Prying block type methanol cracking hydrogen production device

Abstract

The utility model discloses a skid-mounted methanol cracking hydrogen production device which comprises a support, and a storage tank mechanism, a methanol cracking conversion mechanism and a hydrogen extraction adsorption mechanism are arranged on the support. The methanol cracking conversion mechanism comprises a methanol head tank communicated with the storage tank mechanism, a circulating liquid tank communicated with the methanol head tank through a first pipeline, a mixer communicated with the first pipeline, a heat exchanger communicated with the mixer, and a vaporization superheater and a cooler which are communicated with the heat exchanger; the converter is communicated with a gas outlet of the vaporization superheater, the washing tower is communicated with an outlet of the cooler, the converter is communicated with the heat exchanger, a gas outlet of the washing tower is communicated with the hydrogen extraction adsorption mechanism, a desalted water conveying pipeline is arranged on the circulating liquid tank, and three first conveying pumps are arranged between the first pipeline and the mixer in parallel; the vaporization superheater and the converter are connected in series with an external heat-conducting oil furnace through a heat-conducting oil pipeline; and a washing water pipe and a return pipe are arranged between the washing tower and the circulating liquid tank. The skid-mounted device can be used for skid-mounting a methanol cracking hydrogen production device, and is convenient to transport.

Description

TECHNICAL FIELD

[0001] The utility model relates to a kind of methanol cracking hydrogen production devices, especially a kind of pry block type methanol cracking hydrogen production device. BACKGROUND

[0002] Traditional methanol cracking hydrogen production equipment generally sends each component and container to site, utilizes the container foundation that customer does in advance to carry out positioning, installation is carried out in site, generally needs 2-3 months, installation cycle is long, quality control is difficult in site installation, high in cost, high to installation personnel requirement, and it is not suitable for moving machine, simultaneously, traditional methanol cracking device converter heating is using natural gas, which requires that customer site must have natural gas. CONTENT OF UTILITY MODEL

[0003] The utility model aims at overcoming the insufficient prior art and provides a pry block type methanol cracking hydrogen production device, solves the problems of traditional methanol cracking hydrogen production device structure dispersion, installation difficulty and inability to transport integrally.

[0004] To achieve the above-mentioned purpose, the utility model adopts the technical scheme of a pry block type methanol cracking hydrogen production device, including support and centralized control mechanism, the support is sequentially pryed and installed with storage tank mechanism, methanol cracking conversion mechanism and hydrogen extraction adsorption mechanism according to the process sequence of hydrogen production, the centralized control mechanism remotely controls storage tank mechanism, methanol cracking conversion mechanism and hydrogen extraction adsorption mechanism, the methanol cracking conversion mechanism includes methanol high tank communicated with storage tank mechanism, circulating liquid tank communicated with methanol high tank through first pipeline, first conveying pump group arranged on first pipeline, second pipeline communicated with the outlet end of first conveying pump group, mixer communicated with second pipeline, heat exchanger communicated with the outlet of mixer, vaporization superheater and cooler communicated with the gas outlet of heat exchanger, converter communicated with the gas outlet of vaporization superheater and washing tower communicated with the outlet of cooler, the gas outlet of converter is communicated with heat exchanger, catalyst is arranged in the converter, the gas outlet of washing tower is communicated with hydrogen extraction adsorption mechanism, desalted water conveying pipeline is arranged on circulating liquid tank, cooling water inlet pipe and cooling water outlet pipe are externally connected on cooler, the first conveying pump group includes three first conveying pumps arranged in parallel between first pipeline and second pipeline, first valve and second valve are respectively arranged on first pipeline between every two first conveying pumps, vaporization superheater and converter are externally connected heat conduction oil furnace through heat conduction oil pipeline in series, washing water pipe and reflux pipe are arranged between washing tower and circulating liquid tank, second conveying pump group is arranged on washing water pipe, and the second conveying pump group includes two second conveying pumps arranged in parallel.

