CN208700566U - A kind of chemistry of fuel chain hydrogen generating system - Google Patents
A kind of chemistry of fuel chain hydrogen generating system Download PDFInfo
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- CN208700566U CN208700566U CN201820266134.1U CN201820266134U CN208700566U CN 208700566 U CN208700566 U CN 208700566U CN 201820266134 U CN201820266134 U CN 201820266134U CN 208700566 U CN208700566 U CN 208700566U
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Abstract
The utility model is about a kind of chemistry of fuel chain hydrogen generating system, including two identical burning chemistry chains reactors, burning chemistry chains reactor includes outer tube and the inner tube with outer coaxial tube setting, and inner tube is filled with the first oxygen carrier, and the interlayer between outer tube and inner tube is filled with the second oxygen carrier；The upper end of inner tube is connected with vapor import pipe and fuel inlet pipe road, and the lower end of inner tube is connected with gas eduction tube road.When the first burning chemistry chains reactor imports vapor and reduction-state oxygen carrier carries out the oxidation reaction of oxygen carrier, the second burning chemistry chains reactor imports fuel and oxidation state oxygen carrier carries out the reduction reaction of oxygen carrier.The chemistry of fuel chain hydrogen generating system simple process of the utility model, reactor is compact and is easy to minimize, and expeditiously can produce pure hydrogen from gaseous state or liquid fuel.
Description
Technical field
The utility model relates to fuel hydrogen producing technology fields, in particular to a kind of efficiently to produce from gaseous state or liquid fuel
It can be directly used for the chemistry of fuel chain hydrogen producing technology of the hydrogen of Proton Exchange Membrane Fuel Cells (PEMFC) pure hydrogen electric stack.
Background technique
Hydrogen Energy and fuel cell are an important development directions of field of new energy technologies, and how efficiently from natural
The various biogas making pure hydrogen such as various coal gas, the biogas such as the various fossil fuels such as gas, diesel oil, kerosene, gasoline, coke-stove gas
Gas is an important subject.In various fuel cells, PEMFC is due to fuel cell car (FCV) and distribution
The big purposes of cogeneration system two and be concerned.So far, it generallys use for the PEMFC of FCV using pure hydrogen as fuel
Pure hydrogen electric stack (H2- PEMFC), and the PEMFC for being used for distributed heat chp system is generallyd use to reform gas (by hydrocarbon
Steam reforming, self-heating recapitalization or the partial oxidative steam reforming of compound and obtain, contain 20% or more CO2) be fuel weight
Whole pneumoelectric heap (reforming gas-PEMFC).
H2Advantage-PEMFC high, at low cost and big power density with generating efficiency compared to reformation gas-PEMFC, because
And produce pure hydrogen from fuel-efficients such as natural gases, then with H2- PEMFC forms fuel-H2- PEMFC distributed heat electricity supply
System will have good energy conservation and economic benefit.
By taking natural gas as an example, the process flow that common natural gas produces pure hydrogen has steam reforming+CO water-gas shift
+ PSA method, steam reforming+CO water-gas shift+CO2Chemical absorption method and steam reforming+CO water-gas shift+CO2It is organic molten
Agent absorption process.Due to PSA, CO2Chemical absorbing and CO2Organic solvent absorption technique is complicated, energy consumption is high and is difficult to minimize, because
And it is not particularly suited for natural gas-H2- PEMFC distributed heat chp system.
In recent years, CO is trapped with zero energy consumption2Start the pass by researcher for the Coal Gasification chemistry chain hydrogen manufacturing of characteristic
Note.The process flow of the hydrogen production of chemical chain includes that FeO reacts generation Fe with vapor3O4With hydrogen, Fe3O4It is raw with air reaction
At Fe2O3And Fe2O3FeO and CO is generated with fuel reaction2+H2Tri- independent links of O.So, it is necessary to three
Reactor, which carries out touring switching, can just continuously acquire hydrogen, thus system is sufficiently complex.Furthermore two kinds of high temperature cigarettes are discharged in the system
Gas (Fe3O4With the flue gas and Fe of air reaction discharge2O3The flue gas generated with fuel reaction), thus the recycling of heat is tired
Difficulty causes hydrogen production efficiency to reduce.Therefore, existing hydrogen production of chemical chain technique is not suitable for natural gas-H2- PEMFC distributed heat
Chp system.
Utility model content
In order to solve the above-mentioned problems of the prior art, the utility model provides one kind and can produce from various fuel-efficients
The chemistry of fuel chain hydrogen generating system of pure hydrogen, is provided in particular in a kind of combustion combined based on steam reforming with burning chemistry chains
Expect hydrogen production of chemical chain system.In turn, this chemistry of fuel chain hydrogen generating system is applicable not only to extensive hydrogen manufacturing, is also easy to minimize,
To be very suitable for fuel-H2- PEMFC distributed heat chp system.
It the purpose of this utility model and solves its technical problem and adopts the following technical solutions to realize.
According to the utility model proposes a kind of chemistry of fuel chain hydrogen generating system, including two identical chemical chains combustions
Burn reactor, wherein the burning chemistry chains reactor includes outer tube and the inner tube with outer coaxial tube setting, said inner tube filling
There is the first oxygen carrier, the interlayer between outer tube and inner tube is filled with the second oxygen carrier；The upper end of said inner tube is connected with vapor
Import pipe and fuel inlet pipe road, the lower end of inner tube are connected with gas eduction tube road, and the gas eduction tube road passes through the 3rd three
Port valve exports pipeline with hydrogen and reduction reaction product gas connecting pipe is connect, the reduction reaction product gas connecting pipe
The other end connect with the lower end of the interlayer；The upper end of the interlayer is connected with the export pipeline of combustion product gases, under interlayer
End is connected with combustion air import pipe；The vapor import pipe of described two burning chemistry chains reactors passes through the 1st threeway
Valve is connected, and fuel inlet pipe road is connected by the 2nd triple valve, and combustion air import pipe is connected by the 5th triple valve
It connects.Shell-and-tube reactor can be used in the case where for fairly large hydrogen manufacturing, and the pipe of the shell-and-tube reactor tube bank is interior, manages
Journey fills the first oxygen carrier, and the pipe of tube bank is outer, i.e. shell side fills the second oxygen carrier.
