CN208345753U - By the vapor reforming hydrogen production device of high-temperature flue gas heat supply - Google Patents
By the vapor reforming hydrogen production device of high-temperature flue gas heat supply Download PDFInfo
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- CN208345753U CN208345753U CN201820726671.XU CN201820726671U CN208345753U CN 208345753 U CN208345753 U CN 208345753U CN 201820726671 U CN201820726671 U CN 201820726671U CN 208345753 U CN208345753 U CN 208345753U
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- Prior art keywords
- flue gas
- heat
- gas
- pipe
- efferent duct
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Links
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 179
- 239000003546 flue gas Substances 0.000 title claims abstract description 123
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 106
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 92
- 239000001257 hydrogen Substances 0.000 title claims abstract description 92
- 238000002407 reforming Methods 0.000 title claims abstract description 78
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 48
- 238000006243 chemical reaction Methods 0.000 claims abstract description 93
- 239000007789 gas Substances 0.000 claims abstract description 85
- 239000000463 material Substances 0.000 claims abstract description 74
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 56
- 230000007246 mechanism Effects 0.000 claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 30
- 239000000779 smoke Substances 0.000 claims description 23
- 238000010438 heat treatment Methods 0.000 claims description 14
- 239000002994 raw material Substances 0.000 claims description 14
- 238000007599 discharging Methods 0.000 claims description 9
- 238000006477 desulfuration reaction Methods 0.000 claims description 7
- 230000023556 desulfurization Effects 0.000 claims description 7
- 230000009466 transformation Effects 0.000 claims description 6
- 238000000746 purification Methods 0.000 claims description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 230000003647 oxidation Effects 0.000 claims description 4
- 238000007254 oxidation reaction Methods 0.000 claims description 4
- 239000006096 absorbing agent Substances 0.000 claims description 3
- 238000009825 accumulation Methods 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 238000001914 filtration Methods 0.000 claims description 2
- 239000002918 waste heat Substances 0.000 abstract description 8
- 230000008901 benefit Effects 0.000 abstract description 7
- 239000004215 Carbon black (E152) Substances 0.000 description 16
- 229930195733 hydrocarbon Natural products 0.000 description 16
- 150000002430 hydrocarbons Chemical class 0.000 description 16
- 238000006057 reforming reaction Methods 0.000 description 11
- 239000005864 Sulphur Substances 0.000 description 4
- 238000010612 desalination reaction Methods 0.000 description 4
- 239000002737 fuel gas Substances 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- 229960004424 carbon dioxide Drugs 0.000 description 3
- 229910002090 carbon oxide Inorganic materials 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000005192 partition Methods 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 238000005899 aromatization reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- -1 have: natural gas Chemical class 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000001727 in vivo Methods 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000009423 ventilation Methods 0.000 description 1
Classifications
-
- 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
Landscapes
- Hydrogen, Water And Hydrids (AREA)
Abstract
The utility model discloses a kind of vapor reforming hydrogen production devices by high-temperature flue gas heat supply, it include: reforming reactor, carbon monoxide converter, pressure swing adsorber, the structure of reforming reactor includes: shell, flue gas input pipe is provided on shell, vapor input pipe, material delivery pipe, reform gas efferent duct, it is divided into reformer section and heat-accumulating area in shell, several reaction tubes are provided in reformer section, heat-accumulating area is located at the side of reaction tube discharge end, if being provided with dry material economizer bank in heat-accumulating area, material delivery pipe is connected with the input terminal of material economizer bank, the output end and vapor input pipe of material economizer bank are connected with the feed end of reaction tube, flue gas output mechanism is provided on the shell of heat-accumulating area；It reforms gas efferent duct to be connected with carbon monoxide converter, the conversion gas efferent duct of the bottom of carbon monoxide converter is connected with pressure swing adsorber.Utility model has the advantages that high-temperature flue gas waste heat can be made full use of, hydrogen manufacturing cost is substantially reduced.
Description
Technical field
The utility model relates to vapor reforming hydrogen production equipment technical fields.
