A gaseous hydrocarbon autothermal reforming apparatus and method

Abstract

This invention relates to a gaseous hydrocarbon autothermal reforming apparatus and method. The gaseous hydrocarbon autothermal reforming apparatus includes a gaseous hydrocarbon heating mechanism, a desulfurization tank, a mixer, a catalytic reforming furnace, an oxygen heater, a waste heat recovery mechanism, and a carbon dioxide separator. A gaseous hydrocarbon input pipeline is connected to the desulfurization tank, and a gaseous hydrocarbon heating mechanism is installed on the gaseous hydrocarbon input pipeline. A medium-pressure steam input pipeline and a carbon dioxide input pipeline are connected to the mixer. The desulfurization tank is connected to the medium-pressure steam input pipeline through the desulfurization pipeline. The mixer is connected to the first inlet of the catalytic reforming furnace through a mixing output pipeline. An oxygen input pipeline is connected to the second inlet of the catalytic reforming furnace, and an oxygen heater is installed on the oxygen input pipeline. A boiler water input pipeline is connected to the third inlet of the catalytic reforming furnace. A syngas pipeline is connected to the syngas pipeline, and a waste heat recovery mechanism and a carbon dioxide separator are installed on the syngas pipeline. The carbon dioxide separator is connected to the mixer through a carbon dioxide circulation pipeline.

Description

Technical Field

[0001] This invention relates to the technical field of gaseous hydrocarbon autothermal reforming, specifically to a gaseous hydrocarbon autothermal reforming apparatus and method. Background Technology

[0002] Autothermal reforming of gaseous hydrocarbons has become an important technical route for syngas production due to its combination of rapid exothermic partial oxidation and efficient syngas production via steam reforming. Traditional steam reforming processes are energy-intensive, require external heating, and have high carbon emission intensity. Existing autothermal reforming technologies generally suffer from high water-to-carbon and hydrogen-to-carbon ratios, easy catalyst deactivation due to carbon buildup, and poor CO2 emission control, making it difficult to simultaneously meet the requirements of high-efficiency conversion, stable operation, and low-carbon emission reduction. With the transformation of energy structure and the advancement of dual-carbon policies, industrial production places higher demands on the energy efficiency, economy, and environmental friendliness of syngas production processes. Therefore, developing a novel autothermal reforming technology for syngas production from gaseous hydrocarbons with low energy consumption, low emissions, and stable reaction is of significant practical importance. Summary of the Invention

[0003] In order to solve one or more technical problems existing in the prior art, the present invention provides a gaseous hydrocarbon autothermal reforming apparatus and method.

[0004] The technical solution of this invention to solve the above-mentioned technical problems is as follows: This invention provides a gaseous hydrocarbon self-heating reforming device, including a gaseous hydrocarbon heating mechanism, a desulfurization tank, a mixer, a catalytic reforming furnace, an oxygen heater, a waste heat recovery mechanism, and a carbon dioxide separator. A gaseous hydrocarbon input pipeline is connected to the desulfurization tank, and a gaseous hydrocarbon heating mechanism is installed on the gaseous hydrocarbon input pipeline. A medium-pressure steam input pipeline and a carbon dioxide input pipeline are connected to the mixer. The desulfurization tank is connected and communicates with the medium-pressure steam input pipeline through the desulfurization pipeline. The mixer is connected and communicates with the first inlet of the catalytic reforming furnace through a mixing output pipeline. An oxygen input pipeline is connected to the second inlet of the catalytic reforming furnace, and an oxygen heater is installed on the oxygen input pipeline. A boiler water input pipeline is connected to the third inlet of the catalytic reforming furnace. A syngas pipeline is connected to the outlet of the catalytic reforming furnace. A waste heat recovery mechanism and a carbon dioxide separator are sequentially installed on the syngas pipeline along the syngas conveying direction. The carbon dioxide separator is connected and communicates with the mixer through a carbon dioxide circulation pipeline.

