CN110386590B - Small-size methyl alcohol hydrogen plant - Google Patents
Small-size methyl alcohol hydrogen plant Download PDFInfo
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- CN110386590B CN110386590B CN201910772397.9A CN201910772397A CN110386590B CN 110386590 B CN110386590 B CN 110386590B CN 201910772397 A CN201910772397 A CN 201910772397A CN 110386590 B CN110386590 B CN 110386590B
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- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 133
- 239000001257 hydrogen Substances 0.000 title claims abstract description 133
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 128
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 95
- 238000003860 storage Methods 0.000 claims abstract description 77
- 238000006243 chemical reaction Methods 0.000 claims abstract description 58
- 230000008016 vaporization Effects 0.000 claims abstract description 36
- 238000005336 cracking Methods 0.000 claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 claims abstract description 29
- 238000009834 vaporization Methods 0.000 claims abstract description 29
- 238000010438 heat treatment Methods 0.000 claims abstract description 27
- 239000002918 waste heat Substances 0.000 claims abstract description 18
- 239000007788 liquid Substances 0.000 claims abstract description 12
- 238000011084 recovery Methods 0.000 claims abstract description 11
- 239000007789 gas Substances 0.000 claims description 22
- 239000010865 sewage Substances 0.000 claims description 5
- 239000010935 stainless steel Substances 0.000 claims description 4
- 229910001220 stainless steel Inorganic materials 0.000 claims description 4
- 239000011259 mixed solution Substances 0.000 abstract description 27
- 238000001816 cooling Methods 0.000 abstract description 5
- 229910000831 Steel Inorganic materials 0.000 abstract description 4
- 150000002431 hydrogen Chemical class 0.000 abstract description 4
- 239000010959 steel Substances 0.000 abstract description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 9
- 239000003054 catalyst Substances 0.000 description 9
- 230000001681 protective effect Effects 0.000 description 9
- 229910002092 carbon dioxide Inorganic materials 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 230000009471 action Effects 0.000 description 4
- 229910045601 alloy Inorganic materials 0.000 description 4
- 239000000956 alloy Substances 0.000 description 4
- 229910052761 rare earth metal Inorganic materials 0.000 description 4
- 150000002910 rare earth metals Chemical class 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 230000008676 import Effects 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 230000003139 buffering effect Effects 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 239000007769 metal material Substances 0.000 description 2
- GBMDVOWEEQVZKZ-UHFFFAOYSA-N methanol;hydrate Chemical compound O.OC GBMDVOWEEQVZKZ-UHFFFAOYSA-N 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000010923 batch production Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000000629 steam reforming Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- 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
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/323—Catalytic reaction of gaseous or liquid organic compounds other than hydrocarbons with gasifying agents
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Health & Medical Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Inorganic Chemistry (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention discloses a small-sized methanol hydrogen production device, which comprises a mixed liquid storage tank, a metering pump, a comprehensive reaction tank, a vaporization pipe, a cracking pipe, a heat conduction oil circulation system, a hydrogen storage pipe and a waste heat recovery system, wherein the vaporization pipe is positioned in the comprehensive reaction tank; the heat conduction oil circulation system comprises a heating component, a heat conduction oil pipe and a heat pump, wherein two ends of the heat conduction oil pipe are communicated with the comprehensive reaction tank to form heat conduction oil circulation, the waste heat recovery system can give out hydrogen cooling of a hydrogen port, and the waste heat heats the mixed solution to 40-60 ℃. The vaporization device and the cracking reaction device are combined together, and are uniformly heated to a designated stable state by the conduction oil circulation system, and vaporized and converted to produce hydrogen, so that heating and cracking hydrogen production are realized; a set of heating vaporization device is omitted, and the consumption of steel and heat conducting oil is saved by 50%.
Description
Technical Field
The invention relates to the technical field of hydrogen production equipment, in particular to a small methanol hydrogen production device.
