CN117703375A - Preparation system and method of coal-based high-density fuel - Google Patents
Preparation system and method of coal-based high-density fuel Download PDFInfo
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Abstract
The invention belongs to the technical field of underground coal pyrolysis, and particularly discloses a preparation system and a preparation method of coal-based high-density fuel, wherein a high-temperature mixed heat carrier is introduced into a coal seam for crack pyrolysis, an oil-gas mixture formed is enriched and then transported to a first catalyst layer for primary hydrogenation and upgrading to obtain a first product, and the first product is extracted to a first rectifying tower and is divided into a light fraction product, a heavy fraction product and an oil-gas product; introducing the heavy fraction product into a second catalytic layer, carrying out heavy fraction hydrogenation upgrading, and then conveying to a third catalytic layer for saturated hydrogenation to obtain an oil gas product; introducing the light fraction product into a third catalytic layer for tar saturation hydrogenation to obtain an oil gas product; the oil gas product enters a second rectifying tower, and the second rectifying tower is used for separating to obtain the high-density fuel. Solves the problems of shortage of petroleum resources, heavy weight and poor stability of pure coal-based jet fuel, and the obtained coal-based high-density fuel has the characteristics of coal-based and petroleum-based fuel oil and meets the requirements of future high-performance aircrafts.
Description
Technical Field
The invention belongs to the technical field of underground pyrolysis of coal, and particularly relates to a preparation system and method of coal-based high-density fuel.
Background
With the continuous expansion of the international air transportation industry, the demand for aviation fuel is increasingly urgent. Currently aviation jet fuel is produced primarily from petroleum-based feedstocks. At present, the global situation is relatively unstable, and the energy safety is an important guarantee and demand for development in China.
The existing technology using coal-based oil as raw material is that after coal exploitation, hydrofining or hydrocracking is carried out, then distillation and cutting are carried out on the product, and jet fuel characteristic fraction is cut and taken as jet fuel or jet fuel blending component, and the stability of the jet fuel characteristic fraction obtained at this time is poor.
Disclosure of Invention
The invention aims to provide a preparation system and a preparation method of coal-based high-density fuel, which are used for solving the problem that the stability of the obtained jet fuel characteristic fraction serving as jet fuel or jet fuel blending component is poor when the product is distilled and cut after hydrofining or hydrocracking is carried out after coal exploitation.
In order to achieve the above purpose, the invention is realized by adopting the following technical scheme:
in a first aspect, the present invention provides a system for preparing a coal-based high density fuel, comprising:
the device comprises an injection well, a first catalytic layer, a second catalytic layer, a third catalytic layer, a pumping well, an enrichment well, a hybrid heater, a hybrid pressurizer, a gas separation device, a hydrogen supply module, a first rectifying tower, a second rectifying tower, a hydrogen pressurizer and a hydrogen heater;
the outlet of the mixing heater is connected with the inlet of the mixing pressurizer, the outlet of the mixing pressurizer is connected with the injection well, and the injection well, the third catalytic layer and the extraction well are arranged in the coal seam; the first catalytic layer and the second catalytic layer are arranged at the stratum below the lower boundary of the coal seam;
the enrichment well is closely arranged at the bottom of the lower boundary of the coal bed, the enrichment well is connected with a first inlet of the first catalytic layer, a first outlet of the first catalytic layer is connected with an inlet of the first rectifying tower, an outlet of the second catalytic layer is connected with an inlet of the third catalytic layer, and an outlet of the third catalytic layer is connected with an inlet of the second rectifying tower;
the first outlet of the first rectifying tower is connected with the first inlet of the second catalytic layer, the second outlet of the first rectifying tower is connected with the first inlet of the third catalytic layer, and the third outlet of the first rectifying tower is connected with the inlet of the second rectifying tower;
the outlet of the second catalytic layer is connected with the inlet of the third catalytic layer, the outlet of the third catalytic layer is connected with the inlet of the second rectifying tower, the outlet of the second rectifying tower is connected with the inlet of the gas separation device, the outlet of the gas separation device is respectively connected with the inlet of the hybrid heater and the inlets of the three hydrogen heaters, and the outlets of the three hydrogen heaters are respectively connected with the inlets of the corresponding hydrogen pressurizer; the outlets of the three hydrogen pressurizers are respectively connected with three hydrogen supply pipelines, and are respectively connected with the second inlet of the first catalytic layer, the second inlet of the second catalytic layer and the second inlet of the third catalytic layer through the three hydrogen supply pipelines; the outlet of the hydrogen supply module is connected with the gas separation device.
