Structural catalytic reactor for subcritical / supercritical hydrothermal modification of inferior heavy oil and use method of structural catalytic reactor

Abstract

The invention belongs to the technical field of petrochemical engineering, and particularly discloses a structural catalytic reactor for subcritical / supercritical hydrothermal modification of inferior heavy oil and a using method thereof.The structural catalytic reactor comprises an inner pipe and an outer pipe, the inner pipe is arranged in the outer pipe, the inner pipe and the outer pipe are coaxially arranged, and the outer pipe is arranged in the inner pipe; a first feeding port is formed in one end of the inner pipe, a second feeding port and a discharging port are formed in the two ends of the outer pipe respectively, an end is arranged between the inner pipe and the discharging port, the inner pipe is a porous pipe body, and the inner pipe is formed by alternately filling and sintering a stainless steel metal net and metal oxide powder. Wherein the stainless steel mesh plays a role in physical support and resistance to internal and external pressure difference, and the metal oxide plays a role in catalysis to catalyze flowing-through inferior heavy oil and water, so that the inferior heavy oil and water are subjected to in-situ hydrogen supply modification reaction. According to the invention, oil, water and catalyst three-phase mass and heat transfer can be enhanced from the molecular scale, so that the subcritical / supercritical water thermal cracking modification of the inferior heavy oil is improved.

Description

Technical Field

[0001] The invention relates to the technical field of petrochemical industry, and in particular to a structural catalytic reactor for sub- / supercritical hydrothermal reforming of inferior heavy oil and a use method thereof. Background Art

[0002] Globally, conventional oil with good quality has been exhausted in the past century, but unconventional oil and gas reservoirs such as heavy oil have been discovered continuously, accounting for more than 70% of the reserves. In addition, liquefied oil produced from coal and biomass resources is also low-quality heavy oil. Therefore, low-quality heavy oil will be one of the main petroleum raw materials in the future.

[0003] Low-quality heavy oil has the characteristics of high viscosity, many heteroatoms, large molecular weight, and low H / C. It needs to be hydrocracking and reformed into low-viscosity petroleum for easy mining, transportation, and subsequent processing and utilization. Hydrothermal reforming technology using sub- / supercritical water as the reaction medium has been widely studied for the reforming of low-quality heavy oil, but sub- / supercritical water mainly acts as a solvent for dissolving and dispersing low-quality heavy oil, and its hydrogen supply reaction ability is weak, which is difficult to meet the hydrogenation requirements of low-quality heavy oil reforming. Therefore, it is necessary to add a catalyst to enhance the hydrogen supply capacity of sub- / supercritical water.

[0004] Metal oxides have been widely proven to have good catalytic effects on the sub- / supercritical hydrothermal reforming process of inferior heavy oil. However, due to the high viscosity of inferior heavy oil, it is still difficult to effectively disperse it in sub- / supercritical water, resulting in the existence of water-rich and oil-rich areas in the hydrothermal reforming reaction system. Sub- / supercritical water, as a hydrogen source, needs to cross the interface resistance between the water-rich and oil-rich areas to contact the inferior heavy oil and catalyst in the oil-rich area, thereby generating an in-situ hydrogen supply reforming reaction. Therefore, how to strengthen the interfacial mass transfer between oil, water, and catalyst is the key to improving the sub- / supercritical hydrothermal reforming of inferior heavy oil. Summary of the invention

[0005] In view of the deficiencies in the prior art, the object of the present invention is to provide a structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil and a method of using the same, so as to enhance the interfacial mass transfer among oil, water and catalyst and improve the subcritical / supercritical hydrothermal reforming of inferior heavy oil.

[0006] In order to achieve the above object, the present invention adopts the following technical scheme:

[0007] In the first aspect, the present invention provides a structural catalytic reactor for sub- / supercritical hydrothermal reforming of inferior heavy oil, the structural catalytic reactor comprising an inner tube and an outer tube, the inner tube being arranged inside the outer tube, the inner tube being coaxially arranged with the outer tube, a first feed port being arranged at one end of the inner tube, a second feed port and a discharge port being respectively arranged at both ends of the outer tube, an end cap being arranged between the inner tube and the discharge port, and the inner tube being a porous tube body.

[0008] Furthermore, the outer tube is a solid stainless steel tube, and the material used includes one of 316, 316L, HC276 and Inconel 625. The outer tube can withstand a high temperature of less than 550°C and an internal pressure of less than 50MPa.