Background technique
Currently, the structure of vapor reforming hydrogen production device specifically includes that reforming reactor, carbon monoxide converter, transformation
Absorber is provided with several reaction tubes in the shell of reforming reactor, fuel gas delivery pipe, sky is connected on reforming reactor
Letter shoot, vapor input pipe and material delivery pipe and reformation gas efferent duct, fuel gas delivery pipe and air delivery pipe
It is connected respectively with the shell of reforming reactor, to will act as the gas of fuel respectively and for combustion-supporting air delivery to shell
One end combustion heat supplying of igniter is installed in vivo, vapor input pipe and material delivery pipe respectively with shell is intracorporal each reacts
The feed end of pipe is connected, so that the vapor for participating in reaction and hydrocarbon material are delivered to the intracorporal each reaction tube of shell respectively
Feed end, reform gas efferent duct stretch out shell be connected with carbon monoxide converter, the reformation gas of generation is reacted in reaction tube
Body is delivered in carbon monoxide converter by reformation gas efferent duct, and the carbon monoxide converter is using jacket type heating knot
Structure, the heat medium in carbon monoxide converter chuck layer is conduction oil, and the bottom of carbon monoxide converter is provided with conversion gas
Efferent duct, conversion gas efferent duct are connected with pressure swing adsorber, and the converted gas of generation is reacted in carbon monoxide converter by turning
Ventilation efferent duct, which is delivered in pressure swing adsorber, to be purified, and tail gas efferent duct and hydrogen efferent duct are provided on pressure swing adsorber, is become
The ultra-pure hydrogen that pressure absorber purification generates is exported by hydrogen efferent duct, and the pressure-variable adsorption tail gas that pressure swing adsorber generates is by tail gas
Efferent duct output.
Above-mentioned vapor reforming hydrogen production device has the following deficiencies: one, needs additionally using fuel gas heat supply, this leads
Cause hydrogen manufacturing with high costs.Two, fuel gas and combustion-supporting gas needs are lighted in reforming reactor shell side shell, reforming reactor
Interior to need additionally mounted igniter, this makes reforming reactor, and structure is complicated.
In addition, the high-temperature flue gas for having many industries to generate at present, such as coke oven high-temperature flue gas, the waste heat of high-temperature flue gas is mostly all
It is not fully used, this causes thermal energy to be largely lost.
Utility model content
The purpose of this utility model is: provide it is a kind of can make full use of high-temperature flue gas waste heat and can substantially reduce hydrogen manufacturing at
This vapor reforming hydrogen production device by high-temperature flue gas heat supply.
In order to achieve the above purposes, the technical solution adopted by the utility model is: by high-temperature flue gas heat supply steam reforming
Device for producing hydrogen, comprising: reforming reactor, carbon monoxide converter, pressure swing adsorber, the structure of reforming reactor include: shell,
It is provided with flue gas input pipe on shell, vapor input pipe, material delivery pipe, reforms gas efferent duct, is divided into reformer section in shell
And heat-accumulating area, several reaction tubes are provided in reformer section, and flue gas input pipe is connected with the shell of reaction tube feed end, reforms gas
Efferent duct is connected with the discharge end of reaction tube, and heat-accumulating area is located at the side of reaction tube discharge end, is provided in heat-accumulating area several
Material economizer bank, material delivery pipe are connected with the input terminal of material economizer bank, the output end and vapor of material economizer bank
Input pipe is connected with the feed end of reaction tube, flue gas output mechanism is provided on the shell of heat-accumulating area, high-temperature flue gas is by cigarette
Gas input pipe enters to the reformer section of reaction tube feed end, and the high-temperature flue gas in reformer section is moved to instead by the feed end of reaction tube
Should pipe discharge end subsequently into heat-accumulating area, the flue gas of heat-accumulating area is discharged by flue gas output mechanism；Reform gas efferent duct and one
Carbonoxide converter is connected, and the reformed gas that reaction inner reaction tube generates is delivered to carbon monoxide conversion by reformation gas efferent duct
In device, the bottom of carbon monoxide converter is provided with conversion gas efferent duct, and conversion gas efferent duct is connected with pressure swing adsorber, and one
The carbon monoxide converted gas that reaction generates in carbonoxide converter is delivered in pressure swing adsorber by conversion gas efferent duct to be purified,
Pressure swing adsorber is connected with tail gas efferent duct and hydrogen efferent duct, and the ultra-pure hydrogen that pressure swing adsorber purification generates is exported by hydrogen
Pipe output, the pressure-variable adsorption tail gas that pressure swing adsorber generates are exported by tail gas efferent duct.
Further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein the flue gas of heat-accumulating area is defeated
Mechanism is connected with heat exchange boiler out, and the flue gas of heat-accumulating area enters to heat supply in heat exchange boiler by flue gas output mechanism, heat exchange
It is connected with water pipe and jet chimney with water pump on boiler, is provided with smoke discharging pipe at the top of heat exchange boiler, in heat exchange boiler
Flue gas is discharged from smoke discharging pipe, the heat medium input of the heating jacket of the jet chimney and carbon monoxide converter of heat exchange boiler
End is connected, and the water pipe of heat exchange boiler is connected with the heat medium output end of the heating jacket of carbon monoxide converter, heat exchange
The steam generated in boiler constantly passes through jet chimney and enters in the heating jacket of carbon monoxide converter, thus for an oxidation
Heat supply in carbon converter, the interior water formed of the heating jacket of carbon monoxide converter constantly pass through water pipe and enter to heat exchange boiler
In.
Further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein heat exchange boiler with again
Whole reactor becomes one.
Further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein carbon monoxide converter
The conversion gas efferent duct of bottom is first sequentially communicated to cooler and steam trap, is then connected again with pressure swing adsorber.
