Method and device for preparing liquid fuel based on plasma reactor

Abstract

The invention discloses a preparation method and device of liquid fuel based on a plasma reactor, the preparation device comprises a liquid fuel gas synthesis part, the gas synthesis part comprises a storage assembly, a first heat exchange assembly, a second mixing unit, the plasma reactor, a third heat exchange assembly and a first flash tank which are connected in sequence, the storage assembly is used for storing gas and liquid; the fuel synthesis part comprises a compressor, a mixing assembly, a second heat exchange assembly, a Fischer-Tropsch reactor, a fourth heat exchange assembly, a second flash tank, a dryer and a fuel collection unit which are sequentially connected, the compressor is connected with the first flash tank, the mixing assembly is connected with the top of the second flash tank, and the fuel collection unit is used for collecting liquid fuel. According to the invention, the liquid fuel can be obtained, and the energy efficiency and the net CO2 emission reduction rate can be respectively 46.28% and 64.57%.

Description

Technical Field

[0001] The invention relates to the technical field of liquid fuel, and in particular to a method and a device for preparing liquid fuel based on a plasma reactor. Background Art

[0002] With the acceleration of urbanization, the amount of urban garbage in my country has increased dramatically. Landfill, as one of the traditional ways of garbage disposal, has alleviated the pressure of garbage disposal to a certain extent, but the accompanying environmental pollution problem has also become increasingly prominent. During the landfill process, a large amount of landfill gas (LFG) will be produced due to the decomposition of microorganisms, the main component of which is methane ( ) and carbon dioxide ( ), both of which are major greenhouse gases and have made significant contributions to global warming. In particular, methane has a greenhouse effect dozens of times greater than carbon dioxide. If it is directly emitted into the atmosphere, it will not only cause serious environmental pollution, but also cause huge energy waste.

[0003] In order to effectively deal with this problem, domestic and foreign scholars and research institutions are committed to exploring ways to utilize landfill gas as a resource. The traditional approach is to collect landfill gas and use it for combustion to generate electricity. Although this method can partially achieve energy recovery, the overall utilization efficiency is low, and the deep conversion and utilization of the two key components, methane and carbon dioxide, are limited.

[0004] In recent years, with the rapid development of plasma technology, it has shown great application potential in the fields of environmental governance and energy conversion. Plasma reactors use the inelastic collisions between high-energy electrons and gas molecules to initiate and accelerate chemical reactions under low temperature and pressure conditions. They are particularly suitable for treating complex gas mixtures, such as landfill gas. Compared with traditional catalytic reforming technology, plasma reactors have the advantages of no need for complex catalysts, mild operating conditions, fast reaction speed, low coking, and small equipment size, providing new ideas for the efficient conversion of landfill gas.

[0005] Specifically, a plasma reactor is used to reform the methane and carbon dioxide in landfill gas into synthesis gas (mainly carbon monoxide and hydrogen, The ratio is about 1:1), which not only effectively reduces greenhouse gas emissions, but also provides high-quality raw materials for subsequent chemical processes such as Fischer-Tropsch synthesis. Fischer-Tropsch synthesis is an important process for converting synthesis gas into liquid hydrocarbons (such as gasoline, diesel and other liquid fuels). The ratio directly affects the distribution and yield of the product. Therefore, the liquid fuel preparation method based on the plasma reactor not only solves the environmental pollution problem of landfill gas, but also promotes the recycling of resources, which has far-reaching significance for promoting sustainable development of energy, reducing greenhouse gas emissions, and improving the living environment of human beings.

[0006] Therefore, the present application proposes a method and device for preparing liquid fuel based on a plasma reactor. Summary of the invention

[0007] The object of the present invention is to provide a method and apparatus for preparing liquid fuel based on a plasma reactor, which can prepare liquid fuel and achieve energy efficiency and net CO2 emission reduction rate of 46.28% and 64.57% respectively.

[0008] The purpose of the present invention is achieved by the following technical solutions: In one aspect, the present invention provides a liquid fuel preparation device based on a plasma reactor, comprising: A gas synthesis section, the gas synthesis section comprises a storage component, a first heat exchange component, a second mixing unit, a plasma reactor, a third heat exchange component and a first flash tank connected in sequence, wherein the storage component is used to store gas and / or liquid, the storage component is connected to the low temperature end of the first heat exchange component, the high temperature end of the first heat exchange component is connected to the second mixing unit, the plasma reactor is connected to the high temperature end of the third heat exchange component, and the low temperature end of the third heat exchange component is connected to the first flash tank; A fuel synthesis section, which includes a compressor, a mixing component, a second heat exchange component, a Fischer-Tropsch reactor, a fourth heat exchange component, a second flash tank, a dryer, and a fuel collection unit connected in sequence, wherein the compressor is connected to the first flash tank, the mixing component is connected to the top of the second flash tank and the low-temperature end of the second heat exchange component, the high-temperature end of the second heat exchange component is connected to the Fischer-Tropsch reactor, the high-temperature end of the fourth heat exchange component is connected to the Fischer-Tropsch reactor, the low-temperature end of the fourth heat exchange component is connected to the second flash tank, and the fuel collection unit is used to collect liquid fuel.

[0009] Furthermore, the storage component includes: A first storage unit, wherein the first storage unit is used to store CO2; A second storage unit, the second storage unit is used to store CH4 / N2; A third storage unit, the third storage unit is used to store H2O, and an output end of the third storage unit is connected to a low temperature end of the first heat exchange component; A first mixing unit, wherein an input end of the first mixing unit is connected to the first storage unit and the second storage unit, and an output end of the first mixing unit is connected to a low-temperature end of the first heat exchange component.