[0005] Further, the storage mechanism comprises a methanol tank body, a feed pipe communicated with the top of the tank body, a discharge pipe communicated with the bottom of the tank body, a conveying pipeline communicated with the feed pipe and the methanol high tank, a reflux circulation mechanism and a cooling mechanism. The reflux circulation mechanism comprises a fifth pipeline, a sixth pipeline and a seventh pipeline arranged in parallel between the feed pipe and the discharge pipe. One end of the discharge pipe is arranged at the bottom of the tank body, and the other end is communicated with the feed pipe. The third conveying pump is arranged on the sixth pipeline and the seventh pipeline. The conveying pipeline is arranged on the feed pipe between the sixth pipeline and the seventh pipeline. The third valve is arranged on the discharge pipe between the fifth pipeline and the sixth pipeline. The first raw material pipe is arranged on the discharge pipe between the fifth pipeline and the third valve. The fourth valve is arranged on the feed pipe between the fifth pipeline and the sixth pipeline. The fifth valve is arranged on the discharge pipe between the tank body and the fifth pipeline.

[0006] Further, the adsorption mechanism comprises a gas-liquid separation buffer tank communicated with the washing tower, five adsorption towers arranged in parallel, and a hydrogen buffer tank. Each adsorption tower is provided with a gas outlet pipe at the top and a gas inlet pipe at the bottom. The second raw material pipe and the reverse discharge pipe are arranged on the gas inlet pipe. The sixth valve is arranged on the second raw material pipe. The seventh valve is arranged on the reverse discharge pipe. The one pressure reduction pipe, the second pressure reduction pipe, the third pressure reduction pipe and the first gas pipe are arranged in parallel on the gas outlet pipe. The pressure equalizing valve is arranged on each of the one pressure reduction pipe, the second pressure reduction pipe and the third pressure reduction pipe. The eighth valve is arranged on the first gas pipe. The first communication pipeline, the second communication pipeline, the third communication pipeline and the fourth communication pipeline are further arranged on the support. The first communication pipeline is communicated with the one pressure reduction pipe. The second communication pipeline is communicated with the second pressure reduction pipe. The third communication pipeline is communicated with the third pressure reduction pipe. The fourth communication pipeline is communicated with the first gas pipe. The tail end of the fourth communication pipeline is communicated with the gas inlet of the hydrogen buffer tank. The fifth communication pipeline and the sixth communication pipeline are further arranged at the lower part of the support. The fifth communication pipeline is communicated with the raw material pipe. The sixth communication pipeline is communicated with the reverse discharge pipe. The fifth communication pipeline is communicated with the gas outlet of the gas-liquid separation buffer tank. The tail end of the sixth communication pipeline is provided with a gas discharge port. The product gas pipe is arranged at the gas outlet of the hydrogen buffer tank.

[0007] Further, the heat exchanger is provided with the third pipeline and the fourth pipeline. The third pipeline is communicated with the bottom of the vaporization superheater. The fourth pipeline is communicated with the middle part of the vaporization superheater.

[0008] Further, the three first conveying pumps in the first conveying pump group are divided into the methanol pumping pump, the desalted water pumping pump and the standby pump according to the division of work. The first conveying pump and the second conveying pump adopt the metering booster pump.

[0009] Further, the methanol high tank and the circulating liquid tank are each provided with a breather valve at the top.

[0010] Further, the methanol high tank and the circulating liquid tank are provided with liquid level monitoring sensors.

[0011] Further, a raw material liquid metering pump is arranged between the storage tank mechanism and the methanol high tank.

[0012] Further, a desalted water metering pump is arranged on the desalted water conveying pipeline.

[0013] Further, the catalyst is a copper-based catalyst.

[0014] The pry block type methanol cracking hydrogen production device provided by the utility model has the pry block type structure, the pry blocks are in butt joint, can be assembled in a factory in advance and then shipped, is easy to control quality, can save 1 / 4 cost of the whole set of equipment, is obviously economical, can meet the needs of customers for relocation at any time, realizes circulation backflow in the pipeline of the storage tank mechanism, avoids excessive pumping, the methanol cracking conversion mechanism can directly use methanol to heat the vaporization superheater and the converter to rise temperature, so that the customer can avoid no natural gas source on site, and the five adsorption towers of the hydrogen extraction adsorption mechanism can maximize the hydrogen recovery rate. BRIEF DESCRIPTION OF DRAWINGS

[0015] The technical scheme of the utility model will be further described below with reference to the drawings:

[0016] Figure 1 The pry block type methanol cracking hydrogen production device provided by the utility model has the structure schematic view.

