CN211419566U - Liquid fuel catalytic reforming device - Google Patents

Abstract

The utility model provides a liquid fuel catalytic reforming device, which relates to the technical field of hydrogen production devices and comprises a shell and a high-temperature heat pipe; a reaction cavity is arranged in the shell, the reaction cavity comprises a catalytic reforming region, and the catalytic reforming region is filled with a catalyst; the parts of the shell, which are positioned at the two ends of the catalytic reforming region, are respectively provided with a reaction cavity inlet and a reaction cavity outlet; the high temperature heat pipe is configured to be capable of fitting inside the catalytic reforming region to equalize the temperature of the catalyst filled inside the catalytic reforming region in a direction along the flow of fluid from the reaction chamber inlet to the reaction chamber outlet. The utility model discloses the technical problem that the liquid fuel reforming in-process catalyst bed layer that exists among the prior art "overheated" or "subcooling", inside temperature gradient is big has been alleviated at least.

Description

Liquid fuel catalytic reforming device

Technical Field

The utility model relates to a hydrogen plant technical field especially relates to a liquid fuel catalytic reforming device.

Background

The fuel cell is a novel energy supply technology, has the advantages of high efficiency which can reach 60 percent at most, low noise, almost no pollution emission and the like, is suitable for a plurality of fields of automobile power supplies, portable power supplies, distributed energy systems, household combined heat and power supplies and the like, and is a vital technology in a 'hydrogen economy' system. However, at present, there is still a bottleneck in key technologies such as hydrogen production, storage and transportation, which limits the large-scale popularization of fuel cell technology, and the development of mobile and miniaturized hydrogen production devices and technologies based on reforming and converting liquid fuels such as gasoline and diesel oil is an important way to solve the above problems.

The liquid fuel represented by gasoline and diesel oil has the advantages of high energy density, complete set of technologies and facilities for production, storage, transportation, supply and the like, and is particularly suitable for mobile and miniaturized field hydrogen production equipment. Reforming processes can be generally divided into three categories, depending on the feedstock required and the reactions taking place: steam reforming, partial oxidation reforming, and autothermal reforming. Steam reforming adopts steam as an oxidant, so that the advantages of carbon deposition inhibition and high hydrogen content are achieved, but the whole reaction process needs to absorb a large amount of heat, needs an additional heating device, and is complex in system and large in volume; partial oxidation reforming adopts oxygen or air with a less than stoichiometric ratio as an oxidant, the heat is released in the conversion process, the self-maintenance under a high-temperature condition can be realized, but the risk of carbon deposition is high in the process, and the hydrogen content is low; the autothermal reforming adopts partial steam and air as oxidants, has the advantages of the two reforming methods in the aspects of system efficiency, carbon deposition, reaction temperature and the like, but has relatively complex regulation and control of operating condition parameters and certain risk of carbon deposition.

In the three liquid fuel reforming modes, the problems of overheating inside a catalyst bed layer, namely overhigh area temperature or overcooling inside the catalyst bed layer, namely overlow area temperature and large temperature gradient inside the catalyst bed layer which can reach 200 ℃/cm at most generally exist, so that the problems of catalyst sintering, surface carbon deposition, carrier cracking and the like are often caused, the catalytic performance and the long-term service life of the catalyst are influenced, and the overall performance of a liquid fuel reforming device is severely limited.

SUMMERY OF THE UTILITY MODEL

An object of the utility model is to provide a liquid fuel catalytic reforming device, this liquid fuel catalytic reforming device can alleviate the liquid fuel reforming in-process catalyst bed layer "overheated" or "subcooling" that exists among the prior art at least, the big technical problem of inside temperature gradient.

For realizing the purpose of the utility model, the embodiment of the utility model adopts the following technical scheme:

the embodiment of the utility model provides a liquid fuel catalytic reforming device, which comprises a shell and a high-temperature heat pipe; a reaction cavity is arranged in the shell, the reaction cavity comprises a catalytic reforming region, and the catalytic reforming region is filled with a catalyst; a reaction cavity inlet and a reaction cavity outlet are respectively formed in the positions, located at the two ends of the catalytic reforming region, of the shell; the high temperature heat pipe is configured to be capable of fitting inside the catalytic reforming region to equalize a temperature of the catalyst filled inside the catalytic reforming region in a direction along a fluid flowing from the reaction chamber inlet to the reaction chamber outlet.

In an alternative embodiment, the concentration of the catalyst is gradually increased in the direction of fluid flow from the reaction chamber inlet to the reaction chamber outlet with the interior of the catalytic reforming zone filled with catalyst.

In an alternative embodiment, the liquid fuel catalytic reformer further comprises a feed assembly; the feeding assembly comprises a feeding pipeline, and an outlet of the feeding pipeline is communicated with an inlet of the reaction cavity.

In an alternative embodiment, the feed lines include a fuel line and an oxidant line; the outlet of the fuel pipeline and the outlet of the oxidant pipeline are both communicated with the inlet of the reaction cavity;

the feed assembly further comprises a first nozzle; the first nozzle is a two-fluid nozzle, the outlet of the fuel pipeline and the outlet of the oxidant pipeline are connected to the inlet end of the two-fluid nozzle, and the outlet end of the two-fluid nozzle extends into the inlet of the reaction cavity.

In an alternative embodiment, the feed assembly further comprises a second nozzle having a plurality of nozzles; the oxidant pipeline is provided with a plurality of pipeline outlets, one pipeline outlet is connected to the inlet end of the double-fluid nozzle, the other pipeline outlets are connected to the inlet ends of the second nozzles in a one-to-one correspondence manner, and the outlet ends of the second nozzles extend into the inlet of the reaction cavity; the plurality of second nozzles are arranged at intervals in pairs around the first nozzle, and the plurality of second nozzles are arranged so that the discharged fluid rotationally flows in a diameter direction of an imaginary circle having a point on a center line of the fluid discharged from the first nozzle as a center point to form a tangential rotational flow.

In an alternative embodiment, the liquid fuel catalytic reformer further comprises a heating assembly;

the heating assembly is arranged in the reaction cavity at a position close to the inlet of the reaction cavity, and is positioned at the upstream of the catalytic reforming region along the direction of the fluid flowing from the inlet of the reaction cavity to the outlet of the reaction cavity, and is used for igniting or evaporating the fluid injected into the inlet of the reaction cavity before the fluid injected into the inlet of the reaction cavity flows to the catalytic reforming region.