[0009] Furthermore, the inner tube is formed by sintering solid catalyst powder wrapped in multiple layers of stainless steel metal mesh, and its overall pore size is between 10 nanometers and 10 microns, and it can withstand high temperatures within 550°C and internal and external pressure differences within 5 MPa.

[0010] Furthermore, the material of the stainless steel metal mesh includes 316, 316L, HC276, Inconel 625 and / or titanium alloy, and the thickness of the stainless steel metal mesh is between 1 micron and 1 millimeter.

[0011] Furthermore, the solid catalyst powder is an oxide containing at least one or more elements of Ca, Mg, Al, Mn, Fe, Cr, Ce, Ni, Co, Sn, Zn, Cu, Si, and Zr.

[0012] Furthermore, the end head is detachable, and is formed by sintering ceramic powder wrapped in multiple layers of stainless steel metal mesh, with an overall pore size between 1 nanometer and 1000 nanometers, and can withstand high temperatures within 550°C and internal and external pressure differences within 5 MPa.

[0013] Furthermore, the characteristic dimensions of the structural catalytic reactor include the inner diameter of the outer tube, the outer diameter of the inner tube, the thickness of the inner tube, the inner diameter of the inner tube, the gap between the outer tube and the inner tube, and the thickness of the end cap, wherein the inner diameter of the outer tube is 10 to 1000 mm, the ratio of the outer diameter of the inner tube to the outer diameter of the outer tube is 0.4 to 0.8, the ratio of the inner tube thickness to the outer diameter of the inner tube is 0.2 to 0.33, the ratio of the inner diameter of the inner tube to the outer diameter of the inner tube is 0.33 to 0.6, the ratio of the gap between the outer and inner tubes to the inner diameter of the outer tube is 0.1 to 0.3, and the thickness of the end cap is 10 to 100 mm.

[0014] Furthermore, the spatial placement angle of the structural catalytic reactor is any angle from vertical placement to horizontal placement to inverted vertical placement.

[0015] In a second aspect, the present invention provides a method for using the above-mentioned structured catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil, the method comprising:

[0016] A first fluid and a second fluid are introduced into the outer tube and the inner tube respectively; wherein the first fluid is sub- / supercritical water, the second fluid is a mixture of inferior heavy oil and sub- / supercritical water, the oil-water ratio of the second fluid is between 1 and 3, the flow ratio of the first fluid to the second fluid is between 0.1 and 2, the inlet temperature of the second fluid is between 275° C. and 374° C., the inlet temperature of the first fluid is between 10° C. and 100° C. higher than the inlet temperature of the second fluid, and the inlet pressure of the second fluid is between 0.1 MPa and 5 MPa higher than the inlet pressure of the first fluid;

[0017] The second fluid is squeezed through the porous wall of the inner tube, and a catalytic cracking and reforming reaction occurs. After the product enters the gap between the inner tube and the outer tube, it is washed away by the first fluid with a higher temperature and further reformed and reduced in viscosity. After unreacted macromolecules and impurities are filtered out at the end, they are discharged through the discharge port.

[0018] Furthermore, when the second fluid is squeezed through the porous wall of the inner tube, the following catalytic reaction occurs:

[0019] Cracking of low-quality heavy oil catalyzed by metal oxides: R1–R2+MO n →R1·+R2O·+MO n-1 ;

[0020] Regeneration of reduced metal oxides to decompose water: MO n-1 +H2O→MO n +H·;

[0021] In-situ hydrogen supply to produce light oil: R·+H·→RH.

[0022] Compared with the prior art, the present invention has the following beneficial effects:

[0023] (1) Low-quality heavy oil has high viscosity and its molecular size ranges from a few nanometers to several hundred nanometers. Therefore, in fluid 2, 1 to 3 times of subcritical water or supercritical water is first used to dissolve, dilute, and physically reduce the viscosity of the low-quality heavy oil to improve its fluidity. Secondly, the low-quality heavy oil is squeezed through a porous inner tube with a pore size ranging from 10 nanometers to 10 microns by the internal and external pressure difference, thereby dispersing the low-quality heavy oil at the molecular scale to facilitate catalytic cracking reaction;

[0024] (2) The inner tube is made of stainless steel mesh and metal oxide powder alternately filled and sintered, wherein the stainless steel mesh plays a role of physical support and resisting the pressure difference between the inside and outside, and the metal oxide plays a catalytic role, catalyzing the low-quality heavy oil and water flowing through, causing them to undergo an in-situ hydrogen supply reforming reaction;