[0005] The beneficial effects of this invention are: the gaseous hydrocarbon autothermal reforming device of this invention can not only flexibly adjust the hydrogen-carbon ratio of the synthesis gas to meet the production needs of various chemical products, such as methanol, ethanol, ethylene glycol, acetic acid and Fischer-Tropsch synthesis products, but also reduce CO2 emissions, achieving the purpose of energy conservation and emission reduction.

[0006] Based on the above technical solution, the present invention can be further improved as follows.

[0007] Furthermore, the gaseous hydrocarbon heating mechanism includes a gaseous hydrocarbon heater, the heating temperature range of which is 230℃~380℃.

[0008] Furthermore, the gaseous hydrocarbon heating mechanism includes a heating furnace, the gaseous hydrocarbon input pipeline is connected and communicates with the convection section input port of the heating furnace, the convection section output port of the heating furnace is connected and communicates with the desulfurization tank, the medium-pressure steam input pipeline is connected and communicates with the radiation section input port of the heating furnace, and the radiation section output port of the heating furnace is connected and communicates with the mixer.

[0009] The beneficial effect of adopting the above-mentioned further scheme is that, through the high-temperature heating of the radiant section of the heating furnace, medium-pressure steam and gaseous hydrocarbons can undergo thermal oxygen self-ignition without ignition after entering the catalytic reformer.

[0010] Furthermore, the heating temperature range of the convection section is 230℃~380℃, and the heating temperature range of the radiation section is 450℃~650℃.

[0011] Furthermore, the waste heat recovery mechanism includes a waste heat boiler and a boiler water heater. The waste heat boiler, boiler water heater, and carbon dioxide separator are sequentially installed on the syngas pipeline along the syngas conveying direction. A waste heat recovery pipeline is connected to the boiler water input pipeline. The waste heat recovery pipeline connects the boiler water heater and the waste heat boiler in series. The syngas temperature passing through the waste heat boiler in the syngas pipeline is 350℃~400℃, and the syngas temperature passing through the boiler water heater in the syngas pipeline is 180℃~250℃.

[0012] Furthermore, a catalyst bed is installed at the bottom of the catalytic reformer, and the catalyst bed is an anti-carbon deposition catalyst bed.

[0013] Furthermore, the first inlet of the catalytic reforming furnace is located on the top side wall of the catalytic reforming furnace, the second inlet of the catalytic reforming furnace is located on the top wall of the catalytic reforming furnace, the outlet of the catalytic reforming furnace is located on the bottom wall of the catalytic reforming furnace, and the third inlet of the catalytic reforming furnace is located on the bottom side wall of the jacket.

[0014] Furthermore, the working pressure of the catalytic reforming furnace is 2MPa~3MPa, and the outlet temperature of the catalytic reforming furnace is 800℃~1000℃; the oxygen heater preheats the oxygen in the oxygen input pipeline to 200℃~230℃.

[0015] The present invention also provides a method for self-heating reforming of gaseous hydrocarbons, which is implemented using a gaseous hydrocarbon self-heating reforming apparatus as described above, and includes the following steps: Gaseous hydrocarbons are heated to 230℃~380℃ through a gaseous hydrocarbon heating mechanism on the gaseous hydrocarbon input pipeline, and then enter the desulfurization tank for desulfurization to form desulfurized gas. The desulfurized gas is input into the medium-pressure steam input pipeline through the desulfurization pipeline and mixed with the medium-pressure steam. It is then input into the mixer through the mixing input pipeline and mixed with the carbon dioxide input into the mixer through the carbon dioxide input pipeline to form raw material mixed gas. The oxygen supplied by the oxygen input pipeline is preheated to 200-230°C by the oxygen heater and then supplied to the catalytic reformer. The raw material mixture in the mixer is also supplied to the catalytic reformer and reacts with the preheated oxygen at high temperature. An exothermic oxidation reaction first occurs in the upper part of the catalytic reformer, and an endothermic catalytic reforming reaction occurs in the lower catalytic bed region of the catalytic reformer to generate syngas. The syngas is output through a syngas pipeline, and the waste heat recovery mechanism recovers waste heat from the syngas in the syngas pipeline.

