CN106744704B - A kind of method of Crouse's direct current method Recovered sulphur - Google Patents
A kind of method of Crouse's direct current method Recovered sulphur Download PDFInfo
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- CN106744704B CN106744704B CN201611079809.3A CN201611079809A CN106744704B CN 106744704 B CN106744704 B CN 106744704B CN 201611079809 A CN201611079809 A CN 201611079809A CN 106744704 B CN106744704 B CN 106744704B
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- acid gas
- temperature
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 180
- 239000005864 Sulphur Substances 0.000 title claims abstract description 169
- 238000000034 method Methods 0.000 title claims abstract description 49
- 239000002253 acid Substances 0.000 claims abstract description 161
- 239000007789 gas Substances 0.000 claims description 223
- 239000002918 waste heat Substances 0.000 claims description 26
- 238000002485 combustion reaction Methods 0.000 claims description 24
- 238000006243 chemical reaction Methods 0.000 claims description 19
- 239000007788 liquid Substances 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 4
- 238000011084 recovery Methods 0.000 abstract description 16
- 229910052717 sulfur Inorganic materials 0.000 abstract description 11
- 239000011593 sulfur Substances 0.000 abstract description 11
- 238000010438 heat treatment Methods 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 11
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 11
- 238000002156 mixing Methods 0.000 description 3
- 230000000694 effects 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
- 230000001105 regulatory effect Effects 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000006479 redox reaction Methods 0.000 description 1
- RAHZWNYVWXNFOC-UHFFFAOYSA-N sulfur dioxide Inorganic materials O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/02—Preparation of sulfur; Purification
- C01B17/04—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides
- C01B17/0404—Preparation of sulfur; Purification from gaseous sulfur compounds including gaseous sulfides by processes comprising a dry catalytic conversion of hydrogen sulfide-containing gases, e.g. the Claus process
-
- 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
-
- 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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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The present invention relates to a kind of methods of Crouse's direct current method Recovered sulphur, belong to Clausius equlity sulphur technical field.The present invention is by being arranged third-stage reactor and three-level gas-gas heat exchanger, binding reactor temperature control valve (TCV) and temperature of reactor transmitter, high temperature acid gas and low temperature acid gas exchange heat in systems, Recovered sulphur, solve the problems, such as heating of the acid gas from sulphur cooler to reactor region, reduce high concentration acid gas and enters reactor, sulfur recovery rate is improved, energy consumption is reduced, it is cost-effective, sulfur recovery rate is improved to 96-99%, is higher than the 94-97% of conventional Claus direct current method sulfur recovery rate.
Description
Technical field
The present invention relates to a kind of methods of Recovered sulphur, it is more particularly related to which a kind of Crouse's direct current method returns
The method for receiving sulphur, belongs to Clausius equlity sulphur technical field.
Background technology
It is that current utilization rate is most wide that Claus method, which handles hydrogen sulfide acid gas and Recovered sulphur, the highest technique of efficiency, H2S acid
Gas is after buffering, in combustion furnace, by supplementing appropriate air, makes H2S burn incompletelies in combustion furnace, H2S portion burns
It is converted into SO2, adjust air inlet amount.H in combustion furnace2S and SO2Ratio is 2:1, H2S and SO2Reaction occurs under ignition temperature
Redox reaction can obtain gaseous elemental sulphur（Sulphur）.Mix waste gas makes gaseous elemental sulphur be cooled to liquid through over cure cooler
State sulphur, acid gas includes H at this time2S、SO2、COS、CS2、H2After O and sulphur steam etc., reheated device or high temperature blending valve, acid gas temperature
It is increased to claus reaction device required temperature, using LT claus reaction device, under the effect of the catalyst, COS, CS2Then
With H2Hydrolysis occurs for O, obtains H2S, H2S and SO2It is further continued for reacting, acid gas further recycles sulphur through over cure cooler after reaction
Sulphur.Acid gas passes through three-level（Two-stage）After reactor, still there is minute quantity H in tail gas2S、SO2、COS、CS2、H2O and sulphur steam
Deng recycling certain sulphur by catching sulphur device and fully burn into SO using incinerator2After discharge.