Furthermore, the injection well and the extraction well are perpendicular to the ground, and are arranged from the upper boundary of the coal bed to the lower boundary of the coal bed in the coal bed.
Further, the first catalytic layer and the second catalytic layer are parallel to the ground and are arranged at the stratum below the lower boundary of the coal seam, and the first catalytic layer is arranged at the lower part of the second catalytic layer; the third catalytic layer is perpendicular to the ground and is arranged in the coal seam.
Further, the first catalytic layer is an iron-molybdenum catalyst layer for primary hydrogenation upgrading; the second catalytic layer is a nickel-molybdenum catalyst layer for heavy fraction hydrogenation upgrading; the third catalytic layer is a nickel-molybdenum catalyst layer for tar saturation hydrogenation.
Further, the hydrogen heater comprises a first hydrogen heater, a second hydrogen heater and a third hydrogen heater; the hydrogen pressurizer comprises a first hydrogen pressurizer, a second hydrogen pressurizer and a third hydrogen pressurizer; the hydrogen supply pipeline comprises a first hydrogen supply pipeline, a second hydrogen supply pipeline and a third hydrogen supply pipeline; the outlet of the gas separation device is respectively connected with inlets of the mixing heater, the first hydrogen heater, the second hydrogen heater and the third hydrogen heater; the outlet of the first hydrogen heater is connected with the inlet of the first hydrogen pressurizer, the outlet of the first hydrogen pressurizer is connected with a first hydrogen supply pipeline, and the first hydrogen supply pipeline is connected with the first catalytic layer and is used for supplying hydrogen to the first catalytic layer; the outlet of the second hydrogen heater is connected with the inlet of the second hydrogen pressurizer, the outlet of the second hydrogen pressurizer is connected with a second hydrogen supply pipeline, and the second hydrogen supply pipeline is connected with the second catalytic layer and is used for supplying hydrogen to the second catalytic layer; the outlet of the third hydrogen heater is connected with the inlet of the third hydrogen pressurizer, the outlet of the third hydrogen pressurizer is connected with a third hydrogen supply pipeline, and the third hydrogen supply pipeline is connected with the third catalytic layer and is used for supplying hydrogen to the third catalytic layer.
Furthermore, the hydrogen production module comprises two vertical wells and the bottom of the two vertical wells, wherein the two vertical wells are communicated with the bottom of the two vertical wells through horizontal wells, a methanation catalyst filling layer is arranged in the horizontal wells, methane steam reforming catalyst filling layers are arranged in the middle parts of the two vertical wells, and air outlets of the two vertical wells are connected with an inlet of the gas separation device.
In a second aspect, the present invention provides a method for preparing a coal-based high density fuel, based on the preparation system of the coal-based high density fuel described in any one of the above, comprising:
the method comprises the steps of mining an injection well and a drainage well, arranging a hydrogen production module, and fracturing a coal bed to form a coal bed fracture; a third catalytic layer is vertically arranged in the coal seam, and a first catalytic layer and a second catalytic layer are arranged at the stratum below the lower boundary of the coal seam;
CO 2 and H 2 O is mixed and heated in a mixing heater, and then is introduced into a mixing pressurizer, a high-temperature mixed heat carrier is formed after pressurization, the high-temperature mixed heat carrier is introduced into a coal seam crack through an injection well, the coal seam is heated and pyrolyzed, and an oil-gas mixture is generated;
H 2 heating and pressurizing three sets of hydrogen heaters and hydrogen pressurizers which are mutually independent to working conditions, and then introducing 3 catalyst layers through respective hydrogen supply pipelines to supply hydrogen;
enriching the oil-gas mixture at an enrichment well, transporting the oil-gas mixture to a first catalyst layer for primary hydrogenation upgrading, extracting an obtained first product to a first rectifying tower for prefractionation, and dividing the first product into a light fraction product, a heavy fraction product and an oil-gas product;
conveying the heavy fraction product to a second catalytic layer, conveying the light fraction product to a third catalytic layer, and conveying the residual oil gas product to a second rectifying tower;
the heavy fraction product is fed into a second catalytic layer, heavy fraction hydrogenation upgrading is carried out firstly, and tar after heavy fraction hydrogenation upgrading is completed is conveyed to a third catalytic layer for saturated hydrogenation, so that an oil gas product is obtained;
introducing the light fraction product into a third catalytic layer for tar saturation hydrogenation to obtain an oil gas product;
the oil gas product enters a second rectifying tower, the second rectifying tower is used for separating to obtain diesel oil, high-density fuel, phenol oil and mixed gas, the mixed gas is continuously conveyed to a gas separation device for separation, pyrolysis gas is separated, and the separated pyrolysis gas is conveyed to a mixed heater and three hydrogen heaters for recycling;
and enabling gas phase products generated by coal bed pyrolysis to enter a hydrogen production module to perform methanation reaction and methane steam reforming reaction, extracting the gas to a gas separation device for separation, and enabling separated hydrogen to be used for subsequently introducing the first catalytic layer, the second catalytic layer and the third catalytic layer for reaction.