[0010] Furthermore, the storage component also includes: A fourth storage unit is used to store landfill gas, and an output end of the fourth storage unit is connected to an input end of the first mixing unit or a low-temperature end of the first heat exchange component.

[0011] Furthermore, the first heat exchange component includes: A first heating unit, the first heating unit comprising a first heat exchanger and a second heat exchanger, the low temperature end of the first heat exchanger is connected to the first mixing unit, the high temperature end of the first heat exchanger is connected to the low temperature end of the second heat exchanger, and the high temperature end of the second heat exchanger is connected to the second mixing unit; a second heating unit, the second heating unit comprising: a third heat exchanger and a fourth heat exchanger, the low temperature end of the third heat exchanger is connected to the third storage unit, the high temperature end of the third heat exchanger is connected to the low temperature end of the fourth heat exchanger, and the high temperature end of the fourth heat exchanger is connected to the second mixing unit; The second heat exchange component includes: a sixth heat exchanger and a seventh heat exchanger, the low-temperature end of the sixth heat exchanger is connected to the mixing component, the high-temperature end of the sixth heat exchanger is connected to the low-temperature end of the seventh heat exchanger, and the high-temperature end of the seventh heat exchanger is connected to the Fischer-Tropsch reactor.

[0012] Further, the third heat exchanger comprises: a ninth heat exchanger and a fourth heat exchanger, the high temperature end of the ninth heat exchanger is connected to the plasma reactor, the low temperature end of the ninth heat exchanger is connected to the high temperature end of the fourth heat exchanger, and the low temperature end of the fourth heat exchanger is connected to the first flash tank; The fourth heat exchange component includes: an eleventh heat exchanger and an eighth heat exchanger, the high temperature end of the eleventh heat exchanger is connected to the Fischer-Tropsch reactor, the low temperature end of the eleventh heat exchanger is connected to the high temperature end of the eighth heat exchanger, and the low temperature end of the eighth heat exchanger is connected to the second flash tank.

[0013] Further, the third heat exchange component includes: a ninth heat exchanger and a fourth heat exchanger; The outlet of the plasma reactor is connected to the high temperature end of the third heat exchanger, the low temperature end of the third heat exchanger is connected to the high temperature end of the first heat exchanger, the low temperature end of the first heat exchanger is connected to the high temperature end of the ninth heat exchanger, the low temperature end of the ninth heat exchanger is connected to the high temperature end of the fourth heat exchanger, and the low temperature end of the fourth heat exchanger is connected to the first flash tank; The fourth heat exchanger comprises: an eleventh heat exchanger and an eighth heat exchanger; The outlet of the Fischer-Tropsch reactor is connected to the high-temperature end of the sixth heat exchanger, the low-temperature end of the sixth heat exchanger is connected to the high-temperature end of the eleventh heat exchanger, the low-temperature end of the eleventh heat exchanger is connected to the high-temperature end of the eighth heat exchanger, and the low-temperature end of the eighth heat exchanger is connected to the second flash tank.

[0014] Furthermore, the liquid fuel preparation device also includes: A power generation unit, the power generation unit comprising: a first power generation component, the first power generation component comprising a first steam turbine, a tenth heat exchanger and a second booster pump, the first steam turbine being used to supply power to the plasma reactor, one end of the first steam turbine being connected to the low temperature end of the ninth heat exchanger, the other end of the first steam turbine being connected to the low temperature end of the tenth heat exchanger, one end of the second booster pump being connected to the high temperature end of the tenth heat exchanger, and the other end of the second booster pump being connected to the low temperature end of the third heat exchanger; a second power generation component, the second power generation component comprising a second steam turbine, a twelfth heat exchanger and a third booster pump, the second steam turbine is used to supply power to the plasma reactor, one end of the second steam turbine is connected to the low temperature end of the eleventh heat exchanger, the other end of the second steam turbine is connected to the low temperature end of the twelfth heat exchanger, one end of the third booster pump is connected to the high temperature end of the twelfth heat exchanger, and the other end of the third booster pump is connected to the low temperature end of the fourth heat exchanger; The third power generation component includes a thirteenth heat exchanger, a third steam turbine, a fourteenth heat exchanger and a fourth booster pump connected in sequence, the high temperature end of the thirteenth heat exchanger is connected to the Fischer-Tropsch reactor, the third steam turbine supplies power to the plasma reactor, and the high temperature end of the fourteenth heat exchanger is connected to the high temperature end of the thirteenth heat exchanger.

[0015] Further, the mixing assembly comprises: a flow splitter connected to the top of the second flash tank; A third mixing unit, one end of which is connected to the compressor and a part of the diverter, and the other end of which is connected to the low-temperature end of the second heat exchange component.