[0017] Figure 2 The methanol cracking conversion mechanism has the structure schematic view.

[0018] Figure 3 The methanol cracking conversion mechanism has the process flow chart.

[0019] Figure 4 The storage tank mechanism has the structure schematic view.

[0020] Figure 5 The hydrogen extraction adsorption mechanism has the structure schematic view.

[0021] Wherein: 1, support; 2, storage tank mechanism; 3, methanol cracking conversion mechanism; 4, hydrogen extraction adsorption mechanism; 5, methanol high tank; 6, first pipeline; 7, circulating liquid tank; 8, second pipeline; 9, mixer; 10, heat exchanger; 11, vaporization superheater; 12, cooler; 13, converter; 14, washing tower; 15, desalted water delivery pipeline; 16, cooling water inlet pipe; 17, cooling water outlet pipe; 18, first delivery pump; 19, first valve; 20, second valve; 21, heat conducting oil pipeline; 22, washing water pipe; 23, second delivery pump; 24, third pipeline; 25, fourth pipeline; 26, breather valve; 27, raw material liquid metering pump; 28, desalted water metering pump; 29, return pipe; 201, methanol tank body; 202, feed pipe; 203, discharge pipe; 204, delivery pipeline; 205, fifth pipeline; 206, sixth pipeline; 207, seventh pipeline; 208, third delivery pump; 209, fourth valve; 210, first raw material pipe; 211, fifth valve; 212, nitrogen filling mechanism; 401, vapor-liquid separation buffer tank; 402, adsorption tower; 403, hydrogen buffer tank; 404, gas outlet pipe; 405, gas inlet pipe; 406, second raw material pipe; 407, reverse discharge pipe; 408, sixth valve; 409, seventh valve; 410, one equal pressure reducing pipe; 411, two equal pressure reducing pipes; 412, three equal pressure reducing pipes; 413, first gas pipe; 414, equalizing valve; 415, eighth valve; 416, first communication pipeline; 417, second communication pipeline; 418, third communication pipeline; 419, fourth communication pipeline; 420, fifth communication pipeline; 421, sixth communication pipeline; 422, gas discharge port. DETAILED DESCRIPTION

[0022] In order to make the person skilled in the art better understand the scheme of the present application, the technical scheme in the embodiments of the present application will be described clearly and completely below in conjunction with the drawings in the embodiments of the present application. Obviously, the described embodiments are only a part of the embodiments of the present application, rather than all the embodiments. Based on the embodiments in the present application, all other embodiments obtained by the person skilled in the art without creative labor should belong to the protection scope of the present application.

[0023] The designer of the utility model in view of the demand of methanol cracking hydrogen production device, innovatively proposed a pry block type methanol cracking hydrogen production device, all mechanisms of methanol cracking hydrogen production can be pryed together, convenient transportation.

[0024] As Figures 1 to 5The pry block type methanol cracking hydrogen production device shown, including support 1 and control mechanism, the support 1 according to the process sequence of hydrogen production is sequentially pry installed with storage tank mechanism 2, methanol cracking conversion mechanism 3 and hydrogen extraction adsorption mechanism 4, the control mechanism remotely controls storage tank mechanism 2, methanol cracking conversion mechanism 3 and hydrogen extraction adsorption mechanism 4, the methanol cracking conversion mechanism 3 includes methanol high tank 5 communicated with storage tank mechanism 2, circulating liquid tank 7 communicated with methanol high tank 5 through first pipeline 6, first delivery pump group arranged on the first pipeline 6, second pipeline 8 communicated with the outlet end of the first delivery pump group, mixer 9 communicated with the second pipeline 8, heat exchanger 10 communicated with the outlet of the mixer 9, vaporization superheater 11 and cooler 12 communicated with the gas outlet of the heat exchanger 10, converter 13 communicated with the gas outlet of the vaporization superheater 11 and scrubbing tower 14 communicated with the outlet of the cooler 12, the gas outlet of the converter 13 is communicated with the heat exchanger 10, the converter 13 is provided with a catalyst, the gas outlet of the scrubbing tower 14 is communicated with the hydrogen extraction adsorption mechanism 4, the circulating liquid tank 7 is provided with desalted water delivery pipeline 15, the cooler 12 is externally connected with cooling water inlet pipe 16 and cooling water outlet pipe 17, the first delivery pump group includes three first delivery pumps 18 arranged in parallel between the first pipeline 6 and the second pipeline 8, the first pipeline 6 is provided with first valve 19 and second valve 20 between the three first delivery pumps 18 respectively, the vaporization superheater 11 and the converter 13 are connected in series through heat conducting oil pipeline 21 to form a heating circulation system, the heat conducting oil furnace is fueled by methanol, the temperature of the heat conducting oil in the heat conducting oil pipe can reach 200-300 DEG C, the scrubbing tower 14 and the circulating liquid tank 7 are provided with scrubbing water pipe 22 and reflux pipe 29, the scrubbing water pipe 22 is arranged on the upper part of the scrubbing tower 14, the reflux pipe 29 is arranged at the bottom of the scrubbing tower 14, the scrubbing water pipe 22 is provided with second delivery pump 23 group, the second delivery pump 23 group includes two second delivery pumps 23 arranged in parallel.