Further, the first catalyst layer is located 810-830 meters below the ground, the second catalyst layer is located 490 meters below the ground, and the third catalyst layer is located 170 meters below the ground.
Furthermore, the gas phase product generated by pyrolysis enters the horizontal well to perform methanation reaction and methane steam reforming reaction with the methanation catalyst filling layer and the methane steam reforming catalyst filling layer.
Further, the reaction conditions of the primary hydrogenation upgrading are as follows: 320-420 ℃ and 20MPa, wherein the catalyst adopts an iron-molybdenum catalyst; the reaction conditions for hydrogenating and upgrading the heavy fraction are as follows: 180-300 ℃ and 12MPa, and a nickel-molybdenum catalyst is adopted as the catalyst; the reaction conditions of the tar saturation hydrogenation are as follows: 360-400 ℃ and 4.2MPa, and the catalyst adopts a nickel-molybdenum catalyst.
The invention has at least the following beneficial effects:
the invention exploits the injection well, set up multiple catalytic layers in coal seam and stratum, let the high-temperature mixed heat carrier into the seam fracture from the injection well, pyrolyze and form the oil-gas mixture, the oil-gas mixture is transported to the first catalytic layer and hydrogenated and upgraded in the first step after enriching the well and get the first product, the first product is extracted to the first rectifying tower, carry on the prefractionation, divide into light fraction product, heavy fraction product and oil-gas product; the heavy fraction product is fed into a second catalytic layer, heavy fraction hydrogenation upgrading is carried out firstly, and tar after heavy fraction hydrogenation upgrading is completed is conveyed to a third catalytic layer for saturated hydrogenation, so that an oil gas product is obtained; introducing the light fraction product into a third catalytic layer for tar saturation hydrogenation to obtain an oil gas product; the oil gas product enters a second rectifying tower, and the second rectifying tower is used for separating to obtain the high-density fuel. Solves the problems of shortage of petroleum resources, heavy weight and poor stability of pure coal-based jet fuel, and the obtained coal-based high-density fuel has the characteristics of coal-based and petroleum-based fuel oil and meets the requirements of future high-performance aircrafts.
2. The invention can directly upgrade tar underground without carrying out process operation on the ground after extraction and separation; avoiding the transportation and processing of tar products, improving the industrial process efficiency and reducing the energy consumption.
Drawings
The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the invention.
In the drawings:
FIG. 1 is a schematic diagram of a system for preparing a coal-based high density fuel;
reference numerals: 1. an injection well; 2. an upper boundary of the coal seam; 3. a coal seam; 4. a lower boundary of the coal seam; 5. a first catalytic layer; 6. a second catalytic layer; 7. a third catalytic layer; 8. extracting well; 9. an enrichment well; 10. a hybrid heater; 11. a mixing pressurizer; 12. a gas separation device; 13. a hydrogen production module; 131. a methane steam reforming catalyst packing layer; 132. a methanation catalyst packing layer; 14. a first rectifying column; 15. a second rectifying column; 51. a first hydrogen heater; 61. a second hydrogen heater; 71. a third hydrogen heater; 52. a first hydrogen pressurizer; 62. a second hydrogen pressurizer; 72. a third hydrogen pressurizer; 53. a first hydrogen supply pipe; 63. a second hydrogen supply pipe; 73. and a third hydrogen supply pipeline.
Detailed Description
The invention will be described in detail below with reference to the drawings in connection with embodiments. It should be noted that, without conflict, the embodiments of the present invention and features of the embodiments may be combined with each other.