It the purpose of this utility model and solves its technical problem also following technical measures can be used to further realize.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, wherein the fuel is gaseous state or liquid fuel,
First oxygen carrier is using iron oxide as the oxygen carrier of main active, and second oxygen carrier is iron-based oxygen carrier
Body, copper-based oxygen carrier, Ni-based oxygen carrier, calcium base load oxysome, manganese base load oxysome or two of them or two or more mixing
Object.Second oxygen carrier can also be substituted by catalyst for catalytic combustion.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, wherein vapor is added in the fuel, it is described
The first oxygen carrier filling layer above be filled with steam reforming catalyst, carry out the steam reforming reaction and CO water of fuel
Vapour conversion reaction.Ni system reforming catalyst or Ru system reforming catalyst can be used in the steam reforming catalyst.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, wherein the filling of the steam reforming catalyst
The top of layer is filled with desulfurizing agent, carries out the desulphurization reaction of fuel.Iron oxide or copper oxide desulfurization can be used in the desulfurizing agent
Agent.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, hydrogen export and are provided with methanator on pipeline,
Methanation catalyst is filled in the methanator.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, is additionally provided with the flue gas of flue gas and water on flue
Heat exchanger, vapor needed for the vapor of generation is used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, is additionally provided with the first of hydrogen and water on Hydrogen Line
Hydrogen heat exchanger, vapor needed for the vapor of generation is used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, on the Hydrogen Line of methanator outlet
It is additionally provided with the second hydrogen heat exchanger of hydrogen and water, water needed for the vapor of generation is used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain
Steam.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, further includes second-kind absorption-type heat pump subsystem, described
Second-kind absorption-type heat pump subsystem includes generator, condenser, the first evaporator, the first absorber and solution heat exchanger, institute
Stating generator includes solution spraying device and generation heat exchanger；Condenser includes condensing heat exchanger, and the entrance of condensing heat exchanger connects
The first water import pipe is connect, the outlet of condensing heat exchanger connects the first vapor and exports pipeline；First evaporator includes working medium spray
Shower device and evaporating heat exchanger；First absorber includes solution spraying device and the first absorption heat-exchange device, the first absorption heat-exchange device
Entrance connect the second water import pipe, the outlet of the first absorption heat-exchange device connects the second vapor and exports pipeline；The condensation
Vapor needed for the vapor that heat exchanger and the first absorption heat-exchange device generate is used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, the generation heat exchanger include the first generation heat exchanger
Heat exchanger occurs with second；The evaporating heat exchanger includes the first evaporating heat exchanger and the second evaporating heat exchanger；First hair
The entrance of raw heat exchanger is connect with flue gas export pipeline, and first occurs the outlet of heat exchanger connects with the entrance of the first evaporating heat exchanger
It connects, the entrance of the second generation heat exchanger is connect with hydrogen export pipeline, and second occurs the outlet of heat exchanger and the methane
Change the entrance connection of reactor, the outlet of methanator is connect with the entrance of the second evaporating heat exchanger.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, further include first-class absorption type heat pump subsystem or
Absorption refrigeration subsystem, the first-class absorption type heat pump subsystem or absorption refrigeration subsystem include generator, cold
Condenser, the second evaporator, the second absorber and solution heat exchanger, the generator include solution spraying device and exchange heat
Device；Condenser includes condensing heat exchanger, and the entrance of condensing heat exchanger connects the first water import pipe, and the outlet of condensing heat exchanger connects
Connect the first vapor export pipeline；Second evaporator includes working medium spray equipment and third evaporating heat exchanger；Second absorber packet
Include solution spraying device and the second absorption heat-exchange device；The vapor that condensing heat exchanger generates is used as chemistry of fuel chain hydrogen generating system system
Vapor needed for hydrogen.
Preferably, a kind of chemistry of fuel chain hydrogen generating system above-mentioned, the generation heat exchanger include the first generation heat exchanger
Heat exchanger occurs with second；The entrance of the first generation heat exchanger is connect with flue gas export pipeline, and described second exchanges heat
The entrance of device is connect with hydrogen export pipeline, and the outlet of the second generation heat exchanger is connect with the entrance of the methanator.
It the purpose of this utility model and solves its technical problem also the following technical solution is employed to realize.
According to the utility model proposes a kind of chemistry of fuel chain hydrogen production process, using chemistry of fuel chain hydrogen manufacturing system above-mentioned
System, hydrogen production process include, when the first burning chemistry chains reactor in two burning chemistry chains reactors passes through the vapor
Import pipe imports vapor and reduction-state oxygen carrier carries out the oxidation reaction of oxygen carrier and generates hydrogen, is led by the hydrogen
Out when pipeline export hydrogen, the second burning chemistry chains reactor passes through the mixture import pipe of fuel or fuel and vapor
The mixture and oxidation state oxygen carrier for importing fuel or fuel and vapor carry out the reduction reaction of oxygen carrier and generate reduction
Reduction reaction product gas is imported interlayer by reduction reaction product gas connecting pipe, by combustion-supporting by reaction product gas
Combustion air is imported the burning chemistry chains reaction that interlayer carries out reduction reaction product gas, the chemical chain by air leading-in conduit road
Combustion reaction provides heat for the reduction reaction of the oxidation state oxygen carrier；
At the end of the oxidation reaction of the reduction-state oxygen carrier in the first burning chemistry chains reactor, by switching the 1st to
5th triple valve makes the first burning chemistry chains reactor carry out the reduction reaction and reduction reaction product gas of oxidation state oxygen carrier
Burning chemistry chains reaction, the second burning chemistry chains reactor carry out reduction-state oxygen carrier oxidation reaction.
It the purpose of this utility model and solves its technical problem also following technical measures can be used to further realize.
Preferably, a kind of chemistry of fuel chain hydrogen production process above-mentioned, the reduction-state in the first burning chemistry chains reactor
At the end of the oxidation reaction of oxygen carrier, switches the 1st and the 2nd triple valve first, the first burning chemistry chains reactor is made to start to carry out
The reduction reaction of oxidation state oxygen carrier and the burning chemistry chains reaction of reduction reaction product gas, the second burning chemistry chains reactor
The oxidation reaction for starting progress reduction-state oxygen carrier, after time t, then switches the 3rd to the 5th triple valve.
Preferably, a kind of chemistry of fuel chain hydrogen production process above-mentioned, wherein the time t is 5~30 seconds.
Preferably, a kind of chemistry of fuel chain hydrogen production process above-mentioned, wherein the oxidation reaction of the reduction-state oxygen carrier
Temperature is 700~850 DEG C；The reduction reaction temperature of oxidation state oxygen carrier is 700~850 DEG C；The combustion of reduction reaction product gas
Burning reaction temperature is 850~1000 DEG C.
