CN107118817A - A kind of fuel gas-hydrogen joint production process - Google Patents
A kind of fuel gas-hydrogen joint production process Download PDFInfo
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- CN107118817A CN107118817A CN201610101898.0A CN201610101898A CN107118817A CN 107118817 A CN107118817 A CN 107118817A CN 201610101898 A CN201610101898 A CN 201610101898A CN 107118817 A CN107118817 A CN 107118817A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/08—Production of synthetic natural gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/103—Sulfur containing contaminants
Abstract
Fuel gas-hydrogen joint production process, using two sections or three sections of methanation furnaces, virgin gas is preheated, mix with compressor outlet gas after hydrolysis, anti-into one after two anti-outlets, an anti-entrance heat exchanger；Work off one's feeling vent one's spleen and be divided into two strands after steam superheater, an anti-entrance heat exchanger, steam generator, one is mixed into two anti-outlet heat exchangers with virgin gas, another burst of entrance two is anti-, and hydrogen-rich methane rich fuel gas is made after two anti-outlet heat exchangers, fresh air preheater, boiler water preheater two and three, boiler water preheater one, point flow container one in two anti-gas.Boiler water preheater three is worked off one's feeling vent one's spleen can also enter three anti-, three anti-gas obtained hydrogen-rich methane rich fuel gas after boiler water preheater four, three anti-entrance heat exchangers, boiler water preheater one, point flow container one through a point flow container two, three anti-entrance heat exchangers.The inventive method technological process is simple, and small, flexible and convenient operation is taken up an area in investment, fuel supply and the hydrogen balance of full factory is solved the problems, such as, with good economic benefit.
Description
Technical field
This technology belongs to coal gasification technical field of comprehensive utilization.
Background technology
Fuel consumption is one of important indicator of large-scale Coal Chemical Engineering Project Technical Economy.Hydrogen is weight in Coal Chemical Engineering Project
One of intermediate product wanted, hydrogen balance and its economy overall using project is also related to.
The common fuel of Coal Chemical Engineering Project has fuel oil, liquefied gas（Canned or pipe is defeated）, coal gas, natural gas（LNG is managed defeated）
Deng.Generally, it is higher using fuel oil and liquefied gas cost, and calorific value of gas is relatively low, does not often reach use requirement.From heat
Value, convenience, environment friendly, economy many-side consider, and natural gas is a relatively good selection.But due to item
Limited to mesh construction, the not supporting pipeline gas in many areas, therefore some projects are also selected than pipeline gas valency
Ge Genggao LNG is used as fuel.
The content of the invention
It is an object of the invention to provide a kind of fuel gas-hydrogen joint production process, in large-scale Coal Chemical Engineering Project first stage of construction solution
The fuel supply of Jue Quan factories and hydrogen balance problem.
The present invention's is mainly characterized by：Fuel gas-hydrogen joint production process flow is simple, and small, the flexible side of operation is taken up an area in investment
Just, fuel supply and the hydrogen balance problem of full factory are can solve the problem that, with good economic benefit.
The main technical schemes of the present invention：Fuel gas-hydrogen joint production process, it is characterised in that：Virgin gas enters virgin gas
Preheater shell side, exchanges heat, the unstripped gas after preheating enters hydrolysis reactor with the high methane gas of two anti-outlet heat exchanger tube pass
Generation hydrolysis, is inorganic sulfur by the tempreture organic sulphur hydrolysis in unstripped gas, then occurs desulphurization reaction, reduction by desulfurization reactor
Total sulfur content prevents methane synthesizing catalyst from occurring sulfur poisoning to below 50PPb in synthesis gas；Come from desulfurization reactor by de-
Through two anti-outlet heat exchangers heat exchange after the virgin gas of sulphur, the gas mixing exported with recycle compressor, exit gas through one it is counter enter
Enter the first methane synthesis reactor after mouth heat exchanger and an anti-heat exchange of working off one's feeling vent one's spleen；First methane synthesis reactor exit gas is passed through
Steam superheater it is counter to steam superheating, an anti-entrance heat exchanger preheating one enter implication, steam generator generation steam after be divided into
Two strands, one through the feedwater of compressor entrance heat exchanger preboiler, preceding steady tank voltage stabilizing, recycle compressor boosting, after steady tank voltage stabilizing
Afterwards as circulating air with being mixed into two anti-outlet heat exchangers, another burst of entrance from desulfurization reactor come the virgin gas by desulfurization
Second methane synthesis reactor, two counter work off one's feeling vent one's spleen instead export heat exchangers, fresh air preheater, boiler water preheater two, pot through two
Hydrogen-rich methane rich fuel gas is made after exchanging heat in economizer three, boiler water preheater one after point one point of liquid of flow container；Boiler water
The reacting gas that preheater three is exported also can enter leucoaurin synthetic reaction through a point flow container two, three anti-entrance heat exchanger tube pass
Device, three it is counter work off one's feeling vent one's spleen through the preboiler water of boiler water preheater four, three anti-entrance heat exchanger shell pass preheatings three it is counter enter implication after
Into boiler water preheater one, hydrogen-rich methane rich fuel gas is made after heat exchange after point one point of liquid of flow container.