In an alternative embodiment, the liquid fuel catalytic reforming device further comprises a heat conducting member mounted inside the reaction chamber at a position close to the reaction chamber inlet, and located upstream of the catalytic reforming region in a direction of fluid flow from the reaction chamber inlet to the reaction chamber outlet, and configured to: in a case where the inside of the catalytic reforming region is filled with a catalyst, one end of the heat conductive member near the catalyst is in contact with the catalyst.

In an alternative embodiment, the heat conducting member is porous.

In an alternative embodiment, an insulating layer is provided on the outside of the housing.

In an alternative embodiment, the shell comprises an inner shell and an outer shell, a first reaction chamber is arranged inside the inner shell, and a second reaction chamber is arranged inside the outer shell; the catalytic reforming region is arranged in the first reaction cavity, a first reaction cavity inlet and a first reaction cavity outlet are respectively formed in the inner shell body at the positions at the two ends of the catalytic reforming region, and a second reaction cavity inlet and a second reaction cavity outlet are formed in the outer shell body; the inner shell is arranged in the second reaction cavity, and the inlet of the first reaction cavity is communicated with the inlet of the second reaction cavity in a sealing way;

the outlet of the fuel pipeline and the outlet of the oxidant pipeline are both communicated with the inlet of the first reaction cavity; the oxidant pipeline passes through the second reaction cavity.

In an optional embodiment, the second reaction chamber outlet is opened at one end of the outer shell far away from the first reaction chamber outlet, and the second reaction chamber outlet is close to the first reaction chamber inlet; the oxidant pipeline passes through the inner space of the second reaction chamber at a position close to the outlet of the second reaction chamber.

The embodiment of the utility model provides a liquid fuel catalytic reforming device can realize following beneficial effect:

the embodiment of the utility model provides a liquid fuel catalytic reforming device, which comprises a shell and a high-temperature heat pipe; a reaction cavity is arranged in the shell, the reaction cavity comprises a catalytic reforming region, and the catalytic reforming region is filled with a catalyst; the parts of the shell, which are positioned at the two ends of the catalytic reforming region, are respectively provided with a reaction cavity inlet and a reaction cavity outlet; the high temperature heat pipe is configured to be capable of fitting inside the catalytic reforming region to equalize the temperature of the catalyst filled inside the catalytic reforming region in a direction along the flow of fluid from the reaction chamber inlet to the reaction chamber outlet.

In the embodiment of the utility model, the liquid fuel catalytic reforming device comprises a shell, a reaction cavity is arranged in the shell, the reaction cavity comprises a catalytic reforming area, and the catalytic reforming area is used for filling a catalyst; the parts of the shell, which are positioned at the two ends of the catalytic reforming region, are respectively provided with a reaction cavity inlet and a reaction cavity outlet. When in use, a catalyst is filled in the catalytic reforming region of the reaction cavity, the catalytic reforming reaction is started, the mixed gas of the liquid fuel and the oxidant after being heated is introduced into the reaction cavity and fully reacts with the catalyst to be converted into the reformed gas containing a large amount of hydrogen and carbon monoxide, and then the reformed gas is discharged from the outlet of the reaction cavity, in the whole process, along with the process that the mixed gas flows through the catalyst from the inlet of the reaction cavity to the outlet of the reaction cavity, the temperature of part of the region with overhigh temperature inside the catalyst is too high and the temperature of part of the region with overlow temperature is too low, at the moment, because the liquid fuel catalytic reforming device of the embodiment also comprises the high-temperature heat pipe, the high-temperature heat pipe is configured to be assembled inside the catalytic reforming region to balance the temperature of the catalyst filled inside the catalytic reforming region in the direction that the, the catalyst can be evaporated and absorb heat at a catalyst with higher temperature by utilizing a working medium in the high-temperature heat pipe, the working medium naturally circulates in the pipe, the heat is carried to a catalyst with lower temperature for condensation and heat release, the heat between the high temperature and the low temperature of the catalyst is quickly transferred, the huge temperature gradient of the catalyst in the direction extending from the inlet of the reaction cavity to the outlet of the reaction cavity is quickly balanced, the temperature of the catalyst is uniformly distributed in the direction extending from the inlet of the reaction cavity to the outlet of the reaction cavity, the damage of local overheating or local supercooling to the catalyst is avoided, the service life of the catalyst is further prolonged, meanwhile, the time for waiting for the temperature of each part of the catalyst to rise to the temperature suitable for catalytic reforming reaction is shortened by the arrangement of the high.

To sum up, the embodiment of the utility model provides an at least have the injury that avoids local "overheated" or local "subcooling" to cause the catalyst in order to prolong the life of catalyst to and shorten the time of waiting for catalyst temperature everywhere all to rise to the suitable temperature of catalytic reforming reaction, improve the beneficial effect of catalytic reforming efficiency.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the embodiments or the technical solutions in the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to these drawings without creative efforts.

Fig. 1 is a schematic diagram of an overall structure of a liquid fuel catalytic reforming apparatus according to an embodiment of the present invention;

fig. 2 is a schematic fluid flow direction diagram of a liquid fuel catalytic reforming device according to an embodiment of the present invention, in which fluid flows inside a reaction chamber;

FIG. 3 is a schematic diagram illustrating the flow direction of fluid injected into the inlet of the reaction chamber in a liquid fuel catalytic reforming apparatus according to an embodiment of the present invention;

fig. 4 is a schematic diagram of the overall structure of a liquid fuel catalytic reforming device according to an embodiment of the present invention;

fig. 5 is a schematic fluid flow direction diagram of a fluid flowing inside a first reaction chamber in a liquid fuel catalytic reforming device provided by an embodiment of the present invention;

fig. 6 is a schematic flow direction diagram of a fluid injected into an inlet of a first reaction chamber in a liquid fuel catalytic reforming apparatus according to an embodiment of the present invention.

Icon: 1-a shell; 11-reaction chamber inlet; 12-the outlet of the reaction chamber; 2-high temperature heat pipe; 3-a catalyst; 41-fuel line; 42-an oxidant line; 43-a first nozzle; 44-a second nozzle; 5-a heating assembly; 6-a thermally conductive member; 7-insulating layer; 101-an inner housing; 1011-first reaction chamber inlet; 1012-first reaction chamber outlet; 102-an outer shell; 1021-second reaction chamber inlet; 1022-second reaction chamber outlet.

