CN114874803A - Method and device for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation powered by solar energy - Google Patents
Method and device for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation powered by solar energy Download PDFInfo
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- CN114874803A CN114874803A CN202210543244.9A CN202210543244A CN114874803A CN 114874803 A CN114874803 A CN 114874803A CN 202210543244 A CN202210543244 A CN 202210543244A CN 114874803 A CN114874803 A CN 114874803A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/50—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon dioxide with hydrogen
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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
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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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/33—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used
- C10G2/334—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts characterised by the catalyst used containing molecular sieve catalysts
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/133—Renewable energy sources, e.g. sunlight
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method and a device for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation powered by solar energy, wherein the preparation method comprises the following steps: the carbon dioxide and the hydrogen are subjected to catalytic reaction in a catalytic reaction tower, the mixed liquid is input into a two-stage high-pressure separation tank, the gas and the liquid are separated, the liquid is sent into a product separation tank, the separated gasoline fraction hydrocarbon is sent into a dehydrogenation tower for dehydrogenation, and the gasoline fraction hydrocarbon is output to a gasoline fraction hydrocarbon storage tank by a product output pump after dehydrogenation. The device comprises a solar device, an inverter, a catalytic reaction tower, a high-pressure separation tank I, a high-pressure separation tank II, a product separation tank, a dehydrogenation tower and a product output pump. The invention has low cost and simple process, improves the yield by utilizing two high-pressure separation tanks, and further improves the purity of the product by adopting product separation and dehydrogenation technologies. The invention has high product quality, accords with the national standard, uses carbon dioxide as a raw material, is beneficial to realizing the cyclic utilization of carbon resources, reduces the environmental pollution, and is a green and environment-friendly production system.
Description
Technical Field
The present invention relates to a method and an apparatus for producing gasoline fraction hydrocarbons, and more particularly to a method and an apparatus for producing gasoline fraction hydrocarbons by hydrogenation of carbon dioxide, and particularly to a method and an apparatus for producing gasoline fraction hydrocarbons by hydrogenation of carbon dioxide supplied by solar energy.
Background
At present, gasoline is mainly produced by technologies such as direct fractionation of crude oil, and petroleum resources are developed in large quantities and are less and less, so that various countries seek different ways to produce gasoline. On the other hand, the large-scale use of fossil fuels also consumes a large amount of energy and generates a large amount of carbon dioxide gas, causing serious environmental pollution. Therefore, how to change carbon dioxide into valuable is a subject before accountants. Through long-term research, people find that the gasoline hydrocarbon compounds can be synthesized by carbon dioxide hydrogenation, which is a great contribution to the society. In practice, various processes have been invented, but how to effectively realize the production process is continuously explored.
Disclosure of Invention
The invention aims to invent a low-cost and high-efficiency device for synthesizing gasoline fraction hydrocarbon. In addition, as solar energy is utilized as energy, the pollution is further reduced, and the production cost is reduced.
The purpose of the invention is realized by the following technical scheme:
the method for preparing gasoline fraction hydrocarbon by hydrogenating carbon dioxide powered by solar energy comprises the following steps:
mixing carbon dioxide and hydrogen in a catalytic reaction tower, carrying out catalytic reaction, inputting the mixed solution into a two-stage high-pressure separation tank, separating gas from liquid, sending the liquid into a product separation tank, dehydrogenating the separated gasoline fraction hydrocarbon in a dehydrogenation tower, outputting the hydrogen and the gasoline fraction hydrocarbon to a hydrogen and gasoline fraction hydrocarbon storage tank by a product output pump after dehydrogenation. A device for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation powered by solar energy comprises a solar device, an inverter, a catalytic reaction tower, a high-pressure separation tank I, a high-pressure separation tank II, a product separation tank, a dehydrogenation tower and a product output pump;
the solar device consists of a plurality of solar panels and a storage battery pack, is connected with the inverter and is converted into 220V alternating current to supply power to the whole device;
a carbon dioxide feeding pipe is introduced into the catalytic reaction tower from a carbon dioxide feeding hole at the top of the catalytic reaction tower, and a hydrogen feeding pipe is introduced into the catalytic reaction tower from a hydrogen feeding hole at the upper part of the catalytic reaction tower; a pipeline below the catalytic reaction tower is connected to the middle part of the high-pressure separation tank I; the bottom pipeline of the high-pressure separation tank I is connected to the product separation tank, the top outlet of the high-pressure separation tank I is connected to the middle part of the high-pressure separation tank II, and the high-pressure separation tank II is also connected to the middle part of the product separation tank through the pipeline at the bottom; the bottommost part of the product separation tank is provided with a water outlet, the upper layer of the water outlet is a fraction hydrocarbon outlet, and the fraction hydrocarbon is connected to the middle part of the dehydrogenation tower through a pipeline; the top of the product separation tank is provided with a waste gas outlet; the pipeline at the top of the dehydrogenation tower is connected with a cooler II, and an outlet pipeline of the cooler II is connected with the upper part of the dehydrogenation tower; two pipelines are arranged at the bottom of the dehydrogenation tower, one pipeline is introduced into the product output pump, and the other pipeline is connected back to the dehydrogenation tower through a reboiler; the output end of the product output pump is provided with a gasoline fraction hydrocarbon pipeline which is connected to a gasoline fraction hydrocarbon storage tank.
