CN102838088B - Integrated sour gas treating process - Google Patents
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Abstract
The invention discloses an integrated sour gas treating process, and aims at the sour gas which contains light concentration H2S and is generated in a desulfuration decarburization device. The integrated sour gas treating process comprises the following steps of: adding a sour gas concentrating segment before a two-level Claus sulfur recovery segment, concentrating the H2S concentration in sour gas to more than 50%, and enabling the sour gas after concentrating to enter the two-level Claus sulfur recovery segment to carry out reaction, wherein the sulphur recovery rate of a sour gas concentrating + sulfur recovery segment is improved by 1%-2% compared with the general two-level Claus sulfur recovery segment, thereby being beneficial for sulfur recovery to obtain high sulfur recovery ratio. The integration sour gas treating process provided by the invention has the advantages that the technological operation is flexible and reliable, the investment is saved, the energy consumption is low, the total sulfur recovery ratio can achieve more than 99.8%, and the strict environmental standard requirements are met.
Description
Technical field
What the present invention relates to is a kind ofly for gas-processing plant, to process containing lower concentration H
2the acid gas integrating technology of S.
Background technology
For containing H
2the Sweet natural gas of S gas field output, generally adopt amine method and sulfone amine method to remove the H in Sweet natural gas
2s, yet the H that contains that desulfuration solution is regenerated and separated out
2the acid gas of S, must process after reaching the environmental emission standard and can discharge.Usually according to H in the separated out acid gas of regenerating in the desulfurization and decarburization process
2the number of the content of S is selected the acid gas treatment process.
Generally speaking, for H
2s content is greater than the higher concentration acid gas of 50mol %, mostly enters Crouse (Claus) device and adopts flow-through method that hydrogen sulfide is converted into to elemental sulfur.The principal feature of flow-through method is that whole acid gas enter the roasting kiln reaction together with the air of allocating on demand, pass through waste heat boiler, two-stage or more catalytic conversion reactor and corresponding sulphur condensation water cooler, after trapping sulphur, reclamation tail gas burning is emptying or enter exhaust gas processing device again.The advantage of this method maximum is in roasting kiln, to have the elementary sulfur of 60%-70% to generate, and this has just greatly alleviated the conversion load of catalytic section and has contributed to improve sulfur recovery rate.
At present for H
2s content is less than the low concentration acid gas of 50mol %, and technique commonly used mainly contains Claus shunting process, Lo-Cat technique and alkali absorb method etc.H in acid gas
2s concentration can adopt the Claus shunting process higher than 15% the time again lower than 50%, and typical shunting process makes 1/3 of acid gas amount enter with the air of metering the H that roasting kiln will be wherein
2s changes into SO fully
2, this strand of air-flow is mixed into catalytic conversion stage with 2/3 other acid gas after waste heat boiler, and in this kind of technique, sulphur is in catalytic section, to generate fully.The sulfur recovery rate of conventional two-stage Claus device is at 95%-97%, can improve to a certain extent sulfur recovery rate though further increase the conversion progression of Claus device itself, but the cost expended is high and be difficult to reach desired total sulfur yield, therefore the strict area for environmental protection standard, usual method is to set up exhaust gas processing device after the conventional Claus device of two-stage, by the SO in Claus tail gas
2deng being reduced into H
2s, improve H in tail gas through an absorption and regeneration technique afterwards
2s concentration, then by the H of concentrate
2s sends the Claus device back to and reclaims sulphur.For processing lower concentration H
2the acid gas of S, this kind of Claus shunting+tail gas treatment process can reach the total sulfur recovery more than 99.5%, meets very strict environmental requirement.The shortcoming of this technique is because the part acid gas directly enters catalytic conversion stage without roasting kiln, and while containing the impurity such as heavy hydrocarbon, especially aromatic hydrocarbon in acid gas, they may pollute catalyzer, causes catalyst activity to reduce, shorten its work-ing life.