The sulfur recovery rate of conventional Claus technique is typically only capable to reach 94-97%, and the rate of recovery is limited following reason：
1, since thermodynamics limits, the conversion reaction of sulphur can not possibly completely, and Process Gas still has H2S、SO2, limit sulphur
Conversion ratio.
2, claus reaction will generate a certain amount of steam, with the increase of steam, relative reduction H2S and SO2It is dense
Degree, affects the balance of claus reaction, hinders the generation of sulphur.
3, due to CO in acid gas2And the presence of hydro carbons, Process Gas can form COS and CS2, it is necessary to it is allowed to that hydrolysis occurs,
For this purpose, the temperature of reactor must be controlled at 300-340 DEG C, though high temperature is conducive to hydrolyze, it is unfavorable for the flat of claus reaction
Weighing apparatus, limits the conversion ratio of sulphur.
4, the conversion ratio of conventional Claus technique sulphur is not normal to the proportioning of air and acid gas very sensitive, if cannot keep
H2S：SO2=2:1 optimal proportion will cause the conversion ratio of sulphur to reduce.
Heating problem of the acid gas from sulphur cooler to reactor region exists in the prior art, conventional method has reheater, electricity
Heating, high temperature admix valve, and sulphur cooler can be exported to the raising of acid gas temperature and reach the requirement of reactor intake air temperature.But three is
There are its disadvantage, reheater and high temperature blending valve that can introduce high-temperature and high concentration acid gas, to cause reactor load, lead to sulfur recovery rate
Decline, and electrically heated power consumption cost is higher.
Invention content
Present invention seek to address that liter of the prior art Clausius equlity sulphur method acid gas from sulphur cooler to reactor region
Warm problem provides a kind of method of Crouse's direct current method Recovered sulphur, can solve liter of the acid gas from sulphur cooler to reactor region
Warm problem, additionally it is possible to ensure higher sulfur recovery rate.
In order to achieve the above-mentioned object of the invention, specific technical solution is as follows：
A kind of method of Crouse's direct current method Recovered sulphur, it is characterised in that：Including following methods step：
A, combustion furnace and waste heat boiler connect, and the combustion furnace passes through high-temperature acid flow control valves and the first gas-gas heat exchange
Device, the second gas-gas heat exchanger are connected with the high temperature acid gas import of third gas-gas heat exchanger；Waste heat boiler is connect with pre- sulphur cooler；Institute
It states the high temperature acid gas in combustion furnace and enters first gas-gas heat exchanger, the low temperature acid gas in the waste heat boiler passes through described pre-
Sulphur cooler enters first gas-gas heat exchanger, and two kinds of acid gas carry out gas-gas heat exchange in first gas-gas heat exchanger；
B, the low temperature acid gas outlet of first gas-gas heat exchanger is connect with first-stage reactor, first gas-gas heat exchanger
High temperature acid gas outlet and the waste heat boiler connect with the pipeline of pre- sulphur cooler junction, the height of first gas-gas heat exchanger
Warm acid gas exit is provided with first-stage reactor temperature control valve (TCV), and aperture is anti-by the level-one being arranged on the first-stage reactor
Device temperature transmitter is answered to control；Low temperature acid gas after heat exchange enters the first-stage reactor, and the high temperature acid gas after heat exchange returns to institute
State pre- sulphur cooler；
C, the first-stage reactor temperature transmitter on the first-stage reactor controls the first-stage reactor temperature control valve (TCV)
Aperture, to control the low temperature acid gas temperature into first-stage reactor；The first-stage reactor connects with the level-one sulphur cooler
It connects, the low temperature acid gas after reaction enters the level-one sulphur cooler Recovered sulphur, and the low temperature acid gas after Recovered sulphur enters the second gas
Gas heat exchanger enters second reactor after exchanging heat with high temperature acid gas, and the high-temperature acid gas outlet of second gas-gas heat exchanger is set
It is equipped with second reactor temperature control valve (TCV), aperture is by the second reactor temperature transmitter that is arranged on the second reactor
Control；High temperature acid gas by heat exchange returns to the pre- sulphur cooler；
D, the second reactor temperature transmitter on the second reactor controls the second reactor temperature control valve (TCV)
Aperture, to control the low temperature acid gas temperature into second reactor；The second reactor connects with the two level sulphur cooler
It connects, the low temperature acid gas after reaction enters the two level sulphur cooler Recovered sulphur, and the low temperature acid gas after Recovered sulphur enters third gas
Gas heat exchanger enters third-stage reactor after exchanging heat with high temperature acid gas, and the high-temperature acid gas outlet of the third gas-gas heat exchanger is set
It is equipped with third-stage reactor temperature control valve (TCV), aperture is by the third-stage reactor temperature transmitter that is arranged on the third-stage reactor
Control；High temperature acid gas by heat exchange returns to the pre- sulphur cooler；
E, the third-stage reactor temperature transmitter on the third-stage reactor controls the third-stage reactor temperature control valve (TCV)
Aperture, to control the low temperature acid gas temperature into third-stage reactor；The third-stage reactor is connect with three-level sulphur cooler, instead
Low temperature acid gas after answering enters the three-level sulphur cooler Recovered sulphur.
