CN102556977B - Inner-cooling type direct oxidation sulfur recovery method and device - Google Patents
Inner-cooling type direct oxidation sulfur recovery method and device Download PDFInfo
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- CN102556977B CN102556977B CN2010106164331A CN201010616433A CN102556977B CN 102556977 B CN102556977 B CN 102556977B CN 2010106164331 A CN2010106164331 A CN 2010106164331A CN 201010616433 A CN201010616433 A CN 201010616433A CN 102556977 B CN102556977 B CN 102556977B
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 92
- 238000000034 method Methods 0.000 title claims abstract description 89
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 62
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 61
- 239000011593 sulfur Substances 0.000 title claims abstract description 60
- 230000003647 oxidation Effects 0.000 title claims abstract description 56
- 238000011084 recovery Methods 0.000 title claims abstract description 29
- 238000001816 cooling Methods 0.000 title abstract description 5
- 239000007789 gas Substances 0.000 claims abstract description 95
- 238000006243 chemical reaction Methods 0.000 claims abstract description 65
- 230000008569 process Effects 0.000 claims abstract description 47
- 239000003054 catalyst Substances 0.000 claims abstract description 24
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 21
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 19
- 239000002253 acid Substances 0.000 claims abstract description 16
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 10
- 239000002918 waste heat Substances 0.000 claims abstract description 10
- 230000003068 static effect Effects 0.000 claims abstract description 7
- 238000002485 combustion reaction Methods 0.000 claims abstract description 6
- 238000000926 separation method Methods 0.000 claims abstract description 4
- 239000005864 Sulphur Substances 0.000 claims description 30
- 239000002826 coolant Substances 0.000 claims description 7
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims description 6
- 238000009833 condensation Methods 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 238000006477 desulfuration reaction Methods 0.000 claims description 3
- 230000023556 desulfurization Effects 0.000 claims description 3
- 238000011143 downstream manufacturing Methods 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 239000003595 mist Substances 0.000 claims description 3
- 239000002912 waste gas Substances 0.000 claims description 3
- 239000000779 smoke Substances 0.000 claims description 2
- 230000009471 action Effects 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 abstract 1
- 230000001590 oxidative effect Effects 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 5
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000010622 cold drawing Methods 0.000 description 3
- 230000002779 inactivation Effects 0.000 description 3
- GVGLGOZIDCSQPN-PVHGPHFFSA-N Heroin Chemical compound O([C@H]1[C@H](C=C[C@H]23)OC(C)=O)C4=C5[C@@]12CCN(C)[C@@H]3CC5=CC=C4OC(C)=O GVGLGOZIDCSQPN-PVHGPHFFSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000007062 hydrolysis Effects 0.000 description 2
- 238000006460 hydrolysis reaction Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- XAQHXGSHRMHVMU-UHFFFAOYSA-N [S].[S] Chemical compound [S].[S] XAQHXGSHRMHVMU-UHFFFAOYSA-N 0.000 description 1
- 230000003044 adaptive effect Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Exhaust Gas Treatment By Means Of Catalyst (AREA)
- Treating Waste Gases (AREA)
- Catalysts (AREA)
Abstract
The invention relates to an inner-cooling type direct oxidation sulfur recovery method and device; the acid gas and the air are combusted and subjected to Claus reaction in a main combustion furnace; the gas flow coming out enters a waste heat boiler, most of sulfur steam is condensed and enters a first-stage Claus reactor after being heated, and H in the process gas2S and SO2Generating elemental sulfur; the process gas enters a first-stage condenser to condense most of sulfur steam into liquid sulfur for separation, the process gas enters a second-stage Claus reactor after being heated, and the liquid sulfur is condensed and separated by the condenser; mixing the Claus tail gas with air in a static mixer, heating, introducing into an internal cooling type direct oxidation reactor, oxidizing hydrogen sulfide in the tail gas into elemental sulfur under the action of a catalyst, and using an internal cooling type structureTaking away heat generated by direct oxidation of hydrogen sulfide, condensing process gas, separating liquid sulfur, introducing the liquid sulfur into a liquid sulfur trap, introducing the liquid sulfur into a tail gas incinerator, and discharging the liquid sulfur through a chimney; the sulfur recovery rate of the method can be stabilized to be more than 85 percent.