Detailed Description

In order to make the objects, technical solutions and advantages of the embodiments of the present invention clearer, the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is obvious that the described embodiments are some, but not all, embodiments of the present invention. The components of embodiments of the present invention, as generally described and illustrated in the figures herein, may be arranged and designed in a wide variety of different configurations.

Thus, the following detailed description of the embodiments of the present invention, presented in the accompanying drawings, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention. Based on the embodiments in the present invention, all other embodiments obtained by a person skilled in the art without creative efforts belong to the protection scope of the present invention.

It should be noted that: like reference numbers and letters refer to like items in the following figures, and thus, once an item is defined in one figure, it need not be further defined and explained in subsequent figures.

In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "vertical", "horizontal", "inner", "outer", and the like indicate the position or positional relationship based on the position or positional relationship shown in the drawings, or the position or positional relationship which is usually placed when the product of the present invention is used, and are only for convenience of description and simplification of the description, but do not indicate or imply that the device or element to which the term refers must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and the like are used merely to distinguish one description from another, and are not to be construed as indicating or implying relative importance.

Furthermore, the terms "horizontal", "vertical" and the like do not imply that the components are required to be absolutely horizontal or pendant, but rather may be slightly inclined. For example, "horizontal" merely means that the direction is more horizontal than "vertical" and does not mean that the structure must be perfectly horizontal, but may be slightly inclined.

In the description of the present invention, it should also be noted that, unless explicitly stated or limited otherwise, the terms "disposed," "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood in specific cases to those skilled in the art.

Some embodiments of the present invention will be described in detail below with reference to the accompanying drawings. The embodiments described below and the features of the embodiments can be combined with each other without conflict.

Example one

Referring to fig. 1, 2 and 3, the present embodiment provides a liquid fuel catalytic reforming apparatus including a case 1 and high temperature heat pipes 2; a reaction chamber is arranged in the shell 1, the reaction chamber comprises a catalytic reforming region, and the catalytic reforming region is filled with a catalyst 3; the parts of the shell 1, which are positioned at the two ends of the catalytic reforming region, are respectively provided with a reaction cavity inlet 11 and a reaction cavity outlet 12; the high temperature heat pipe 2 is configured to be able to fit inside the catalytic reforming region to equalize the temperature of the catalyst 3 filled inside the catalytic reforming region in the direction of fluid flow from the reaction chamber inlet 11 to the reaction chamber outlet 12.

The heat pipe is a heat transfer device with excellent heat conductivity, which transfers heat by repeatedly carrying out physical phase change or chemical reaction on a specific working medium enclosed in the pipe, when one end of the heat pipe is heated, the working medium in the pipe absorbs the heat and is vaporized into steam, and the steam flows to the other end of the heat pipe under a small pressure difference and emits the heat to the outside to be condensed into liquid. The condensate returns to the heated end along the inner wall of the heat pipe and is heated and vaporized again, and the steps are repeated in a circulating way. The heat pipes are classified into low-temperature heat pipes at the temperature of-270-0 ℃, normal-temperature heat pipes at the temperature of 0-200 ℃, medium-temperature heat pipes at the temperature of 200-600 ℃ and high-temperature heat pipes at the temperature of more than 600 ℃ according to the temperature, the high-temperature heat pipes take liquid metal (sodium, potassium, steel and the like) as working media, have good thermal stability and very low saturated steam pressure, take stainless steel or other heat-resistant steel as pipe shells and can work in high-temperature smoke gas at the temperature of more than 1100 ℃. The type of the catalyst 3 can be selected according to the catalytic reforming mode of the liquid fuel, and can be a supported type or a non-supported type, wherein the supported type catalyst includes, but is not limited to, a catalyst of active metal such as Ni, Pd, Ru, Rh or Pt, etc., which is supported by a porous carrier such as alumina, ceria, zirconia or molecular sieve, etc.; the unsupported catalyst includes, but is not limited to, perovskite-type catalyst powder, an active metal skeletal catalyst such as Ni, Pd, Ru, Rh, or Pt, an active metal powder catalyst such as Ni, Pd, Ru, Rh, or Pt, and the like.

In the present embodiment, the liquid fuel catalytic reforming apparatus includes a housing 1, a reaction chamber is provided inside the housing 1, the inside of the reaction chamber includes a catalytic reforming region for filling with a catalyst 3; the shell 1 is provided with a reaction chamber inlet 11 and a reaction chamber outlet 12 at the two ends of the catalytic reforming region. When the device is used, the catalyst 3 is filled in the catalytic reforming region of the reaction cavity, the catalytic reforming reaction is started, the mixed gas of the liquid fuel and the oxidant after being heated is introduced into the reaction cavity and fully reacts with the catalyst 3 to be converted into the reformed gas containing a large amount of hydrogen and carbon monoxide, then the reformed gas is discharged from the outlet 12 of the reaction cavity, and in the whole process, along with the process that the mixed gas flows through the catalyst 3 from the inlet 11 of the reaction cavity to the outlet 12 of the reaction cavity, the temperature of the area with the overhigh temperature in the internal part of the catalyst 3 is overlow, at the moment, because the liquid fuel catalytic reforming device of the embodiment also comprises the high-temperature heat pipe 2, the high-temperature heat pipe 2 is configured to be assembled in the catalytic reforming region so as to balance the temperature of the catalyst 3 filled in the catalytic reforming region in the direction that the fluid flows from the inlet 11 of the, therefore, the working medium in the high-temperature heat pipe 2 can be used for absorbing heat by evaporation at the catalyst 3 with higher temperature, the working medium naturally circulates in the pipe, the heat is carried to the catalyst 3 with lower temperature for condensation and heat release, the heat between the high temperature and the low temperature of the catalyst 3 is quickly transferred, the huge temperature gradient of the catalyst 3 in the direction extending from the reaction cavity inlet 11 to the reaction cavity outlet 12 is quickly balanced, the temperature of the catalyst 3 in the direction extending from the reaction cavity inlet 11 to the reaction cavity outlet 12 is uniformly distributed, the damage to the catalyst 3 caused by local overheating or local supercooling is avoided, the service life of the catalyst 3 is further prolonged, meanwhile, the time for waiting for the temperature of each part of the catalyst 3 to rise to the temperature suitable for catalytic reforming reaction is shortened by the arrangement of the high-temperature heat pipe 2, and the catalytic reforming.

