CN202808346U - Methyl alcohol steam reforming hydrogen production equipment - Google Patents
Methyl alcohol steam reforming hydrogen production equipment Download PDFInfo
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- CN202808346U CN202808346U CN 201220468195 CN201220468195U CN202808346U CN 202808346 U CN202808346 U CN 202808346U CN 201220468195 CN201220468195 CN 201220468195 CN 201220468195 U CN201220468195 U CN 201220468195U CN 202808346 U CN202808346 U CN 202808346U
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Abstract
The utility model discloses methyl alcohol steam reforming hydrogen production equipment. The hydrogen production equipment comprises a liquid storage container, main hydrogen production equipment and one or more sub-hydrogen production equipment, wherein the main hydrogen production equipment performs steps of heat exchange, gasifying, reforming and separation to obtain hydrogen; the exhausted residual gas is conveyed to one of the sub-hydrogen production equipment; the sub-hydrogen production equipment receives the residual gas (including useful gas without reacting completely) exhausted by the main hydrogen production equipment or/and the sub-hydrogen production equipment per se or/and other sub-hydrogen production equipment; and the hydrogen is prepared by the residual gas. With the methyl alcohol steam reforming hydrogen production equipment, the residual gas generated by the main hydrogen production equipment is reformed for one time or several times, so that the directly-exhausted residual gas can be reduced, the pollution to the environment is reduced, and the conversion rate of the hydrogen can be improved at the same time.
Description
Technical field
The utility model belongs to technical field of hydrogen preparation, relates to a kind of hydrogen producer, relates in particular to a kind of hydrogen production from methanol-steam reforming equipment.
Background technology
In numerous new forms of energy, Hydrogen Energy will become the optimal energy of 21 century.This is because in the situation of coal, gasoline and hydrogen of burning identical weight, the energy that hydrogen produces is maximum, and the product of its burning is water, does not have lime-ash and waste gas, does not pollute the environment; Be carbonic acid gas and sulfurous gas and coal and oil combustion generate, can produce respectively Greenhouse effect and acid rain.Coal and reserves are limited, and hydrogen mainly is stored in the water, and unique product also is water after the burning, can produce continuously hydrogen, is finished never.
Hydrogen is a kind of colourless gas.Burning one gram Hydrogen Energy discharges your heat of 142 kilojoules, is 3 times of gasoline thermal value.The weight of hydrogen is light especially, and it has all gently been howed than gasoline, Sweet natural gas, kerosene, thereby carries, transports conveniently, is the only fuel of the vehicles that fly at a high speed such as space flight, aviation.Hydrogen can burn in oxygen, and the temperature of hydrogen flame can be up to 2500 ℃, thereby people's hydrogen cutting commonly used or weldable steel iron material.
In the Nature, the distribution of hydrogen is very extensive.Water is exactly large " warehouse " of hydrogen, wherein contains 11% hydrogen.There is 1.5% hydrogen the earth Rio; All contain hydrogen in the oil, coal, Sweet natural gas, animal and plant body etc.The main body of hydrogen is that the form with compound water exists, and earth surface about 70% is covered by water, and moisture storage capacity is very large, therefore can say that hydrogen is the energy of " inexhaustible, nexhaustible ".If can be with suitable method preparing hydrogen from water, hydrogen also will be the quite cheap energy of a kind of price so.
Having many uses of hydrogen, suitability is strong.It can not only be used as fuel, and metal hydride has the function that chemical energy, heat energy and mechanical energy are changed mutually.For example, hydrogen storage metal has the ability of inhaling the hydrogen heat release and absorbing heat and putting hydrogen, heat can be stored, and uses as heating and air-conditioning in the room.
Hydrogen at first is used on the automobile as geseous fuel.In May, 1976, the U.S. develops a kind of automobile of making fuel with hydrogen; Afterwards, Japan also succeeded in developing a kind of automobile take liquid hydrogen as fuel; In the latter stage seventies, the Mercedes of front Germany tests hydrogen, and they have only used five kg of hydrogen, has just made running car 110 kilometers.