[0025] (3) The first fluid is set to be subcritical / supercritical water with a temperature slightly higher than that of the second fluid, and its flow rate is 0.1 to 2 times that of the second fluid. On the one hand, it can further improve the catalytic cracking reaction, and on the other hand, it can also take away the reacted reformed products, further strengthening the reaction process;

[0026] (4) The temperature of the second fluid is set to the subcritical temperature. This is because inferior heavy oil is not easy to condense and form coke in subcritical water. This prevents inferior heavy oil from condensing and forming coke due to lack of hydrogen source before it encounters the catalyst for catalytic cracking and reforming reaction, thereby causing blockage of the inner tube wall surface gap;

[0027] (5) The end is set to a porous material with a finer pore size (1 to 1000 nanometers). On the one hand, it prevents the inferior heavy oil that has not reacted fully from being directly discharged from the reactor, thereby ensuring the reaction efficiency. On the other hand, the detachable structure makes it easier to clean the reactor.

[0028] In summary, the structural catalytic reactor and the method of use provided by the present invention can enhance the three-phase mass transfer and heat transfer of oil, water and catalyst at the molecular scale, which is creative and novel; the simple and detachable reactor structure is also easy to operate and maintain, and has strong practicality. BRIEF DESCRIPTION OF THE DRAWINGS

[0029] In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings required for use in the embodiments or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For ordinary technicians in this field, other drawings can be obtained based on the structures shown in these drawings without paying creative work.

[0030] Figure 1 A longitudinal cross-sectional view of a structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil provided in an embodiment of the present invention.

[0031] Figure 2 A cross-sectional view of a structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil provided in an embodiment of the present invention.

[0032] Figure 3 A cross-sectional view of the inner tube of a structural catalytic reactor for sub- / supercritical hydrothermal reforming of inferior heavy oil provided in an embodiment of the present invention.

[0033] Reference numerals:

[0034] 10. Inner tube; 11. Stainless steel wire mesh; 12. Solid catalyst powder; 20. Outer tube; 30. First feed port; 40. Second feed port; 50. Discharge port; 60. End; 1. First fluid; 2. Second fluid. DETAILED DESCRIPTION

[0035] The following describes the embodiments of the present invention by specific examples, and those skilled in the art can easily understand other advantages and effects of the present invention from the contents disclosed in this specification. The present invention can also be implemented or applied through other different specific embodiments, and the details in this specification can also be modified or changed in various ways based on different viewpoints and applications without departing from the spirit of the present invention. It should be noted that the following embodiments and features in the embodiments can be combined with each other without conflict.

[0036] In the description of the present invention, unless otherwise specified, "plurality" means two or more than two; the orientations or positional relationships indicated by the terms "upper", "lower", "left", "right", "inner", "outer", "front end", "rear end", "head", "tail", etc. are based on the orientations or positional relationships shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, be constructed and operate in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, the terms "first", "second", "third", etc. are only used for descriptive purposes and cannot be understood as indicating or implying their relative importance.

[0037] In the description of the present invention, it should be noted that, unless otherwise clearly specified and limited, the terms "connected" and "connection" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0038] The present invention will now be further described with reference to the accompanying drawings.

[0039] The embodiment of the present invention provides a structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil, such as Figure 1 and Figure 2 As shown, the structural catalytic reactor for sub- / supercritical hydrothermal reforming of inferior heavy oil includes an inner tube 10 and an outer tube 20, wherein the inner tube 10 is arranged inside the outer tube 20, and the inner tube 10 and the outer tube 20 are arranged coaxially, a first feed port 30 is arranged at one end of the inner tube 10, a second feed port 40 and a discharge port 50 are respectively arranged at both ends of the outer tube 20, an end cap 60 is arranged between the inner tube 10 and the discharge port 30, and the inner tube 10 is a porous tube body.

[0040] In this embodiment, by setting a nested inner and outer tube structure, different fluids can be injected into the inner tube 10 and the outer tube 20 respectively. The liquid in the inner tube 10 can pass through the inner tube 10 under the action of the pressure difference. In the process of passing through the inner tube 10, the inner tube 10 plays a catalytic role, so that it can disperse the inferior heavy oil at the molecular scale, which is convenient for catalytic cracking reaction. The reaction products entering the gap between the outer tube 20 and the inner tube 10 will be filtered through the end head 60 under the flushing action of the liquid injected into the outer tube 20 and then discharged from the reactor through the discharge port 30 set on the outer tube 20.

[0041] In some embodiments, the outer tube 20 is a solid stainless steel tube, and the materials include 316, 316L, HC276, and Inconel 625, which can withstand high temperatures within 550° C. and internal pressures within 50 MPa.

