CN117339488A - Low-energy-consumption green methanol synthesis system - Google Patents
Low-energy-consumption green methanol synthesis system Download PDFInfo
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- CN117339488A CN117339488A CN202311276075.8A CN202311276075A CN117339488A CN 117339488 A CN117339488 A CN 117339488A CN 202311276075 A CN202311276075 A CN 202311276075A CN 117339488 A CN117339488 A CN 117339488A
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 228
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 58
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 57
- 238000005265 energy consumption Methods 0.000 title claims abstract description 24
- 239000001257 hydrogen Substances 0.000 claims abstract description 145
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 145
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 141
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 98
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 49
- 239000007787 solid Substances 0.000 claims abstract description 49
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 47
- 239000007789 gas Substances 0.000 claims abstract description 33
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 238000002156 mixing Methods 0.000 claims description 14
- 238000007599 discharging Methods 0.000 claims description 11
- 230000000087 stabilizing effect Effects 0.000 claims description 11
- 238000010521 absorption reaction Methods 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 239000011232 storage material Substances 0.000 claims description 4
- 239000013589 supplement Substances 0.000 claims description 4
- 239000002918 waste heat Substances 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 abstract description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 7
- 238000011161 development Methods 0.000 abstract description 6
- 238000006555 catalytic reaction Methods 0.000 abstract description 5
- 238000005516 engineering process Methods 0.000 abstract description 5
- 239000000446 fuel Substances 0.000 abstract description 4
- 230000002194 synthesizing effect Effects 0.000 abstract description 4
- 238000005984 hydrogenation reaction Methods 0.000 abstract description 3
- 238000000034 method Methods 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 239000013535 sea water Substances 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 3
- 229910052987 metal hydride Inorganic materials 0.000 description 3
- 150000004681 metal hydrides Chemical class 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 238000005868 electrolysis reaction Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000007726 management method Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- QCWXUUIWCKQGHC-UHFFFAOYSA-N Zirconium Chemical compound [Zr] QCWXUUIWCKQGHC-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 229910017052 cobalt Inorganic materials 0.000 description 1
- 239000010941 cobalt Substances 0.000 description 1
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000011033 desalting Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000011156 evaluation Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 229910052761 rare earth metal Inorganic materials 0.000 description 1
- 150000002910 rare earth metals Chemical class 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229910052726 zirconium Inorganic materials 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/153—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used
- C07C29/154—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used containing copper, silver, gold, or compounds thereof
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
- C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
- C07C29/153—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used
- C07C29/156—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used containing iron group metals, platinum group metals or compounds thereof
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- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a low-energy-consumption green methanol synthesis system, belongs to the technical field of methanol synthesis, and particularly relates to a system for synthesizing methanol capable of serving as fuel through low-energy-consumption hydrogenation catalysis by utilizing carbon dioxide discharged by ship tail gas, so as to realize a carbon circulation target. The invention consists of an electrolytic tank (1), a low-power-consumption hydrogen supply pressurizing system (2), a low-power-consumption carbon dioxide supply pressurizing system (3), a synthetic gas circulating pressurizing system (4), a methanol synthesizing device (5), a methanol gas-liquid separating device (6), a methanol purifying device (7) and a methanol storage tank (8). The invention provides a low-power-consumption green methanol synthesis system by means of a carbon capturing, storing and utilizing technology and a solid hydrogen storage technology, which can effectively solve the problem, greatly reduces the power consumption of the methanol synthesis system, and becomes an important development direction in the future energy field.
Description
Technical Field
The invention relates to the technical field of methanol synthesis, in particular to a method for synthesizing methanol capable of being used as fuel by hydrogenation catalysis with low energy consumption by utilizing carbon dioxide discharged by ship tail gas, so as to realize a carbon circulation target.
