CN102942162A - Liquid-phase treatment process of tail gas from sulfur recovery - Google Patents
Liquid-phase treatment process of tail gas from sulfur recovery Download PDFInfo
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- CN102942162A CN102942162A CN2012105175569A CN201210517556A CN102942162A CN 102942162 A CN102942162 A CN 102942162A CN 2012105175569 A CN2012105175569 A CN 2012105175569A CN 201210517556 A CN201210517556 A CN 201210517556A CN 102942162 A CN102942162 A CN 102942162A
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Abstract
The invention belongs to the technical field of sulfur recovery, and particularly relates to a liquid-phase treatment process of tail gas from sulfur recovery. The liquid-phase treatment process comprises the following steps: recovering sulfur from acid gas through a Claus sulfur recovery device to generate sulfur production tail gas; introducing the sulfur production tail gas into a water film reactor, wherein all the sulfur dioxide and excessive hydrogen sulfide react to generate sulfur and H2S-containing tail gas; enabling the H2S-containing tail gas to be in direct contact with water to cool the H2S-containing tail gas, and discharging the condensed process waste water; oxidating the H2S-containing tail gas in an oxidation reactor to generate in-process gas; cooling the in-process gas through a sulfur cooler, and then further reacting in the water film reactor; and incinerating the waste gas, and then discharging. According to the process, the water film reactor is utilized to solve the problem on sulfur fog collection, and the water film reaction is used in the sulfur production tail gas treatment for the first time, thereby greatly improving the sulfur conversion rate, greatly shortening the process, and greatly reducing the construction investment, the operating cost and the energy consumption.
Description
Technical field
The invention belongs to the sulphur recovery technical field, be specifically related to a kind of sulfur recovery tail gas liquid phase treatment process.
Background technology
The raw material of claus sulphur recovery units mainly contains H
2The S sour gas.Enter the claus sulphur recovery units recovery sulphur, the total sulfur yield of Cross unit is about 95～97%wt; Through discharging after hydrogenating reduction-absorption-burning, the total sulfur yield can reach more than 99.8% sulphur tail gas processed again.
According to prior art, sour gas through the detailed process of claus sulphur recovery units recovery sulphur generation sulphur tail gas processed is first: enter the burner for producing sulfur burner combustion after upstream device H 2 S-containing gas and the air mixed, enter the one-level condensate cooler after in waste heat boiler occurs, pressing the saturation steam recovery waste heat, the elementary sulfur that reaction is generated is solidifying for liquid, and molten sulfur is captured to separate and enters molten sulfur product pond; According to the temperature of reaction requirement, one-level condensate cooler Process Gas out mixes intensification through the one-level high-temp mixing valve with a part of high temperature gas flow in the burner for producing sulfur, enters the one-level convertor, under the effect of catalyzer, and the H in the Process Gas
2S and SO
2Carry out the Claus reaction, be converted into elementary sulfur, enter the Process Gas heat exchanger tube pass from one-level convertor pyroprocess gas out, enter again the B-grade condensation water cooler, Process Gas is through B-grade condensation water cooler generation low-pressure saturated steam and make elementary sulfur solidifying for liquid, and molten sulfur enters the sulphur sealed cans after capturing and separating; Again through entering the secondary convertor after the intensification of Process Gas heat exchanger shell pass, make remaining H in the Process Gas by B-grade condensation water cooler Process Gas out
2S and SO
2Catalyzed conversion further occurs, and secondary convertor exit procedure gas is through three grades of condensate cooler generation low-pressure saturated steams and make elementary sulfur solidifying for liquid, and molten sulfur is captured to separate and enters molten sulfur product pond; Three grades of condensate coolers sulphur tail gas processed out enters tail gas and divides flow container to capture further that molten sulfur is laggard to enter the vent gas treatment part.From the sulphur tail gas processed that sulphur recovery is partly discharged, still contain a small amount of H
2S, SO
2, COS, S
xDeng material, the environmental requirement that discharging does not reach national regulation after directly burning.For this reason, the tail gas of sulphur part processed need to be proceeded vent gas treatment.It is as follows that existing Claus tail-gas hydrogenation reduces-absorb the treatment technology technical process: divide flow container sulphur tail gas processed out by tail gas, enter hydrogenator, SO under the effect of low temperature hydrogenation catalyzer behind heat exchange, mixed hydrogen
2And COS etc. is reduced to H by hydrogenation hydrolyzation
2S.Enter the vapour generator recovery waste heat from hydrogenator air-flow out, enter quench tower after the generation low-pressure steam and directly contact cooling down to normal temperature with quenched water.Tail gas after the chilling cooling out enters tail gas absorber from cat head, and the amine liquid (～25% MDEA amine liquid) of sending here with regeneration section absorbs H wherein
2S, tail gas absorber eject the purified gas that comes and enter the tail gas burning furnace burning.Under 570～600 ℃ of fire box temperatures of tail gas burning furnace, the H of remnants in the purified gas
2S is combusted as SO
2, residue H
2Become CO with hydrocarbon fuel
2And H
2O, from tail gas burning furnace high-temperature flue gas out behind tail gas waste heat boiler recovery waste heat by smoke stack emission.Rich solution after tail gas absorber uses is pumped to amine liquid regeneration section with rich solution and carries out solvent reclamation.
