CN112573481B - Stepped slow temperature-changing methanol hydrogen production line - Google Patents
Stepped slow temperature-changing methanol hydrogen production line Download PDFInfo
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- CN112573481B CN112573481B CN202011578236.5A CN202011578236A CN112573481B CN 112573481 B CN112573481 B CN 112573481B CN 202011578236 A CN202011578236 A CN 202011578236A CN 112573481 B CN112573481 B CN 112573481B
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- 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
- C01B3/22—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by decomposition of gaseous or liquid organic compounds
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- 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
- C01B2203/0266—Processes for making hydrogen or synthesis gas containing a decomposition step
- C01B2203/0277—Processes for making hydrogen or synthesis gas containing a decomposition step containing a catalytic decomposition step
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- 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
- C01B2203/12—Feeding the process for making hydrogen or synthesis gas
- C01B2203/1205—Composition of the feed
- C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
- C01B2203/1217—Alcohols
- C01B2203/1223—Methanol
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Abstract
The application relates to a stepwise slow temperature-changing methanol hydrogen production line, which relates to the technical field of methanol hydrogen production, and comprises a raw material bin, a heat exchanger, a superheater and a converter which are sequentially connected, wherein the production line also comprises a cooler, a separator and a pressure swing adsorber, the converter is connected with a heat conduction device, the heat conduction device comprises an oil guide pipe, the oil guide pipe is connected with a plurality of heating microtubes, each heating microtube is divided into a heating section and a shunting section, the heating sections of the heating microtubes are uniformly wound on a reaction body, and the lengths of the shunting sections of the heating microtubes are sequentially increased. The heat conduction device provides a heat source to sequentially enter the heating section to heat the converter, and the catalyst can realize the effects of slowly heating and cooling.
Description
Technical Field
The application relates to the field of methanol hydrogen production, in particular to a stepwise slow temperature-changing methanol hydrogen production line.
Background
Hydrogen is one of the common industrial gases, is an important synthesis raw material gas in industries such as petroleum, chemical industry, fine chemical industry, medical intermediates and the like, is an indispensable shielding gas in metallurgy, electronic glass and mechanical manufacturing, is also used as an aerospace fuel, and is increasingly widely used as clean energy source abroad.
In the related art, methanol and desalted water are mixed according to a certain proportion, preheated by a heat exchanger and then sent into a vaporization tower, vaporized water-methanol steam is overheated by the heat exchanger and then enters a converter to carry out catalytic cracking and conversion reaction on a catalyst bed layer, converted gas containing about 74% of hydrogen and 24% of carbon dioxide is produced, the converted gas enters a water-washing absorption tower after heat exchange, cooling and condensation, unconverted methanol and water are collected at a tower bottom for recycling, and tower top gas is sent to a pressure swing adsorption device for purification. The methanol steam cracking reaction is an endothermic reaction, a certain temperature is needed in the catalytic cracking process of the raw material, and the higher the temperature is in the catalytic cracking process, the higher the conversion rate is. The converter comprises a reaction body, an electric heating tube is arranged in the reaction body, and the temperature in the reaction body is increased in an electric heating mode.
For the related art, the inventor considers that in the related art, the converter is convenient to operate in an electric heating mode, but the heating speed of the electric heating tube after being electrified is higher, so that the temperature rising and lowering speed in the reaction body is higher, the internal stress of the catalyst internal structure is increased due to rapid thermal expansion and contraction, the internal structure is broken and damaged, and the service life is shortened.
Disclosure of Invention
In order to solve the problem of the reduction of the service life of a catalyst caused by the over-high temperature rising and lowering speed of a converter, the application provides a stepped slow temperature-changing methanol hydrogen production line.
The application provides a stepwise slow temperature-changing methanol hydrogen production line which adopts the following technical scheme:
the utility model provides a cascaded slow alternating temperature methyl alcohol hydrogen manufacturing production line, the production line is including former feed bin, heat exchanger, superheater and the converter that connects gradually, the production line still includes cooler, separator, pressure swing adsorber and heat conduction device, the converter includes the reaction body, heat conduction device includes leads oil pipe, it is connected with a plurality of heating microtubes to lead oil pipe, every heating microtubes divide into heating section and reposition of redundant personnel section, a plurality of the even winding of heating section of heating microtubes is in on the reaction body, a plurality of the reposition of redundant personnel section of heating microtubes is located between reaction body and the heat conduction device and the length increases gradually.