[0016] In another aspect, the present invention provides a method for preparing liquid fuel based on a plasma reactor, comprising the following steps: The landfill gas and water in the storage component are heated by the first heat exchange component, and after being uniformly mixed in the second mixing unit, a first mixed gas is obtained, and the first mixed gas is introduced into the plasma reactor for reaction to obtain high-temperature synthesis gas; The high-temperature synthesis gas is cooled by the third heat exchange component to obtain low-temperature synthesis gas, and the low-temperature synthesis gas is passed into the first flash tank for flash separation to obtain dry synthesis gas; After the dry synthesis gas is compressed by a compressor, a compressed synthesis gas is obtained; the compressed synthesis gas and the mixed gas separated by flash evaporation in a second flash tank are placed in a mixing assembly for uniform mixing to obtain a second mixed gas; the second mixed gas is heated by a second heat exchange assembly and then introduced into a Fischer-Tropsch reactor for reaction to obtain a high-temperature hydrocarbon mixture; The high-temperature hydrocarbon mixture is cooled by the fourth heat exchange component to obtain a low-temperature hydrocarbon mixture, and the low-temperature hydrocarbon mixture is passed into a second flash tank for flash separation to obtain a mixed gas and a water-containing liquid fuel; The water-containing liquid fuel is dehydrated by using a dryer to obtain liquid fuel.

[0017] Furthermore, in the plasma reactor: the temperature is 850-900°C; the pressure is 1-3 bar; In the first flash tank: temperature is 5-20°C; pressure is 1-3 bar; In the compressor: the pressure is 15-25 bar; In the Fischer-Tropsch reactor: the temperature is 200-250°C; the pressure is 15-25 bar; In the second flash tank: the temperature is 5-20°C; the pressure is 15-25 bar; In the dryer: the temperature is 5-20°C; the pressure is 1-3 bar. Compared with the prior art, the beneficial effects of the present invention include at least: The landfill gas and water of the present invention are preheated and mixed, and then reacted in a plasma reactor to obtain high-temperature synthesis gas; the high-temperature synthesis gas is cooled, flashed, pressurized and preheated, and then reacted in a Fischer-Tropsch reactor to obtain a high-temperature hydrocarbon mixture; the high-temperature hydrocarbon mixture is cooled, flashed to remove unreacted mixed gas therein, and water-containing liquid fuel is obtained, and water in the water-containing liquid fuel is removed through a dryer to obtain liquid fuel. The energy efficiency and net CO2 emission reduction rate of the entire process are 46.28% and 64.57% respectively. BRIEF DESCRIPTION OF THE DRAWINGS

[0018] Figure 1 It is a schematic structural diagram of a liquid fuel preparation device based on a plasma reactor according to an embodiment of the present invention.

[0019] In the figure: F100, splitter; R101, plasma reactor; R102, Fischer-Tropsch reactor; M100, first mixing unit; M101, second mixing unit; M102, third mixing unit; E100, first heat exchanger; E101, second heat exchanger; E102, third heat exchanger; E103, fourth heat exchanger; E105, sixth heat exchanger; E106, seventh heat exchanger; E107, eighth heat exchanger; E201, ninth heat exchanger; E20 2. The tenth heat exchanger; E301, the eleventh heat exchanger; E302, the twelfth heat exchanger; E401, the thirteenth heat exchanger; E402, the fourteenth heat exchanger; V100, the first flash tank; V101, the second flash tank; P201, the second booster pump; P301, the third booster pump; P401, the fourth booster pump; T201, the first steam turbine; T301, the second steam turbine; T401, the third steam turbine; D101, the dryer; C100, the compressor. DETAILED DESCRIPTION

[0020] Example embodiments will now be described more fully with reference to the accompanying drawings. However, example embodiments can be implemented in a variety of forms and should not be construed as limited to the embodiments set forth herein; rather, these embodiments are provided to make the present invention more comprehensive and complete and to fully convey the concepts of example embodiments to those skilled in the art. The same reference numerals in the figures represent the same or similar structures, and thus their repeated description will be omitted.

[0021] The words expressing positions and directions described in the present invention are all explained with reference to the accompanying drawings as examples, but they can be changed as needed, and all such changes are included in the protection scope of the present invention.

[0022] The liquid fuel preparation device based on the plasma reactor R101 of the present invention comprises: a gas synthesis unit and a fuel synthesis unit. Furthermore, the preparation device may also comprise: a power generation unit.

[0023] The gas synthesis unit of the present invention comprises a storage assembly, a first heat exchange assembly, a second mixing unit, a plasma reactor R101, a third heat exchange assembly and a first flash tank V100 connected in sequence. The storage assembly is used to store gas and / or liquid, and the storage assembly is connected to the low temperature end of the first heat exchange assembly, and the high temperature end of the first heat exchange assembly is connected to the second mixing unit.

[0024] In some preferred embodiments, the storage assembly includes: a first storage unit, a second storage unit, a third storage unit and a first mixing unit M100. Furthermore, the storage assembly of the present invention may also include: a fourth storage unit.

[0025] When used, the first storage unit is used to store CO2; the second storage unit is used to store CH4 / N2; the third storage unit is used to store H2O; and the fourth storage unit is used to store landfill gas. The first storage unit and the second storage unit are connected to the input end of the first mixing unit M100, and the output end of the first mixing unit M100 is connected to the low temperature end of the first heat exchange component; the output end of the fourth storage unit and the output end of the third storage unit are connected to the low temperature end of the first heat exchange component. When used in practice, the first storage unit, the second storage unit, and the fourth storage unit are all connected to the input end of the first mixing unit M100.

[0026] In some preferred embodiments, the first heat exchange component includes: a first heating unit and a second heating unit.

[0027] When used, the first heating unit includes a first heat exchanger E100 and a second heat exchanger E101 connected to each other, the low-temperature end of the first heat exchanger E100 is connected to the first mixing unit M100, and the high-temperature end of the second heat exchanger E101 is connected to the second mixing unit; the second heating unit includes a third heat exchanger E102 and a fourth heat exchanger E103 connected to each other, the low-temperature end of the third heat exchanger E102 is connected to the third storage unit, and the high-temperature end of the fourth heat exchanger E103 is connected to the second mixing unit.