Preferably, a kind of chemistry of fuel chain hydrogen production process above-mentioned, wherein the steam reforming reaction temperature is 450
~750 DEG C, steam/hydrocarbons ratio is 0.5~2.0；Alternatively, the desulfurization reaction temperature is 100~450 DEG C；Methanation reaction temperature
It is 150~400 DEG C.
Preferably, a kind of chemistry of fuel chain hydrogen production process above-mentioned, by the high-temperature part of fume afterheat and hydrogen waste heat
High-temperature part is used as the driving heat source of the second-kind absorption-type heat pump subsystem generator, by the low temperature part of fume afterheat and
The low temperature part of hydrogen waste heat is used as the low-temperature heat source of second-kind absorption-type heat pump subsystem evaporator.
Preferably, a kind of chemistry of fuel chain hydrogen production process above-mentioned, by the high-temperature part of fume afterheat and hydrogen waste heat
High-temperature part be used as the driving heat source of the first-class absorption type heat pump subsystem or absorption refrigeration subsystem generator into
Row refrigeration or cold and heat combined supply, using low grade heat energies such as air-source, Di Yuan, water source, industrial exhaust heat, solar energy, underground heat as institute
The low-temperature heat source for stating the second evaporator carries out heat supply.
The second-kind absorption-type heat pump subsystem, first-class absorption type heat pump or refrigeration subsystem adopt water as work
Matter, using LiBr, LiCl, LiNO3、CaCl2Or KNO3One of or two or more mixtures as absorbent.
By above-mentioned technical proposal, a kind of chemistry of fuel chain hydrogen generating system of the utility model is at least had the advantage that
(1) as the system for producing pure hydrogen from fuel, the technique letter of the chemistry of fuel chain hydrogen generating system of the utility model
List, structure of reactor are simple, be compact, easy to miniaturization and hydrogen production efficiency is high.
(2) pass through Fe3O4Oxidation reaction, the polluter contained in fuel are carried out to fuel at a high temperature of 700 DEG C or more
It is innoxious, to achieve the effect that Air Pollutants emission reduction.Such as the NH contained in blast furnace gas3, organic amine and cyaniding
The nitrogenous compounds such as object are converted into nitrogen gas and water and carbon dioxide；H2S and organic sulfur compound sulfides are converted into vulcanization
Iron；The VOCs such as benzene, dimethylbenzene, naphthalene are converted into water and carbon dioxide.
(3) by adding vapor in fuel, fuel and Fe are effectively inhibited3O4Carbon distribution in reaction process.
(4) due to organically combining steam reforming and hydrogen production of chemical chain, in hydrocarbon fuel and Fe3O4React it
It is preceding by steam reforming reaction by hydrocarbon fuel pre-conversion be reducing power stronger CO and H2, to make Fe3O4It is reduced to
Temperature needed for FeO is substantially reduced, and reduction reaction temperature window is obviously widened, and is avoided the sintering of oxygen carrier, is extended oxygen carrier
The service life of body.In turn, CO and H2The FeO of a part can be reduced further into Fe, so that it is raw to increase the first oxygen carrier
At H2Ability.
(5) steam reforming reaction of fuel is strong endothermic reaction.It is urged by filling steam reforming on the top of inner tube
Agent makes the reaction gas of steam reforming reaction and combustion product gases form counterflow heat exchange, significantly reduces going out for combustion product gases
Mouth temperature, to further improve hydrogen production efficiency.
(6) when carrying out the switching of two burning chemistry chains reactors, first switch the 1st and the 2nd triple valve, at 5~30 seconds
Switch the 3rd to the 5th triple valve again afterwards.In this way, having increased hydrogen amount to obtain not only to improve hydrogen production efficiency, but also reduces and be mixed into hydrogen
The CO of gas2, the foreign gases such as CO.
(7) methanator is set on hydrogen export pipeline, a small amount of CO being mixed into hydrogen when by switching2Turn with CO
It turns to H2The harmless CH of pemfc stack4。
(8) hydrogen that the flue gas heat-exchange unit of flue gas and water is set on flue, hydrogen and water are set on Hydrogen Line
Gas heat exchanger, vapor needed for generating chemistry of fuel chain hydrogen generating system using the waste heat of flue gas and hydrogen, to further mention
High hydrogen production efficiency.
(9) by setting second-kind absorption-type heat pump subsystem, ladder is carried out to high-grade fume afterheat and hydrogen waste heat
Grade utilizes, to reduce systemLoss, improves the energy utilization efficiency of system.That is, by by flue gas and hydrogen waste heat
High-temperature part is used as the driving heat source of the heat pump subsystem generator, and the low temperature part of flue gas and hydrogen waste heat is used as should
The low-temperature heat source of heat pump subsystem evaporator, so that script cannot function as chemistry of fuel chain hydrogen generating system institute because grade is too low
The heat of vapor needed for the low temperature exhaust heat of the flue gas and hydrogen that need vapor heat source is partially converted into chemistry of fuel chain hydrogen generating system
Source further improves hydrogen production efficiency.
(10) by setting first-class absorption type heat pump or absorption refrigeration subsystem, to high-grade fume afterheat and
Hydrogen waste heat carries out cascade utilization, to reduce systemLoss, improves the energy utilization efficiency of system.That is, by by cigarette
The driving heat source that the high-temperature part of gas and hydrogen waste heat is used as the heat pump subsystem generator carries out refrigeration or cold and heat combined supply,
The low-temperature heat source that nearest obtainable low-grade heat can serve as the second evaporator is subjected to heat supply, it can be real while hydrogen making
Existing cold and heat combined supply.In turn, by combining pemfc stack to form distributed fuel cell power station, it can be achieved that efficient distribution
Formula cold, heat and power triple supply system.
Obviously, the chemistry of fuel chain hydrogen generating system of the utility model not only can with high efficiency, produce pure hydrogen on a large scale, also
It is very suitable for fuel-H2- PEMFC distributed fuel cell cogeneration or cold, heat and power triple supply system.
It is only the general introduction of technical solutions of the utility model, in order to understand the technical means of the present invention more clearly,
And can be implemented in accordance with the contents of the specification, it is described in detail on the preferred embodiment of the present invention and the accompanying drawings below such as
Afterwards.