Still further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein carbon monoxide conversion
Conversion gas efferent duct between device and cooler is connected to feed-water preheating boiler, and feed pipe is provided on feed-water preheating boiler and is gone out
Water pipe, outlet pipe are connected to evaporator, and the steam output end of evaporator is connected with the vapor input pipe of reforming reactor, weight
Whole gas efferent duct is first connected to evaporator and is connected again with carbon monoxide converter, and the reformation gas for reforming the output of gas efferent duct is advanced
Enter and is entered back into carbon monoxide converter after carrying out heat exchange to evaporator.
Further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein on material delivery pipe according to
It is secondary to be connected with devulcanizer and filter, by material delivery pipe conveying material successively through devulcanizer desulfurization, filter filtering after again
It is transported in the material economizer bank in reforming reactor heat-accumulating area；The flue gas output mechanism of reforming reactor heat-accumulating area also with it is de-
Sulphur device is connected, and the flue gas of reforming reactor heat-accumulating area enters to heat supply in devulcanizer through flue gas output mechanism.
Further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein in material delivery pipe
Material exported by raw material buffer gear, raw material buffer gear includes: the raw material surge tank and preheater being sequentially communicated, and raw material is slow
It is delivered in devulcanizer after rushing the preheated device preheating of the material in tank by material delivery pipe, is arranged between devulcanizer and preheater
There is devulcanizer smoke discharge tube, the flue gas being discharged from devulcanizer enters in preheater through devulcanizer smoke discharge tube, preheater
On be provided with blow-down pipe, the flue gas in preheater is discharged from blow-down pipe.
Still further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein pressure swing adsorber
Hydrogen efferent duct is connected to hydrogen gas buffer, circulating hydrogen delivery pipe is provided on hydrogen gas buffer and outer for hydrogen delivery tube,
Circulating hydrogen delivery pipe is connected with devulcanizer, and the hydrogen partial in hydrogen gas buffer enters to desulfurization through circulating hydrogen delivery pipe
Desulphurization reaction is carried out in device, remaining hydrogen in hydrogen gas buffer is supplied through outer for hydrogen delivery tube outward.
Further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein set on flue gas input pipe
It is equipped with thermoregulator, is entered back into after the temperature regulated device adjustment temperature of high-temperature flue gas to the shell of reforming reactor.
Further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein thermoregulator is
Conduction oil thermostat, conduction oil thermostat are connected with conduction oil heat exchanger tube, and the conduction oil heat exchanger tube is arranged in heat exchange boiler
It is interior, it is provided with Heat-transfer Oil Pump on conduction oil heat exchanger tube, under the action of Heat-transfer Oil Pump, conduction oil is constantly from conduction oil thermostat
It enters to from conduction oil heat exchanger tube, is then entered in conduction oil thermostat from the output end of conduction oil heat exchanger tube again；High temperature
Flue gas through flue gas input pipe enter in conduction oil thermostat carry out temperature adjusting after, enter back into the shell of reforming reactor.
Further, the vapor reforming hydrogen production device above-mentioned by high-temperature flue gas heat supply, wherein reforming reactor shell
The reformer section of reaction tubes charging end position is provided with mixer, and material economizer bank output end and vapor input pipe first connect
Mixer is passed to, mixer is connected to each reaction tube feed end again.
The utility model has the advantages that: one, using high-temperature flue gas heat supply, fume afterheat is made full use of, to reduce hydrogen manufacturing
Cost.Two, be divided into reformer section and heat-accumulating area in the shell of reforming reactor, the material economizer bank in heat-accumulating area to enter reaction tube
The hydrocarbon material of interior reaction is preheated, and the waste heat of flue gas is not only taken full advantage of, moreover it is possible to be effectively improved in reaction tube and be reformed instead
The rate and conversion ratio answered.Three, heat exchange boiler is set, the flue gas after heat exchange will have been carried out with material economizer bank in heat-accumulating area
It is delivered to heat supply in heat exchange boiler, the steam of the generation in heat exchange boiler is used as the heat medium of carbon monoxide converter, this is big
The energy consumption for reducing hydrogen production process greatly, thus effectively save hydrogen manufacturing cost.Four, the conversion that reaction generates in carbon monoxide converter
Gas is introduced into evaporator heat supply, and the desalination vapor as reforming reaction that evaporator generates, this can further be dropped again
Heat energy loss in low hydrogen production process, to further reduced hydrogen manufacturing cost.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the vapor reforming hydrogen production device described in the utility model by high-temperature flue gas heat supply.
Fig. 2 is the structural schematic diagram that the heat exchange boiler in Fig. 1 becomes one with reforming reactor.
Specific embodiment
The utility model is described in further detail with preferred embodiment with reference to the accompanying drawing.
