CN213294670U - Catalytic heating coupling methanol hydrogen production system - Google Patents
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Abstract
The utility model discloses a catalytic heating coupling methanol hydrogen production system, which solves the defects that the prior methanol hydrogen production system uses two catalytic burners, so that the equipment occupies large area, the cost is high, and the heat efficiency utilization rate is low, and comprises a catalytic oxidation reactor, wherein the catalytic oxidation reactor comprises a reactor barrel body with two closed ends and connected with a plurality of inlet and outlet pipes, a central pipe is arranged in the reactor barrel body, a mixer is arranged at the upper part of the central pipe in the reaction cylinder, a plurality of reaction tubes are uniformly arranged on the periphery of the central pipe, a combined catalyst bed layer is arranged in each reaction tube, a desorption gas inlet and an air inlet are formed in the central pipe on the outer side of the reactor cylinder, a methanol inlet is also formed in the outer side of the reactor cylinder, a high-temperature flue gas outlet is formed in the side wall of the reactor cylinder above the reaction tubes, and a mixing fan is arranged at the bottom of the reactor cylinder; only one catalytic oxidation reactor is needed, and the uniformly mixed feed gas can completely react and then reach the discharge standard.
Description
Technical Field
The utility model provides a catalytic heating coupling methyl alcohol hydrogen manufacturing system, the utility model belongs to hydrogen manufacturing system technical field, concretely relates to methyl alcohol hydrogen manufacturing technical field.
Background
The reformed gas of the traditional methanol steam reforming hydrogen production process is subjected to pressure swing adsorption or membrane hydrogen extraction to obtain the required product H2In addition, the rest is the analytic gas, H in the analytic gas2The content is 30-40%; product H of the currently common direct methanol cracking process2CO, exhaust gas H after use2The content is more than 95 percent. The method has two treatment modes, one is that the waste gas is sent into a boiler combustion system for boiler combustion, and because the gas source is unstable, obvious potential safety hazard is caused to the boiler combustion system; in addition, the device is directly emptied, a large amount of combustible gas is emptied, the potential safety hazard is great, and clean energy waste is also caused. The treatment of the combustible tail gas becomes a difficult problem for the safe production of the methanol hydrogen production device.
Application number CN200910311040.7 discloses a methanol steam hydrogen manufacturing technology of catalytic combustion flue gas as heat source to methyl alcohol and demineralized water are the raw materials, loop through preheating, gasification, overheated, conversion process, obtain the transformation gas, and transformation gas rethread pressure swing adsorption obtains product hydrogen, exhaust tail gas, and wherein the conversion process is provided heat by the conduction oil system, tail gas produces the heat through catalytic combustion to with the conduction oil of above-mentioned heat transfer in the conduction oil system, the purpose is to solve in the current methanol steam hydrogen manufacturing technology with the tail gas evacuation and not make use of the wasting of resources problem that causes.
The system of the methanol steam hydrogen production process relates to two catalytic combustors, so that the equipment occupies large area, has high cost and low heat efficiency and utilization rate, and is not saved.
SUMMERY OF THE UTILITY MODEL
The utility model aims to provide a: the catalytic heating coupled methanol hydrogen production system is provided to solve the defects that the existing methanol hydrogen production system uses two catalytic burners, so that the equipment has large occupied area, high cost, low heat efficiency utilization rate and is not economical.
The utility model adopts the technical scheme as follows:
a catalytic heating coupling methanol hydrogen production system comprises a catalytic oxidation reactor, wherein the catalytic oxidation reactor comprises a reactor cylinder body, the two ends of the reactor cylinder body are sealed, the reactor cylinder body is connected with a plurality of inlet and outlet pipes, a central pipe is arranged in the reactor cylinder body, the central pipe extends to the outer side of the top of the reactor cylinder body, a mixer is arranged at the upper part of the central pipe in the reactor cylinder body, a plurality of reaction tubes are uniformly arranged at the periphery of the central pipe, a combined catalyst bed layer is arranged in each reaction tube, the central pipe and the reaction tubes are open at the two ends, a heat-conducting medium outlet and a heat-conducting medium inlet are arranged on the cylinder wall of the reactor cylinder body between the two ends of the reaction tubes, an air inlet is arranged on the central pipe at the outer side of the reactor cylinder body, a methanol inlet is also arranged at the outer side of the reactor cylinder body, and is communicated with the central, a high-temperature flue gas outlet is formed in the side wall of the reactor cylinder above the reaction tubes, and a mixing fan is arranged at the bottom of the reactor cylinder; and a first oxygen online analyzer is arranged at the high-temperature flue gas outlet, and a second oxygen online analyzer is arranged at the inlet of the reaction tube array.