Description
Technical field
The present invention relates to a kind of inner-cooled direct oxidation sulfur recovery method and device, high sulfuric acid gas in being applicable to process, belong to natural gas and refinery gas manufacture field.
Background technology
At present, from the sulfide hydrogen sour gas, the technology of Recovered sulphur mainly contains conventional Claus method, conventional Claus+Reducing and absorption class vent gas treatment method and Crouse and extends class, and their basic skills and shortcoming are described below:
1, conventional Claus method
The conventional Claus method was come out in 1883, within 1938, realized the master that industrialization, the method relate to
Want chemical reaction to have two kinds,
The one, chemical reaction in main burning furnace comprises:
H
2S+3O
2→2H
2O+2SO
2；2H
2S+SO
2→2H
2O+3S
x/x；CH
4+SO
2→COS+H
2O+H
2；CO+S→COS；CO
2+H
2S→COS+H
2O；CH
4+2S→CS
2+2H
2S；2CO+S
2→CO
2+CS
2。
The 2nd, the chemical reaction in catalytic reactor comprises:
2H
2S+SO
2→2H
2O+3/8S
8；COS+H
2O→CO
2+H
2S；CS
2+2H
2O→CO
2+2H
2S
Above-mentioned reaction is exothermic reaction.
According to facts have proved in a large number, conventional Claus device sulfur recovery rate can only reach 94%～97% usually, and its total sulphur rate of recovery is restricted mainly contains following reason:
(1) be subject to thermodynamic limitation, the sulphur conversion reaction can not be fully.Still there is a small amount of H in Process Gas
2S and SO
2, limited the sulphur conversion ratio;
(2) claus reaction can produce steam.Moisture content increases affects the claus reaction balance, hinders sulphur and generates, and has limited the sulphur conversion ratio;
(3) for guaranteeing COS and CS
2Fully hydrolysis, the temperature of first order reactor must be controlled at 300 ℃～340 ℃.Although high temperature is conducive to hydrolysis, be unfavorable for carrying out claus reaction and carry out, limited the sulphur conversion ratio;
(4) the sulphur conversion ratio requires harshness to the air distribution ratio, must keep H
2S: SO
2=2: 1 optimal proportion, otherwise can cause the sulphur conversion ratio to reduce.
2, conventional Claus+Reducing and absorption class vent gas treatment method
These class methods are that the sulphur of various forms in Claus tail gases and sulfide are reduced to H
2S, then absorbed, and total sulfur recovery can reach more than 99.8%, SO in incineration tail gas
2For 300ppm or lower; These class methods comprise SSR, RAR, HCR, SCOT and BSRP, what wherein be most widely used is SCOT and BSRP method, but this class device flow process complexity, equipment is many, capital expenditure and operating cost are quite high, generally only at sulfur recovery facility, be on a grand scale, or just use these class methods in the very strict situation of environmental requirement.
3, Crouse extends class
Such mainly contains MCRC method, CBA method, super Claus method and super excellent Claus method.
MCRC method and CBA low-temperature Claus technique owned by France, major defect is: the device total sulfur recovery easily produces fluctuation, is strict with and controls H in tail gas
2S/SO
2Ratio, thus device air distribution difficulty increased, catalyst is gone through absorption/regenerative process, easy inactivation.
Super Claus method adds the super claus reaction device of one-level by two-stage or three grades of conventional Claus reactors and forms, and leaves H in the Process Gas of afterbody conventional Claus section
2S content maintains 0.6～1.0% (V).Process Gas mixes the laggard super claus reaction device that enters, the H in tail gas through reheating to 220 ℃ of left and right with air
2S direct oxidation on the catalyst for selective oxidation bed is elementary sulfur, and the conversion ratio in this reactor is about 85%, and super Claus method total sulfur recovery is about 99.2%.
Super excellent Claus method is developed on super Claus method basis, and purpose is on the basis that does not increase additional investment, and sulfur recovery rate is brought up to 99.4% or higher.Both are at difference: super excellent Claus method has in the end loaded one deck hydrogenating reduction catalyst below the claus catalyst in one-level claus catalytic reaction device bed, by SO
2Be reduced into S and H
2S, be greatly improved total sulfur recovery.According to the difference of sour gas inlet amount and catalytic reactor quantity, super excellent Claus sulfur recovery rate can reach more than 99.4%.
