CN115594147A - Method for preparing hydrogen from methanol and system for preparing hydrogen from methanol - Google Patents
Method for preparing hydrogen from methanol and system for preparing hydrogen from methanol Download PDFInfo
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- CN115594147A CN115594147A CN202110778622.7A CN202110778622A CN115594147A CN 115594147 A CN115594147 A CN 115594147A CN 202110778622 A CN202110778622 A CN 202110778622A CN 115594147 A CN115594147 A CN 115594147A
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- 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
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
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- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
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- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
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- 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
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Abstract
The invention relates to a method for preparing hydrogen from methanol and a system for preparing hydrogen from methanol, wherein the method for preparing hydrogen from methanol comprises the following steps: the method comprises the following steps of (1) carrying out heat exchange on a methanol raw material to form methanol steam, mixing the methanol steam with medium-pressure steam to obtain mixed steam, and sending the mixed steam into a reactor to carry out methanol cracking reaction to obtain a product gas; enabling ultrahigh-pressure steam to enter the reactor as a heat source for the methanol cracking reaction for heat exchange to obtain ultrahigh-pressure steam condensate; and performing the heat exchange on the product gas serving as a heat medium and the methanol raw material to obtain the methanol steam and the heat-exchanged product gas. The invention utilizes the product gas to exchange heat with the methanol and utilizes the ultrahigh pressure steam system to supply heat for the methanol cracking reaction, can cancel a large amount of equipment, saves investment and land occupation, and can realize a skid-mounted methanol hydrogen production system by the method.
Description
Technical Field
The application relates to the field of organic chemistry, in particular to a method for preparing hydrogen from methanol and a system for preparing hydrogen from methanol.
Background
The methanol cracking hydrogen production is generally used for hydrogen for industrial use in a factory, and the device scale is small, generally 4000Nm 3 The ratio of the reaction time to the reaction time is less than h. The methanol cracking hydrogen production system comprises a methanol storage tank, a methanol delivery pump, a methanol-water mixing tank, a methanol booster pump, a raw material product preheater, a raw material superheater, a methanol reactor, a water cooler, a heat conducting oil system and a PSA unit. The existing methanol hydrogen production system has more equipment and larger occupied area, and increases the investment.
Disclosure of Invention
The device aims to solve the problems that a methanol hydrogen production system has more devices and occupies a larger area. The present disclosure provides, in a first aspect, a method for producing hydrogen from methanol, the method comprising: the method comprises the following steps of (1) carrying out heat exchange on a methanol raw material to form methanol steam, mixing the methanol steam with medium-pressure steam to obtain mixed steam, and sending the mixed steam into a reactor to carry out methanol cracking reaction to obtain a product gas; enabling ultrahigh-pressure steam to enter the reactor as a heat source for the methanol cracking reaction for heat exchange to obtain ultrahigh-pressure steam condensate; and performing the heat exchange on the product gas serving as a heat medium and the methanol raw material to obtain the methanol steam and the heat-exchanged product gas.
Optionally, the methanol steam and the medium pressure steam are mixed and then enter the tube side of the reactor, and the ultrahigh pressure steam enters the shell side of the reactor.
Optionally, prior to forming the methanol vapor, the method further comprises: boosting the pressure of the methanol raw material to 1-3 MPa, preferably 1.5-2.8 MPa; the temperature of the methanol steam obtained by heat exchange is 100-250 ℃, and preferably 150-220 ℃; the pressure of the medium-pressure steam is 2-4 MPa, preferably 2.5-4 MPa; the temperature of the mixed steam is 250 to 340 ℃, preferably 270 to 290 ℃.
Optionally, the method further comprises: and separating the ultrahigh-pressure steam condensate, returning the obtained balance gas to the shell side of the reactor, and feeding the obtained liquid phase into a medium-pressure steam condensate unit for recycling.
Optionally, sending the ultrahigh-pressure steam condensate to an ultrahigh-pressure steam condensate tank for liquid separation, and sending a liquid phase in the ultrahigh-pressure steam condensate tank to a flash tank for flash evaporation; sending the obtained medium-pressure saturated steam after flashing as the medium-pressure steam to the inlet of the reactor to be mixed with the methanol steam; the pressure of the ultrahigh pressure steam is 5.0-13 MPa, preferably 6.5-12.5 MPa; the inlet temperature and the outlet temperature of the reactor are respectively 200-300 ℃, preferably 270-290 ℃; the pressure of the flash tank is 1.0 to 4.0MPa, preferably 1.5 to 3.0MPa.