[0028] In some preferred embodiments, the third heat exchanger comprises a ninth heat exchanger E201 and a fourth heat exchanger E103 which are connected to each other.

[0029] When used, the high-temperature end of the ninth heat exchanger E201 is connected to the plasma reactor R101, and the low-temperature end of the fourth heat exchanger E103 is connected to the first flash tank V100.

[0030] In actual application, the outlet of the plasma reactor R101 is connected to the high temperature end of the third heat exchanger E102, the low temperature end of the third heat exchanger E102 is connected to the high temperature end of the first heat exchanger E100, the low temperature end of the first heat exchanger E100 is connected to the high temperature end of the ninth heat exchanger E201, the low temperature end of the ninth heat exchanger E201 is connected to the high temperature end of the fourth heat exchanger E103, and the low temperature end of the fourth heat exchanger E103 is connected to the first flash tank V100.

[0031] The fuel synthesis unit of the present invention comprises a compressor C100, a mixing assembly, a second heat exchange assembly, a Fischer-Tropsch reactor R102, a fourth heat exchange assembly, a second flash tank V101, a dryer D101, and a fuel collection unit connected in sequence. The compressor C100 is connected to the top of the first flash tank V100, the mixing assembly is connected to the top of the second flash tank V101, and the fuel collection unit is used to collect the dehydrated liquid fuel.

[0032] In some preferred embodiments, the mixing assembly includes: a flow splitter F100 and a third mixing unit M102.

[0033] When in use, the input end of the splitter F100 is connected to the top of the second flash tank V101; the output end of the splitter F100 includes a first port and a second port, the first port is connected to one end of the third mixing unit M102, and the second port is connected to an external waste gas recovery device. N2, CO2, CO, H2, CH4, C3H6, and C3H8 all enter the third mixing unit M102 through the first port, and other gases enter the external waste gas recovery device through the second port. Furthermore, the output end of the compressor C100 is connected to one end of the third mixing unit M102, and the other end of the third mixing unit M102 is connected to the low-temperature end of the second heat exchange component.

[0034] In some preferred embodiments, the second heat exchanger includes: a sixth heat exchanger E105 and a seventh heat exchanger E106.

[0035] When used, the third mixing unit M102 of the mixing assembly is connected to the low-temperature end of the sixth heat exchanger E105, the high-temperature end of the sixth heat exchanger E105 is connected to the low-temperature end of the seventh heat exchanger E106, and the high-temperature end of the seventh heat exchanger E106 is connected to the Fischer-Tropsch reactor R102.

[0036] In some preferred embodiments, the fourth heat exchanger includes: an eleventh heat exchanger E301 and an eighth heat exchanger E107.

[0037] When used, the Fischer-Tropsch reactor R102 is connected to the high temperature end of the eleventh heat exchanger E301, the low temperature end of the eleventh heat exchanger E301 is connected to the high temperature end of the eighth heat exchanger E107, and the low temperature end of the eighth heat exchanger E107 is connected to the second flash tank V101.

[0038] In actual application, the outlet of the Fischer-Tropsch reactor R102 is connected to the high temperature end of the sixth heat exchanger E105, the low temperature end of the sixth heat exchanger E105 is connected to the high temperature end of the eleventh heat exchanger E301, the low temperature end of the eleventh heat exchanger E301 is connected to the high temperature end of the eighth heat exchanger E107, and the low temperature end of the eighth heat exchanger E107 is connected to the second flash tank V101.

[0039] The power generation unit of the present invention includes: a first power generation component, a second power generation component and a third power generation component.

[0040] In some preferred embodiments, the first power generation component includes a first steam turbine T201, a tenth heat exchanger E202 and a second booster pump P201.

[0041] When used, the first steam turbine T201 is used to power the plasma reactor R101.

[0042] In actual application, refer to Figure 1 The low-temperature end of the ninth heat exchanger E201 is connected to one end of the first steam turbine T201, the other end of the first steam turbine T201 is connected to the low-temperature end of the tenth heat exchanger E202, the high-temperature end of the tenth heat exchanger E202 is connected to one end of the second booster pump P201, and the other end of the second booster pump P201 is connected to the low-temperature end of the ninth heat exchanger E201 of the third heat exchange component.

[0043] In some preferred embodiments, the second power generation component includes a second steam turbine T301, a twelfth heat exchanger E302 and a third booster pump P301.

[0044] When used, the second steam turbine T301 is used to power the plasma reactor R101.

[0045] In actual application, refer to Figure 1 The low-temperature end of the eleventh heat exchanger E301 is connected to one end of the second steam turbine T301, the other end of the second steam turbine T301 is connected to the low-temperature end of the twelfth heat exchanger E302, the high-temperature end of the twelfth heat exchanger E302 is connected to one end of the third pressure pump P301, and the other end of the third pressure pump P301 is connected to the low-temperature end of the eleventh heat exchanger E301 of the fourth heat exchange component.

[0046] In some preferred embodiments, the third power generation assembly includes a thirteenth heat exchanger E401, a third steam turbine T401, a fourteenth heat exchanger E402 and a fourth booster pump P401 connected in sequence.

[0047] When used, the third steam turbine T401 supplies power to the plasma reactor R101.