In step A of the present invention, the temperature of the high temperature acid gas in the combustion furnace is 1000-1200 DEG C.
In step B of the present invention, the temperature of the low temperature acid gas in the waste heat boiler is 340-350 DEG C, it is cold by pre- sulphur
The temperature of low temperature acid gas is 140-160 DEG C after device.
In step C of the present invention, the temperature of the low temperature acid gas into first-stage reactor is 280-310 DEG C.
In step D, the temperature of the low temperature acid gas into second reactor is 250-280 DEG C to the present invention.
For the present invention in step E, the temperature of the low temperature acid gas into third-stage reactor is 180-200 DEG C.
For the present invention in step E, the low temperature acid gas outlet of the three-level sulphur cooler, which is connected with, catches sulphur device.
It pre- sulphur cooler of the present invention, level-one sulphur cooler, two level sulphur cooler, three-level sulphur cooler and catches sulphur device and passes through pipeline
It is connect with sulphur liquid collecting tank, the sulphur of recycling is stored into the sulphur liquid collecting tank.
Sulphur device of the present invention of catching also is connected with incinerator and chimney in turn.
The conventional products of this field can be used in all devices, device and component in the present invention.
The advantageous effects that the present invention is brought：
1, reheater is to draw hydrogen sulfide acid gas to ignite in natural gas in the prior art, and oxygen combustion in air, releasing
Heat mixes acid gas and is mixed with sulphur cooler acid gas, to realize the promotion of acid gas temperature after burning.Because introducing high concentration at this
Acid gas, increase reactor load, sulfur recovery rate reduce.The present invention reduces high concentrated acid compared with reheater in direct current method
Gas enters reactor, improves sulfur recovery rate.
2, electrical heating process is to use electrical heating sulphur cooler acid gas in the prior art, to reach temperature of reactor requirement.This
Invention reduces energy consumption, has saved cost compared with electrical heating.
3, after high-temp mixing valve mixes sulphur cooler acid gas and high-temperature and high concentration acid gas in the prior art, reach temperature of reactor
After demand, it is delivered to reaction in reactor.The present invention reduces high concentration acid gas and enters reactor, carry compared with high temperature admixes valve
High sulfur recovery rate.
4, sulfur recovery rate of the present invention is improved to 96-99%, is higher than the 94-97% of conventional Claus direct current method sulfur recovery rate.
Description of the drawings
Fig. 1 is the system connection diagram that the method for the present invention uses.
Reference numeral：1 it is combustion furnace, 2 be waste heat boiler, 3 be high-temperature acid flow control valves, 4 is the first gas-gas heat exchange
Device, 5 be the second gas-gas heat exchanger, 6 be third gas-gas heat exchanger, 7 be pre- sulphur cooler, 8 be first-stage reactor, 9 be first order reaction
Device temperature control valve (TCV), 10 be first-stage reactor temperature transmitter, 11 be level-one sulphur cooler, 12 be second reactor, 13 be two level
Temperature of reactor regulating valve, 14 be second reactor temperature transmitter, 15 be two level sulphur cooler, 16 be third-stage reactor, 17 be
Third-stage reactor temperature control valve (TCV), 18 be third-stage reactor temperature transmitter, 19 be three-level sulphur cooler, 20 to catch sulphur device, 21 be
Sulphur liquid collecting tank, 22 be incinerator, 23 be chimney.