As automobile fuel, not only clean with hydrogen, start easily at low temperatures, and little to the corrosive nature of engine, can prolong the work-ing life of engine.Because hydrogen can evenly mix with air, can save vaporizer used on the general automobile fully, thereby can simplify the structure of existing automobile.More interesting is to need only the hydrogen of adding 4% in gasoline.Use it as motor car engine fuel, but just fuel-economizing 40%, and need not petrol engine is done great improvement.
Hydrogen is easy to become liquid under certain pressure and temperature, thereby it is all very convenient with iron flask car, on-highway tractor or ship transportation.Liquid hydrogen both can be used as the fuel of automobile, aircraft, also can be used as the fuel of rocket, guided missile.The fly to Apollo Personnel investigation Program of the moon of the U.S. " Long March launch vehicle that number spaceship and China launch a man-made satellite., all make fuel with liquid hydrogen.
In addition, use hydrogen-hydrogen fuel cell directly to change into electric energy to Hydrogen Energy, make utilizing of Hydrogen Energy more convenient.At present, this fuel cell obtains using at spaceship and undersea boat, and effect is pretty good.Certainly, because cost is higher, also be difficult to generally use for the moment.
The annual production of hydrogen is about 3,600 ten thousand tons in the world now, and wherein the overwhelming majority is produced from oil, coal and Sweet natural gas, and this must consume original just mineral fuel very in short supply; The hydrogen that other has 4% is to produce with the method for brine electrolysis, but the electric energy that consumes is too many, does not calculate very much, and therefore, people are trying to explore to study the hydrogen manufacturing novel method.And can reduce the energy consumption in the Chemical Manufacture and reduce cost with methyl alcohol, water reformation hydrogen production, be expected to substitute the technique of " water electrolysis hydrogen production " that be called as electricity-eating tiger, utilize advanced methanol vapor to reform--pressure swing adsorption making pure hydrogen and be rich in CO
2Mixed gas, through further aftertreatment, can obtain simultaneously hydrogen and carbon dioxide gas.
Methyl alcohol and water vapour pass through catalyzer under certain temperature, pressure condition, under the effect of catalyzer, the transformationreation of methanol decomposition reaction and carbon monoxide occurs, generate hydrogen and carbonic acid gas, this is the gas solid catalytic reaction system of component more than, many reactions.Reactional equation is as follows:
CH
3OH→CO+2H
2 (1)
H
2O+CO→CO
2+H
2 (2)
CH
3OH+H
2O→CO
2+3H
2 (3)
The H that reforming reaction generates
2And CO
2, pass through again pressure swing adsorption process (PSA) or palladium membrane sepn with H
2And CO
2Separate, obtain high-purity hydrogen.The power consumption of pressure swing adsorption process is high, equipment is large, and is not suitable for small-scale hydrogen preparation.
Existing preparation method usually only does once and to reform, and then residual air is directly discharged or burns, and contains obnoxious flavour owing in the residual air, and direct discharge can have a strong impact on environment and people's health.By the mode of direct burning, then can waste resource, reduce transformation efficiency.
The utility model content
Technical problem to be solved in the utility model is: a kind of hydrogen production from methanol-steam reforming equipment is provided, can improves the transformation efficiency of hydrogen, save cost, reduce simultaneously residual air to the pollution of environment.
For solving the problems of the technologies described above, the utility model adopts following technical scheme:
A kind of hydrogen production from methanol-steam reforming equipment, described hydrogen producer comprises: liquid container, main hydrogen producer, one or more sub-hydrogen producer; Described main hydrogen producer prepares hydrogen, simultaneously the residual air of discharging is delivered in the sub-hydrogen producer; Described sub-hydrogen producer receives main hydrogen producer or/and self is or/and the residual air that other sub-hydrogen producers are discharged utilizes this residual air to continue preparation hydrogen.