Background
The hydrogen production by methanol refers to a process of mixing methanol with steam and then performing a catalytic reaction under certain temperature and pressure conditions to make the methanol undergo a cracking reaction and finally obtain hydrogen and carbon dioxide. The main chemical reaction formula of methanol and steam reforming is as follows:
CH3OH→CO+2H2 (1)；
H2O+CO→CO2+H2 (2)；
CH3OH+H2O→CO2+3H2 (3)；
The specific method for preparing hydrogen from methanol in industry is that methanol and desalted water are mixed according to a certain proportion and then are sent into a vaporization tower to be vaporized, vaporized water-methanol steam is overheated by a superheater and then enters a converter, a catalyst is arranged in the converter, and the water-methanol steam is subjected to a cracking reaction in the converter under the action of the catalyst to generate hydrogen and carbon dioxide. The main defects of the methanol hydrogen production equipment in the prior art are as follows: 1. the whole equipment is huge and complex, and the manufacturing cost is high; 2. the design method has the defect that the design is designed by skid-mounting without leaving one machine; 3. the heat conducting oil for providing heat source for the superheater and the converter is heated by a stainless steel thermocouple, and has uneven heating area, high power consumption, and short service life.
Disclosure of Invention
The invention provides a small-sized methanol hydrogen production device which reduces the volume of methanol hydrogen production equipment, reduces the manufacturing cost of the equipment (reduces the consumption of steel), improves the safety and the reliability, changes the heating mode of heat conduction oil and reduces the energy consumption.
11. In order to achieve the above purpose, the technical scheme adopted by the invention is that the small-sized methanol hydrogen production device comprises a comprehensive reaction tank, a vaporization pipe, a cracking pipe and a heat conduction oil circulation system, wherein heat conduction oil is filled in the comprehensive reaction tank, the vaporization pipe and the cracking pipe are positioned in the comprehensive reaction tank, gas vaporized by the vaporization pipe enters the cracking pipe, the heat conduction oil circulation system comprises a heating component, a heat conduction oil pipe and a heat pump, the heating component and the heat pump are respectively communicated with the heat conduction oil pipe, and two ends of the heat conduction oil pipe are communicated with the comprehensive reaction tank so as to form heat conduction oil circulation.
The vaporization device and the cracking reaction device are combined together, and are uniformly heated to a designated stable state by the conduction oil circulation system, and vaporized and converted to produce hydrogen, so that heating and cracking hydrogen production are realized; a set of heating vaporization device is omitted, and 50% of steel and heat conduction oil consumption can be saved.
Preferably, the hydrogen production device further comprises a hydrogen storage tube, wherein a hydrogen outlet at the bottom of the comprehensive reaction tank is connected with the hydrogen storage tube, and the hydrogen storage tube is an S-shaped hydrogen storage tube. The existing hydrogen storage tank is replaced by a hydrogen storage pipe, the occupied area can be reduced, and the hydrogen storage tank is replaced by a pipe with a large caliber, so that the hydrogen production container is more compact in design, convenient to operate and smaller in size, and various metal materials are saved.
Preferably, the hydrogen plant further comprises a buffer tube, the hydrogen storage tube is arranged inside the buffer tube and extends out of the buffer tube, and the buffer tube is an S-shaped buffer tube. The buffer tube is a hollow S-shaped tube, so that the hydrogen storage tube is of an S-shaped structure, the S-shaped hydrogen storage tube is selected, and compared with a linear structure, the gas enters the S-shaped tube body, so that the vertical downward impact force can be dispersed, the gas pressure is buffered, the impact force of the gas is reduced, and the S-shaped structure can play a role in buffering; and select the S type hydrogen storage pipe of using, for sharp hydrogen storage pipe, gas enters into the S type body, can disperse vertical decurrent impact force, buffer gas pressure reduces gaseous impact force, and S type structure can play the cushioning effect.