Detailed description of the invention
Fig. 1 is the schematic diagram of the embodiment 1 of the chemistry of fuel chain hydrogen generating system of the utility model.
Fig. 2 is the schematic diagram of the embodiment 2 of the chemistry of fuel chain hydrogen generating system of the utility model.
Fig. 3 is the schematic diagram of the embodiment 3 of the chemistry of fuel chain hydrogen generating system of the utility model.
Fig. 4 is the schematic diagram of the embodiment 4 of the chemistry of fuel chain hydrogen generating system of the utility model.
Fig. 5 is the schematic diagram of the embodiment 5 of the chemistry of fuel chain hydrogen generating system of the utility model.
Fig. 6 is the schematic diagram of the embodiment 6 of the chemistry of fuel chain hydrogen generating system of the utility model.
Specific embodiment
Further to illustrate that the utility model is the technical means and efficacy reaching predetermined purpose of utility model and being taken,
Below in conjunction with attached drawing and preferred embodiment, to according to the utility model proposes a kind of chemistry of fuel chain hydrogen generating system, it is specific
Embodiment, structure, feature and its effect, detailed description is as follows.In the following description, different " embodiment " or " implementation
What example " referred to is not necessarily the same embodiment.In addition, the special characteristic, structure or feature in one or more embodiments can be by any
Suitable form combination.
Embodiment 1
A kind of chemistry of fuel chain hydrogen generating system is present embodiments provided, as shown in Figure 1.
Chemistry of fuel chain hydrogen generating system provided in this embodiment, including two identical burning chemistry chains reactors,
That is the first burning chemistry chains reactor 10 and the second burning chemistry chains reactor 20, wherein two burning chemistry chains reactors are equal
Inner tube 12 including outer tube 11 and with outer coaxial tube setting, inner tube are filled with the first oxygen carrier 13, the folder between outer tube and inner tube
Layer is filled with the second oxygen carrier 14；The upper end of inner tube is connected with vapor import pipe 41 and fuel inlet pipe road 42, inner tube
Lower end is connected with gas eduction tube road, and the gas eduction tube road is led by the 3rd triple valve 53 (or the 4th triple valve 54) with hydrogen
Pipeline 43 and reduction reaction product gas connecting pipe 44 connect out, the other end of reduction reaction product gas connecting pipe 44 with
The lower end of the interlayer connects；The upper end of interlayer is connected with combustion product gases export pipeline 46, and the lower end of interlayer is connected with combustion-supporting sky
Gas import pipe 45；The vapor import pipe 41 of two burning chemistry chains reactors is connected by the 1st triple valve 51, fuel
Import pipe 42 is connected by the 2nd triple valve 52, and combustion air import pipe 45 is connected by the 5th triple valve 55.
A kind of chemistry of fuel chain hydrogen generating system is present embodiments provided, pure hydrogen, technique can be produced from various fuel-efficients
Simply, structure of reactor is simple, be compact, easy to miniaturization and hydrogen production efficiency is high, is very suitable for fuel-H2- PEMFC distribution
Formula cogeneration system.
Further, the fuel is gaseous state or liquid fuel；First oxygen carrier is based on iron oxide
Want the oxygen carrier of active constituent；Second oxygen carrier is iron-based oxygen carrier, copper-based oxygen carrier, Ni-based oxygen carrier, calcium base load oxysome, manganese
Base load oxysome or two of them or two or more mixtures.
Embodiment 2
A kind of chemistry of fuel chain hydrogen generating system is present embodiments provided, as shown in Figure 2.
In chemistry of fuel chain hydrogen generating system provided in this embodiment, vapor, the filling of the first oxygen carrier are added in fuel
The top of layer is also filled with steam reforming catalyst 15, carries out steam reforming reaction and the CO water gas shift reation of fuel.
Preferably, Ni system reforming catalyst or Ru system reforming catalyst can be used in the steam reforming catalyst.
In chemistry of fuel chain hydrogen generating system provided in this embodiment, vapor is filled with above the first oxygen carrier filling layer
Reforming catalyst makes fuel and Fe3O4Before reaction, by steam reforming reaction, more for reducing power by fuel pre-conversion
Strong CO and H2, to make Fe3O4Temperature needed for being reduced to FeO is substantially reduced, and reduction reaction temperature window is obviously widened, and is kept away
The sintering for having exempted from oxygen carrier extends the service life of oxygen carrier.In turn, CO and H2The FeO of a part can further be restored
For Fe, so that increasing the 1st oxygen carrier generates H2Ability.Also, the steam reforming reaction of fuel is strong endothermic reaction.It is logical
It crosses the top in inner tube and fills steam reforming catalyst, form the reaction gas of steam reforming reaction with combustion product gases inverse
Stream heat exchange, significantly reduces the outlet temperature of combustion product gases, to further improve hydrogen production efficiency.
Further, in chemistry of fuel chain hydrogen generating system provided in this embodiment, the steam reforming catalyst
The top of filling layer is also filled with desulfurizing agent 16, carries out the desulphurization reaction of fuel.Preferably, iron oxide can be used in the desulfurizing agent
Or copper oxide desulfurizing agent.
Can add micro sulphur system odor additive such as thiophane etc. in usual natural gas, the present embodiment using iron oxide or
Copper oxide desulfurizing agent 100 DEG C or more at a temperature of by Chemisorption can deep sulfide removing, so that water be avoided to steam
The sulfur poisoning of gas reforming catalyst inactivates.
Embodiment 3
A kind of chemistry of fuel chain hydrogen generating system is present embodiments provided, as shown in Figure 3.
In chemistry of fuel chain hydrogen generating system provided in this embodiment, methanator is additionally provided on hydrogen export pipeline
30, methanation catalyst 31 is filled in the methanator.
In the present embodiment, methanator is set on hydrogen export pipeline, is mixed into when by switching a small amount of in hydrogen
CO2It is converted into CO to H2The harmless CH of pemfc stack4。
Embodiment 4
A kind of chemistry of fuel chain hydrogen generating system is present embodiments provided, as shown in Figure 4.
In chemistry of fuel chain hydrogen generating system provided in this embodiment, the flue gas of flue gas and water is additionally provided on flue 46
Heat exchanger 64, vapor needed for the vapor of generation is used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain.
Further, in chemistry of fuel chain hydrogen generating system provided in this embodiment, hydrogen is additionally provided on Hydrogen Line 43
With the first hydrogen heat exchanger 60 of water, vapor needed for the vapor of generation is used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain.Into
And the flow of the water of the first hydrogen heat exchanger 60 is imported by control, the temperature of Lai Youhua methanation reaction.
