A
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Abstract
The invention relates to an SWSR (SunWay Sulfur recovery)-1 device and technique. The invention relates to a tail gas treatment combination device and technique by adopting Claus sulfur recovery and ionic liquid cycle absorption process. The device comprises a sulfur production burning furnace, a Claus reaction system, a sulfur production tail gas incinerator, a rich SO2 process gas heat exchanger, an SO2 absorption tower, a rich liquid pump, a lean and rich liquid heat exchanger, an SO2 regeneration tower and a lean liquid feed pump. The technique comprises the steps: (1) enabling hydrogen sulfide-containing acid gas to generate a Claus reaction, and recovering sulfur and heat energy in the reaction process; (2) burning sulfur production tail gas to generate SO2; (3) removing SO2 from rich SO2 process gas through an ionic liquid absorption tower; and (4) feeding rich SO2 ionic liquid into a regeneration tower for separating and regenerating sulfur. The ionic liquid is an aqueous solution which takes organic positive ions and inorganic anions as main components and a little amount of activating agent and antioxidant as additives. The SWSR-1 device and technique are low in equipment investment, high in material safety, short in technique flow, safe and reliable in technique processes, high in SO2 recovery rate, and the content of SO2 in effluent gas can be reduced by 50ppm below which can meet the national regulation requirement.
Description
Technical field
The present invention relates to a kind of novel process that is applicable to sulphur recovery and vent gas treatment, what be specifically related to is that a kind of conventional Claus technique and ionic liquid utilized reclaims sulphur recovery and the vent gas treatment novel process that the sulfurous gas process optimization improves formation.
Background technology
China advocates energy-saving and emission-reduction work always, strictly controls the sulfur dioxide in air quantity discharged, and before 2012, the sulfur dioxide emissioning concentration of national Specification is not for higher than 960mg/g.National departments concerned is being fermented the revision discharge standard of air pollutants at present, requires newly-built sulphur unit sulfur dioxide emissioning concentration to be less than 400mg/Nm
3(the particular locality emission concentration is less than 200mg/Nm
3).Sinopec is actively implemented the green low-carbon development strategy, using reducing sulphur unit SO 2 from fume emission concentration, as the oil refining plate, strives for one of world-class important indicator, requires sulfur dioxide emissioning concentration in the 2015 (400mg/Nm that reaches world-class levels
3), Some Enterprises reaches world lead level (200mg/Nm
3).
At present domestic sulphur recovery and tail gas treatment process technology adopt Crouse (Claus) the sulfur recovery technique of high temperature thermal response and two-stage catalyzed reaction, in sulphur tail gas processed, contain a small amount of H
2s, SO
2, COS, S
xetc. objectionable impurities, the environmental requirement that after directly burning, discharge does not reach national regulation.The sulfur recovery tail gas treatment process mainly contains low-temperature Claus method, selective oxidation method, Reducing and absorption method.The hydrogenating reduction absorption technique is by the element S in sulfur recovery tail gas, SO
2, COS and CS etc., under very little hydrogen dividing potential drop and extremely low working pressure (about 0.01MPa～0.06MPa), with special vent gas treatment Special hydrogenation catalyzer, by its reduction or be hydrolyzed to H
2s, then absorb with alkanolamine solution, the alkanolamine solution after regeneration recycles.Absorbed H
2the rich solution of S, through manipulation of regeneration, is rich in H
2s gas returns to upstream units, the total sulfur<300ppm in absorbing the purified gas after processing.This technical process is long, need use hydrogen addition technology, and equipment safety is controlled and had relatively high expectations, and the sulfur recovery effect can not meet the needs that environmental requirement further improves.
Summary of the invention
The object of the present invention is to provide a kind of SWSR-1(SWSR-SunWay Sulfur recovery) sulfur recovery unit and technique, combination unit and the technique of Crouse's sulphur recovery and ionic liquid absorption cycle vent gas treatment, to reduce equipment investment, shortened process, reduction energy consumption, save occupation of land, to improve the material security, and the content of sulfur dioxide of processing in rear tail gas is reduced to below 50ppm.