In the application, only one catalytic oxidation reactor is needed, catalytic oxidation raw material gas is mixed by a mixer at the upper part in a central tube, then flows to the lower part through the central tube and enters a high-speed fan, the mixed gas is mixed under the action of the high-speed fan under the pressure of 3-8KPa, so that the mixed gas entering a catalytic oxidation system is uniform, and the uniformly mixed raw material gas can be completely reacted in the catalytic oxidation heating reactor and then is discharged after reaching the standard; a second oxygen on-line analyzer is arranged at the inlet of a reaction tube array of the catalytic oxidation reactor, so that the feed gas for catalytic oxidation can be automatically adjusted in a proper proportion, and the complete catalytic oxidation of the reaction gas is ensured; a first oxygen online analyzer detects the oxygen content in the high-temperature flue gas at the outlet and judges whether the reaction is complete; the combined catalyst bed layer in each reaction tube is reasonable in collocation, small in airflow resistance and high in reaction efficiency.
Furthermore, the combined catalyst bed layer comprises a honeycomb cylindrical medium-temperature catalyst positioned at the lower part of each reaction tube and a spherical medium-temperature catalyst positioned at the upper part of the honeycomb cylindrical medium-temperature catalyst. The catalyst does not need an additional supporting piece, and the honeycomb cylindrical medium-temperature catalyst and the spherical medium-temperature catalyst are directly loaded into the reaction tube in sequence and proportion during installation.
Further, the volume ratio of the spherical medium-temperature catalyst to the honeycomb cylindrical medium-temperature catalyst is 1:4-1: 10.
Further, the volume ratio of the spherical medium-temperature catalyst to the honeycomb cylindrical medium-temperature catalyst is 1: 5.
Furthermore, an energy saver is arranged on one side of the catalytic oxidation reactor, a chimney is arranged on one side of the energy saver, the high-temperature flue gas outlet is communicated with the chimney through the energy saver, the high-temperature flue gas outlet is communicated with the air inlet through a return pipe, the air inlet is communicated with an air pipeline, and the air pipeline is communicated with the air inlet after passing through the energy saver. And a high-temperature flue gas part discharged from the high-temperature flue gas outlet enters the catalytic oxidation reactor from the air inlet through the return pipe to be used as protective gas, the rest part is cooled by the energy saver and then is exhausted by the chimney, and the analyzed gas and the air can enter the catalytic oxidation reactor to react after being heated by the energy saver or not.
Further, the periphery of each reaction tube is wound with fins. The purpose of the fin is to promote heat exchange efficiency.
The system further comprises a methanol hydrogen production reactor, a vaporization superheater, an oil-gas separator, an air cooler, a pressure swing adsorber or a membrane separator, wherein the vaporization superheater is communicated with the methanol hydrogen production reactor through a methanol and water vapor pipeline, and the methanol hydrogen production reactor is sequentially communicated with the vaporization superheater, the air cooler and the pressure swing adsorber or the membrane separator through connecting pipes; the catalytic oxidation reactor is communicated with the methanol hydrogen production reactor through a heat-conducting medium outlet, and the methanol hydrogen production reactor is sequentially communicated with the steam superheater, the oil-gas separator and the heat-conducting medium inlet through heat-conducting medium pipelines.
Furthermore, a desorption gas inlet is arranged on the central pipe on the outer side of the reactor cylinder, and the pressure swing absorber or the membrane separator is sequentially communicated with the energy saver and the desorption gas inlet through a first desorption gas pipeline.