By adopting the technical scheme, the heat conduction device provides a heat source, and the heat source is introduced into the heating section of the heating microtube from the flow dividing section of the heating microtube, so that raw materials in the reaction body are subjected to catalytic pyrolysis under the combined action of the catalyst and the temperature. The lengths of the split flow sections of the heating microtubes are different, the lengths of the heat sources enter the heating sections are different, the lengths of the split flow sections are sequentially increased, the heat sources sequentially enter the heating sections, and meanwhile, after the machine is stopped, the heat sources in the heating microtubes are sequentially discharged, so that the reaction body can realize the effects of slowly heating and cooling, the catalyst can realize the effects of slowly heating and cooling, and the service life of the catalyst is prolonged.
Optionally, the heat conduction device comprises a heating furnace, an oil tank is arranged in the heating furnace, the pressure swing adsorber is connected with a desorption gas pipe and a hydrogen pipe which can discharge combustible fuel, the desorption gas pipe is connected with the heating furnace to supply fuel for the heating furnace, and the oil tank is filled with heat conduction oil for providing heat sources for the reactant and the superheater.
Through adopting above-mentioned technical scheme, in the methyl alcohol hydrogen manufacturing process, pressure swing adsorption ware is the purification step of last hydrogen manufacturing, after the purification through pressure swing adsorption ware, the higher hydrogen of follow hydrogen pipe discharge purity, other waste gas are discharged from desorption trachea, and wherein include a small amount of hydrogen and carbon dioxide etc. are connected with desorption trachea through the heating furnace, utilize this waste gas on heat-conducting device, play resource-saving effect.
Optionally, the heat conduction device further comprises a first heat insulation box and heat conduction oil, one end of the first heat insulation box is connected with the oil tank, an electric heating tube is arranged in the first heat insulation box, the electric heating tube is electrically connected with a control switch, the converter is connected with a temperature detector, and the temperature detector is electrically connected with the control switch; the other end of the first heat preservation box is connected with the oil guide pipe, a second heat preservation box is connected between the first heat preservation box and the reaction body, and the shunting section of the heating microtube and the oil guide pipe are positioned in the second heat preservation box.
Through adopting above-mentioned technical scheme, heat conduction device mainly provides heat energy to the converter, but the waste gas passes through the heat that the heating furnace produced, after the conduction oil transmission, the converter easily has the problem that the heat source is not enough. When the temperature of the waste gas is insufficient, the control switch is started, and the heat conduction oil in the first heat preservation box is heated through the electric heating tube. When the temperature of the waste gas is insufficient, the temperature in the reactor can be slowly reduced, the temperature detector is arranged, the condition that the energy of the waste gas is insufficient can be found in time, and when the temperature detector detects that the temperature in the reactor is lower than a set temperature range, the control switch is automatically started to be started, and the electric heating tube heats heat conduction oil in the first heat preservation box. The shunting section is the heat source and reaches the position initially, and the temperature is higher, scalds the workman easily, plays the isolation protection effect through the setting of second insulation can, reduces the heat loss simultaneously to the holistic simplicity of heat conduction device outward appearance has been improved.
Optionally, a plurality of heating microtubes keep away from the one end of leading oil pipe extends there is the heating pipe, the heating pipe spirals in the superheater, the heating pipe is kept away from the one end of leading oil pipe is connected with out oil pipe, it is connected with the circulating pump to go out oil pipe to keep away from the one end of heating pipe, the circulating pump with the oil tank intercommunication.
By adopting the technical scheme, after the heat oil in the heating microtubes conducts heat to the converter, a large amount of heat still exists in the heat oil in the heating microtubes, and the heating pipes extending from the heating microtubes pass through the positions of the superheaters and are wound on the superheaters to heat raw materials in the superheaters. The circulation pump circulates the used heat conduction oil into the oil tank for repeated circulation, thereby playing a role in saving resources.
Optionally, the separator is connected with outlet duct and drain pipe, the outlet duct with vary voltage adsorber is connected, the drain pipe is connected with the storage tank, the storage tank is connected with the liquid phase spectrometer.