This technological process flow process is long, construction investment is large, working cost and energy consumption are high, and total sulphur rate of recovery is low.
Summary of the invention
For the problems referred to above, the invention provides a kind of sulfur recovery tail gas liquid phase treatment process, can obtain higher total sulfur yield, qualified discharge, simultaneously process simplification, saving construction investment, minimizing working cost and energy consumption.
Sulfur recovery tail gas liquid phase treatment process provided by the invention, carry out according to the following steps:
(1) sour gas produces sulphur tail gas processed after the claus sulphur recovery units recovery sulphur;
(2) sulphur tail gas processed enters the moisture film reactor, and all the reaction of sulfurous gas and excess hydrogen sulfide generates sulphur, produces to contain H
2S tail gas;
(3) contain H
2S tail gas directly contacts cooling with water, and the processing wastewater that condenses effluxes processing;
(4) contain H
2S tail gas enters the oxidation reactor oxidation, production process gas;
(5) Process Gas enters the cooling of sulphur cooler, then enters the moisture film reactor and further reacts;
(6) discharge behind the burned waste gas.
Wherein:
Sour gas adopts ripe one-level pyroreaction, the Claus unit sulfur recovery unit of two-stage catalyzed conversion, 95% sulfide in the sour gas is produced elementary sulfur reclaimed, and contains H in the sulphur tail gas processed of generation
2S, SO
2, N
2, CO
2Deng material.
The total reaction of Sulfur Recovery Unit can be expressed as:
Because complicated sour gas forms, and in the Reaktionsofen following side reaction may occur:
Because oxidation reactor can generate sulphur with the direct oxidation of hydrogen sulfide in the Process Gas, but helpless to sulfurous gas, so the control of claus reaction of the present invention requires from conventional different, require hydrogen sulfide little excessive, guarantee through no longer containing sulfurous gas in the Process Gas after the one-level moisture film reactor, since the hydrogen sulfide of 2mol can with the sulfurous gas complete reaction of 1mol, so the mol ratio of hydrogen sulfide in the step (2) and sulfurous gas is controlled at 3～4:1.In sulphur part secondary convertor outlet processed hydrogen sulfide/sulfurous gas on-line analysis instrument is set, to hydrogen sulfide, content of sulfur dioxide analysis in the Process Gas, the air capacity realization by control sulphur processed part is to the control of the mol ratio of hydrogen sulfide and sulfurous gas with reference to this equipment.The moisture film reactor is to utilize hydrogen sulfide and sulfurous gas that thoroughly reaction can occur in moisture film rapidly, and the sulfurous gas in the Process Gas is removed.
For guaranteeing that the moisture film reaction is thorough and rapidly, the temperature of moisture film reactor is controlled at 160～170 ℃ in the step (2).
The principal reaction of moisture film reactor is as follows:
2H
2S＋SO
2＝3S＋2H
2O……………………………………………………………(6)
The purpose of cooling is that the Molten sulphur cooling that will generate in the moisture film reaction forms fine-particle solid sulphur in the step (3), reclaims by pressure filter or vacuum filtration machine after the cooling.
Step contains H in (4)
2Enter the oxidation reactor that is filled with the direct oxidation catalyzer behind S tail gas heating to 190～210 ℃.The direct oxidation catalyzer is commercial, state inner catalyst supplier stock, and this catalyzer becomes sulphur with direct oxidation of hydrogen sulfide, is existing mature technology, and wherein about 95% direct oxidation of hydrogen sulfide becomes sulphur, and about 2% transform generation sulfurous gas.The Process Gas main component that step (4) produces is unoxidized H
2The SO of S and excessive oxidation
2
The principal reaction of oxidation reactor is as follows:
2H
2S＋O
2＝2S＋2H
2O……………………………………………………………(7)
The temperature of moisture film reactor is controlled at 160～170 ℃ in the step (5).
