CN220976588U - Methanol steam cracking hydrogen production device with fused salt energy storage system - Google Patents
Methanol steam cracking hydrogen production device with fused salt energy storage system Download PDFInfo
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- CN220976588U CN220976588U CN202322899966.0U CN202322899966U CN220976588U CN 220976588 U CN220976588 U CN 220976588U CN 202322899966 U CN202322899966 U CN 202322899966U CN 220976588 U CN220976588 U CN 220976588U
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- 150000003839 salts Chemical class 0.000 title claims abstract description 273
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 147
- 229910052739 hydrogen Inorganic materials 0.000 title claims abstract description 57
- 239000001257 hydrogen Substances 0.000 title claims abstract description 57
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 38
- 238000004146 energy storage Methods 0.000 title claims abstract description 25
- 238000004230 steam cracking Methods 0.000 title claims description 8
- 238000003860 storage Methods 0.000 claims abstract description 90
- 238000000197 pyrolysis Methods 0.000 claims abstract description 62
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 61
- 239000007788 liquid Substances 0.000 claims abstract description 56
- 239000007789 gas Substances 0.000 claims abstract description 54
- 238000010521 absorption reaction Methods 0.000 claims abstract description 45
- 239000002994 raw material Substances 0.000 claims abstract description 45
- 238000002156 mixing Methods 0.000 claims abstract description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- 238000009834 vaporization Methods 0.000 claims abstract description 30
- 230000008016 vaporization Effects 0.000 claims abstract description 29
- 238000004458 analytical method Methods 0.000 claims abstract description 9
- 238000011033 desalting Methods 0.000 claims abstract description 6
- 238000010992 reflux Methods 0.000 claims description 25
- 238000010612 desalination reaction Methods 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 5
- 230000005611 electricity Effects 0.000 abstract description 8
- 238000000034 method Methods 0.000 description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 238000005336 cracking Methods 0.000 description 5
- 150000002431 hydrogen Chemical class 0.000 description 4
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 description 4
- VWDWKYIASSYTQR-UHFFFAOYSA-N sodium nitrate Chemical compound [Na+].[O-][N+]([O-])=O VWDWKYIASSYTQR-UHFFFAOYSA-N 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 239000012495 reaction gas Substances 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 238000003795 desorption Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 2
- 239000004323 potassium nitrate Substances 0.000 description 2
- 235000010333 potassium nitrate Nutrition 0.000 description 2
- 239000004317 sodium nitrate Substances 0.000 description 2
- 235000010344 sodium nitrate Nutrition 0.000 description 2
- LPXPTNMVRIOKMN-UHFFFAOYSA-M sodium nitrite Chemical compound [Na+].[O-]N=O LPXPTNMVRIOKMN-UHFFFAOYSA-M 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 1
- 230000001133 acceleration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- XGZVUEUWXADBQD-UHFFFAOYSA-L lithium carbonate Chemical compound [Li+].[Li+].[O-]C([O-])=O XGZVUEUWXADBQD-UHFFFAOYSA-L 0.000 description 1
- 229910052808 lithium carbonate Inorganic materials 0.000 description 1
- 229910001629 magnesium chloride Inorganic materials 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 229910000027 potassium carbonate Inorganic materials 0.000 description 1
- 239000001103 potassium chloride Substances 0.000 description 1
- 235000011164 potassium chloride Nutrition 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 229910000029 sodium carbonate Inorganic materials 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 235000010288 sodium nitrite Nutrition 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a methanol vapor pyrolysis hydrogen production device with a fused salt energy storage system, which comprises a cold molten salt storage tank, wherein a cold fused salt pump in the cold molten salt storage tank is connected with a fused salt electric heater and a mixed salt tank, and the fused salt electric heater is connected with a hot fused salt storage tank; a hot molten salt pump in the hot molten salt storage tank is connected with the salt mixing tank; the cold molten salt storage tank, the salt mixing tank, the heat conducting oil pump and the vaporization superheater are respectively connected with the oil salt heat exchanger; the vaporization superheater is connected with the conversion reactor; the methanol storage tank, the desalting water tank and the preheater are respectively connected with the raw material liquid storage tank; the preheater is respectively connected with the vaporization superheater, the conversion reactor and the condenser; the condenser is connected with a pyrolysis gas water scrubber which is respectively connected with a pyrolysis gas buffer tank and a raw material liquid storage tank; the pyrolysis gas buffer tank is respectively connected with the raw material liquid storage tank and the absorption tower; the absorption tower is respectively connected with the analysis tower and the hydrogen storage tank. The device can utilize valley electricity, wind power and photovoltaic to discard electricity and store energy, and has stable operation, high hydrogen production efficiency and high economy.