Purpose of the present invention can reach by following measure:
A kind of SWSR-1 sulfur recovery unit, comprise burner for producing sulfur, claus reaction system, sulphur tail gas burning furnace processed, rich SO
2process Gas interchanger, SO
2absorption tower, rich solution pump, poor rich liquid heat exchanger, SO
2regenerator column and lean solution fresh feed pump;
Mode of connection is as follows: burner for producing sulfur connects claus reaction system, sulphur tail gas burning furnace processed, rich SO successively
2process Gas interchanger and SO
2the bottom on absorption tower, SO
2the bottom on absorption tower connects the rich solution pump, the rich solution pump is connected with poor rich liquid heat exchanger, poor rich liquid heat exchanger and SO
2the top of regenerator column connects, SO
2the bottom of regenerator column is connected with the lean solution fresh feed pump, and the lean solution fresh feed pump connects poor rich liquid heat exchanger, and poor rich liquid heat exchanger connects SO
2the top on absorption tower, SO
2the top of regenerator column connects burner for producing sulfur.
Described SO
2the column internals on absorption tower is board-like rotation filler.Board-like rotation filler can make liquid be subject to the effect of the shearing force of the effect of hundreds of times or higher gravity field and rotation filler, be drawn as film as thin as a wafer, very thin silk and small dripping, surface is upgraded rapidly, produce huge alternate contact area, make 1～3 order of magnitude of raising in the traditional tower of interphase mass transfer speed ratio, strengthened mass transfer process, there is very high mass transfer coefficient and very large turndown ratio, there is short, the advantage such as microcosmic mixes, liquid holdup is little of the residence time simultaneously, make absorption process complete, the equipment tower diameter reduces, and reduces cost of equipment.
Described SO
2the column internals of regenerator column is structured packing and rotation filler combination.Structured packing has that specific surface area is large, pressure drop is little, even fluid distribution, mass-and heat-transfer efficiency advantages of higher, the centrifugal force much larger than gravity that rotation filler utilization rotation produces, gas-liquid is contacted under high turbulence, the reinforcing mass transfer process, improve mass-transfer efficiency, therefore, structured packing and rotation filler are used in combination to SO
2on regenerator column, but can reduce tower working pressure, improve that separation efficiency is high, turndown ratio strengthens, the stronger save energy of adaptability, reduce tower diameter.
A kind of SWSR-1 sulfur recovery technique, concrete steps are as follows:
1. sulfide hydrogen sour gas generation claus reaction also reclaims sulphur and heat energy wherein
The sulfide hydrogen sour gas, through burner for producing sulfur, claus reaction system, generates sulphur and sulphur tail gas processed, and wherein sulphur recovery is sent into the molten sulfur storage facility, and sulphur tail gas processed is sent into sulphur tail gas burning furnace processed;
2. sulphur exhaust combustion processed generates sulfurous gas
Sulphur tail gas processed and air mixed are sent into sulphur tail gas burning furnace processed and are burned, and all sulfur-containing mediums all are converted into SO
2, form and be rich in SO
2process Gas, then through rich SO
2the Process Gas interchanger is cooled to below 80 ℃, sends into SO
2absorption tower;
3. rich SO
2process Gas removes SO through the ionic liquid absorption tower
2
Rich SO
2process Gas is at SO
2contact the SO in Process Gas in absorption tower with the ionic liquid lean solution
2absorbed by the ionic liquid lean solution, at the bottom of entering tower, remove SO
2after purified gas send into air flue emission;
4. rich SO
2ionic liquid is sent into the separation regeneration that regenerator column carries out sulphur
Absorb SO
2after the ionic liquid rich solution, be pumped into after the poor rich liquid heat exchanger heat exchange is warmed up to 80-130 ℃ and send into SO through rich solution
2regenerator column, stripping removes the SO in the ionic liquid rich solution
2after by SO
2send into burner for producing sulfur, remove SO
2after the ionic liquid lean solution send into SO through lean solution fresh feed pump, poor rich liquid heat exchanger
2absorption tower;
Described ionic liquid lean solution recycles, and through lean solution fluid infusion line, supplements in case of necessity.