By adopting the technical scheme, the methanol and desalted water form steam in the superheater, the steam enters the converter, and hydrogen mainly containing carbon dioxide is generated under the action of the catalyst of the converter and high temperature. The gas returns to the heat exchanger, and after being used as a heat exchange medium to exchange heat with the methanol and desalted water which enter the heat exchanger, the gas enters the cooler to be cooled, and the gas enters the steam-water separator to be washed and separated, so that the gas with low impurity content and the methanol and desalted water which are not completely reacted are formed, and the gas enters the pressure swing adsorber to be purified. When methanol and desalted water enter a hydrogen production line, the ratio of the methanol to the desalted water is 1:1.8 in order to allow the methanol to react well. When the methanol and desalted water react in the reactor, the content of the formed incompletely reacted methanol and desalted water is uncertain due to other external factors such as catalyst deactivation, methanol volatilization, equipment corrosion and the like, and when the proportion of the incompletely reacted methanol and the desalted water is kept to be larger than the proportion of the methanol, the incompletely reacted methanol and the desalted water directly enter a raw material bin, so that the subsequent continuous use is not influenced. When the proportion of desalted water which is not fully reacted is smaller than the proportion of methanol under the influence of the external environment of the reactor, the heat exchanger, the cooler and the separator, the desalted water is directly recycled to the raw material bin for use, hydrogen production is not influenced, but the hydrogen production yield of a production line is easily influenced, and the hydrogen production yield value of the production line cannot be planned in advance, so that the follow-up work is influenced. And connecting a liquid outlet of the separator with a storage tank, firstly storing the methanol which is not fully reacted with the desalted water in the storage tank, and carrying out on-line detection and analysis on the content ratio of the methanol which is not fully reacted with the desalted water through a connected liquid phase spectrometer when a certain amount is collected.
Optionally, the storage tank is connected with first charging tank and second charging tank, the storage tank with be equipped with first valve between the first charging tank, the storage tank with be equipped with the second valve between the second charging tank.
Through adopting above-mentioned technical scheme, detect the chromatographic peak analysis of methyl alcohol or desalted water according to the liquid phase spectrometer, when obtaining that the result methyl alcohol content is less, through opening first valve, add the methyl alcohol volume in the storage jar, make the methyl alcohol in the storage jar and the desalted water proportion at 1:1.8 floatable ratio range. When the desalted water content is low, the second valve is opened, and the desalted water amount is added into the storage tank, so that the ratio of the methanol to the desalted water in the storage tank is within a floatable ratio range. So that the hydrogen product amount is in a controllable range in the subsequent hydrogen production process of the production line.
Optionally, the storage tank is connected with the tee bend ball valve, the tee bend ball valve includes first opening, second opening and third opening, first opening is connected with the storage tank, the second opening is connected with the liquid phase spectrometer, the third opening is connected with former feed bin, the storage tank with be connected with the filter component who can dismantle the connection between the first opening.
Through adopting above-mentioned technical scheme, converter, heat exchanger and cooler can appear corroding or the condition of impurity through long-term the use, can exist the impurity in the methanol and the desalted water of incomplete conversion that the separator separated. But the liquid phase spectrometer has higher liquid precision requirement on detection, and needs to be filtered by a filtering component, methanol and desalted water led out of a storage tank are filtered by the filtering component and then are led into the liquid phase spectrometer, so that the liquid phase spectrometer is protected, and the detection precision of the liquid phase spectrometer can reach the standard for a long time. When the mixed liquid in the storage tank is detected, the storage tank is controlled to be communicated with the liquid phase spectrometer through the three-way ball valve, after the content of methanol and desalted water in the storage tank is filled, the storage tank is controlled to be communicated with the raw material bin through the three-way ball valve, and the mixed liquid with the proportion consistent with that in the raw material bin is introduced into the raw material bin.
Optionally, the filtration subassembly includes filtration membrane and first mounting dish and the second mounting dish of pegging graft each other, be formed with the cavity after first mounting dish and the second mounting dish are pegged graft, the whole that forms is the filtration dish, filtration membrane is located the cavity, it has the rubber circle to filter dish outer wall circumference upward parcel, first mounting dish keep away from the one end of second mounting dish with storage tank sealing connection, the second mounting dish keep away from the one end of first mounting dish with tee bend ball valve sealing connection.
Through adopting above-mentioned technical scheme, filter the methyl alcohol and the desalted water that draw forth through filtration membrane to the storage tank, first mounting dish and storage tank sealing connection, second mounting dish and tee bend ball valve sealing connection, the rubber circle is used for sealed first mounting dish and second mounting dish hookup location.
Optionally, the filtering membrane is made of polyethersulfone material.
By adopting the technical scheme, the polyether sulfone material has good chemical resistance and can be filtered for a long time.
Optionally, the first mounting dish, the second mounting dish and the rubber ring are all made of medical plastic.
Through adopting above-mentioned technical scheme, simultaneously, first mounting dish, second mounting dish and rubber circle are made by medical plastics, reduce filter unit and carry out secondary pollution to methyl alcohol and desalted water.