The pipeline at the top of the high-pressure separation tank II is connected to a heater II, the heater II is connected to an adsorption tower, the pipeline at the lower part of the adsorption tower is connected to a circulating compression pump, and the outlet of the circulating compression pump is connected with a carbon dioxide feed inlet at the top of the catalytic reaction tower.
The carbon dioxide feeding pipe is introduced into the catalytic reaction tower through a preheater I and a heater I, the temperature in the preheater I is 10-50 ℃, and the temperature in the heater I is 250-500 ℃.
A hydrogen feeding pipe is introduced into the catalytic reaction tower through a preheater II, and the preheating temperature in the preheater II is 10-50 ℃.
An iron-based molecular sieve catalyst is used in the catalytic reaction tower.
The pipeline below the catalytic reaction tower is connected to the middle part of the high-pressure separation tank I through a cooler I, and the cooling temperature of the cooler I is 5-15 ℃.
The outlet at the top of the high-pressure separation tank I is connected to the middle part of the high-pressure separation tank II through a deep cooler, and the cooling temperature of the deep cooler is-30 ℃ to 10 ℃.
The reboiler heating temperature is 160 ℃.
The invention has the beneficial effects that:
the invention has low cost and simple process, can improve the yield by utilizing two high-pressure separation tanks to carry out cryogenic reflux on gas, and further improves the purity of the product by adopting product separation and dehydrogenation technologies. The invention has good production effect, and the prepared product has high quality and meets the national standard. The invention uses carbon dioxide as a raw material, is beneficial to realizing the cyclic utilization of carbon resources, reduces the environmental pollution and is a green and environment-friendly production system.
Drawings
FIG. 1 is a schematic diagram of a solar-powered apparatus for producing gasoline fraction hydrocarbons by hydrogenation of carbon dioxide.
In the figure: the system comprises a solar device 1, an inverter 2, a preheater I3, a heater I4, a preheater II5, a catalytic reaction tower 6, a cooler I7, a high-pressure separation tank I8, a high-pressure separation tank II9, a deep cooler 10, a product separation tank 11, a dehydrogenation tower 12, a reboiler 13, a product output pump 14, a cooler II15, a heater II16, an adsorption tower 17 and a circulating compression pump 18.
Detailed Description
The method for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation comprises the following steps:
And 2, introducing the hydrogen in the hydrogen feeding pipe into the catalytic reaction tower 6 from a hydrogen feeding hole at the upper part of the catalytic reaction tower 6 through a preheater II5, wherein the preheating temperature in the preheater II5 is 10-50 ℃, and the feeding pressure is 1-7 Mpa.
And 3, introducing hydrogen/carbon dioxide into the catalytic reaction tower 6 at a molar ratio of 0.5-8, mixing the carbon dioxide and the hydrogen in the catalytic reaction tower 6, and carrying out catalytic reaction under the action of an iron-based molecular sieve catalyst at a reaction temperature of 250-500 ℃ and a reaction pressure of 1-6 MPa.