As shown in Figure 1 and Figure 2, by the vapor reforming hydrogen production device of high-temperature flue gas heat supply, comprising: reforming reactor 1, one
Carbonoxide converter 2, pressure swing adsorber 3.In the present embodiment, the structure of reforming reactor 1 includes: shell 11, is set on shell 11
It is equipped with flue gas input pipe 12, vapor input pipe 13, material delivery pipe 14, reforms gas efferent duct 15.It is divided into reformation in shell 11
Area 101 and heat-accumulating area 102.Several reaction tubes 16, flue gas input pipe 12 and 16 feed end of reaction tube are provided in reformer section 101
Shell 11 is connected, and reforms gas efferent duct 15 and is connected with the discharge end of reaction tube 16.Heat-accumulating area 102 is located at the discharging of reaction tube 16
The side at end, if being provided with dry material economizer bank 17 in heat-accumulating area 102, the input terminal of material delivery pipe 14 and material economizer bank 17
It is connected, the output end and vapor input pipe 13 of material economizer bank 17 are connected with the feed end of reaction tube 16, accumulation of heat
Flue gas output mechanism is provided on the shell 11 in area 102.High-temperature flue gas enters to 16 feed end of reaction tube by flue gas input pipe 12
Reformer section 101, the discharge end that the high-temperature flue gas in reformer section 101 moves to reaction tube 16 by the feed end of reaction tube 16 is laggard
Enter heat-accumulating area 102, the flue gas of heat-accumulating area 102 is discharged by flue gas output mechanism.
In the present embodiment, mixer 19, material economizer bank 17 are provided in the reformer section 101 of the charging end position of reaction tube 16
Output end and vapor input pipe 13 be first connected to mixer 19, mixer 19 is connected to the charging of each reaction tube 16 again
End.The purpose that mixer 19 is arranged is: entering back into the hydrocarbon material for participating in reforming reaction and vapor after mixing instead
Should be in pipe 16, this can effectively improve the conversion ratio of reforming reaction in reaction tube 16.
Gas efferent duct 15 is reformed to be connected with carbon monoxide converter 2, in reaction tube 16 reformed gas of reaction generation by
Gas efferent duct 15 is reformed to be delivered in carbon monoxide converter 2.The bottom of carbon monoxide converter 2 is provided with conversion gas efferent duct
21, conversion gas efferent duct 21 is connected with pressure swing adsorber 3.The carbon monoxide conversion that reaction generates in carbon monoxide converter 2
Gas is delivered in pressure swing adsorber 3 by conversion gas efferent duct 21 and is purified.Pressure swing adsorber 3 is connected with tail gas efferent duct 31 and hydrogen
Gas efferent duct 32, the ultra-pure hydrogen that the purification of pressure swing adsorber 3 generates are exported by hydrogen efferent duct 32, what pressure swing adsorber 3 generated
Pressure-variable adsorption tail gas is exported by tail gas efferent duct 31.
Flue gas output mechanism in heat-accumulating area 102 is connected with heat exchange boiler 4, and the part of smoke in heat-accumulating area 102 is logical
It crosses flue gas output mechanism and enters to heat supply in heat exchange boiler 4.Water pipe 41 and steam with water pump 411 are connected on heat exchange boiler 4
Pipeline 42, the top of heat exchange boiler 4 are provided with smoke discharging pipe 43, and the flue gas in heat exchange boiler 4 is discharged from smoke discharging pipe 43, this
The air blower 431 for constantly conveying flue gas outward is additionally provided in embodiment on smoke discharging pipe 43.The jet chimney of heat exchange boiler 4
42 are connected with the heat medium input terminal of the heating jacket of carbon monoxide converter 2, the water pipe 41 of heat exchange boiler 4 and an oxidation
The heat medium output end of the heating jacket of carbon converter 2 is connected, and the steam generated in heat exchange boiler 4 constantly passes through steam pipe
Road 42 enters in the heating jacket of carbon monoxide converter 2, to be 2 heat supply of carbon monoxide converter, carbon monoxide conversion
The water formed in the heating jacket of device 2 constantly passes through water pipe 41 and enters in heat exchange boiler 4.
In order to which the temperature to the high-temperature flue gas entered in reforming reactor 1 is adjusted and controls, on flue gas input pipe 12
It is provided with thermoregulator, is entered back into after the temperature regulated device adjustment temperature of high-temperature flue gas to reforming reactor 1.Specifically,
Thermoregulator is conduction oil thermostat 120 in the present embodiment, and conduction oil thermostat 120 is connected with conduction oil heat exchanger tube 121, institute
The conduction oil heat exchanger tube 121 stated is arranged in heat exchange boiler 4, and Heat-transfer Oil Pump 122 is provided on conduction oil heat exchanger tube 121, is being led
Under the action of hot oil pump 122, conduction oil is constantly entered to from conduction oil heat exchanger tube 121 from conduction oil thermostat 120, then
It is entered in conduction oil thermostat 120 from the output end of conduction oil heat exchanger tube 121 again；High-temperature flue gas enters through flue gas input pipe 12
After carrying out temperature adjusting in conduction oil thermostat 120, enter back into the shell 11 of reforming reactor 1, this can effectively ensure instead
Should in pipe 16 reforming reaction reaction temperature, to effectively improve reforming reaction efficiency.