There are common shortcoming: a process using H in super Claus method and super excellent Claus method
2The excessive operation of S, but to H
2The S upper limit of concentration has strict demand.Enter the H in the selective oxidation reaction device
2The S excessive concentration will cause that the beds temperature rise is excessive, cause catalyst because of the overtemperature inactivation, and by H
2S is converted into the elective reduction of sulphur, makes the conversion reaction of sulphur incomplete, and then affects total sulfur recovery.
Summary of the invention
The object of the invention is to provide a kind of inner-cooled direct oxidation sulfur recovery method and device, and the heat-insulating direct oxidation reactor that replaces super Claus method and super excellent Claus method to adopt with inner-cooled direct oxidation reactor, used cooling medium by H
2S oxidation reaction liberated heat is taken away, thereby reaches the purpose of controlling reaction bed temperature.With super Crouse, with super excellent claus process, compare, this method and device can effectively improve catalyst sulfur recovery rate and device adaptive capacity.
Inner-cooled direct oxidation sulfur recovery method of the present invention comprises high-temp combustion part and low-temp reaction part.High-temp combustion partly comprises main burning furnace and waste heat boiler, the H in acid gas
2S partial oxidation in main burning furnace generates SO
2, combustion reaction is H
2S+1.5O
2→ SO
2+ H
2O, approximately have 1/3 H
2S and air generate SO in the burning reaction in furnace
2, the SO that part generates simultaneously
2With unburned SO
2Carry out claus reaction, generate sulphur.Process Gas enters the waste heat boiler condensation of being lowered the temperature afterwards.Low-temp reaction partly comprises sulfur condenser, claus reaction device, reheater and inner-cooled direct oxidation reactor etc.Waste heat boiler exit procedure gas enters one-level claus reaction device after heat again through the one-level reheater.In the claus reaction device, the key reaction occurred under conventional activated alumina catalyst effect is 2H
2S+SO
2→ 3S+2H
2O.Heat-claus reaction the process of Process Gas repeats condensation-more afterwards.Usually this process repeats 2～3 times.Last Process Gas is through condensation, entrained air, enter inner-cooled direct oxidation reactor after heat again.In inner-cooled direct oxidation reactor, take silica as carrier, under the catalyst action that iron oxide is active component, the H of remnants in Process Gas
2S is sulphur: H by oxygen to directly oxidize
2S+0.5O
2→ S+H
2O.Simultaneously, the cooling system arranged in reactor is by H
2S is direct oxidation into sulphur institute liberated heat and takes away, prevents the catalyst overheating inactivation, maintains the direct oxidation beds at the optimal reaction temperature of 220 ℃～240 ℃ simultaneously.In this process, reactor is horizontal type structure, adopts cold drawing as heat exchange element, is embedded in beds and vertically places side by side, and cold drawing one end is connected with fixed tube sheet by tube connector, other end energy free-extension; The bobbin carriage cylindrical shell utilizes bolt, nut to be connected by flange with reactor shell, in whole cold drawing Shu Kecong housing, extracts out.Reactor does not require strict isothermal, only need to take partial reaction heat away, the direct oxidation reaction bed temperature is maintained in 220 ℃～240 ℃ scopes and get final product.Finally, Process Gas enters tail gas burning furnace, after burning disposal, by chimney, enters atmosphere.
