CN104671203A - Method for generating hydrogen through methanol decomposition and pressure swing adsorption - Google Patents
Method for generating hydrogen through methanol decomposition and pressure swing adsorption Download PDFInfo
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- CN104671203A CN104671203A CN201510057655.7A CN201510057655A CN104671203A CN 104671203 A CN104671203 A CN 104671203A CN 201510057655 A CN201510057655 A CN 201510057655A CN 104671203 A CN104671203 A CN 104671203A
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Abstract
The invention relates to a method for generating hydrogen through methanol decomposition and pressure swing adsorption. The method comprises the following steps: (1) uniformly mixing methanol and desalted water at a molar ratio to obtain a methanol aqueous solution; (2) conveying the methanol aqueous solution into a shell pass of a heat exchanger by a metering pump through a flowmeter to perform preliminary preheating; (3) guiding the methanol aqueous solution after the preliminary preheating into a vaporizing tower for vaporization; (4) heating the methanol steam from the gasifying tower by a tube pass of a heater; (5) guiding the heated methanol steam into a converter for conversion; (6) guiding the converted gas into the tube pass and shell pass of the heat exchanger; (7) guiding the cooled converted gas into a water scrubber for absorption separation; and (8) performing water scrubbing to obtain a decomposition gas, and performing pressure swing adsorption of the decomposition gas to extract hydrogen. According to the method provided by the invention, the conversion rate of methanol is over 99%; the purity of the prepared hydrogen can reach 99.99%; the gas supply quantity is stable; the gas transmission pressure is high, thereby being safer and more convenient; and no pollutant is generated in the preparation process.
Description
Technical field
The present invention relates to a kind of method of hydrogen manufacturing, be specifically related to a kind of method of methanol decomposition and pressure swing adsorption hydrogen production, belong to chemical field.
Background technology
Along with the fast development of the hydrogenation industry that becomes more meticulous, as benzene hydrogenation, neopentyl glycol hydrogenation, chemical industry hydrogen amount improves constantly, and it is also more and more higher to the requirement of hydrogen source, as high pressure, high purity, the invention provides a kind of method of methanol decomposition and pressure swing adsorption hydrogen production, can the high-purity high pressure hydrogen of continuous seepage, meet the requirement that hydrogen is used.
Summary of the invention
The object of the present invention is to provide a kind of method of methanol decomposition and pressure swing adsorption hydrogen production, concrete technical scheme is as follows:
(1) methyl alcohol and de-salted water in molar ratio 1:0.5-0.6 mix in circulation fluid storage tank, obtain methanol aqueous solution; Preferably, the mol ratio of methyl alcohol and de-salted water is 1:0.55-0.58; Most preferred, mol ratio is 1:0.56;
(2) methanol aqueous solution is transported to heat exchanger shell pass through under meter by volume pump and carries out preliminary preheating, and the temperature after methanol aqueous solution preheating is 75-100 DEG C; Preferably, the temperature after methanol aqueous solution preheating is 80-90 DEG C;
(3) vaporize in the methanol aqueous solution importing vaporization tower after preliminary preheating, obtain methanol steam, utilize methanol steam to carry to 1.05 MPas by vaporization tower internal pressure, vaporization tower heat-conducting oil heating, the temperature that vaporization tower is exported reaches 150-180 DEG C; Preferably, the temperature of vaporization tower outlet is 160-165 DEG C;
(4) be heated to 170-175 DEG C from vaporization tower methanol steam heater via tube side out, well heater shell side by thermal oil to methanol steam temperature raising;
(5) methanol steam after heating is imported converter, be 1.05 MPas at pressure, temperature is under the condition of 230-300 DEG C, utilizes copper-zinc-Al catalysts to make methanol steam generation scission reaction, obtains reforming gas; In the present invention, the composition of reforming gas is methanol steam and the carbon monoxide of hydrogen about 80%, carbonic acid gas about 19% and trace; Preferably, the methanol steam after heating is imported converter, and be 1.05 MPas at pressure, temperature is under the condition of 240-280 DEG C, utilizes copper-zinc-Al catalysts to make methanol steam generation scission reaction;
(6) reforming gas is imported heat exchanger tube pass and shell side, wherein, methanol aqueous solution heat exchange enters the cooling of housing of cooler journey after reclaiming heat, water cooler tube side circulating water cooling is to 30-40 DEG C; Preferably, water cooler tube side circulating water cooling is to 35-40 DEG C;
