CN110316703A - A kind of self-heating preparing hydrogen by reforming methanol reaction system - Google Patents
A kind of self-heating preparing hydrogen by reforming methanol reaction system Download PDFInfo
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- CN110316703A CN110316703A CN201910537996.2A CN201910537996A CN110316703A CN 110316703 A CN110316703 A CN 110316703A CN 201910537996 A CN201910537996 A CN 201910537996A CN 110316703 A CN110316703 A CN 110316703A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 251
- 239000001257 hydrogen Substances 0.000 title claims abstract description 44
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 44
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 36
- 238000002407 reforming Methods 0.000 title claims abstract description 28
- 238000010438 heat treatment Methods 0.000 title claims abstract description 26
- 239000007789 gas Substances 0.000 claims abstract description 121
- 238000002485 combustion reaction Methods 0.000 claims abstract description 40
- 239000003054 catalyst Substances 0.000 claims abstract description 29
- 239000007864 aqueous solution Substances 0.000 claims abstract description 19
- 238000001704 evaporation Methods 0.000 claims abstract description 11
- 230000008020 evaporation Effects 0.000 claims abstract description 11
- 230000008676 import Effects 0.000 claims description 19
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 7
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 claims description 6
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 claims description 3
- 229910052802 copper Inorganic materials 0.000 claims description 3
- 239000010949 copper Substances 0.000 claims description 3
- 229910052697 platinum Inorganic materials 0.000 claims description 3
- 239000010970 precious metal Substances 0.000 claims description 3
- 238000001651 catalytic steam reforming of methanol Methods 0.000 abstract description 8
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 238000005516 engineering process Methods 0.000 abstract description 5
- 238000006057 reforming reaction Methods 0.000 abstract description 5
- 230000002779 inactivation Effects 0.000 abstract 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 11
- 229910002092 carbon dioxide Inorganic materials 0.000 description 7
- 239000003502 gasoline Substances 0.000 description 7
- 238000007086 side reaction Methods 0.000 description 7
- 239000001569 carbon dioxide Substances 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 238000000034 method Methods 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 239000002283 diesel fuel Substances 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000003912 environmental pollution Methods 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000002360 explosive Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 150000002431 hydrogen Chemical class 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000010792 warming Methods 0.000 description 2
- YZCKVEUIGOORGS-IGMARMGPSA-N Protium Chemical compound [1H] YZCKVEUIGOORGS-IGMARMGPSA-N 0.000 description 1
- 241000720974 Protium Species 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000005474 detonation Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002032 methanolic fraction Substances 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 238000012857 repacking Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000002207 thermal evaporation Methods 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02B—INTERNAL-COMBUSTION PISTON ENGINES; COMBUSTION ENGINES IN GENERAL
- F02B43/00—Engines characterised by operating on gaseous fuels; Plants including such engines
- F02B43/10—Engines or plants characterised by use of other specific gases, e.g. acetylene, oxyhydrogen
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
- F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
- F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
- F02M21/0203—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels characterised by the type of gaseous fuel
- F02M21/0206—Non-hydrocarbon fuels, e.g. hydrogen, ammonia or carbon monoxide
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
- F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
- F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
- F02M21/0218—Details on the gaseous fuel supply system, e.g. tanks, valves, pipes, pumps, rails, injectors or mixers
- F02M21/023—Valves; Pressure or flow regulators in the fuel supply or return system
- F02M21/0236—Multi-way valves; Multiple valves forming a multi-way valve system
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
- C01B2203/0233—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step the reforming step being a steam reforming step
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/08—Methods of heating or cooling
- C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
- C01B2203/0833—Heating by indirect heat exchange with hot fluids, other than combustion gases, product gases or non-combustive exothermic reaction product gases
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1047—Group VIII metal catalysts
- C01B2203/1064—Platinum group metal catalysts
- C01B2203/107—Platinum catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/10—Catalysts for performing the hydrogen forming reactions
- C01B2203/1041—Composition of the catalyst
- C01B2203/1076—Copper or zinc-based catalysts
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1217—Alcohols
- C01B2203/1223—Methanol
-
- 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
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T10/00—Road transport of goods or passengers
- Y02T10/10—Internal combustion engine [ICE] based vehicles
- Y02T10/30—Use of alternative fuels, e.g. biofuels
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Combustion & Propulsion (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The present invention relates to hydrogen production system employing reforming technologies, and in particular to is self-heating preparing hydrogen by reforming methanol reaction system, including preheating chamber, reformer chamber and internal combustion engine, further includes evaporator and heat-exchanging chamber；Evaporator, preheating chamber, reformer chamber, heat-exchanging chamber are in turn connected to form the first route by pipeline；Heat-exchanging chamber, evaporator, internal combustion engine are in turn connected to form the second route by pipeline；First line is connected in heat-exchanging chamber with the second route；Internal combustion engine, heat-exchanging chamber, reformer chamber, preheating chamber are in turn connected to form tail gas route by pipeline.The present invention using methanol steam reforming generate hydrogen burn on internal combustion engine after high-temperature tail gas, heat is released by the indoor heat for reforming aspiration high-temperature tail gas of heat exchange and in evaporator to the methanol aqueous solution progress heating evaporation under room temperature, and enough heats are provided and are carried out for reforming reaction；High-temperature tail gas temperature is passed through reformer chamber after reducing again, avoids that high-temperature tail gas temperature is excessively high to cause catalyst inactivation.