Method step is described below: the acid gas come from desulfurization unit is isolated liquid through the acid gas separator, again after the heating of acid gas preheater, enter main burning furnace, the air after air preheater heating of sending here with main air blower carries out partial combustion and the claus reaction of hydrogen sulfide; From main burning furnace, high temperature gas flow out enters waste heat boiler, cools the temperature to 150～170 ℃, and wherein most of sulphur steam is condensed, and remaining Process Gas is heated to 220～280 ℃ through the one-level reheater, enters one-level claus reaction device, the H in Process Gas
2S and SO
2At beds cogenerator element sulphur; A reactor exit procedure gas enters first-stage condenser and is cooled to 150～170 ℃, and most sulphur steam-condensations are wherein become to molten sulfur and separate, and reduces and enters the sulfur content in downstream process gas; First-stage condenser exit procedure gas enters secondary claus reaction device after the secondary reheater is heated to 200～220 ℃, the H of remainder in Process Gas
2S and SO
2Carry out claus reaction on beds; The Process Gas that goes out secondary claus reaction device enters secondary condenser and is cooled to 150～170 ℃, the wherein molten sulfur separation that continues to be condensed.Now, by controlling the main burning furnace air distribution, by the content of sulfur dioxide in tail gas, control lowly as far as possible, be beneficial to improve the device total sulfur recovery; Claus tail gases mixes in static mixer with air by three grades of reheater heating, enter inner-cooled direct oxidation reactor with 200～220 ℃ of left and right, under the effect of catalyst for selective oxidation, hydrogen sulfide in tail gas directly is oxidized to elementary sulfur, the heat that simultaneously adopts the inner-cooled structure that direct oxidation of hydrogen sulfide is produced is taken away, makes beds maintain the optimal reaction temperature of 220 ℃～240 ℃; The Process Gas that goes out inner-cooled direct oxidation reactor enters three grades of condensers and is cooled to 120～140 ℃, isolate after molten sulfur wherein and enter the molten sulfur trap and trap remaining sulphur drop and sulphur mist, Process Gas enters tail gas burning furnace afterwards, and the waste gas after burning is by smoke stack emission.Catalyst for selective oxidation is for take silica as carrier, and iron oxide is active component; Claus reaction device catalyst used is conventional activated alumina catalyst.
The present invention has following advantage:
1, the process that the present invention adopts makes the concentration of hydrogen sulfide upper limit that enters the selective oxidation reaction device reach 4%, and the concentration of hydrogen sulfide upper limit of the selective oxidation reaction device allowed in conventional super Crouse or super excellent claus process is generally 1.0～1.3%.Operating process does not need strictly to control concentration of hydrogen sulfide, efficiently solves the beds problem of temperature rise that concentration of hydrogen sulfide raises and brings.In addition, acid gas for high hydrogen sulfide content, super Crouse or super excellent claus process require Crouse's section must adopt three reactors usually, this technique without this restriction, can adopt two even a claus reaction device add the acid gas that the direct oxidation reactor is processed high hydrogen sulfide content.
2, after the inner-cooled direct oxidation reactor that the present invention adopts is taken reaction heat away, can make the catalyst for selective oxidation bed in the optimal reaction temperature of 220 ℃～240 ℃, more hydrogen sulfide directly is oxidized to elementary sulfur, has improved the device total sulfur recovery.
Effect of the present invention is as follows:
1, for H in acid gas
2The operating mode of S content 30～50%, novel inner-cooled direct oxidation recovery technology of sulfur adopts one-level claus reaction device to add direct oxidation reactor or secondary claus reaction device to add the structure that direct oxidation reactor or three grades of claus reaction devices add the direct oxidation reactor and all can process; For H in acid gas
2The operating mode of S content 50～80%, novel inner-cooled direct oxidation recovery technology of sulfur adopts secondary claus reaction device to add the structure that direct oxidation reactor or three grades of claus reaction devices add the direct oxidation reactor and all can process; For H in acid gas
2S content is higher than 80% operating mode, and the structure that novel inner-cooled direct oxidation recovery technology of sulfur can adopt three grades of claus reaction devices to add the direct oxidation reactor is processed.
If 2 enter H in the Process Gas of direct oxidation reactor
2S content surpasses 2%, hydrogen sulfide selective oxidation catalyst for sulphur sulfur recovery rate in heat-insulating direct oxidation reactor will be reduced to below 80%, and inner-cooled direct oxidation reactor can be controlled at reaction bed temperature 220 ℃～240 ℃, the catalyst sulfur recovery rate can be stabilized in more than 85%.
The accompanying drawing explanation:
Fig. 1 is process chart.
Shown in Fig. 1: 1, main burning furnace, 2, waste heat boiler, 3, the one-level reheater, 4, one-level claus reaction device, 5, first-stage condenser, 6, the secondary reheater, 7, secondary claus reaction device, 8, secondary condenser, 9, three grades of reheaters, 10, static mixer, 11, inner-cooled direct oxidation reactor, 12, three grades of condensers, 13, the molten sulfur trap, 14, tail gas burning furnace, 15, chimney.
Fig. 2 is inner-cooled structure of reactor figure.
Shown in Fig. 2: 16, lower chambers, 17 diaphragm plates, 18, cooling medium inlet, 19, heat exchanger plates import, 20, heat exchanger plates outlet, 21, catalyst supports screen, 22, heat exchanger plates support bar, 23, gas vent, 24, end socket, 25, thermocouple, 26, gas feed, 27, reactor shell, 28, heat exchanger plates, 29, fixed tube sheet, 30, flange, 31, cooling medium outlet, 32, upper chamber.