Background
With the increasing global warming emissions, the research and application of green energy has become increasingly important. Among them, methanol is attracting attention as a clean, renewable fuel. The green methanol synthesis system is a novel methanol production mode, adopts advanced technology and process, and can realize high-efficiency and low-emission methanol production. The green methanol synthesis system has wide application prospect. The method can be applied to the fields of transportation, industrial manufacture, household heating and the like, and becomes an important choice for future energy transformation. Meanwhile, the method can promote the development and utilization of renewable energy sources and promote the realization of global emission reduction targets.
The advantage of the green methanol synthesis system is that it uses renewable raw materials and energy sources. The method can utilize resources such as biomass, waste, solar energy and the like to produce the methanol, so that the dependence on non-renewable energy sources such as traditional petroleum, natural gas and the like is reduced, and the emission of greenhouse gases is effectively reduced. In addition, the green methanol synthesis system has the advantages of high efficiency, safety, controllability and the like. The novel catalyst and the reactor are adopted, so that the efficiency and the yield of methanol synthesis can be improved. Meanwhile, the method can also control parameters such as temperature, pressure and the like in the reaction process, and ensure the safety and controllability of the production process. Meanwhile, the development of the energy industry needs to balance environmental protection and economic benefits, and cannot consider only one aspect. Therefore, in the process of popularizing the green methanol synthesis system, scientific evaluation and planning are required to be made in consideration of the influence of the green methanol synthesis system on aspects of ecology, economy and the like, so that sustainable development of the green methanol synthesis system can be ensured and practical benefits are brought to society.
As global economy evolves and population grows, energy demands will become greater. Therefore, we need to take positive measures to accelerate energy transformation, optimize energy structure, promote clean energy, reduce pollution and carbon emission, so as to cope with challenges brought by energy problems.
However, the existing green methanol synthesis system has some technical problems and cost problems, especially the compression energy consumption of synthesis gas is generally high, and the energy utilization rate in the production process is greatly limited. Therefore, a low-power-consumption green methanol synthesis system is provided by relying on a carbon capturing, storing and utilizing technology and a solid hydrogen storage technology, the problem can be effectively solved, the power consumption of the methanol synthesis system is greatly reduced, the important development direction of the future energy field is realized, and the application of the green methanol synthesis system contributes to realizing the aim of sustainable development of carbon neutralization.
Disclosure of Invention
Aiming at the problems of the green methanol synthesis system, the invention provides a method and equipment for the low-energy-consumption green methanol synthesis system.
A low-energy-consumption green methanol synthesis system is a system for synthesizing methanol by using renewable energy sources or other low-carbon energy sources. The system is generally composed of a plurality of components, including an electrolytic tank (1), a low-power-consumption hydrogen supply pressurizing system (2), a low-power-consumption carbon dioxide supply pressurizing system (3), a synthesis gas circulation pressurizing system (4), a methanol synthesis device (5), a methanol gas-liquid separation device (6), a methanol purifying device (7), a methanol storage tank (8) and the like. The basic principle is that raw materials such as hydrogen, carbon dioxide and the like are subjected to chemical reaction under the action of a catalyst to generate methanol.
The system can collect carbon dioxide discharged by ship exhaust, and can synthesize methanol which can be used as fuel through hydrogenation catalysis, so as to realize the carbon circulation target.
The low-power consumption carbon dioxide supply pressurizing system (3) consists of a carbon dioxide buffer tank (31), a carbon dioxide immersed liquid booster pump (32), a carbon dioxide metering unit (33), a carbon dioxide gasifier (34) and a pressure stabilizing pipeline.