In summary, the present application includes at least one of the following beneficial technical effects:
1. the length of the heating microtubes is controlled to be gradually increased in a shunting section mode, and heat conduction oil in the heat conduction device slowly enters the heating section to heat the converter, so that the converter is slowly heated, and the effect of prolonging the service life of a catalyst in the converter can be achieved;
2. the desorbing gas is utilized through the arrangement of the connection of the heating furnace and the desorbing pipe, so that the effect of saving resources can be achieved;
3. through the setting of liquid phase spectrometer, detect the mixed solution of retrieving in the storage jar, rethread testing result, the proportion of adjustment mixed solution is retrieved to former feed bin in practicality, can play the effect that makes the hydrogen output of production line be in controllable scope.
Drawings
FIG. 1 is a schematic diagram of the overall structure of a methanol to hydrogen production line in an embodiment of the application.
Fig. 2 is a schematic view showing an internal structure of a heat conduction device in an embodiment of the present application.
Fig. 3 is a cross-sectional view of a raw stock bin, heat exchanger, superheater and converter in an embodiment of the present application.
Fig. 4 is an enlarged view of a portion a in fig. 1.
Fig. 5 is a cross-sectional view of the portion B of fig. 1 taken along line C-C.
Fig. 6 is an enlarged view of the portion D in fig. 2.
Reference numerals illustrate: 1. a heat conduction device; 11. heat conducting oil; 12. a circulation pump; 13. a heating furnace; 14. an oil tank; 15. a first incubator; 151. an electric heating tube; 152. a control switch; 16. a second incubator; 17. an oil guide pipe; 18. heating the microtube; 181. a shunt section; 182. a heating section; 183. the first spacer bush; 184. heating pipes; 19. an oil outlet pipe; 2. a raw material bin; 3. a heat exchanger; 31. an inner cavity; 32. an outer cavity; 4. a superheater; 41. a superheated body; 5. a converter; 51. a reaction body; 6. a cooler; 7. a separator; 71. an air outlet pipe; 72. a liquid outlet pipe; 8. a pressure swing adsorber; 81. a hydrogen pipe; 82. a desorption gas pipe; 9. a storage tank; 91. a liquid phase spectrometer; 92. a first charging tank; 921. a first valve; 93. a second charging tank; 931. a second valve; 94. three-way ball valve; 941. a first port; 942. a second port; 943. a third port; 95. a filter assembly; 951. a first mounting dish; 9511. a first connection portion; 9512. a first plug-in connection; 952. a second mounting dish; 9521. a second connecting portion; 9522. a second plug-in connection; 9523. filtering the dish; 9524. a filtering membrane; 9525. a rubber ring.
Detailed Description
The application is described in further detail below with reference to fig. 1-6.
The embodiment of the application discloses a stepwise slow temperature-changing methanol hydrogen production line. Referring to fig. 1 and 2, a stepped slow temperature-changing methanol hydrogen production line comprises a raw material bin 2, a heat exchanger 3, a superheater 4 and a converter 5 which are sequentially connected, and further comprises a cooler 6, a separator 7 and a pressure swing adsorber 8 which are sequentially connected. The raw material bin 2 is internally provided with methanol and desalted water as hydrogen production raw materials. The raw material bin 2 is connected with a negative pressure pump, and when hydrogen production is carried out through a production line, raw materials in the raw material bin 2 are drained into the heat exchanger 3 under the action of the negative pressure pump. In this embodiment, the ratio of methanol to desalted water in the raw material bin 2 is 1:1.8. in the ratio, the amount of the methanol is smaller than the desalted water ratio, and is mainly set according to the actual production requirement, and the reaction degree of the methanol is improved by increasing the desalted water ratio so that the methanol can fully react.
Referring to fig. 2 and 3, the heat exchanger 3 includes an inner chamber 31 and an outer chamber 32, and the raw material passes through the outer chamber 32 of the heat exchanger 3, is preheated by a heat exchange medium in the inner chamber 31, and then enters the superheater 4 to be heated. The raw material heated by the superheater 4 forms steam, which is led into the converter 5 for catalytic fission. Ideally, the feedstock is catalytically fissionally formed to 75% hydrogen, 24% carbon dioxide and other minor gases. The formed mixed gas is then introduced into the inner cavity 31 of the heat exchanger 3 and serves as a heat exchange medium to preheat the raw material entering the outer cavity 32 of the heat exchanger 3, thereby playing a role in saving resources. Therefore, in the initial stage of hydrogen production, there is no heat exchange medium in the inner chamber 31 of the heat exchanger 3, and the first methanol and desalted water form a recyclable mixed gas via the converter 5, and then the mixed gas enters the inner chamber 31 of the heat exchanger 3 to be used as the heat exchange medium. The mixed gas flows from the inner cavity 31 of the heat exchanger 3 to the cooler 6 for cooling, and the cooled mixed gas is led to the separator 7 and separated into methanol which is not completely converted, desalted water and gas mainly containing hydrogen under the action of the separator 7. And finally introducing the gas containing hydrogen into a pressure swing adsorber 8 for purification to obtain high-purity hydrogen and other desorption gases.