Description
Technical field
The present invention relates to hydrogen production system employing reforming technologies, and in particular to is a kind of self-heating preparing hydrogen by reforming methanol reaction system.
Background technique
With the development of industry, environmental pollution caused by fossil fuel largely burns, caused by fossil energy exhaustive exploitation
The problems such as energy crisis, is increasingly serious, and new energy has been developed into urgent problem on human development road.Hydrogen Energy is
A kind of new energy that current research is hotter, combustion heat value is high, and combustion product is pollution-free, and it is one that acquisition modes, which are easy, and multiplicity
The ideal clean energy resource of kind.But hydrogen room temperature is in gaseous state, and inflammable and explosive, leads to storage, transport difficult, these problems
In the presence of being allowed to be widely applied so far.
To solve these problems, there are many live hydrogen producing technologies, wherein reforming technique is that recent research is relatively broad
One kind.Reforming technique is varied, and raw material is also not quite similar, and studying widest raw material at present is methanol, mainly due to it
With being easily made, it is readily transported, hypotoxicity, the advantages such as product environmental sound meet current mainstream demand.Currently, methanol
There are mainly three types of the methods of hydrogen manufacturing: hydrogen production from methanol-steam reforming, methanol partial oxidation reforming and methanol self-heating recapitalization.Wherein,
Methanol partial oxidation reforming is exothermic reaction, stablizes and is not required to extraneous heat supply after carrying out, but temperature should not control；Methanol self-heating recapitalization
It is a kind of technology in conjunction with methanol steam reforming and methanol partial oxidation reforming, the heat generated using methanol partial oxidation reforming
Amount supply methanol steam reforming, adjusts reactant ratio, can reach the balance under set temperature, is not necessarily to external heat supply, but need
Air and oxygen is wanted to participate in, and hydrogen output is less.
Summary of the invention
It should not be controlled the purpose of the present invention is to solve methanol fractions oxidation hydrogen manufacturing temperature and methanol self-heating recapitalization needs
The problem that air and oxygen participate in and hydrogen output is less is wanted, a kind of self-heating preparing hydrogen by reforming methanol reaction system is provided, belongs to
Hydrogen production from methanol-steam reforming method.
To realize the above technical purpose, the invention adopts the following technical scheme:
A kind of self-heating preparing hydrogen by reforming methanol reaction system, including preheating chamber, reformer chamber and internal combustion engine, further include evaporator
And heat-exchanging chamber；Evaporator, preheating chamber, reformer chamber, heat-exchanging chamber are in turn connected to form the first route by pipeline；Heat exchange
Room, evaporator, internal combustion engine are in turn connected to form the second route by pipeline；First line in heat-exchanging chamber with the second route phase
Connection；Internal combustion engine, heat-exchanging chamber, reformer chamber, preheating chamber are in turn connected to form tail gas route by pipeline；Combustion in IC engine generates
High-temperature tail gas carry out heat in heat-exchanging chamber with the reformation gas that reformer chamber generates and exchange, exhaust temperature enters after reducing to be reformed
Room；The reformation gas for increasing temperature enters in evaporator along the second route to be exchanged with the methanol aqueous solution progress heat in evaporator,
Enter preheating chamber along the first route after methanol aqueous solution heat exchange evaporation, reforms after gas exchanges heat in evaporator and enter along the second route
Combustion in IC engine, the high-temperature tail gas that combustion in IC engine generates enter heat-exchanging chamber along tail gas route.
Further, the preheating chamber is provided with exhaust emission tube, the tail gas of heat-exchanging chamber outflow along tail gas route successively
It is discharged after exchanging heat in reformer chamber, preheating chamber by exhaust emission tube.
Further, the first via spool road of the preheating chamber outlet is provided with the first temperature sensor；The reformer chamber
Inside is equipped at least three second temperature sensors, and second temperature sensor is equally spaced；The first via of the reformer chamber outlet
Spool road is provided with third temperature sensor.
Further, the exhaust pipe of the preheating chamber import is provided with the first three-way control valve, the first threeway tune
Exhaust pipe between section valve and the reformer chamber is provided with triple valve, the exhaust pipe setting the two or three of the reformer chamber import
The exhaust pipe of logical regulating valve, the preheating chamber outlet is provided with the 4th three-way control valve.