Specifically, the method for fuel gas-hydrogen coproduction is in the present invention：
Virgin gas enters the fresh shell side of air preheater 15, and the high methane gas come with the two anti-outlet tube sides of heat exchanger 14 exchanges heat, preheating
Unstripped gas afterwards enters hydrolysis reactor 1 and occurs hydrolysis, is inorganic sulfur by the tempreture organic sulphur hydrolysis in unstripped gas, then by de-
Total sulfur content in desulphurization reaction, reduction synthesis gas, which occurs, for reaction of Salmon-Saxl device 2, to below 50PPb, prevents methane synthesizing catalyst
Sulfur poisoning.
Carry out the virgin gas by desulfurization from desulfurization reactor 2, with recycle compressor export gas mixing after through two it is counter go out
Mouthful heat exchanger 14 exchanges heat to 220 DEG C ~ 260 DEG C, exit gas through an anti-entrance heat exchanger 9 and one it is counter work off one's feeling vent one's spleen exchange heat after into the
One methane synthesis reactor 3.The reactor is using adiabatic form, 260 DEG C ~ 310 DEG C of inlet temperature, outlet temperature 600 DEG C ~
650℃。
The exit gas of first methane synthesis reactor 3 is pre- to steam superheating, an anti-entrance heat exchanger 9 through steam superheater 11
Heat one it is counter enter implication, steam generator 12 generation steam after be divided into two strands, one is through the foreheater of compressor entrance heat exchanger 13
Stove feedwater, the preceding steady voltage stabilizing of tank 6, recycle compressor 10 are boosted, after the rear steady voltage stabilizing of tank 7 as circulating air with from desulfurization reactor 2
Virgin gas by desulfurization is mixed into two anti-outlet heat exchangers 14, another strand of the second methane synthesis reactor of entrance 4, two anti-gas
It is pre- through two anti-outlet heat exchangers 14, fresh air preheater 15, boiler water preheater 2 17, boiler water preheater 3 20, boiler water
Hydrogen-rich methane rich fuel gas is made after exchanging heat in hot device 1 after point one 8 points of liquid of flow container.
If the methane content being actually needed is higher, the reacting gas that boiler water preheater 3 20 is exported is through a point flow container 29, three
The anti-tube side of entrance heat exchanger 18 enters leucoaurin synthesis reactor 5, and three counter work off one's feeling vent one's spleen through the foreheater of boiler water preheater 4 21
Lu Shui, three anti-shell sides of entrance heat exchanger 18 preheatings three it is counter enter implication after enter boiler water preheater 1, through dividing a liquid after heat exchange
Hydrogen-rich methane rich fuel gas is made after one 8 points of liquid of tank.
The inlet temperature of second methane synthesis reactor 4 and leucoaurin synthesis reactor 5 is 250 DEG C ~ 260 DEG C respectively,
240 DEG C ~ 260 DEG C, outlet temperature is 450 DEG C ~ 490 DEG C, 360 DEG C ~ 400 DEG C respectively.First passed through before entering leucoaurin synthesis reactor 5
29 points of water of undue flow container, are conducive to methane synthetic reaction towards the direction movement of generation methane, improve product quality.
Methane volumetric fraction in the exit gas of second methane synthesis reactor 4（Butt）About 71.0% ~ 78.0%, leucoaurin
Methane volumetric fraction in the exit gas of synthesis reactor 5（Butt）About 91.0% ~ 94.5%.
The process condensate water for fill 1 from preceding steady tank 6, rear steady tank 7, point liquid, dividing liquid to fill 29 is mixed into process condensate water
Stripper, stripping vapor flashes off fixed gas, and the process condensate water after processing transfers out battery limit (BL) by process condensate water pump.