[0016] The beneficial effects of this invention are: the gaseous hydrocarbon autothermal reforming method of this invention can not only flexibly adjust the hydrogen-carbon ratio of the synthesis gas to meet the production needs of various chemical products, such as methanol, ethanol, ethylene glycol, acetic acid and Fischer-Tropsch synthesis products, but also reduce CO2 emissions, achieving the purpose of energy conservation and emission reduction.

[0017] Furthermore, the molar ratio of carbon dioxide input through the carbon dioxide input pipeline to gaseous hydrocarbons input through the gaseous hydrocarbon input pipeline is 0.1 to 0.7; the molar ratio of water vapor input through the medium-pressure steam input pipeline to gaseous hydrocarbons input through the gaseous hydrocarbon input pipeline is 0.05 to 1; and the molar ratio of oxygen input through the oxygen input pipeline to gaseous hydrocarbons input through the gaseous hydrocarbon input pipeline is 0.5 to 0.65. Attached Figure Description

[0018] Figure 1 This is a schematic diagram of the structure of the gaseous hydrocarbon autothermal reforming device of the present invention. Figure 1 ; Figure 2 This is a schematic diagram of the structure of the gaseous hydrocarbon autothermal reforming device of the present invention. Figure 2 .

[0019] The attached diagram lists the components represented by each number as follows: 1. Gas hydrocarbon heater; 2. Heating furnace; 21. Convection section; 22. Radiation section; 3. Desulfurization tank; 31. Gaseous hydrocarbon input pipeline; 32. Desulfurization pipeline; 4. Mixer; 41. Medium-pressure steam input line; 42. Carbon dioxide input line; 43. Mixing input line; 5. Catalytic reformer; 51. Oxygen input pipeline; 52. Oxygen heater; 53. Boiler water input pipeline; 54. Syngas pipeline; 55. Mixed output pipeline; 6. Carbon dioxide separator; 61. Carbon dioxide circulation pipeline; 7. Waste heat boiler; 71. Boiler water heater; 72. Waste heat recovery pipeline. Detailed Implementation

[0020] The principles and features of the present invention are described below. The examples given are only for explaining the present invention and are not intended to limit the scope of the present invention.

[0021] Example 1 like Figure 1 and Figure 2 As shown, this embodiment of a gaseous hydrocarbon self-heating reforming device includes a gaseous hydrocarbon heating mechanism, a desulfurization tank 3, a mixer 4, a catalytic reforming furnace 5, an oxygen heater 52, a waste heat recovery mechanism, and a carbon dioxide separator 6. A gaseous hydrocarbon input pipeline 31 is connected to the desulfurization tank 3, and the gaseous hydrocarbon heating mechanism is installed on the gaseous hydrocarbon input pipeline 31. A medium-pressure steam input pipeline 41 and a carbon dioxide input pipeline 42 are connected to the mixer 4. The desulfurization tank 3 is connected and communicates with the medium-pressure steam input pipeline 41 through the desulfurization pipeline 32. The mixer 4 outputs a mixture... Pipeline 55 is connected to and communicates with the first inlet of the catalytic reformer 5. The second inlet of the catalytic reformer 5 is connected to an oxygen input pipeline 51, and an oxygen heater 52 is installed on the oxygen input pipeline 51. The third inlet of the catalytic reformer 5 is connected to a boiler water input pipeline 53. The outlet of the catalytic reformer 5 is connected to a syngas pipeline 54. A waste heat recovery mechanism and a carbon dioxide separator 6 are installed sequentially on the syngas pipeline 54 along the syngas conveying direction. The carbon dioxide separator 6 is connected to and communicates with the mixer 4 through a carbon dioxide circulation pipeline 61.

[0022] like Figure 1 and Figure 2 As shown, the first inlet of the catalytic reformer 5 is located on the top side wall of the catalytic reformer 5, the second inlet of the catalytic reformer 5 is located on the top wall of the catalytic reformer 5, the outlet of the catalytic reformer 5 is located on the bottom wall of the catalytic reformer 5, and the third inlet of the catalytic reformer 5 is located on the bottom side wall of the jacket of the catalytic reformer 5.