Further, it is equipped between first three-way control valve and the 4th three-way control valve in parallel with preheating chamber
First exhaust pipe；Second offgas duct in parallel with reformer chamber is equipped between second three-way control valve and the triple valve
Road, the second exhaust pipe are provided with third three-way control valve.
It further, further include the first intelligent controller and the second intelligent controller；First intelligent controller is according to first
Temperature sensor adjusts the first three-way control valve and third three-way control valve respectively, and control enters the methanol steam of reformer chamber
Temperature；Second intelligent controller adjusts the second three-way control valve according to second temperature sensor, controls reformer chamber catalyst temperature
Degree.
It further, further include flow pump and accumulator tank, the methanol aqueous solution in accumulator tank enters evaporator through flow pump
Interior, the pipeline between flow pump and evaporator is provided with temperature sensor.
It further, is methanol: water=1:1 methanol-water raw material in accumulator tank.
Further, the catalyst of reformer chamber is industrial copper-based catalysts or precious metals platinum catalyst.
Compared with the prior art, the invention has the benefit that
One, the tail gas that combustor generates, which initially enters in heat-exchanging chamber, exchanges heat, and temperature is passed through reformer chamber after reducing again
It is interior, it avoids high-temperature tail gas and is passed directly into reformer chamber and cause catalyst temperature excessively high and inactivate；With the high temperature weight after tail gas heat exchange
Whole gas exchanges heat with the methanol aqueous solution in evaporator, and gas heat is reformed in effective use, improves energy utilization efficiency；High temperature
Tail gas first passes through reformer chamber, then enters preheating chamber, avoids in traditional scheme tail gas first by methanol water evaporation then into reformation
Room bring reforms the too low problem of room temperature；
Two, the high-temperature tail gas after the present invention is burnt on internal combustion engine using the hydrogen that methanol steam reforming generates is handed over by heat
It changes the indoor heat for reforming aspiration high-temperature tail gas and releases heat in evaporator and the methanol aqueous solution under room temperature is carried out
Heating evaporation, and enough heats are provided and are carried out for reforming reaction；And the hydrogen that reforming reaction generates continues into internal combustion engine progress
Combustion reaction provides power, forms autothermal equilibrium；While reaction, reaction temperature is controlled with intelligence control system, keeps urging
Agent most highly active；Exhaust emissions is free from environmental pollution, largely solves the problems, such as to burn the emission reduction of gasoline, diesel oil, and effectively
Using the heat of high-temperature tail gas, capacity usage ratio is improved；
Three, the present invention uses efficient heat transfer technology, and the heat energy from waste gas that internal combustion engine is discharged is directed to reformer chamber
It is interior, and so that reformation room temperature is reached almost the same by intelligence control system, methanol is reformed to be made completely and reforms gas gas, and
It is mixed and burned acting in proportion with enough air, achievees the effect that complete replacing gasoline, diesel oil；The present invention can be originally with combustion
Oil is the various internal combustion engine repackings such as automobile, ship, engine of fuel or is designed to alcohol hydrogen power device, makes to start
The power of machine is improved.
Detailed description of the invention
Fig. 1 is a kind of self-heating preparing hydrogen by reforming methanol reaction system figure of the present invention.
In figure: 1 accumulator tank, 2 flow pumps, 4 evaporators, 6 preheating chambers, 7 first three-way control valves, 8 first intelligent controllers,
9 first temperature sensors, 11 triple valves, 12 reformer chambers, 13 second temperature sensors, 14 second intelligent controllers, 15 third temperature
Spend sensor, 16 second three-way control valves, 19 heat-exchanging chambers, 21 third three-way control valves, 23 the 4th three-way control valves, 29 cut-offs
Valve, 30 internal combustion engines, 32 control valves.
Specific embodiment
The present invention is described further combined with specific embodiments below, but protection scope of the present invention is not limited in
This.