Heating methanol and water vapor by a heat exchanger, vaporizing by a vaporization superheater, and introducing into a methanol hydrogen production reactor to produce H2The hydrogen is produced through a pressure swing absorber or a membrane separator after passing through a heat exchanger and then entering an air cooler, and simultaneously, the hydrogen is produced into analysis gas, the analysis gas is preheated through an energy saver in sequence, is mixed with air and the standard-reaching tail gas after partial catalytic oxidation, and is subjected to catalytic oxidation reaction and heat transfer, wherein the volume ratio of the analysis gas to the air to the standard-reaching tail gas after the partial catalytic oxidation is 1-5:1-5: 2-8; the heat is absorbed by the heat-conducting medium and supplies heat to the methanol hydrogen production reactor, and the heat-conducting medium after heat supply enters the catalytic oxidation reactor from the heat-conducting medium inlet after passing through the vaporization superheater and the oil-gas separator.
The device further comprises a methanol cracking reactor, a vaporization superheater, an oil-gas separator, an air cooler, a pressure swing absorber and a combustible gas pipeline, wherein the vaporization superheater is communicated with the methanol cracking reactor through a methanol pipeline; the catalytic oxidation reactor is communicated with the connecting pipe through a heat-conducting medium outlet, and the connecting pipe is sequentially communicated with the steam superheater, the oil-gas separator and the heat-conducting medium inlet through a heat-conducting medium pipeline.
Furthermore, a combustible gas inlet is formed in the central pipe on the outer side of the reactor barrel, the pressure swing adsorber is communicated with the combustible gas pipeline through a second gas analysis pipeline, and the combustible gas pipeline is communicated with the energy saver and the combustible gas inlet.
Heating methanol by a heat exchanger, vaporizing the methanol by a vaporization superheater, feeding the vaporized methanol into a methanol cracking reactor, feeding the generated cracked gas into an air cooler by a heat exchanger, feeding part of the cracked gas into a pressure swing adsorption device to prepare product gas, feeding the rest of the cracked gas into a cracked gas pipeline, feeding the analyzed gas from the pressure swing adsorption device into a combustible gas pipeline after passing through a second analyzed gas pipeline and communicating the cracked gas pipeline with the second analyzed gas pipeline, preheating the combustible gas by an energy saver, mixing the combustible gas with air and the standard tail gas after part of catalytic oxidation to perform catalytic oxidation reaction and transfer heat, wherein the volume ratio of the combustible gas to the air to the standard tail gas after part of catalytic oxidation is 1-5:1-5:2-8, absorbing the heat by a heat-conducting medium and supplying heat to the methanol reforming hydrogen production reactor, and feeding the heat-conducting medium after heat supply into the methanol reforming hydrogen production reactor from the heat-conducting medium inlet after passing through the vaporization superheater and an oil-gas separator A catalytic oxidation reactor. The product gas comprises CO and/or H2。
In the technical scheme of the application, the type of the medium-temperature catalyst is CAS-KR-MF-EG type methanol combustion catalyst, and the medium-temperature catalyst comprises a spherical and/or honeycomb cylindrical shape; the catalyst can enable methanol and air to generate catalytic oxidation reaction to generate heat under the condition of 100 ℃ and above.
According to the technical scheme, the heat exchanger is arranged at the lower part of the vaporization superheater, the vaporization superheater is arranged at the upper part of the vaporization superheater, and the integrated equipment occupies small space and saves space;
the heat conducting medium comprises heat conducting oil or heat conducting oil gas, the pressure of the heat conducting oil or the heat conducting oil gas is 0.01-0.5MPa, and the heating temperature is 200-350 ℃.
To sum up, owing to adopted above-mentioned technical scheme, the beneficial effects of the utility model are that:
1. in the utility model, a catalytic oxidation reactor is needed, after the catalytic oxidation raw material gas is mixed by an upper mixer in the center tube, the catalytic oxidation raw material gas enters a high-speed fan from the lower part of the center tube, and the mixed gas is mixed by 3-8KPa pressure under the action of the high-speed fan, so that the mixed gas entering the catalytic oxidation system is uniform, and the raw material gas after uniform mixing can be discharged after the complete reaction in the catalytic oxidation heating reactor;
2. a second oxygen on-line analyzer is arranged at the inlet of a reaction tube array of the catalytic oxidation reactor, so that the feed gas for catalytic oxidation can be automatically adjusted in a proper proportion, and the complete catalytic oxidation of the reaction gas is ensured;
3. a first oxygen online analyzer detects the oxygen content in the high-temperature flue gas at the outlet and judges whether the reaction is complete; the combined catalyst bed layer in each reaction tube is reasonable in collocation, small in airflow resistance and high in reaction efficiency;
4. the tail gas from the catalytic oxidation reactor is partially recycled, and inert gas is not additionally used for explosion suppression;
5. the heat-conducting medium of the catalytic heating coupling methanol hydrogen production system can be heat-conducting oil or heat-conducting oil gas, and the heat-conducting oil gas is selected to be more beneficial to energy conservation without using a heat-conducting oil circulating pump;
6. the high-speed fan is a high-temperature resistant centrifugal fan without a fan shell, so that the air quantity entering the catalytic oxidation reactor is uniform and stable;
7. the application field of the system is the methanol steam reforming hydrogen production process or the methanol cracking CO and H preparation2And (5) processing.