The inventive method technological process is simple, and small, flexible and convenient operation is taken up an area in investment, solve full factory fuel supply and
Hydrogen balance problem, with good economic benefit.
Brief description of the drawings
Fig. 1 is the process flow diagram of fuel gas of the embodiment of the present invention-hydrogen coproduction.
In figure, 1. hydrolysis reactors；2. desulfurization reactor；3. the first methane synthesis reactor；4. the synthesis of the second methane is anti-
Answer device；5. leucoaurin synthesis reactor；6. before steady tank；7. after steady tank；8. point flow container one；9. point flow container two；10. circulation compression
Machine；11. steam superheater；12. steam generator；13. suction port of compressor heat exchanger；14. two anti-outlet heat exchangers；15. it is fresh
Air preheater；16. boiler water preheater one；17. boiler water preheater two；18. three anti-entrance heat exchangers；19. an anti-entrance is changed
Hot device；20. boiler water preheater three；21. boiler water preheater four.
Embodiment
The present invention is described in detail with reference to the accompanying drawings and examples.
Embodiment 1
As shown in Figure 1,3.5MPa, 40 DEG C of unstripped gas (the gas composition molar fraction H come from upstream2 0.7515、CO
0.2147、CO2 0.0281、CH4 0.0009、N2 0.0034、Ar 0.0014、H2S+COS≤0.1ppmv）, into virgin gas
The shell side of preheater 15, the high methane gas come with the two anti-outlet tube sides of heat exchanger 14 exchanges heat, and it is anti-that the unstripped gas after preheating enters hydrolysis
Answer device 1 to occur hydrolysis, be inorganic sulfur by the tempreture organic sulphur hydrolysis in unstripped gas, then it is anti-by the generation desulfurization of desulfurization reactor 2
Should, total sulfur content prevents methane synthesizing catalyst from occurring sulfur poisoning to 50PPb in reduction synthesis gas.
Carry out the virgin gas by desulfurization from desulfurization reactor 2, with recycle compressor export gas mixing after through two it is counter go out
Mouth heat exchanger 14 exchanges heat to 260 DEG C, and exit gas enters the first methane after the anti-heat exchange of working off one's feeling vent one's spleen of an anti-entrance heat exchanger 9 and one
Synthesis reactor 3.The adiabatic form of reactor use, 310 DEG C of inlet temperature, outlet temperature is at 650 DEG C.
The exit gas of first methane synthesis reactor 3 is through steam superheater 11 to steam superheating, an anti-entrance heat exchanger 19
Preheating one it is counter enter implication, steam generator 12 generation steam after be divided into two strands, one is preheated through compressor entrance heat exchanger 13
Boiler feedwater, the preceding steady voltage stabilizing of tank 6, recycle compressor 10 are boosted, after the rear steady voltage stabilizing of tank 7 as circulating air with from desulfurization reactor 2
Two anti-outlet heat exchangers 14 are mixed into come the virgin gas by desulfurization, another strand of the second methane synthesis reactor of entrance 4, two is anti-
Gas is through two anti-outlet heat exchangers 14, fresh air preheater 15, boiler water preheater 2 17, boiler water preheater 3 20, point flow container
29, the three anti-tube sides of entrance heat exchanger 18 enter leucoaurin synthesis reactor 5, and three counter work off one's feeling vent one's spleen through boiler water preheater 4 21
Preboiler water, three anti-shell sides of entrance heat exchanger 18 preheatings three it is counter enter implication after into boiler water preheater 1, after heat exchange
Hydrogen-rich methane rich fuel gas is made after point one 8 points of liquid of flow container.
The inlet temperature of second methane synthesis reactor 4 and leucoaurin synthesis reactor 5 is 260 DEG C, 260 DEG C respectively,
Outlet temperature is 490 DEG C, 400 DEG C respectively.
Methane volumetric fraction in the exit gas of second methane synthesis reactor 4（Butt）71.0%, leucoaurin synthetic reaction
Methane volumetric fraction in the exit gas of device 5（Butt）91.0%.