Further, in chemistry of fuel chain hydrogen generating system provided in this embodiment, the hydrogen pipe of methanator outlet
The second hydrogen heat exchanger 62 of hydrogen and water is additionally provided on road, the vapor of generation is used as chemistry of fuel chain hydrogen generating system hydrogen manufacturing institute
The vapor needed.
In chemistry of fuel chain hydrogen generating system provided in this embodiment, includes flue gas heat-exchange unit and hydrogen heat exchanger, utilize
Vapor needed for the waste heat of flue gas and hydrogen produces chemistry of fuel chain hydrogen generating system, to further improve hydrogen production efficiency.
Embodiment 5
A kind of chemistry of fuel chain hydrogen generating system is present embodiments provided, as shown in Figure 5.
It further include second-kind absorption-type heat pump subsystem in chemistry of fuel chain hydrogen generating system provided in this embodiment, it is described
Second-kind absorption-type heat pump subsystem includes generator 70, condenser 130, the first evaporator 80, the first absorber 90 and solution
Heat exchanger 100, the generator 70 include solution spraying device 71 and generation heat exchanger；Condenser 130 includes condensing heat exchanger
132, the entrance of condensing heat exchanger 132 connects the first water import pipe 133, and the outlet of condensing heat exchanger 132 connects the first water and steams
Gas delivery line road 134；Generator 70 is connected to condenser 130 by refrigerant vapor channel 134；First evaporator 80 includes working medium
Spray equipment 81 and evaporating heat exchanger；First absorber 90 include solution spraying device 91 and the first absorption heat-exchange device 92, first
The entrance of absorption heat-exchange device 92 connects the second water import pipe 93, and the outlet of the first absorption heat-exchange device 92 connects the second vapor and leads
Pipeline 94 out；First evaporator 80 is connected to the first absorber 90 by refrigerant vapor channel 84；Generator 70 is molten by first
Liquid circulating line 103 and the second solution circulating line 104 are connect with the first absorber 90, are set on the first solution circulating line 103
There are solution circulation pump 74 and solution heat exchanger 100, the second solution circulating line 104 is equipped with solution heat exchanger 100 and throttle valve
101；Condensation working medium is delivered to the first evaporator 80 by condenser 130 by condensation working medium pump 136 and condensation working medium pipeline 135.
Further, the generation heat exchanger includes that heat exchanger 73 occurs for the first generation heat exchanger 72 and second；The steaming
Sending out heat exchanger includes the first evaporating heat exchanger 82 and the second evaporating heat exchanger 83；Described first occurs the entrance and cigarette of heat exchanger 72
Gas delivery line road 46 connects, and the outlet of the first generation heat exchanger is connect with the entrance of the first evaporating heat exchanger 82, second hair
The entrance of raw heat exchanger 73 is connect with hydrogen export pipeline 43, and second occurs the outlet of heat exchanger 73 and the methanator
30 entrance connection, the outlet of methanator 30 is connect with the entrance of the second evaporating heat exchanger 83.In generator 70, come from
Dilute absorbent solution of first absorber 90 passes through the first generation heat exchanger 72 and second respectively and occurs more than the absorption flue gas of heat exchanger 73
Heat high-temperature part and hydrogen waste heat high-temperature part and generate refrigerant vapor, while dilute absorbent solution be concentrated into it is dense absorb it is molten
Liquid, the refrigerant vapor enter condenser 130 by refrigerant vapor channel 84, and the dense absorbent solution is recycled by the first solution
Pipeline 103, solution circulation pump 74 and solution heat exchanger 100 enter the first absorber 90；In condenser 130, led via the first water
The water for entering pipeline 133 is evaporated to pressure higher than 0.1MPa, temperature by the condensation heat that condensing heat exchanger 132 absorbs refrigerant vapor
Vapor higher than 100 DEG C, while refrigerant vapor is condensed into condensation working medium, the condensation working medium passes through condensation working medium pump 136
Enter the first evaporator 80 with condensation working medium pipeline 135；In the first evaporator 80, carry out the condensation working medium difference of condenser 130
It absorbs the low temperature part of fume afterheat and the low temperature part of hydrogen waste heat and generates refrigerant vapor, the refrigerant vapor passes through working medium
Steam channel 84 enters the first absorber 90；In the first absorber 90, dense absorbent solution from generator 70 is absorbed from the
The refrigerant vapor of one evaporator 80 and release the absorption heat that temperature grade improves, while dense absorbent solution is diluted as dilute suction
Solution is received, the absorption heat is absorbed by the first absorption heat-exchange device 92 via the water of the second water import pipe 93 and is evaporated to pressure
Power is higher than the vapor of 0.1MPa, temperature higher than 100 DEG C, and dilute absorbent solution passes through the second solution circulating line 104, solution
Heat exchanger 100 and throttle valve 101 enter generator 70.The present embodiment is by the high temperature of the high-temperature part of fume afterheat and hydrogen waste heat
Part is used as the driving heat source of the second-kind absorption-type heat pump subsystem generator 70, by the low temperature part of fume afterheat and hydrogen
The low temperature part of gas waste heat is used as the low-temperature heat source of second-kind absorption-type heat pump subsystem evaporator 80, by condensing heat exchanger 132
Vapor needed for being used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain with the vapor that the first absorption heat-exchange device 92 generates, thus into
One step improves the hydrogen production efficiency of system.
Embodiment 6
A kind of chemistry of fuel chain hydrogen generating system is present embodiments provided, as shown in Figure 6.
It further include first-class absorption type heat pump subsystem or suction in chemistry of fuel chain hydrogen generating system provided in this embodiment
Receipts formula refrigeration subsystem, the first-class absorption type heat pump subsystem or absorption refrigeration subsystem include generator 70, cold
Condenser 130, the second evaporator 110, the second absorber 120 and solution heat exchanger 100, the generator 70 are filled including solution spraying
It sets 71 and heat exchanger occurs；Condenser 130 includes condensing heat exchanger 132, and the entrance of condensing heat exchanger 132 connects the first water and imports
Pipeline 133, the outlet of condensing heat exchanger 132 connect the first vapor and export pipeline 134；Generator 70 and condenser 130 pass through
Refrigerant vapor channel 134 is connected to；Second evaporator 110 includes working medium spray equipment 111 and third evaporating heat exchanger 112；Second
Absorber 120 includes solution spraying device 121 and the second absorption heat-exchange device 122；Second evaporator 110 and the second absorber 120
It is connected to by refrigerant vapor channel 114；Generator 70 passes through third solution circulating line 105 and the 4th solution circulating line 106
It is connect with the second absorber 120, the 4th solution circulating line 106 is equipped with solution circulation pump 74 and solution heat exchanger 100, third
Solution circulating line 105 is equipped with solution heat exchanger 100 and throttle valve 101；It condenses working medium and passes through condensation working medium pipeline 107 and section
It flows valve 102 and second evaporator 110 is delivered to by condenser 130.