(7) reforming gas after cooling is imported water wash column and carry out absorption extraction, by water wash column tower top spray de-salted water, unreacted methyl alcohol is reclaimed;
(8) after step (7) washing, obtain splitting gas, splitting gas is not from water wash column Base top contact, carry hydrogen containing carrying out pressure-variable adsorption after carbon monoxide through buffering, sample examination;
(9) pressure-variable adsorption is put forward the step of hydrogen and is:
Pressure-variable adsorption comprises 6 adsorption towers, and the operational process of each adsorption tower is:
1. boosting utilizes and containing the splitting gas of carbon monoxide, adsorption tower is not boosted to 1.0 MPas;
2. adsorb and keep adsorption column pressure constant, input splitting gas, exports light constituent at tower top simultaneously, and at light constituent and the hydrogen of tower top output, in adsorption tower, heavy constituent is attracted on sorbent material;
3. pressure is reduced along the direction of putting along entering splitting gas, effluent air is still light constituent, for bed boosting or the flushing of other adsorption towers, constantly declines in the process with bed layer pressure, heavy constituent on sorbent material is by continuous desorb, and heavy constituent moves toward adsorption column outlet bed;
4. inverse put reduces pressure against the direction entering splitting gas output light constituent, until adsorption tower internal pressure is close to normal atmosphere, the heavy component major part of adsorption bed is got rid of outside adsorption tower with air-flow;
5. vacuumize the way utilizing vacuum pump to aspirate and constantly reduce adsorption tower internal pressure, make heavy constituent continue desorb and be drawn out of adsorption tower, vacuum level requirements reaches negative 0.09 MPa.
Adsorption tower 6 tower runs simultaneously, and wherein, the charging simultaneously of every 2 towers, all presses for 3 times, regeneration of finding time.
Pressure swing adsorption is that under utilizing sorbent material easily to adsorb high boiling point component (as carbonic acid gas), not easily absorption lower boiling component (as hydrogen) and high pressure at the same pressure, adsorptive capacity increases, adds the characteristic depressed adsorptive capacity and reduce by sorbent material (porosu solid material) interior surface to based on the physical adsorption of gas molecule.By splitting gas under stress by adsorbent bed, high boiling point component by selective absorbing, low-boiling point material not easily adsorbs and by adsorbent bed, reaches the separation of weight component.Then under reduced pressure desorb is made sorbent material obtain regeneration by the component adsorbed, and is beneficial to again carry out fractionation by adsorption impurity.
In the present invention, to carry out vaporization after metering overheated for methyl alcohol and de-salted water, conversion reaction is there is after entering vaporization tower, arrive absorption tower de-salted water again to absorb, after absorbing, water-fast gas goes pressure-variable adsorption to carry out absorption purification, obtain product hydrogen, wherein absorbed methyl alcohol becomes de-salted water recycling, and the stripping gas that pressure-variable adsorption produces contains can combusting component, sends to natural gas boiler room and carries out burning providing heat to thermal oil.Whole set process contamination-free, heat makes full use of.
The present invention compared with prior art has the following advantages:
1, the transformation efficiency of methyl alcohol is stabilized in more than 99%, unreacted Methanol Recovery recycling, cost-saving;
2, the hydrogen purity that prepared by the present invention can reach 99.99%, is applicable to the industry higher to hydrogen purity requirement;
3, air demand is stablized, and distribution pressure is high, makes high pressure hydrogen storage equipment save compression link, safer, convenient;
4, in preparation process of the present invention, contamination-free produces.
Accompanying drawing explanation
fig. 1 is present invention process schema.
Embodiment
Further describe the present invention below in conjunction with specific embodiment, advantage and disadvantage of the present invention will be more clear along with description.But embodiment is only exemplary, does not form any restriction to scope of the present invention.It will be understood by those skilled in the art that and can modify to the details of technical solution of the present invention and form or replace down without departing from the spirit and scope of the present invention, but these amendments and replacement all fall within the scope of protection of the present invention.