Embodiment 2
As shown in Figure 1,3.5MPa, 40 DEG C of unstripped gas (the gas composition molar fraction H come from upstream2 0.7515、CO
0.2147、CO2 0.0281、CH4 0.0009、N2 0.0034、Ar 0.0014、H2S+COS≤0.1ppmv）, into virgin gas
The shell side of preheater 15, the high methane gas come with the two anti-outlet tube sides of heat exchanger 14 exchanges heat, and it is anti-that the unstripped gas after preheating enters hydrolysis
Answer device 1 to occur hydrolysis, be inorganic sulfur by the tempreture organic sulphur hydrolysis in unstripped gas, then it is anti-by the generation desulfurization of desulfurization reactor 2
Should, total sulfur content is to 45PPb in reduction synthesis gas.
Carry out the virgin gas by desulfurization from desulfurization reactor 2, with recycle compressor export gas mixing after through two it is counter go out
Mouth heat exchanger 14 exchanges heat to 220 DEG C, and exit gas enters the first methane after the anti-heat exchange of working off one's feeling vent one's spleen of an anti-entrance heat exchanger 9 and one
Synthesis reactor 3.The adiabatic form of reactor use, 260 DEG C of inlet temperature, outlet temperature is at 600 DEG C.
The exit gas of first methane synthesis reactor 3 is through steam superheater 11 to steam superheating, an anti-entrance heat exchanger 19
Preheating one it is counter enter implication, steam generator 12 generation steam after be divided into two strands, one is preheated through compressor entrance heat exchanger 13
Boiler feedwater, the preceding steady voltage stabilizing of tank 6, recycle compressor 10 are boosted, after the rear steady voltage stabilizing of tank 7 as circulating air with from desulfurization reactor 2
Two anti-outlet heat exchangers 14 are mixed into come the virgin gas by desulfurization, another strand of the second methane synthesis reactor of entrance 4, two is anti-
Gas is through two anti-outlet heat exchangers 14, fresh air preheater 15, boiler water preheater 2 17, boiler water preheater 3 20, point flow container
29, the three anti-tube sides of entrance heat exchanger 18 enter leucoaurin synthesis reactor 5, and three counter work off one's feeling vent one's spleen through boiler water preheater 4 21
Preboiler water, three anti-shell sides of entrance heat exchanger 18 preheatings three it is counter enter implication after into boiler water preheater 1, after heat exchange
Hydrogen-rich methane rich fuel gas is made after point one 8 points of liquid of flow container.
The inlet temperature of second methane synthesis reactor 4 and leucoaurin synthesis reactor 5 is 250 DEG C, 240 DEG C respectively,
Outlet temperature is 450 DEG C, 360 DEG C respectively.
Methane volumetric fraction in the exit gas of second methane synthesis reactor 4（Butt）78.0%, leucoaurin synthetic reaction
Methane volumetric fraction in the exit gas of device 5（Butt）94.5%.
Embodiment 3
As shown in Figure 1,3.5MPa, 40 DEG C of unstripped gas (the gas composition molar fraction H come from upstream2 0.7515、CO
0.2147、CO2 0.0281、CH4 0.0009、N2 0.0034、Ar 0.0014、H2S+COS≤0.1ppmv）, into virgin gas
The shell side of preheater 15, the high methane gas come with the two anti-outlet tube sides of heat exchanger 14 exchanges heat, and it is anti-that the unstripped gas after preheating enters hydrolysis
Answer device 1 to occur hydrolysis, be inorganic sulfur by the tempreture organic sulphur hydrolysis in unstripped gas, then it is anti-by the generation desulfurization of desulfurization reactor 2
Should, total sulfur content is to 40PPb in reduction synthesis gas.
Carry out the virgin gas by desulfurization from desulfurization reactor 2, with recycle compressor export gas mixing after through two it is counter go out
Mouth heat exchanger 14 exchanges heat to 240 DEG C, and exit gas enters the first methane after the anti-heat exchange of working off one's feeling vent one's spleen of an anti-entrance heat exchanger 9 and one
Synthesis reactor 3.The adiabatic form of reactor use, 285 DEG C of inlet temperature, outlet temperature is at 630 DEG C.