Lo-Cat technique is a kind of redox process of processing the lower concentration acid gas, and it adopts the two chelated iron catalyzer of distinctive environment-friendly type H
2s transforms into nontoxic elemental sulfur.Overall process is: H
2s+1/
2o
2→ H
2o+S(solid).Oxygen in this reaction is provided by the air that blasts catalyst solution.Without consuming the chelated iron catalyzer, so need only in reaction, add appropriate catalyzer to supplement the catalyst loss caused because of mechanical reason due to reaction process.In addition, also need to add micro-alkaline matter to keep the pH value of solution value to be slightly alkalescence, add a small amount of sequestrant to supplement the sequestrant decomposed in time.The total sulfur recovery of Lo-Cat technique can reach more than 99.5%, also can meet very strict environmental requirement.With other acid gas processing device, compare, Lo-Cat process unit running cost is higher, and is difficult to operation, and the sulfur product of production is difficult to meet sells requirement, and market application foreground is not very wide in general.
Alkali absorb method is mainly usingd basic solution as the absorption agent of sour gas, and this method can remove sour gas effectively, also can reach higher environmental requirement.Its main drawback is that alkali lye consumption alkali lye large, that absorbed sour gas causes secondary pollution, and is only applicable to process the acid gas of the low sulfur content of diving, and current this method seldom is applied in the Sweet natural gas process and processes in acid gas.
For above-mentioned Claus shunting process and Lo-Cat technique to processing H in acid gas
2the restriction of S concentration, improve H in acid gas
2the concentration of S is to meet the requirement (H of Claus DC processes to concentration
2s>50%) become a main direction of current process modification.
Summary of the invention
In order to overcome the above-mentioned shortcoming of prior art, the invention provides a kind of integrated acid gas treatment process.
The technical solution adopted for the present invention to solve the technical problems is: a kind of integrated acid gas treatment process, comprise acid gas enriching section, sulphur recovery section and vent gas treatment section, wherein:
One, acid gas enriching section:
Low H
2at first the acid gas of S concentration enters methyldiethanolamine solution in ， absorption tower, absorption tower and absorbs the H in acid gas
2s, unabsorbed acid gas is discharged by the absorption tower tower top, removes incinerator; The rich amine liquid gone out by absorber column bottoms stream enters regenerator column after poor rich liquid heat exchanger cooling, in regenerator column desorb H
2the poor amine liquid of S goes out through tower bottom flow, and after reboiler, a part returns to regenerator column, and another part enters the poor rich liquid heat exchanger precooling, and the temperature after precooling is down to 92.6 ℃ by 125.8 ℃, then with the amine liquid from the storage tank preparation, together returns in absorption tower; Regenerator column tower top expellant gas enters return tank after condenser condenses, and in return tank, acid gas is separated with phlegma, and the phlegma after separation refluxes and enters regenerator column, simultaneously, and H
2s concentration>acid gas of 50 mol% enters the sulphur recovery section after the acid gas separator separates;
Two, sulphur recovery section:
From the acid gas enriching section out containing high density H
2the acid gas of S directly enters the roasting kiln of sulphur recovery section, most of H in roasting kiln after the gas-liquid separation of acid gas separator
2s changes S into
2from roasting kiln, Process Gas out enters waste heat boiler and oiler feed indirect heat exchange, enter first-stage condenser after making Process Gas be cooled to 300 ℃ and further be cooled to 175 ℃, then be warming up to through the one-level reheater A reactor that enters the Claus catalytic section after 270 ℃, complete H
2the conversion reaction of S and sulphur and COS, CS
2hydrolysis reaction; During in Claus catalytic section A reactor, reacted Process Gas enters secondary condenser, a part separates molten sulfur for condensation, another part is through the heat exchange of secondary reheater, by the second reactor that enters the Claus catalytic section after 175 ℃ of heat exchange to 200 ℃, further reacted, reacted Process Gas enters the last condenser stage condensation and separates molten sulfur, and the tail gas of generation enters the vent gas treatment section after online roasting kiln burning;
Three, vent gas treatment section:
Gas after the online roasting kiln burning of sulphur recovery section enters the reaction of hydrogenation reduction device, and the sulphur of various forms in Claus tail gas is converted into to H
2s, Process Gas is chilled to 175 ℃ in advance through pre-cooler afterwards, then enters quench tower, enters the acid gas enriching section after continuing to be cooled to 40 ℃.