As shown in Figure 1, a kind of self-heating preparing hydrogen by reforming methanol reaction system, including preheating chamber 6, reformer chamber 12 and internal combustion engine
30, it further include evaporator 4 and heat-exchanging chamber 19.Evaporator 4, preheating chamber 6, reformer chamber 12, heat-exchanging chamber 19 pass through pipeline successively
Connection forms the first route.Heat-exchanging chamber 19, evaporator 4, internal combustion engine 30 are in turn connected to form the second route by pipeline.First
Route is connected in heat-exchanging chamber 19 with the second route.Internal combustion engine 30, heat-exchanging chamber 19, reformer chamber 12, preheating chamber 6 pass through pipe
Road is in turn connected to form tail gas route.The reformation gas that the high-temperature tail gas and reformer chamber 12 that the burning of internal combustion engine 30 generates generate is handed in heat
It changes and carries out heat exchange in room 19, exhaust temperature enters reformer chamber 12 after reducing.Increase temperature reformation gas along the second route into
Enter in evaporator 4 and exchanged with the methanol aqueous solution progress heat in evaporator 4, along the first route after methanol aqueous solution heat exchange evaporation
Into preheating chamber 6, reforms and enter the burning of internal combustion engine 30, the burning life of internal combustion engine 30 along the second route after gas exchanges heat in evaporator 4
At high-temperature tail gas enter heat-exchanging chamber 19 along tail gas route.The hydrogen that the present embodiment is generated using methanol steam reforming is in internal combustion
High-temperature tail gas after burning on machine 30, by the heat of the reformation aspiration high-temperature tail gas in heat-exchanging chamber 19 and in evaporator 4
It releases heat and heating evaporation is carried out to the methanol aqueous solution under room temperature, and provide enough heats for the progress of reforming reaction, and weigh
The hydrogen that whole reaction generates continues into internal combustion engine 30 and carries out combustion reaction offer power, forms autothermal equilibrium.
Evaporator 4 is provided with methanol aqueous solution import, methanol steam outlet, reforms gas import, reforms gas outlet.Evaporation
4 methanol aqueous solution import of device is communicated by flow pump 2 with methanol-water accumulator tank 1, the outlet of 4 methanol steam of evaporator and preheating chamber
Methanol steam import communicates in 6.Temperature sensor is provided on the pipeline of 4 methanol steam of evaporator outlet.4 weight of evaporator
Whole gas import is connected with gas outlet is reformed in heat exchanger 19, evaporator 4 reform gas outlet and the reformation gas of internal combustion engine 30 into
Mouth is connected.Evaporator 4 reforms gas export pipeline and is equipped with temperature sensor and control valve 32.Hot fluid in evaporator 4 is
The reformation gas of high temperature is reformed gas and is made of hydrogen and carbon dioxide, contains a small amount of carbon monoxide.Cold fluid in evaporator 4 is
Methanol aqueous solution at room temperature.Methanol aqueous solution flows into evaporator 4 through flow pump 2 from accumulator tank 1, changes with the reformation gas of high temperature
Thermal evaporation leaves evaporator 4 into preheating chamber 6 after forming mixed vapour.
Preheating chamber 6 is provided with methanol steam import, methanol steam outlet, inlet exhaust gas and offgas outlet.Preheating chamber 6
Methanol steam import is connected with evaporator 4, and the outlet of 6 methanol steam of preheating chamber is connected with reformer chamber 12,6 tail of preheating chamber
Gas import is connected to the offgas outlet of reformer chamber 12, and exhaust emission tube is arranged in 6 offgas outlet of preheating chamber, what heat-exchanging chamber 19 flowed out
Tail gas is successively discharged after heat exchange by exhaust emission tube in reformer chamber 12, preheating chamber 6 along tail gas route.Hot-fluid in preheating chamber 6
Body is high-temperature tail gas, and cold fluid is the low-temperature steam by being formed after methanol water evaporation, low-temperature steam in preheating chamber 6 with high temperature tail
Gas heat exchange heating, reaches 270 DEG C of catalysts optimum activity temperature, at a temperature of this, methanol steam reforming reaction efficiency compared with
Height, and the carbon monoxide generated is less.Preheating chamber 6 is adjusted into being respectively provided with the first threeway on tail gas mouth and tail gas mouth pipeline out
Valve 7 and the 4th three-way control valve 23, convenient for controlling the amount for entering tail gas in preheating chamber 6.The methanol steam inlet tube of preheating chamber 6
Road is equipped with temperature sensor, and methanol steam export pipeline is equipped with the first temperature sensor 9 and flow sensor.
Reformer chamber 12 is provided with methanol steam import, reforms gas outlet, inlet exhaust gas and offgas outlet.12 first of reformer chamber
The import of alcohol vapor is connected with the outlet of the methanol steam of preheating chamber 6.Reformer chamber 12 is reformed in gas outlet and heat-exchanging chamber 19
Gas import is reformed to be connected.12 inlet exhaust gas of reformer chamber is connected with offgas outlet in heat-exchanging chamber 19.12 tail gas of reformer chamber goes out
Mouth is connected with inlet exhaust gas in preheating chamber 6.Be equally spaced at least three second temperature sensors 13 inside reformer chamber 12, accurately
Monitor 12 internal accelerator temperature of reformer chamber.The first temperature sensor 9, flow are provided in 12 methanol-water inlet ductwork of reformer chamber
Sensor is reformed and is provided with third temperature sensor 15 and flow sensor on gas export pipeline, is equipped on inlet exhaust gas pipeline
Second three-way control valve 16, convenient for adjusting the amount that tail gas enters reformer chamber 12.Between first three-way control valve 7 and reformer chamber 12
Exhaust pipe is provided with triple valve 11.