[0042] In some embodiments, Figure 3 As shown, the inner tube 10 is formed by sintering a solid catalyst powder 12 wrapped in multiple layers of a stainless steel metal mesh 11, and its overall pore size is between 10 nanometers and 10 microns, and can withstand a high temperature of less than 550°C and an internal and external pressure difference of less than 5 MPa.

[0043] In some embodiments, the stainless steel metal mesh 11 of the inner tube 10 is made of materials including 316, 316L, HC276, Inconel 625, and titanium alloy, and the pore size of the stainless steel mesh is between 1 micron and 1 millimeter.

[0044] In some embodiments, the solid catalyst powder 12 contained in the inner tube 10 is an oxide containing at least one or more elements of Ca, Mg, Al, Mn, Fe, Cr, Ce, Ni, Co, Sn, Zn, Cu, Si, and Zr.

[0045] In some embodiments, the end cap 60 is disposed at the inner end of the outer tube 20 in a detachable manner. The end cap 60 is formed by sintering ceramic powder wrapped in multiple layers of stainless steel metal mesh. Its overall pore size is between 1 nanometer and 1000 nanometers, and it can withstand high temperatures within 550°C and internal and external pressure differences within 5 MPa.

[0046] In some embodiments, the structural catalytic reactor has characteristic dimensions including: 10 mm ≤ outer tube inner diameter (D) ≤ 1000 mm, inner tube outer diameter (d out ) / D=0.4~0.8、Inner tube thickness (Δ) / d out =0.2~0.33, inner diameter of inner tube (d in ) / d out =0.33~0.6, gap between outer tube and inner tube (δ) / D=0.1~0.3, 10mm≤end thickness (Ψ)≤100mm.

[0047] In some embodiments, the spatial placement angle of the reactor is between ±0 and 90°, that is, the spatial layout of the reactor can be any angle from vertical placement (in from top and out from bottom) to horizontal placement (in from left and out from right) to inverted vertical placement (in from bottom and out from top);

[0048] The embodiment of the present invention also provides a method for using the structured catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil as described above, which comprises the following steps:

[0049] Step 1, introducing a first fluid 1 and a second fluid 2 into the outer tube and the inner tube respectively; wherein the first fluid 1 is sub- / supercritical water, the second fluid 2 is a mixture of inferior heavy oil and sub- / supercritical water, the oil-water ratio of the second fluid 2 is between 1 and 3, the flow ratio of the first fluid 1 to the second fluid 2 is between 0.1 and 2, the inlet temperature of the second fluid 2 is between 275° C. and 374° C., the inlet temperature of the first fluid 1 is between 10° C. and 100° C. higher than the inlet temperature of the second fluid 2, and the inlet pressure of the second fluid 2 is between 0.1 MPa and 5 MPa higher than the inlet pressure of the first fluid 1;

[0050] In step 2, the second fluid 2 is squeezed through the porous wall of the inner tube 10, and a catalytic cracking and reforming reaction occurs. The product enters the gap between the inner tube 10 and the outer tube 20 and is washed away by the first fluid 1 with a higher temperature and further reformed and reduced in viscosity. After the unreacted macromolecules and impurities are filtered out through the end head 60, they are discharged through the discharge port 50.

[0051] In some embodiments, the first fluid 1 and the second fluid 2 enter the reactor through independent feeding systems, and the following catalytic reaction process occurs when passing through the porous wall of the inner tube:

[0052] Cracking of low-quality heavy oil catalyzed by metal oxides: R1–R2+MO n →R1·+R2O·+MO n-1 ;

[0053] Regeneration of reduced metal oxides to decompose water: MO n-1 +H2O→MO n +H·;

[0054] In-situ hydrogen supply to produce light oil: R·+H·→RH.

[0055] Among them, R1–R2 represents heavy organic matter, MO n represents metal oxide catalyst, R1· represents organic free radical, R2O· represents oxygen-containing organic free radical, MO n-1 represents reduced metal oxide catalyst, H· represents active hydrogen, R· represents organic free radical, and RH represents light oil.

[0056] To further verify the feasibility and advancement of the present invention, three specific embodiments are provided below to fully illustrate the present invention.