As a kind of preferred version of the present utility model, described main hydrogen producer comprises: interchanger, vaporizer, reformer chamber, separate chamber; Described liquid container, interchanger, vaporizer, reformer chamber, separate chamber connect successively by pipeline; First alcohol and water in the described liquid container is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange; Methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer; Be provided with membrane separation apparatus in the described separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus, residual air is discharged.
As a kind of preferred version of the present utility model, Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output.
As a kind of preferred version of the present utility model, described sub-hydrogen producer comprises: sub-reformer chamber, sub-separate chamber; Described sub-reformer chamber, sub-separate chamber connect successively by pipeline; The residual air that described sub-hydrogen producer is collected enters sub-reformer chamber and reforms, and the Transfer pipe between sub-reformer chamber and the sub-separate chamber is through a sub-preheating temperature-controlling mechanism, and this sub-preheating temperature-controlling mechanism is in order to the gas of heating from sub-reformer chamber output; Described sub-preheating temperature-controlling mechanism is as the buffering between sub-reformer chamber and the sub-separate chamber, so that identical or approaching with the temperature of sub-separate chamber from the temperature of the gas of sub-reformer chamber output; Gas after the reformation enters sub-separate chamber to be separated; Be provided with membrane separation apparatus in the sub-separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus, residual air is discharged, perhaps continue to enter self or other sub-hydrogen producer reformation hydrogen productions.
The beneficial effects of the utility model are: the hydrogen production from methanol-steam reforming Apparatus and method for that the utility model proposes, carrying out one or many by the residual air that main hydrogen producer is produced reforms again, can reduce the residual air of direct discharge, minimizing can improve the transformation efficiency of hydrogen simultaneously to the pollution of environment.
Description of drawings
Fig. 1 is the composition synoptic diagram of the utility model hydrogen producer.
Fig. 2 is the schema of the utility model hydrogen production process.
Embodiment
Describe preferred embodiment of the present utility model in detail below in conjunction with accompanying drawing.
Embodiment one
See also Fig. 1, the utility model has disclosed a kind of hydrogen production from methanol-steam reforming equipment, and described hydrogen producer comprises: liquid container 10, main hydrogen producer 20, one or more sub-hydrogen producer 30.
Described main hydrogen producer 20 comprises: interchanger, vaporizer, reformer chamber, separate chamber; Described liquid container, interchanger, vaporizer, reformer chamber, separate chamber connect successively by pipeline.
First alcohol and water in the described liquid container 10 is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange.Methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °.
Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output; Reformer chamber is provided with catalyzer: Cu-ZnO-Al
2O
3Or/and Cu-ZnO-ZrO.
Temperature Setting in the described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus, residual air is discharged, include in the residual air without crossing the fully valuable gases of reaction.
Described sub-hydrogen producer 30 receives main hydrogen producers 20 or/and self is or/and the residual air that other sub-hydrogen producers are discharged (in the present embodiment, a sub-hydrogen producer 30 receives the residual air that main hydrogen producer 20 is discharged, a sub-hydrogen producer 30 receives the residual air that other sub-hydrogen producers 30 are discharged), utilize in this residual air and continue preparation hydrogen without the valuable gases of crossing fully reaction.Described sub-hydrogen producer comprises: sub-reformer chamber, sub-separate chamber; Described sub-reformer chamber, sub-separate chamber connect successively by pipeline.
The residual air that described sub-hydrogen producer 30 is collected enters sub-reformer chamber and reforms, and the Transfer pipe between sub-reformer chamber and the sub-separate chamber is through a sub-preheating temperature-controlling mechanism, and this sub-preheating temperature-controlling mechanism is in order to the gas of heating from sub-reformer chamber output; Described sub-preheating temperature-controlling mechanism is as the buffering between sub-reformer chamber and the sub-separate chamber, so that identical or approaching with the temperature of sub-separate chamber from the temperature of the gas of sub-reformer chamber output; Reformer chamber is provided with catalyzer: Cu-ZnO-Al
2O
3Or/and Cu-ZnO-ZrO.