In order to which the converted gas exported to carbon monoxide converter 2 cools down, carbon monoxide converter 2 in the present embodiment
The conversion gas efferent duct 21 of bottom is first sequentially communicated to cooler 22 and steam trap 23, then again with 3 phase of pressure swing adsorber
Connection.Cooler 22 is preferably fin cooler.
Further, converted gas and the reforming reactor output in order to make full use of carbon monoxide converter 2 to export
Reformed gas waste heat, the conversion gas efferent duct 21 in the present embodiment between carbon monoxide converter 2 and cooler 22 connects
To feed-water preheating boiler 5.Feed pipe 51 and outlet pipe 52 are provided on feed-water preheating boiler 5, outlet pipe 52 is connected to evaporator
6, the steam output end of evaporator 6 is connected with the vapor input pipe 13 of reforming reactor 1, reforms gas efferent duct 15 and is first connected to
It is connected again with carbon monoxide converter 2 to evaporator 6, reforms the reformed gas that gas efferent duct 15 exports and be introduced into evaporator
It is entered back into carbon monoxide converter 2 after carrying out heat exchange in 6.
It is connected in turn on material delivery pipe 14 in addition, in order to improve the transformation efficiency of reforming reaction, in the present embodiment de-
Sulphur device 7 and filter 8, the material conveyed by material delivery pipe 14 are successively defeated again after 7 desulfurization of devulcanizer, filter 8 filter
It send into the material economizer bank 17 in 1 heat-accumulating area 102 of reforming reactor.Flue gas output mechanism in heat-accumulating area 102 also with it is de-
Sulphur device 7 is connected, and the partial fume in 1 heat-accumulating area 102 of reforming reactor enters in devulcanizer 7 through flue gas output mechanism to be supplied
Heat.
As shown in Figure 1, the material in material delivery pipe 14 is provided by raw material buffer gear, raw material buffer gear include: according to
The raw material surge tank 9 and preheater 10 of secondary connection.The preheated device 10 of reaction raw materials in raw material surge tank 9 passes through material after preheating
Delivery pipe 14 is delivered in devulcanizer 7, and devulcanizer smoke discharge tube 71 is provided between devulcanizer 7 and preheater 10, from desulfurization
The flue gas being discharged in device 7 enters to heat supply in preheater 10 through devulcanizer smoke discharge tube 71, and emptying is provided on preheater 10
Pipe 100, the flue gas in preheater 10 are discharged from blow-down pipe 100.The flue gas being discharged in devulcanizer 7 is delivered in preheater 10
The material conveyed to material delivery pipe 14 preheats, to take full advantage of the waste heat of flue gas.
In the present embodiment, the hydrogen efferent duct 32 of pressure swing adsorber 3 is connected to hydrogen gas buffer 20, on hydrogen gas buffer 20
It is provided with circulating hydrogen delivery pipe 201 and outer for hydrogen delivery tube 202, circulating hydrogen delivery pipe 201 is connected with devulcanizer 7,
Hydrogen partial in hydrogen gas buffer 20 is entered to through circulating hydrogen delivery pipe 201 carries out desulphurization reaction in devulcanizer 7, hydrogen is slow
Remaining hydrogen rushed in tank 20 is supplied through outer for hydrogen delivery tube 202 outward.
In order to simplify structure, equipment occupation space is reduced, heat exchange boiler 4 can integrate with reforming reactor 1 and be integrated, such as
Shown in Fig. 2.Pass through partition between the drum of the heat exchange boiler 4 to become one and the reformer section and heat-accumulating area of reforming reactor 1
111 separate.The structure of the flue gas output mechanism of the heat-accumulating area 102 of reforming reactor 1 includes: in 17 input terminal position of material economizer bank
Several exhaust smoke holes 110 are offered on the partition 111 at the place of setting, exhaust smoke hole 110 is connected with the drum of heat exchange boiler 4, pre- in material
Heat-accumulating area smoke discharge tube 112, heat-accumulating area flue gas row are additionally provided on the shell for the heat-accumulating area 102 that heat pipe 17 inputs at end position
Outlet pipe 112 is connected to devulcanizer 7, and the part of smoke of heat-accumulating area 102 enters to heat supply in heat exchange boiler 4 by exhaust smoke hole 110,
Part of smoke enters to heat supply in devulcanizer 7 by heat-accumulating area smoke discharge tube 112.Heat exchange boiler 4 and reforming reactor 1 collect
The structure being integrally formed also has the advantage that the flue gas in heat-accumulating area 102 can be entered in heat exchange boiler 4 with shortest path,
This can effectively reduce the loss of flue gas heat.