The low-power consumption carbon dioxide supply pressurizing system (3) can pressurize the liquid carbon dioxide to 4-10MPa through a carbon dioxide submerged booster pump (32);
the low-power consumption carbon dioxide supply pressurizing system (3) can gasify the pressurized liquid carbon dioxide through heat exchange by a carbon dioxide gasifier (34) and a pressure stabilizing pipeline, heat the carbon dioxide to 100-220 ℃, and stabilize the gasified carbon dioxide at 3-8MPa through the pressure stabilizing pipeline;
the low-power-consumption hydrogen supply pressurizing system (2) consists of a low-pressure solid hydrogen storage device (21), a low-pressure buffer tank (26), a high-pressure solid hydrogen storage device (22), a high-pressure buffer tank (27), a low-temperature heat exchange system (23), a high-temperature heat exchange system (24), a hydrogen charging and discharging control system (28) and a hydrogen pressurizing device (25) pressure stabilizing pipeline
The low-power hydrogen is supplied to the pressurizing system (2), after hydrogen is absorbed by the metal hydride at a lower temperature (generally room temperature) and a lower pressure, the temperature of the metal hydride material is increased to a higher temperature, and the metal hydride releases the pressurized hydrogen. The discharge pressure is temperature dependent and follows the Van' tvoff equation (lnpde=Δh/RT- Δs/T), which does not have the problem of the compression ratio limitation of conventional mechanical hydrogen compressors.
The low-power-consumption hydrogen supply pressurizing system (2) controls the low-temperature heat exchange system (23) to circulate a low-temperature medium to the low-pressure solid hydrogen storage device (21) for cooling through the hydrogen charging and discharging control system (28), and the low-pressure solid hydrogen storage device (21) starts to absorb hydrogen; after the low-pressure solid hydrogen storage device (21) reaches hydrogen absorption balance, the high-temperature heat exchange system (24) circularly heats and pressurizes the low-pressure solid hydrogen storage device (21) by a high-temperature medium, and then discharges hydrogen to the low-pressure buffer tank (26); the pressurized hydrogen enters a high-pressure solid hydrogen storage device (22) for cooling, and a low-temperature heat exchange system (23) circulates a low-temperature medium to the high-pressure solid hydrogen storage device (22), so that the high-pressure solid hydrogen storage device (22) starts to absorb hydrogen; after the high-pressure solid hydrogen storage device (22) reaches hydrogen absorption balance, the high-temperature heat exchange system (24) heats and pressurizes the high-pressure solid hydrogen storage device (22) by using a high-temperature circulating medium, and after the high-pressure solid hydrogen storage device reaches a preset pressure, the control system adjusts a corresponding valve to collect high-pressure hydrogen into a high-pressure buffer bottle (27); the hydrogen charging and discharging control system (28) automatically supplements the high-pressure hydrogen to the gas mixing device (41) according to the pressure and the gas content of the mixer.
The low-power consumption hydrogen is supplied to a low-temperature heat exchange system (23) and a high-temperature heat exchange system (24) of the pressurizing system (2), and heat sources of the low-power consumption hydrogen are provided by waste heat generated by thermocatalysis of the synthetic methanol synthesis device (5), so that the heat efficiency of the whole system can be improved. The low-power-consumption hydrogen supply pressurizing system (2) uses a connecting mode of one to three sets of low-pressure solid hydrogen storage devices (21) corresponding to one set of high-pressure solid hydrogen storage devices (22), is matched with a pressure stabilizing pipeline, can provide continuous output, and can control the pressure of released hydrogen to be 9MPa to 12MPa.
The low-power-consumption hydrogen supply pressurizing system (2) comprises a low-pressure solid hydrogen storage device (21) and a high-pressure solid hydrogen storage device (22) which are connected through a hydrogen conveying pipeline, and hydrogen control valves are arranged on the hydrogen conveying pipelines between adjacent solid hydrogen storage systems.
The low-pressure solid hydrogen storage device (21) is filled with a low-platform-pressure hydrogen storage material, can absorb hydrogen with the pressure of 1.6-3.5 MPa, and can release hydrogen with the pressure of 5-6 MPa.
The high-pressure solid hydrogen storage device (22) is filled with a high-platform-pressure hydrogen storage material, can absorb 5-6 MPa of hydrogen and can release 9-12 MPa of hydrogen.
The low-power-consumption hydrogen supply pressurizing system (2) is provided with a set of hydrogen pressurizing device (25) for supplying high-pressure hydrogen to the gas mixing device (41) in a system starting stage, and after the whole set of system stably operates, the hydrogen charging and discharging control system (28) can automatically switch to a solid hydrogen storage pressurizing mode to supplement hydrogen to the gas mixing device (41).