Heat-exchanging chamber 19, which is provided with, to be reformed gas import, reforms gas outlet, inlet exhaust gas and offgas outlet.Wherein, heat exchange
Room 19 reforms gas import and is connected with gas outlet is reformed in reformer chamber 12, and heat-exchanging chamber 19 reforms gas outlet and weight in evaporator 4
Whole gas import is connected.19 inlet exhaust gas of heat-exchanging chamber is connected with offgas outlet in internal combustion engine 30, and 19 tail gas of heat-exchanging chamber goes out
Mouth is connected with gas inlet in reformer chamber 12.Temperature sensor is provided on 19 offgas outlet pipeline of heat-exchanging chamber, flow passes
Sensor is provided with temperature sensor, flow sensor, shut-off valve 29 on gas inlet pipeline.Heat-exchanging chamber 19 reforms gas import
Third temperature sensor 15 and flow sensor are provided on pipeline.Heat-exchanging chamber 19 is reformed and is provided with temperature on gas export pipeline
Sensor.
First exhaust pipe in parallel with preheating chamber 6 is equipped between first three-way control valve 7 and the 4th three-way control valve 23.
Second exhaust pipe in parallel with reformer chamber 12 is equipped between second three-way control valve 16 and triple valve 11, the second exhaust pipe is set
It is equipped with third three-way control valve 21.To guarantee that catalyst temperature is in normal working temperature in reformer chamber 12, the present embodiment is also wrapped
The first intelligent controller 8 and the second intelligent controller 14 are included, the first intelligent controller 8 is adjusted respectively according to the first temperature sensor 9
The first three-way control valve 7 and third three-way control valve 21 are saved, control enters the temperature of the methanol steam of reformer chamber 12.Second intelligence
It can control device 14 and second three-way control valve 16 adjusted according to second temperature sensor 13, to reach catalysis in control reformer chamber 12
Agent temperature.
When first temperature sensor 9 shows that methanol steam temperature is too low, the first intelligent controller 8 adjusts third threeway tune
Valve 21 is saved, tail gas is made to flow to triple valve 11 through third three-way control valve 21, that is, increases the amount that tail gas enters preheater 6, Jin Ersheng
The temperature of high methanol vapor；Temperature sensor 9 shows methanol steam when the temperature is excessively high, and intelligent controller 8 adjusts the one or three
Logical regulating valve 7, makes high-temperature tail gas when by the first three-way control valve 7, walks the first exhaust pipe around preheater 6, that is, reduces
Tail gas enters the amount of preheater 6, and then reduces the temperature of methanol steam.Second temperature sensor 13 or third temperature sensor
15 when the temperature is excessively high, and intelligence sensor 14 adjusts the second three-way control valve 16, and high-temperature tail gas is made to walk the second exhaust pipe, reduces tail
Gas enters the amount of reformer chamber 12, and then reduces catalyst temperature；15 temperature of second temperature sensor 13 or third temperature sensor
When too low, intelligence sensor 14 adjusts the second three-way control valve 16, increases the amount that tail gas enters reformer chamber 12, and then improve catalysis
Agent temperature makes catalyst keep most highly active.
The present embodiment further includes flow pump 2 and accumulator tank 1, and the storage of accumulator tank 1 is equipped with methanol: water=1:1 methanol-water is former
Material is connected to flow pump 2, to react transferring raw material.Methanol-water raw material flows into evaporator 4 via flow pump 2, the reformation with high temperature
Gas carries out heat exchange evaporation, forms methanol steam.Pipeline between flow pump 2 and evaporator 4 is provided with temperature sensor.Methanol
Vapor exchanges heat in preheating chamber 6 with high-temperature tail gas, and methanol steam is warming up to the reaction required temperature 473K-573K of setting,
High-temperature tail gas is cooled to 150 DEG C or less discharges.In reformer chamber 12, weight occurs under the effect of the catalyst for the methanol steam of high temperature
Whole reaction, generating content is about 75%H2And 25%CO2And the CO side reaction product that content is about 1%, it is referred to as reforming gas,
In, reaction institute's calorific requirement is provided by high-temperature tail gas.In high temperature heat-exchanging chamber 19, reforms gas and exchange heat with high-temperature tail gas, to tail
Gas cools down, and prevents high-temperature tail gas from keeping catalyst temperature in reformer chamber 12 excessively high, and makes to reform gas lift temperature, is convenient for evaporator 4
Needed for middle methanol aqueous solution evaporation.Reformation gas and air after cooling down in evaporator 4, which enter in internal combustion engine 30, burn instead
It answers, amount of heat is discharged in reaction process and does work, generate high-temperature tail gas.