Referring to fig. 1 and 2, the separator 7 is connected to an outlet pipe 71 and a liquid outlet pipe 72, the outlet pipe 71 is connected to the pressure swing adsorber 8, and the gas containing hydrogen separated by the separator 7 enters the pressure swing adsorber 8 through the outlet pipe 71. The liquid outlet pipe 72 is connected with a storage tank 9, and the methanol and desalted water which are not completely converted are conveyed from the liquid outlet pipe 72 into the storage tank 9. The proportion of methanol and desalted water which are not completely converted into the storage tank 9 is affected due to the influence of methanol volatilization, catalyst deactivation, equipment corrosion and the like of the raw materials. The liquid phase spectrometer 91, the first charging tank 92 and the second charging tank 93 are connected to the storage tank 9. The first charging tank 92 is internally provided with methanol, and a first valve 921 is arranged between the first charging tank 92 and the storage tank 9; the second charging tank 93 is filled with desalted water, and a second valve 931 is arranged between the second charging tank 93 and the storage tank 9. After the mixed liquid in the storage tank 9 is collected to a certain degree, the liquid phase spectrometer 91 is started, part of the mixed liquid is extracted into the storage tank 9 through an infusion pump of the liquid phase spectrometer 91, and the mixed liquid enters a detector of the liquid phase spectrometer 91 for detection. When an operator analyzes the detection result and the methanol content in the storage tank 9 is low, adding methanol by opening the first valve 921 until the ratio of the methanol to the desalted water in the storage tank 9 reaches the ratio of the methanol to the desalted water in the raw material bin 2; when the desalted water content in the storage tank 9 is low, the second valve 931 is opened to add the desalted water until the ratio of the methanol to the desalted water in the storage tank 9 reaches the ratio of the methanol to the desalted water in the raw material bin 2, so that the hydrogen yield of the whole production line is in a controllable range.
Referring to fig. 1 and 4, the storage tank 9 is connected with a three-way ball valve 94, the three-way ball valve 94 includes a first port 941, a second port 942, and a third port 943, the first port 941 is communicated with the storage tank 9, the second port 942 is connected with the liquid phase spectrometer 91, and the third port 943 is communicated with the raw stock bin 2. The storage tank 9 is communicated with the liquid phase spectrometer 91, the mixed liquid in the storage tank 9 is detected by the liquid phase spectrometer 91, and when the proportion of methanol to desalted water is the same as that of the raw material bin 2, the storage tank 9 is communicated with the raw material bin 2. Through the action of the negative pressure pump, the mixed liquid in the storage tank 9 is led into the raw material bin 2 for reuse, and the effect of saving resources is achieved.
Referring to fig. 1 and 4, since the purity of the sample is required to be high when the liquid spectrometer 91 detects the sample, a filter unit 95 is installed between the storage tank 9 and the first port 941, and the mixed liquid entering the liquid spectrometer 91 is filtered by the filter unit 95.
Referring to fig. 1 and 5, the filter assembly 95 includes a first mounting dish 951 and a second mounting dish 952 that are inserted into each other, the first mounting dish 951 including a first connection portion 9511 and a first insertion portion 9512, and the second mounting dish 952 including a second connection portion 9521 and a second insertion portion 9522. The first plug-in connection portion 9512 and the second plug-in connection portion 9522 are both , the first connection portion 9511 is in sealing connection with a pipeline connected with the storage tank 9, the second plug-in connection portion 9522 is plugged with the first plug-in connection portion 9512 to form a filter dish 9523, a cavity is formed in the filter dish 9523, a filter membrane 9524 is arranged in the cavity, the filter membrane 9524 is made of polyether sulfone materials, and the second connection portion 9521 is in sealing connection with the pipeline connected with the first through hole 941 on the three-way ball valve 94. The mixed liquid in the storage tank 9 enters a filter 9523, is filtered by a filter membrane 9524, and then enters a liquid phase spectrometer 91 for detection. In this embodiment, the first connection portion 9511 and the storage tank 9, and the second connection portion 9521 and the pipeline connected to the three-way ball valve 94 are sealed in a manner of combining interference fit and a hoop, so that the filter assembly 95 is convenient to detach, and the filter membrane 9524 is replaced. The rubber ring 9525 is wrapped outside the filter vessel 9523, the connection position of the first plug-in connection portion 9512 and the second plug-in connection portion 9522 is fixed through the tightening effect of the rubber ring, and meanwhile the connection position of the first plug-in connection portion 9512 and the second plug-in connection portion 9522 can be sealed, so that external impurities are reduced from entering the filter vessel 9523, and pollution is caused to the filter membrane 9524. In this embodiment, rubber ring 9525, first mounting dish 951 and second mounting dish 952 are all made of medical grade plastic material, reducing the secondary contamination of the passing methanol and desalted water by filter assembly 95 itself.