The ionic liquid lean solution is to be main by organic cation, inorganic anion, adds the aqueous solution that a small amount of activator, antioxidant form, and is a kind of ionic liquid of novelty, and vapour pressure is extremely low, nontoxic, harmless, do not fire, not quick-fried, removing SO
2, NO
x, when Hg, As, do not discharge NH
3, CO
2, the regeneration of ionic liquid rich solution (removes SO
2become the ionic liquid lean solution) time produce high-purity SO
2gas.
Active principle in the ionic liquid lean solution is selected from one or more in following material: diglycolamine 1～25wt%, hydroxyethylethylene diamine 1～35wt%, SO
4 2-0.5～28wt%, citric acid 0.01～5wt%, sulfo-dipropyl phenol two fat 0.01～6wt%, 2-send pyridine ethanol (PE) 1～30wt%, tartrate 0.01～3wt%, mercaptan 0.01～2wt%.Above-mentioned weight percent is each component proportion in the ionic liquid lean solution.
Reaction equation:
SO
2+H
2O←→H
++HSO
3 - (1)
R+H
+←→RH
+ (2)
Net reaction:
SO
2+H
2O+R←→RH
++HSO
3 - (3)
In above formula, R represents ionic liquid SO
2absorption agent, (3) formula is reversible reaction, and reaction (3) is carried out from left to right under 10-70 ℃, and reaction (3) is carried out from right to left under 80-130 ℃.Ionic liquid circulation absorbs and utilizes just this principle, at 10-70 ℃ of lower sulfur dioxide absorption, under 80-130 ℃ by sulfur dioxide desorption in absorption agent, thereby reach remove with recovered flue gas in SO
2purpose.
Described claus reaction system is common process.
Burning in described sulphur tail gas burning furnace processed is oxygen-excess combustion technique, in order to sulfide all is converted into to sulfurous gas.
Described SO
2the service temperature on absorption tower is 10～70 ℃.
Described SO
2the service temperature of regenerator column is 80～130 ℃.
Compared with prior art, the present invention has the following advantages:
(1) first Crouse's recovery technology of sulfur is combined with ionic liquid absorption cycle tail gas treatment process, and use in sulphur recovery and vent gas treatment process, belong to international pioneering, and can make to discharge in gas content of sulfur dioxide and drop to minimumly, its effect reached is far superior to when both work separately the effect that can play.
(2) equipment investment is low, and material is safe, and technical process is short, and energy consumption is low, takes up an area and economizes, and without loaded down with trivial details unmanageable hydrogenation process, technological process is safe and reliable, technique and equipment that not dangerous property is larger.
(3) ionic liquid can recycle, and has reduced production cost.
(4) by the design of interchanger, energy can the oneself be utilized in system, save the energy.
(5) in vent gas treatment, the rate of recovery of sulfurous gas is high, and in discharge gas, the content of sulfurous gas can be reduced to below 50ppm, has reduced sulphur recovery and the exhaust gas processing device quantity to airborne release sulfurous gas, meets the requirement of national regulation.
The accompanying drawing explanation
Fig. 1 is SWSR-1 sulfur recovery process flow diagram of the present invention.
In figure: the 1-burner for producing sulfur; 2-claus reaction system; The 3-incinerator; The rich SO of 4-
2the Process Gas interchanger; 5-SO
2absorption tower; 6-rich solution pump; The 7-poor rich liquid heat exchanger; 8-SO
2regenerator column; 9-lean solution fresh feed pump.
Embodiment
Below in conjunction with drawings and Examples, the present invention will be further described.