The reaction that methanol-water is reformed is:
Main reaction: CH3OH+H2O→CO2+3H2
It is reacted with 1 methanol decomposition of side reaction: CH3OH→CO+H2
With 2 Water-gas shift reaction of side reaction:
Main reaction need to have a higher reaction speed between 250 DEG C to 280 DEG C of catalyst, and the reaction activity of side reaction 1
Higher than main reaction, catalyst temperature is higher, and the extent of reaction of side reaction 1 is higher, and the methanol of phase homogenous quantities is converted into the amount of hydrogen
Also fewer, and side reaction 2 is reversible reaction, and reacts few and carry out, and can only convert a small amount of CO.In order to guarantee main reaction into
Row, takes following measures:
One, the present embodiment setting evaporator 4 and 6 two heating devices of preheating chamber, guarantee that methanol steam enters reformer chamber
Minimum temperature needed for temperature is higher than catalyst in 12；
Two, heat-exchanging chamber 19 is arranged in the present embodiment, makes high-temperature tail gas first and reforms gas heat exchange cooling, then enters reformer chamber
12, it ensure that catalyst will not be damaged because temperature is excessively high；
Three, the present embodiment use intelligence control system, according to catalyst temperature in reformer chamber 12 and reform gas outlet temperature,
Control of flow and pressure tail gas enters the amount of reformer chamber 12, it is ensured that catalyst temperature is in reasonable interval.
The calorific value (21MJ/kg) of methanol is the 48% of gasoline heat value (44MJ/kg), and the calorific value (132MJ/kg) of hydrogen is vapour
3 times of oily calorific value (44MJ/kg), the burning velocity of hydrogen are gasoline more than 7 times, and the explosive force of hydrogen is gasoline more than 7 times, and pure hydrogen
Burning is also easy to produce detonation in internal combustion engine 30, and hydrogen content keeps burning anti-73% or so in the reformation gas that methanol recapitalization generates
The progress answered more is stablized easy to control.
Reformation gas after methanol recapitalization contains: hydrogen 70-75%, carbon monoxide 0.3-2%, carbon dioxide 20-25%.Weight
Become water and carbon dioxide after whole gas burning:
Main reaction: 2H2+O2→2H2O
Side reaction: 2CO+O2→2CO2
Exhaust emissions is free from environmental pollution, meets environmentally protective theory.Using methanol as raw material, protium content in methanol
Higher than fuel such as conventional gasoline, diesel oil, reduce the discharge amount of carbon dioxide, solves the problems, such as to burn the emission reduction of gasoline, diesel oil.
Catalyst in reformer chamber 12 is industrial copper-based catalysts or precious metals platinum catalyst.Methanol steam is in reformer chamber 12
Interior catalyst carrier flows in the micropore of porous ceramic ball and gap, and the micropore of catalyst carrier increases to the maximum extent
The path of the contact area of methanol steam and catalyst and the flowing for increasing methanol steam, allows the catalytic reforming of methanol more
It is fast more effectively to carry out.
When the present embodiment is run, methanol aqueous solution enters evaporator 4 through flow pump 2 by storage tank 1, flashes to gas by heat exchange
State flows into preheater 6, and methanol steam, which is first warming up to high-temperature tail gas heat exchange, reacts required temperature, then flows into reformer chamber
In 12, under the effect of the catalyst, carry out reforming reaction and generate to reform gas being about 75% hydrogen and 25% carbon dioxide and a small amount of
Carbon monoxide.It reforms after gas enters high temperature heat-exchanging chamber 19 and tail gas heat exchange heating and flows into evaporator 4, heat is provided and is opened for one
The room temperature methanol aqueous solution for beginning to enter in evaporator 4 from storage tank 1, which heats up, to gasify, and the hydrogen-rich gas after cooling down continues to flow into internal combustion
Work by combustion is carried out in machine 30, the tail gas formed after burning is successively through 6 heel row of over-heat-exchanger 30, reformer chamber 12 and preheating chamber
Out.
The embodiment of invention is described in detail above, for those of ordinary skill in the art, according to this hair
The thought of bright offer, will change in specific embodiment, and these changes should also be regarded as the scope of the invention.