Description
Technical Field
The utility model relates to a methanol vapor pyrolysis hydrogen production device with a fused salt energy storage system, which adopts fused salt as an energy storage medium and heat conducting oil as a heat carrying medium to carry out the methanol vapor pyrolysis hydrogen production.
Background
The hydrogen energy fuel cell automobile is increasingly focused as a green and environment-friendly transportation tool, the demand of high-purity hydrogen is gradually increased, and higher requirements are put on the efficiency, economy, flexibility and safety of the hydrogen production process and device. The methanol steam cracking and pressure swing adsorption are suitable for small and medium-scale distributed hydrogen production routes, and have the advantages of low investment, low energy consumption, readily available raw materials, convenience in transportation and storage and modularization.
With the acceleration of the electrification process in China, the social power load demand continuously and rapidly increases, the installed ratio of new energy power generation mainly based on wind power and photovoltaic is rapidly increased, and high-proportion new energy grid connection becomes a necessary trend. The new energy has the characteristics of large volatility and difficult regulation, and the large-scale energy storage and conversion of the molten salt into hydrogen energy are feasible energy storage technologies, so that the output characteristics of the new energy power station can be optimized. In the existing hydrogen production process by methanol vapor pyrolysis, natural gas or electric energy is mostly adopted as a process heat source, so that the production cost is high, and therefore, the hydrogen production device by methanol vapor pyrolysis needs to be provided for improving the economy and flexibility in the hydrogen production process.
Disclosure of utility model
The utility model aims at: aiming at the defects of the prior art, the methanol vapor pyrolysis hydrogen production device with the molten salt energy storage system can utilize valley electricity or wind power and photovoltaic waste electricity energy storage for the methanol vapor pyrolysis hydrogen production. In the running process of the system, molten salt is used as an energy storage medium, and heat conducting oil is used as a heat carrying medium, so that the system has the characteristics of stable running parameters, high hydrogen production efficiency and high running cost economy, and has great market value.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
The methanol vapor pyrolysis hydrogen production device with the molten salt energy storage system comprises a cold molten salt storage tank, a molten salt electric heater, a hot molten salt storage tank, a salt mixing tank, a heat conducting oil tank, an oil salt heat exchanger, a methanol storage tank, a desalting water tank, a raw material liquid storage tank, a preheater, a vaporization superheater, a conversion reactor, a condenser, a pyrolysis gas water scrubber, a pyrolysis gas buffer tank, an absorption tower, an analysis tower and a hydrogen storage tank.
In the utility model, the cold molten salt storage tank, the molten salt electric heater and the hot molten salt storage tank are used for converting electric energy into heat energy and storing the heat energy; the salt mixing tank, the heat conducting oil pump and the oil salt heat exchanger are used for releasing heat energy stored by molten salt for the hydrogen production process; the raw material liquid storage tank of the methanol storage tank and the desalted water tank is used for storing raw materials required by hydrogen production; the preheater, the vaporization superheater, the conversion reactor, the pyrolysis gas water scrubber, the pyrolysis gas buffer tank, the absorption tower and the desorption tower are used for cracking and purifying the raw material liquid to prepare hydrogen.