Specific implementation mode
Embodiment 1
A kind of method of Crouse's direct current method Recovered sulphur, including following methods step：
A, combustion furnace and waste heat boiler connect, and the combustion furnace passes through high-temperature acid flow control valves and the first gas-gas heat exchange
Device, the second gas-gas heat exchanger are connected with the high temperature acid gas import of third gas-gas heat exchanger；Waste heat boiler is connect with pre- sulphur cooler；Institute
It states the high temperature acid gas in combustion furnace and enters first gas-gas heat exchanger, the low temperature acid gas in the waste heat boiler passes through described pre-
Sulphur cooler enters first gas-gas heat exchanger, and two kinds of acid gas carry out gas-gas heat exchange in first gas-gas heat exchanger；
B, the low temperature acid gas outlet of first gas-gas heat exchanger is connect with first-stage reactor, first gas-gas heat exchanger
High temperature acid gas outlet and the waste heat boiler connect with the pipeline of pre- sulphur cooler junction, the height of first gas-gas heat exchanger
Warm acid gas exit is provided with first-stage reactor temperature control valve (TCV), and aperture is anti-by the level-one being arranged on the first-stage reactor
Device temperature transmitter is answered to control；Low temperature acid gas after heat exchange enters the first-stage reactor, and the high temperature acid gas after heat exchange returns to institute
State pre- sulphur cooler；
C, the first-stage reactor temperature transmitter on the first-stage reactor controls the first-stage reactor temperature control valve (TCV)
Aperture, to control the low temperature acid gas temperature into first-stage reactor；The first-stage reactor connects with the level-one sulphur cooler
It connects, the low temperature acid gas after reaction enters the level-one sulphur cooler Recovered sulphur, and the low temperature acid gas after Recovered sulphur enters the second gas
Gas heat exchanger enters second reactor after exchanging heat with high temperature acid gas, and the high-temperature acid gas outlet of second gas-gas heat exchanger is set
It is equipped with second reactor temperature control valve (TCV), aperture is by the second reactor temperature transmitter that is arranged on the second reactor
Control；High temperature acid gas by heat exchange returns to the pre- sulphur cooler；
D, the second reactor temperature transmitter on the second reactor controls the second reactor temperature control valve (TCV)
Aperture, to control the low temperature acid gas temperature into second reactor；The second reactor connects with the two level sulphur cooler
It connects, the low temperature acid gas after reaction enters the two level sulphur cooler Recovered sulphur, and the low temperature acid gas after Recovered sulphur enters third gas
Gas heat exchanger enters third-stage reactor after exchanging heat with high temperature acid gas, and the high-temperature acid gas outlet of the third gas-gas heat exchanger is set
It is equipped with third-stage reactor temperature control valve (TCV), aperture is by the third-stage reactor temperature transmitter that is arranged on the third-stage reactor
Control；High temperature acid gas by heat exchange returns to the pre- sulphur cooler；
E, the third-stage reactor temperature transmitter on the third-stage reactor controls the third-stage reactor temperature control valve (TCV)
Aperture, to control the low temperature acid gas temperature into third-stage reactor；The third-stage reactor is connect with three-level sulphur cooler, instead
Low temperature acid gas after answering enters the three-level sulphur cooler Recovered sulphur.
Embodiment 2
On the basis of embodiment 1：
Preferably, in step, the temperature of the high temperature acid gas in the combustion furnace is 1000 DEG C.
Preferably, in stepb, the temperature of the low temperature acid gas in the waste heat boiler is 340 DEG C, after pre- sulphur cooler
The temperature of low temperature acid gas is 140 DEG C.
Preferably, in step C, the temperature of the low temperature acid gas into first-stage reactor is 280 DEG C.