Further, the generation heat exchanger includes that heat exchanger 73 occurs for the first generation heat exchanger 72 and second；Described
The entrance of one generation heat exchanger 72 is connect with flue gas export pipeline 46, and first occurs the outlet of heat exchanger 72 and flue gas heat-exchange unit 64
Entrance connection, entrance and hydrogen the export pipeline 43 of the second generation heat exchanger 73 connect, the second generation heat exchanger 73
Outlet is connect with the entrance of the methanator 30, the outlet of methanator 30 and entering for the second heat exchanger of hydrogen 62
Mouth connection.The entrance and exit of the third evaporating heat exchanger 112 respectively with the inlet duct 117 and outlet of refrigerant fluid
Road 118 connects；Alternatively, the entrance and exit of the third evaporating heat exchanger 112 inlet duct with low-temperature heat source fluid respectively
117 and outlet conduit 118 connect, the entrance and exit of the second absorption heat-exchange device 122 inlet duct with heating agent fluid respectively
123 and outlet conduit 124 connect.In generator 70, dilute absorbent solution from the second absorber 120 passes through the first generation respectively
Heat exchanger 72 and the second generation heat exchanger 73 absorb the high-temperature part of fume afterheat and the high-temperature part of hydrogen waste heat and generate work
Matter steam, while dilute absorbent solution is concentrated into dense absorbent solution, the refrigerant vapor is entered cold by refrigerant vapor channel 84
Condenser 130, the dense absorbent solution enter the by third solution circulating line 105, solution heat exchanger 100 and throttle valve 101
Two absorbers 120；In condenser 130, working medium is absorbed by condensing heat exchanger 132 via the water of the first water import pipe 133 and is steamed
The condensation heat of gas and be evaporated to pressure and be higher than 100 DEG C of vapor higher than 0.1MPa, temperature, while refrigerant vapor be condensed into it is cold
Solidifying working medium, the condensation working medium enter the second evaporator 110 by condensation working medium pipeline 107 and throttle valve 102；In the second evaporation
Device 110 carrys out inlet duct of the condensation working medium of condenser 130 by the absorption of third evaporating heat exchanger 112 via refrigerant fluid
The heat of 117 refrigerant fluid and generate refrigerant vapor, and realize via the outlet conduit of refrigerant fluid 118 to external cooling supply,
The refrigerant vapor enters the second absorber 120 by refrigerant vapor channel 114, alternatively, carrying out the condensation working medium of condenser 130
The heat of the low-temperature heat source fluid of the inlet duct 117 via low-temperature heat source fluid is absorbed by third evaporating heat exchanger 112
Generate refrigerant vapor；In the second absorber 120, the dense absorbent solution from generator 70 is absorbed from the second evaporator 110
Refrigerant vapor and release the absorption heat that temperature grade improves, while dense absorbent solution is diluted as dilute absorbent solution, via
The heating agent fluid of the inlet duct 123 of heating agent fluid absorbs the absorption heat by the second absorption heat-exchange device 122, and via heat
The outlet conduit 124 of matchmaker's fluid realizes that, to external heating, dilute absorbent solution passes through the 4th solution circulating line 106, solution
Circulating pump 74 and solution heat exchanger 100 enter generator 70.The present embodiment is by the high-temperature part of fume afterheat and hydrogen waste heat
The driving heat source that high-temperature part is used as the absorption refrigeration subsystem generator 70 is freezed；Or by the height of fume afterheat
The high-temperature part of isothermal segment and hydrogen waste heat is used as the driving heat source of the first-class absorption type heat pump subsystem generator 70, will
The low-temperature heat source that low-grade heat can serve as first-class absorption type heat pump subsystem evaporator 110 carries out heat supply, while condensation being changed
The vapor that hot device 132, flue gas heat-exchange unit 64 and the second heat exchanger of hydrogen 62 generate is used as chemistry of fuel chain hydrogen generating system
Vapor needed for hydrogen manufacturing, to further improve the hydrogen production efficiency and complex energy utilization efficiency of system.
Embodiment 7
Present embodiments provide a kind of chemistry of fuel chain hydrogen production process.
When the first burning chemistry chains reactor in two burning chemistry chains reactors passes through the vapor import pipe
It imports vapor and reduction-state oxygen carrier carries out the oxidation reaction of oxygen carrier and generates hydrogen, pipeline is exported by the hydrogen and is led
Out when hydrogen, the second burning chemistry chains reactor imports fuel by the mixture import pipe of fuel or fuel and vapor
Or the mixture and oxidation state oxygen carrier of fuel and vapor carry out the reduction reaction of oxygen carrier and generate reduction reaction product
Reduction reaction product gas is imported interlayer by reduction reaction product gas connecting pipe, is imported by combustion air by gas
Combustion air is imported the burning chemistry chains reaction that interlayer carries out reduction reaction product gas by pipeline；
At the end of the oxidation reaction of the reduction-state oxygen carrier in the first burning chemistry chains reactor, by switching the 1st to
5th triple valve makes the first burning chemistry chains reactor carry out the reduction reaction and reduction reaction product gas of oxidation state oxygen carrier
Burning chemistry chains reaction, the second burning chemistry chains reactor carry out reduction-state oxygen carrier oxidation reaction.
Fuel is with CH4For, the first oxygen carrier is to use iron-based oxygen carrier Fe3O4/Al2O3, reduction-state oxygen carrier and water steam
The oxygen carrier oxidating of gas reacts and the reaction equation of the oxygen carrier reduction reaction of oxidation state oxygen carrier and fuel and 750 DEG C
Under standard free energy variation and reaction heat it is as follows:
The reduction reaction of oxidation state oxygen carrier:
4Fe3O4+CH4=12FeO+CO2+2H2O (1)
Δ G=-39.9kJ/mol；Δ H=367.9kJ/mol
Fe3O4/Al2O3Reduction reaction (1) be strong endothermic reaction.