The method of embodiment 1 one kinds of methanol decompositions and pressure swing adsorption hydrogen production, concrete steps are as follows:
(1) methyl alcohol and de-salted water in molar ratio 1:0.56 mix in circulation fluid storage tank, obtain methanol aqueous solution;
(2) methanol aqueous solution is transported to heat exchanger shell pass through under meter by volume pump and carries out preliminary preheating, and the temperature after methanol aqueous solution preheating is 80-90 DEG C;
(3) vaporize in the methanol aqueous solution importing vaporization tower after preliminary preheating, obtain methanol steam, utilize methanol steam to carry to 1.05 MPas by vaporization tower internal pressure, vaporization tower heat-conducting oil heating, the temperature that vaporization tower is exported is 160-165 DEG C;
(4) be heated to 170-175 DEG C from vaporization tower methanol steam heater via tube side out, well heater shell side by thermal oil to methanol steam temperature raising;
(5) methanol steam after heating is imported converter, be 1.05 MPas at pressure, temperature is under the condition of 240-280 DEG C, utilizes copper-zinc-Al catalysts to make methanol steam generation scission reaction, obtains reforming gas;
(6) reforming gas is imported heat exchanger tube pass and shell side, wherein, methanol aqueous solution heat exchange enters the cooling of housing of cooler journey after reclaiming heat, water cooler tube side circulating water cooling is to 35-40 DEG C;
(7) reforming gas after cooling is imported water wash column and carry out absorption extraction, by water wash column tower top spray de-salted water, unreacted methyl alcohol is reclaimed;
(8) after step (7) washing, obtain splitting gas, splitting gas is not from water wash column Base top contact, carry hydrogen containing carrying out pressure-variable adsorption after carbon monoxide through buffering, sample examination;
(9) pressure-variable adsorption is put forward the step of hydrogen and is:
Pressure-variable adsorption comprises 6 adsorption towers, and the operational process of each adsorption tower is:
1. boosting utilizes and containing the splitting gas of carbon monoxide, adsorption tower is not boosted to 1.0 MPas;
2. adsorb and keep adsorption column pressure constant, input splitting gas, exports light constituent at tower top simultaneously, and at light constituent and the hydrogen of tower top output, in adsorption tower, heavy constituent is attracted on sorbent material;
3. pressure is reduced along the direction of putting along entering splitting gas, effluent air is still light constituent, for bed boosting or the flushing of other adsorption towers, constantly declines in the process with bed layer pressure, heavy constituent on sorbent material is by continuous desorb, and heavy constituent moves toward adsorption column outlet bed;
4. inverse put reduces pressure against the direction entering splitting gas output light constituent, until adsorption tower internal pressure is close to normal atmosphere, the heavy component major part of adsorption bed is got rid of outside adsorption tower with air-flow;
5. vacuumize the way utilizing vacuum pump to aspirate and constantly reduce adsorption tower internal pressure, make heavy constituent continue desorb and be drawn out of adsorption tower, vacuum level requirements reaches negative 0.09 MPa.
Adsorption tower 6 tower runs simultaneously, and wherein, the charging simultaneously of every 2 towers, all presses for 3 times, regeneration of finding time.
The method of embodiment 2 one kinds of methanol decompositions and pressure swing adsorption hydrogen production, concrete steps are as follows:
(1) methyl alcohol and de-salted water in molar ratio 1:0.55 mix in circulation fluid storage tank, obtain methanol aqueous solution;
(2) methanol aqueous solution is transported to heat exchanger shell pass through under meter by volume pump and carries out preliminary preheating, and the temperature after methanol aqueous solution preheating is 75-85 DEG C;
(3) vaporize in the methanol aqueous solution importing vaporization tower after preliminary preheating, obtain methanol steam, utilize methanol steam to carry to 1.05 MPas by vaporization tower internal pressure, vaporization tower heat-conducting oil heating, the temperature that vaporization tower is exported reaches 150-165 DEG C;
(4) be heated to 170-175 DEG C from vaporization tower methanol steam heater via tube side out, well heater shell side by thermal oil to methanol steam temperature raising;
(5) methanol steam after heating is imported converter, be 1.05 MPas at pressure, temperature is under the condition of 230-250 DEG C, utilizes copper-zinc-Al catalysts to make methanol steam generation scission reaction, obtains reforming gas;
(6) reforming gas is imported heat exchanger tube pass and shell side, wherein, methanol aqueous solution heat exchange enters the cooling of housing of cooler journey after reclaiming heat, water cooler tube side circulating water cooling is to 30-35 DEG C;
(7) reforming gas after cooling is imported water wash column and carry out absorption extraction, by water wash column tower top spray de-salted water, unreacted methyl alcohol is reclaimed;