Preferably, in step D, the temperature of the low temperature acid gas into second reactor is 250 DEG C.
Preferably, in step E, the temperature of the low temperature acid gas into third-stage reactor is 180 DEG C.
Embodiment 3
On the basis of embodiment 1：
Preferably, in step, the temperature of the high temperature acid gas in the combustion furnace is 1200 DEG C.
Preferably, in stepb, the temperature of the low temperature acid gas in the waste heat boiler is 350 DEG C, after pre- sulphur cooler
The temperature of low temperature acid gas is 160 DEG C.
Preferably, in step C, the temperature of the low temperature acid gas into first-stage reactor is 310 DEG C.
Preferably, in step D, the temperature of the low temperature acid gas into second reactor is 280 DEG C.
Preferably, in step E, the temperature of the low temperature acid gas into third-stage reactor is 200 DEG C.
Embodiment 4
On the basis of embodiment 1：
Preferably, in step, the temperature of the high temperature acid gas in the combustion furnace is 1100 DEG C.
Preferably, in stepb, the temperature of the low temperature acid gas in the waste heat boiler is 345 DEG C, after pre- sulphur cooler
The temperature of low temperature acid gas is 150 DEG C.
Preferably, in step C, the temperature of the low temperature acid gas into first-stage reactor is 295 DEG C.
Preferably, in step D, the temperature of the low temperature acid gas into second reactor is 265 DEG C.
Preferably, in step E, the temperature of the low temperature acid gas into third-stage reactor is 190 DEG C.
Embodiment 5
On the basis of embodiment 1：
Preferably, in step, the temperature of the high temperature acid gas in the combustion furnace is 1150 DEG C.
Preferably, in stepb, the temperature of the low temperature acid gas in the waste heat boiler is 342 DEG C, after pre- sulphur cooler
The temperature of low temperature acid gas is 155 DEG C.
Preferably, in step C, the temperature of the low temperature acid gas into first-stage reactor is 300 DEG C.
Preferably, in step D, the temperature of the low temperature acid gas into second reactor is 270 DEG C.
Preferably, in step E, the temperature of the low temperature acid gas into third-stage reactor is 185 DEG C.
Embodiment 6
On the basis of embodiment 1：
Preferably, in step E, the low temperature acid gas outlet of the three-level sulphur cooler, which is connected with, catches sulphur device.
Further, it the pre- sulphur cooler, level-one sulphur cooler, two level sulphur cooler, three-level sulphur cooler and catches sulphur device and passes through
Pipeline is connect with sulphur liquid collecting tank, and the sulphur of recycling is stored into the sulphur liquid collecting tank.
Further, the sulphur device of catching also is connected with incinerator and chimney in turn.
Embodiment 7
The temperature of high temperature acid gas in combustion furnace 1 is 1000-1200 DEG C, the waste heat boiler after combustion furnace 1, waste heat boiler 2
In low temperature acid gas be 340-350 DEG C, into after 7 condensing recovery sulphur of pre- sulphur cooler, the temperature of low temperature acid gas is 140-160
DEG C, after the heating of the first gas-gas heat exchanger 4, temperature rise is to 280-310 DEG C, into first-stage reactor 8, after reacted, acid gas
Temperature is increased to 340-350 DEG C, and temperature is reduced to 140-160 DEG C after level-one sulphur cooler 11, after the second gas-gas heat exchanger 5,
Temperature rise is to 250-280 DEG C, and into second reactor 12, after reacted, acid gas temperature is 290-310 DEG C, cold through two level sulphur
After 15 condensing recovery sulphur of device, temperature is reduced to 140-160 DEG C, then after third gas-gas heat exchanger 6, temperature rise to 180-
200 DEG C, into third-stage reactor 16, after reacted, acid gas temperature is 190-220 DEG C, then through 19 condensing recovery of three-level sulphur cooler
After sulphur, temperature is reduced to 140-160 DEG C.Three-level sulphur cooler 19 exports acid gas into sulphur device 20 is caught, and traps sulphur steam in acid gas
Recovery section sulphur.