And 4, discharging the crude fraction hydrocarbon mixed gas generated in the catalytic reaction tower 6 from the lower part of the catalytic reaction tower 6, connecting the crude fraction hydrocarbon mixed gas to the middle part of a high-pressure separation tank I8 through a cooler I7 by a lower pipeline, and controlling the cooling temperature of the cooler I7 to be 5-15 ℃. In the high-pressure separation tank I8, the crude fraction hydrocarbon mixed gas is subjected to high-pressure separation at 2-5MPa, and the gas and the liquid are separated and respectively output from the top and the bottom. The bottom of high pressure knockout drum I8 is piped to product knockout drum 11, sending impure distillate hydrocarbon liquids to product knockout drum 11. The top outlet of high-pressure separator tank I8 was connected to the middle of high-pressure separator tank II9 via chiller 10 and was cryogenically refluxed to high-pressure separator tank II 9. The cooling temperature of the deep cooler 10 is-30 ℃ to 10 ℃. In the high-pressure separation tank II9, the distillate hydrocarbon liquid after further processing is sent to the middle part of the product separation tank 11 through a pipeline at the bottom after the high-pressure separation treatment of 2-5 Mpa.
And 5, separating the input liquid by the product separation tank 11, wherein the product separation tank 11 is separated into three layers, the upper layer is waste gas, the lower layer is water with the highest density, and the middle layer is product gasoline fraction hydrocarbon with the density lighter than that of the water. The product separation tank 11 is used for discharging water and waste gas to extract gasoline fraction hydrocarbons. A water outlet is arranged at the bottommost part of the product separation tank 11, and water is discharged from the bottom of the tank; the top is provided with an exhaust gas outlet, and exhaust gas is discharged from the top. The upper layer of the water outlet is a gasoline fraction hydrocarbon outlet, and the gasoline fraction hydrocarbon is connected to the middle part of the dehydrogenation tower 12 through a pipeline.
And step 6, the main work of the dehydrogenation tower 12 is purification, the top pipeline of the dehydrogenation tower 12 is connected with a cooler II15, the outlet pipeline of the cooler II15 is connected with the upper part of the dehydrogenation tower 12, and the gas at the top of the dehydrogenation tower 12 is cooled by a cooler II15 and then flows back to the tower. The cooling temperature of the cooler II15 is 5-15 ℃. The bottom of the dehydrogenation tower 12 is provided with two pipelines, one pipeline is introduced into a product output pump 14, the other pipeline is introduced into a reboiler 13, the purification is carried out under the boiling action, the heating temperature is 160 ℃, the gasoline fraction hydrocarbon is boiled, trace other gases in the gasoline fraction hydrocarbon are discharged, the gasoline fraction hydrocarbon is output and flows back to the dehydrogenation tower 12, and the pure gasoline fraction hydrocarbon is output from the bottom of the dehydrogenation tower 12.
And 7, arranging a gasoline fraction hydrocarbon pipeline at the output end of the product output pump 14, connecting the gasoline fraction hydrocarbon storage tank, and outputting the gasoline fraction hydrocarbon to the gasoline fraction hydrocarbon storage tank.
Further, in step 4, the top of the high-pressure separation tank II9 was connected to a heater II16 by a pipe, and the mixed gas was fed to a heater II16, and a heater II16 was connected to the adsorption column 17, and the mixed gas was fed to the adsorption column 17 after heating at 20 ℃ to 60 ℃. The pressure in the adsorption tower 17 is 0.4-3Mpa, the temperature is 20-60 ℃, and the molecular sieve adsorbent is filled in the adsorption tower 17 and is used for adsorbing hydrogen and carbon dioxide. The pipeline at the lower part of the adsorption tower 17 is connected to a circulating compression pump 18, the outlet of the circulating compression pump 18 is connected with a carbon dioxide feed inlet at the top of the catalytic reaction tower 6, and the adsorbed hydrogen and carbon dioxide are pressurized to 1-7Mpa and then returned to the catalytic reaction tower 6 through the feed inlet.
Referring to fig. 1, the device for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation through solar power supply comprises a solar device 1, an inverter 2, a catalytic reaction tower 6, a high-pressure separation tank I8, a high-pressure separation tank II9, a product separation tank 11, a dehydrogenation tower 12 and a product output pump 14.
The solar device 1 and the inverter 2 supply power to the entire device. The solar device 1 is composed of a plurality of solar panels and a storage battery pack, electric energy generated by solar energy is stored in the storage battery pack, then the storage battery pack is connected to an inverter 2, and the electric energy is converted into 220V alternating current to supply power to the whole device. Solar power systems are mature technologies and will not be described in detail herein.