The hydrogen production process of the vapor reforming hydrogen production device by high-temperature flue gas heat supply is described further below.
Hydrocarbon material being conveyed by material delivery pipe 14, may be used as hydrogen manufacturing can be generally divided into gaseous hydrocarbon and liquid
Hydrocarbon, gaseous hydrocarbon mainly have: natural gas, biogas plus hydrogen dry gas, coking dry gas and aromatization dry gas etc.；Liquid hydrocarbon mainly has:
The light naphthar of straight-run naphtha plus hydrogen, the raffinating oil of reformer production, tops, saturation liquefied petroleum gas etc..
By being sequentially entered outside to raw material surge tank 9 and preheater 10, hydrocarbon material obtains hydrocarbon material in preheater 10
Preliminary preheating, subsequently into sulphur is removed in devulcanizer 7, the hydrocarbon material for completing desulfurization is filtered to remove impurity through filter 8, then
It is further preheated in the material economizer bank 17 being delivered in the heat-accumulating area 102 of reforming reactor 1 by material delivery pipe 14, object
Hydrocarbon material in material economizer bank 17 enters in mixer 19 from the output end of material economizer bank 17.The preheated device of hydrocarbon material
Then 10 preliminary preheatings are further preheated in heat-accumulating area 102, thus to do into progress reforming reaction in reaction tube 16
Good adequate preparation, this can greatly speed up the reaction speed of reforming reaction, while effectively improve the conversion ratio of reforming reaction.
Demineralized water is entered in feed-water preheating boiler 5 by feed pipe 51 and is preheated, the demineralized water after preheating through outlet pipe 52 into
Enter to evaporator 6, the desalination water vapour generated in evaporator 6 enters in mixer 19 from vapor input pipe 13.
Hydrocarbon material is entered in each reaction tube 16 after mixing in mixer 19 with desalination vapor and is reformed
Reaction.Reaction generates reformed gas in reaction tube 16.Reformed gas is first delivered in evaporator 16 by reformation gas efferent duct 15 and is supplied
Then heat is entered in carbon monoxide converter 2 again from reformation gas efferent duct 15 and is reacted.It is anti-in carbon monoxide converter 2
The converted gas that should be generated successively is delivered to feed-water preheating boiler 5, cooler 22, steam trap by conversion gas efferent duct 21
23, converted gas discharges heat in feed-water preheating boiler 5, is cooled down in cooler 22, removes in steam trap 23
Moisture is removed, is purified subsequently into pressure swing adsorber 3, generates ultra-pure hydrogen and change after the purification of pressure swing adsorber 3
Press absorption tail gas.Ultra-pure hydrogen is delivered in hydrogen gas buffer 20 by hydrogen efferent duct 32, and pressure-variable adsorption tail gas is exported by tail gas
Pipe 31 exports.Ultra-pure hydrogen a part in hydrogen gas buffer 20 is entered in disconnector 7 by circulating hydrogen delivery pipe 201 to be used
Make desulfurization.Another part ultra-pure hydrogen in hydrogen gas buffer 20 is then conveyed by outer for hydrogen delivery tube 202 outward, such as to fuel
Battery conveying is for power generation etc..
In above-mentioned hydrogen production process, high-temperature flue gas is first input in conduction oil thermostat 120 by flue gas input pipe 12 and carries out temperature
Degree is adjusted, and the high-temperature flue gas after having adjusted temperature enters to the reformer section 101 of reforming reactor 1 to be 16 heat supply of reaction tube,
High-temperature flue gas moves to release largely in reformer section 101 from the feed end of reaction tube 16 to the direction of discharge of reaction tube 16
Heat, the flue gas for releasing amount of heat enters to heat-accumulating area 102, and the flue gas and material economizer bank 17 of heat-accumulating area 102 carry out
Heat exchange further discharges heat, and flue gas a part that heat-accumulating area 102 releases heat enters in heat exchange boiler 4, a part
Into in devulcanizer 7.Into in heat exchange boiler 4 flue gas and heat exchange boiler 4 in heat exchanging water pipe and conduction oil heat exchanger tube 121
Heat exchange is carried out, to sufficiently discharge heat, the flue gas that heat is sufficiently discharged in heat exchange boiler 4 is discharged from smoke discharging pipe 43.
Heat is provided to further discharge heat, in order to more into one into the flue gas in devulcanizer 7 for the desulphurization reaction in devulcanizer 7
Step ground utilizes the waste heat of flue gas, and the flue gas that heat is released in devulcanizer 7 enters to preheater from devulcanizer smoke discharge tube 71
Heat supply in 10 tentatively preheats hydrocarbon material into flue gas in preheater 10, is then discharged from blow-down pipe 100.