Drawings
FIG. 1 is a schematic structural diagram of a methanol steam reforming hydrogen production system of the present invention;
FIG. 2 is a schematic structural diagram of the methanol cracking hydrogen production system of the present invention;
FIG. 3 is a top view of the catalytic oxidation reactor of the present invention;
FIG. 4 is a schematic structural view of the reaction tubes and fins of the present invention;
fig. 5 is a longitudinal sectional view of fig. 4.
The labels in the figure are: 1-an energy saver, 2-a catalytic oxidation reactor, 3-a high-temperature flue gas outlet, 4-a central tube, 5-a reaction tube array, 6-a mixing fan, 7-a methanol inlet, 8-a heat-conducting medium outlet, 9-a heat-conducting medium inlet, 10-a methanol hydrogen production reactor, 11-a return pipe, 12-a vaporization superheater, 13-an oil-gas separator, 14-an air cooler, 15-a pressure swing adsorber, 16-a first oxygen online analyzer, 17-a second oxygen online analyzer, 18-a methanol cracking reactor, 19-a mixer, 20-a fin, 21-a desorption gas inlet, 22-an air inlet, 23-a combustible gas inlet, 24-an air pipeline, 25-a chimney and 26-a heat-conducting medium pipeline, 27-methanol and water vapor pipeline, 28-first analysis gas pipeline, 29-methanol pipeline, 30-combustible gas pipeline, 31-honeycomb cylindrical medium temperature catalyst, 32-spherical medium temperature catalyst, 33-second analysis gas pipeline and 34-pyrolysis gas pipeline.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more clearly understood, the present invention is further described in detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the invention.
Example 1
Referring to fig. 1-3, a catalytic heating coupled methanol hydrogen production system includes a catalytic oxidation reactor 2, the catalytic oxidation reactor 2 includes a reactor cylinder with two closed ends and connected with a plurality of inlet and outlet pipes, a central pipe 4 is disposed in the reactor cylinder, the central pipe 4 extends to the outside of the top of the reactor cylinder, a mixer 19 is disposed on the upper portion of the central pipe 4 in the reactor cylinder, a plurality of reaction tubes 5 are uniformly disposed on the periphery of the central pipe 4, a combined catalyst bed layer is disposed in each reaction tube 5, both ends of the central pipe 4 and the reaction tubes 5 are open, a heat-conducting medium outlet 8 and a heat-conducting medium inlet 9 are disposed on the wall of the reactor cylinder between both ends of the reaction tubes 5, a desorption gas inlet 21 is disposed on the central pipe 4 outside the reactor cylinder, the reactor comprises an air inlet 22, a methanol inlet 7 is further arranged on the outer side of the reactor barrel, the methanol inlet 7 is communicated with the central pipe 4 above the mixer 19 in the reactor barrel, a high-temperature flue gas outlet 3 is arranged on the side wall of the reactor barrel above the reaction tube array 5, and a mixing fan 6 is arranged at the bottom of the reactor barrel; a first oxygen online analyzer 16 is arranged at the high-temperature flue gas outlet 3, and a second oxygen online analyzer 17 is arranged at the inlet of the reaction tube array 5.
In the application, only one catalytic oxidation reactor 2 is needed, catalytic oxidation raw material gas is mixed by an upper mixer 19 in a central tube 4, then flows to the lower part through the central tube 4 and enters a high-speed fan, the mixed gas is mixed under the action of the high-speed fan under the pressure of 3-8KPa, so that the mixed gas entering a catalytic oxidation system is uniform, and the uniformly mixed raw material gas can be completely reacted in the catalytic oxidation heating reactor and then is discharged after reaching the standard; a second oxygen on-line analyzer 17 is arranged at the inlet of the reaction tube array 5 of the catalytic oxidation reactor 2, so that the catalytic oxidation of the reaction gas can be completely ensured by automatically adjusting the proper proportion of the catalytic oxidation raw material gas; a first oxygen online analyzer 16 detects the oxygen content in the high-temperature flue gas at the outlet and judges whether the reaction is complete; the combined catalyst bed layer in each reaction tube 5 is reasonable in collocation, small in airflow resistance and high in reaction efficiency.