Compared with prior art, positively effect of the present invention is: for the desulfurization and decarburization device, produce containing lower concentration H
2the acid gas of S had increased the acid gas enriching section, by H in acid gas before two-stage Claus sulphur recovery section
2more than S concentration concentrate to 50%, acid gas after concentrate enters two-stage Claus sulphur recovery section again and is reacted, the sulfur recovery rate of acid gas concentrate+sulphur recovery section has improved 1%-2% than conventional two-stage Claus sulphur recovery section, not only is conducive to sulphur recovery, to obtain high sulfur recovery rate; And technological operation of the present invention flexibly, reliable, reduced investment, energy consumption are low, total sulfur recovery rate all can reach more than 99.8%, meets very strict environmental protection standard requirement.
The accompanying drawing explanation
Examples of the present invention will be described by way of reference to the accompanying drawings, wherein:
Fig. 1 is process flow sheet of the present invention;
Fig. 2 is the process flow sheet of the embodiment of the present invention one;
Fig. 3 is the process flow sheet of the embodiment of the present invention two;
Fig. 4 is the process flow sheet of the embodiment of the present invention three.
Embodiment
As shown in Figures 1 to 4, the related device of technique of the present invention comprises: absorption tower (ABT) 1, incinerator (INCT) 2, poor rich liquid heat exchanger (EXG) 3, regenerator column (RET) 4, condenser (CL1) 5, return tank (SEP) 6, roasting kiln (RF) 7, waste heat boiler (WHE) 8, first-stage condenser (CD1) 9, one-level reheater (RH1) 10, A reactor (CV1) 11, secondary condenser (CD2) 12, secondary reheater (RH2) 13, second reactor (CV2) 14, last condenser stage (CD3) 15, online roasting kiln (RGG) 16, hydrogenation reduction device (HBED) 17, pre-cooler (CL2) 18, quench tower (QTWR) 19, small-sized acid gas concentration unit (ABSA) 20, amine absorption tower (ABT2) 21, compressor (CMP) 22, storage tank (AMT) 23 etc.
The objective of the invention is the lower concentration H produced for deep natural gas desulfurization and decarburization process
2s acid gas operating mode, the acid gas treatment process of special exploitation.
As shown in Figure 1, integrated acid gas treatment process of the present invention comprises acid gas enriching section, sulphur recovery section and vent gas treatment section, and the concrete technology flow process is as follows:
One, acid gas enriching section:
Low H
2at first the acid gas of S concentration enters absorption tower 1, the H in the interior methyldiethanolamine in absorption tower 1 (MDEA) solution optionally absorbs acid gas
2s, unabsorbed acid gas is discharged by the absorption tower tower top, removes incinerator 2; The rich amine liquid gone out by absorber column bottoms stream enters regenerator column 4 after poor rich liquid heat exchanger 3 cooling, in regenerator column 4 interior desorbs H
2the poor amine liquid of S goes out through tower bottom flow, after reboiler (REB), a part returns to regenerator column 4, and another part enters poor rich liquid heat exchanger 3 precoolings, temperature after precooling is down to 92.6 ℃ by 125.8 ℃, then with the fresh amine liquid from storage tank (AMT) preparation, together returns in absorption tower 1; Regenerator column 4 tower top expellant gas enter return tank 6 after condenser 5 condensations, at the interior acid gas of return tank 6, with phlegma, are separated, and the phlegma after separation refluxes and reenters regenerator column 4, simultaneously, and containing high density H
2s(>50 mol%) acid gas enter the sulphur recovery section after the acid gas separator separates;
Two, sulphur recovery section:
From the acid gas enriching section out containing high density H
2s(>50 mol%) acid gas directly enter the roasting kiln 7 of sulphur recovery section, most of H in roasting kiln after the gas-liquid separation of acid gas separator
2s changes S into
2from roasting kiln, Process Gas out enters waste heat boiler 8 and oiler feed indirect heat exchange, enter first-stage condenser 9 after making Process Gas be cooled to 300 ℃ and further be cooled to 175 ℃, then be warming up to through one-level reheater 10 A reactor 11 that enters the Claus catalytic section after 270 ℃, complete H
2the conversion reaction of S and sulphur and COS, CS
2hydrolysis reaction; In the interior reacted Process Gas of Claus catalytic section A reactor 11 enters secondary condenser 12, a part separates molten sulfur for condensation, another part is through 13 heat exchange of secondary reheater, by the second reactor 14 that enters the Claus catalytic section after 175 ℃ of heat exchange to 200 ℃, further reacted, reacted Process Gas enters last condenser stage 15 condensations and separates molten sulfur, and the tail gas of generation enters the vent gas treatment section after online roasting kiln 16 burnings;
Three, vent gas treatment section:
Gas after online roasting kiln 16 burnings of sulphur recovery section enters 17 reactions of hydrogenation reduction device, and the sulphur of various forms in Claus tail gas is converted into to H
2s, Process Gas is chilled to 175 ℃ in advance through pre-cooler 18 afterwards, then enters quench tower 19, enters the acid gas enriching section after continuing to be cooled to 40 ℃.