In summary, the present embodiment at least has the beneficial effects of avoiding damage to the catalyst 3 caused by local "overheating" or local "undercooling" to prolong the service life of the catalyst 3, and shortening the time for waiting for the temperature of each part of the catalyst 3 to rise to the temperature suitable for the catalytic reforming reaction, thereby improving the catalytic reforming efficiency.

It should be noted that, in this embodiment, there are various ways for the high temperature heat pipe 2 to be installed in the catalytic reforming region in the reaction chamber of the casing 1, for example, but not limited to, the high temperature heat pipe 2 is inserted into the catalyst 3 filled in the catalytic reforming region, or, a mounting bracket is provided on the inner wall of the casing 1, and the high temperature heat pipe 2 is mounted on the mounting bracket; the specific arrangement form of the high temperature heat pipe 2 is various, for example, but not limited to, a straight pipe type high temperature heat pipe 2 is adopted, and the length direction of the high temperature heat pipe 2 extends from the reaction chamber inlet 11 to the reaction chamber outlet 12, of course, other forms of high temperature heat pipe 2 may be used, for example, but not limited to, a plate type or a ring pipe type high temperature heat pipe 2, and the like, wherein the direction extending from the reaction chamber inlet 11 to the reaction chamber outlet 12 may be a linear direction or a curved direction, and the like, as long as the high temperature heat pipe 2 is arranged in the direction flowing along the fluid from the reaction chamber inlet 11 to the reaction chamber outlet 12, so that the high temperature heat pipe 2 is configured to balance the temperature of the catalyst 3 filled in the catalytic reforming region in the direction extending from the reaction chamber inlet 11 to the reaction chamber outlet 12, and preferably, the high temperature heat pipe 2 penetrates through the catalytic reforming region in the direction extending from the first reaction chamber inlet 1011 to the first reaction chamber outlet 1012 (ii) a In addition, the number of the high-temperature heat pipes 2 may be 1 or more, and is not limited in this embodiment. In addition, in order to add the catalyst 3 into the catalytic reforming region, a catalyst addition port may be opened in a casing wall of the casing 1, a seal cover may be attached to the catalyst addition port, and the catalyst 3 may be added into the catalytic reforming region by opening and closing the seal cover, and similarly, in order to replace the catalyst 3, a catalyst discharge port may be opened in a casing wall of the casing 1, a seal cover may be attached to the catalyst discharge port, and the catalyst 3 may be discharged by opening and closing the seal cover.

In addition, in the reforming catalytic reaction process, the first stage of the reforming process is a violent exothermic process mainly involving oxidation, and the catalyst 3 near the inlet 11 of the reaction chamber has the highest temperature, and thus the problems such as "overheating" and catalyst sintering are most likely to occur.

In contrast, referring to fig. 1 and 2, in at least one alternative embodiment of this embodiment, in the case where the catalyst 3 is filled in the inside of the catalytic reforming region, the concentration of the catalyst 3 gradually increases in the direction in which the fluid flows from the reaction chamber inlet 11 to the reaction chamber outlet 12, that is, the concentration of the upstream catalyst 3 is appropriately decreased in the direction in which the fluid flows in the reaction chamber. Through the structure, the extension and the heat sharing of a violent heat release area to the downstream catalyst 3 are facilitated, the temperature peak value is reduced, the temperature gradient of the catalyst 3 is reduced, the tolerance of the catalyst 3 is improved, meanwhile, the catalyst 3 with gradually-increased concentration can ensure higher outlet conversion rate, the optional embodiment enables the catalyst 3 to carry out graded catalyst step conversion on the mixed gas of the liquid fuel and the oxidant after being heated in the reaction cavity, so that the dosage of the catalyst 3 is reasonably distributed, and the beneficial effects of improving the tolerance of the catalyst 3, improving the outlet conversion rate of reformed gas generation and reducing the cost of the catalyst 3 are at least achieved.

With continued reference to fig. 1 and 2, in at least one alternative embodiment of this embodiment, the liquid fuel catalytic reformer further includes a feed assembly; the feeding assembly comprises a feeding pipeline, and an outlet of the feeding pipeline is communicated with the inlet 11 of the reaction cavity. The supply line may have only one line, the reaction material may be a mixed gas of a liquid fuel and an oxidant after being heated, a mixed fluid of an unheated liquid fuel and an unheated oxidant, or a mixed fluid of an unheated liquid fuel and a preheated oxidant, or the like, and the supply line may include a plurality of branch lines individually communicating with the reaction chamber inlet 11 to supply the liquid fuel and the oxidant into the reaction chamber inlet 11, respectively.

Alternatively, referring to fig. 1, 2 and 3, the feed lines include a fuel line 41 and an oxidant line 42; the outlet of the fuel pipeline 41 and the outlet of the oxidant pipeline 42 are both communicated with the inlet 11 of the reaction cavity; the feed assembly further comprises a first nozzle 43; the first nozzle 43 is a two-fluid nozzle, the outlet of the fuel line 41 and the outlet of the oxidant line 42 being connected to the inlet end of the two-fluid nozzle, the outlet end of the two-fluid nozzle extending into the interior of the reaction chamber inlet 11. The two-fluid nozzle includes, but is not limited to, a pressure type two-fluid nozzle, a siphon type two-fluid nozzle, and the like. In this alternative embodiment, by providing the first nozzle 43 and making the first nozzle 43 a two-fluid nozzle, the step of mixing the liquid fuel and the oxidizing agent in advance can be omitted, the liquid fuel and the oxidizing agent can be directly mixed at the two-fluid nozzle and injected into the inlet of the reaction chamber after being crushed and atomized in the two-fluid nozzle, the step of supplying can be simplified, wherein the liquid fuel, which may be heated or not, is supplied in the fuel line 41, and the oxidizing agent, which may be heated or not, is supplied in the oxidizing agent line 42, wherein the oxidizing agent can be selected according to the type of catalytic reforming reaction whether to be heated before being introduced.