The low-power-consumption hydrogen supply pressurizing system (2) can automatically control a hydrogen control valve of the solid hydrogen storage system and a heat transfer medium control valve of the low-temperature heat exchange system (23) and the high-temperature heat exchange system (24) through the hydrogen charging and discharging control system (28), and the flow of hydrogen is controlled through a pressure stabilizing pipeline. A low-pressure buffer tank (26) is arranged between the low-pressure solid hydrogen storage device (21) and the high-pressure solid hydrogen storage device (22) of the low-power-consumption hydrogen supply pressurizing system (2), and a high-pressure buffer tank (27) is arranged between the high-pressure solid hydrogen storage device (22) and the gas mixing device (41) and used for stabilizing the hydrogen supply pressure;
the low-power-consumption hydrogen is supplied to a low-pressure solid-state hydrogen storage device (21), a high-pressure solid-state hydrogen storage device (22), a low-pressure buffer tank (26) and a high-pressure buffer tank (27) of the pressurizing system (2), and safety release devices are arranged on the low-pressure solid-state hydrogen storage device and the high-pressure buffer tank.
The methanol synthesis device (5) consists of a fixed bed reactor, a catalyst filling tube, a catalyst, a thermal management device and a pipeline.
The temperature of the catalyst and the reaction gas in the reactor is controlled by the thermal management device, so that the temperature of the reaction chamber is kept between 220 and 360 ℃.
The low-energy-consumption green methanol synthesis system is characterized in that one or more of cobalt, zirconium, nickel, rare earth and other elements are added into a copper-based catalyst in the methanol synthesis device (5).
Drawings
FIG. 1 is a workflow of a low power green methanol synthesis system.
In the figure, an electrolytic tank (1), a low-power-consumption hydrogen supply pressurizing system (2), a low-power-consumption carbon dioxide supply pressurizing system (3), a synthetic gas circulating pressurizing system (4), a methanol synthesis device (5), a methanol gas-liquid separation device (6), a methanol purification device (7), a methanol storage tank (8), a low-pressure solid hydrogen storage device (21), a low-pressure buffer tank (26), a high-pressure solid hydrogen storage device (22), a high-pressure buffer tank (27), a low-temperature heat exchange system (23), a high-temperature heat exchange system (24), a hydrogen charging and discharging control system (28), a hydrogen pressurizing device (25), a carbon dioxide buffer tank (31), a carbon dioxide submersible booster pump (32), a carbon dioxide metering unit (33), a carbon dioxide gasifier (34), a gas mixing device (41), a synthetic gas preheating device (42) and a synthetic gas circulating pressurizing device (43).
Detailed Description
The experimental methods used in the following examples are conventional methods unless otherwise specified.
As shown in FIG. 1, the working flow of the low-power-consumption green methanol synthesis system provided by the invention is shown.
The flow of the method of the present invention is described in connection with fig. 1:
the seawater after the sea wind power electrolysis is used for desalting is utilized for preparing hydrogen, and the purity of the hydrogen is more than or equal to 99 percent after adsorption and purification. Specifically, seawater is filtered by an RO reverse osmosis membrane to prepare fresh water, and then electrolyzed in an electrolytic tank (1) (figure 1), and hydrogen and oxygen are respectively collected at a cathode and an anode;
the hydrogen generated by electrolysis enters a low-power-consumption hydrogen supply pressurizing system (2), is pressurized by a hydrogen pressurizing device (25), and then enters a gas mixing device (41).
The tail gas discharged by the ship contains a large amount of CO2, the CO2 is collected and recovered by the CCSU system, is transported to a carbon dioxide liquid storage tank on a platform, is supplied to a pressurizing system (3) through low-power-consumption carbon dioxide, and is transported to a gas mixing device (41). Is a kind of medium.