In the utility model, a cold molten salt pump is arranged in the cold molten salt storage tank; a hot molten salt pump is arranged in the hot molten salt storage tank; the cold molten salt pump is connected with the molten salt electric heater through a pipeline; the molten salt electric heater is connected with the hot molten salt storage tank through a pipeline; the cold molten salt pump is connected with the salt mixing tank through a pipeline; the hot molten salt pump is connected with the salt mixing tank through a pipeline. The cold molten salt storage tank, the molten salt electric heater and the hot molten salt storage tank are connected through connecting pipelines to form a molten salt energy storage system.
In the utility model, a cold-melt salt pump outlet valve and a cold-melt salt pump return pipe are arranged on a cold-melt salt pump outlet pipeline, and a cold-melt salt pump return valve is arranged on the cold-melt salt pump return pipe; the hot molten salt pump outlet valve and the hot molten salt pump reflux pipe are arranged on the hot molten salt pump outlet pipeline, and the hot molten salt pump reflux pipe is provided with the hot molten salt pump reflux valve; an electric heater cold molten salt inlet valve is arranged between the cold molten salt pump outlet valve and the molten salt electric heater, and a salt mixing tank cold molten salt inlet valve is arranged between the cold molten salt pump outlet valve and the salt mixing tank; and a hot molten salt inlet valve of the salt mixing tank is arranged between the hot molten salt pump outlet valve and the salt mixing tank. In the valley period or the power-off period, the cold molten salt pump conveys cold molten salt in the cold molten salt storage tank to the molten salt electric heater, and the cold molten salt (160-300 ℃) is heated by the molten salt electric heater to become hot molten salt (400-600 ℃) which enters the hot molten salt storage tank for storage.
In the utility model, the salt mixing tank, the heat conducting oil pump, the oil salt heat exchanger, the vaporization superheater and the conversion reactor are connected through pipelines. And a closed molten salt circulation loop is formed among the cold molten salt storage tank, the molten salt electric heater, the hot molten salt storage tank, the salt mixing tank and the oil salt heat exchanger by connecting pipelines. And a closed heat conduction oil circulation loop is formed among the heat conduction oil tank, the oil salt heat exchanger, the vaporization superheater and the conversion reactor by connecting pipelines. Under the working condition of hydrogen production operation, the hot molten salt is pumped to a salt mixing tank from a hot molten salt storage tank, is mixed with cold molten salt from the cold molten salt storage tank in the salt mixing tank and is delivered to an oil salt heat exchanger after being delivered to the oil salt heat exchanger after being pressurized by a heat conducting oil pump, the hot molten salt and the heat conducting oil exchange heat in the oil salt heat exchanger, and the heat of the molten salt is transferred to the heat conducting oil.
In the utility model, a heat conduction oil pump is arranged behind the heat conduction oil tank, and the heat conduction oil pump is connected with an oil salt heat exchanger through a pipeline; the salt mixing tank is connected with the oil-salt heat exchanger through a pipeline; the oil salt heat exchanger is connected with the cold molten salt storage tank through a pipeline; the oil salt heat exchanger is connected with the vaporization superheater through a pipeline, and the vaporization superheater is connected with the conversion reactor through a pipeline. The heat transfer oil is heated to about 300 ℃ after passing through the oil-salt heat exchanger, and is sent to the vaporization superheater from the oil-salt heat exchanger, and is sent to the conversion reactor after the vaporization superheater releases part of heat and the temperature is reduced to about 280 ℃, and is sent to the heat transfer oil tank for the next circulation through a pipeline after the conversion reactor continuously releases heat.
In the utility model, the methanol storage tank is connected with the raw material liquid storage tank through a pipeline, and a methanol metering pump and a methanol stop valve are arranged on the pipeline; the desalting water tank is connected with the raw material liquid storage tank through a pipeline, and a desalting water metering pump and a desalting water stop valve are arranged on the pipeline; the raw material liquid storage tank is connected with the preheater through a pipeline, and a raw material liquid metering pump is arranged on the pipeline. Under the working condition of hydrogen production, methanol and desalted water are pumped into a raw material liquid storage tank from a methanol storage tank and a desalted water tank respectively, mixed in the raw material liquid storage tank, pumped into a preheater through a raw material liquid metering pump, and subjected to heat exchange with cracking gas after reaction in the preheater.