Utility model has the advantages that one, using high-temperature flue gas heat supply, fume afterheat can be made full use of, thus significantly
Reduce hydrogen manufacturing cost.Two, it is divided into reformer section 101 and heat-accumulating area 102, the object in heat-accumulating area 102 in the shell 11 of reforming reactor 1
17 pairs of economizer bank of material enter the hydrocarbon material reacted in reaction tube 16 and preheat, and not only take full advantage of the waste heat of flue gas, also
The rate and conversion ratio of reforming reaction in reaction tube 16 can be effectively improved.Three, heat exchange boiler 4 is set, it will be in heat-accumulating area 102
The flue gas after heat exchange, which has been carried out, with material economizer bank 17 is delivered to heat supply in heat exchange boiler 4, the steaming of the generation in heat exchange boiler 4
Vapour be used as carbon monoxide converter 2 heat medium, this greatly reduces the energy consumption of hydrogen production process, thus effectively save hydrogen manufacturing at
This.Four, the converted gas that reaction generates in carbon monoxide converter 2 is introduced into the heat supply into evaporator 6, to make evaporator 6
The desalination vapor for being used as reforming reaction is generated, this further reduces the heat energy loss in hydrogen production process, thus further
Reduce hydrogen manufacturing cost.
Claims (11)
1. by the vapor reforming hydrogen production device of high-temperature flue gas heat supply, comprising: reforming reactor, carbon monoxide converter, transformation
Absorber, it is characterised in that: the structure of reforming reactor includes: shell, and flue gas input pipe, vapor input are provided on shell
Pipe, material delivery pipe reform gas efferent duct, are divided into reformer section and heat-accumulating area in shell, several reaction tubes are provided in reformer section,
Flue gas input pipe is connected with the shell of reaction tube feed end, reforms gas efferent duct and is connected with the discharge end of reaction tube, accumulation of heat
Area is located at the side of reaction tube discharge end, if being provided with dry material economizer bank in heat-accumulating area, material delivery pipe and material economizer bank
Input terminal be connected, the output end and vapor input pipe of material economizer bank are connected with the feed end of reaction tube, store
Flue gas output mechanism is provided on the shell of hot-zone, high-temperature flue gas is entered to the reformation of reaction tube feed end by flue gas input pipe
Area, the high-temperature flue gas in reformer section move to the discharge end of reaction tube subsequently into heat-accumulating area, accumulation of heat by the feed end of reaction tube
The flue gas in area is discharged by flue gas output mechanism；It reforms gas efferent duct to be connected with carbon monoxide converter, reacts inner reaction tube
The reformed gas of generation is delivered in carbon monoxide converter by reformation gas efferent duct, and the bottom of carbon monoxide converter is provided with
Gas efferent duct is converted, conversion gas efferent duct is connected with pressure swing adsorber, the oxidation that reaction generates in carbon monoxide converter
Carbon converted gas is delivered in pressure swing adsorber by conversion gas efferent duct and is purified, and pressure swing adsorber is connected with tail gas efferent duct and hydrogen
Gas efferent duct, the ultra-pure hydrogen that pressure swing adsorber purification generates are exported by hydrogen efferent duct, and the transformation that pressure swing adsorber generates is inhaled
Attached tail gas is exported by tail gas efferent duct.
2. the vapor reforming hydrogen production device according to claim 1 by high-temperature flue gas heat supply, it is characterised in that: heat-accumulating area
Flue gas output mechanism be connected with heat exchange boiler, the flue gas of heat-accumulating area is entered in heat exchange boiler by flue gas output mechanism and is supplied
Heat is connected with water pipe and jet chimney with water pump on heat exchange boiler, is provided with smoke discharging pipe, heat exchange pot at the top of heat exchange boiler
Flue gas in furnace is discharged from smoke discharging pipe, and the heating of the heating jacket of the jet chimney and carbon monoxide converter of heat exchange boiler is situated between
Matter input terminal is connected, and the water pipe of heat exchange boiler is connected with the heat medium output end of the heating jacket of carbon monoxide converter
Logical, the steam generated in heat exchange boiler constantly passes through jet chimney and enters in the heating jacket of carbon monoxide converter, thus
For heat supply in carbon monoxide converter, the water formed in the heating jacket of carbon monoxide converter, which constantly passes through water pipe and enters to, to be changed
In heat boiler.
3. the vapor reforming hydrogen production device according to claim 2 by high-temperature flue gas heat supply, it is characterised in that: heat exchange pot
Furnace becomes one with reforming reactor.
4. the vapor reforming hydrogen production device according to claim 1 or 2 or 3 by high-temperature flue gas heat supply, it is characterised in that:
The conversion gas efferent duct of carbon monoxide converter bottom is first sequentially communicated to cooler and steam trap, is then inhaled again with transformation
Adnexa is connected.