[0057] Example 1: Subcritical / supercritical hydrothermal catalytic cracking of light heavy oil with molecular size between 10 and 100 nanometers

[0058] The outer tube is a solid 316 stainless steel tube (D = 500 mm); the inner tube is a porous tube (d = 10 μm) made by sintering Co-Cu bimetallic oxide powder wrapped in a titanium alloy mesh with a pore size of 10 μm. out =400mm, d in =100mm, Δ=150mm, overall pore size 200 nanometers); the gap between the outer tube and the inner tube δ=50mm; the end is a porous detachable component (Ψ=100mm, overall pore size 50 nanometers) formed by sintering zirconia powder wrapped in 10-micron pore Inconel 625 mesh; the reactor is placed horizontally as a whole (left in and right out); the first fluid 1 is supercritical water at 24.5MPa, 400℃, and 20mL / min; the second fluid 2 is an oil-water mixture at 24.8MPa, 370℃, 100mL / min, and a mass ratio of 1:1; under the action of a pressure difference of 0.3MPa between the inside and the outside, the second fluid 2 (oil-water mixture) is squeezed through the porous wall of the inner tube, and a catalytic cracking and reforming reaction occurs with the Co-Cu bimetallic oxide at a molecular dispersion level. After the product enters the gap between the inner tube and the outer tube, it is washed away by the supercritical water with a slightly higher temperature and further reformed and reduced in viscosity, and is discharged from the reactor after filtering unreacted macromolecules and impurities through the porous component at the end.

[0059] Example 2: Subcritical / supercritical hydrothermal catalytic cracking of medium-heavy oil with molecular size between 50 and 500 nanometers

[0060] The outer tube is a solid HC276 stainless steel tube (D = 300 mm); the inner tube is a porous tube (d = 20 μm) made by sintering Cr-Al bimetallic oxide powder wrapped in 316L mesh with a pore size of 20 μm. out =240mm, d in=80mm, Δ=80mm, overall pore size 800 nanometers); the gap between the outer tube and the inner tube δ=30mm; the end is a porous detachable component (Ψ=100mm, overall pore size 300 nanometers) formed by sintering alumina powder wrapped in a 50-micron pore size 316 mesh; the reactor is placed vertically as a whole (upper inlet and lower outlet); the first fluid 1 is supercritical water at 30MPa, 425°C, and 30mL / min; the second fluid 2 is an oil-water mixture at 31MPa, 350°C, 50mL / min, and a mass ratio of 2:1; under the action of a pressure difference of 1MPa between the inside and the outside, the second fluid 2 (oil-water mixture) is squeezed through the porous wall of the inner tube, and a catalytic cracking and reforming reaction occurs with the Cr-Al bimetallic oxide at a molecular dispersion level. After the product enters the gap between the inner tube and the outer tube, it is washed away by supercritical water with a higher temperature and further reformed and reduced in viscosity, and is discharged from the reactor after filtering unreacted macromolecules and impurities through the porous component at the end.

[0061] Example 3: Subcritical / supercritical hydrothermal catalytic cracking of heavy oil with molecular size between 100 and 1000 nanometers

[0062] The outer tube is a solid HC276 stainless steel tube (D = 800 mm); the inner tube is a porous tube (d = 30 μm) made by sintering Ni-Fe-Ce ternary metal oxide powder wrapped in 316 mesh. out =600mm, d in =200mm, Δ=200mm, overall pore size 1200 nanometers); the gap between the outer tube and the inner tube δ=100mm; the end is a porous detachable component (Ψ=100mm, overall pore size 500 nanometers) formed by sintering titanium oxide powder wrapped in a 20-micron pore Inconel 625 mesh; the reactor is placed vertically and inverted as a whole (bottom in and top out); the first fluid 1 is supercritical water at 40MPa, 380°C, and 100mL / min; the second fluid 2 is an oil-water mixture at 42MPa, 300°C, 200mL / min, and a mass ratio of 3:1; under the action of a pressure difference of 2MPa between the inside and the outside, the second fluid 2 (oil-water mixture) is squeezed through the porous wall of the inner tube, and a catalytic cracking and reforming reaction occurs with the Ni-Fe-Ce ternary metal oxide at a molecular dispersion level. After the product enters the gap between the inner tube and the outer tube, it is washed away by supercritical water with a higher temperature and further reformed and reduced in viscosity, and is discharged from the reactor after filtering unreacted macromolecules and impurities through the porous component at the end.

[0063] The above embodiments are only used to illustrate the technical solutions of the present invention, rather than to limit the same. Although the present invention has been described in detail with reference to the above embodiments, those skilled in the art should understand that the technical solutions described in the above embodiments may still be modified, or some or all of the technical features may be replaced by equivalents. Such modifications or replacements do not deviate the essence of the corresponding technical solutions from the scope of the technical solutions of the embodiments of the present invention, and should all be included in the scope of the claims and specification of the present invention.