In the utility model, the preheater is connected with the vaporization superheater through a pipeline; the vaporization superheater is connected with the conversion reactor through a pipeline. Under the working condition of hydrogen production, the raw material liquid is heated by the preheater and then enters the vaporization superheater, vaporization is carried out in the vaporization superheater, the raw material liquid is overheated to the reaction temperature and then enters the conversion reactor, and the conversion reaction is carried out in the conversion reactor to generate cracking gas, unreacted methanol and water vapor.
In the utility model, the conversion reactor is connected with the preheater through a pipeline; the preheater is connected with the condenser through a pipeline; the condenser is connected with the pyrolysis gas water scrubber through a pipeline; the pyrolysis gas water scrubber is connected with the pyrolysis gas buffer tank through a pipeline; the pyrolysis gas water scrubber is connected with the raw material liquid storage tank through a pipeline, and a water scrubber drain valve is arranged on the pipeline; the cracking gas buffer tank is connected with the raw material liquid storage tank through a pipeline, and a drain valve of the cracking gas buffer tank is arranged on the pipeline. Under the working condition of hydrogen production, carrying out conversion reaction in a conversion reactor to generate pyrolysis gas, wherein the pyrolysis gas contains hydrogen, carbon dioxide, carbon monoxide and unreacted methanol and water vapor, the pyrolysis gas flows from the conversion reactor to a preheater, flows to a condenser after heat exchange with raw material liquid in the preheater and temperature reduction, flows to a water scrubber after condensation of reaction gas, unreacted methanol and water vapor and the like, the pyrolysis gas, water and methanol mixture are separated in the water scrubber, the pyrolysis gas after water scrubbing separation enters a pyrolysis gas buffer tank, enters an absorption tower after temporary storage of the pyrolysis gas buffer tank, the absorption tower separates carbon dioxide to produce hydrogen, the hydrogen enters a hydrogen storage tank for storage, the unreacted water and the methanol enter a raw material liquid storage tank again through a water scrubber drain valve and a pyrolysis gas buffer tank drain valve, and the absorption liquid enters an absorption liquid circulation pump for recycling after decompression and analysis of the absorption liquid.
In the utility model, the pyrolysis gas buffer tank is connected with the absorption tower through a pipeline; the absorption tower is connected with the analysis tower through a pipeline; the absorption tower is connected with the hydrogen storage tank through a pipeline; an absorption liquid recycling pipeline is arranged between the absorption tower and the analysis tower, and an absorption liquid circulating pump is arranged on the absorption liquid recycling pipeline.
In the utility model, the molten salt can be mixed molten salt of sodium nitrate and potassium nitrate, or mixed salt of sodium nitrite, sodium nitrate and potassium nitrate, or mixed salt of lithium carbonate, sodium carbonate and potassium carbonate, or mixed salt of magnesium chloride, sodium chloride and potassium chloride.
After the scheme is adopted, the beneficial effects of the utility model are as follows:
(1) The device integrates molten salt energy storage, heat exchange and pyrolysis hydrogen production processes, adopts molten salt as an energy storage medium, adopts heat transfer oil as a heat transfer medium to crack methanol and water vapor to produce hydrogen, can accurately control reaction temperature, and has higher production efficiency and hydrogen quality.
(2) The fused salt energy storage device is configured, reasonable utilization of energy is realized by utilizing the difference of electricity abandoning or peak-valley electricity price of photovoltaic and wind power, and the method has higher economical efficiency.
(3) The device is mainly composed of methanol and water, and is wide in raw material source and convenient to popularize in the market.
(4) The system has simple process flow, the device can be miniaturized, and the method is suitable for a distributed hydrogen production system.
Drawings
The accompanying drawings are included to provide a further understanding of the utility model, and are incorporated in and constitute a part of this specification.