The exit gas of first methane synthesis reactor 3 is through steam superheater 11 to steam superheating, an anti-entrance heat exchanger 19
Preheating one it is counter enter implication, steam generator 12 generation steam after be divided into two strands, one is preheated through compressor entrance heat exchanger 13
Boiler feedwater, the preceding steady voltage stabilizing of tank 6, recycle compressor 10 are boosted, after the rear steady voltage stabilizing of tank 7 as circulating air with from desulfurization reactor 2
Two anti-outlet heat exchangers 14 are mixed into come the virgin gas by desulfurization, another strand of the second methane synthesis reactor of entrance 4, two is anti-
Gas is through two anti-outlet heat exchangers 14, fresh air preheater 15, boiler water preheater 2 17, boiler water preheater 3 20, point flow container
29, the three anti-tube sides of entrance heat exchanger 18 enter leucoaurin synthesis reactor 5, and three counter work off one's feeling vent one's spleen through boiler water preheater 4 21
Preboiler water, three anti-shell sides of entrance heat exchanger 18 preheatings three it is counter enter implication after into boiler water preheater 1, after heat exchange
Hydrogen-rich methane rich fuel gas is made after point one 8 points of liquid of flow container.
The inlet temperature of second methane synthesis reactor 4 and leucoaurin synthesis reactor 5 is 250 DEG C, 250 DEG C respectively,
Outlet temperature is 470 DEG C, 380 DEG C respectively.
Methane volumetric fraction in the exit gas of second methane synthesis reactor 4（Butt）75.0%, leucoaurin synthetic reaction
Methane volumetric fraction in the exit gas of device 5（Butt）92.0%.
Embodiment 4
As shown in Figure 1,3.5MPa, 40 DEG C of unstripped gas (the gas composition molar fraction H come from upstream2 0.6871、CO
0.1954、CO2 0.0224、CH4 0.0899、N2 0.0031、Ar 0.0021、H2S+COS≤0.1ppmv）, into virgin gas
The shell side of preheater 15, the high methane gas come with the two anti-outlet tube sides of heat exchanger 14 exchanges heat, and it is anti-that the unstripped gas after preheating enters hydrolysis
Answer device 1 to occur hydrolysis, be inorganic sulfur by the tempreture organic sulphur hydrolysis in unstripped gas, then it is anti-by the generation desulfurization of desulfurization reactor 2
Should, total sulfur content is to 40PPb in reduction synthesis gas.
Carry out the virgin gas by desulfurization from desulfurization reactor 2, with recycle compressor export gas mixing after through two it is counter go out
Mouth heat exchanger 14 exchanges heat to 240 DEG C, and exit gas enters the first first after the anti-heat exchange of working off one's feeling vent one's spleen of an anti-entrance heat exchanger 19 and one
Alkane synthesis reactor 3.The adiabatic form of reactor use, 280 DEG C of inlet temperature, outlet temperature is at 620 DEG C.
The exit gas of first methane synthesis reactor 3 is pre- to steam superheating, an anti-entrance heat exchanger 9 through steam superheater 11
Heat one it is counter enter implication, steam generator 12 generation steam after be divided into two strands, one is through the foreheater of compressor entrance heat exchanger 13
Stove feedwater, the preceding steady voltage stabilizing of tank 6, recycle compressor 10 are boosted, after the rear steady voltage stabilizing of tank 7 as circulating air with from desulfurization reactor 2
Virgin gas by desulfurization is mixed into two anti-outlet heat exchangers 14, another strand of the second methane synthesis reactor of entrance 4, two anti-gas
Through two anti-outlet heat exchangers 14, fresh air preheater 15, boiler water preheater 2 17, boiler water preheater 3 20, point flow container two
9th, the three anti-tube sides of entrance heat exchanger 18 enter leucoaurin synthesis reactor 5, three it is counter work off one's feeling vent one's spleen it is pre- through boiler water preheater 4 21
Heat boiler water, three anti-shell sides of entrance heat exchanger 18 preheatings three it is counter enter implication after into boiler water preheater 1, passed through after heat exchange
Divide and hydrogen-rich methane rich fuel gas is made after one 8 points of liquid of flow container.
The inlet temperature of second methane synthesis reactor 4 and leucoaurin synthesis reactor 5 is 250 DEG C, 250 DEG C respectively,
Outlet temperature is 460 DEG C, 370 DEG C respectively.
Methane volumetric fraction in the exit gas of second methane synthesis reactor 4（Butt）77.0%, leucoaurin synthetic reaction
Methane volumetric fraction in the exit gas of device 5（Butt）93.0%.