The carbon dioxide feeding pipe is introduced into the catalytic reaction tower 6 from a carbon dioxide feeding port at the top of the catalytic reaction tower 6 through a preheater I3 and a heater I4, the temperature in the preheater I3 is 10-50 ℃, and the temperature in the heater I4 is 250-500 ℃. A hydrogen feed pipe is led into the catalytic reaction tower 6 from a hydrogen feed port at the upper part of the catalytic reaction tower 6 through a preheater II5, and the preheating temperature in the preheater II5 is 10-50 ℃. An iron-based molecular sieve catalyst is used in the catalytic reaction tower 6, a pipeline below the catalytic reaction tower 6 is connected to the middle part of a high-pressure separation tank I8 through a cooler I7, and the cooling temperature of the cooler I7 is 5-15 ℃. The bottom pipe of the high-pressure separation tank I8 is connected to the product separation tank 11, the top outlet of the high-pressure separation tank I8 is connected to the middle part of the high-pressure separation tank II9 through a chiller 10, and the cooling temperature of the chiller 10 is-30 ℃ to 10 ℃. High-pressure separator tank II9 is also connected to the middle of product separator tank 11 via a conduit at the bottom. The product separating tank 11 is a gas-liquid separating device in the existing industry, has a structure similar to that of a high-pressure separating tank, and is also a device for separating oil, water and gas, wherein a water outlet is arranged at the bottommost part of the product separating tank, and water is discharged from the bottom of the product separating tank. The upper layer of the water outlet is a fraction hydrocarbon outlet which is connected to the middle part of the dehydrogenation tower 12 through a pipeline, and the top of the product separation tank 11 is provided with a waste gas outlet. The pipeline at the top of the dehydrogenation tower 12 is connected with a cooler II15, the outlet pipeline of the cooler II15 is connected with the upper part of the dehydrogenation tower 12, and the gas at the top of the dehydrogenation tower 12 flows back to the tower after being cooled by a cooler II 15. The dehydrogenation column 12 has two lines at its bottom, one line leading to a product take-off pump 14 and the other line leading to a reboiler 13, the take-off line of which is connected back to the dehydrogenation column 12. The output end of the product output pump 14 is provided with a gasoline fraction hydrocarbon pipeline which is connected with a gasoline fraction hydrocarbon storage tank and outputs the gasoline fraction hydrocarbon to the gasoline fraction hydrocarbon storage tank.
The top pipeline of the high-pressure separation tank II9 is connected to a heater II16, a heater II16 is connected to the adsorption tower 17, a molecular sieve adsorbent is arranged in the adsorption tower 17 and used for adsorbing hydrogen and carbon dioxide, the pipeline at the lower part of the adsorption tower 17 is connected to a circulating compression pump 18, and the outlet of the circulating compression pump 18 is connected with a carbon dioxide feed inlet at the top of the catalytic reaction tower 6.
The solar energy device 1 and the inverter 2 are used for supplying power to the whole device. The solar device 1 is composed of a plurality of solar panels and a storage battery pack, electric energy generated by solar energy is stored in the storage battery pack, then the storage battery pack is connected to an inverter 2, and the electric energy is converted into 220V alternating current to supply power to the whole device.
Claims (10)
1. A method for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation powered by solar energy comprises the steps of supplying power to the whole device by a solar device (1) and an inverter (2); mixing carbon dioxide and hydrogen in a catalytic reaction tower (6), carrying out catalytic reaction, inputting the mixed solution into a two-stage high-pressure separation tank, separating gas from liquid, sending the liquid into a product separation tank (11), sending the separated gasoline fraction hydrocarbon into a dehydrogenation tower (12) for dehydrogenation, and outputting the hydrogen and the gasoline fraction hydrocarbon to a hydrogen and gasoline fraction hydrocarbon storage tank by a product output pump (14) after dehydrogenation.