[0023] The gaseous hydrocarbon autothermal reforming unit in this embodiment not only allows for flexible adjustment of the hydrogen-to-carbon ratio in the synthesis gas, ranging from 1.1 to 2.3, to meet the production needs of various chemical products, such as methanol, ethanol, ethylene glycol, acetic acid, and Fischer-Tropsch synthesis products, but also reduces CO2 emissions, achieving energy conservation and emission reduction. This embodiment employs a catalytic reformer and recovers carbon dioxide, resulting in a lower outlet temperature for the catalytic reformer compared to reformers without a catalyst bed. This extends the service life of the waste heat boiler and reduces its maintenance frequency and operating costs.

[0024] Example 2 Based on Example 1, this example provides an alternative solution for a gaseous hydrocarbon heating mechanism, such as... Figure 1 As shown, the gaseous hydrocarbon heating mechanism includes a gaseous hydrocarbon heater 1, and the heating temperature range of the gaseous hydrocarbon heater 1 is 230℃~380℃.

[0025] Example 3 Based on Example 1, this example provides an alternative solution for a gaseous hydrocarbon heating mechanism, such as... Figure 2 As shown, the gaseous hydrocarbon heating mechanism includes a heater 2, which comprises a convection section 21 and a radiation section 22 from top to bottom. The gaseous hydrocarbon input pipeline 31 is connected to and communicates with the input port of the convection section 21 of the heater 2, and the output port of the convection section 21 of the heater 2 is connected to and communicates with the desulfurization tank 3. The medium-pressure steam input pipeline 41 is connected to and communicates with the input port of the radiation section 22 of the heater 2, and the output port of the radiation section 22 of the heater 2 is connected to and communicates with the mixer 4. Through high-temperature heating in the heater, the feed gas can spontaneously combust after entering the catalytic reformer without ignition.

[0026] Specifically, the heating temperature range of the convection section 21 is 230℃~380℃, and the heating temperature range of the radiation section 22 is 450℃~650℃.

[0027] Example 4 Based on any of the above embodiments, this embodiment provides a specific solution for a waste heat recovery mechanism, such as... Figure 1 and Figure 2 As shown, the waste heat recovery mechanism includes a waste heat boiler 7 and a boiler water heater 71. The waste heat boiler 7, the boiler water heater 71, and the carbon dioxide separator 6 are sequentially installed on the syngas pipeline 54 along the syngas conveying direction. A waste heat recovery pipeline 72 is connected to the boiler water input pipeline 53. The waste heat recovery pipeline 72 is connected in series with the boiler water heater 71 and the waste heat boiler 7. The syngas temperature passing through the waste heat boiler 7 in the syngas pipeline 54 is 350℃~400℃, and the syngas temperature passing through the boiler water heater 71 in the syngas pipeline 54 is 180℃~250℃.

[0028] Example 5 Based on any of the above embodiments, this embodiment provides an optional structure for the catalytic reformer 5, such as... Figure 1 and Figure 2 As shown, a catalyst bed is installed at the bottom of the catalytic reformer 5. The catalyst bed can be a commonly used anti-carbon deposition catalyst, such as a typical nickel-based catalyst like Ni / Ce. 0.8 Zr 0.2 O 2-x , Ni-La2O2CO3 / Al2O3, Ni-Pr / Al2O3, Ni-Ga / ZrO2-Al2O3, Ni / CeO x -Al2O3, or polymetallic LaAl 0.3 Mn 0.2 Ni 0.5 O 3-δ CoNi / Al2O3.

[0029] Example 6 Based on any of the above embodiments, the working pressure of the catalytic reformer 5 in this embodiment is 2MPa~3MPa, and the outlet temperature of the catalytic reformer 5 is 800℃~1000℃; the oxygen heater 52 preheats the oxygen in the oxygen input pipeline 51 to 200℃~230℃.