5. the vapor reforming hydrogen production device according to claim 4 by high-temperature flue gas heat supply, it is characterised in that: an oxidation
Conversion gas efferent duct between carbon converter and cooler is connected to feed-water preheating boiler, is provided with water supply on feed-water preheating boiler
Pipe and outlet pipe, outlet pipe are connected to evaporator, the vapor input pipe phase of the steam output end and reforming reactor of evaporator
Connection, reformation gas efferent duct are first connected to evaporator and are connected again with carbon monoxide converter, reform the weight of gas efferent duct output
Whole gas enters back into carbon monoxide converter after being introduced into evaporator progress heat exchange.
6. the vapor reforming hydrogen production device according to claim 1 or 2 or 3 by high-temperature flue gas heat supply, it is characterised in that:
Be connected with devulcanizer and filter on material delivery pipe in turn, by material delivery pipe conveying material successively through devulcanizer desulfurization,
It is transported in the material economizer bank in reforming reactor heat-accumulating area again after filter filtering；The flue gas of reforming reactor heat-accumulating area
Output mechanism is also connected with devulcanizer, and the flue gas of reforming reactor heat-accumulating area enters in devulcanizer through flue gas output mechanism to be supplied
Heat.
7. the vapor reforming hydrogen production device according to claim 6 by high-temperature flue gas heat supply, it is characterised in that: material is defeated
The material in pipe is sent to be exported by raw material buffer gear, raw material buffer gear includes: the raw material surge tank and preheater being sequentially communicated,
Be delivered in devulcanizer after the preheated device preheating of material in raw material surge tank by material delivery pipe, devulcanizer and preheater it
Between be provided with devulcanizer smoke discharge tube, from devulcanizer be discharged flue gas entered in preheater through devulcanizer smoke discharge tube,
Blow-down pipe is provided on preheater, the flue gas in preheater is discharged from blow-down pipe.
8. the vapor reforming hydrogen production device according to claim 7 by high-temperature flue gas heat supply, it is characterised in that: transformation is inhaled
The hydrogen efferent duct of adnexa is connected to hydrogen gas buffer, and circulating hydrogen delivery pipe and outer defeated for hydrogen is provided on hydrogen gas buffer
Pipe is sent, circulating hydrogen delivery pipe is connected with devulcanizer, and the hydrogen partial in hydrogen gas buffer enters through circulating hydrogen delivery pipe
Desulphurization reaction is carried out in devulcanizer, remaining hydrogen in hydrogen gas buffer is supplied through outer for hydrogen delivery tube outward.
9. the vapor reforming hydrogen production device according to claim 1 or 2 or 3 by high-temperature flue gas heat supply, it is characterised in that:
It is provided with thermoregulator on flue gas input pipe, enters back into after the temperature regulated device adjustment temperature of high-temperature flue gas to reforming reactor
Shell in.
10. the vapor reforming hydrogen production device according to claim 9 by high-temperature flue gas heat supply, it is characterised in that: temperature
Adjuster is conduction oil thermostat, and conduction oil thermostat is connected with conduction oil heat exchanger tube, and the conduction oil heat exchanger tube setting exists
In heat exchange boiler, it is provided with Heat-transfer Oil Pump on conduction oil heat exchanger tube, under the action of Heat-transfer Oil Pump, conduction oil is constantly from conduction oil
It is entered in thermostat in conduction oil heat exchanger tube, then enters to conduction oil thermostat from the output end of conduction oil heat exchanger tube again
It is interior；High-temperature flue gas through flue gas input pipe enter in conduction oil thermostat carry out temperature adjusting after, enter back into reforming reactor
In shell.
11. the vapor reforming hydrogen production device according to claim 1 or 2 or 3 by high-temperature flue gas heat supply, feature exist
The reformer section of: reforming reactor shell reaction tubes charging end position is provided with mixer, material economizer bank output end and
Vapor input pipe is first connected to mixer, and mixer is connected to each reaction tube feed end again.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820726671.XU CN208345753U (en) | 2018-05-16 | 2018-05-16 | By the vapor reforming hydrogen production device of high-temperature flue gas heat supply |
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| CN201820726671.XU CN208345753U (en) | 2018-05-16 | 2018-05-16 | By the vapor reforming hydrogen production device of high-temperature flue gas heat supply |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108394863A (en) * | 2018-05-16 | 2018-08-14 | 张家港氢云新能源研究院有限公司 | By the vapor reforming hydrogen production device of high-temperature flue gas heat supply |
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2018
- 2018-05-16 CN CN201820726671.XU patent/CN208345753U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108394863A (en) * | 2018-05-16 | 2018-08-14 | 张家港氢云新能源研究院有限公司 | By the vapor reforming hydrogen production device of high-temperature flue gas heat supply |
| CN108394863B (en) * | 2018-05-16 | 2024-07-30 | 张家港氢云新能源研究院有限公司 | Steam reforming hydrogen production device with heat supplied by high-temperature flue gas |
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