Optionally, the method further comprises: cooling the heat-exchanged product gas to 20-80 ℃, preferably 40-45 ℃; the cooling adopts an air cooler and/or a water cooler, and preferably adopts a water cooler; sending the cooled product gas into a hydrogen purification device for hydrogen purification; the hydrogen purification method is selected from one or more of physical adsorption, chemical adsorption, low-temperature separation and PSA, and preferably PSA.
A second aspect of the present disclosure provides a methanol hydrogen production system, which includes a methanol evaporator, a reactor, an ultra-high pressure steam source, and an intermediate pressure steam source; the methanol evaporator comprises a methanol raw material inlet, a methanol steam outlet, a heat medium inlet and a heat medium outlet; the reactor is provided with a raw material inlet, a product gas outlet, a heat medium inlet and a heat medium outlet; a raw material inlet of the reactor is respectively communicated with the medium-pressure steam source and a methanol steam outlet of the methanol evaporator; the product gas outlet of the reactor is communicated with the heat medium inlet of the methanol evaporator; and a heat medium inlet of the reactor is communicated with the ultrahigh pressure gas source.
Optionally, the reactor has a tube side and a shell side, the raw material inlet and the product gas outlet of the reactor are respectively communicated with the tube side, and the heat medium inlet and the heat medium outlet of the reactor are respectively communicated with the shell side.
Optionally, the system further comprises a methanol booster pump, an outlet of the methanol booster pump is communicated with a methanol raw material inlet of the methanol evaporator; the system also comprises a product gas cooling device, wherein the inlet of the product gas cooling device is communicated with the heat medium outlet of the methanol evaporator; the system also comprises a hydrogen purification device, wherein the outlet of the product gas cooling device is communicated with the inlet of the hydrogen purification device; the hydrogen outlet of the hydrogen purification device is communicated with a hydrogen pipe network, and the flare gas outlet of the hydrogen purification device is communicated with a flare; wherein the product gas purification device is selected from a water cooler and/or an air cooler, preferably a water cooler; the hydrogen purification device is selected from a PSA device, a physical adsorption device, a cryogenic separation device and/or a chemical adsorption device, preferably a PSA device.
Optionally, the system further comprises an ultrahigh-pressure vapor condensate tank and a medium-pressure flash tank, wherein an inlet of the ultrahigh-pressure vapor condensate tank is communicated with the heat medium outlet of the reactor, a liquid-phase outlet of the ultrahigh-pressure vapor condensate tank is communicated with an inlet of the medium-pressure flash tank, and a gas-phase outlet of the ultrahigh-pressure vapor condensate tank is communicated with the shell pass of the reactor.
By the technical scheme, the methanol raw material is evaporated by utilizing the product gas of the methanol cracking reaction and is mixed with the steam to the reaction temperature, so that the number of raw material evaporation devices can be reduced; the heat required by the methanol reactor is provided by ultrahigh pressure steam, a liquid phase obtained by condensing the ultrahigh pressure steam is sent to a medium-pressure flash tank, and medium-pressure saturated steam obtained by flash evaporation returns to be mixed with the raw materials. The method can eliminate a methanol storage tank, a raw material superheater and the whole heat conduction oil system, thereby reducing the number of equipment, reducing the occupied area, saving the investment and possibly realizing the skid-mounted methanol hydrogen production device.
Additional features and advantages of the disclosure will be set forth in the detailed description which follows.
Drawings
The accompanying drawings, which are included to provide a further understanding of the disclosure and are incorporated in and constitute a part of this specification, illustrate embodiments of the disclosure and together with the description serve to explain the disclosure, but do not constitute a limitation of the disclosure. In the drawings:
FIG. 1 is a process flow diagram of one embodiment of a methanol to hydrogen process of the present disclosure.
Description of the reference numerals
1. Methanol raw material 2, pressure boosting methanol 3, mixed steam 4, product gas 5, heat exchanged product gas 6, cooled product gas 7, feed gas 8, condensed water 9, hydrogen 10, torch gas 11, medium pressure steam 12, ultrahigh pressure steam 13, ultrahigh pressure steam condensate 14, pressure reducing ultrahigh pressure condensate 15, balance gas 16, medium pressure saturated steam 17 and medium pressure steam condensate;
A. methanol booster pump B, methanol evaporator C, reactor D, water cooler E, liquid separation tank F, PSA G, ultra-high pressure steam condensate tank H, medium pressure flash tank.