Gas after the reformation enters sub-separate chamber to be separated; Temperature Setting in the described sub-separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the sub-separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus, residual air is discharged, perhaps continue to enter self or other sub-hydrogen producer reformation hydrogen productions.
More than introduced the composition of the utility model hydrogen production from methanol-steam reforming equipment, the utility model also discloses a kind of hydrogen production process of above-mentioned hydrogen production from methanol-steam reforming equipment when disclosing above-mentioned hydrogen production from methanol-steam reforming equipment; See also Fig. 2, described method comprises the steps: step 1, main hydrogen producer reformation preparation hydrogen; Step 2, sub-hydrogen producer utilize the residual air preparation hydrogen of reforming, and then residual air are discharged or is delivered to self or other sub-hydrogen producer reformation hydrogen productions.
Described step 1 specifically comprises:
First alcohol and water in [step S11] described liquid container is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange.
Methanol vapor and water vapour after [step S12] gasification enter reformer chamber, and reformer chamber is provided with catalyzer, and the temperature of reformer chamber is 280 °-409 °.
Transfer pipe between [step S13] reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output; Described preheating temperature-controlling mechanism is as the buffering between reformer chamber and the separate chamber, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output; Reformer chamber is provided with catalyzer: Cu-ZnO-Al
2O
3Or/and Cu-ZnO-ZrO.
Temperature Setting in [step S14] described separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus, residual air is discharged.Described step 2 specifically comprises:
The residual air that [step S21] described sub-hydrogen producer is collected enters sub-reformer chamber and reforms, and the Transfer pipe between sub-reformer chamber and the sub-separate chamber is through a sub-preheating temperature-controlling mechanism, and this sub-preheating temperature-controlling mechanism is in order to the gas of heating from sub-reformer chamber output; Described sub-preheating temperature-controlling mechanism is as the buffering between sub-reformer chamber and the sub-separate chamber, so that identical or approaching with the temperature of sub-separate chamber from the temperature of the gas of sub-reformer chamber output; Reformer chamber is provided with catalyzer: Cu-ZnO-Al
2O
3Or/and Cu-ZnO-ZrO.
Gas after [step S22] reforms enters sub-separate chamber to be separated; Temperature Setting in the described sub-separate chamber is 400 °-460 °; Be provided with membrane separation apparatus in the sub-separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus, residual air is discharged, perhaps continue to enter self or other sub-hydrogen producer reformation hydrogen productions.
In sum, the hydrogen production from methanol-steam reforming Apparatus and method for that the utility model proposes carries out one or many by the residual air that main hydrogen producer is produced and reforms, can reduce the residual air of direct discharge, minimizing can improve the transformation efficiency of hydrogen simultaneously to the pollution of environment.
Here description of the present utility model and application is illustrative, is not to want with scope restriction of the present utility model in the above-described embodiments.Here the distortion of disclosed embodiment and change is possible, and the various parts of the replacement of embodiment and equivalence are known for those those of ordinary skill in the art.Those skilled in the art are noted that in the situation that does not break away from spirit of the present utility model or essential characteristic, and the utility model can be with other form, structure, layout, ratio, and realize with other assembly, material and parts.In the situation that does not break away from the utility model scope and spirit, can carry out other distortion and change to disclosed embodiment here.
Claims (4)
1. a hydrogen production from methanol-steam reforming equipment is characterized in that, described hydrogen producer comprises: liquid container, main hydrogen producer, one or more sub-hydrogen producer;
Described main hydrogen producer prepares hydrogen, simultaneously the residual air of discharging is delivered in the sub-hydrogen producer;
Described sub-hydrogen producer receives main hydrogen producer or/and self is or/and the residual air that other sub-hydrogen producers are discharged utilizes this residual air to continue preparation hydrogen.