(8) after step (7) washing, obtain splitting gas, splitting gas is not from water wash column Base top contact, carry hydrogen containing carrying out pressure-variable adsorption after carbon monoxide through buffering, sample examination;
(9) pressure-variable adsorption is put forward the step of hydrogen and is:
Pressure-variable adsorption comprises 6 adsorption towers, and the operational process of each adsorption tower is:
1. boosting utilizes and containing the splitting gas of carbon monoxide, adsorption tower is not boosted to 1.0 MPas;
2. adsorb and keep adsorption column pressure constant, input splitting gas, exports light constituent at tower top simultaneously, and at light constituent and the hydrogen of tower top output, in adsorption tower, heavy constituent is attracted on sorbent material;
3. pressure is reduced along the direction of putting along entering splitting gas, effluent air is still light constituent, for bed boosting or the flushing of other adsorption towers, constantly declines in the process with bed layer pressure, heavy constituent on sorbent material is by continuous desorb, and heavy constituent moves toward adsorption column outlet bed;
4. inverse put reduces pressure against the direction entering splitting gas output light constituent, until adsorption tower internal pressure is close to normal atmosphere, the heavy component major part of adsorption bed is got rid of outside adsorption tower with air-flow;
5. vacuumize the way utilizing vacuum pump to aspirate and constantly reduce adsorption tower internal pressure, make heavy constituent continue desorb and be drawn out of adsorption tower, vacuum level requirements reaches negative 0.09 MPa.
Adsorption tower 6 tower runs simultaneously, and wherein, the charging simultaneously of every 2 towers, all presses for 3 times, regeneration of finding time.
The method of embodiment 3 one kinds of methanol decompositions and pressure swing adsorption hydrogen production, concrete steps are as follows:
(1) methyl alcohol and de-salted water in molar ratio 1:0.58 mix in circulation fluid storage tank, obtain methanol aqueous solution;
(2) methanol aqueous solution is transported to heat exchanger shell pass through under meter by volume pump and carries out preliminary preheating, and the temperature after methanol aqueous solution preheating is 85-95 DEG C;
(3) vaporize in the methanol aqueous solution importing vaporization tower after preliminary preheating, obtain methanol steam, utilize methanol steam to carry to 1.05 MPas by vaporization tower internal pressure, vaporization tower heat-conducting oil heating, the temperature that vaporization tower is exported reaches 170-180 DEG C;
(4) be heated to 170-175 DEG C from vaporization tower methanol steam heater via tube side out, well heater shell side by thermal oil to methanol steam temperature raising;
(5) methanol steam after heating is imported converter, be 1.05 MPas at pressure, temperature is under the condition of 260-300 DEG C, utilizes copper-zinc-Al catalysts to make methanol steam generation scission reaction, obtains reforming gas;
(6) reforming gas is imported heat exchanger tube pass and shell side, wherein, methanol aqueous solution heat exchange enters the cooling of housing of cooler journey after reclaiming heat, water cooler tube side circulating water cooling is to 36-40 DEG C;
(7) reforming gas after cooling is imported water wash column and carry out absorption extraction, by water wash column tower top spray de-salted water, unreacted methyl alcohol is reclaimed;
(8) after step (7) washing, obtain splitting gas, splitting gas is not from water wash column Base top contact, carry hydrogen containing carrying out pressure-variable adsorption after carbon monoxide through buffering, sample examination;
(9) pressure-variable adsorption is put forward the step of hydrogen and is:
Pressure-variable adsorption comprises 6 adsorption towers, and the operational process of each adsorption tower is:
1. boosting utilizes and containing the splitting gas of carbon monoxide, adsorption tower is not boosted to 1.0 MPas;
2. adsorb and keep adsorption column pressure constant, input splitting gas, exports light constituent at tower top simultaneously, and at light constituent and the hydrogen of tower top output, in adsorption tower, heavy constituent is attracted on sorbent material;
3. pressure is reduced along the direction of putting along entering splitting gas, effluent air is still light constituent, for bed boosting or the flushing of other adsorption towers, constantly declines in the process with bed layer pressure, heavy constituent on sorbent material is by continuous desorb, and heavy constituent moves toward adsorption column outlet bed;
4. inverse put reduces pressure against the direction entering splitting gas output light constituent, until adsorption tower internal pressure is close to normal atmosphere, the heavy component major part of adsorption bed is got rid of outside adsorption tower with air-flow;
5. vacuumize the way utilizing vacuum pump to aspirate and constantly reduce adsorption tower internal pressure, make heavy constituent continue desorb and be drawn out of adsorption tower, vacuum level requirements reaches negative 0.09 MPa.