[0048] In actual application, refer to Figure 1 The Fischer-Tropsch reactor R102 is connected to the high temperature end of the thirteenth heat exchanger E401, the low temperature end of the thirteenth heat exchanger E401 is connected to one end of the third steam turbine T401, the other end of the third steam turbine T401 is connected to the low temperature end of the fourteenth heat exchanger E402, the high temperature end of the fourteenth heat exchanger is connected to one end of the fourth booster pump P401, and the other end of the fourth booster pump P401 is connected to the high temperature end of the thirteenth heat exchanger E401.

[0049] The method for preparing liquid fuel based on the plasma reactor R101 of the present invention includes steps S1 to S5.

[0050] In step S1, the landfill gas and water in the storage component are heated by the first heat exchange component, and after being uniformly mixed in the second mixing unit, a first mixed gas is obtained, and the first mixed gas is introduced into the plasma reactor R101 for reaction to obtain high-temperature synthesis gas.

[0051] In the plasma reactor: the temperature is 850-900°C; the pressure is 1-3 bar.

[0052] When used, landfill gas and water vapor are reacted in a plasma reactor R101 equipped with a catalyst to prepare a first mixed gas through a methane double reaction.

[0053] In step S2, the high-temperature synthesis gas is cooled by the third heat exchange component to obtain low-temperature synthesis gas, and the low-temperature synthesis gas is introduced into the first flash tank V100 for flash separation to obtain dry synthesis gas.

[0054] In the first flash tank V100: the temperature is 5-20°C; the pressure is 1-3 bar.

[0055] In step S3, the dry synthesis gas is compressed by the compressor C100 to obtain compressed synthesis gas, and the compressed synthesis gas and the mixed gas separated by flash evaporation in the second flash tank V101 are placed in a mixing assembly for uniform mixing to obtain a second mixed gas, and the second mixed gas is heated by a second heat exchange assembly and then introduced into a Fischer-Tropsch reactor R102 for reaction to obtain a high-temperature hydrocarbon mixture.

[0056] In compressor C100: pressure is 15-25 bar.

[0057] In the Fischer-Tropsch reactor R102: the temperature is 200-250°C; the pressure is 15-25 bar.

[0058] In step S4, the high-temperature hydrocarbon mixture is cooled by the fourth heat exchange component to obtain a low-temperature hydrocarbon mixture, and the low-temperature hydrocarbon mixture is passed into the second flash tank V101 for flash separation to obtain a mixed gas and a water-containing liquid fuel.

[0059] In the second flash tank V101: the temperature is 5-20°C; the pressure is 15-25 bar.

[0060] In step S5, the dryer D101 is used to dehydrate the water-containing liquid fuel to obtain liquid fuel.

[0061] In dryer D101: temperature is 5-20°C; pressure is 1-3 bar.

[0062] In some preferred embodiments, the method for preparing liquid fuel further includes step S6 and step S7.

[0063] Step S6: preheating the first mixed gas by using the high-temperature synthesis gas, and preheating the second mixed gas by using the high-temperature hydrocarbon mixture.

[0064] When applied, in order to achieve effective utilization of high-quality heat inside the system, the high-temperature synthesis gas (temperature of 850℃-900℃) at the outlet of the plasma reactor R101 is preheated step by step to heat the first mixed gas. Furthermore, the high-temperature hydrocarbon mixture (temperature of 200℃-250℃) at the outlet of the Fischer-Tropsch reactor R102 is preheated to heat the second mixed gas at its inlet.

[0065] Step S7: Utilize the high-temperature synthesis gas, the high-temperature hydrocarbon mixture and the reaction heat released by the Fischer-Tropsch synthesis reactor to provide heat for the power generation component.

[0066] When applied, in order to achieve effective utilization of low-quality waste heat inside the system, the high-temperature synthesis gas (temperature of 180°C-220°C) at the outlet of the plasma reactor R101 after heat exchange in step 6 enters the first power generation component to generate electricity, providing power for the plasma reactor R101. Further, the high-temperature hydrocarbon mixture (temperature of 150°C-200°C) at the outlet of the Fischer-Tropsch reactor R102 after heat exchange in step 6 enters the second power generation component to generate electricity, providing power for the plasma reactor R101. Furthermore, the reaction heat (temperature of 200°C-250°C) released by the Fischer-Tropsch synthesis reactor is used to preheat saturated water to generate saturated steam, thereby driving the third steam turbine T401 of the third power generation component to generate electricity, providing power for the plasma reactor R101.

[0067] In some preferred embodiments, the method for preparing the liquid fuel of the present invention comprises the following steps: (1) Preparation of dry synthesis gas.

[0068] CO2 and CH4 / N2 are mixed in the first mixing unit M100 to obtain a premixed gas, which is heated to 850-900°C by the first heating unit, and H2O is heated to 850-900°C by the second heating unit to obtain water vapor to meet the feed conditions of the plasma reactor R101. Further, the heated premixed gas and water vapor are mixed in the second mixing unit to obtain a first mixed gas, and the first mixed gas is sent to the plasma reactor R101 for reaction and converted into high-temperature synthesis gas.

[0069] The high temperature synthesis gas is cooled to 5-40°C by the third heat exchange component to obtain low temperature synthesis gas, which is then sent to the first flash tank V100. The moisture in the low temperature synthesis gas is removed from the bottom of the first flash tank V100 to obtain dry synthesis gas, which is then sent to the compressor C100 through the top of the first flash tank V100. When used, the dry synthesis includes N2, CO2, CO, and H2.