2. The method of claim 2, wherein: the method comprises the following specific steps:
step 1, introducing carbon dioxide gas in a carbon dioxide feeding pipe into a catalytic reaction tower (6) from a carbon dioxide feeding hole at the top of the catalytic reaction tower (6) through a preheater I (3) and a heater I (4);
step 2, introducing the hydrogen in the hydrogen feeding pipe into the catalytic reaction tower (6) from a hydrogen feeding hole at the upper part of the catalytic reaction tower (6) through a preheater II (5);
step 3, introducing hydrogen/carbon dioxide into the catalytic reaction tower (6) at a molar ratio of 0.5-8, mixing carbon dioxide and hydrogen in the catalytic reaction tower (6), and carrying out catalytic reaction under the action of an iron-based molecular sieve catalyst at a reaction temperature of 250-500 ℃ and a reaction pressure of 1-6 Mpa;
step 4, discharging the crude fraction hydrocarbon mixed gas generated in the catalytic reaction tower (6) from the lower part of the catalytic reaction tower (6), connecting the crude fraction hydrocarbon mixed gas to the middle part of a high-pressure separation tank I (8) through a cooler I (7) by virtue of a pipeline at the lower part, and in the high-pressure separation tank I (8), separating the crude fraction hydrocarbon mixed gas by virtue of high-pressure separation of 2-5Mpa, and outputting the gas and liquid from the top and the bottom respectively; the bottom of the high-pressure separation tank I (8) is connected to a product separation tank (11) through a pipeline, and impure distillate hydrocarbon liquid is sent to the product separation tank (11); the outlet at the top of the high-pressure separation tank I (8) is connected to the middle part of the high-pressure separation tank II (9) through a deep cooler (10), and the high-pressure separation tank II (9) is refluxed with deep cooling; in the high-pressure separation tank II (9), the distillate hydrocarbon liquid after further processing is sent to the middle part of the product separation tank (11) through a pipeline at the bottom after 2-5Mpa high-pressure separation treatment;
step 5, the input liquid is separated by a product separation tank (11), the product separation tank (11) is separated into three layers, the upper layer is waste gas, the lower layer is water with the highest density, and the middle layer is product gasoline fraction hydrocarbon; water is discharged from the bottom of the product separating tank (11); the waste gas is discharged from the top; the gasoline fraction hydrocarbon is sent to the middle part of the dehydrogenation tower (12) through a pipeline;
step 6, connecting a pipeline at the top of the dehydrogenation tower (12) with a cooler II (15), cooling the gas at the top of the dehydrogenation tower (12) by the cooler II (15) and then refluxing the cooled gas into the tower; the bottom of the dehydrogenation tower (12) is provided with two pipelines, one pipeline is communicated with a product output pump (14), the other pipeline is communicated with a reboiler (13), the output of the reboiler (13) returns to the dehydrogenation tower (12), and pure gasoline distillate hydrocarbon is output from the bottom of the dehydrogenation tower (12) to the product output pump (14);
and 7, arranging a gasoline fraction hydrocarbon pipeline at the output end of the product output pump (14), connecting the gasoline fraction hydrocarbon storage tank, and outputting the gasoline fraction hydrocarbon to the gasoline fraction hydrocarbon storage tank.
3. The method of claim 1, wherein: in the step 4, a pipeline at the top of the high-pressure separation tank II (9) is connected to a heater II (16), the mixed gas is sent to the heater II (16), the heater II (16) is connected to an adsorption tower (17), and the mixed gas is sent to the adsorption tower (17) after being heated to 20-60 ℃; the pressure in the adsorption tower (17) is 0.4-3Mpa, the temperature is 20-60 ℃, and a molecular sieve adsorbent is filled in the adsorption tower (17) and is used for adsorbing hydrogen and carbon dioxide; the pipeline at the lower part of the adsorption tower (17) is connected to a circulating compression pump (18), the outlet of the circulating compression pump (18) is connected with a carbon dioxide feed inlet at the top of the catalytic reaction tower (6), and the adsorbed hydrogen and carbon dioxide are pressurized to 1-7Mpa and then returned to the catalytic reaction tower (6) through the feed inlet.
4. The method of claim 1, wherein:
in the step 1, the preheating temperature of carbon dioxide in a preheater I (3) is 10-50 ℃, the heating temperature in a heater I (4) is 250-500 ℃, and the feeding pressure is 1-7 Mpa;
in the step 2, the preheating temperature in the preheater II (5) is 10-50 ℃, and the feeding pressure is 1-7 Mpa;
in the step 4, the cooling temperature of the cooler I (7) is 5-15 ℃; the cooling temperature of the deep cooler (10) is-30-10 ℃;
in step 6, the cooling temperature of the cooler II (15) is 5-15 ℃; the reboiler (13) heats up to 160 ℃.