Preferably, the hydrogen production device further comprises a waste heat recovery system, the waste heat recovery system comprises a first sleeve and a second sleeve, one end of the first sleeve is connected with the sleeve inlet of the buffer tube and is communicated with the interior of the buffer tube, the other end of the first sleeve is communicated with the mixed liquid outlet pipeline of the mixed liquid storage tank, one end of the second sleeve is connected with the sleeve outlet of the buffer tube and is communicated with the interior of the buffer tube, and the other end of the second sleeve is communicated with the outlet pipeline of the mixed liquid storage tank.
According to the waste heat recovery system, when the methanol-desalted water in the comprehensive reaction tank is subjected to cracking reaction to convert hydrogen, the hydrogen is conveyed to the hydrogen storage tube and enters the hydrogen storage tube in the buffer tube, the hydrogen temperature in the buffer tube reaches 146 ℃, meanwhile, the mixed liquid in the mixed liquid storage tank enters the sleeve inlet along the first sleeve so as to enter the buffer tube, the mixed liquid flows outside the hydrogen storage tube in the buffer tube, on one hand, the hydrogen at a hydrogen outlet can be cooled, on the other hand, the temperature in the hydrogen storage tube is utilized to absorb the waste heat at 146 ℃, the mixed liquid is heated to 40-60 ℃ through the collected waste heat, and then enters the metering pump inlet through the sleeve outlet, so that the preheating temperature required by the comprehensive reaction tank is reasonably and effectively obtained, and meanwhile, the hydrogen at the hydrogen outlet can be cooled effectively so as to reach the temperature suitable for running of a pressure gauge and the like.
Preferably, the mixed liquor outlet of the mixed liquor storage tank is higher than the sleeve inlet of the buffer tube, and preferably, the outlet of the mixed liquor storage tank is 3-5 meters higher than the sleeve inlet of the buffer tube. Because the outlet of the mixed solution storage tank is 3-5 meters higher than the sleeve inlet of the buffer tube, the pressure difference exists, and under the action of the metering pump, the mixed solution in the mixed solution storage tank enters the sleeve inlet along the first sleeve so as to enter the buffer tube, the mixed solution flows outside the hydrogen storage tube in the buffer tube,
Preferably, the hydrogen storage tube is provided with a safety valve, and the buffer tube is provided with a drain outlet. The sewage can be discharged through the sewage outlet.
Preferably, the vaporizing tube is spirally wound on the outer wall of the cracking tube. Thus, the extension length of the vaporization pipe can be increased, and the area heated by the heat conduction oil can be increased, so that a better heating effect is obtained, and a better vaporization effect is obtained.
Preferably, a stainless steel filter screen is arranged at the bottom end of the cracking tube.
Preferably, the hydrogen production device further comprises a mixed liquor storage tank and an electromagnetic metering pump, and the metering pump is connected between the mixed liquor storage tank and the comprehensive reaction tank.
Preferably, a pipeline for introducing the shielding gas is connected with a pipeline for connecting the metering pump with the comprehensive reaction tank. The pipeline connecting the metering pump and the comprehensive reaction tank is connected with a protective gas pipeline for introducing protective gas so that the hydrogen production device can be filled with the protective gas to protect the catalyst during the shutdown period.
The invention has the beneficial effects that:
1. the small-sized methanol hydrogen production device ensures that methanol hydrogen production equipment really gets rid of the regulations that the hydrogen production equipment must be placed in a chemical region and the complicated manufacturing process of chemical skid-mounting, really realizes civilian use, and realizes batch production, and is applied to industries needing hydrogen production and hydrogenation in various industries and boiler and kiln combustion;
2. The system is more integrated, and can be controlled remotely to master the working state in real time;
3. The hydrogen storage tank is replaced by a hydrogen storage pipe, and the safety valve is arranged on a large-caliber pipeline; the electromechanical cabinet enables the vaporizer and the reaction kettle to be integrated into a comprehensive reaction device, has more compact structure, smaller volume and effective contraction of occupied area, and saves a large amount of steel materials and 50% of heat conduction oil.