In order to mix the liquid fuel and the oxidant injected into the inlet 11 of the reaction chamber sufficiently and uniformly, avoid local "oxygen deficiency" and "peroxide" phenomena caused by uneven distribution of the materials, and serious carbon deposition tendency and local hot spot problem caused thereby, and improve the fuel utilization rate, on the basis of the above-mentioned alternative embodiment of the present embodiment, preferably, referring to fig. 3, in combination with fig. 1 and 2, the above-mentioned feeding assembly further includes a second nozzle 44, and the second nozzle 44 has a plurality of second nozzles; the oxidant pipeline 42 has a plurality of pipeline outlets, wherein one pipeline outlet is connected to the inlet end of the two-fluid nozzle, the other pipeline outlets are connected to the inlet ends of the plurality of second nozzles 44 in a one-to-one correspondence, and the outlet ends of the plurality of second nozzles 44 all extend into the reaction chamber inlet 11; the plurality of second nozzles 44 are arranged at intervals of two by two around the first nozzle 43, and the plurality of second nozzles 44 are arranged such that the discharged fluid swirls in a radial direction of an imaginary circle having a point on a center line of the fluid discharged from the first nozzle 43 as a center point to form a tangential swirl flow. With such a structure, a reaction raw material premixing area can be formed at a position of the reaction chamber at the reaction chamber inlet 11, preferably, referring to fig. 1, 2 and 3, the opening of the reaction chamber inlet 11 is directed upward, the first nozzle 43 is vertically arranged in the center area of the reaction chamber inlet 11 in a suspended manner, and the plurality of second nozzles 44 are arranged around the first nozzle 43 at equal intervals two by two in a horizontal plane; further preferably, the plurality of second nozzles 44 are located obliquely below the first nozzle 43, and a part of the oxidant and the liquid fuel are crushed and atomized by the first nozzle 43 and then dispersed and sprayed into the inlet 11 of the reaction chamber; the rest of the oxidant is crushed and atomized by the second nozzle 44 and then sprayed into the inlet 11 of the reaction chamber to form a tangential rotational flow, and the tangential rotational flow is fully contacted and mixed with the mixed fluid of the fuel and the oxidant which are sprayed by the first nozzle 43 and are dispersed in a conical shape, so that the oxidant and the fuel can be fully mixed, and the efficient mixing effect can be achieved.

With additional reference to fig. 1 and 2, in the present embodiment, on the basis that the liquid fuel catalytic reforming device further includes a supply assembly, optionally, the liquid fuel catalytic reforming device further includes a heating assembly 5; the heating assembly 5 is mounted inside the reaction chamber adjacent to the reaction chamber inlet 11 and the heating assembly 5 is located upstream of the catalytic reforming zone in the direction of fluid flow from the reaction chamber inlet 11 to the reaction chamber outlet 12 for igniting or evaporating the fluid injected into the reaction chamber inlet 11 before the fluid injected into the reaction chamber inlet 11 flows to the catalytic reforming zone. The specific structure of the heating assembly 5 is various, including but not limited to a heating rod, a glow plug, a heating net, etc., the heating assembly 5 is mounted on the wall of the housing 1, and the heating assembly 5 is provided with a heating wire which passes through the wall of the housing and is connected with an external power supply.

When the device is used for carrying out catalytic reforming reaction of liquid fuel, the device mainly comprises three stages of starting, stable operation and stopping, and the device is as follows:

starting: oxidant and liquid fuel are sprayed into the inlet 11 of the reaction cavity according to the working condition proportion of equivalent or oxygen-enriched combustion to form mixed fluid; the mixed fluid is ignited by the glowing heating assembly after entering the reaction cavity to generate combustion reaction; then the burned flue gas enters a catalytic reforming region to sweep the catalyst 3, so that the temperature of the catalyst 3 is gradually increased, when the temperature is gradually increased to the point that the catalyst 3 can react, the catalyst 3 accelerates the further oxidation and heat release of the flue gas components which are not completely oxidized, and in the process that the burned flue gas enters the catalytic reforming region to sweep the catalyst 3, the temperature of each part of the catalyst 3 is rapidly balanced under the action of the high-temperature heat pipe 2 until the temperature reaches the proper temperature of the reforming reaction; then, the working condition is switched to the working condition proportion of reforming reaction, the proportion of the oxidant is gradually increased according to a proper speed, the operation parameters of the heating assembly 5 are changed, the surface temperature of the heating assembly 5 is reduced, the heating assembly 5 is used for evaporating the mixed fluid, and finally the mixed fluid enters a stable operation state;

and (3) stable operation: the oxidant and the liquid fuel are supplied to the inlet of the reaction cavity according to the designed stable conversion ratio, the heating assembly keeps the evaporation purpose, and the stable reforming conversion process is carried out;

stopping the machine: gradually reducing the amount of the oxidant and the liquid fuel at the inlet of the reaction chamber to reduce the heat release; when the temperature is lower than 600 ℃, switching the working condition to the equivalent combustion working condition to avoid carbon deposition and further slowly reducing the inlet flow of the reaction cavity; when the temperature is gradually reduced to be below 350 ℃, the liquid fuel is stopped to be supplied, and the oxidant is continuously and slowly reduced; when the temperature gradually drops below 100 ℃, the supply of the oxidant is stopped until the liquid fuel catalytic reformer is completely cooled.

By this heating assembly 5, the above-mentioned starting phase of ignition and the evaporation during steady operation can be achieved, and compared with the ignition or evaporation of the liquid fuel and the oxidizer before the mixed fluid enters the reaction chamber, the reaction is more consistent when the alternative embodiment is used, and the overall volume of the liquid fuel catalytic reforming device is smaller, which is beneficial to saving space.

In addition, with continuing reference to fig. 1 and 2, in the present embodiment, on the basis that the liquid fuel catalytic reforming apparatus further includes a supply assembly, optionally, the liquid fuel catalytic reforming apparatus further includes a heat conduction member 6, the heat conduction member 6 is installed inside the reaction chamber at a position close to the reaction chamber inlet 11, and in a direction in which the fluid flows from the reaction chamber inlet 11 to the reaction chamber outlet 12, the heat conduction member 6 is located upstream of the catalytic reforming region, and the heat conduction member 6 is configured to: in the case where the catalyst 3 is filled in the inside of the catalytic reforming region, the end of the heat-conducting member 6 close to the catalyst 3 is in contact with the catalyst 3, wherein the way in which the end of the heat-conducting member 6 close to the catalyst 3 is in contact with the catalyst 3 includes, but is not limited to, the way in which the end of the heat-conducting member 6 close to the catalyst 3 is inserted in the inside of the catalyst 3. In this alternative embodiment, the heat emitted from the front stage of the catalytic reforming region downstream of the heat transfer member 6 may be transferred upstream by the heat transfer member 6 to preheat the mixed fluid of the fuel and the oxidant, thereby further improving the catalytic reforming efficiency.