[0025] The tank mechanism 2 comprises a methanol tank body 201, a feed pipe 202 communicating with the top of the methanol tank body 201, a discharge pipe 203 communicating with the bottom of the methanol tank body 201, a conveying pipe 204 connecting the feed pipe 202 and the methanol high tank 5, a backflow circulation mechanism and a cooling mechanism. The backflow circulation mechanism comprises a fifth pipe 205, a sixth pipe 206 and a seventh pipe 207 arranged in parallel between the feed pipe 202 and the discharge pipe 203. One end of the discharge pipe 203 is arranged at the bottom of the methanol tank body 201, and the other end communicates with the feed pipe 202. The sixth pipe 206 and the seventh pipe 207 are provided with a third conveying pump 208. The conveying pipe 204 is arranged on the feed pipe 202 between the sixth pipe 206 and the seventh pipe 207. A third valve is arranged on the discharge pipe 203 between the fifth pipe 205 and the sixth pipe 206. A first raw material pipe 210 is arranged on the discharge pipe 203 between the fifth pipe 205 and the third valve. A fourth valve 209 is arranged on the feed pipe 202 between the fifth pipe 205 and the sixth pipe 206. A fifth valve 211 is arranged on the discharge pipe 203 between the methanol tank body 201 and the fifth pipe 205. A breather valve is arranged at the top of the methanol tank body 201. A nitrogen charging mechanism 212 is arranged at the top of the methanol tank body 201. Nitrogen charging at the top of the methanol tank body 201 can avoid methanol evaporation.

[0026] The adsorption mechanism comprises a vapor-liquid separation buffer tank 401 communicated with the washing tower 14, five adsorption towers 402 arranged in parallel, and a hydrogen buffer tank 403, each of the adsorption towers 402 is provided with a gas outlet pipe 404 at the top and a gas inlet pipe 405 at the bottom, the gas inlet pipe 405 is provided with a second raw material pipe 406 and a reverse discharge pipe 407, the second raw material pipe 406 is provided with a sixth valve 408, the reverse discharge pipe 407 is provided with a seventh valve 409, the gas outlet pipe 404 is provided with a first pressure reducing pipe 410, a second pressure reducing pipe 411, a third pressure reducing pipe 412 and a first gas pipe 413 in parallel, each of the first pressure reducing pipe 410, the second pressure reducing pipe 411 and the third pressure reducing pipe 412 is provided with a pressure equalizing valve 414, the first gas pipe 413 is provided with an eighth valve 415, the bracket 1 is further provided with a first communication pipeline 416, a second communication pipeline 417, a third communication pipeline 418 and a fourth communication pipeline 419, the first communication pipeline 416 is communicated with the first pressure reducing pipe 410, the second communication pipeline 417 is communicated with the second pressure reducing pipe 411, the third communication pipeline 418 is communicated with the third pressure reducing pipe 412, and the fourth communication pipeline 419 is communicated with the first gas pipe 413, the tail end of the fourth communication pipeline 419 is communicated with the gas inlet of the hydrogen buffer tank 403, the lower part of the bracket 1 is further provided with a fifth communication pipeline 420 and a sixth communication pipeline 421, the fifth communication pipeline 420 is communicated with the raw material pipe, and the sixth communication pipeline 421 is communicated with the reverse discharge pipe 407, the fifth communication pipeline 420 is communicated with the gas outlet of the vapor-liquid separation buffer tank 401, the tail end of the sixth communication pipeline 421 is provided with a gas discharge port 422, and the gas outlet of the hydrogen buffer tank 403 is provided with a product gas pipe.