[0070] (2) Preparation of liquid fuel.

[0071] The dry synthesis gas extracted from the top of the first flash tank V100 is pressurized to 15-25 bar by the compressor C100 to obtain compressed synthesis gas, and the compressed synthesis gas is mixed evenly with the mixed gas separated by flash evaporation in the second flash tank V101 in the third mixing unit M102 to obtain the second mixed gas. When used, the mixed gas includes N2, CO2, CO, H2, CH4, C3H6, and C3H8. The second mixed gas is heated to 200-250°C by the second heat exchange component to meet the feeding conditions of the Fischer-Tropsch reactor R102. Further, a high-temperature hydrocarbon mixture is generated by reaction in the Fischer-Tropsch reactor R102, and the high-temperature hydrocarbon mixture contains unreacted mixed gas. The high-temperature hydrocarbon mixture is cooled to 5-40°C by the fourth heat exchange component to obtain a low-temperature hydrocarbon mixture, and the low-temperature hydrocarbon mixture is passed into the second flash tank V101 for flash separation to remove the unreacted mixed gas therein, that is, the mixed gas and the water-containing liquid fuel are separated.

[0072] The mixed gas flows out from the top of the second flash tank V101 to the splitter F100, the water-containing liquid fuel is extracted from the bottom of the second flash tank V101, and the water-containing liquid fuel is sent to the dryer D101 to remove the water therein, and the dehydrated liquid fuel is obtained in the dryer D101.

[0073] (3) Cascade utilization of system energy.

[0074] 3.1 Using high temperature synthesis gas to preheat the first mixed gas.

[0075] First, the high-temperature synthesis gas at the outlet of the plasma reactor R101 exchanges heat with the raw gas (eg, the first mixed gas) entering the plasma reactor R101 in the third heat exchanger E102 and the first heat exchanger E100.

[0076] 3.2 Use high temperature synthesis gas to provide thermal energy for the first power generation component.

[0077] Next, the high-temperature synthesis gas after treatment in 3.1 enters the ninth heat exchanger E201 and exchanges heat with the liquid organic working fluid in the ninth heat exchanger E201 to obtain the gaseous organic working fluid. The gaseous organic working fluid is sent to the first steam turbine T201, so that the first steam turbine T201 generates electricity to provide electrical energy for the plasma reactor R101, and produces low-pressure gaseous organic working fluid. The low-pressure gaseous organic working fluid enters the tenth heat exchanger E202 and is condensed into liquid organic working fluid. The liquid organic working fluid is sent to the second booster pump P201, and the second booster pump P201 pressurizes the liquid organic working fluid to 2-5 bar, and sends the pressurized liquid organic working fluid back to the ninth heat exchanger E201.

[0078] 3.3 Preheat the second mixed gas using the high temperature hydrocarbon mixture.

[0079] The high-temperature hydrocarbon mixture at the outlet of the Fischer-Tropsch reactor R102 exchanges heat with the second mixed gas entering the Fischer-Tropsch reactor R102 in the sixth heat exchanger E105.

[0080] 3.4 Use the high temperature hydrocarbon mixture to provide thermal energy for the second power generation component.

[0081] Next, the high-temperature hydrocarbon mixture after treatment in 3.3 enters the eleventh heat exchanger E301, and exchanges heat with the liquid organic working fluid in the eleventh heat exchanger E301 to obtain gaseous organic working fluid, which is sent to the second steam turbine T301 to generate electricity and provide electrical energy for the plasma reactor R101. The generated low-pressure gaseous organic working fluid enters the twelfth heat exchanger E302 and is condensed into liquid organic working fluid, which is sent to the third booster pump P301. The third booster pump P301 pressurizes the liquid organic working fluid to 2-5 bar, and the pressurized liquid organic working fluid is sent back to the eleventh heat exchanger E301.

[0082] 3.5 Utilize the reaction heat released by the Fischer-Tropsch synthesis reactor to provide thermal energy for the third power generation component.

[0083] The reaction heat released by the Fischer-Tropsch synthesis reactor is sent to the thirteenth heat exchanger E401, and the saturated water in the thirteenth heat exchanger E401 is preheated to generate saturated steam, and the saturated steam is sent to the third steam turbine T401 to drive the third steam turbine T401 to generate electricity and provide electric energy for the plasma reactor R101. The generated unsaturated steam enters the fourteenth heat exchanger E402 and condenses into saturated water. The condensed saturated water is sent to the fourth booster pump P401, and the fourth booster pump P401 pressurizes the condensed saturated water to 20-40 bar. The pressurized saturated water is sent back to the thirteenth heat exchanger E401. Example 1

[0084] By using the liquid fuel preparation device based on the plasma reactor R101 of the present invention, the landfill gas and water are used to perform the above steps: (1) preparing dry synthesis gas and (2) preparing liquid fuel, thereby obtaining liquid fuel. The energy utilization rate of this embodiment is 42.13%, and the net CO2 emission reduction rate is 61.59%. Example 2

[0085] By using the liquid fuel preparation device based on the plasma reactor R101 of the present invention, the landfill gas and water are used to perform the above steps: (1) preparing dry synthesis gas and (2) preparing liquid fuel, 3.1 preheating the first mixed gas using the high-temperature synthesis gas and 3.3 preheating the second mixed gas using the high-temperature hydrocarbon mixture, thereby obtaining liquid fuel. The energy utilization rate of this embodiment is 45.23%, and the net CO2 emission reduction rate is 63.29%. Example 3

[0086] By using the liquid fuel preparation device based on the plasma reactor R101 of the present invention, landfill gas and water are used to perform the above steps: (1) preparing dry synthesis gas, (2) preparing liquid fuel, and (3) cascade utilization of system energy, thereby obtaining liquid fuel. The energy efficiency of this embodiment is 46.28%, and the net CO2 emission reduction rate is 64.57%.