Example 2
Referring to FIG. 5, based on example 1, the combined catalyst bed comprises a honeycomb cylindrical middle temperature catalyst 31 located at the lower part of each reaction tube 5 and a spherical middle temperature catalyst 32 located at the upper part of the honeycomb cylindrical middle temperature catalyst 31. The catalyst does not need an additional support piece, and the honeycomb cylindrical medium-temperature catalyst 31 and the spherical medium-temperature catalyst 32 are directly loaded into the reaction tube array 5 in sequence and proportion during installation.
Example 3
As shown in fig. 5, on the basis of example 2,
the volume ratio of the spherical medium-temperature catalyst 32 to the honeycomb cylindrical medium-temperature catalyst 31 is 1:4-1: 10.
Example 4
As shown in fig. 5, based on example 3, the volume ratio of the spherical medium-temperature catalyst 32 to the honeycomb cylindrical medium-temperature catalyst 31 is 1: 5.
Example 5
Referring to fig. 1-2, on the basis of embodiment 1, an economizer 1 is disposed at one side of the catalytic oxidation reactor 2, a chimney 25 is disposed at one side of the economizer 1, the high-temperature flue gas outlet 3 is communicated with the chimney 25 through the economizer 1, the high-temperature flue gas outlet 3 is communicated with the air inlet 22 through a return pipe 11, an air duct 24 is communicated with the air inlet 22, and the air duct 24 is communicated with the air inlet 22 after passing through the economizer 1. The high-temperature flue gas part discharged from the high-temperature flue gas outlet 3 enters the catalytic oxidation reactor 2 from the air inlet 22 through the return pipe 11 to be used as protective gas, the rest part is cooled by the energy saver 1 and then is exhausted by the chimney 25, and the desorption gas and the air can enter the catalytic oxidation reactor 2 to react after being heated by the energy saver 1 or not.
Example 6
As shown in fig. 4 to 5, on the basis of example 1, each of the reaction tubes 5 has fins 20 wound around the outer periphery thereof. The purpose of the fins 20 is to improve heat exchange efficiency.
Example 7
As shown in fig. 1, 3-5, on the basis of embodiment 1, the system further includes a methanol hydrogen production reactor 10, a vaporization superheater 12, an oil-gas separator 13, an air cooler 14, and a pressure swing adsorber 15 or a membrane separator, where the vaporization superheater 12 is communicated with the methanol hydrogen production reactor 10 through a methanol and water vapor pipeline 27, and the methanol hydrogen production reactor 10 is sequentially communicated with the vaporization superheater 12, the air cooler, and the pressure swing adsorber 15 or the membrane separator through connecting pipes; the catalytic oxidation reactor 2 is communicated with the methanol hydrogen production reactor 10 through a heat-conducting medium outlet 8, and the methanol hydrogen production reactor 10 is sequentially communicated with the steam superheater, the oil-gas separator 13 and the heat-conducting medium inlet 9 through a heat-conducting medium pipeline 26; a desorption gas inlet 21 is formed in the central pipe 4 on the outer side of the reactor cylinder, and the pressure swing absorber 15 or the membrane separator is sequentially communicated with the energy saver 1 and the desorption gas inlet 21 through a first desorption gas pipeline 28; the methanol and the water vapor are heated by a heat exchanger, enter a methanol hydrogen production reactor 10 after being vaporized by a vaporization superheater 12, and generate H2Passing through a heat exchanger, then entering an air cooler 14, then passing through a pressure swing adsorber 15 or a membrane separator to prepare product hydrogen, simultaneously generating analytic gas, sequentially preheating through the economizer 1, mixing with air and partial tail gas reaching the standard after catalytic oxidation to generate catalytic oxidation reaction,heat transfer, wherein the volume ratio of the analyzed gas to the air to the tail gas reaching the standard after partial catalytic oxidation is 1-5:1-5: 2-8; the heat is absorbed by the heat-conducting medium and supplies heat to the methanol hydrogen production reactor 10, and the heat-conducting medium after heat supply enters the catalytic oxidation reactor 2 from the heat-conducting medium inlet 9 after passing through the vaporization superheater 12 and the oil-gas separator 13.