The oxidation reaction of reduction-state oxygen carrier:
3FeO+H2O=Fe3O4+H2 (2)
Δ G=1.3kJ/mol；Δ H=-44.5kJ/mol
FeO/Al2O3Reduction reaction (2) be exothermic reaction.
Second oxygen carrier is to use Ni-based oxygen carrier NiO/Al2O3For, reduction reaction product gas (principal component CH4)
It is reacted with the burning chemistry chains of air including oxidation state oxygen carrier NiO/Al2O3Reduction reaction link and reduction-state oxygen carrier Ni/
Al2O3Oxidation regeneration react link, standard free energy variation and the following institute of reaction heat at reaction equation and 900 DEG C
Show:
The reduction reaction of oxidation state oxygen carrier:
4NiO+CH4=4Ni+CO2+2H2O (3)
Δ G=-265.9kJ/mol；Δ H=136.2kJ/mol
The oxidation reaction of reduction-state oxygen carrier:
4Ni+2O2=4NiO (4)
Δ G=-534.0kJ/mol；Δ H=-938.4kJ/mol
The burning chemistry chains overall reaction of reduction reaction product gas:
CH4+2O2=CO2+2H2O (5)
Δ G=-799.9kJ/mol；Δ H=-802.2kJ/mol
The burning chemistry chains reaction (5) of reduction reaction product gas is strong exothermal reaction.
Steam reforming reaction is to use Ni/Al2O3For reforming catalyst, steam/hydrocarbons ratio are 1.5, CH4Steam reforming
Reaction changes with the standard free energy at the reaction equation of CO water gas shift reation and 750 DEG C and reaction heat is as follows:
Steam reforming reaction:
CH4+H2O=3H2+CO (6)
Δ G=-32.6kJ/mol；Δ H=224.7kJ/mol
CH4Steam reforming reaction (6) be strong endothermic reaction.
CO water gas shift reation:
CO+H2O=H2+CO2 (7)
Δ G=-2.1kJ/mol；Δ H=-34.6kJ/mol
CO water gas shift reation (7) is exothermic reaction.
Methanation catalyst is to use Ni/Al2O3For methanation catalyst, a small amount of CO and CO2Methanation reaction
Standard free energy variation and reaction heat at reaction equation and 250 DEG C is as follows:
CO+3H2=CH4+H2O (8)
Δ G=-90.7kJ/mol；Δ H=-214.8kJ/mol
CO2+4H2=CH4+2H2O (9)
Δ G=-71.2kJ/mol；Δ H=-175.1kJ/mol
Further, at the end of the oxidation reaction of the reduction-state oxygen carrier in the first burning chemistry chains reactor, first
Switch the 1st and the 2nd triple valve, the first burning chemistry chains reactor is made to start to carry out the reduction reaction and reduction of oxidation state oxygen carrier
The burning chemistry chains of reaction product gas react, and the oxidation that the second burning chemistry chains reactor starts to carry out reduction-state oxygen carrier is anti-
It answers, after time t, then switches the 3rd to the 5th triple valve.The time t is more preferably 5~30 seconds.
When carrying out the switching of two burning chemistry chains reactors, first switch the 1st and the 2nd triple valve, after 5~30 seconds again
Switch the 3rd to the 5th triple valve.In this way, having increased hydrogen amount to obtain not only to improve hydrogen production efficiency, but also reduces and be mixed into hydrogen
CO2, the foreign gases such as CO.
Further, the oxidizing reaction temperature of reduction-state oxygen carrier is 700~850 DEG C；The reduction of oxidation state oxygen carrier is anti-
Answering temperature is 700~850 DEG C；The combustion reaction temperature of reduction reaction product gas is 850~1000 DEG C.Steam reforming is anti-
Answering temperature is 450~750 DEG C, and steam/hydrocarbons ratio is 0.5~2.0；The desulfurization reaction temperature is 100~450 DEG C；Methanation reaction
Temperature is 150~400 DEG C.
Further, although FeO/Al2O3Oxidation reaction (2) and CO water gas shift reation (7) be exothermic reaction, but its
Thermal discharge is significantly lower than Fe3O4/Al2O3Reduction reaction (1) and CH4Steam reforming reaction (6) caloric receptivity, insufficient portion
Burning chemistry chains heat of the needs by reduction reaction product gas is divided to undertake.Under conditions of producing a certain amount of hydrogen, this reality
With novel in addition to changing CH4Flow except, also by control steam reforming reaction temperature and steam/hydrocarbons ratio, Lai Youhua CH4
Conversion ratio, make that the heat of burning chemistry chains reactor matches and Temperature Distribution is met, so that improves fuel produces effect
Rate.
In the above-described embodiments, it all emphasizes particularly on different fields to the description of each embodiment, there is no the portion being described in detail in some embodiment
Point, reference can be made to the related descriptions of other embodiments.
It is understood that the correlated characteristic in above-mentioned apparatus can be referred to mutually.In addition, in above-described embodiment " the
One ", " second " etc. is and not represent the superiority and inferiority of each embodiment for distinguishing each embodiment.
Numberical range described in the utility model includes numerical value all within the scope of this, and including any within the scope of this
The value range of two values composition.
Technical characteristic in the utility model claims and/or specification can be combined, and a combination thereof mode is unlimited
The combination obtained in claim by adduction relationship.Group is carried out by the technical characteristic in claim and/or specification
Close obtained technical solution and the protection scope of the utility model.
The above descriptions are merely preferred embodiments of the present invention, not makees in any form to the utility model
Limitation, any simple modification, equivalent change and modification made by the above technical examples according to the technical essence of the present invention,
It is still within the scope of the technical solutions of the present invention.
Claims (10)
1. a kind of chemistry of fuel chain hydrogen generating system, which is characterized in that including two identical burning chemistry chains reactors,
In,
The burning chemistry chains reactor includes outer tube and the inner tube with outer coaxial tube setting, and said inner tube is filled with the first oxygen carrier
Body, the interlayer between outer tube and inner tube are filled with the second oxygen carrier；
The upper end of said inner tube is connected with vapor import pipe and fuel inlet pipe road, and the lower end of inner tube is connected with gas export
Pipeline, the gas eduction tube road exports pipeline by the 3rd triple valve and hydrogen and reduction reaction product gas connecting pipe connects
It connects, the other end of the reduction reaction product gas connecting pipe is connect with the lower end of the interlayer；
The upper end of the interlayer is connected with the export pipeline of combustion product gases, and the lower end of interlayer is connected with combustion air import pipe；
The vapor import pipe of described two burning chemistry chains reactors is connected by the 1st triple valve, fuel inlet pipe road
It is connected by the 2nd triple valve, combustion air import pipe is connected by the 5th triple valve.