The pressurized hydrogen and carbon dioxide are mixed in a gas mixing device (41), and the mixing mole ratio of the hydrogen to the carbon dioxide is 3:1, the synthesis gas pressure is 5MPa. Then exchanging heat with a high-temperature medium from the methanol synthesis device (5), heating to 200 ℃, and then entering the methanol synthesis device (5) for catalytic reaction, wherein the methanol synthesis reaction temperature is 450 ℃.
The heat generated during the synthesis of the methanol is transmitted to a high-temperature heat exchange system (24) to provide the hydrogen release temperature of 80 ℃ for the low-pressure solid hydrogen storage device (21) and the high-pressure solid hydrogen storage device (22) through heat exchange. The charging and discharging hydrogen control system (28) controls the switching of the high-temperature heat exchange system (24) and the low-temperature heat exchange system (23) to realize the low-power consumption pressurization of hydrogen. At the same time, after the solid state pressurization is started, the system turns off the hydrogen pressurizing device (25).
The product from the methanol synthesis device (5) is separated into unreacted synthesis gas by a methanol gas-liquid separation device (6), and the part of the synthesis gas is conveyed back to the gas mixing device (41) after being pressurized by a synthesis gas circulating and pressurizing device (43). The separated methanol solution is purified by a methanol purifying device (7) and then stored in a methanol storage tank (8), and the concentration of the methanol is 99 percent.
According to the invention, the carbon dioxide trapped by the ship tail gas and the hydrogen are subjected to catalytic reaction to prepare the methanol, and only the trapped carbon dioxide is subjected to deep purification, so that the process scheme design can be carried out according to the actual trapping amount of the carbon dioxide, the zero emission of the carbon dioxide is basically realized, and the high added value of the carbon dioxide is improved.
The invention adopts the offshore wind power to electrolyze the seawater to prepare the hydrogen, thereby not only utilizing the seawater resource on site, but also greatly saving the conveying cost and improving the energy utilization rate compared with the transmission of the power by an offshore cable.
In the invention, the solid hydrogen storage is adopted to boost the pressure of the hydrogen, so that compared with the continuous high energy consumption of a hydrogen compressor, the energy is greatly saved, in addition, the low-power consumption pressurizing system utilizes the waste heat generated by the thermocatalysis of the methanol synthesis device (5) to provide, and the heat efficiency of the system is improved.
Although the present invention has been described with reference to the foregoing embodiments, it will be apparent to those skilled in the art that modifications may be made to the embodiments described, or equivalents may be substituted for elements thereof, and any modifications, equivalents, improvements and changes may be made without departing from the spirit and principles of the present invention.
Claims (10)
1. The low-energy-consumption green methanol synthesis system is characterized by comprising an electrolytic tank (1), a low-power-consumption hydrogen supply pressurizing system (2), a low-power-consumption carbon dioxide supply pressurizing system (3), a synthesis gas circulation pressurizing system (4), a methanol synthesis device (5), a methanol gas-liquid separation device (6), a methanol purification device (7) and a methanol storage tank (8).
2. The low-energy-consumption green methanol synthesis system according to claim 1, wherein the low-energy-consumption carbon dioxide supply pressurizing system (3) is composed of a carbon dioxide buffer tank (31), a carbon dioxide submersible booster pump (32), a carbon dioxide metering unit (33) and a carbon dioxide gasifier (34);
the carbon dioxide supply pressurizing system (3) pressurizes liquid carbon dioxide to 4-6MPa through a carbon dioxide submerged booster pump (32);
the carbon dioxide supply pressurizing system (3) gasifies the pressurized liquid carbon dioxide through heat exchange by a carbon dioxide gasifier (34) and a pressure stabilizing pipeline, heats the carbon dioxide to 100-220 ℃, and stabilizes the gasified carbon dioxide at 3-5MPa through the pressure stabilizing pipeline.
3. The low energy consumption green methanol synthesis system according to claim 1, wherein the synthesis gas circulation pressurizing system (4) is composed of a gas mixing device (41), a synthesis gas preheating device (42) and a synthesis gas circulation pressurizing device (43).