Embodiment 8
System used by the method for the present invention：
A kind of system of Crouse's direct current method Recovered sulphur, including combustion furnace 1 and waste heat boiler 2；The combustion furnace 1 and institute
The connection of waste heat boiler 2 is stated, the combustion furnace 1 passes through high-temperature acid flow control valves 3 and the first gas-gas heat exchanger 4, the second gas gas
Heat exchanger 5 is connected with the high temperature acid gas import of third gas-gas heat exchanger 6；The waste heat boiler 2 passes through pre- sulphur cooler 7 and described the
The low temperature acid gas import of one gas-gas heat exchanger 4 connects；The low temperature acid gas of first gas-gas heat exchanger 4 exports and first-stage reactor
8 connections, the pipeline of high temperature the acid gas outlet and the waste heat boiler 2 and pre- 7 junction of sulphur cooler of first gas-gas heat exchanger 4
Connection, the high-temperature acid gas outlet of first gas-gas heat exchanger 4 are provided with first-stage reactor temperature control valve (TCV) 9, aperture by
The first-stage reactor temperature transmitter 10 being arranged on the first-stage reactor 8 controls；The first-stage reactor 8 passes through level-one sulphur
Cooler 11 is connect with the low temperature acid gas import of second gas-gas heat exchanger 5, and the low temperature acid gas of second gas-gas heat exchanger 5 goes out
Mouthful connect with second reactor 12, the high temperature acid gas of second gas-gas heat exchanger 5 export and the waste heat boiler 2 with it is described pre-
The pipeline of 7 junction of sulphur cooler connects, and the high-temperature acid gas outlet of second gas-gas heat exchanger 5 is provided with second reactor temperature
Regulating valve 13 is spent, aperture is controlled by the second reactor temperature transmitter 14 being arranged on the second reactor 12；It is described
Second reactor 12 is connect by two level sulphur cooler 15 with the low temperature acid gas import of the third gas-gas heat exchanger 6, the third
The low temperature acid gas outlet of gas-gas heat exchanger 6 is connect with third-stage reactor 16, the high temperature acid gas outlet of the third gas-gas heat exchanger 6
It is connect with the waste heat boiler 2 with the pipeline of pre- 7 junction of sulphur cooler, the high temperature acid gas of the third gas-gas heat exchanger 6
Exit is provided with third-stage reactor temperature control valve (TCV) 17, and aperture is by being arranged the third-order reaction on the third-stage reactor 16
Device temperature transmitter 18 controls；The third-stage reactor 16 is connect with three-level sulphur cooler 19.
Preferably, the low temperature acid gas outlet of the three-level sulphur cooler 19, which is connected with, catches sulphur device 20.
Further, the pre- sulphur cooler 7, level-one sulphur cooler 11, two level sulphur cooler 15, three-level sulphur cooler 19 and sulphur is caught
Device 20 is connect by pipeline with sulphur liquid collecting tank 21.
Further, the sulphur device 20 of catching also is connected with incinerator 22 and chimney 23 in turn.