The present invention also integrates acid gas enriching section, sulphur recovery section and vent gas treatment section, has proposed following three kinds and has further improved technique:
improve technique I:
As shown in Figure 2, the tail gas be cooled to 40 ℃ from the quench tower 19 of vent gas treatment section first passes through small-sized acid gas concentration unit 20, enters incinerator 2 by the absorption tower tail gas out of small-sized acid gas concentration unit 20 and burns and enter atmosphere by chimney (STK); The roasting kiln 7 that the acid gas of being discharged by the regenerator column tower top of small-sized acid gas concentration unit 20 both can enter the sulphur recovery section further reclaims sulphur, the further concentrate in absorption tower 1 that also can enter the acid gas enriching section.The absorption liquid part on its middle-size and small-size acid gas concentration unit 20 absorption towers is from the regenerated liquid of its regenerator column, and a part is from the fresh amine liquid of same storage tank 23 preparations in addition.
Improve the acid gas enriching section of technique I and vent gas treatment section and share a kind of selective desulfurization solvent (MDEA fill a prescription solvent), greatly saved installation cost and operation cost; Secondly, according to the situation of the sulfur recovery rate of Real-Time Monitoring, but the tail gas desulfuration sulphur recovery zone that the vent gas treatment section produces through small-sized acid gas concentration unit continue to reclaim sulphur, also can return to the further concentrate of acid gas enriching section.
improve technique II:
As shown in Figure 3, from the quench tower 19 of vent gas treatment section, be cooled to tail gas 40 ℃ through amine absorption tower 21, the rich amine liquid gone out from amine absorption tower 21 tower bottom flows directly enters the regenerator column 4 of acid gas enriching section.
The vent gas treatment section and the acid gas enriching section that improve technique II can share (amine liquid) regenerator column 4, have saved investment cost.
improve technique III:
As shown in Figure 4, concentrate is carried out on the absorption tower 1 that directly enters the acid gas enriching section after the quench tower 19 of vent gas treatment section is cooled to compressed machine 22 superchargings of tail gas 40 ℃.
The vent gas treatment section and the acid gas enriching section that improve technique III can share a set of absorption-regeneration concentration unit, have greatly saved cost of investment and running cost.
Take and improve technique I and principle of the present invention is described as follows as example below in conjunction with concrete operations:
(1) acid gas enriching section:
The 1st step, the acid gas (T=40 ℃, P=0.17 MPa(g) out from the desulfurization and decarburization device, H
2s:26.033 mol%, CO
2: 67.969 mol%) by absorption tower 1 bottom pipeline, entered, the absorption agent in absorption tower (ABT) is the MDEA aqueous solution (45mol%), and this solvent can selectivity absorb the H in acid gas
2s.
The 2nd step, absorbed H
2the rich amine liquid of S (T=52.6 ℃, P=0.16 MPa(g), MDEA:86.841 mol %, H
2s:2.655 mol%, CO
2: 2.1796 mol%) from absorption tower, flow out on 1 tower bottom tube road.
The 3rd step, be not absorbed the gas (T=25.7 ℃, P=0.14 MPa(g) that tower absorbs, CO acid gas out from the desulfurization and decarburization device
2: 94.35 mol%) pipeline by the top, absorption tower removes incinerator (INCT) 2.