Adsorption tower 6 tower runs simultaneously, and wherein, the charging simultaneously of every 2 towers, all presses for 3 times, regeneration of finding time.
Test example 1
After testing, in the present invention, the transformation efficiency of methyl alcohol is stabilized in more than 99%; And hydrogen purity prepared by the present invention can reach 99.99%.
Claims (8)
1. a method for methanol decomposition and pressure swing adsorption hydrogen production, is characterized in that, comprises the following steps:
(1) methyl alcohol and de-salted water in molar ratio 1:0.5-0.6 mix in circulation fluid storage tank, obtain methanol aqueous solution;
(2) methanol aqueous solution is transported to heat exchanger shell pass through under meter by volume pump and carries out preliminary preheating, and the temperature after methanol aqueous solution preheating is 75-100 DEG C;
(3) vaporize in the methanol aqueous solution importing vaporization tower after preliminary preheating, obtain methanol steam, utilize methanol steam to carry to 1.05 MPas by vaporization tower internal pressure, vaporization tower heat-conducting oil heating, the temperature that vaporization tower is exported reaches 150-180 DEG C;
(4) be heated to 170-175 DEG C from vaporization tower methanol steam heater via tube side out, well heater shell side by thermal oil to methanol steam temperature raising;
(5) methanol steam after heating is imported converter, be 1.05 MPas at pressure, temperature is under the condition of 230-300 DEG C, utilizes copper-zinc-Al catalysts to make methanol steam generation scission reaction, obtains reforming gas;
(6) reforming gas is imported heat exchanger tube pass and shell side, wherein, methanol aqueous solution heat exchange enters the cooling of housing of cooler journey after reclaiming heat, water cooler tube side circulating water cooling is to 30-40 DEG C;
(7) reforming gas after cooling is imported water wash column and carry out absorption extraction, by water wash column tower top spray de-salted water, unreacted methyl alcohol is reclaimed;
(8) after step (7) washing, obtain splitting gas, splitting gas is not from water wash column Base top contact, carry hydrogen containing carrying out pressure-variable adsorption after carbon monoxide through buffering, sample examination.
2. method according to claim 1, is characterized in that, in described step (1), the mol ratio of methyl alcohol and de-salted water is 1:0.55-0.58.
3. method according to claim 2, is characterized in that, in described step (1), the mol ratio of methyl alcohol and de-salted water is 1:0.56.
4. method according to claim 1, is characterized in that, the temperature in described step (2) after methanol aqueous solution preheating is 80-90 DEG C.
5. method according to claim 1, is characterized in that, in described step (3), the temperature of vaporization tower outlet is 160-165 DEG C.
6. method according to claim 1, it is characterized in that, in described step (5), the methanol steam after heating being imported converter, is 1.05 MPas at pressure, temperature is under the condition of 240-280 DEG C, utilizes copper-zinc-Al catalysts to make methanol steam generation scission reaction.
7. method according to claim 1, is characterized in that, in described step (6), water cooler tube side circulating water cooling is to 35-40 DEG C.