In the above alternative embodiment, it is preferable that the heat-conducting member 6 is porous, and may be made of a wire mesh, a metal foam, a porous ceramic, or the like, so that the mixed fluid diffuses in the catalytic reforming region downstream along the porous medium and at the same time diffuses in a transverse direction, which is a direction perpendicular to a direction in which the reaction chamber inlet 11 extends toward the reaction chamber outlet 12, inside the porous heat-conducting member 6, so as to improve the uniformity of the mixed fluid in the transverse direction, thereby increasing the contact area between the mixed fluid and the catalyst 3, and further improving the catalytic reforming efficiency.

In addition, referring to fig. 1 and 2, on the basis of any optional embodiment of this embodiment, an insulating layer 7 is further disposed outside the casing 1, and the insulating layer 7 may be an insulating layer structure made of an insulating cotton layer, a foam sleeve, or other insulating materials, and plays a role in insulating the casing 1 and avoiding heat loss.

Example two

Referring to fig. 4 and 5, the present embodiment provides another liquid fuel catalytic reforming device including a case and high-temperature heat pipes 2; the shell comprises an inner shell 101 and an outer shell 102, a first reaction cavity is arranged inside the inner shell 101, a second reaction cavity is arranged inside the outer shell 102, the first reaction cavity comprises a catalytic reforming region inside, and the catalytic reforming region is used for filling a catalyst 3; a first reaction chamber inlet 1011 and a first reaction chamber outlet 1012 are respectively formed at the two ends of the catalytic reforming region of the inner casing 101, and the high-temperature heat pipe 2 is configured to be capable of being assembled inside the catalytic reforming region so as to balance the temperature of the catalyst 3 filled inside the catalytic reforming region in the direction extending from the first reaction chamber inlet 1011 to the first reaction chamber outlet 1012; a second reaction cavity inlet 1021 and a second reaction cavity outlet 1022 are arranged on the outer shell 102; the inner housing 101 is disposed inside the second reaction chamber, and the inlet 1011 of the first reaction chamber is in sealed communication with the inlet 1021 of the second reaction chamber.

The type of the catalyst 3 can be selected according to the catalytic reforming mode of the liquid fuel, and can be a supported type or a non-supported type, wherein the supported type catalyst includes, but is not limited to, a catalyst of active metal such as Ni, Pd, Ru, Rh or Pt, etc., which is supported by a porous carrier such as alumina, ceria, zirconia or molecular sieve, etc.; the unsupported catalyst includes, but is not limited to, perovskite-type catalyst powder, an active metal skeletal catalyst such as Ni, Pd, Ru, Rh, or Pt, an active metal powder catalyst such as Ni, Pd, Ru, Rh, or Pt, and the like. In addition, there are various ways for the high temperature heat pipe 2 to be assembled in the catalytic reforming region, for example, but not limited to, the high temperature heat pipe 2 is inserted into the catalyst 3 filled in the catalytic reforming region, or a mounting bracket is arranged on the inner wall of the casing 1, and the high temperature heat pipe 2 is mounted on the mounting bracket; the specific arrangement form of the high temperature heat pipe 2 is various, for example, but not limited to, a straight pipe type high temperature heat pipe 2 is adopted, and the length direction of the high temperature heat pipe 2 extends from the first reaction chamber inlet 1011 to the first reaction chamber outlet 1012, of course, other forms of high temperature heat pipes 2 may also be used, for example, but not limited to, a plate type or a ring pipe type high temperature heat pipe 2, etc., wherein the direction extending from the first reaction chamber inlet 1011 to the first reaction chamber outlet 1012 may extend along a straight line direction or a curved line direction, etc., as long as the high temperature heat pipe 2 is arranged in the direction flowing along the fluid from the first reaction chamber inlet 1011 to the first reaction chamber outlet 1012, so that the high temperature heat pipe 2 is configured to balance the temperature of the catalyst 3 filled in the inside of the catalytic reforming region in the direction extending from the first reaction chamber inlet 1011 to the first reaction chamber outlet 1012, preferably, the high temperature heat pipe 2 is caused to penetrate the catalytic reforming region in a direction extending from the first reaction chamber inlet 1011 towards the first reaction chamber outlet 1012; in addition, the number of the high-temperature heat pipes 2 may be 1 or more, and is not limited in this embodiment. In addition, in order to add the catalyst 3 into the catalytic reforming region, catalyst adding ports may be opened in the casing walls of the inner casing 101 and the outer casing 102, and a sealing cap may be mounted on each catalyst adding port, the catalyst 3 is added to the catalytic reforming zone by opening and closing the seal cover, and, similarly, to replace the catalyst 3, the catalyst can be discharged through opening catalyst discharge ports in the walls of the inner case 101 and the outer case 102, and installing a sealing cap on each catalyst discharge port, the catalyst 3 may be discharged by opening and closing the seal cover, only the catalyst addition port and the catalyst discharge port may be opened in the inner casing 101, the seal cover may be attached to both the catalyst addition port and the catalyst discharge port, and at the same time, an attachment opening is opened in the outer case 102, and a seal cover is attached to the attachment opening so that the inner case 101 can be taken out or attached to the outer case 102 or the like through the attachment opening.

The liquid fuel catalytic reforming device also comprises a feeding assembly; the feeding assembly comprises a feeding pipeline, and an outlet of the feeding pipeline is communicated with the inlet 11 of the reaction cavity; the supply lines include a fuel line 41 and an oxidizer line 42; the outlet of the fuel pipeline 41 and the outlet of the oxidant pipeline 42 are both communicated with the inlet 1011 of the first reaction cavity; the feed assembly further comprises a first nozzle 43; the first nozzle 43 is a two-fluid nozzle, the outlet of the fuel line 41 and the outlet of the oxidant line 42 being connected to the inlet end of the two-fluid nozzle, the outlet end of the two-fluid nozzle extending into the interior of the first reaction chamber inlet 1011. The two-fluid nozzle includes, but is not limited to, a pressure type two-fluid nozzle, a siphon type two-fluid nozzle, and the like.

Wherein, the outlet of the fuel pipeline 41 and the outlet of the oxidant pipeline 42 are both communicated with the inlet 1011 of the first reaction chamber; an oxidant line 42 passes through the second reaction chamber.