The 4th step, from the rich amine liquid (T=79.6 ℃, P=0.22 MPa(g) after interchanger (EXG) 3 heat exchange of discharging at the bottom of absorbing tower, H
2s:2.655 mol%, CO
2: 2.1796 mol%) by pipeline, enter regenerator column 4 regeneration.
The 5th step, from the liquid (T=125.1 ℃, P=0.22 MPa(g) of discharging at the bottom of the regenerator column tower, H
2s:0.0178 mol%, CO
2: 0.0227 mol%), H
2o:92.34 mol %, MDEA:7.62 mol %.) through reboiler (REB) rear portion (T=125.1 ℃, P=0.22 MPa(g), H
2s:0.0236 mol%, CO
2: 0.0779 mol%, H
2o:99.845 mol %) return to regenerator column, another part (P=0.22 MPa(g), H
2s:0.0167 mol%, CO
2: 0.0115 mol%, MDEA:9.15 mol %, H
2o:90.82 mol %) enter rich or poor interchanger (EXG) 3 precoolings, the poor amine liquid temp after precooling is down to 92.6 ℃ by 125.8 ℃.
The 6th step, the fresh amine liquid (from storage tank AMT) of the poor amine liquid after precooling and preparation together returns to absorption tower.
The 7th step, from regenerator column tower top expellant gas (T=93.4 ℃, P=0.2 MPa(g), H
2s:32.66 mol%, CO
2: 26.8 mol%), after entering condenser (CL1) condensation by pipeline, enter return tank (SEP), in tank, acid gas is separated with water of condensation.Acid gas (T=48.9 ℃, P=0.19 MPa(g), H
2s:51.38 mol%, CO
2: 42.22 mol%) enter by the road the sulphur recovery section; Water of condensation (T=48.9 ℃, P=0.19 MPa(g), H
2s:0.1135 mol%, CO
2: 0.281 mol%, H
2o:99.845 mol %) reenter by the road regenerator column.
The 8th step, the acid gas (T=48.9 ℃, P=0.19 MPa(g) out from the acid gas enriching section, H
2s:51.38 mol%, CO
2: 42.22 mol%) after the further gas-liquid separation of acid gas separator, directly enter the roasting kiln (RF) of sulphur recovery section, the main reaction occurred in roasting kiln under 955 ℃ is:
The high temperature of roasting kiln is mainly maintained by reaction (1) liberated heat, adopts flow-through method that the H of 60%-70% is arranged in roasting kiln
2s is converted into S
2.In roasting kiln, except main reaction, also have complicated side reaction to occur, comprise oxidizing reaction, the H of hydro carbons in acid gas
2the scission reaction of S and organosulfur (COS and CS
2) formation reaction etc., mainly comprise following reaction:
（3）
The 9th step, enter the middle pressure steam of waste heat boiler (WHE) and oiler feed (T=120 ℃) indirect heat exchange (producing 3.3MPa(g) from Process Gas out in roasting kiln) make Process Gas be cooled to 300 ℃ to enter condenser (CD1) by pipeline, further be cooled to 175 ℃, be warming up to 270 ℃ after interchanger (RH1), enter by the road the A reactor (CV1) of Claus catalytic section.Catalyst reaction section is selected titania-based catalyst, completes H
2the conversion reaction of S and sulphur and COS, CS
2hydrolysis reaction.The catalyst reaction section main reaction is:
In addition, also have a series of hydrolysis reaction to occur:
（10）
The 10th step, enter the low-pressure steam of condenser (CD2) (producing Pg=0.6MPa(g) by the road from reacted Process Gas in Claus catalytic section A reactor) condensation, the reaction occurred in condensation process has:
（11）
The molten sulfur that condensation obtains separates and enters the molten sulfur pond, and the gas of complete reaction does not enter the second reactor (CV2) of Claus catalytic section by 175 ℃ of heat exchange to 200 ℃ by pipeline through interchanger (RH2).
The 11st step, Process Gas enters Claus catalytic section second reactor by pipeline, and in second reactor, lower temperature is beneficial to the direction that reaction (8) generates along sulphur and carries out, and has improved the sulphur transformation efficiency.The Process Gas completed after catalyzed reaction enters the vapor pressure of condenser (CD3) (producing P=0.1MPa(g) by the road) condensation, condensing temperature T=127 ℃, (11), (12), (13) react in condensation process, condensed molten sulfur is sent into the molten sulfur pond, through acid gas concentrate, two-stage Claus reaction, sulfur recovery rate is promoted to 97%, than the rate of recovery of simple two-stage Claus sulphur recovery section, has promoted 0.1-0.2%.