The specific embodiment:
Inner-cooled direct oxidation sulfur recovery facility of the present invention is by main burning furnace 1, waste heat boiler 2, one-level reheater 3, one-level claus reaction device 4, first-stage condenser 5, secondary reheater 6, secondary claus reaction device 7,8, three grades of reheaters 9 of secondary condenser, static mixer 10,11, three grades of condensers 12 of inner-cooled direct oxidation reactor, molten sulfur trap 13, tail gas burning furnace 14, chimney 15 is in series successively.
Wherein inner-cooled direct oxidation reactor 11 is by reactor shell 27, end socket 24, and diaphragm plate 17, catalyst supports screen 21, heat exchanger plates support bar 22, thermocouple 25, heat exchanger plates 28, fixed tube sheet 29, flange 30 forms; Fixed tube sheet 29 vertically is positioned at reactor shell 27, by flange 30, is fixed on reactor shell 27, and reactor is separated into to former and later two spaces; Heat exchanger plates 28 is a cylindrical shell, with reactor shell 27, coaxially is positioned on the heat exchanger plates support bar 22 of back space, and an end is connected with fixed tube sheet 29, and the other end is connected with end socket 24, makes heat exchanger plates 28 outer walls and reactor shell 27 inwalls form an annular space; Diaphragm plate 17 is parallel to be positioned in the middle of inside reactor, one end is fixed on front head, and inside reactor is divided into to upper chamber 32 and lower chambers 16, and the other end is through fixed tube sheet 29, go deep in heat exchanger plates 28 cylindrical shells lower channel on heat exchanger plates 28 cylindrical shell rear portions form; On fixed tube sheet 29, heat exchanger plates 28 places, diaphragm plate 17 are respectively equipped with heat exchanger plates import 19 and heat exchanger plates outlet 20 up and down, are respectively equipped with cooling medium entrance 18 and cooling medium outlet 31 on the reactor shell 27 between fixed tube sheet 29 and front head; Catalyst supports screen 21, and heat exchanger plates support bar 22 is positioned at the bottom of reactor, is fixed on fixed tube sheet 29 and rear head 24, and reactor shell 27 is provided with gas vent 23 and gas access 26; Thermocouple 25 is positioned at heat exchanger plates 28.
Embodiment 1: consult Fig. 1.The acid gas come from desulfurization unit is isolated liquid through the acid gas separator, then after the heating of acid gas preheater, enters the air proportion after the air preheater heating that main burning furnace 1 and main air blower send here and carry out claus reaction in stove; From main burning furnace 1, high temperature gas flow out cools the temperature to 164 ℃ through waste heat boiler 2, and wherein most of sulphur steam is condensed, and remaining Process Gas is heated to 280 ℃ through one-level reheater 3, enters one-level claus reaction device 4, the H in Process Gas
2S and SO
2Generate element sulphur on beds, the Process Gas temperature is elevated to 325 ℃; One-level claus reaction device 4 exit procedure gas enter first-stage condenser 5 and are cooled to 164 ℃, and most sulphur steam-condensations are wherein become to molten sulfur and separate, and reduce and enter the sulfur content in downstream process gas; First-stage condenser exports 5 Process Gas and is heated to 215 ℃ through secondary reheater 6 and enters secondary claus reaction device 7, H in remaining Process Gas
2S and SO
2Carry out claus reaction on beds, the Process Gas temperature is elevated to 223 ℃; The Process Gas that goes out second reactor 7 enters secondary condenser 8 and is cooled to 164 ℃, the wherein molten sulfur separation that continues to be condensed, and now the content of sulfur dioxide in tail gas, far below hydrogen sulfide, is conducive to the raising of device total sulfur recovery; Claus tail gases mixes in static mixer 10 with air by 9 heating of three grades of reheaters, enter inner-cooled direct oxidation reactor 11 with 210 ℃ of left and right, under the effect of catalyst for selective oxidation, hydrogen sulfide in tail gas is elementary sulfur by direct oxidation, the heat that simultaneously adopts the inner-cooled structure that direct oxidation of hydrogen sulfide is produced is taken away, makes beds maintain the optimal reaction temperature of 230 ℃; The Process Gas that goes out inner-cooled direct oxidation reactor 11 enters three grades of condensers 12 and is cooled to 125 ℃, enter molten sulfur trap 13 after isolating molten sulfur, enter tail gas burning furnace 14 after remaining sulphur drop and sulphur mist are trapped, the waste gas after burning is by chimney 15 discharges.