[0027] The heat exchanger 10 is provided with a third pipeline 24 and a fourth pipeline 25, the third pipeline 24 is communicated with the bottom of the vaporization superheater 11, and the fourth pipeline 25 is communicated with the middle part of the vaporization superheater 11.

[0028] The three first conveying pumps 18 in the first conveying pump group are divided into a methanol pump, a desalted water pump and a standby pump according to the division of work, and the first conveying pump 18 and the second conveying pump 23 adopt a metering booster pump.

[0029] The methanol high tank 5 and the circulating liquid tank 7 are each provided with a breather valve 26 at the top.

[0030] The methanol high tank 5 and the circulating liquid tank 7 are provided with a liquid level monitoring sensor, which can monitor that the liquid in the methanol high tank 5 or the circulating liquid tank 7 maintains a certain height.

[0031] The raw material liquid metering pump 27 is arranged between the storage tank mechanism 2 and the methanol high tank 5.

[0032] The desalted water metering pump 28 is arranged on the desalted water conveying pipeline 15.

[0033] The catalyst uses a copper-based catalyst.

[0034] When the tank is filled, the third valve and the fourth valve 209 are opened, the fifth valve 211 is closed, and the third delivery pump 208 is started. Methanol enters the feed pipe 202 through the third delivery pump 208 from the raw material pipe, and enters the tank through the feed pipe 202, and the capacity of methanol in the tank is monitored by the first liquid level sensor and the second liquid level sensor.

[0035] When the tank delivers to the methanol high tank 5, the third valve, the fourth valve 209 and the fifth valve 211 are opened, and the third delivery pump 208 is started. Methanol enters the feed pipe 202 through the third delivery pump 208 from the discharge pipe 203, and enters the delivery pipeline 204 through the feed pipe 202 to the methanol high tank 5, at the same time, the excess methanol in the feed pipe 202 is returned to the discharge pipe 203 through the fifth pipeline 205, and the methanol is supplemented and circulated by the discharge pipe 203.

[0036] The methanol entering the methanol high tank 5 is pumped into the mixer 9 by the first delivery pump group, at the same time, the desalted water is delivered into the circulating liquid tank 7 by the desalted water delivery pipeline 15, and the desalted water is pumped into the mixer 9 from the circulating liquid tank 7 by the first delivery pump group after mixing with methanol, and then delivered into the heat exchanger 10 to be heated to 200 degrees to vaporize, the vaporized gas is further heated to 250-300 degrees to vaporize in the vaporization superheater 11, enters the converter 13 to react with the catalyst to generate 24% carbon dioxide, 75% hydrogen mixed gas and unreacted mixed gas, the mixed gas in the converter 13 enters the heat exchanger 10 to exchange heat and cool down, the cooled mixed gas further enters the cooler 12 to cool down, and the cooled mixed gas enters the washing tower 14, at the same time, the second delivery pump 23 pumps the desalted water from the circulating liquid tank 7 into the washing tower 14 to wash the mixed gas, washes out the unreacted mixed gas in the mixed gas and discharges the carbon dioxide and hydrogen mixed gas into the pressure swing adsorption hydrogen extraction mechanism, and the excess desalted water in the washing tower 14 is returned to the circulating liquid tank 7 through the return pipe 29.