Embodiment 1
SWSR-1 sulfur recovery unit as shown in Figure 1, comprise burner for producing sulfur 1, claus reaction system 2, sulphur tail gas burning furnace 3 processed, rich SO
2process Gas interchanger 4, SO
2absorption tower 5, rich solution pump 6, poor rich liquid heat exchanger 7, SO
2regenerator column 8 and lean solution fresh feed pump 9;
Mode of connection is as follows: burner for producing sulfur 1 connects claus reaction system 2, sulphur tail gas burning furnace 3 processed, rich SO successively
2process Gas interchanger 4 and SO
2the bottom on absorption tower 5, SO
2the bottom on absorption tower 5 connects rich solution pump 6, rich solution pump 6 is connected with poor rich liquid heat exchanger 7, poor rich liquid heat exchanger 7 and SO
2the top of regenerator column 8 connects, SO
2the bottom of regenerator column 8 is connected with lean solution fresh feed pump 9, and lean solution fresh feed pump 9 connects poor rich liquid heat exchanger 7, and poor rich liquid heat exchanger 7 connects SO
2the top on absorption tower 5, SO
2the top of regenerator column 8 connects burner for producing sulfur 1.
SO
2the column internals on absorption tower 5 is board-like rotation filler.
SO
2the column internals of regenerator column 8 is structured packing and rotation filler combination.
The concrete steps of SWSR-1 sulfur recovery technique are as follows:
1. sulfide hydrogen sour gas generation claus reaction also reclaims sulphur and heat energy wherein
The sulfide hydrogen sour gas, through burner for producing sulfur 1, claus reaction system 2, generates sulphur and sulphur tail gas processed, and wherein sulphur recovery is sent into the molten sulfur storage facility, and sulphur tail gas processed is sent into sulphur tail gas burning furnace 3 processed;
2. sulphur exhaust combustion processed generates sulfurous gas
Sulphur tail gas processed and air mixed are sent into sulphur tail gas burning furnace 3 processed and are burned, and air excess injects, and all sulfur-containing mediums are converted into to SO
2, form and be rich in SO
2process Gas, then through rich SO
2process Gas interchanger 4 is cooled to 10 ℃, sends into SO
2absorption tower 5;
3. rich SO
2process Gas removes SO through the ionic liquid absorption tower
2
Rich SO
2process Gas is at the SO of 10 ℃
2contact the SO in Process Gas in absorption tower 5 with the ionic liquid lean solution
2absorbed by the ionic liquid lean solution, at the bottom of entering tower, remove SO
2after purified gas send into air flue emission;
4. rich SO
2ionic liquid is sent into the separation regeneration that regenerator column carries out sulphur
Absorb SO
2after the ionic liquid rich solution, send into after poor rich liquid heat exchanger 7 heat exchange are warmed up to 80 ℃ and send into SO through rich solution pump 6
2 regenerator column 8, SO
2the working temperature of regenerator column 8 is 80 ℃, by stripping, removes the SO in the ionic liquid rich solution
2after by SO
2send into burner for producing sulfur 1, remove SO
2after the ionic liquid lean solution send into SO through lean solution fresh feed pump 9, poor rich liquid heat exchanger 7
2 absorption tower 5; The ionic liquid lean solution recycles.
Consisting of of ionic liquid lean solution: 2-sends pyridine ethanol (PE) 20%(weight), tartrate 0.1%(weight), mercaptan 0.2%(weight), SO
4 2-12%(weight), all the other are water.
The content that detects sulfurous gas in discharge gas is 36ppm.
SWSR-1 sulfur recovery unit as shown in Figure 1, comprise burner for producing sulfur 1, claus reaction system 2, sulphur tail gas burning furnace 3 processed, rich SO
2process Gas interchanger 4, SO
2 absorption tower 5, rich solution pump 6, poor rich liquid heat exchanger 7, SO
2 regenerator column 8 and lean solution fresh feed pump 9;
Mode of connection is as follows: burner for producing sulfur 1 connects claus reaction system 2, sulphur tail gas burning furnace 3 processed, rich SO successively
2process Gas interchanger 4 and SO
2the bottom on absorption tower 5, SO
2the bottom on absorption tower 5 connects rich solution pump 6, rich solution pump 6 is connected with poor rich liquid heat exchanger 7, poor rich liquid heat exchanger 7 and SO
2the top of regenerator column 8 connects, SO
2the bottom of regenerator column 8 is connected with lean solution fresh feed pump 9, and lean solution fresh feed pump 9 connects poor rich liquid heat exchanger 7, and poor rich liquid heat exchanger 7 connects SO
2the top on absorption tower 5, SO
2the top of regenerator column 8 connects burner for producing sulfur 1.