Example 8
As shown in fig. 2, 3-5, on the basis of embodiment 1, the system further includes a methanol cracking reactor 18, a vaporization superheater 12, an oil-gas separator 13, an air cooler 14, a pressure swing adsorber 15, and a combustible gas pipeline 30, wherein the vaporization superheater 12 is communicated with the methanol cracking reactor 18 through a methanol pipeline 29, the methanol cracking reactor 18 is sequentially communicated with the vaporization superheater 12, the air cooler, and the pressure swing adsorber 15 through connecting pipes, and the air cooler 14 is communicated with the combustible gas pipeline 30 through a cracked gas pipeline 34; the catalytic oxidation reactor 2 is communicated with the connecting pipe through a heat-conducting medium outlet 8, and the connecting pipe is sequentially communicated with the steam superheater, the oil-gas separator 13 and the heat-conducting medium inlet 9 through a heat-conducting medium pipeline 26; the pressure swing adsorber 15 is communicated with the combustible gas pipeline 30 through a second analysis gas pipeline 33, and the combustible gas pipeline 30 is communicated with the economizer 1 and the combustible gas inlet 23; methanol is heated by a heat exchanger to a vaporization superheater 12 for vaporization and then enters a methanol cracking reactor 18, the generated cracked gas passes through the heat exchanger and then enters an air cooler 14, part of the cracked gas passes through a pressure swing adsorber 15 to prepare product gas, the rest of the cracked gas passes through a cracked gas pipeline 34, the desorbed gas from the pressure swing adsorber 15 passes through a second desorbed gas pipeline 33, the cracked gas pipeline 34 is communicated with the second desorbed gas pipeline 33 and then enters a combustible gas pipeline 30, the rest of the cracked gas and the desorbed gas from the pressure swing adsorber 15 form combustible gas, the combustible gas is preheated by the energy saver 1, the combustible gas is mixed with air and the up-to-standard tail gas after part of the catalytic oxidation to generate catalytic oxidation reaction and heat transfer, the volume ratio of the combustible gas, the air and the up-to-standard tail gas after part of the catalytic oxidation is 1-5:1-5:2-8, the heat is absorbed by a heat-conducting medium and supplies, the heat-conducting medium after heat supply enters the heat-conducting medium from the heat-conducting medium inlet 9 after passing through the vaporizing superheater 12 and the oil-gas separator 13A catalytic oxidation reactor 2. The product gas comprises CO and/or H2。
The above description is only exemplary of the present invention and should not be taken as limiting the scope of the present invention, as any modifications, equivalents, improvements and the like made within the spirit and principles of the present invention are intended to be included within the scope of the present invention.
Claims (10)
1. A catalytic heating coupling methanol hydrogen production system is characterized by comprising a catalytic oxidation reactor (2), wherein the catalytic oxidation reactor (2) comprises a reactor cylinder body with two closed ends and connected with a plurality of inlet and outlet pipes, a central pipe (4) is arranged in the reactor cylinder body, the central pipe (4) extends to the outer side of the top of the reactor cylinder body, a mixer (19) is arranged at the upper part of the central pipe (4) in the reactor cylinder body, a plurality of reaction tubes (5) are uniformly arranged on the periphery of the central pipe (4), a combined catalyst bed layer is arranged in each reaction tube (5), two ends of the central pipe (4) and the reaction tubes (5) are both open, a heat-conducting medium outlet (8) and a heat-conducting medium inlet (9) are arranged on the wall of the reactor cylinder body between the two ends of the reaction tubes (5), an air inlet (22) is formed in the central tube (4) on the outer side of the reactor cylinder, a methanol inlet (7) is further formed in the outer side of the reactor cylinder, the methanol inlet (7) is communicated with the central tube (4) above the mixer (19) in the reactor cylinder, a high-temperature flue gas outlet (3) is formed in the side wall of the reactor cylinder above the reaction tube array (5), and a mixing fan (6) is arranged at the bottom of the reactor cylinder; a first oxygen online analyzer (16) is arranged at the high-temperature flue gas outlet (3), and a second oxygen online analyzer (17) is arranged at the inlet of the reaction tube array (5).