Embodiment 5
As shown in Figure 1,1.0MPa, 40 DEG C of unstripped gas (the gas composition molar fraction H come from upstream2 0.7515、CO
0.2147、CO2 0.0281、CH4 0.0009、N2 0.0034、Ar 0.0014、H2S+COS≤0.1ppmv）, into virgin gas
The shell side of preheater 15, the high methane gas come with the two anti-outlet tube sides of heat exchanger 14 exchanges heat, and it is anti-that the unstripped gas after preheating enters hydrolysis
Answer device 1 to occur hydrolysis, be inorganic sulfur by the tempreture organic sulphur hydrolysis in unstripped gas, then it is anti-by the generation desulfurization of desulfurization reactor 2
Should, total sulfur content is to 45PPb in reduction synthesis gas.
Carry out the virgin gas by desulfurization from desulfurization reactor 2, with recycle compressor export gas mixing after through two it is counter go out
Mouth heat exchanger 14 exchanges heat to 220 DEG C, and exit gas enters the first methane after the anti-heat exchange of working off one's feeling vent one's spleen of an anti-entrance heat exchanger 9 and one
Synthesis reactor 3.The adiabatic form of reactor use, 270 DEG C of inlet temperature, outlet temperature is at 600 DEG C.
The exit gas of first methane synthesis reactor 3 is through steam superheater 11 to steam superheating, an anti-entrance heat exchanger 19
Preheating one it is counter enter implication, steam generator 12 generation steam after be divided into two strands, one is preheated through compressor entrance heat exchanger 13
Boiler feedwater, the preceding steady voltage stabilizing of tank 6, recycle compressor 10 are boosted, after the rear steady voltage stabilizing of tank 7 as circulating air with from desulfurization reactor 2
Two anti-outlet heat exchangers 14 are mixed into come the virgin gas by desulfurization, another strand of the second methane synthesis reactor of entrance 4, two is anti-
Gas is through two anti-outlet heat exchangers 14, fresh air preheater 15, boiler water preheater 2 17, boiler water preheater 3 20, point flow container
29, the three anti-tube sides of entrance heat exchanger 18 enter leucoaurin synthesis reactor 5, and three counter work off one's feeling vent one's spleen through boiler water preheater 4 21
Preboiler water, three anti-shell sides of entrance heat exchanger 18 preheatings three it is counter enter implication after into boiler water preheater 1, after heat exchange
Hydrogen-rich methane rich fuel gas is made after point one 8 points of liquid of flow container.
The inlet temperature of second methane synthesis reactor 4 and leucoaurin synthesis reactor 5 is 260 DEG C, 250 DEG C respectively,
Outlet temperature is 450 DEG C, 360 DEG C respectively.
Methane volumetric fraction in the exit gas of second methane synthesis reactor 4（Butt）75.8%, leucoaurin synthetic reaction
Methane volumetric fraction in the exit gas of device 5（Butt）92.5%.
Embodiment 6
As shown in Figure 1,8.0MPa, 40 DEG C of unstripped gas (the gas composition molar fraction H come from upstream2 0.7515、CO
0.2147、CO2 0.0281、CH4 0.0009、N2 0.0034、Ar 0.0014、H2S+COS≤0.1ppmv）, into virgin gas
The shell side of preheater 15, the high methane gas come with the two anti-outlet tube sides of heat exchanger 14 exchanges heat, and it is anti-that the unstripped gas after preheating enters hydrolysis
Answer device 1 to occur hydrolysis, be inorganic sulfur by the tempreture organic sulphur hydrolysis in unstripped gas, then it is anti-by the generation desulfurization of desulfurization reactor 2
Should, total sulfur content prevents methane synthesizing catalyst from occurring sulfur poisoning to 50PPb in reduction synthesis gas.
Carry out the virgin gas by desulfurization from desulfurization reactor 2, with recycle compressor export gas mixing after through two it is counter go out
Mouth heat exchanger 14 exchanges heat to 260 DEG C, and exit gas enters the first methane after the anti-heat exchange of working off one's feeling vent one's spleen of an anti-entrance heat exchanger 9 and one
Synthesis reactor 3.The adiabatic form of reactor use, 305 DEG C of inlet temperature, outlet temperature is at 650 DEG C.