FIG. 1 is a schematic diagram of a system for producing hydrogen from methanol steam cracking with a molten salt energy storage system according to the present utility model, wherein: 101-cold molten salt storage tank, 108-molten salt electric heater, 110-hot molten salt storage tank, 117-salt mixing tank, 118-heat conducting oil tank, 121-oil salt heat exchanger, 122-methanol storage tank, 123-desalination water tank, 128-raw material liquid storage tank, 130-preheater, 131-vaporization superheater, 132-conversion reactor, 133-condenser, 135-pyrolysis gas water scrubber, 136-pyrolysis gas buffer tank, 140-absorption tower, 141-resolution tower and 142-hydrogen storage tank;
102-cold molten salt pump, 111-hot molten salt pump, 103-cold molten salt pump outlet valve, 105-cold molten salt pump reflux valve, 104-cold molten salt pump reflux pipe, 112-hot molten salt pump outlet valve, 113-hot molten salt pump reflux valve, 114-hot molten salt pump reflux pipe and 116-cold molten salt reflux pipe; 106-an electric heater cold molten salt inlet valve, 107-a mixed salt tank cold molten salt inlet valve and 115-a mixed salt tank hot molten salt inlet valve; 119-heat conduction oil pump, 124-methanol metering pump, 125-methanol stop valve, 126-desalted water metering pump, 127-desalted water stop valve and 129-raw material liquid metering pump; 137-a water scrubber drain valve, 138-a pyrolysis gas buffer tank drain valve, 134-a water scrubber desalted water inlet valve and 143-an absorption liquid circulating pump.
Detailed Description
The present utility model will now be described in detail with reference to the drawings and the specific embodiments thereof, wherein the exemplary embodiments and the description are for the purpose of illustrating the utility model only and are not to be construed as limiting the utility model.
As shown in fig. 1: methanol steam cracking hydrogen production device with fused salt energy storage system includes: cold molten salt storage tank 101, molten salt electric heater 108, hot molten salt storage tank 110, cold molten salt pump 102, hot molten salt pump 111, cold molten salt pump outlet valve 103, cold molten salt pump reflux valve 105, cold molten salt pump reflux pipe 104, hot molten salt pump outlet valve 112, hot molten salt pump reflux valve 113, hot molten salt pump reflux pipe 114, salt mixing tank 117, heat conducting oil tank 118, oil salt heat exchanger 121, cold molten salt reflux pipe 116, methanol storage tank 122, desalination water tank 123, raw material liquid storage tank 128, preheater 130, vaporization superheater 131, conversion reactor 132, condenser 133, pyrolysis gas water scrubber 135, pyrolysis gas buffer tank 136, absorber 140, analytical tower 141, hydrogen storage tank 142; an electric heater cold molten salt inlet valve 106, a mixed salt tank cold molten salt inlet valve 107, and a mixed salt tank hot molten salt inlet valve 115; a heat conduction oil pump 119, a methanol metering pump 124, a methanol stop valve 125, a desalted water metering pump 126, a desalted water stop valve 127 and a raw material liquid metering pump 129; a water scrubber drain valve 137, a cracked gas buffer tank drain valve 138, a water scrubber demineralized water inlet valve 134, and an absorption liquid circulation pump 143.
A cold molten salt pump 102 is arranged in the cold molten salt storage tank 101; the cold molten salt pump 102 is connected with the molten salt electric heater 108 through a pipeline; the molten salt electric heater 108 is connected with the hot molten salt storage tank 110 through a pipeline; the cold molten salt pump 102 is connected with the salt mixing tank 117 through a pipeline; the hot molten salt pump 111 is connected with the salt mixing tank 117 through a pipeline. The cold molten salt storage tank, the molten salt electric heater and the hot molten salt storage tank are connected through connecting pipelines to form a molten salt energy storage system.