2. A system for producing hydrogen from methanol by catalytic heating coupling according to claim 1, wherein the combined catalyst bed comprises a honeycomb cylindrical medium-temperature catalyst (31) located at the lower part of each reaction tube (5) and a spherical medium-temperature catalyst (32) located at the upper part of the honeycomb cylindrical medium-temperature catalyst (31).
3. A catalytic heating coupled methanol hydrogen production system according to claim 2, characterized in that the volume ratio of the spherical medium-temperature catalyst (32) to the honeycomb cylindrical medium-temperature catalyst (31) is 1:4-1: 10.
4. A catalytic heating coupled methanol hydrogen production system according to claim 2, characterized in that the volume ratio of the spherical medium-temperature catalyst (32) to the honeycomb cylindrical medium-temperature catalyst (31) is 1: 5.
5. The system for producing hydrogen from methanol through catalytic heating coupling according to claim 1, wherein an economizer (1) is arranged on one side of the catalytic oxidation reactor (2), a chimney (25) is arranged on one side of the economizer (1), the high-temperature flue gas outlet (3) is communicated with the chimney (25) through the economizer (1), the high-temperature flue gas outlet (3) is communicated with the air inlet (22) through a return pipe (11), an air pipeline (24) is communicated with the air inlet (22) through the air inlet (22), and the air pipeline (24) is communicated with the air inlet (22) after passing through the economizer (1).
6. A catalytic heating coupled methanol hydrogen production system according to claim 1, characterized in that the outer periphery of each reaction tube array (5) is wound with fins (20).
7. The system for producing hydrogen from methanol by catalytic heating coupling as claimed in claim 1, further comprising a methanol hydrogen production reactor (10), a vaporization superheater (12), an oil-gas separator (13), an air cooler (14), and a pressure swing adsorber (15) or a membrane separator, wherein the vaporization superheater (12) is communicated with the methanol hydrogen production reactor (10) through a methanol and water vapor pipeline (27), and the methanol hydrogen production reactor (10) is sequentially communicated with the vaporization superheater (12), a cold air cooler, and the pressure swing adsorber (15) or the membrane separator through connecting pipes; the catalytic oxidation reactor (2) is communicated with the methanol hydrogen production reactor (10) through a heat-conducting medium outlet (8), and the methanol hydrogen production reactor (10) is sequentially communicated with the vaporization superheater (12), the oil-gas separator (13) and the heat-conducting medium inlet (9) through a heat-conducting medium pipeline (26).
8. A catalytic heating coupling methanol hydrogen production system according to claim 7, characterized in that a gas analysis inlet (21) is arranged on the central pipe (4) outside the reactor cylinder, and the pressure swing adsorber (15) or the membrane separator is sequentially communicated with the economizer (1) and the gas analysis inlet (21) through a first gas analysis pipeline (28).
9. The system for producing hydrogen by catalytic heating coupled methanol according to claim 1, further comprising a methanol cracking reactor (18), a vaporization superheater (12), an oil-gas separator (13), an air cooler (14), a pressure swing adsorber (15), and a combustible gas pipeline (30), wherein the vaporization superheater (12) is communicated with the methanol cracking reactor (18) through a methanol pipeline (29), the methanol cracking reactor (18) is sequentially communicated with the vaporization superheater (12), the air cooler and the pressure swing adsorber (15) through connecting pipes, and the air cooler (14) is communicated with the combustible gas pipeline (30) through a cracked gas pipeline (34); the catalytic oxidation reactor (2) is communicated with the connecting pipe through a heat-conducting medium outlet (8), and the connecting pipe is sequentially communicated with the vaporization superheater (12), the oil-gas separator (13) and the heat-conducting medium inlet (9) through a heat-conducting medium pipeline (26).
10. A system for producing hydrogen from methanol by catalytic heating coupling according to claim 9, wherein a combustible gas inlet (23) is provided on the central tube (4) outside the reactor cylinder, the pressure swing adsorber (15) is communicated with the combustible gas pipeline (30) through a second desorption gas pipeline (33), and the combustible gas pipeline (30) is communicated with the economizer (1) and the combustible gas inlet (23).
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