Claims (9)
1. a kind of self-heating preparing hydrogen by reforming methanol reaction system, including preheating chamber (6), reformer chamber (12) and internal combustion engine (30),
It is characterized in that:
It further include evaporator (4) and heat-exchanging chamber (19)；Evaporator (4), preheating chamber (6), reformer chamber (12), heat-exchanging chamber (19)
The first route is in turn connected to form by pipeline；Heat-exchanging chamber (19), evaporator (4), internal combustion engine (30) are successively connected by pipeline
It connects to form the second route；First line is connected in heat-exchanging chamber (19) with the second route；Internal combustion engine (30), heat-exchanging chamber
(19), reformer chamber (12), preheating chamber (6) are in turn connected to form tail gas route by pipeline；
The reformation gas that the high-temperature tail gas and reformer chamber (12) that internal combustion engine (30) burning generates generate carries out in heat-exchanging chamber (19)
Heat exchange, exhaust temperature enter reformer chamber (12) after reducing；The reformation gas for increasing temperature enters evaporator (4) along the second route
The interior methanol aqueous solution in evaporator (4) carries out heat and exchanges, and enters after methanol aqueous solution heat exchange evaporation along the first route pre-
Hot cell (6) reforms gas and enters internal combustion engine (30) burning, internal combustion engine (30) burning along the second route after heat exchange in evaporator (4)
The high-temperature tail gas of generation enters heat-exchanging chamber (19) along tail gas route.
2. self-heating preparing hydrogen by reforming methanol reaction system according to claim 1, it is characterised in that: the preheating chamber (6)
It is provided with exhaust emission tube, the tail gas of heat-exchanging chamber (19) outflow is successively interior in reformer chamber (12), preheating chamber (6) along tail gas route
It is discharged after heat exchange by exhaust emission tube.
3. self-heating preparing hydrogen by reforming methanol reaction system according to claim 1, it is characterised in that: the preheating chamber (6)
The first via spool road of outlet is provided with the first temperature sensor (9)；At least three second are equipped with inside the reformer chamber (12)
Temperature sensor (13), second temperature sensor (13) are equally spaced；The first via spool road of reformer chamber (12) outlet is set
It is equipped with third temperature sensor (15).
4. self-heating preparing hydrogen by reforming methanol reaction system according to claim 3, it is characterised in that: the preheating chamber (6)
The exhaust pipe of import is provided with the first three-way control valve (7), first three-way control valve (7) and the reformer chamber (12) it
Between exhaust pipe be provided with triple valve (11), the second three-way control valve is arranged in the exhaust pipe of reformer chamber (12) import
(16), the exhaust pipe of preheating chamber (6) outlet is provided with the 4th three-way control valve (23).
5. self-heating preparing hydrogen by reforming methanol reaction system according to claim 4, it is characterised in that: the first threeway tune
It saves and is equipped with first exhaust pipe in parallel with preheating chamber (6) between valve (7) and the 4th three-way control valve (23)；Described second
Second exhaust pipe in parallel with reformer chamber (12), the second tail gas are equipped between three-way control valve (16) and the triple valve (11)
Pipeline is provided with third three-way control valve (21).
6. self-heating preparing hydrogen by reforming methanol reaction system according to claim 5, it is characterised in that:
It further include the first intelligent controller (8) and the second intelligent controller (14)；First intelligent controller (8) is according to the first temperature
Sensor (9) adjusts the first three-way control valve (7) and third three-way control valve (21) respectively, and control enters the first of reformer chamber (12)
The temperature of alcohol vapor；Second intelligent controller (14) adjusts the second three-way control valve according to second temperature sensor (13)
(16), reformer chamber (12) interior catalyst temperature is controlled.
7. self-heating preparing hydrogen by reforming methanol reaction system according to claim 1, it is characterised in that:
It further include flow pump (2) and accumulator tank (1), the methanol aqueous solution in accumulator tank (1) enters evaporator through flow pump (2)
(4) in, the pipeline between flow pump (2) and evaporator (4) is provided with temperature sensor.
8. self-heating preparing hydrogen by reforming methanol reaction system according to claim 1, it is characterised in that: be first in accumulator tank
Alcohol: water=1:1 methanol-water raw material.
9. self-heating preparing hydrogen by reforming methanol reaction system according to claim 1, it is characterised in that: in reformer chamber (12)
Catalyst is industrial copper-based catalysts or precious metals platinum catalyst.