4. The low-energy-consumption green methanol synthesis system according to claim 1, wherein the low-energy-consumption hydrogen supply pressurizing system (2) is composed of a low-pressure solid hydrogen storage device (21), a low-pressure buffer tank (26), a high-pressure solid hydrogen storage device (22), a high-pressure buffer tank (27), a low-temperature heat exchange system (23), a high-temperature heat exchange system (24), a hydrogen charging and discharging control system (28), a hydrogen pressurizing device (25) and a pressure stabilizing pipeline.
5. The low-energy-consumption green methanol synthesis system according to claim 4, wherein the low-energy-consumption hydrogen supply pressurizing system (2) controls the low-temperature heat exchange system (23) to circulate a low-temperature medium to the low-pressure solid hydrogen storage device (21) for cooling through the hydrogen charging and discharging control system (28), and the low-pressure solid hydrogen storage device (21) starts hydrogen absorption; after the low-pressure solid hydrogen storage device (21) reaches hydrogen absorption balance, the high-temperature heat exchange system (24) circularly heats and pressurizes the low-pressure solid hydrogen storage device (21) by a high-temperature medium, and then discharges hydrogen to the low-pressure buffer tank (26); the pressurized hydrogen enters a high-pressure solid hydrogen storage device (22) for cooling, and a low-temperature heat exchange system (23) circulates a low-temperature medium to the high-pressure solid hydrogen storage device (22), so that the high-pressure solid hydrogen storage device (22) starts to absorb hydrogen; after the high-pressure solid hydrogen storage device (22) reaches hydrogen absorption balance, the high-temperature heat exchange system (24) heats and pressurizes the high-pressure solid hydrogen storage device (22) by using a high-temperature circulating medium, and after the high-pressure solid hydrogen storage device reaches a preset pressure, the control system adjusts a corresponding valve to collect high-pressure hydrogen into a high-pressure buffer bottle (27); the hydrogen charging and discharging control system (28) automatically supplements the high-pressure hydrogen to the gas mixing device (41) according to the pressure and the gas content of the mixer.
6. The low-energy-consumption green methanol synthesis system according to claim 4, wherein the low-energy-consumption hydrogen is supplied to the low-temperature heat exchange system (23) and the high-temperature heat exchange system (24) of the pressurizing system (2) and the heat source of the high-temperature heat exchange system (24) is provided by waste heat generated by thermocatalysis of the synthetic methanol synthesis device (5), so that the heat efficiency of the whole system can be improved.
7. The low-energy-consumption green methanol synthesis system according to claim 4, wherein the low-energy-consumption hydrogen supply pressurization system (2) uses a connection mode of one to three sets of low-pressure solid hydrogen storage devices (21) corresponding to one set of high-pressure solid hydrogen storage devices (22), and is matched with a pressure stabilizing pipeline, so that continuous output can be provided, and the pressure of released hydrogen is controlled to be 9-12 MPa.
8. The low-energy-consumption green methanol synthesis system according to claim 4, wherein the low-pressure solid hydrogen storage device (21) is filled with a low-platform-pressure hydrogen storage material, can absorb 1.6-3.5 MPa hydrogen and can release 5-6 MPa hydrogen.
9. The low-energy-consumption green methanol synthesis system according to claim 4, wherein the high-pressure solid hydrogen storage device (22) is filled with a high-platform-pressure hydrogen storage material, can absorb 5-6 MPa hydrogen and can release 9-12 MPa hydrogen.
10. The low-power consumption green methanol synthesis system according to claim 4, wherein the low-power consumption hydrogen supply pressurization system (2) is provided with a set of hydrogen pressurization device (25) for supplying high-pressure hydrogen to the gas mixing device (41) in a system start-up stage, and after the whole system stably operates, the charging and discharging control system (28) can automatically switch to a solid hydrogen storage pressurization mode to supplement hydrogen to the gas mixing device (41).
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