Step (6) waste gas is discharging after incinerator burns.
Compared with prior art, the present invention has the following advantages:
(1) utilize the moisture film reactor to solve the difficult problem that the sulphur mist captures, moisture film is reacted first Application in sulphur vent gas treatment processed, sulfur recovery rate has improved sulfur recovery rate greatly up to more than 99.98%;
(2) reduce-absorb the tediously long technological process for the treatment of technology with existing Claus tail-gas hydrogenation and compare, flow process shortens greatly, and construction investment, running cost and energy consumption reduce more than 30%.
Description of drawings
Fig. 1 is Crouse's sulfur recovery tail gas treatment process synoptic diagram.
Among the figure: 1-sulphur tail gas processed; 2-moisture film reactor; The 3-well heater; The 4-oxidation reactor; 5-sulphur cooler; The 6-water circulating pump; The 7-incinerator; The 8-chimney.
Embodiment
The invention will be further described below in conjunction with embodiment.
Embodiment 1
Sour gas produces sulphur tail gas processed after the claus sulphur recovery units recovery sulphur; The mol ratio of control hydrogen sulfide and sulfurous gas is at 3:1, and sulphur tail gas processed enters the moisture film reactor, and the temperature of reactor is controlled at 160 ± 3 ℃, and reaction generates sulphur, produces to contain H
2S tail gas; Contain H
2S tail gas directly contacts cooling with water, and the processing wastewater that condenses effluxes processing; Contain H
2S tail gas heating to 190 ± 3 ℃ enter oxidation reactor oxidation, production process gas; Process Gas enters the cooling of sulphur cooler, then enters the moisture film reactor and further reacts, and the temperature of moisture film reactor is controlled at 160 ± 3 ℃; Discharge behind the burned waste gas.Sulfur recovery rate is 99.98%.
Embodiment 2
Sour gas produces sulphur tail gas processed after the claus sulphur recovery units recovery sulphur; The mol ratio of control hydrogen sulfide and sulfurous gas is at 4:1, and sulphur tail gas processed enters the moisture film reactor, and the temperature of reactor is controlled at 170 ± 3 ℃, and reaction generates sulphur, produces to contain H
2S tail gas; Contain H
2S tail gas directly contacts cooling with water, and the processing wastewater that condenses effluxes processing; Contain H
2S tail gas heating to 210 ± 3 ℃ enter oxidation reactor oxidation, production process gas; Process Gas enters the cooling of sulphur cooler, then enters the moisture film reactor and further reacts, and the temperature of moisture film reactor is controlled at 170 ± 3 ℃; Discharge behind the burned waste gas.Sulfur recovery rate is 99.99%.
Embodiment 3
Sour gas produces sulphur tail gas processed after the claus sulphur recovery units recovery sulphur; The mol ratio of control hydrogen sulfide and sulfurous gas is at 3:1, and sulphur tail gas processed enters the moisture film reactor, and the temperature of reactor is controlled at 165 ± 3 ℃, and reaction generates sulphur, produces to contain H
2S tail gas; Contain H
2S tail gas directly contacts cooling with water, and the processing wastewater that condenses effluxes processing; Contain H
2S tail gas heating to 200 ± 3 ℃ enter oxidation reactor oxidation, production process gas; Process Gas enters the cooling of sulphur cooler, then enters the moisture film reactor and further reacts, and the temperature of moisture film reactor is controlled at 165 ± 3 ℃; Discharge behind the burned waste gas.Sulfur recovery rate is 99.98%.
Claims (5)
1. sulfur recovery tail gas liquid phase treatment process is characterized in that: carry out according to the following steps:
(1) sour gas produces sulphur tail gas processed after the claus sulphur recovery units recovery sulphur;
(2) sulphur tail gas processed enters the moisture film reactor, and all the reaction of sulfurous gas and excess hydrogen sulfide generates sulphur, produces to contain H
2S tail gas;
(3) contain H
2S tail gas directly contacts cooling with water, and the processing wastewater that condenses effluxes processing;
(4) contain H
2S tail gas enters the oxidation reactor oxidation, production process gas;
(5) Process Gas enters the cooling of sulphur cooler, then enters the moisture film reactor and further reacts;
(6) discharge behind the burned waste gas.