8. the method according to any one of claim 1-7, is characterized in that, described pressure-variable adsorption carries hydrogen, comprises the following steps:
Pressure-variable adsorption comprises 6 adsorption towers, and the operational process of each adsorption tower is:
1. boosting utilizes and containing the splitting gas of carbon monoxide, adsorption tower is not boosted to 1.0 MPas;
2. adsorb and keep adsorption column pressure constant, input splitting gas, exports light constituent at tower top simultaneously, and at light constituent and the hydrogen of tower top output, in adsorption tower, heavy constituent is attracted on sorbent material;
3. reduce pressure along the direction of putting along entering splitting gas, constantly decline with bed layer pressure, the heavy constituent on sorbent material is by continuous desorb, and heavy constituent moves toward adsorption column outlet bed;
4. inverse put reduces pressure against the direction entering splitting gas output light constituent, until adsorption tower internal pressure is close to normal atmosphere, makes the heavy component major part of adsorption bed get rid of outside adsorption tower with air-flow;
5. vacuumize the pressure utilized in vacuum pump reduction adsorption tower, make heavy constituent continue desorb and be drawn out of adsorption tower, vacuum tightness is negative 0.09 MPa.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107572478A (en) * | 2017-09-22 | 2018-01-12 | 重庆润泰节能科技有限公司 | A kind of preparation method and hydrogen-containing fuel of methanol decomposition hydrogen manufacturing gas |
| CN109650335A (en) * | 2019-01-21 | 2019-04-19 | 武汉理工大学 | A kind of pressure varying adsorption of purified device for producing hydrogen and hydrogen production process |
| CN110342712A (en) * | 2019-06-28 | 2019-10-18 | 金澳科技（湖北）化工有限公司 | A kind of processing system and method applied to MTBE extraction water |
| CN110357038A (en) * | 2019-08-01 | 2019-10-22 | 苏州新瑞净化设备有限公司 | A kind of electric heating preparing hydrogen by reforming methanol device and its hydrogen production process |
| CN110577190A (en) * | 2018-06-11 | 2019-12-17 | 河南车权健新能源科技有限公司 | process for preparing hydrogen by cracking methanol |
| CN110963462A (en) * | 2019-12-11 | 2020-04-07 | 宁夏泰富能源有限公司 | Methanol hydrogen production system |
| CN112142004A (en) * | 2020-08-18 | 2020-12-29 | 广东醇氢新能源研究院有限公司 | Hydrogen production and purification method by methanol-water reforming reaction |
| CN112657431A (en) * | 2020-12-01 | 2021-04-16 | 安徽成泰医药科技有限公司 | Evacuating device for hydrogen production by methanol cracking |
| CN112707369A (en) * | 2021-02-19 | 2021-04-27 | 山东东昌精细化工科技有限公司 | Process and device for efficiently preparing carbon monoxide and hydrogen by utilizing methanol cracking |
| CN113860996A (en) * | 2021-04-23 | 2021-12-31 | 东营市海科瑞林化工有限公司 | Raw material methanol oil removal treatment process in methanol hydrogen production process |
| CN115893315A (en) * | 2022-11-29 | 2023-04-04 | 本源精化环保科技有限公司 | Preparation method of high-purity hydrogen |
| TWI831412B (en) * | 2022-10-12 | 2024-02-01 | 中興電工機械股份有限公司 | Integrated hydrogen production and charging system and method thereof |
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| CN107572478A (en) * | 2017-09-22 | 2018-01-12 | 重庆润泰节能科技有限公司 | A kind of preparation method and hydrogen-containing fuel of methanol decomposition hydrogen manufacturing gas |
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| CN110342712A (en) * | 2019-06-28 | 2019-10-18 | 金澳科技（湖北）化工有限公司 | A kind of processing system and method applied to MTBE extraction water |
| CN110357038A (en) * | 2019-08-01 | 2019-10-22 | 苏州新瑞净化设备有限公司 | A kind of electric heating preparing hydrogen by reforming methanol device and its hydrogen production process |
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| CN112142004A (en) * | 2020-08-18 | 2020-12-29 | 广东醇氢新能源研究院有限公司 | Hydrogen production and purification method by methanol-water reforming reaction |
| CN112142004B (en) * | 2020-08-18 | 2023-06-27 | 广东醇氢新能源研究院有限公司 | Hydrogen production and purification method by methanol-water reforming reaction |
| CN112657431A (en) * | 2020-12-01 | 2021-04-16 | 安徽成泰医药科技有限公司 | Evacuating device for hydrogen production by methanol cracking |
| CN112707369A (en) * | 2021-02-19 | 2021-04-27 | 山东东昌精细化工科技有限公司 | Process and device for efficiently preparing carbon monoxide and hydrogen by utilizing methanol cracking |
| CN112707369B (en) * | 2021-02-19 | 2024-05-17 | 山东东昌精细化工科技有限公司 | Process and device for efficiently preparing carbon monoxide and hydrogen by utilizing methanol pyrolysis |
| CN113860996A (en) * | 2021-04-23 | 2021-12-31 | 东营市海科瑞林化工有限公司 | Raw material methanol oil removal treatment process in methanol hydrogen production process |
| TWI831412B (en) * | 2022-10-12 | 2024-02-01 | 中興電工機械股份有限公司 | Integrated hydrogen production and charging system and method thereof |
| CN115893315A (en) * | 2022-11-29 | 2023-04-04 | 本源精化环保科技有限公司 | Preparation method of high-purity hydrogen |
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Application publication date: 20150603 |