Claims

1. A structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil, characterized in that: The structural catalytic reactor includes an inner tube and an outer tube, wherein the inner tube is arranged inside the outer tube, and the inner tube and the outer tube are arranged coaxially, a first feed port is arranged at one end of the inner tube, a second feed port and a discharge port are arranged at both ends of the outer tube, an end cap is arranged between the inner tube and the discharge port, and the inner tube is a porous tube body.

2. The structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil according to claim 1, characterized in that: The outer tube is a solid stainless steel tube, and the material used includes one of 316, 316L, HC276 and Inconel 625. The outer tube can withstand a high temperature of less than 550°C and an internal pressure of less than 50MPa.

3. The structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil according to claim 1, characterized in that: The inner tube is formed by sintering solid catalyst powder wrapped in multiple layers of stainless steel metal mesh, and its overall pore size is between 10 nanometers and 10 microns. It can withstand high temperatures within 550°C and internal and external pressure differences within 5 MPa.

4. The structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil according to claim 3, characterized in that: The material of the stainless steel metal mesh includes 316, 316L, HC276, Inconel625 and / or titanium alloy, and the thickness of the stainless steel metal mesh is between 1 micron and 1 millimeter.

5. The structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil according to claim 3, characterized in that: The solid catalyst powder is an oxide containing at least one or more elements of Ca, Mg, Al, Mn, Fe, Cr, Ce, Ni, Co, Sn, Zn, Cu, Si, and Zr.

6. The structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil according to claim 1, characterized in that: The end head is detachable and is formed by sintering ceramic powder wrapped in multiple layers of stainless steel metal mesh. The overall pore size is between 1 nanometer and 1000 nanometers and can withstand high temperatures within 550°C and internal and external pressure differences within 5 MPa.

7. The structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil according to claim 1, characterized in that: The characteristic dimensions of the structural catalytic reactor include the inner diameter of the outer tube, the outer diameter of the inner tube, the thickness of the inner tube, the inner diameter of the inner tube, the gap between the outer tube and the inner tube, and the thickness of the end cap, wherein the inner diameter of the outer tube is 10 to 1000 mm, the ratio of the outer diameter of the inner tube to the outer diameter of the outer tube is 0.4 to 0.8, the ratio of the thickness of the inner tube to the outer diameter of the inner tube is 0.2 to 0.33, the ratio of the inner diameter of the inner tube to the outer diameter of the inner tube is 0.33 to 0.6, the ratio of the gap between the outer tube and the inner tube to the inner diameter of the outer tube is 0.1 to 0.3, and the thickness of the end cap is 10 to 100 mm.

8. The structural catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil according to claim 1, characterized in that: The spatial placement angle of the structural catalytic reactor is any angle from vertical placement to horizontal placement to inverted vertical placement.

9. A method for using a structured catalytic reactor for subcritical / supercritical hydrothermal reforming of inferior heavy oil according to any one of claims 1 to 8, characterized in that: The method of use includes: A first fluid and a second fluid are introduced into the outer tube and the inner tube respectively; wherein the first fluid is sub- / supercritical water, the second fluid is a mixture of inferior heavy oil and sub- / supercritical water, the oil-water ratio of the second fluid is between 1 and 3, the flow ratio of the first fluid to the second fluid is between 0.1 and 2, the inlet temperature of the second fluid is between 275°C and 374°C, the inlet temperature of the first fluid is between 10°C and 100°C higher than the inlet temperature of the second fluid, and the inlet pressure of the second fluid is between 0.1MPa and 5MPa higher than the inlet pressure of the first fluid; The second fluid is squeezed through the porous wall of the inner tube, and a catalytic cracking and reforming reaction occurs. After the product enters the gap between the inner tube and the outer tube, it is washed away by the first fluid with a higher temperature and further reformed and reduced in viscosity. After unreacted macromolecules and impurities are filtered out at the end, they are discharged through the discharge port.

10. The method of use according to claim 9, characterized in that: When the second fluid is squeezed through the porous wall of the inner tube, the following catalytic reaction occurs: Cracking of low-quality heavy oil catalyzed by metal oxides: R1–R2+MO n →R1·+R2O·+MO n-1 ; Regeneration of reduced metal oxides to decompose water: MO n-1 +H2O→MO n +H·; In-situ hydrogen supply to produce light oil: R·+H·→RH.

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