Referring to fig. 1, the gas separated by the separator 7 enters a pressure swing adsorber 8, and is purified to form high-purity hydrogen and desorption gas. The pressure swing adsorber 8 is connected with a hydrogen pipe 81 and a desorption pipe 82, the stored hydrogen is collected through the hydrogen pipe 81, and the desorption pipe 82 outputs other waste gases.
Referring to fig. 3 and 6, the converter 5 includes a reactant 51, the superheater 4 includes a superheated body 41, and the converter 5 and the superheater 4 need to be heated during operation, so the production line further includes a heat conduction device 1, and the heat conduction device 1 provides heat energy for the superheated body 41 and the reactant 51.
Referring to fig. 2 and 6, the heat conduction device 1 includes a circulation pump 12, a heating furnace 13, an oil tank 14, a first heat insulation box 15 and a second heat insulation box 16, the oil tank 14 is fixed in the heating furnace 13, an ignition head is arranged on the heating furnace 13, and the heat conduction oil 11 is filled in the oil tank 14 and the first heat insulation box 15. The exhaust gas output by the desorption gas pipe 82 contains a small amount of combustible gas, the heating furnace 13 is connected with the desorption gas pipe 82, and the exhaust gas discharged by the desorption gas pipe 82 is used as fuel of the heating furnace 13, the desorption gas in the heating furnace is ignited by the ignition head, and the burnt fuel can heat the heat conduction oil 11 in the oil tank 14. In this embodiment, the oil tank 14 is made of a high temperature resistant material.
Referring to fig. 2 and 6, the circulation pump 12 is in communication with the oil tank 14, and the heat transfer oil 11 in the oil tank 14 enters the first insulation tank 15 under the action of the circulation pump 12.
Referring to fig. 3 and 6, the first insulation can 15 is connected with an oil guide pipe 17, the oil guide pipe 17 is connected with a plurality of heating microtubes 18, the heating microtubes 18 comprise a shunt section 181 and a heating section 182 which are connected with each other, and the shunt section 181 is communicated with an outlet of the oil guide pipe 17. The diversion section 181 is positioned in the second insulation can 16 to reduce heat loss of the heat conduction oil 11. The heating sections 182 of the heating microtubes 18 are sequentially wound on the peripheral wall of the reaction body 51, and the first spacer 183 is sleeved outside the reaction body 51 and used for isolating the heating sections 182 so as to prevent the condition that the heating sections 182 directly expose scalding staff. The heating section 182 of each heating microtube 18 is extended with a heating tube 184, the heating tube 184 being coiled in a spiral fashion within the superheater 41. The shunt section 181 and the heating section 182 and the heating pipe 184 are wrapped with heat insulation sleeves in the direct exposure stage, so that the condition of scalding workers is reduced.
Referring to fig. 2 and 3, a plurality of heating pipes 184 are connected to the same oil outlet pipe 19, and the oil outlet pipe 19 is connected to the circulation pump 12. The heat conduction oil 11 is pressurized from the oil tank 14 and the first heat insulation box 15 through the circulating pump 12 and enters different heating microtubes 18, the heat conduction oil 11 in the shortest shunt section 181 firstly enters the heating section 182 connected with the heat conduction oil 11 after passing through the shunt section 181 of each heating microtube 18, the heat conduction oil 11 enters the heating pipe 184 after passing through the heating section 182, the heat conduction oil 11 in the heating pipe 184 enters the oil outlet pipe 19 after being conducted, and finally the heat conduction oil 11 of the oil outlet pipe 19 circulates to the oil tank 14 and is recycled through heating.