An outlet pipeline of the cold molten salt pump 102 is provided with a cold molten salt pump outlet valve 103 and a cold molten salt pump reflux pipe 104, and the cold molten salt pump reflux pipe 104 is provided with a cold molten salt pump reflux valve 105; a hot molten salt pump outlet valve 112 and a hot molten salt pump reflux pipe 114 are arranged on an outlet pipeline of the hot molten salt pump 111, and a hot molten salt pump reflux valve 113 is arranged on the hot molten salt pump reflux pipe 114; an electric heater cold molten salt inlet valve 106 is arranged between the cold molten salt pump outlet valve 103 and the molten salt electric heater 108, and a salt mixing tank cold molten salt inlet valve 107 is arranged between the cold molten salt pump outlet valve 103 and the salt mixing tank 117; a salt mixing tank hot molten salt inlet valve 115 is arranged between the hot molten salt pump outlet valve 112 and the salt mixing tank 117.
A heat conduction oil pump 119 is arranged behind the heat conduction oil tank 118, and the heat conduction oil pump 119 is connected with an oil salt heat exchanger 121 through a pipeline; the oil salt heat exchanger 121 is connected with the vaporization superheater 131 through a pipeline, and the vaporization superheater 131 is connected with the conversion reactor 132 through a pipeline; the preheater 130 is connected with the vaporization superheater 131 through a pipeline; the conversion reactor 132 is connected with the preheater 130 through a pipeline; the preheater 130 is connected with the condenser 133 through a pipeline; the condenser 133 is connected with the pyrolysis gas water scrubber 135 through a pipeline; the pyrolysis gas water scrubber 135 is connected with the pyrolysis gas buffer tank 136 through a pipeline; the pyrolysis gas water scrubber 135 is connected with the raw material liquid storage tank 128 through a pipeline, and a water scrubber drain valve 137 is arranged on the pipeline; the pyrolysis gas buffer tank 136 is connected with the raw material liquid storage tank 128 through a pipeline, and a pyrolysis gas buffer tank drain valve 138 is arranged on the pipeline; the pyrolysis gas buffer tank 136 is connected with the absorption tower 140 through a pipeline; the absorption tower 140 is connected with the analysis tower 141 through a pipeline; the absorption tower 140 is connected with the hydrogen storage tank 142 through a pipeline; an absorption liquid recirculation line is provided between the absorption tower 140 and the desorption tower 141, and an absorption liquid circulation pump 143 is provided on the absorption liquid recirculation line.
In the valley period or the power-off period, the electric heater cold molten salt inlet valve 106 is opened, the cold molten salt pump 102 conveys cold molten salt in the cold molten salt storage tank 101 to the molten salt electric heater 108, the cold molten salt (160-300 ℃) is heated by the molten salt electric heater 108 to become hot molten salt (400-600 ℃) and enters the hot molten salt storage tank 110 for storage, and the purpose of storing electric energy by heat energy is achieved.
Under the working condition of hydrogen production operation of the device, the hot molten salt self-heating molten salt storage tank 110 is pressurized by the hot molten salt pump 111 and then pumped to the salt mixing tank 117, the flow of the cold molten salt and the hot molten salt is controlled by adjusting the opening of the cold molten salt inlet valve 107 of the salt mixing tank and the hot molten salt inlet valve 115 of the salt mixing tank, so that the cold molten salt and the hot molten salt are uniformly mixed in the salt mixing tank 117 and molten salt (300-350 ℃) with proper temperature is produced, the molten salt with proper temperature is sent to the oil-salt heat exchanger 121, the heat is transferred to heat conduction oil after the hot molten salt and the heat conduction oil exchange in the oil-salt heat exchanger 121, the temperature of the molten salt is reduced to be cold molten salt, and the cold molten salt returns to the cold molten salt tank through the cold molten salt return pipe 116 to prepare for the next circulation.
Under the hydrogen production operating condition of the device, the temperature of the heat conduction oil is increased to about 300 ℃ after passing through the oil-salt heat exchanger 121, the heat conduction oil is sent to the vaporization superheater 131 from the oil-salt heat exchanger 121, the temperature is reduced to about 280 ℃ after the vaporization superheater 131 releases part of heat, and the heat conduction oil is sent to the conversion reactor 132 through a pipeline after the heat release is continued in the conversion reactor 132, so that the heat conduction oil is ready for the next circulation.