SO
2the column internals on absorption tower 5 is board-like rotation filler.
SO
2the column internals of regenerator column 8 is structured packing and rotation filler combination.
The concrete steps of SWSR-1 sulfur recovery technique are as follows:
1. sulfide hydrogen sour gas generation claus reaction also reclaims sulphur and heat energy wherein
The sulfide hydrogen sour gas, through burner for producing sulfur 1, claus reaction system 2, generates sulphur and sulphur tail gas processed, and wherein sulphur recovery is sent into the molten sulfur storage facility, and sulphur tail gas processed is sent into sulphur tail gas burning furnace 3 processed;
2. sulphur exhaust combustion processed generates sulfurous gas
Sulphur tail gas processed and air mixed are sent into sulphur tail gas burning furnace 3 processed and are burned, and air excess injects, and all sulfur-containing mediums are converted into to SO
2, form and be rich in SO
2process Gas, then through rich SO
2process Gas interchanger 4 is cooled to 40 ℃, sends into SO
2absorption tower 5;
3. rich SO
2process Gas removes SO through the ionic liquid absorption tower
2
Rich SO
2process Gas is at the SO of 40 ℃
2contact the SO in Process Gas in absorption tower 5 with the ionic liquid lean solution
2absorbed by the ionic liquid lean solution, at the bottom of entering tower, remove SO
2after purified gas send into air flue emission;
4. rich SO
2ionic liquid is sent into the separation regeneration that regenerator column carries out sulphur
Absorb SO
2after the ionic liquid rich solution, send into after poor rich liquid heat exchanger 7 heat exchange are warmed up to 100 ℃ and send into SO through rich solution pump 6
2 regenerator column 8, SO
2the working temperature of regenerator column 8 is 100 ℃, by stripping, removes the SO in the ionic liquid rich solution
2after by SO
2send into burner for producing sulfur 1, remove SO
2after the ionic liquid lean solution send into SO through lean solution fresh feed pump 9, poor rich liquid heat exchanger 7
2 absorption tower 5; The ionic liquid lean solution recycles.
Consisting of of ionic liquid lean solution: diglycolamine 5%(weight), hydroxyethylethylene diamine 15%(weight), SO
4 2-8%(weight), citric acid 0.6%(weight), sulfo-dipropyl phenol two fat 0.6%(weight), all the other are water.
The content that detects sulfurous gas in discharge gas is 22ppm.
SWSR-1 sulfur recovery unit as shown in Figure 1, comprise burner for producing sulfur 1, claus reaction system 2, sulphur tail gas burning furnace 3 processed, rich SO
2process Gas interchanger 4, SO
2 absorption tower 5, rich solution pump 6, poor rich liquid heat exchanger 7, SO
2 regenerator column 8 and lean solution fresh feed pump 9;
Mode of connection is as follows: burner for producing sulfur 1 connects claus reaction system 2, sulphur tail gas burning furnace 3 processed, rich SO successively
2process Gas interchanger 4 and SO
2the bottom on absorption tower 5, SO
2the bottom on absorption tower 5 connects rich solution pump 6, rich solution pump 6 is connected with poor rich liquid heat exchanger 7, poor rich liquid heat exchanger 7 and SO
2the top of regenerator column 8 connects, SO
2the bottom of regenerator column 8 is connected with lean solution fresh feed pump 9, and lean solution fresh feed pump 9 connects poor rich liquid heat exchanger 7, and poor rich liquid heat exchanger 7 connects SO
2the top on absorption tower 5, SO
2the top of regenerator column 8 connects burner for producing sulfur 1.