In this embodiment, the housing includes the inner housing 101 and the outer housing 102, and the oxidant pipeline 42 passes through the second reaction chamber, so that the reformed gas flowing out from the outlet 1012 of the first reaction chamber flows to the outlet 1022 of the second reaction chamber along the inner wall of the outer housing in the second reaction chamber, and when the reformed gas passes through the oxidant pipeline 42, the reformed gas can not only cool the reformed gas itself, but also preheat the oxidant in the oxidant pipeline 42 before reaction, thereby fully utilizing the residual heat of the reformed gas and improving the catalytic reforming reaction efficiency.

With continued reference to FIGS. 4 and 5, in an alternative embodiment of this embodiment, the second reaction chamber outlet 1022 is open at an end of the outer shell 102 remote from the first reaction chamber outlet 1012, and the second reaction chamber outlet 1022 is close to the first reaction chamber inlet 1011; oxidant line 42 passes through the interior space of the second reaction chamber at a location adjacent to second reaction chamber outlet 1022. Therefore, the path of the reformed gas flowing in the second reaction cavity along the inner wall of the outer shell to the outlet 1022 of the second reaction cavity is a reverse backflow path around the outer wall of the inner shell, and the inside of the first reaction cavity can be insulated in the backflow process, so that the heat loss in the inside of the first reaction cavity is avoided, and the efficient and stable operation of the catalytic reforming reaction is ensured.

Referring to fig. 6, in conjunction with fig. 4 and 5, in this embodiment, or on the basis of the above alternative embodiment, the above-mentioned feed assembly may further include a second nozzle 44, and the second nozzle 44 may have a plurality; the oxidant pipeline 42 has a plurality of pipeline outlets, wherein one pipeline outlet is connected to the inlet end of the two-fluid nozzle, the other pipeline outlets are connected to the inlet ends of the plurality of second nozzles 44 in a one-to-one correspondence manner, and the outlet ends of the plurality of second nozzles 44 all extend into the inlet 1011 of the first reaction chamber; the plurality of second nozzles 44 are arranged at intervals of two by two around the first nozzle 43, and the plurality of second nozzles 44 are arranged such that the discharged fluid swirls in a radial direction of an imaginary circle having a point on a center line of the fluid discharged from the first nozzle 43 as a center point to form a tangential swirl flow. With such a structure, a reaction raw material premixing area can be formed at the position of the reaction chamber at the inlet 1011 of the first reaction chamber, preferably, referring to fig. 4, 5 and 6, the opening of the inlet 1011 of the first reaction chamber is upward, the first nozzle 43 is vertically suspended in the central area of the inlet 1011 of the first reaction chamber, and the plurality of second nozzles 44 are arranged around the first nozzle 43 at equal intervals two by two in a horizontal plane; further preferably, the plurality of second nozzles 44 are located obliquely below the first nozzle 43, and part of the oxidant and the liquid fuel are crushed and atomized together by the first nozzle 43 and then dispersed to be sprayed into the inlet 1011 of the first reaction chamber; the rest of the oxidant is crushed and atomized by the second nozzle 44 and then sprayed into the inlet 11 of the reaction chamber to form a tangential rotational flow, and the tangential rotational flow is fully contacted and mixed with the mixed fluid of the fuel and the oxidant which are sprayed by the first nozzle 43 and are dispersed in a conical shape, so that the oxidant and the fuel can be fully mixed, and the efficient mixing effect can be achieved.

In addition, in any optional embodiment of the present embodiment, a manifold may be installed at the outlet 1012 of the first reaction chamber to dredge the reformed gas, a flow guide member such as a flow guide plate member may be installed inside the second reaction chamber to guide the flow path of the reformed gas, and the outlet 1022 of the second reaction chamber may be connected to a solid oxide fuel cell for power generation, or connected to a gas purification and separation apparatus to generate hydrogen for power generation of a proton exchange membrane fuel cell or chemical synthesis.

Additionally, referring to fig. 4 and 5, in some alternative embodiments of the present embodiment, in the case where the inside of the catalytic reforming region is filled with the catalyst 3, the concentration of the catalyst 3 gradually increases in a direction in which the fluid flows from the first reaction chamber inlet 1011 to the first reaction chamber outlet 1012.

In addition, referring to fig. 4 and 5, on the basis that the liquid fuel catalytic reforming device provided in the present embodiment further includes a supply assembly, optionally, the liquid fuel catalytic reforming device further includes a heating assembly 5; the heating assembly 5 is mounted inside the reaction chamber adjacent to the first reaction chamber inlet 1011 and the heating assembly 5 is located upstream of the catalytic reforming zone in the direction of fluid flow from the first reaction chamber inlet 1011 to the first reaction chamber outlet 1012 for igniting or evaporating the fluid injected into the first reaction chamber inlet 1011 before the fluid injected into the first reaction chamber inlet 1011 flows towards the catalytic reforming zone. The specific structure of the heating assembly 5 includes, but is not limited to, a heating rod, a glow plug, a heating net, etc., wherein the heating assembly 5 is mounted on the wall of the inner housing 101, and the heating assembly 5 is provided with a heating wire which passes through the wall of the inner housing 101 and the wall of the outer housing 102 in turn and is connected to an external power source.

Further, referring to fig. 4 and 5, in some alternative embodiments of this embodiment, the liquid fuel catalytic reforming device further comprises a heat conducting member 6, the heat conducting member 6 is installed inside the reaction chamber at a position close to the first reaction chamber inlet 1011, and the heat conducting member 6 is located upstream of the catalytic reforming region in a direction in which the fluid flows from the first reaction chamber inlet 1011 to the first reaction chamber outlet 1012, and the heat conducting member 6 is configured to: in the case where the catalyst 3 is filled in the inside of the catalytic reforming region, the end of the heat-conducting member 6 close to the catalyst 3 is in contact with the catalyst 3, wherein the way in which the end of the heat-conducting member 6 close to the catalyst 3 is in contact with the catalyst 3 includes, but is not limited to, the way in which the end of the heat-conducting member 6 close to the catalyst 3 is inserted in the inside of the catalyst 3. Preferably, the heat-conducting member 6 is porous, and may be made of a wire mesh, a metal foam, a porous ceramic, or the like.

In addition, referring to fig. 4 and 5, in some alternative embodiments of this embodiment, an insulating layer 7 is further disposed outside the outer casing 102, and preferably, as shown in fig. 4 and 5, the portions of the fuel pipe 41 and the oxidant pipe 42 close to the inlet 1011 of the first reaction chamber are located inside the insulating layer 7, or insulating materials may be separately wrapped outside the fuel pipe 41 and outside the oxidant pipe 42 to avoid heat loss of the preheated oxidant. Further, if some parts of the inner housing 101 are located outside the second reaction chamber, for example, the part of the inner housing 101, which is opened with the inlet 1011 of the first reaction chamber, is located outside the second reaction chamber, it is preferable that the part of the inner housing 101, which is located outside the second reaction chamber, is also located inside the insulating layer 7, so as to avoid heat loss inside the first reaction chamber.