2. chemistry of fuel chain hydrogen generating system according to claim 1, which is characterized in that steamed in the fuel added with water
Gas is filled with steam reforming catalyst above the first oxygen carrier filling layer, and the steam reforming for carrying out fuel is anti-
It should be with CO water gas shift reation；
Alternatively,
It is filled with desulfurizing agent above the filling layer of the steam reforming catalyst, carries out the desulphurization reaction of fuel.
3. the chemistry of fuel chain hydrogen generating system described in any one of according to claim 1~2, which is characterized in that hydrogen is led
Methanator is provided on pipeline out, is filled with methanation catalyst in the methanator.
4. chemistry of fuel chain hydrogen generating system according to claim 3, which is characterized in that be additionally provided with flue gas on flue
With the flue gas heat-exchange unit of water, vapor needed for the vapor of generation is used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain.
5. chemistry of fuel chain hydrogen generating system according to claim 4, which is characterized in that be additionally provided with hydrogen on Hydrogen Line
With the first hydrogen heat exchanger of water, vapor needed for the vapor of generation is used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain.
6. chemistry of fuel chain hydrogen generating system according to claim 3, which is characterized in that the methanator outlet
The second hydrogen heat exchanger of hydrogen and water is additionally provided on Hydrogen Line, the vapor of generation is used as chemistry of fuel chain hydrogen generating system system
Vapor needed for hydrogen.
7. chemistry of fuel chain hydrogen generating system according to claim 3, which is characterized in that further include the second kind absorption type heat
Pump subsystem, the second-kind absorption-type heat pump subsystem include generator, condenser, the first evaporator, the first absorber and
Solution heat exchanger, the generator include solution spraying device and generation heat exchanger；Condenser includes condensing heat exchanger, and condensation is changed
The entrance of hot device connects the first water import pipe, and the outlet of condensing heat exchanger connects the first vapor and exports pipeline；First evaporation
Device includes working medium spray equipment and evaporating heat exchanger；First absorber includes solution spraying device and the first absorption heat-exchange device, and
The entrance of one absorption heat-exchange device connects the second water import pipe, and the outlet of the first absorption heat-exchange device connects the second vapor delivery line
Road；Water needed for the vapor that condensing heat exchanger and the first absorption heat-exchange device generate is used as the hydrogen generating system hydrogen manufacturing of chemistry of fuel chain steams
Gas.
8. chemistry of fuel chain hydrogen generating system according to claim 7, which is characterized in that the generation heat exchanger includes first
Heat exchanger and second occurs, heat exchanger occurs；The evaporating heat exchanger includes the first evaporating heat exchanger and the second evaporating heat exchanger；
The entrance of the first generation heat exchanger is connect with flue gas export pipeline, and first occurs the outlet of heat exchanger and the first evaporation and heat-exchange
The entrance of device connects, and the entrance of the second generation heat exchanger is connect with hydrogen export pipeline, and second occurs the outlet of heat exchanger
It is connect with the entrance of the methanator, the outlet of methanator is connect with the entrance of the second evaporating heat exchanger.
9. chemistry of fuel chain hydrogen generating system according to claim 3, which is characterized in that further include first-class absorption type heat pump
Perhaps the absorption refrigeration subsystem first-class absorption type heat pump subsystem or absorption refrigeration subsystem include subsystem
Generator, condenser, the second evaporator, the second absorber and solution heat exchanger, the generator include solution spraying device and
Heat exchanger occurs；Condenser includes condensing heat exchanger, and the entrance of condensing heat exchanger connects the first water import pipe, condensing heat exchanger
Outlet connect the first vapor export pipeline；Second evaporator includes working medium spray equipment and third evaporating heat exchanger；Second
Absorber includes solution spraying device and the second absorption heat-exchange device；The vapor that condensing heat exchanger generates is used as chemistry of fuel chain system
Vapor needed for hydrogen system hydrogen manufacturing.
10. chemistry of fuel chain hydrogen generating system according to claim 9, which is characterized in that the generation heat exchanger includes the
One, which occurs heat exchanger and second, occurs heat exchanger；The entrance of the first generation heat exchanger is connect with flue gas export pipeline, described
The entrance of second generation heat exchanger is connect with hydrogen export pipeline, and second occurs the outlet of heat exchanger and the methanator
Entrance connection.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110131725A (en) * | 2019-05-21 | 2019-08-16 | 中石化炼化工程（集团）股份有限公司 | A kind of heating means, heating device and its flue gas processing method |
| WO2019161776A1 (en) * | 2018-02-24 | 2019-08-29 | 北京联力源科技有限公司 | Fuel chemical looping hydrogen production system and method |
| CN110319708A (en) * | 2019-07-11 | 2019-10-11 | 北京联力源科技有限公司 | Emission coal gas boiler system, its operation method and the converter gas system including it |
| CN112682691A (en) * | 2021-01-12 | 2021-04-20 | 江苏国富氢能技术装备股份有限公司 | Hydrogen filling system for liquid hydrogen storage and transportation type hydrogen filling station |
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2018
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| Publication number | Priority date | Publication date | Assignee | Title |
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| WO2019161776A1 (en) * | 2018-02-24 | 2019-08-29 | 北京联力源科技有限公司 | Fuel chemical looping hydrogen production system and method |
| CN110131725A (en) * | 2019-05-21 | 2019-08-16 | 中石化炼化工程（集团）股份有限公司 | A kind of heating means, heating device and its flue gas processing method |
| CN110131725B (en) * | 2019-05-21 | 2020-04-28 | 中石化炼化工程（集团）股份有限公司 | Heating method, heating device and flue gas treatment method thereof |
| CN110319708A (en) * | 2019-07-11 | 2019-10-11 | 北京联力源科技有限公司 | Emission coal gas boiler system, its operation method and the converter gas system including it |
| CN112682691A (en) * | 2021-01-12 | 2021-04-20 | 江苏国富氢能技术装备股份有限公司 | Hydrogen filling system for liquid hydrogen storage and transportation type hydrogen filling station |
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