The 12nd step, the tail gas of process condenser (CD3) enters online roasting kiln (RGG) by pipeline, and the reaction occurred in roasting kiln is:
(14);
(15).Gas after burning (mainly comprises CO, H
2, CO
2, SO
2, H
2s, H
2o) enter the vent gas treatment section by pipeline.
The 13rd step, the gas after online roasting kiln burning enters hydrogenation reduction device (HBED) (T=285 ℃, P=0.018MPa(g) by the road), the sulphur of various forms in Claus tail gas is converted into to H
2s, in this process, SO
2with elementary sulfur are all hydrogenation reactions, hydrolysis reaction mainly occurs in organosulfur, reaction equation is as follows:
The 14th step, by hydrogenation reduction device (HBED), (main component is H for Process Gas out
2s and CO
2) enter by the road pre-cooler, be chilled in advance 175 ℃.
The 15th step, through pre-cooler, cooling gas enters quench tower (QTWR) by the road, and quench tower (QTWR) continues cooling gas to 40 ℃ and enters small-sized acid gas upgrading system (ABSA) by pipeline.
The 16th step, enter by the road incinerator (INCT) burning by small-sized acid gas upgrading system (ABSA) absorption tower tail gas out and enter atmosphere by chimney (STK); Acid gas (the H discharged by small-sized acid gas upgrading system (ABSA) regenerator column tower top
2s:15mol%, CO
2: 77mol%; T=55 ℃, P=0.081MPa(g)) both having entered by the road the Claus recovery zone further reclaims sulphur, also can enter by the road the further concentrate of acid gas enriching section.The absorption liquid part on its middle-size and small-size acid gas upgrading system (ABSA) absorption tower is from the regenerated liquid of its regenerator column, and a part is from the fresh amine liquid of same storage tank (AMT) preparation in addition.
Claims (5)
1. an integrated acid gas treatment process is characterized in that: comprise acid gas enriching section, sulphur recovery section and vent gas treatment section, wherein:
One, acid gas enriching section:
Low H
2at first the acid gas of S concentration enters methyldiethanolamine solution in ， absorption tower, absorption tower and absorbs the H in acid gas
2s, unabsorbed acid gas is discharged by the absorption tower tower top, removes incinerator; The rich amine liquid gone out by absorber column bottoms stream enters regenerator column after poor rich liquid heat exchanger cooling, in regenerator column desorb H
2the poor amine liquid of S goes out through tower bottom flow, and after reboiler, a part returns to regenerator column, and another part enters the poor rich liquid heat exchanger precooling, and the temperature after precooling is down to 92.6 ℃ by 125.8 ℃, then with the amine liquid from the storage tank preparation, together returns in absorption tower; Regenerator column tower top expellant gas enters return tank after condenser condenses, and in return tank, acid gas is separated with phlegma, and the phlegma after separation refluxes and enters regenerator column, simultaneously, and H
2s concentration>acid gas of 50 mol% enters the sulphur recovery section after the acid gas separator separates;
Two, sulphur recovery section:
From the acid gas enriching section out containing high density H
2the acid gas of S directly enters the roasting kiln of sulphur recovery section, most of H in roasting kiln after the gas-liquid separation of acid gas separator
2s changes S into
2from roasting kiln, Process Gas out enters waste heat boiler and oiler feed indirect heat exchange, enter first-stage condenser after making Process Gas be cooled to 300 ℃ and further be cooled to 175 ℃, then be warming up to through the one-level reheater A reactor that enters the Claus catalytic section after 270 ℃, complete H
2the conversion reaction of S and sulphur and COS, CS
2hydrolysis reaction; During in Claus catalytic section A reactor, reacted Process Gas enters secondary condenser, a part separates molten sulfur for condensation, another part is through the heat exchange of secondary reheater, by the second reactor that enters the Claus catalytic section after 175 ℃ of heat exchange to 200 ℃, further reacted, reacted Process Gas enters the last condenser stage condensation and separates molten sulfur, and the tail gas of generation enters the vent gas treatment section after online roasting kiln burning;
Three, vent gas treatment section:
Gas after the online roasting kiln burning of sulphur recovery section enters the reaction of hydrogenation reduction device, and the sulphur of various forms in Claus tail gas is converted into to H
2s, Process Gas is chilled to 175 ℃ in advance through pre-cooler afterwards, then enters quench tower, enters the acid gas enriching section after continuing to be cooled to 40 ℃.