Claims (2)
1. an inner-cooled direct oxidation sulfur recovery facility, by main burning furnace, waste heat boiler, the one-level reheater, one-level claus reaction device, first-stage condenser, the secondary reheater, secondary claus reaction device, secondary condenser, three grades of reheaters, static mixer, inner-cooled direct oxidation reactor, three grades of condensers, the molten sulfur trap, tail gas burning furnace, chimney is in series successively, wherein inner-cooled direct oxidation reactor is by reactor shell, end socket, diaphragm plate, catalyst supports screen, the heat exchanger plates support bar, thermocouple, heat exchanger plates, fixed tube sheet, flange forms, it is characterized in that: fixed tube sheet vertically is positioned at reactor shell, by flange, is fixed on reactor shell, and reactor is separated into to former and later two spaces, heat exchanger plates is a cylindrical shell, with reactor shell, coaxially is positioned on the heat exchanger plates support bar of back space, and an end is connected with fixed tube sheet, and the other end is connected with end socket, makes heat exchanger plates outer wall and reactor shell inwall form an annular space, diaphragm plate is parallel to be positioned in the middle of inside reactor, and an end is fixed on front head, and inside reactor is divided into to upper chamber and lower chambers, and the other end, through fixed tube sheet, gos deep in the heat exchanger plates cylindrical shell, lower channel on heat exchanger plates cylindrical shell rear portion forms, on fixed tube sheet, heat exchanger plates place, diaphragm plate be respectively equipped with heat exchanger plates import and heat exchanger plates outlet up and down, is respectively equipped with cooling medium entrance and cooling medium outlet on the reactor shell between fixed tube sheet and front head, catalyst supports screen, and the heat exchanger plates support bar is positioned at the bottom of reactor, is fixed on fixed tube sheet and rear head, and reactor shell is provided with gas vent and gas access, thermocouple is positioned at heat exchanger plates.
2. an inner-cooled direct oxidation sulfur recovery method that utilizes the described retracting device of claim 1, it is characterized in that: the acid gas come from desulfurization unit is isolated liquid through the acid gas separator, again after the heating of acid gas preheater, enter main burning furnace, the air after air preheater heating of sending here with main air blower carries out partial combustion and the claus reaction of hydrogen sulfide; From main burning furnace, high temperature gas flow out enters waste heat boiler, cools the temperature to 150～170 ℃, and most of sulphur steam is condensed, and remaining Process Gas is heated to 220～280 ℃ through the one-level reheater, enters one-level claus reaction device, the H in Process Gas
2S and SO
2At beds cogenerator element sulphur; One-level claus reaction device exit procedure gas enters first-stage condenser and is cooled to 150～170 ℃, becomes molten sulfur to separate most sulphur steam-condensations, reduces and enters the sulfur content in downstream process gas; First-stage condenser exit procedure gas enters secondary claus reaction device after the secondary reheater is heated to 200～220 ℃, the H of remainder in Process Gas
2S and SO
2Carry out claus reaction on beds; The Process Gas that goes out secondary claus reaction device enters secondary condenser and is cooled to 150～170 ℃, the molten sulfur separation that continues to be condensed; By controlling the main burning furnace air distribution, by the content of sulfur dioxide in tail gas, control lowly as far as possible; Claus tail gases mixes in static mixer with air by three grades of reheater heating, enter inner-cooled direct oxidation reactor with 200～220 ℃, under the effect of catalyst for selective oxidation, hydrogen sulfide in tail gas directly is oxidized to elementary sulfur, the heat that simultaneously adopts the inner-cooled structure that direct oxidation of hydrogen sulfide is produced is taken away, makes beds maintain the optimal reaction temperature of 220 ℃～240 ℃; The Process Gas that goes out inner-cooled direct oxidation reactor enters three grades of condensers and is cooled to 120～140 ℃, isolate after molten sulfur wherein and enter the molten sulfur trap and trap remaining sulphur drop and sulphur mist, Process Gas enters tail gas burning furnace afterwards, and the waste gas after burning is by smoke stack emission.
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