Under the hydrogen production operation working condition of the device, methanol and desalted water are pumped to a raw material liquid storage tank 128 from a methanol storage tank 122 and a desalted water tank 123 respectively through a methanol metering pump 124 and a desalted water metering pump 126, the raw material liquid is mixed with unreacted methanol and water from a pyrolysis gas water washing tower 135 and a pyrolysis gas storage tank 136 in the raw material liquid storage tank 128 to form raw material liquid, the raw material liquid is pumped to a preheater 130 through the raw material liquid metering pump 129, the raw material liquid exchanges heat with pyrolysis gas from a conversion reactor 132 in the preheater 130 and increases in temperature, the raw material liquid enters a vaporization superheater 131 after being heated by the preheater 130, the raw material liquid is vaporized in the vaporization superheater 131 and enters the conversion reactor 132 after being heated to the reaction temperature, the conversion reaction gas is converted in the conversion reactor 132, the pyrolysis gas contains hydrogen, carbon dioxide, carbon monoxide and unreacted methanol and water vapor, the pyrolysis gas is sent to the preheater 130 from the conversion reactor 132, the pyrolysis gas is sent to the preheater 130 after being subjected to heat exchange with the raw material liquid, is sent to a condenser 133 after being reduced in temperature, the reaction gas and the unreacted methanol and water vapor are sent to the pyrolysis gas 135 after being condensed, the pyrolysis gas enters the absorption tower 135, the absorption tower is sent to the absorption tower through the absorption tower and the absorption tower 140 after being separated by the water tank, the absorption tower 140, the hydrogen gas is recycled to enter the absorption tower 140, and the absorption tower is recycled to the absorption tower 140, and the absorption tower is made to be absorbed by the absorption tower 140.
In the embodiment, the methanol vapor pyrolysis hydrogen production device with the fused salt energy storage system is provided, the fused salt energy storage, heat exchange and methanol vapor pyrolysis hydrogen production process are integrated, the fused salt is used as an energy storage medium, the heat conducting oil is used as a heat carrying medium for carrying out the methanol vapor pyrolysis hydrogen production, the reasonable utilization of energy is realized by utilizing the difference of the electricity discarding or peak-valley electricity price of photovoltaic and wind power, the hydrogen production cost is reduced, no pollutant is generated in the operation process, and the environment is friendly. The system has the characteristics of stable operation, high hydrogen production efficiency, high economy and miniaturization, and can be applied to a distributed hydrogen production system.
The foregoing description is only of the preferred embodiments of the utility model, and all changes and modifications that come within the meaning and range of equivalency of the structures, features and principles of the utility model are therefore intended to be embraced therein.
Claims (4)
1. The methanol vapor pyrolysis hydrogen production device with the molten salt energy storage system is characterized by comprising a cold molten salt storage tank (101), a molten salt electric heater (108), a hot molten salt storage tank (110), a salt mixing tank (117), a heat conducting oil tank (118), an oil salt heat exchanger (121), a methanol storage tank (122), a desalting water tank (123), a raw material liquid storage tank (128), a preheater (130), a vaporization superheater (131), a conversion reactor (132), a condenser (133), a pyrolysis gas water scrubber (135), a pyrolysis gas buffer tank (136), an absorption tower (140), an analysis tower (141) and a hydrogen storage tank (142);
A cold molten salt pump (102) is arranged in the cold molten salt storage tank (101); a hot molten salt pump (111) is arranged in the hot molten salt storage tank (110); the cold molten salt pump (102) is connected with the molten salt electric heater (108) through a pipeline; the molten salt electric heater (108) is connected with the hot molten salt storage tank (110) through a pipeline; the cold molten salt pump (102) is connected with the salt mixing tank (117) through a pipeline; the hot molten salt pump (111) is connected with the salt mixing tank (117) through a pipeline;
A heat conduction oil pump (119) is arranged behind the heat conduction oil tank (118), and the heat conduction oil pump (119) is connected with the oil salt heat exchanger (121) through a pipeline; the salt mixing tank (117) is connected with the oil-salt heat exchanger (121) through a pipeline; the oil-salt heat exchanger (121) is connected with the cold molten salt storage tank (101) through a pipeline;