2. integrated acid gas treatment process according to claim 1, it is characterized in that: the Process Gas be cooled to 40 ℃ from the quench tower of vent gas treatment section first passes through small-sized acid gas concentration unit, enters incinerator by the absorption tower tail gas out of small-sized acid gas concentration unit and burns and enter atmosphere by chimney; The roasting kiln that the acid gas of being discharged by the regenerator column tower top of small-sized acid gas concentration unit enters the sulphur recovery section further reclaims sulphur, or enters the further concentrate in absorption tower of acid gas enriching section.
3. integrated acid gas treatment process according to claim 2 is characterized in that: the absorption liquid part on described small-sized acid gas concentration unit absorption tower is from the regenerated liquid of its regenerator column, and a part is from the amine liquid of storage tank preparation in addition.
4. integrated acid gas treatment process according to claim 1, it is characterized in that: the Process Gas be cooled to 40 ℃ from the quench tower of vent gas treatment section is introduced into the amine absorption tower, and the rich amine liquid gone out from amine absorption tower tower bottom flow directly enters the regenerator column of acid gas enriching section.
5. integrated acid gas treatment process according to claim 1 is characterized in that: concentrate is carried out on the absorption tower that directly enters the acid gas enriching section after the quench tower of vent gas treatment section is cooled to the compressed machine supercharging of Process Gas 40 ℃.
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| CN103979500B (en) * | 2014-05-21 | 2015-09-09 | 中国石油集团工程设计有限责任公司 | The sulphur recovery of comprehensive hydrogen manufacturing and exhaust treatment system and technique |
| CN105776148B (en) * | 2016-04-08 | 2018-03-13 | 中国石油工程建设有限公司 | A kind of sulfur recovery facility and method suitable for big operating flexibility |
| CN106115632B (en) * | 2016-06-28 | 2018-09-14 | 山东三维石化工程股份有限公司 | Improve the device and its recovery method of sulfur recovery rate |
| CN110548370A (en) * | 2019-09-04 | 2019-12-10 | 大连理工大学 | Acid gas purification process and device for producing hydrogen sulfide with various purities |
| CN110713175A (en) * | 2019-10-17 | 2020-01-21 | 山西潞安煤基清洁能源有限责任公司 | Method and device for improving sulfur recovery efficiency |
| CN113122345A (en) * | 2019-12-30 | 2021-07-16 | 中国石油化工股份有限公司 | System and method for treating high-sulfur natural gas |
| CN113860266B (en) * | 2020-06-30 | 2023-06-16 | 中国石油化工股份有限公司 | Method for starting sulfur recovery process |
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| CN101508905A (en) * | 2008-11-15 | 2009-08-19 | 中国石油化工股份有限公司荆门分公司 | Desulfurization process for removing hydrogen sulphide from solvent |
| CN102451608A (en) * | 2010-10-18 | 2012-05-16 | 袁俊海 | Tail gas treatment process applicable to natural gas with high sulfur |
| CN102580473A (en) * | 2012-03-20 | 2012-07-18 | 中国石油化工股份有限公司 | Absorbent for selectively removing H2S and organic sulfur |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101508905A (en) * | 2008-11-15 | 2009-08-19 | 中国石油化工股份有限公司荆门分公司 | Desulfurization process for removing hydrogen sulphide from solvent |
| CN102451608A (en) * | 2010-10-18 | 2012-05-16 | 袁俊海 | Tail gas treatment process applicable to natural gas with high sulfur |
| CN102580473A (en) * | 2012-03-20 | 2012-07-18 | 中国石油化工股份有限公司 | Absorbent for selectively removing H2S and organic sulfur |
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