Detailed Description
The following describes in detail specific embodiments of the present disclosure. It should be understood that the detailed description and specific examples, while indicating the present disclosure, are given by way of illustration and explanation only, not limitation.
The present disclosure provides a method for producing hydrogen from methanol, comprising: the method comprises the following steps of (1) carrying out heat exchange on a methanol raw material to form methanol steam, mixing the methanol steam with medium-pressure steam to obtain mixed steam, and sending the mixed steam into a reactor to carry out methanol cracking reaction to obtain a product gas; enabling ultrahigh-pressure steam to enter the reactor as a heat source for the methanol cracking reaction for heat exchange to obtain ultrahigh-pressure steam condensate; and performing the heat exchange on the product gas serving as a heat medium and the methanol raw material to obtain the methanol steam and the heat-exchanged product gas.
Through the technical scheme, the methanol is preheated by utilizing the reaction product gas, so that heat loss can be reduced to the greatest extent, and energy and cost are saved. The gasified methanol and the medium-pressure steam are directly mixed to the reaction temperature, so that the number of raw material evaporation devices can be reduced; supplying heat for the methanol cracking reaction by using ultrahigh pressure steam; the product gas after the reaction preheats the methanol, and is sent to a downstream hydrogen purification unit after being cooled by a cooler. The whole heat conduction oil system, the methanol storage tank and the raw material superheater can be eliminated by the invention, wherein the heat conduction oil system comprises a heat conduction oil elevated tank, a heat conduction oil storage tank, a heat conduction oil pump and a heat conduction oil heater; therefore, equipment can be reduced, the occupied land is saved, and the skid-mounted methanol hydrogen production device can be realized most probably.
In a preferred embodiment, the methanol vapor is mixed with the medium pressure vapor and then enters the tube side of the reactor, and the ultrahigh pressure vapor enters the shell side of the reactor. In the preferred embodiment, methanol steam enters the tube side of the reactor after exchanging heat with medium-pressure steam for reaction, and because the hydrogen production by methanol cracking is an endothermic reaction, the tube side is continuously heated to maintain the temperature required by the reaction. Through superhigh pressure steam gets into the shell side of reactor can last the heat supply and can improve heat exchange efficiency for the reaction.
As a preferred embodiment, prior to forming the methanol vapor, the method further comprises: boosting the methanol raw material to 1-3 MPa, preferably 1.5-2.8 MPa by using a methanol booster pump; the temperature of the methanol steam obtained by heat exchange is 100-250 ℃, and preferably 150-220 ℃; the pressure of the medium-pressure steam is 2-4 MPa, preferably 2.5-4 MPa; the temperature of the mixed steam is 250 to 340 ℃, preferably 270 to 290 ℃.
In the preferred embodiment, the methanol after being pressurized exchanges heat with the product gas, and then is mixed with medium-pressure steam for heat exchange to obtain mixed steam, wherein the temperature of the mixed steam is 250-340 ℃, preferably 270-290 ℃, and reaches the temperature condition of the methanol cracking reaction. By the method, heat loss can be further reduced, and cost is saved.
As a preferred embodiment, the method further comprises: and separating the ultrahigh pressure steam condensate, returning the obtained balance gas to the shell pass of the reactor, and sending the obtained liquid phase into a medium pressure steam condensate unit for recycling. Wherein, the medium-pressure steam condensate unit can be conventional for a methanol hydrogen production system.
In a preferred embodiment, the ultrahigh-pressure steam condensate is sent to an ultrahigh-pressure steam condensate tank for liquid separation, and the liquid phase in the ultrahigh-pressure steam condensate tank is sent to a medium-pressure flash tank for flash evaporation; sending the obtained medium-pressure saturated steam after flash evaporation to the inlet of the reactor as the medium-pressure steam to be mixed with the methanol steam, wherein the pressure of the ultrahigh-pressure steam is 5.0-13 MPa, and preferably 6.5-12.5 MPa; the inlet temperature and the outlet temperature of the reactor are respectively 200-300 ℃, preferably 270-290 ℃; the pressure of the flash tank is 1.0 to 4.0MPa, preferably 1.5 to 3.0MPa.
In the preferred embodiment, after the ultrahigh pressure steam is used for supplying heat to the reaction, the reaction enters an ultrahigh pressure steam condensate tank, the condensed liquid is sent to a medium pressure flash tank for flash evaporation, the gas phase returns to be mixed with the raw material methanol, and the liquid phase is sent to a condensate pipe network. The method can fully utilize the heat in the ultrahigh pressure steam, and recycle the condensate formed after the ultrahigh pressure steam is subjected to heat exchange, thereby further improving the logistics and heat utilization efficiency of the system.