[0087] From the above embodiments, it can be seen that: after the landfill gas and water are preheated and mixed, they react in the plasma reactor R101 to obtain high-temperature synthesis gas; the high-temperature synthesis gas mainly contains CO2, CO, H2 and H2O, and the high-temperature synthesis gas is cooled and flashed to remove the H2O therein, and the dry synthesis gas is pressurized and preheated, and then reacted in the Fischer-Tropsch reactor R102 to obtain a high-temperature hydrocarbon mixture; the high-temperature hydrocarbon mixture contains unreacted mixed gas, and the high-temperature hydrocarbon mixture is cooled and flashed to remove the unreacted mixed gas therein to obtain water-containing liquid fuel, which contains a small amount of H2O, and the water therein is removed by the dryer D101 to obtain liquid fuel.

[0088] In addition, the present invention also uses the remaining heat in the process in a cascaded manner: using high-temperature synthesis gas to preheat the first mixed gas, and using high-temperature hydrocarbon mixture to preheat the second mixed gas, so as to improve energy efficiency and net CO2 emission reduction rate. Further, high-temperature synthesis gas is used to provide heat energy for the first power generation component, high-temperature hydrocarbon mixture is used to provide heat energy for the second power generation component, and the reaction heat released by the Fischer-Tropsch synthesis reactor is used to provide heat energy for the third power generation component, so as to achieve energy efficiency and net CO2 emission reduction rate of 46.28% and 64.57% respectively.

[0089] Although the embodiments of the present invention have been shown and described above, it is to be understood that the above embodiments are exemplary and are not to be construed as limitations on the present invention. A person skilled in the art may change, modify, substitute and modify the above embodiments within the scope of the invention without departing from the principles and purpose of the present invention. All such changes should fall within the scope of protection of the claims of the present invention.

Claims

1. A liquid fuel preparation device based on a plasma reactor, characterized in that: include: A gas synthesis section, the gas synthesis section comprises a storage component, a first heat exchange component, a second mixing unit, a plasma reactor, a third heat exchange component and a first flash tank connected in sequence, wherein the storage component is used to store gas and liquid, the storage component is connected to the low temperature end of the first heat exchange component, the high temperature end of the first heat exchange component is connected to the second mixing unit, the plasma reactor is connected to the high temperature end of the third heat exchange component, and the low temperature end of the third heat exchange component is connected to the first flash tank; A fuel synthesis section, which includes a compressor, a mixing component, a second heat exchange component, a Fischer-Tropsch reactor, a fourth heat exchange component, a second flash tank, a dryer, and a fuel collection unit connected in sequence, wherein the compressor is connected to the first flash tank, the mixing component is connected to the top of the second flash tank and the low-temperature end of the second heat exchange component, the high-temperature end of the second heat exchange component is connected to the Fischer-Tropsch reactor, the high-temperature end of the fourth heat exchange component is connected to the Fischer-Tropsch reactor, the low-temperature end of the fourth heat exchange component is connected to the second flash tank, and the fuel collection unit is used to collect liquid fuel.

2. The liquid fuel preparation device based on a plasma reactor according to claim 1, characterized in that: The storage component comprises: A first storage unit, wherein the first storage unit is used to store CO2; A second storage unit, the second storage unit is used to store CH4 / N2; A third storage unit, the third storage unit is used to store H2O, and an output end of the third storage unit is connected to a low temperature end of the first heat exchange component; A first mixing unit, wherein an input end of the first mixing unit is connected to the first storage unit and the second storage unit, and an output end of the first mixing unit is connected to a low-temperature end of the first heat exchange component.

3. The liquid fuel preparation device based on a plasma reactor according to claim 2, characterized in that: The storage component also includes: A fourth storage unit is used to store landfill gas, and an output end of the fourth storage unit is connected to an input end of the first mixing unit or a low-temperature end of the first heat exchange component.

4. The liquid fuel preparation device based on a plasma reactor according to claim 2, characterized in that: The first heat exchange component comprises: A first heating unit, the first heating unit comprising a first heat exchanger and a second heat exchanger, the low temperature end of the first heat exchanger is connected to the first mixing unit, the high temperature end of the first heat exchanger is connected to the low temperature end of the second heat exchanger, and the high temperature end of the second heat exchanger is connected to the second mixing unit; a second heating unit, the second heating unit comprising: a third heat exchanger and a fourth heat exchanger, the low temperature end of the third heat exchanger is connected to the third storage unit, the high temperature end of the third heat exchanger is connected to the low temperature end of the fourth heat exchanger, and the high temperature end of the fourth heat exchanger is connected to the second mixing unit; The second heat exchange component includes: a sixth heat exchanger and a seventh heat exchanger, the low-temperature end of the sixth heat exchanger is connected to the mixing component, the high-temperature end of the sixth heat exchanger is connected to the low-temperature end of the seventh heat exchanger, and the high-temperature end of the seventh heat exchanger is connected to the Fischer-Tropsch reactor.