2. hydrogen production from methanol-steam reforming equipment according to claim 1 is characterized in that:
Described main hydrogen producer comprises: interchanger, vaporizer, reformer chamber, separate chamber; Described liquid container, interchanger, vaporizer, reformer chamber, separate chamber connect successively by pipeline;
First alcohol and water in the described liquid container is delivered to the interchanger heat exchange by e Foerderanlage, enters the vaporizer gasification after the heat exchange;
Methanol vapor and water vapour after the gasification enter reformer chamber, and reformer chamber is provided with catalyzer;
Be provided with membrane separation apparatus in the described separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus, residual air is discharged.
3. hydrogen production from methanol-steam reforming equipment according to claim 2 is characterized in that:
Transfer pipe between reformer chamber and the separate chamber is through a preheating temperature-controlling mechanism, and this preheating temperature-controlling mechanism is in order to the gas of heating from reformer chamber output, so that identical or approaching with the temperature of separate chamber from the temperature of the gas of reformer chamber output.
4. hydrogen production from methanol-steam reforming equipment according to claim 1 is characterized in that:
Described sub-hydrogen producer comprises: sub-reformer chamber, sub-separate chamber; Described sub-reformer chamber, sub-separate chamber connect successively by pipeline;
The residual air that described sub-hydrogen producer is collected enters sub-reformer chamber and reforms, and the Transfer pipe between sub-reformer chamber and the sub-separate chamber is through a sub-preheating temperature-controlling mechanism, and this sub-preheating temperature-controlling mechanism is in order to the gas of heating from sub-reformer chamber output; Described sub-preheating temperature-controlling mechanism is as the buffering between sub-reformer chamber and the sub-separate chamber, so that identical or approaching with the temperature of sub-separate chamber from the temperature of the gas of sub-reformer chamber output;
Gas after the reformation enters sub-separate chamber to be separated; Be provided with membrane separation apparatus in the sub-separate chamber, obtain hydrogen from the aerogenesis end of membrane separation apparatus, residual air is discharged, perhaps continue to enter self or other sub-hydrogen producer reformation hydrogen productions.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220468195 CN202808346U (en) | 2012-09-13 | 2012-09-13 | Methyl alcohol steam reforming hydrogen production equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220468195 CN202808346U (en) | 2012-09-13 | 2012-09-13 | Methyl alcohol steam reforming hydrogen production equipment |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202808346U true CN202808346U (en) | 2013-03-20 |
Family
ID=47867267
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220468195 Expired - Fee Related CN202808346U (en) | 2012-09-13 | 2012-09-13 | Methyl alcohol steam reforming hydrogen production equipment |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202808346U (en) |
-
2012
- 2012-09-13 CN CN 201220468195 patent/CN202808346U/en not_active Expired - Fee Related
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: GUANGDONG NENGTAI TECHNOLOGY INVESTMENT CO.,LTD. Assignor: SHANGHAI HYDROGEN MOBILE REFRMER INSTRUMENT Co.,Ltd. Contract record no.: 2014440000168 Denomination of utility model: Apparatus and method for hydrogen production through methanol steam reforming Granted publication date: 20130320 License type: Common License Record date: 20140417 |
|
| LICC | Enforcement, change and cancellation of record of contracts on the licence for exploitation of a patent or utility model | ||
| PP01 | Preservation of patent right |
Effective date of registration: 20210918 Granted publication date: 20130320 |
|
| PP01 | Preservation of patent right | ||
| PD01 | Discharge of preservation of patent |
Date of cancellation: 20220913 Granted publication date: 20130320 |
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| PD01 | Discharge of preservation of patent | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130320 Termination date: 20210913 |
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| CF01 | Termination of patent right due to non-payment of annual fee |