[0037] The carbon dioxide and hydrogen mixed gas after being cleaned by the washing tower 14 enters a vapor-liquid separation buffer tank 401 through a feed port, and enters a second raw material pipe 406 through a fifth communication pipe 420 and finally enters the adsorption tower 402, the mixed gas selectively adsorbs some components in the mixed gas by changing the pressure through the filler in the adsorption tower 402, and separates hydrogen from the mixture, when the pressure in the adsorption tower 402 reaches a certain limit, the pressure needs to be released slowly, the oxygen adsorbed by the adsorbent is desorbed, so that the adsorbent regains the adsorption capacity, the tail gas after the pressure relief is discharged through the tower bottom reverse pipe 407, and is treated or directly discharged into the atmosphere, in order to release the adsorbed substances in the adsorbent, the pressure of the adsorption tower 402 needs to be reduced to a very low level, after desorption, the adsorption tower 402 needs to be flushed once to remove the residual adsorbent and adsorbed substances in the adsorption tower 402, the flushing is usually carried out by using a fluid which does not react with the adsorbent, after flushing, the adsorption tower 402 needs to be regenerated to make the adsorption tower 402 regain the adsorption capacity, regeneration usually includes exposing the adsorbent to appropriate temperature and pressure to completely remove the adsorbed substances in the adsorbent, the regenerated adsorbent can be converted into adsorption after pressure equalization and product pressure rise; after regeneration, the adsorption tower 402 returns to the initial working state and is ready for the next adsorption cycle, when the device is working, one of the five adsorption towers 402 is in the process of pressure equalization adsorption, so that the mixed gas enters the hydrogen buffer tank 403 through the secondary pressure equalization adsorption, the five adsorption towers 402 are used alternately, so that the purpose of continuous separation of air to produce hydrogen is achieved, and the hydrogen after adsorption enters the hydrogen buffer tank 403 for buffering and storage and is discharged from the product gas pipe.

[0038] The methanol cracking hydrogen production device provided by the utility model adopts a pry block structure, pry block butt joint, can be assembled in a factory in advance, is easy to control quality, can save 1 / 4 cost of the whole set of equipment, is obviously economical, can meet the needs of customers for relocation at any time, realizes circulation reflux in the pipeline of the storage tank mechanism, avoids too much pumping, and the methanol cracking conversion mechanism can directly use methanol to heat the vaporizer and the converter to avoid the absence of natural gas sources on site of customers, and the five adsorption towers of the hydrogen extraction adsorption mechanism can maximize the hydrogen recovery rate.

[0039] The above-described embodiments are merely used to illustrate the technical solutions of the present application, rather than limit the present application; although the present application has been described in detail with reference to the foregoing embodiments, those skilled in the art should understand that: the technical solutions recorded in the foregoing embodiments can still be modified, or some technical features can be replaced equivalently; and these modifications or replacements do not make the essence of the corresponding technical solutions deviate from the spirit and scope of the technical solutions of the embodiments of the present application.

Claims

1. A pry block type methanol cracking hydrogen production device comprising a support and a centralized control mechanism, characterized in that, The rack is sequentially provided with a storage tank mechanism, a methanol cracking conversion mechanism and a hydrogen extraction adsorption mechanism according to the hydrogen production process sequence, a centralized control mechanism remotely controls the storage tank mechanism, the methanol cracking conversion mechanism and the hydrogen extraction adsorption mechanism, the methanol cracking conversion mechanism comprises a methanol high tank in communication with the storage tank mechanism, a circulating liquid tank in communication with the methanol high tank through a first pipeline, a first delivery pump group arranged on the first pipeline, a second pipeline in communication with the outlet end of the first delivery pump group, a mixer in communication with the second pipeline, a heat exchanger in communication with the outlet of the mixer, a vaporization superheater and a cooler in communication with the gas outlet of the heat exchanger, a converter in communication with the gas outlet of the vaporization superheater and a scrubbing tower in communication with the outlet of the cooler, the gas outlet of the converter is in communication with the heat exchanger, a catalyst is arranged in the converter, the gas outlet of the scrubbing tower is in communication with the hydrogen extraction adsorption mechanism, a desalted water delivery pipeline is arranged on the circulating liquid tank, a cooling water inlet pipeline and a cooling water outlet pipeline are externally connected to the cooler, the first delivery pump group comprises three first delivery pumps arranged in parallel between the first pipeline and the second pipeline, first valves and second valves are respectively arranged on the first pipeline between the three first delivery pumps, the vaporization superheater and the converter are externally connected to a heat conduction oil furnace through a heat conduction oil pipeline in series, a scrubbing water pipeline and a reflux pipeline are arranged between the scrubbing tower and the circulating liquid tank, a second delivery pump group is arranged on the scrubbing water pipeline, and the second delivery pump group comprises two second delivery pumps arranged in parallel.