As a preferred embodiment, the method further comprises: cooling the heat-exchanged product gas to 20-80 ℃, preferably 40-45 ℃; the cooling adopts an air cooler and/or a water cooler, and preferably adopts a water cooler; sending the cooled product gas into a hydrogen purification device for hydrogen purification; the hydrogen purification method is selected from one or more of physical adsorption, chemical adsorption, low-temperature separation and PSA, and preferably PSA.
In the preferred embodiment, the product gas after heat exchange with methanol enters a water cooler to be cooled to 20-80 ℃, preferably 40-45 ℃ to obtain the product gas after heat exchange, the product gas after heat exchange enters a liquid separation tank, the top gas is sent to a hydrogen purification unit, and the bottom condensed water is sent to a sewage treatment plant. Hydrogen from the top of the PSA is sent to a piping network and flare gas from the bottom is sent to flare. The method can better separate the product gas obtained by the reaction to obtain the hydrogen meeting the use requirement of a pipe network, and both the condensed water and the impurity gas are better treated and have less pollution.
A second aspect of the present disclosure provides a methanol hydrogen production system, which includes a methanol evaporator, a reactor, an ultra-high pressure steam source, and an intermediate pressure steam source; the methanol evaporator comprises a methanol raw material inlet, a methanol steam outlet, a heat medium inlet and a heat medium outlet; the reactor is provided with a raw material inlet, a product gas outlet, a heat medium inlet and a heat medium outlet; a raw material inlet of the reactor is respectively communicated with the medium-pressure steam source and a methanol steam outlet of the methanol evaporator; the product gas outlet of the reactor is communicated with the heat medium inlet of the methanol evaporator; and a heat medium inlet of the reactor is communicated with the ultrahigh pressure gas source.
According to the technical scheme, a raw material inlet of the reactor is respectively communicated with the medium-pressure steam source and a methanol steam outlet of the methanol evaporator, so that the methanol steam and the medium-pressure steam are mixed to obtain mixed steam and then enter the reactor for reaction; a product gas outlet of the reactor is communicated with a heat medium inlet of the methanol evaporator, so that the product gas enters a shell side of the methanol evaporator and further exchanges heat with methanol to change the methanol into methanol steam, and the heat loss can be reduced; and a heat medium inlet of the reactor is communicated with the ultrahigh pressure gas source, so that ultrahigh pressure steam can enter the shell side of the reactor to continuously supply heat for reaction.
As a preferred embodiment, the reactor has a tube side and a shell side, the raw material inlet and the product gas outlet of the reactor are respectively communicated with the tube side, the heat medium inlet and the heat medium outlet of the reactor are respectively communicated with the shell side, so that the methanol steam and the medium-pressure steam are mixed and then enter the tube side of the reactor, and the ultrahigh-pressure steam enters the shell side of the reactor, so as to further improve the heat exchange efficiency. Among them, the reactor is preferably a tubular reactor.
In a preferred embodiment, the system further comprises a methanol booster pump, and an outlet of the methanol booster pump is communicated with a methanol raw material inlet of the methanol evaporator, so that the methanol is pressurized by the methanol booster pump and then sent to the methanol evaporator to exchange heat with the product gas.
In one embodiment, the system further comprises a product gas cooling device, wherein the inlet of the product gas cooling device is communicated with the heat medium outlet of the methanol evaporator, so that the product gas after heat exchange can enter the product gas cooling device for cooling. The product gas cooling device comprises a water cooler and/or a liquid separation tank and is used for cooling the heat-exchanged product gas and then separating the gas into the liquid separation tank, delivering the gas at the top of the liquid separation tank to the PSA device, and delivering the condensed water at the bottom of the liquid separation tank to a sewage treatment plant.
In one embodiment, the system further comprises a hydrogen purification device, wherein an outlet of the product gas cooling device is communicated with an inlet of the hydrogen purification device, so that the cooled product gas enters the hydrogen purification device, and the cooled product gas is further purified to obtain hydrogen which is suitable for a pipe network. The hydrogen outlet of the hydrogen purification device is communicated with a hydrogen pipe network, and the flare gas outlet of the hydrogen purification device is communicated with a flare; wherein the hydrogen purification device is selected from a PSA device, a physical adsorption device, a cryogenic separation device and/or a chemical adsorption device, preferably a PSA device.