5. A device for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation powered by solar energy is characterized in that: the device comprises a solar device (1), an inverter (2), a catalytic reaction tower (6), a high-pressure separation tank I (8), a high-pressure separation tank II (9), a product separation tank (11), a dehydrogenation tower (12) and a product output pump (14);
the solar device (1) consists of a plurality of solar panels and a storage battery pack, is connected with the inverter (2), converts the solar panels into 220V alternating current and supplies power to the whole device;
a carbon dioxide feeding pipe is introduced into the catalytic reaction tower (6) from a carbon dioxide feeding hole at the top of the catalytic reaction tower (6), and a hydrogen feeding pipe is introduced into the catalytic reaction tower (6) from a hydrogen feeding hole at the upper part of the catalytic reaction tower (6); a pipeline below the catalytic reaction tower (6) is connected to the middle part of the high-pressure separation tank I (8); the bottom pipeline of the high-pressure separation tank I (8) is connected to the product separation tank (11), the top outlet of the high-pressure separation tank I (8) is connected to the middle part of the high-pressure separation tank II (9), and the high-pressure separation tank II (9) is also connected to the middle part of the product separation tank (11) through the pipeline at the bottom; a water outlet is arranged at the bottommost part of the product separation tank (11), the upper layer of the water outlet is a fraction hydrocarbon outlet, and the fraction hydrocarbon is connected to the middle part of the dehydrogenation tower (12) through a pipeline; the top of the product separating tank (11) is provided with a waste gas outlet; the top pipeline of the dehydrogenation tower (12) is connected with a cooler II (15), and the outlet pipeline of the cooler II (15) is connected with the upper part of the dehydrogenation tower (12); two pipelines are arranged at the bottom of the dehydrogenation tower (12), one pipeline is introduced into a product output pump (14), and the other pipeline is connected back to the dehydrogenation tower (12) through a reboiler (13); the output end of the product output pump (14) is provided with a gasoline fraction hydrocarbon pipeline which is connected to a gasoline fraction hydrocarbon storage tank.
6. The apparatus for producing hydrocarbons of gasoline fraction by hydrogenation of carbon dioxide according to claim 5, wherein: the top of the high-pressure separation tank II (9) is connected to a heater II (16) through a pipeline, the heater II (16) is connected to an adsorption tower (17), the pipeline at the lower part of the adsorption tower (17) is connected to a circulating compression pump (18), and the outlet of the circulating compression pump (18) is connected with a carbon dioxide feeding port at the top of the catalytic reaction tower (6).
7. The apparatus for producing hydrocarbons of gasoline fraction by hydrogenation of carbon dioxide according to claim 5, wherein: the carbon dioxide feeding pipe is introduced into the catalytic reaction tower (6) through a preheater I (3) and a heater I (4), the temperature in the preheater I (3) is 10-50 ℃, and the temperature in the heater I (4) is 250-500 ℃; the hydrogen feeding pipe is led into the catalytic reaction tower (6) through the preheater II (5), and the preheating temperature in the preheater II (5) is 10-50 ℃.
8. The apparatus for producing hydrocarbons of gasoline fraction by hydrogenation of carbon dioxide according to claim 5, wherein: the pipeline below the catalytic reaction tower (6) is connected to the middle part of the high-pressure separation tank I (8) through a cooler I (7), and the cooling temperature of the cooler I (7) is 5-15 ℃.
9. The apparatus for producing hydrocarbons of gasoline fraction by hydrogenation of carbon dioxide according to claim 5, wherein: the top outlet of the high-pressure separation tank I (8) is connected to the middle part of the high-pressure separation tank II (9) through a deep cooler (10), and the cooling temperature of the deep cooler (10) is-30 ℃ to 10 ℃.
10. The apparatus for producing hydrocarbons of gasoline fraction by hydrogenation of carbon dioxide according to claim 5, wherein: the reboiler (13) heats up to 160 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210543244.9A CN114874803A (en) | 2022-05-18 | 2022-05-18 | Method and device for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation powered by solar energy |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202210543244.9A CN114874803A (en) | 2022-05-18 | 2022-05-18 | Method and device for preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation powered by solar energy |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111748366A (en) * | 2020-07-13 | 2020-10-09 | 珠海市福沺能源科技有限公司 | Device and method for directly preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation |
| CN113004931A (en) * | 2021-03-29 | 2021-06-22 | 珠海市福沺能源科技有限公司 | Single-tube test device and method for directly preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN111748366A (en) * | 2020-07-13 | 2020-10-09 | 珠海市福沺能源科技有限公司 | Device and method for directly preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation |
| CN113004931A (en) * | 2021-03-29 | 2021-06-22 | 珠海市福沺能源科技有限公司 | Single-tube test device and method for directly preparing gasoline fraction hydrocarbon by carbon dioxide hydrogenation |
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