2. The prizing methanol cracking hydrogen production device of claim 1, wherein: The storage tank mechanism comprises a methanol tank body, a feed pipe in communication with the top of the tank body, a discharge pipe in communication with the bottom of the tank body, a delivery pipeline in communication with the feed pipe and the methanol high tank, a reflux circulation mechanism and a cooling mechanism, the reflux circulation mechanism comprises a fifth pipeline, a sixth pipeline and a seventh pipeline arranged in parallel between the feed pipe and the discharge pipe, one end of the discharge pipe is arranged at the bottom of the tank body, and the other end is in communication with the feed pipe, third delivery pumps are arranged on the sixth pipeline and the seventh pipeline, the delivery pipeline is arranged on the feed pipe between the sixth pipeline and the seventh pipeline, a third valve is arranged on the discharge pipe between the fifth pipeline and the sixth pipeline, a first raw material pipe is arranged on the discharge pipe between the fifth pipeline and the third valve, a fourth valve is arranged on the feed pipe between the fifth pipeline and the sixth pipeline, and a fifth valve is arranged on the discharge pipe between the tank body and the fifth pipeline.

3. The prizing methanol cracking hydrogen generator of claim 1, wherein: The adsorption mechanism comprises a vapor-liquid separation buffer tank communicated with the washing tower, five adsorption towers arranged in parallel, and a hydrogen buffer tank, each adsorption tower is provided with a gas outlet pipe at the top and a gas inlet pipe at the bottom, the gas inlet pipe is provided with a second raw material pipe and a reverse discharge pipe, the second raw material pipe is provided with a sixth valve, the reverse discharge pipe is provided with a seventh valve, the gas outlet pipe is provided with a first gas pipe, a first pressure reduction pipe, a second pressure reduction pipe and a third pressure reduction pipe in parallel, each of the first pressure reduction pipe, the second pressure reduction pipe and the third pressure reduction pipe is provided with a pressure equalizing valve, the first gas pipe is provided with an eighth valve, the support is further provided with a first communication pipeline, a second communication pipeline, a third communication pipeline and a fourth communication pipeline, the first communication pipeline is communicated with the first pressure reduction pipe, the second communication pipeline is communicated with the second pressure reduction pipe, the third communication pipeline is communicated with the third pressure reduction pipe, and the fourth communication pipeline is communicated with the first gas pipe, the tail end of the fourth communication pipeline is communicated with the hydrogen buffer tank gas inlet, the lower part of the support is further provided with a fifth communication pipeline and a sixth communication pipeline, the fifth communication pipeline is communicated with the raw material pipe, and the sixth communication pipeline is communicated with the reverse discharge pipe, the fifth communication pipeline is communicated with the vapor-liquid separation buffer tank gas outlet, the tail end of the sixth communication pipeline is provided with a gas discharge port, and the hydrogen buffer tank gas outlet is provided with a product gas pipe.

4. The prizing methanol cracking hydrogen generator of claim 1, wherein: The heat exchanger is provided with a third pipeline and a fourth pipeline, the third pipeline is communicated with the bottom of the vaporization superheater, and the fourth pipeline is communicated with the middle part of the vaporization superheater.

5. The prizing methanol cracking hydrogen generator of claim 1, wherein: The three first conveying pumps in the first conveying pump group are divided into methanol pumps, desalted water pumps and standby pumps according to the division of work, and the first conveying pump and the second conveying pump adopt metering booster pumps.

6. The prizing methanol cracking hydrogen generation device of claim 1, wherein: The methanol high tank and the circulating liquid tank are each provided with a breathing valve at the top.

7. The prizing methanol cracking hydrogen generation device of claim 1, wherein: The methanol high tank and the circulating liquid tank are provided with liquid level monitoring sensors.

8. The prizing methanol cracking hydrogen generator of claim 1, wherein: A raw material liquid metering pump is arranged between the storage tank mechanism and the methanol high tank.

9. The prizing methanol cracking hydrogen generator of claim 1, wherein: A desalted water metering pump is arranged on the desalted water conveying pipeline.

10. The prizing methanol cracking hydrogen generator of claim 1, wherein: The catalyst adopts a copper-based catalyst.

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