As a preferred embodiment, the system further comprises an ultrahigh pressure vapor condensate tank and a medium pressure flash tank, wherein an inlet of the ultrahigh pressure vapor condensate tank is communicated with the heat medium outlet of the reactor, a liquid phase outlet of the ultrahigh pressure vapor condensate tank is communicated with an inlet of the medium pressure flash tank, and a gas phase outlet of the ultrahigh pressure vapor condensate tank is communicated with the shell side of the reactor, so that the balance gas is returned to the shell side of the reactor for continuous heat exchange, and heat loss can be reduced.
In the preferred embodiment, the system is connected with the device in the system, and is used for separating the ultrahigh-pressure steam condensate in the ultrahigh-pressure steam condensate tank, returning the balance line steam to the reactor, sending the liquid in the ultrahigh-pressure steam condensate tank to the medium-pressure flash tank for flash evaporation, sending the gas after flash evaporation to the reactor, and sending the condensate at the bottom of the flash tank to the medium-pressure steam condensate unit for reuse, so that the cost is further saved.
The present disclosure is further illustrated by the following examples. The raw materials used in the examples are all available from commercial sources.
In a preferred embodiment of the present disclosure, as shown in fig. 1, the methanol hydrogen production method comprises the steps of:
the methanol raw material enters the device and is boosted to 1-3 MPa, preferably 1.5-2.8 MPa by a methanol booster pump A. The mixed steam 3 with the temperature of 250-340 ℃ is obtained after heat exchange with the product gas 4 to 100-250 ℃ through a methanol evaporator B and is mixed with the medium-pressure steam 11, the temperature is preferably 270-290 ℃, the mixed steam enters a reactor C to carry out methanol cracking reaction, in order to maintain the heat required by the reaction, ultrahigh-pressure steam 12 enters the shell side of the reactor C, and the ultrahigh-pressure steam pressure is 5-13 MPa, preferably 6.5-12.5 MPa. The ultrahigh pressure steam condensate 13 enters an ultrahigh pressure steam condensate tank G, the balance gas 15 returns to the reactor C, the liquid phase enters a medium pressure flash tank H, and the medium pressure flash pressure is 1.0-4.0 MPa, preferably 1.5-3.0 MPa. The top medium-pressure saturated steam 16 returns to the inlet of the reactor C, and the medium-pressure steam condensate 17 enters a medium-pressure steam condensate pipe network. And (3) the product gas 4 from the reactor C exchanges heat with the pressure-boosting methanol 2, enters a water cooler D and is cooled to 80-20 ℃, preferably 45-30 ℃, the cooled product gas 6 enters a liquid separation tank E, the top feeding gas 7 is sent to a PSA unit F, the condensed water 8 is sent to a sewage treatment plant, the hydrogen 9 from the top of the PSA unit F is sent to a pipe network, and the flare gas 10 from the bottom is sent to a flare.
In the embodiment, the method for preparing hydrogen can reduce heat loss to the maximum extent and save energy and cost. In addition, the whole heat conduction oil system, the methanol storage tank and the raw material superheater can be eliminated through the invention, so that the equipment can be reduced, the occupied area is saved, and the skid-mounted methanol hydrogen production device can be realized most probably.
The preferred embodiments of the present disclosure have been described in detail above, however, the present disclosure is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present disclosure within the technical idea of the present disclosure, and these simple modifications all fall within the protection scope of the present disclosure.
It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. To avoid unnecessary repetition, the disclosure does not separately describe various possible combinations.
In addition, any combination of various embodiments of the present disclosure may be made, and the same should be considered as the disclosure of the present disclosure, as long as it does not depart from the spirit of the present disclosure.
Claims (10)
1. A method for producing hydrogen from methanol, the method comprising:
the method comprises the following steps of (1) carrying out heat exchange on a methanol raw material to form methanol steam, mixing the methanol steam with medium-pressure steam to obtain mixed steam, and sending the mixed steam into a reactor to carry out methanol cracking reaction to obtain a product gas;
enabling ultrahigh-pressure steam to serve as a heat source of the methanol cracking reaction to enter the reactor for heat exchange to obtain ultrahigh-pressure steam condensate;
and performing the heat exchange on the product gas serving as a heat medium and the methanol raw material to obtain the methanol steam and the heat-exchanged product gas.
2. The process of claim 1, wherein the methanol vapor is mixed with the medium pressure vapor and enters the tube side of the reactor, and the ultra-high pressure vapor enters the shell side of the reactor.