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111883805A (en) * | 2020-08-23 | 2020-11-03 | 浙江工业大学 | Small methanol reforming hydrogen production device system based on tail gas waste heat utilization |
| CN112081690A (en) * | 2020-09-16 | 2020-12-15 | 杰锋汽车动力系统股份有限公司 | Methanol engine waste heat recovery hydrogen production device and hydrogen production method thereof |
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Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52129705A (en) * | 1976-04-24 | 1977-10-31 | Nissan Motor Co Ltd | Methanol-reforming apparatus |
| JPS61286203A (en) * | 1985-06-14 | 1986-12-16 | Mitsubishi Heavy Ind Ltd | Reforming method for methanol |
| JP2001089104A (en) * | 1999-09-22 | 2001-04-03 | Suzuki Motor Corp | Methanol reformer |
| CN101462694A (en) * | 2007-12-19 | 2009-06-24 | 中国科学院大连化学物理研究所 | Miniaturized methanol self-heating reforming hydrogen making integrated apparatus and hydrogen production method |
| CN201376896Y (en) * | 2009-04-22 | 2010-01-06 | 于景瑞 | Methanol steam reforming conversion hydrogen production device for automobile |
| CN102602885A (en) * | 2012-03-12 | 2012-07-25 | 云南大学 | Method for manufacturing hydrogen in reforming way by catalyst loaded at heat conducting material through utilizing heat of tail gas of heat engine |
| CN105649827A (en) * | 2016-01-19 | 2016-06-08 | 上海万寅安全环保科技有限公司 | Hydrogen-oil hybrid power device |
| CN207435019U (en) * | 2017-09-13 | 2018-06-01 | 广东能态科技有限公司 | A kind of hydrogen making machine exhaust and pressure relief system |
| CN210340323U (en) * | 2019-06-20 | 2020-04-17 | 浙江工业大学 | Self-heating methanol reforming hydrogen production reaction system |
-
2019
- 2019-06-20 CN CN201910537996.2A patent/CN110316703B/en active Active
Patent Citations (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52129705A (en) * | 1976-04-24 | 1977-10-31 | Nissan Motor Co Ltd | Methanol-reforming apparatus |
| JPS61286203A (en) * | 1985-06-14 | 1986-12-16 | Mitsubishi Heavy Ind Ltd | Reforming method for methanol |
| JP2001089104A (en) * | 1999-09-22 | 2001-04-03 | Suzuki Motor Corp | Methanol reformer |
| CN101462694A (en) * | 2007-12-19 | 2009-06-24 | 中国科学院大连化学物理研究所 | Miniaturized methanol self-heating reforming hydrogen making integrated apparatus and hydrogen production method |
| CN201376896Y (en) * | 2009-04-22 | 2010-01-06 | 于景瑞 | Methanol steam reforming conversion hydrogen production device for automobile |
| CN102602885A (en) * | 2012-03-12 | 2012-07-25 | 云南大学 | Method for manufacturing hydrogen in reforming way by catalyst loaded at heat conducting material through utilizing heat of tail gas of heat engine |
| CN105649827A (en) * | 2016-01-19 | 2016-06-08 | 上海万寅安全环保科技有限公司 | Hydrogen-oil hybrid power device |
| CN207435019U (en) * | 2017-09-13 | 2018-06-01 | 广东能态科技有限公司 | A kind of hydrogen making machine exhaust and pressure relief system |
| CN210340323U (en) * | 2019-06-20 | 2020-04-17 | 浙江工业大学 | Self-heating methanol reforming hydrogen production reaction system |
Cited By (14)
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|---|---|---|---|---|
| CN111883805A (en) * | 2020-08-23 | 2020-11-03 | 浙江工业大学 | Small methanol reforming hydrogen production device system based on tail gas waste heat utilization |
| CN111883805B (en) * | 2020-08-23 | 2024-04-16 | 浙江工业大学 | Small-size methyl alcohol reforming hydrogen plant system based on tail gas waste heat utilization |
| CN112081690A (en) * | 2020-09-16 | 2020-12-15 | 杰锋汽车动力系统股份有限公司 | Methanol engine waste heat recovery hydrogen production device and hydrogen production method thereof |
| CN112661107A (en) * | 2020-12-10 | 2021-04-16 | 广东醇氢新能源研究院有限公司 | Hydrogen reactor and hydrogen production system |
| CN113184807A (en) * | 2021-06-01 | 2021-07-30 | 上海交通大学 | Pure oxygen combustion system based on waste heat utilization |
| CN114352444B (en) * | 2021-12-14 | 2023-02-28 | 武汉理工大学 | Liquefied natural gas engine and reformer combined operation control system and method |
| CN114352444A (en) * | 2021-12-14 | 2022-04-15 | 武汉理工大学 | Liquefied natural gas engine and reformer combined operation control system and method |
| WO2023124030A1 (en) * | 2021-12-30 | 2023-07-06 | 江苏科技大学 | Methanol reforming hydrogen production system using solar energy |
| CN114348963A (en) * | 2022-01-25 | 2022-04-15 | 山东理工大学 | Autothermal self-ignition reforming hydrogen production integrated device and hydrogen production method |
| CN114790940A (en) * | 2022-03-18 | 2022-07-26 | 大连交通大学 | Reverse reaction activity control compression ignition engine based on methanol dehydration reforming |
| CN115234370A (en) * | 2022-07-28 | 2022-10-25 | 西安交通大学 | System and method for small vehicle-mounted methanol reforming hydrogen production combined internal combustion engine |
| CN115234370B (en) * | 2022-07-28 | 2023-12-19 | 西安交通大学 | System and method for small vehicle-mounted methanol reforming hydrogen production combined internal combustion engine |
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| CN115744822A (en) * | 2022-12-07 | 2023-03-07 | 张宏辉 | High-efficiency methanol reforming hydrogen production device |
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