SO
2the column internals on absorption tower 5 is board-like rotation filler.
SO
2the column internals of regenerator column 8 is structured packing and rotation filler combination.
The concrete steps of SWSR-1 sulfur recovery technique are as follows:
1. sulfide hydrogen sour gas generation claus reaction also reclaims sulphur and heat energy wherein
The sulfide hydrogen sour gas, through burner for producing sulfur 1, claus reaction system 2, generates sulphur and sulphur tail gas processed, and wherein sulphur recovery is sent into the molten sulfur storage facility, and sulphur tail gas processed is sent into sulphur tail gas burning furnace 3 processed;
2. sulphur exhaust combustion processed generates sulfurous gas
Sulphur tail gas processed and air mixed are sent into sulphur tail gas burning furnace 3 processed and are burned, and air excess injects, and all sulfur-containing mediums are converted into to SO
2, form and be rich in SO
2process Gas, then through rich SO
2process Gas interchanger 4 is cooled to 70 ℃, sends into SO
2absorption tower 5;
3. rich SO
2process Gas removes SO through the ionic liquid absorption tower
2
Rich SO
2process Gas is at the SO of 70 ℃
2contact the SO in Process Gas in absorption tower 5 with the ionic liquid lean solution
2absorbed by the ionic liquid lean solution, at the bottom of entering tower, remove SO
2after purified gas send into air flue emission;
4. rich SO
2ionic liquid is sent into the separation regeneration that regenerator column carries out sulphur
Absorb SO
2after the ionic liquid rich solution, send into after poor rich liquid heat exchanger 7 heat exchange are warmed up to 130 ℃ and send into SO through rich solution pump 6
2 regenerator column 8, SO
2the working temperature of regenerator column 8 is 130 ℃, by stripping, removes the SO in the ionic liquid rich solution
2after by SO
2send into burner for producing sulfur 1, remove SO
2after the ionic liquid lean solution send into SO through lean solution fresh feed pump 9, poor rich liquid heat exchanger 7
2 absorption tower 5; The ionic liquid lean solution recycles.
Consisting of of ionic liquid lean solution: diglycolamine 5%(weight), hydroxyethylethylene diamine 15%(weight), SO
4 2-10%(weight), citric acid 0.3%(weight), tartrate 0.3%(weight), sulfo-dipropyl phenol two fat 0.6%(weight), all the other are water.
The content that detects sulfurous gas in discharge gas is 16ppm.
Claims (8)
1. a SWSR-1 sulfur recovery unit, is characterized in that, comprises burner for producing sulfur (1), claus reaction system (2), sulphur tail gas burning furnace processed (3), rich SO
2process Gas interchanger (4), SO
2absorption tower (5), rich solution pump (6), poor rich liquid heat exchanger (7), SO
2regenerator column (8) and lean solution fresh feed pump (9);
Mode of connection is as follows: burner for producing sulfur (1) connects claus reaction system (2), sulphur tail gas burning furnace processed (3), rich SO successively
2process Gas interchanger (4) and SO
2the bottom on absorption tower (5), SO
2the bottom on absorption tower (5) connects rich solution pump (6), rich solution pump (6) is connected with poor rich liquid heat exchanger (7), poor rich liquid heat exchanger (7) and SO
2the top of regenerator column (8) connects, SO
2the bottom of regenerator column (8) is connected with lean solution fresh feed pump (9), and lean solution fresh feed pump (9) connects poor rich liquid heat exchanger (7), and poor rich liquid heat exchanger (7) connects SO
2the top on absorption tower (5), SO
2the top of regenerator column (8) connects burner for producing sulfur (1).
2. SWSR-1 sulfur recovery unit according to claim 1, is characterized in that, described SO
2the column internals on absorption tower (5) is board-like rotation filler.