The following detailed description is exemplary and is intended to provide further details of the invention. Unless defined otherwise, all technical terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments in accordance with the invention.
Example 1
As shown in fig. 1, a system for preparing a coal-based high density fuel, comprising:
injection well 1, first catalytic layer 5, second catalytic layer 6, third catalytic layer 7, extraction well 8, enrichment well 9, mixing heater 10, mixing pressurizer 11, gas separation device 12, hydrogen supply module 13, first rectifying tower 14, second rectifying tower 15, hydrogen pressurizer and hydrogen heater;
the outlet of the mixing heater 10 is connected with the inlet of the mixing pressurizer 11, and the outlet of the mixing pressurizer 11 is connected with the injection well 1; CO 2 And H 2 O is mixed and heated in a mixing heater 10 and then is introduced into a mixing pressurizer 11, a high-temperature mixed heat carrier is formed after pressurization, the high-temperature mixed heat carrier is introduced into a coal seam crack through an injection well 1, and CO 2 For heating coal seams, H 2 O is used for providing a hydrogen-rich environment for pyrolysis of the coal seam; hybrid heater 10 is used for CO 2 And H 2 O is heated at high temperature, and the mixing pressurizer 11 is used for pressurizing the hydrogen and the water vapor heated at high temperature to form a high-temperature mixed heat carrier.
The injection well 1 and the extraction well 8 are vertical to the ground, and are arranged from the upper boundary 2 of the coal bed to the lower boundary 4 of the coal bed in the coal bed 3; fracturing the coal seam 3 to form cracks, and injecting a heated and pressurized high-temperature mixed heat carrier into the injection well 1, wherein the high-temperature mixed heat carrier is pyrolyzed in the cracks of the coal seam to obtain an oil-gas mixture; the extraction well 8 is used for extracting the catalyzed enriched product.
The first catalytic layer 5 and the second catalytic layer 6 are parallel to the ground and are arranged at the stratum below the lower boundary 4 of the coal seam, and the first catalytic layer 5 is arranged at the lower part of the second catalytic layer 6; the third catalytic layer 7 is vertical to the ground and is arranged inside the coal seam 3; the first catalytic layer 5 is an iron-molybdenum catalyst layer for primary hydrogenation upgrading of tar; the second catalytic layer 6 is a nickel-molybdenum catalyst layer for hydrocracking the pyrolysis tar heavy fraction; the third catalytic layer 7 is a nickel-molybdenum catalyst layer for tar saturation hydrogenation;
the enrichment well 9 is arranged close to the bottom of the coal bed lower boundary 4 and is used for collecting the pyrolyzed oil-gas mixture; the enrichment well 9 is connected with a first inlet of the first catalytic layer 5, an outlet of the first catalytic layer 5 is connected with an inlet of the first rectifying tower 14, an outlet of the second catalytic layer 6 is connected with an inlet of the third catalytic layer 9, and an outlet of the third catalytic layer 9 is connected with an inlet of the second rectifying tower 15;
the first outlet of the first rectifying tower 14 is connected with the first inlet of the second catalytic layer 6, the second outlet of the first rectifying tower 14 is connected with the first inlet of the third catalytic layer 7, and the third outlet of the first rectifying tower 14 is connected with the inlet of the second rectifying tower 15; the first rectifying tower 14 is arranged at the bottom of the extraction well 8, and the second rectifying tower 15 is arranged on the ground.
The outlet of the second catalytic layer 6 is connected with the inlet of the third catalytic layer 7, the outlet of the third catalytic layer 7 is connected with the inlet of the second rectifying tower 15, the outlet of the second rectifying tower 15 is connected with the inlet of the gas separation device 12, the outlet of the gas separation device 12 is respectively connected with the inlet of the hybrid heater 10 and the inlets of the three hydrogen heaters, and the outlets of the three hydrogen heaters are respectively connected with the inlets of the corresponding hydrogen pressurizers; the outlets of the three hydrogen pressurizers are respectively connected with three hydrogen supply pipelines, and are respectively connected with the second inlet of the first catalytic layer 5, the second inlet of the second catalytic layer 6 and the second inlet of the third catalytic layer 7 through three hydrogen supply pipelines 11.