The exit gas of first methane synthesis reactor 3 is through steam superheater 11 to steam superheating, an anti-entrance heat exchanger 19
Preheating one it is counter enter implication, steam generator 12 generation steam after be divided into two strands, one is preheated through compressor entrance heat exchanger 13
Boiler feedwater, the preceding steady voltage stabilizing of tank 6, recycle compressor 10 are boosted, after the rear steady voltage stabilizing of tank 7 as circulating air with from desulfurization reactor 2
Two anti-outlet heat exchangers 14 are mixed into come the virgin gas by desulfurization, another strand of the second methane synthesis reactor of entrance 4, two is anti-
Gas is through two anti-outlet heat exchangers 14, fresh air preheater 15, boiler water preheater 2 17, boiler water preheater 3 20, point flow container
29, the three anti-tube sides of entrance heat exchanger 18 enter leucoaurin synthesis reactor 5, and three counter work off one's feeling vent one's spleen through boiler water preheater 4 21
Preboiler water, three anti-shell sides of entrance heat exchanger 18 preheatings three it is counter enter implication after into boiler water preheater 1, after heat exchange
Hydrogen-rich methane rich fuel gas is made after point one 8 points of liquid of flow container.
The inlet temperature of second methane synthesis reactor 4 and leucoaurin synthesis reactor 5 is 255 DEG C, 255 DEG C respectively,
Outlet temperature is 490 DEG C, 400 DEG C respectively.
Methane volumetric fraction in the exit gas of second methane synthesis reactor 4（Butt）73.2%, leucoaurin synthetic reaction
Methane volumetric fraction in the exit gas of device 5（Butt）92.9%.
Claims (6)
1. a kind of fuel gas-hydrogen joint production process, it is characterised in that：Virgin gas enter fresh air preheater shell side, with two it is counter go out
The high methane gas heat exchange that mouth heat exchanger tube pass comes, the unstripped gas after preheating enters hydrolysis reactor and occurs hydrolysis, by raw material
Tempreture organic sulphur hydrolysis in gas is inorganic sulfur, then occurs in desulphurization reaction, reduction synthesis gas total sulfur content extremely by desulfurization reactor
Below 50PPb, prevents methane synthesizing catalyst from occurring sulfur poisoning；Carry out the virgin gas by desulfurization from desulfurization reactor, with circulation
Through two anti-outlet heat exchanger heat exchange after the gas mixing of compressor outlet, exit gas is through an anti-entrance heat exchanger and an anti-outlet
Enter the first methane synthesis reactor after gas heat exchange；First methane synthesis reactor exit gas is through steam superheater to steam mistake
Heat, an anti-entrance heat exchanger preheating one it is counter enter implication, steam generator generation steam after be divided into two strands, one enters through compressor
As circulating air and from desulfurization after the feedwater of mouthful heat exchanger preboiler, preceding steady tank voltage stabilizing, recycle compressor boosting, rear steady tank voltage stabilizing
Reactor is mixed into two anti-outlet heat exchangers come the virgin gas by desulfurization, another strand of methane synthesis reactor of entrance second,
Two counter work off one's feeling vent one's spleen instead export heat exchangers, fresh air preheater, boiler water preheater two, boiler water preheater three, boiler water through two
Hydrogen-rich methane rich fuel gas is made after exchanging heat in preheater one after point one point of liquid of flow container；The reaction gas that boiler water preheater three is exported
Body can also enter leucoaurin synthesis reactor through a point flow container two, three anti-entrance heat exchanger tube pass, and three counter work off one's feeling vent one's spleen through boiler water
The preboiler water of preheater four, three anti-entrance heat exchanger shell pass preheatings three it is counter enter implication after into boiler water preheater one, change
Hydrogen-rich methane rich fuel gas is made after heat after point one point of liquid of flow container.
2. technique as claimed in claim 1, it is characterised in that the first methane synthesis reactor is using adiabatic form, inlet temperature
Scope is 260 DEG C ~ 310 DEG C, and outlet temperature scope is 600 DEG C ~ 650 DEG C.
3. technique as claimed in claim 1, it is characterised in that the second methane synthesis reactor inlet temperature is 250 DEG C ~
260 DEG C, outlet temperature scope is 450 DEG C ~ 490 DEG C.
4. technique as claimed in claim 1, it is characterised in that the inlet temperature of leucoaurin synthesis reactor is 240 DEG C
~ 260 DEG C, outlet temperature scope is 360 DEG C ~ 400 DEG C.
5. technique as claimed in claim 1, it is characterised in that three methane synthesis reactor pressure limits are 1MPa ~ 8MPa.
6. technique as claimed in claim 1, it is characterised in that first in the butt gas of the second methane synthesis reactor exit gas
Alkane volume fraction is 71.0% ~ 78.0%, and methane volumetric fraction is in the butt gas of the exit gas of leucoaurin synthesis reactor 5
91.0%~94.5%。
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