5. The liquid fuel preparation device based on a plasma reactor according to claim 1, characterized in that: The third heat exchanger comprises: a ninth heat exchanger and a fourth heat exchanger, the high temperature end of the ninth heat exchanger is connected to the plasma reactor, the low temperature end of the ninth heat exchanger is connected to the high temperature end of the fourth heat exchanger, and the low temperature end of the fourth heat exchanger is connected to the first flash tank; The fourth heat exchange component includes: an eleventh heat exchanger and an eighth heat exchanger, the high temperature end of the eleventh heat exchanger is connected to the Fischer-Tropsch reactor, the low temperature end of the eleventh heat exchanger is connected to the high temperature end of the eighth heat exchanger, and the low temperature end of the eighth heat exchanger is connected to the second flash tank.

6. The liquid fuel preparation device based on a plasma reactor according to claim 4, characterized in that: The third heat exchanger comprises: a ninth heat exchanger and a fourth heat exchanger; The outlet of the plasma reactor is connected to the high temperature end of the third heat exchanger, the low temperature end of the third heat exchanger is connected to the high temperature end of the first heat exchanger, the low temperature end of the first heat exchanger is connected to the high temperature end of the ninth heat exchanger, the low temperature end of the ninth heat exchanger is connected to the high temperature end of the fourth heat exchanger, and the low temperature end of the fourth heat exchanger is connected to the first flash tank; The fourth heat exchanger comprises: an eleventh heat exchanger and an eighth heat exchanger; The outlet of the Fischer-Tropsch reactor is connected to the high-temperature end of the sixth heat exchanger, the low-temperature end of the sixth heat exchanger is connected to the high-temperature end of the eleventh heat exchanger, the low-temperature end of the eleventh heat exchanger is connected to the high-temperature end of the eighth heat exchanger, and the low-temperature end of the eighth heat exchanger is connected to the second flash tank.

7. The liquid fuel preparation device based on a plasma reactor according to claim 1, characterized in that: The liquid fuel preparation device also includes: A power generation unit, the power generation unit comprising: a first power generation component, the first power generation component comprising a first steam turbine, a tenth heat exchanger and a second booster pump, the first steam turbine being used to supply power to the plasma reactor, one end of the first steam turbine being connected to the low temperature end of the ninth heat exchanger, the other end of the first steam turbine being connected to the low temperature end of the tenth heat exchanger, one end of the second booster pump being connected to the high temperature end of the tenth heat exchanger, and the other end of the second booster pump being connected to the low temperature end of the third heat exchanger; a second power generation component, the second power generation component comprising a second steam turbine, a twelfth heat exchanger and a third booster pump, the second steam turbine is used to supply power to the plasma reactor, one end of the second steam turbine is connected to the low temperature end of the eleventh heat exchanger, the other end of the second steam turbine is connected to the low temperature end of the twelfth heat exchanger, one end of the third booster pump is connected to the high temperature end of the twelfth heat exchanger, and the other end of the third booster pump is connected to the low temperature end of the fourth heat exchanger; The third power generation component includes a thirteenth heat exchanger, a third steam turbine, a fourteenth heat exchanger and a fourth booster pump connected in sequence, the high temperature end of the thirteenth heat exchanger is connected to the Fischer-Tropsch reactor, the third steam turbine supplies power to the plasma reactor, and the high temperature end of the fourteenth heat exchanger is connected to the high temperature end of the thirteenth heat exchanger.

8. The liquid fuel preparation device based on a plasma reactor according to claim 1, characterized in that: The mixing assembly comprises: a flow splitter connected to the top of the second flash tank; A third mixing unit, one end of which is connected to the compressor and a part of the diverter, and the other end of which is connected to the low-temperature end of the second heat exchange component.

9. A method for preparing liquid fuel based on a plasma reactor, characterized in that: The following steps are involved: The landfill gas and water in the storage component are heated by the first heat exchange component, and after being uniformly mixed in the second mixing unit, a first mixed gas is obtained, and the first mixed gas is introduced into the plasma reactor for reaction to obtain high-temperature synthesis gas; The high-temperature synthesis gas is cooled by the third heat exchange component to obtain low-temperature synthesis gas, and the low-temperature synthesis gas is passed into the first flash tank for flash separation to obtain dry synthesis gas; After the dry synthesis gas is compressed by a compressor, a compressed synthesis gas is obtained; the compressed synthesis gas and the mixed gas separated by flash evaporation in a second flash tank are placed in a mixing assembly for uniform mixing to obtain a second mixed gas; the second mixed gas is heated by a second heat exchange assembly and then introduced into a Fischer-Tropsch reactor for reaction to obtain a high-temperature hydrocarbon mixture; The high-temperature hydrocarbon mixture is cooled by the fourth heat exchange component to obtain a low-temperature hydrocarbon mixture, and the low-temperature hydrocarbon mixture is passed into a second flash tank for flash separation to obtain a mixed gas and a water-containing liquid fuel; The water-containing liquid fuel is dehydrated by using a dryer to obtain liquid fuel.

10. The method for preparing liquid fuel based on a plasma reactor according to claim 9, characterized in that: In the plasma reactor: the temperature is 850-900°C; the pressure is 1-3 bar; In the first flash tank: the temperature is 5-20°C; The pressure is 1-3 bar; In the compressor: the pressure is 15-25 bar; In the Fischer-Tropsch reactor: the temperature is 200-250°C; the pressure is 15-25 bar; In the second flash tank: the temperature is 5-20°C; the pressure is 15-25 bar; In the dryer: temperature is 5-20°C; pressure is 1-3 bar.

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