The effects that can be achieved by the same structures in the above-described alternative embodiments of the present embodiment as in the first embodiment can be understood and applied with reference to the first embodiment.

Finally, it should be noted that: in the embodiment of the present invention, the liquid fuel in the first and second embodiments includes but is not limited to liquid fuel such as gasoline, diesel oil, kerosene, alcohols, etc.; reforming conversion methods suitable for the liquid fuel catalytic reforming device include, but are not limited to, steam reforming, autothermal reforming, partial oxidation reforming, and the like.

In addition, the above embodiments are only used for illustrating the technical solutions of the present invention, and not for limiting the same; although the present invention has been described in detail with reference to the foregoing embodiments, it should be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; such modifications and substitutions do not depart from the spirit and scope of the present invention.

Claims (11)

1. The catalytic reforming device for the liquid fuel is characterized by comprising a shell (1) and a high-temperature heat pipe (2);

a reaction chamber is arranged in the shell (1), the interior of the reaction chamber comprises a catalytic reforming area, and the catalytic reforming area is filled with a catalyst (3);

the parts of the shell (1) at the two ends of the catalytic reforming region are respectively provided with a reaction cavity inlet (11) and a reaction cavity outlet (12); the high temperature heat pipe (2) is configured to be able to fit inside the catalytic reforming zone to equalize the temperature of the catalyst (3) filled inside the catalytic reforming zone in the direction of fluid flow from the reaction chamber inlet (11) to the reaction chamber outlet (12).

2. A liquid fuel catalytic reforming apparatus according to claim 1, wherein the concentration of the catalyst (3) is gradually increased in a direction in which a fluid flows from the reaction chamber inlet (11) to the reaction chamber outlet (12) in a case where the inside of the catalytic reforming region is filled with the catalyst (3).

3. The catalytic reformer of claim 1, further comprising a feed assembly; the feeding assembly comprises a feeding pipeline, and an outlet of the feeding pipeline is communicated with the inlet (11) of the reaction cavity.

4. A catalytic reformer in liquid fuel as claimed in claim 3,

the feed line comprises a fuel line (41) and an oxidant line (42); the outlet of the fuel pipeline (41) and the outlet of the oxidant pipeline (42) are both communicated with the inlet (11) of the reaction cavity;

the feed assembly further comprises a first nozzle (43); the first nozzle (43) is a two-fluid nozzle, the outlet of the fuel line (41) and the outlet of the oxidant line (42) are connected to the inlet end of the two-fluid nozzle, and the outlet end of the two-fluid nozzle extends into the interior of the reaction chamber inlet (11).

5. The catalytic reformer of claim 4, wherein the feed assembly further comprises a second nozzle (44), the second nozzle (44) having a plurality;

the oxidant pipeline (42) is provided with a plurality of pipeline outlets, one pipeline outlet is connected to the inlet end of the two-fluid nozzle, the other pipeline outlets are connected to the inlet ends of the second nozzles (44) in a one-to-one correspondence manner, and the outlet ends of the second nozzles (44) all extend into the reaction cavity inlet (11);

the plurality of second nozzles (44) are arranged at intervals in pairs around the first nozzle (43), and the plurality of second nozzles (44) are arranged so that the discharged fluid flows in a swirling manner in a radial direction of an imaginary circle having a point on a center line of the fluid discharged from the first nozzle (43) as a center point, thereby forming a tangential swirling flow.

6. A catalytic reformer for liquid fuels according to any of claims 3 to 5, characterized in that it further comprises a heating assembly (5);

the heating assembly (5) is mounted inside the reaction chamber at a position close to the reaction chamber inlet (11), and in the direction of fluid flow from the reaction chamber inlet (11) to the reaction chamber outlet (12), the heating assembly (5) is located upstream of the catalytic reforming region for igniting or evaporating the fluid injected into the reaction chamber inlet (11) before the fluid injected into the reaction chamber inlet (11) flows towards the catalytic reforming region.

7. A catalytic reformer for liquid fuels according to any of claims 3 to 5, characterized in that it further comprises a heat conducting element (6), the heat conducting element (6) being mounted inside the reaction chamber at a position close to the inlet (11) of the reaction chamber and the heat conducting element (6) being located upstream of the catalytic reforming zone in the direction of fluid flow from the inlet (11) to the outlet (12) of the reaction chamber, and the heat conducting element (6) being configured to: in the case where the inside of the catalytic reforming region is filled with a catalyst (3), one end of the heat-conducting member (6) close to the catalyst (3) is in contact with the catalyst (3).

8. A catalytic reformer according to claim 7, characterized in that the heat-conducting member (6) is porous.

9. Catalytic reformer according to any of the claims 1 to 5, characterized in that an insulating layer (7) is provided outside the shell (1).

10. A catalytic reformer in liquid fuel according to claim 4 or 5,

the shell (1) comprises an inner shell (101) and an outer shell (102), a first reaction cavity is arranged inside the inner shell (101), and a second reaction cavity is arranged inside the outer shell (102); the catalytic reforming region is arranged in the first reaction cavity, the positions, located at two ends of the catalytic reforming region, of the inner shell (101) are respectively provided with a first reaction cavity inlet (1011) and a first reaction cavity outlet (1012), and the outer shell (102) is provided with a second reaction cavity inlet (1021) and a second reaction cavity outlet (1022); the inner shell (101) is arranged inside the second reaction chamber, and an inlet (1011) of the first reaction chamber is communicated with an inlet (1021) of the second reaction chamber in a sealing way;

the outlet of the fuel pipeline (41) and the outlet of the oxidant pipeline (42) are both communicated with the inlet (1011) of the first reaction cavity; the oxidant line (42) passes through the second reaction chamber.

11. A catalytic reformer for liquid fuels according to claim 10, characterized in that the second reaction chamber outlet (1022) opens at an end of the outer shell (102) remote from the first reaction chamber outlet (1012), and the second reaction chamber outlet (1022) is close to the first reaction chamber inlet (1011); the oxidant line (42) passes through the interior space of the second reaction chamber at a location proximate to the second reaction chamber outlet (1022).

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