3. SWSR-1 sulfur recovery unit according to claim 1, is characterized in that, described SO
2the column internals of regenerator column (8) is structured packing and rotation filler combination.
4. a SWSR-1 sulfur recovery technique, is characterized in that, concrete steps are as follows:
1. sulfide hydrogen sour gas generation claus reaction also reclaims sulphur and heat energy wherein
The sulfide hydrogen sour gas, through burner for producing sulfur (1), claus reaction system (2), generates sulphur and sulphur tail gas processed, and wherein sulphur recovery is sent into the molten sulfur storage facility, and sulphur tail gas processed is sent into sulphur tail gas burning furnace processed (3);
2. sulphur exhaust combustion processed generates sulfurous gas
Sulphur tail gas processed and air mixed are sent into sulphur tail gas burning furnace processed (3) and are burned, and all sulfur-containing mediums all are converted into SO
2, form and be rich in SO
2process Gas, then through rich SO
2process Gas interchanger (4) is cooled to 10-80 ℃, sends into SO
2absorption tower (5);
3. rich SO
2process Gas removes SO through the ionic liquid absorption tower
2
Rich SO
2process Gas is at SO
2contact the SO in Process Gas in absorption tower (5) with the ionic liquid lean solution
2absorbed by the ionic liquid lean solution, at the bottom of entering tower, remove SO
2after purified gas send into air flue emission;
4. rich SO
2ionic liquid is sent into the separation regeneration that regenerator column carries out sulphur
Absorb SO
2after the ionic liquid rich solution, send into after poor rich liquid heat exchanger (7) heat exchange is warmed up to 80-130 ℃ and send into SO through rich solution pump (6)
2regenerator column (8), stripping removes the SO in the ionic liquid rich solution
2after by SO
2send into burner for producing sulfur (1), remove SO
2after the ionic liquid lean solution send into SO through lean solution fresh feed pump (9), poor rich liquid heat exchanger (7)
2absorption tower (5);
Described ionic liquid lean solution recycles, and through lean solution fluid infusion line, supplements in case of necessity.
5. SWSR-1 sulfur recovery technique according to claim 4, it is characterized in that, described ionic liquid lean solution is to be main by organic cation, inorganic anion, add the aqueous solution of activator, antioxidant composition, the active principle in the ionic liquid lean solution is selected from one or more in following material: diglycolamine 1～25wt%, hydroxyethylethylene diamine 1～35wt%, SO
4 2-0.5～28wt%, citric acid 0.01～5wt%, sulfo-dipropyl phenol two fat 0.01～6wt%, 2-send pyridine ethanol 1～30wt%, tartrate 0.01～3wt%, mercaptan 0.01～2wt%;
Reaction equation:
SO
2+H
2O←→H
++HSO
3 - (1)
R+H
+←→RH
+ (2)
Net reaction:
SO
2+H
2O+R←→RH
++HSO
3 - (3)
In above formula, R represents ionic liquid SO
2absorption agent, (3) formula is reversible reaction, and reaction (3) is carried out from left to right under 10-70 ℃, and reaction (3) is carried out from right to left under 80-130 ℃.Ionic liquid circulation absorbs and utilizes just this principle, at 10-70 ℃ of lower sulfur dioxide absorption, under 80-130 ℃ by sulfur dioxide desorption in absorption agent, thereby reach remove with recovered flue gas in SO
2purpose.
6. SWSR-1 sulfur recovery technique according to claim 4, is characterized in that, the burning in described sulphur tail gas burning furnace processed (3) is oxygen-excess combustion technique.
7. SWSR-1 sulfur recovery technique according to claim 4, is characterized in that described SO
2the service temperature on absorption tower (5) is 10～70 ℃.
8. SWSR-1 sulfur recovery technique according to claim 4, is characterized in that described SO
2the service temperature of regenerator column (8) is 80～130 ℃.
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| CN105521696A (en) * | 2015-11-26 | 2016-04-27 | 南京大学 | Room-temperature liquid-phase Claus process taking ionic liquid as media |
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