4. The waste heat recovery system of the invention can provide hydrogen cooling of the hydrogen outlet on one hand, and absorbs the waste heat of 146 ℃ by utilizing the temperature inside the hydrogen storage tube, and the mixed liquid is heated to 40-60 ℃ by the collected waste heat and then enters the inlet of the metering pump through the sleeve outlet, so that the preheating temperature required by the input of the comprehensive reaction tank is reasonably and effectively obtained in a two-step way, and meanwhile, the hydrogen cooling of the hydrogen outlet is effectively realized so as to reach the temperature suitable for operation of the pressure gauge and the like.
Drawings
Fig. 1 is a schematic diagram of the overall structure of the present invention.
Detailed Description
The invention will now be described in further detail with reference to the accompanying drawings, which are simplified schematic illustrations, illustrating the basic structure of the invention by way of illustration only, the direction of this embodiment being the direction of fig. 1.
The invention relates to a small-sized methanol hydrogen production device which mainly comprises a mixed solution storage tank 1, a metering pump 2, a comprehensive reaction tank 3, a vaporization pipe 4, a cracking pipe 5, a heat conduction oil circulation system 6, a buffer pipe 7 and a waste heat recovery system;
The mixed solution storage tank 1 is used for storing methanol and desalted water solution for hydrogen production, the top end of the mixed solution storage tank 1 is provided with an air discharge hole 11, the side surface of the mixed solution storage tank is provided with a mixed solution inlet valve 12, and the bottom end of the mixed solution storage tank is provided with a mixed solution outlet valve 13; the mixed liquid outlet valve 13 is connected with the metering pump 2 through a pipeline, the metering pump 2 is connected with the comprehensive reaction tank 3, a protective gas pipeline 20 for introducing protective gas is connected to the pipeline, where the metering pump 2 is connected with the comprehensive reaction tank 3, and the protective gas pipeline is provided with a protective gas valve 201, so that the hydrogen production device can be filled with protective gas to protect catalyst during shutdown. Meanwhile, a pressure gauge 21 is arranged between the metering pump 2 and the protective gas valve 201, and a valve 10 is also arranged between the metering pump 2 and the pressure gauge 21.
The comprehensive reaction tank 3 sequentially comprises a vaporization zone 31, a reaction zone 32 filled with heat conduction oil and a hydrogen zone 33 from top to bottom; the bottom end of the vaporizing tube 4 is connected with the metering pump 2, the vaporizing tube 4 is spirally positioned in the internal reaction zone 32 of the comprehensive reaction tank 4, extends out of the top end of the comprehensive reaction tank 3 and enters the vaporizing zone 31 in the comprehensive reaction tank 3, and a vaporizing inlet valve 41 and a vaporizing outlet valve 42 are arranged on the outer side of the comprehensive reaction tank 3 of the vaporizing tube 4;
the cracking tube 5 is longitudinally arranged in the reaction zone 32 inside the comprehensive reaction tank 3 and provided with a plurality of cracking tubes 5, the bottom ends of the cracking tubes 5 are communicated with the vaporization zone, the bottom ends of the cracking tubes 5 are communicated with the hydrogen zone 33, the vaporization tubes 4 are spirally wound on the outer side of the cracking tubes 5, the cracking tubes 5 are not communicated with the vaporization tubes 4, the inside of the cracking tubes 5 is filled with a catalyst for promoting the reaction, the catalyst and the filling mode are realized by adopting the prior art, and the catalyst and the filling mode are common knowledge, and a stainless steel filter screen is arranged at the bottom ends of the cracking tubes 5;
The heat conduction oil circulation system 6 comprises a heating component 61, a heat conduction oil pipe 62 and a heat pump 63, wherein the heating component 61 and the heat pump 63 are respectively communicated with the heat conduction oil pipe 62, the bottom end of the heat conduction oil pipe 62 is communicated with one side of the bottom end of a reaction zone of the comprehensive reaction tank 3, a heat conduction oil inlet valve 64 is arranged at the position of the heat conduction oil pipe 62, the other end of the heat conduction oil pipe 62 is communicated with one side of the top end of the reaction zone 32 of the comprehensive reaction tank, a heat conduction oil outlet valve 65 is arranged at the position of the heat conduction oil pipe 62, the heat conduction oil in the comprehensive reaction tank 3 is input into the heat conduction oil pipe through the heat pump, the heating component 61 is used for heating, the heat conduction oil inlet valve 64 is opened after heating and enters the comprehensive reaction tank, so as to form a heat conduction oil circulation, the heating component 61 is a heating pipe of a nano rare earth alloy heating material, the heat conduction oil is heated to a specified temperature, so that the heat conduction oil is heated in a container to a plurality of the specified temperature, and the heating pipe can be set as required. The heating component adopts the nano rare earth alloy heating material, so that the vaporization temperature reaches the specified temperature of 250 ℃, and the adopted rare earth nano alloy heating material has the advantages of large heating area, good stability, electricity consumption saving and long service life. Because the rare earth nano alloy heating material is more portable and flexible to use, the heat conduction oil can be heated to the designated temperature required by conversion, pyrolysis and hydrogen production, and the heating problem is solved.