The hydrogen heaters include a first hydrogen heater 51, a second hydrogen heater 61, and a third hydrogen heater 71; the hydrogen pressurizer includes a first hydrogen pressurizer 52, a second hydrogen pressurizer 62 and a third hydrogen pressurizer 72; the hydrogen supply pipes include a first hydrogen supply pipe 53, a second hydrogen supply pipe 63, and a third hydrogen supply pipe 73; the outlets of the gas separation device 12 are respectively connected with inlets of the mixing heater 10, the first hydrogen heater 51, the second hydrogen heater 61 and the third hydrogen heater 71; the outlet of the first hydrogen heater 51 is connected with the inlet of the first hydrogen pressurizer 52, the outlet of the first hydrogen pressurizer 52 is connected with the first hydrogen supply pipeline 53, and the first hydrogen supply pipeline 53 is connected with the first catalytic layer 5 and is used for supplying hydrogen to the first catalytic layer 5; the outlet of the second hydrogen heater 61 is connected with the inlet of the second hydrogen pressurizer 62, the outlet of the second hydrogen pressurizer 62 is connected with a second hydrogen supply pipeline 63, and the second hydrogen supply pipeline 63 is connected with the second catalytic layer 6 and is used for supplying hydrogen to the second catalytic layer 6; the outlet of the third hydrogen heater 71 is connected to the inlet of the third hydrogen pressurizer 72, the outlet of the third hydrogen pressurizer 72 is connected to the third hydrogen supply pipe 73, and the third hydrogen supply pipe 73 is connected to the third catalytic layer 7 for supplying hydrogen to the third catalytic layer 7.
The methane gas separation device further comprises a hydrogen production module 13, the hydrogen production module 13 comprises two vertical wells, the bottoms of the two vertical wells are communicated through a horizontal well, a methanation catalyst filling layer 132 is arranged in the horizontal well, methane steam reforming catalyst filling layers 131 are arranged in the middle of the two vertical wells, and gas outlets of the two vertical wells are connected with an inlet of the gas separation device 12.
When the hydrogen production module 13 works, the coal bed 3 is heated by the heat released by the combustion of the coal bed, the gas phase products generated by the pyrolysis gather towards the upper part of the coal bed 3 due to the action of gravity, the gas phase products enter a horizontal well to perform methanation reaction and methane steam reforming reaction with the methanation catalyst filling layer 132 and the methane steam reforming catalyst filling layer 131, then are extracted to the gas separation device 12 for separation, and the separated hydrogen is used for subsequent reaction of the first catalytic layer 5, the second catalytic layer 6 and the third catalytic layer 7.
Example 2
A method for preparing a coal-based high density fuel, comprising:
s1: the method comprises the steps of (1) mining an injection well and a drainage well, wherein a hydrogen production module 13 is arranged, and fracturing a coal seam 3 to form a coal seam crack; a third catalytic layer 7 is vertically arranged in the coal seam 3, a first catalytic layer 5 and a second catalytic layer 6 are arranged below the lower boundary 4 of the coal seam, and the first catalytic layer 5 is arranged below the second catalytic layer 6;
the first catalytic layer 5 is an iron-molybdenum catalyst layer 1 for primary hydrogenation upgrading of tar; the second catalytic layer 6 is a nickel-molybdenum catalyst layer 2 for hydrocracking pyrolysis tar heavy fraction; the third catalytic layer 7 is a nickel-molybdenum catalyst layer 3 for tar saturation hydrogenation;
S2：CO 2 and H 2 O is mixed and heated in a mixing heater 10 at 600 ℃, then is introduced into a mixing pressurizer 11, a high-temperature mixed heat carrier is formed after the pressure is increased to 4MPa-6MPa, the high-temperature mixed heat carrier is introduced into a coal seam crack through an injection well 1, and a coal seam 3 undergoes an in-situ pyrolysis reaction under the heating of the high-temperature mixed heat carrier to generate an oil-gas mixture; CO 2 For heating coal seams, H 2 O is used for providing a hydrogen-rich environment for pyrolysis of the coal seam;
S3：H 2 from three sets of hydrogen heaters and hydrogen pressurizers which are independent to each other to heat and pressurizeAfter working conditions, 3 catalyst layers are introduced through respective hydrogen supply pipelines to supply hydrogen;
specific: h 2 The first hydrogen heater 51, the second hydrogen heater 61, the third hydrogen heater 71, the first hydrogen pressurizer 52, the second hydrogen pressurizer 62 and the third hydrogen pressurizer 72 are heated and pressurized, and then are conveyed into the first hydrogen supply pipeline 53, the second hydrogen supply pipeline 63 and the third hydrogen supply pipeline 73, and are correspondingly conveyed into the first catalytic layer 5, the second catalytic layer 6 and the third catalytic layer 7 through different hydrogen supply pipelines;
the oil-gas mixture is enriched at an enrichment well 9 at the bottom of the coal bed and transported to a first catalyst layer 5 for primary hydrogenation and upgrading, the obtained first product is extracted to a first rectifying tower 14 for prefractionation, the heavy fraction product is transported to a second catalyst layer 6, the light fraction product is transported to a third catalyst layer 7, and the residual oil-gas product is transported to a second rectifying tower 15;
the first catalyst layer 5 is positioned at 810-830 m underground, and the reaction conditions of primary hydrogenation and upgrading are as follows: 320-420 ℃ and 20MPa, and the catalyst adopts an iron-molybdenum catalyst, namely H 2 Heating to 320-420 ℃ in the corresponding first hydrogen heater 51 and first hydrogen pressurizer 52 to 20MPa before being transported to the first catalyst layer 5;
the first product is cut in the first rectifying column 14, with the main products being three parts, a light fraction product, a heavy fraction product and an oil and gas product.