Referring to fig. 3 and 6, the split sections 181 of the heating microtubes 18 are located in the second incubator 16 and sequentially arranged from top to bottom, each split section 181 is provided as a pipeline including a spiral portion, and the length of the pipeline of the spiral section on each split section 181 sequentially increases from top to bottom, so that the length of the corresponding split section 181 sequentially increases. The heating sections 182 connected with the shortest diversion sections 181 are firstly filled with the heat conduction oil 11, a plurality of heating sections 182 are sequentially filled with the heat conduction oil 11 to heat the reaction body 51, so that the temperature of the reaction body 51 is slowly increased, the condition that the rapid temperature rise of the reaction body 51 affects the catalyst is reduced, the condition that the internal stress of the catalyst material is overlarge and the internal structure of the catalyst material system is disintegrated and damaged is reduced, and the service life of the catalyst is prolonged.
Referring to fig. 3 and 6, in the present embodiment, the oil guide pipe 17, the heating microtube 18, the heating pipe 184 and the oil outlet pipe 19 are made of heat-insulating and corrosion-preventing materials, which has the effects of reducing heat loss and improving safety.
Referring to fig. 2 and 3, an electrothermal tube 151 is disposed in the first insulation can 15, and the electrothermal tube 151 is electrically connected with a control switch 152. The amount of exhaust gas discharged from the desorption gas pipe 82 does not reach the required amount of the production line, and when the fuel of the heating furnace 13 is insufficient, the temperature of the oil tank 14 is slowly lowered, resulting in a subsequent decrease in the temperature in the reactant 51. The temperature detector is installed on the converter 5, the detection end of the temperature detector stretches into the reactant 51, when the temperature detector detects that the temperature in the reactant 51 is lower than the set temperature of the system, the system control switch 152 is turned on, the electric heating tube 151 is electrified to heat the heat conduction oil 11 in the first heat preservation box 15, and the heat conduction oil 11 continuously provides heat energy for the converter 5 and the superheater 4.
Referring to fig. 1, the methanol to hydrogen production line has high safety requirements, and operators need to detect the methanol to hydrogen production line regularly so as to avoid large-area methanol leakage. The methanol content in the air around the methanol hydrogen production line is generally detected through manual timing, the detection frequency is generally once for 2 hours, the detection is frequent, the time and the labor are consumed, a plurality of methanol detectors can be connected to the whole production line, the production line is detected in real time through the methanol detectors, meanwhile, the methanol detectors are connected with alarms, when the methanol detectors detect abnormal conditions, the alarms are started, operators are timely reminded of safety maintenance, and the occurrence probability of dangerous conditions is reduced.
The embodiment of the application relates to a stepwise slow temperature-changing methanol hydrogen production line, which has the implementation principle that: the raw materials in the raw material bin 2 are preheated by the heat exchanger 3 and then heated by the superheater 4, and the heated raw materials are introduced into the converter 5 for conversion. The mixed gas formed by conversion contains larger heat, the mixed gas is used as a heat exchange medium of the heat exchanger 3, passes through the heat exchanger 3 again, and part of heat is still stored in the mixed gas passing through the heat exchanger 3 and enters the cooler 6 for cooling. The cooled mixture is introduced into a separator 7, washed and separated. After separation by the separator 7, mixed gas containing more hydrogen, and methanol and desalted water which are not completely converted are formed, the methanol and the desalted water which are not completely converted are collected into the storage tank 9, and the mixed gas enters the pressure swing adsorber 8 for storage.
After the mixed liquor in the storage tank 9 is collected to a certain degree, the extracted part is detected by the liquid phase spectrometer 91, and methanol or desalted water is supplemented by the first feeding tank 92 and the second feeding tank 93, so that the proportion of the mixed liquor methanol and the desalted water in the storage tank 9 is the same as that in the raw material bin 2, and finally the mixed liquor methanol and the desalted water are led into the raw material bin 2 for reuse.
The heat conduction device 1 provides heat energy for the converter 5 and the superheater 4, the pressure swing adsorber 8 produces high-purity hydrogen and desorption gas after being lifted, and the desorption gas is introduced into the heating furnace 13 and is used as fuel for waste utilization, and the oil tank 14 is heated. When the fuel in the heating furnace 13 is insufficient, the heat conduction oil 11 in the first heat insulation box 15 is heated by the electric heating tube 151, and the heated heat conduction oil 11 slowly heats the reactant 51 through the heating microtube 18. The heat transfer oil 11 enters the heating pipe 184 to heat the superheater 41. After the heat conduction oil 11 is used, the heat conduction oil sequentially enters the oil tank 14 and the first heat insulation box 15 through the circulating pump 12 to be heated, so that a circulating heating system is formed.
The above embodiments are not intended to limit the scope of the present application, so: all equivalent changes in structure, shape and principle of the application should be covered in the scope of protection of the application.