The bottom hydrogen zone 33 of the comprehensive reaction tank 3 is provided with a hydrogen outlet 34, the hydrogen outlet 34 is connected with a hydrogen storage tube 35, the hydrogen storage tube 35 is arranged inside the buffer tube 7 and extends out of the buffer tube 7 to be connected with occasions such as a boiler, a kiln, a hydrogen energy generator and the like; the hydrogen storage tube 35 is provided with the hydrogen outlet valve 351, and the safety valve 352 is arranged at the position of the hydrogen storage tube 35 positioned inside the buffer tube 7, and the buffer tube 7 is a hollow S-shaped tube, so that the hydrogen storage tube 35 is of an S-shaped structure, the existing hydrogen storage tank is replaced by the hydrogen storage tube, the occupied area can be reduced, and the hydrogen storage tank is replaced by a large-caliber tube, so that the hydrogen production container is more compact in design, convenient to operate, smaller in size and capable of saving various metal materials. The S-shaped hydrogen storage tube is selected, and compared with a linear structure, the S-shaped hydrogen storage tube has the advantages that gas enters the S-shaped tube body, so that the vertical downward impact force can be dispersed, the gas pressure is buffered, the impact force of the gas is reduced, and the S-shaped structure can play a role in buffering; be equipped with drain 71, sleeve pipe import 72, sleeve pipe export 73 on the buffer tube 7, wherein, sleeve pipe import 72 sets up the upper end at buffer tube 7, is located hydrogen storage tube 35 hydrogen exit one side, and sleeve pipe export 73 sets up in the bottom, is located hydrogen storage tube 35 hydrogen entrance one side, and drain 7 sets up the bottom at buffer tube 7, and foretell drain 7, sleeve pipe import 72, sleeve pipe export 73 all communicate with buffer tube 7 is inside, and all is equipped with valve 10. The waste heat recovery system comprises a first sleeve 81 and a second sleeve 82, wherein one end of the first sleeve 81 is connected with a sleeve inlet 72 of the buffer tube 7 and is communicated with the interior of the buffer tube 7, the other end of the first sleeve 81 is communicated with an outlet pipeline of the mixed liquor storage tank 1, one end of the second sleeve 82 is connected with a sleeve outlet 72 of the buffer tube 7 and is communicated with the interior of the buffer tube 7, the other end of the first sleeve 81 is communicated with an outlet pipeline of the mixed liquor storage tank 1, the outlet pipeline of the mixed liquor storage tank 1 is connected with the first sleeve and the second sleeve through a tee joint, the outlet of the mixed liquor storage tank 1 is higher than the sleeve inlet of the buffer tube, mixed liquor circulation is realized through pressure difference and a metering pump, and preferably, the outlet of the mixed liquor storage tank 1 is higher than the sleeve inlet of the buffer tube by 3-5 meters.