The oil salt heat exchanger (121) is connected with the vaporization superheater (131) through a pipeline, and the vaporization superheater (131) is connected with the conversion reactor (132) through a pipeline;
The methanol storage tank (122) is connected with the raw material liquid storage tank (128) through a pipeline, and a methanol metering pump (124) and a methanol stop valve (125) are arranged on the pipeline; the desalination water tank (123) is connected with the raw material liquid storage tank (128) through a pipeline, and a desalination water metering pump (126) and a desalination water stop valve (127) are arranged on the pipeline; the raw material liquid storage tank (128) is connected with the preheater (130) through a pipeline, and a raw material liquid metering pump (129) is arranged on the pipeline;
The preheater (130) is connected with the vaporization superheater (131) through a pipeline; the preheater (130) is connected with the conversion reactor (132) through a pipeline; the preheater (130) is connected with the condenser (133) through a pipeline;
the condenser (133) is connected with the pyrolysis gas water scrubber (135) through a pipeline; the pyrolysis gas water scrubber (135) is connected with the pyrolysis gas buffer tank (136) through a pipeline; the pyrolysis gas water scrubber (135) is connected with the raw material liquid storage tank (128) through a pipeline, and a water scrubber drain valve (137) is arranged on the pipeline; the pyrolysis gas buffer tank (136) is connected with the raw material liquid storage tank (128) through a pipeline, and a pyrolysis gas buffer tank drain valve (138) is arranged on the pipeline;
The pyrolysis gas buffer tank (136) is connected with the absorption tower (140) through a pipeline; the absorption tower (140) is connected with the analysis tower (141) through a pipeline; the absorption tower (140) is connected with the hydrogen storage tank (142) through a pipeline; an absorption liquid recycling pipeline is arranged between the absorption tower (140) and the analysis tower (141), and an absorption liquid circulating pump (143) is arranged on the absorption liquid recycling pipeline.
2. The methanol steam cracking hydrogen production device with the molten salt energy storage system according to claim 1, wherein a molten salt pump outlet valve (103) and a molten salt pump reflux pipe (104) are arranged on an outlet pipeline of the molten salt pump (102), and a molten salt pump reflux valve (105) is arranged on the molten salt pump reflux pipe (104); a hot molten salt pump outlet valve (112) and a hot molten salt pump reflux pipe (114) are arranged on an outlet pipeline of the hot molten salt pump (111), and a hot molten salt pump reflux valve (113) is arranged on the hot molten salt pump reflux pipe (114); an electric heater cold molten salt inlet valve (106) is arranged between the cold molten salt pump outlet valve (103) and the molten salt electric heater (108), and a salt mixing tank cold molten salt inlet valve (107) is arranged between the cold molten salt pump outlet valve (103) and the salt mixing tank (117); a salt mixing tank hot molten salt inlet valve (115) is arranged between the hot molten salt pump outlet valve (112) and the salt mixing tank (117).
3. The methanol steam cracking hydrogen plant with molten salt energy storage system of claim 1 wherein a closed conduction oil circulation loop is formed by connecting lines among the conduction oil tank (118), the oil salt heat exchanger (121), the vaporization superheater (131) and the conversion reactor (132).
4. The methanol steam cracking hydrogen production device with a molten salt energy storage system according to claim 1, wherein a closed molten salt circulation loop is formed by connecting pipelines among the cold molten salt storage tank (101), the molten salt electric heater (108), the hot molten salt storage tank (110), the salt mixing tank (117) and the oil salt heat exchanger (121).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322899966.0U CN220976588U (en) | 2023-10-27 | 2023-10-27 | Methanol steam cracking hydrogen production device with fused salt energy storage system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322899966.0U CN220976588U (en) | 2023-10-27 | 2023-10-27 | Methanol steam cracking hydrogen production device with fused salt energy storage system |
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| CN202322899966.0U Active CN220976588U (en) | 2023-10-27 | 2023-10-27 | Methanol steam cracking hydrogen production device with fused salt energy storage system |
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2023
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