2. sulfur recovery tail gas liquid phase treatment process according to claim 1 is characterized in that: the mol ratio of hydrogen sulfide and sulfurous gas is at 3～4:1 in the step (2).
3. sulfur recovery tail gas liquid phase treatment process according to claim 1, it is characterized in that: the temperature of step (2) moisture film reactor is controlled at 160～170 ℃.
4. sulfur recovery tail gas liquid phase treatment process according to claim 1, it is characterized in that: step contains H in (4)
2Enter the direct oxidation reactor behind S tail gas heating to 190～210 ℃.
5. sulfur recovery tail gas liquid phase treatment process according to claim 1, it is characterized in that: the temperature of step (5) moisture film reactor is controlled at 160～170 ℃.
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|---|---|---|---|
| CN201210517556.9A CN102942162B (en) | 2012-12-06 | 2012-12-06 | Liquid-phase treatment process of tail gas from sulfur recovery |
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|---|---|---|---|
| CN201210517556.9A CN102942162B (en) | 2012-12-06 | 2012-12-06 | Liquid-phase treatment process of tail gas from sulfur recovery |
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| CN102942162B CN102942162B (en) | 2014-08-13 |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10106410B2 (en) | 2017-03-10 | 2018-10-23 | Saudi Arabian Oil Company | Enhancement of Claus tail gas treatment by sulfur dioxide-selective membrane technology |
| US10106411B2 (en) * | 2017-03-13 | 2018-10-23 | Saudi Arabian Oil Company | Enhancement of claus tail gas treatment by sulfur dioxide-selective membrane technology and sulfur dioxide-selective absorption technology |
| US10343110B2 (en) | 2017-05-25 | 2019-07-09 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10357741B2 (en) | 2017-09-07 | 2019-07-23 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
| US10399033B2 (en) | 2017-05-25 | 2019-09-03 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desulfurization process and apparatus |
| US10406477B2 (en) | 2017-03-15 | 2019-09-10 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
| US10421040B2 (en) | 2017-07-03 | 2019-09-24 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10583386B2 (en) | 2017-06-14 | 2020-03-10 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US10953365B2 (en) | 2018-07-20 | 2021-03-23 | Jiangnan Environmental Protection Group Inc. | Acid gas treatment |
| US11027234B2 (en) | 2018-04-13 | 2021-06-08 | Jiangnan Environmental Protection Group Inc. | Oxidization of ammonia desulfurization solution |
| US11224838B2 (en) | 2019-12-26 | 2022-01-18 | Jiangnan Environmental Protection Group Inc. | Controlling aerosol production during absorption in ammonia-based desulfurization |
Families Citing this family (1)
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| US9370745B2 (en) | 2013-04-24 | 2016-06-21 | Jiangsu New Century Jiangnan Environmental Protection Co., Ltd | Flue gas-treating method and apparatus for treating acidic tail gas by using ammonia process |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2408952Y (en) * | 1999-12-17 | 2000-12-06 | 梅家明 | Efficient water dedusting devulcanizer |
| US20020022568A1 (en) * | 1993-12-08 | 2002-02-21 | Richard Mackay | Ceramic membranes for use in catalytic membrane reactors with high ionic conductivities and improved mechanical properties |
| CN101289170A (en) * | 2008-06-13 | 2008-10-22 | 西安思瑞迪精馏工程有限公司 | Oxidation, reduction and sulfur recovery multipurpose device |
| CN101585511A (en) * | 2009-06-25 | 2009-11-25 | 中国石油化工集团公司 | Sulfur recycling technique |
-
2012
- 2012-12-06 CN CN201210517556.9A patent/CN102942162B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020022568A1 (en) * | 1993-12-08 | 2002-02-21 | Richard Mackay | Ceramic membranes for use in catalytic membrane reactors with high ionic conductivities and improved mechanical properties |
| CN2408952Y (en) * | 1999-12-17 | 2000-12-06 | 梅家明 | Efficient water dedusting devulcanizer |
| CN101289170A (en) * | 2008-06-13 | 2008-10-22 | 西安思瑞迪精馏工程有限公司 | Oxidation, reduction and sulfur recovery multipurpose device |
| CN101585511A (en) * | 2009-06-25 | 2009-11-25 | 中国石油化工集团公司 | Sulfur recycling technique |