3. The method of claim 1, further comprising, prior to forming the methanol vapor: boosting the pressure of the methanol raw material to 1-3 MPa, preferably 1.5-2.8 MPa;
the temperature of the methanol steam obtained by heat exchange is 100-250 ℃, and preferably 150-220 ℃;
the pressure of the medium-pressure steam is 2-4 MPa, preferably 2.5-4 MPa;
the temperature of the mixed steam is 250-340 ℃, preferably 270-290 ℃.
4. The method of claim 1, further comprising: and separating the ultrahigh pressure steam condensate, returning the obtained balance gas to the shell pass of the reactor, and sending the obtained liquid phase into a medium pressure steam condensate unit for recycling.
5. The method according to claim 4, characterized in that the ultrahigh pressure steam condensate is sent to an ultrahigh pressure steam condensate tank for liquid separation, and the liquid phase in the ultrahigh pressure steam condensate tank is sent to a medium-pressure flash tank for flash evaporation; sending the obtained medium-pressure saturated steam after flashing as the medium-pressure steam to the inlet of the reactor to be mixed with the methanol steam;
the pressure of the ultrahigh pressure steam is 5.0-13 MPa, preferably 6.5-12.5 MPa;
the outlet temperature and the inlet temperature of the reactor are respectively 200-300 ℃, preferably 270-290 ℃;
the pressure of the medium-pressure flash tank is 1.0-4.0 MPa, preferably 1.5-3.0 MPa.
6. The method of claim 1, further comprising: cooling the heat-exchanged product gas to 20-80 ℃, preferably 40-45 ℃; the cooling adopts an air cooler and/or a water cooler, and preferably adopts a water cooler;
optionally, the method further comprises feeding the cooled product gas to a hydrogen purification device for hydrogen purification;
the hydrogen purification method is selected from one or more of physical adsorption, chemical adsorption, low-temperature separation and PSA, and PSA is preferred.
7. A methanol hydrogen production system is characterized by comprising a methanol evaporator, a reactor, an ultrahigh pressure steam source and an intermediate pressure steam source;
the methanol evaporator comprises a methanol raw material inlet, a methanol steam outlet, a heat medium inlet and a heat medium outlet;
the reactor is provided with a raw material inlet, a product gas outlet, a heat medium inlet and a heat medium outlet; a raw material inlet of the reactor is respectively communicated with the medium-pressure steam source and a methanol steam outlet of the methanol evaporator; the product gas outlet of the reactor is communicated with the heat medium inlet of the methanol evaporator; and a heat medium inlet of the reactor is communicated with the ultrahigh pressure gas source.
8. The methanol hydrogen production system according to claim 7, wherein the reactor has a tube side and a shell side, the raw material inlet and the product gas outlet of the reactor are respectively communicated with the tube side, and the heat medium inlet and the heat medium outlet of the reactor are respectively communicated with the shell side.
9. The system for producing hydrogen from methanol as claimed in claim 8, further comprising a methanol booster pump, wherein the outlet of the methanol booster pump is communicated with the methanol raw material inlet of the methanol evaporator;
optionally, the system further comprises a product gas cooling device, an inlet of the product gas cooling device is communicated with the heat medium outlet of the methanol evaporator;
optionally, the system further comprises a hydrogen purification device, wherein the outlet of the product gas cooling device is communicated with the inlet of the hydrogen purification device; the hydrogen outlet of the hydrogen purification device is communicated with a hydrogen pipe network, and the torch gas outlet of the hydrogen purification device is communicated with a torch;
wherein the product gas purification device is selected from a water cooler and/or an air cooler, preferably a water cooler; the hydrogen purification device is selected from a PSA device, a physical adsorption device, a cryogenic separation device and/or a chemical adsorption device, preferably a PSA device.
10. The system for producing hydrogen from methanol according to claim 7, further comprising an ultrahigh-pressure vapor condensate tank and a medium-pressure flash tank, wherein an inlet of the ultrahigh-pressure vapor condensate tank is communicated with a heat medium outlet of the reactor, a liquid-phase outlet of the ultrahigh-pressure vapor condensate tank is communicated with an inlet of the medium-pressure flash tank, and a gas-phase outlet of the ultrahigh-pressure vapor condensate tank is communicated with a shell pass of the reactor.
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| CN112209339A (en) * | 2020-08-18 | 2021-01-12 | 广东醇氢新能源研究院有限公司 | Method for preparing hydrogen by cracking methanol |
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