Claims (9)
1. a kind of method of Crouse's direct current method Recovered sulphur, it is characterised in that：Including following methods step：
A, combustion furnace and waste heat boiler connect, the combustion furnace by high-temperature acid flow control valves and the first gas-gas heat exchanger,
Second gas-gas heat exchanger is connected with the high temperature acid gas import of third gas-gas heat exchanger；Waste heat boiler is connect with pre- sulphur cooler；It is described
High temperature acid gas in combustion furnace enters first gas-gas heat exchanger, and the low temperature acid gas in the waste heat boiler passes through the pre- sulphur
Cooler enters first gas-gas heat exchanger, and two kinds of acid gas carry out gas-gas heat exchange in first gas-gas heat exchanger；
B, the low temperature acid gas outlet of first gas-gas heat exchanger is connect with first-stage reactor, the height of first gas-gas heat exchanger
Warm acid gas outlet and the waste heat boiler are connect with the pipeline of pre- sulphur cooler junction, the high-temperature acid of first gas-gas heat exchanger
Gas outlet is provided with first-stage reactor temperature control valve (TCV), and aperture is by being arranged the first-stage reactor on the first-stage reactor
Temperature transmitter controls；Low temperature acid gas after heat exchange enters the first-stage reactor, and the high temperature acid gas after heat exchange returns to described pre-
Sulphur cooler；
C, the first-stage reactor temperature transmitter on the first-stage reactor controls opening for the first-stage reactor temperature control valve (TCV)
Degree, to control the low temperature acid gas temperature into first-stage reactor；The first-stage reactor is connect with the level-one sulphur cooler, instead
Low temperature acid gas after answering enters the level-one sulphur cooler Recovered sulphur, and the low temperature acid gas after Recovered sulphur enters the second gas-gas heat exchange
Device enters second reactor after exchanging heat with high temperature acid gas, and the high-temperature acid gas outlet of second gas-gas heat exchanger is provided with two
Stage reactor temperature control valve (TCV), aperture are controlled by the second reactor temperature transmitter being arranged on the second reactor；
High temperature acid gas by heat exchange returns to the pre- sulphur cooler；
D, the second reactor temperature transmitter on the second reactor controls opening for the second reactor temperature control valve (TCV)
Degree, to control the low temperature acid gas temperature into second reactor；The second reactor is connect with the two level sulphur cooler, instead
Low temperature acid gas after answering enters the two level sulphur cooler Recovered sulphur, and the low temperature acid gas after Recovered sulphur enters third gas-gas heat exchange
Device enters third-stage reactor after exchanging heat with high temperature acid gas, and the high-temperature acid gas outlet of the third gas-gas heat exchanger is provided with three
Stage reactor temperature control valve (TCV), aperture are controlled by the third-stage reactor temperature transmitter being arranged on the third-stage reactor；
High temperature acid gas by heat exchange returns to the pre- sulphur cooler；
E, the third-stage reactor temperature transmitter on the third-stage reactor controls opening for the third-stage reactor temperature control valve (TCV)
Degree, to control the low temperature acid gas temperature into third-stage reactor；The third-stage reactor is connect with three-level sulphur cooler, after reaction
Low temperature acid gas enter the three-level sulphur cooler Recovered sulphur.
2. a kind of method of Crouse's direct current method Recovered sulphur according to claim 1, it is characterised in that：In step,
The temperature of the high temperature acid gas is 1000-1200 DEG C.
3. a kind of method of Crouse's direct current method Recovered sulphur according to claim 1, it is characterised in that：In stepb,
The temperature of the low temperature acid gas is 140-160 DEG C.
4. a kind of method of Crouse's direct current method Recovered sulphur according to claim 1, it is characterised in that：In step C,
The temperature of the low temperature acid gas into first-stage reactor is 280-310 DEG C.
5. a kind of method of Crouse's direct current method Recovered sulphur according to claim 1, it is characterised in that：In step D,
The temperature of the low temperature acid gas into second reactor is 250-280 DEG C.
6. a kind of method of Crouse's direct current method Recovered sulphur according to claim 1, it is characterised in that：In step E,
The temperature of the low temperature acid gas into third-stage reactor is 180-200 DEG C.
7. a kind of method of Crouse's direct current method Recovered sulphur according to claim 1, it is characterised in that：In step E,
The low temperature acid gas outlet of the three-level sulphur cooler, which is connected with, catches sulphur device.
8. a kind of method of Crouse's direct current method Recovered sulphur according to claim 7, it is characterised in that：The pre- sulphur is cold
It device, level-one sulphur cooler, two level sulphur cooler, three-level sulphur cooler and catches sulphur device and is connect with sulphur liquid collecting tank by pipeline, recycling
Sulphur is stored into the sulphur liquid collecting tank.
9. a kind of method of Crouse's direct current method Recovered sulphur according to claim 7 or 8, it is characterised in that：Described
It catches sulphur device and is also connected with incinerator and chimney in turn.
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| US3833716A (en) * | 1972-08-02 | 1974-09-03 | Amoco Prod Co | Method for using reheat gas in sulfur recovery systems |
| GB2114106B (en) * | 1982-02-02 | 1985-10-02 | Shell Int Research | Process for the production of elemental sulphur |
| 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 |
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