According to the waste heat recovery system, when the methanol-desalted water in the comprehensive reaction tank is subjected to cracking reaction to convert hydrogen, the hydrogen is conveyed to the hydrogen storage tube 35 and enters the hydrogen storage tube 35 in the buffer tube 7, the hydrogen temperature in the buffer tube 7 reaches 146 ℃, meanwhile, the mixed solution in the mixed solution storage tank 1 enters the sleeve inlet along the first sleeve 81 so as to enter the buffer tube 7, the mixed solution flows outside the hydrogen storage tube in the buffer tube 7, on one hand, the hydrogen at a hydrogen outlet can be cooled, on the other hand, the waste heat at 146 ℃ is absorbed by utilizing the temperature in the hydrogen storage tube, the mixed solution is heated to 40-60 ℃ through the collected waste heat, and then enters the metering pump inlet through the sleeve outlet, so that the required preheating temperature required by the comprehensive reaction tank is reasonably and effectively obtained, and meanwhile, the hydrogen at the hydrogen outlet is cooled so as to reach the temperature suitable for running of a pressure meter and the like. Preferably, the first sleeve and the second sleeve are galvanized pipes.
The small-sized methanol hydrogen production device is also provided with a PLC controller, and the PLC controller is connected with the electromagnetic valve, the pressure gauge, the metering pump and the heat pump to realize automatic control.
The working principle of the invention is as follows: firstly, the vaporization of the methanol mixed solution is carried out, the heat conduction oil is heated through a heat conduction oil circulation system, circulation is carried out in the comprehensive reaction tank, the methanol mixed solution is heated to the vaporization temperature required by the methanol mixed solution, at the moment, the methanol mixed solution enters into the vaporization pipe, the methanol mixed solution absorbs heat of the heat conduction oil in the vaporization pipe and is vaporized, the vaporized mixed solution enters into the vaporization area 31 of the comprehensive reaction tank through the upper end of the vaporization pipe and enters into the cracking pipe, the cracking pipe is internally filled with a catalyst, the heat conduction oil at the moment has the working temperature of 240-260 ℃, the cracking reaction is carried out under the action of the catalyst, hydrogen and carbon dioxide mixed gas are generated, and the hydrogen is discharged through the buffer hydrogen storage pipe for various hydrogen users, such as related enterprises including boilers, kiln combustion and the like. When the methanol-desalted water in the comprehensive reaction tank is converted into hydrogen through a cracking reaction and is conveyed to the hydrogen storage tube 35, and enters the hydrogen storage tube 35 in the buffer tube 7, the temperature of the hydrogen in the buffer tube 7 reaches 146 ℃, meanwhile, as the outlet of the mixed solution storage tank 1 is 3-5 meters higher than the sleeve inlet of the buffer tube, the pressure difference exists, and under the action of the metering pump, the mixed solution in the mixed solution storage tank 1 enters the sleeve inlet along the first sleeve 81, so as to enter the buffer tube 7, the mixed solution flows outside the hydrogen storage tube in the buffer tube 7, on one hand, the hydrogen cooling of a hydrogen outlet can be given, on the other hand, the residual heat of 146 ℃ is absorbed by utilizing the internal temperature of the hydrogen storage tube, the mixed solution is heated to 40-60 ℃ through the collected residual heat, and then enters the metering pump inlet through the sleeve outlet, so that the preheating temperature required by the comprehensive reaction tank is reasonably and effectively obtained, and meanwhile, the hydrogen cooling of the hydrogen outlet is effectively obtained, so as to reach the temperature suitable for running of a pressure meter.
The valves of the invention, not specifically illustrated, are designated by 10 in the drawings.
The foregoing description of the preferred embodiments of the invention is not intended to be limiting, but rather to enable any modification, equivalent replacement, improvement or the like to be made within the spirit and principles of the invention.