S4: the heavy fraction product is firstly subjected to heavy fraction hydrogenation upgrading by being led into a second catalytic layer 6; the second catalytic layer 6 is positioned under the ground by about 490 meters, and the heavy fraction hydrogenation and upgrading reaction conditions are as follows: 180-300 ℃ and 12MPa, and a nickel-molybdenum catalyst is adopted as the catalyst; conveying the tar after heavy fraction hydrogenation and upgrading to a third catalytic layer 7 for saturated hydrogenation to obtain an oil gas product, namely H 2 The second hydrogen heater 61 and the second hydrogen pressurizer 62 are heated to 180-300 ℃ and pressurized to 12MPa before being fed to the second catalytic layer 6.
Introducing the light fraction product into a third catalytic layer 7 for tar saturation hydrogenation to obtain an oil gas product; the third catalytic layer 7 is located about 170 m below the ground and is saturated with tarThe reaction conditions of hydrogenation are as follows: 360-400 ℃ and 4.2MPa, and the catalyst adopts nickel-molybdenum catalyst, namely H 2 Heating to 360-400 ℃ in the corresponding second heater 15 and second presser 16 to 4.2MPa before conveying to the third catalyst layer 7;
the oil gas product enters a second rectifying tower 15, the second rectifying tower 15 is used for separation to obtain diesel oil, high-density fuel, phenol oil and mixed gas, and the mixed gas is continuously conveyed into a gas separation device 12; the mixed gas is mainly micromolecular alkane and H 2 、H 2 O and CO 2 The gas is separated by the gas separator 12 to separate CO 2 、H 2 O and H 2 Wherein the separated CO 2 And H 2 O is conveyed to the mixing heater 10 for recycling, and the separated H is separated 2 Conveying the waste gas to three hydrogen heaters for recycling;
s5: when the hydrogen production module 13 works, the coal bed 3 is heated by the heat released by the combustion of the coal bed, the gas phase products generated by the pyrolysis gather towards the upper part of the coal bed 3 due to the action of gravity, the gas phase products enter a horizontal well to perform methanation reaction and methane steam reforming reaction with the methanation catalyst filling layer 132 and the methane steam reforming catalyst filling layer 131, then are extracted to the gas separation device 12 for separation, and the separated hydrogen is used for subsequent reaction of the first catalytic layer 5, the second catalytic layer 6 and the third catalytic layer 7.
Example 3
The rest structures of the preparation system of the coal-based high-density fuel are unchanged, and the first catalytic layer 5, the second catalytic layer 6 and the third catalytic layer 7 are arranged in the extraction well 8 to prepare the coal-based high-density fuel.
It will be appreciated by those skilled in the art that the present invention can be carried out in other embodiments without departing from the spirit or essential characteristics thereof. Accordingly, the above disclosed embodiments are illustrative in all respects, and not exclusive. All changes that come within the scope of the invention or equivalents thereto are intended to be embraced therein.
Finally, it should be noted that: the above embodiments are only for illustrating the technical aspects of the present invention and not for limiting the same, and although the present invention has been described in detail with reference to the above embodiments, it should be understood by those of ordinary skill in the art that: modifications and equivalents may be made to the specific embodiments of the invention without departing from the spirit and scope of the invention, which is intended to be covered by the claims.
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