Claims (6)
1. The utility model provides a cascaded slow alternating temperature methyl alcohol hydrogen manufacturing production line, the production line is including former feed bin (2), heat exchanger (3), superheater (4) and converter (5) that connect gradually, the production line still includes cooler (6), separator (7), pressure swing adsorption ware (8) and heat conduction device (1), converter (5) include reaction body (51), its characterized in that: the heat conduction device (1) comprises an oil conduction pipe (17), the oil conduction pipe (17) is connected with a plurality of heating microtubes (18), each heating microtube (18) is divided into a heating section (182) and a shunting section (181), the heating sections (182) of the heating microtubes (18) are uniformly wound on the reaction body (51), and the shunting sections (181) of the heating microtubes (18) are positioned between the reaction body (51) and the heat conduction device (1) and sequentially increase in length;
the separator (7) is connected with an air outlet pipe (71) and a liquid outlet pipe (72), the air outlet pipe (71) is connected with the pressure swing adsorber (8), the liquid outlet pipe (72) is connected with a storage tank (9), and the storage tank (9) is connected with a liquid phase spectrometer (91);
the storage tank (9) is connected with a first feeding tank (92) and a second feeding tank (93), a first valve (921) is arranged between the storage tank (9) and the first feeding tank (92), and a second valve (931) is arranged between the storage tank (9) and the second feeding tank (93);
the storage tank (9) is connected with a three-way ball valve (94), the three-way ball valve (94) comprises a first through hole (941), a second through hole (942) and a third through hole (943), the first through hole (941) is connected with the storage tank (9), the second through hole (942) is connected with a liquid phase spectrometer (91), the third through hole (943) is connected with a raw material bin (2), and a filtering component (95) is detachably connected between the storage tank (9) and the first through hole (941);
a plurality of heating microtubes (18) are kept away from the one end of leading oil pipe (17) extends there is heating pipe (184), heating pipe (184) spiral is in superheater (4), heating pipe (184) are kept away from the one end of leading oil pipe (17) is connected with out oil pipe (19), go out oil pipe (19) and keep away from the one end of heating pipe (184) is connected with circulating pump (12), circulating pump (12) and oil tank (14) intercommunication.
2. The stepwise slow temperature changing methanol hydrogen production line according to claim 1, wherein: the heat conduction device (1) comprises a heating furnace (13), an oil tank (14) is arranged in the heating furnace (13), a desorption air pipe (82) and a hydrogen pipe (81) which can discharge combustible fuel are connected to the pressure swing adsorption device (8), the desorption air pipe (82) is connected with the heating furnace (13) to supply fuel for the heating furnace (13), and heat conduction oil (11) which supplies heat sources for the reaction body (51) and the superheater (4) is filled in the oil tank (14).
3. The stepwise slow temperature changing methanol hydrogen production line according to claim 2, wherein: the heat conduction device (1) further comprises a first heat insulation box (15) and heat conduction oil (11), one end of the first heat insulation box (15) is connected with the oil tank (14), an electric heating tube (151) is arranged in the first heat insulation box (15), the electric heating tube (151) is electrically connected with a control switch (152), the converter (5) is connected with a temperature detector, and the temperature detector is electrically connected with the control switch (152); the other end of the first heat preservation box (15) is connected with the oil guide pipe (17), a second heat preservation box (16) is connected between the first heat preservation box (15) and the reaction body (51), and a diversion section (181) of the heating microtube (18) and the oil guide pipe (17) are positioned in the second heat preservation box (16).
4. The stepwise slow temperature changing methanol hydrogen production line according to claim 1, wherein: the utility model provides a filter subassembly (95) is including filtration membrane (9524) and first mounting dish (951) and second mounting dish (952) of pegging graft each other, be formed with the cavity after first mounting dish (951) and second mounting dish (952) peg graft, the whole that forms is filtration dish (9523), filtration membrane (9524) are located the cavity, filtration dish (9523) outer wall circumference upward parcel has rubber circle (9525), first mounting dish (951) keep away from the one end of second mounting dish (952) with storage tank (9) sealing connection, one end that second mounting dish (952) kept away from first mounting dish (951) with tee bend ball valve (94) sealing connection.
5. The stepwise slow temperature changing methanol hydrogen production line according to claim 4, wherein: the filtering membrane (9524) is made of polyethersulfone material.
6. The stepwise slow temperature changing methanol hydrogen production line according to claim 4, wherein: the first mounting dish (951), the second mounting dish (952) and the rubber ring (9525) are all made of medical plastic.
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