Cited By (28)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US10508033B2 (en) | 2017-03-10 | 2019-12-17 | Saudi Arabian Oil Company | Enhancement of claus tail gas treatment by sulfur dioxide-selective membrane technology |
| US10106410B2 (en) | 2017-03-10 | 2018-10-23 | Saudi Arabian Oil Company | Enhancement of Claus tail gas treatment by sulfur dioxide-selective membrane technology |
| US10106411B2 (en) * | 2017-03-13 | 2018-10-23 | Saudi Arabian Oil Company | Enhancement of claus tail gas treatment by sulfur dioxide-selective membrane technology and sulfur dioxide-selective absorption technology |
| CN110621389A (en) * | 2017-03-13 | 2019-12-27 | 沙特阿拉伯石油公司 | Optimizing Claus tail gas treatment by sulfur dioxide selective membrane technology and sulfur dioxide selective absorption technology |
| US10479684B2 (en) | 2017-03-13 | 2019-11-19 | Saudi Arabian Oil Compnay | Enhancement of claus tail gas treatment by sulfur dioxide-selective membrane technology and sulfur dioxide-selective absorption technology |
| US10413864B2 (en) | 2017-03-15 | 2019-09-17 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
| US10675584B2 (en) | 2017-03-15 | 2020-06-09 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
| US10406477B2 (en) | 2017-03-15 | 2019-09-10 | Jiangnan Environmental Protection Group Inc. | Method and apparatus for removing sulfur oxides from gas |
| US10406478B2 (en) | 2017-05-25 | 2019-09-10 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desulfurization process and apparatus |
| US10399033B2 (en) | 2017-05-25 | 2019-09-03 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desulfurization process and apparatus |
| US10343110B2 (en) | 2017-05-25 | 2019-07-09 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10413865B2 (en) | 2017-05-25 | 2019-09-17 | Jiangnan Enviromental Protection Group Inc. | Ammonia-based desulfurization process and apparatus |
| US10561982B2 (en) | 2017-05-25 | 2020-02-18 | Jiangnan Environmental Protection Group Inc. | Ammonia-based desulfurization process and apparatus |
| US10471383B2 (en) | 2017-05-25 | 2019-11-12 | Jiangnan Environmental Protection Group Inc. | Dust removal and desulfurization of FCC exhaust gas |
| US10589212B2 (en) | 2017-06-14 | 2020-03-17 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US10583386B2 (en) | 2017-06-14 | 2020-03-10 | Jiangnan Environmental Protection Group Inc. | Ammonia-adding system for ammonia-based desulfurization device |
| US10427097B2 (en) | 2017-07-03 | 2019-10-01 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10421040B2 (en) | 2017-07-03 | 2019-09-24 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10556205B2 (en) | 2017-07-03 | 2020-02-11 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10618001B2 (en) | 2017-07-03 | 2020-04-14 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10561984B2 (en) | 2017-07-03 | 2020-02-18 | Jiangnan Environmental Protection Group Inc. | Desulfurization absorption tower |
| US10449488B2 (en) | 2017-09-07 | 2019-10-22 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
| US10369517B2 (en) | 2017-09-07 | 2019-08-06 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
| US10357741B2 (en) | 2017-09-07 | 2019-07-23 | Jiangnan Environmental Protection Group Inc. | Method for controlling aerosol production during absorption in ammonia desulfurization |
| US11027234B2 (en) | 2018-04-13 | 2021-06-08 | Jiangnan Environmental Protection Group Inc. | Oxidization of ammonia desulfurization solution |
| US10953365B2 (en) | 2018-07-20 | 2021-03-23 | Jiangnan Environmental Protection Group Inc. | Acid gas treatment |
| US11529584B2 (en) | 2018-07-20 | 2022-12-20 | Jiangnan Environmental Protection Group Inc. | Acid gas treatment |
| US11224838B2 (en) | 2019-12-26 | 2022-01-18 | Jiangnan Environmental Protection Group Inc. | Controlling aerosol production during absorption in ammonia-based desulfurization |
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Address after: No. 22, middle refinery Road, Linzi District, Zibo City, Shandong Province, 255400 Patentee after: Shandong Sanwei Chemical Group Co.,Ltd. Address before: No. 22, middle refinery Road, Linzi District, Zibo City, Shandong Province, 255400 Patentee before: SHANDONG SUNWAY PETROCHEMICAL ENGINEERING Co.,Ltd. |