Claims (7)
1. The utility model provides a small-size methyl alcohol hydrogen plant, its characterized in that includes mixed liquor holding vessel, the integrated reaction tank that has the conduction oil in inside, vaporization pipe, schizolysis pipe, conduction oil circulation system, hydrogen storage pipe, buffer tube, waste heat recovery system, vaporization pipe, schizolysis pipe are located the inside of integrated reaction tank, the gaseous entering schizolysis pipe after vaporization of vaporization pipe, conduction oil circulation system includes heating element, conduction oil pipe, heat pump, heating element, heat pump communicate with conduction oil pipe respectively, and conduction oil pipe' S both ends communicate with integrated reaction tank to this constitution conduction oil circulation, the bottom hydrogen outlet of integrated reaction tank connects the hydrogen storage pipe, the hydrogen storage pipe is the S type hydrogen storage pipe, the hydrogen storage pipe sets up inside the buffer tube and extends outside the buffer tube;
The buffer tube is provided with a sewage outlet, a sleeve inlet and a sleeve outlet, the sleeve inlet is arranged at the upper end of the buffer tube and is positioned at one side of the hydrogen outlet of the hydrogen storage tube, the sleeve outlet is arranged at the bottom end of the buffer tube and is positioned at one side of the hydrogen inlet of the hydrogen storage tube, the sewage outlet is arranged at the bottom of the buffer tube, and the sewage outlet, the sleeve inlet and the sleeve outlet are communicated with the inside of the buffer tube and are provided with valves;
The waste heat recovery system comprises a first sleeve and a second sleeve, one end of the first sleeve is connected with the inlet of the sleeve and is communicated with the inside of the buffer tube, the other end of the first sleeve is communicated with the mixed liquid outlet pipeline, one end of the second sleeve is connected with the sleeve outlet and is communicated with the inside of the buffer tube, and the other end of the second sleeve is communicated with the outlet pipeline of the mixed liquid storage tank.
2. A compact methanol to hydrogen plant as in claim 1 wherein the outlet of the mixed liquor storage tank is 3-5 meters above the inlet of the sleeve at the buffer tube.
3. A compact methanol to hydrogen plant as in claim 1 wherein said hydrogen storage tube is provided with a safety valve.
4. A small methanol to hydrogen plant as in claim 1 wherein said vaporization tube spirals outside the cracking tube in a spiral shape.
5. A small methanol to hydrogen plant as in claim 1 wherein a stainless steel filter screen is mounted at the bottom end of the cracking tube.
6. A small-sized methanol hydrogen production device according to claim 1, wherein a metering pump is connected between the mixed liquor storage tank and the comprehensive reaction tank.
7. A small-sized methanol to hydrogen plant as in claim 6 wherein a shielding gas line for introducing shielding gas is connected to the line connecting the metering pump and the integrated reaction tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910772397.9A CN110386590B (en) | 2019-08-19 | 2019-08-19 | Small-size methyl alcohol hydrogen plant |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910772397.9A CN110386590B (en) | 2019-08-19 | 2019-08-19 | Small-size methyl alcohol hydrogen plant |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110386590A CN110386590A (en) | 2019-10-29 |
| CN110386590B true CN110386590B (en) | 2024-04-19 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN201910772397.9A Active CN110386590B (en) | 2019-08-19 | 2019-08-19 | Small-size methyl alcohol hydrogen plant |
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Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111422831B (en) * | 2020-04-29 | 2021-10-19 | 西安交通大学 | Methanol cracking device |
| CN115159457A (en) * | 2022-08-26 | 2022-10-11 | 江西新节氢能源科技有限公司 | Skid-mounted equipment for producing mixed hydrogen |
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| US20050025471A1 (en) * | 2001-12-24 | 2005-02-03 | Ho Lil Achmad | Liquid heater |
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| US20050025471A1 (en) * | 2001-12-24 | 2005-02-03 | Ho Lil Achmad | Liquid heater |
| CN102322753A (en) * | 2011-10-08 | 2012-01-18 | 南京华电节能环保设备有限公司 | Solid particle heat exchanger |
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| CN207050522U (en) * | 2017-08-14 | 2018-02-27 | 四川博蓝科新材料有限公司 | A kind of carbon black raw oil preheating device |
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| CN110386590A (en) | 2019-10-29 |
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