[0030] Example 7 This embodiment provides a method for the self-heating reforming of gaseous hydrocarbons, implemented using a gaseous hydrocarbon self-heating reforming apparatus as described in any of the above embodiments, including the following steps: Gaseous hydrocarbons are heated to 230°C~380°C by a gaseous hydrocarbon heating mechanism (preferably a furnace with a heating section and a radiation section) on the gaseous hydrocarbon input pipeline 31, and then enter the desulfurization tank 3 for desulfurization to form desulfurized gas. The desulfurized gas is input into the medium-pressure steam input pipeline 41 through the desulfurization pipeline 32 and mixed with the medium-pressure steam. It is then input into the mixer 4 through the mixing input pipeline 43 (before being input into the mixer 4, the desulfurized gas and medium-pressure steam can also be heated to 450°C~650°C in the radiation section of the furnace). It is mixed with the carbon dioxide input into the mixer 4 through the carbon dioxide input pipeline 42 to form a raw material mixed gas. The carbon dioxide entering the mixer can be carbon dioxide separated by a carbon dioxide separator, or carbon dioxide from outside the catalytic reformer can be used as supplementary carbon dioxide.

[0031] The oxygen supplied by the oxygen input pipeline 51 is preheated to 200-230°C by the oxygen heater 52 and then supplied to the catalytic reformer 5. The raw material mixture in the mixer 4 is also supplied to the catalytic reformer 5 and reacts with the preheated oxygen at a high temperature. An exothermic oxidation reaction first occurs in the upper part of the catalytic reformer 5, mainly producing carbon dioxide and water, with a furnace temperature of 1300°C-1800°C. In the lower catalytic bed region of the catalytic reformer 5, alkanes (gaseous hydrocarbons), carbon dioxide, and water vapor undergo an endothermic catalytic reforming reaction to produce syngas, with a furnace temperature lower than that of the upper part of the catalytic reformer. The syngas is output through syngas pipeline 54, and the waste heat recovery mechanism recovers waste heat from the syngas within the syngas pipeline 54. The syngas sequentially passes through a waste heat boiler and a boiler water heater for heat recovery. The medium-pressure steam produced by the waste heat boiler goes to the steam network. The cooled syngas passes through a carbon dioxide separator and is then sent to downstream units. The carbon dioxide separated by the carbon dioxide separator is recycled into the catalytic reformer for high-temperature reforming. Part of the boiler water from outside the system is used as cooling water in the cooling water jacket of the catalytic reformer, and the remainder is used as boiler feedwater for the waste heat boiler, producing medium-pressure steam as a byproduct.

[0032] In this embodiment, the gaseous hydrocarbon can be natural gas, methane-rich gas, coke oven gas, coalbed methane, biogas, or other low-carbon hydrocarbons.

[0033] In this embodiment, the molar ratio of carbon dioxide input through carbon dioxide input pipeline 42 to gaseous hydrocarbon input through gaseous hydrocarbon input pipeline 31 is 0.1~0.7; the molar ratio of water vapor input through medium-pressure steam input pipeline 41 to gaseous hydrocarbon input through gaseous hydrocarbon input pipeline 31 is 0.05~2; and the molar ratio of oxygen input through oxygen input pipeline 51 to gaseous hydrocarbon input through gaseous hydrocarbon input pipeline 31 is 0.5~0.65.

[0034] The gaseous hydrocarbon autothermal reforming method of this embodiment uses gaseous hydrocarbons, oxygen, and CO2 as raw materials. After heating, the gaseous hydrocarbons undergo a catalytic partial oxidation high-temperature reforming reaction to generate syngas. After the heat of the high-temperature syngas is recovered, it is separated by CO2. The separated CO2 is then mixed with the gaseous hydrocarbons again to participate in the reforming reaction, thus realizing a production process of zero-carbon or negative-carbon emission combined autothermal reforming.

[0035] Experimental Example 1 The outlet temperature of the heating furnace is 600℃, the hot oxygen temperature is 230℃, the water-to-carbon ratio is 0.8, the oxygen-to-carbon ratio is 0.55, and all the recycled CO2 separated from the syngas re-enters the catalytic reformer to participate in the reaction. The ratio of CO2 to gaseous hydrocarbons is 0.1. The outlet temperature of the catalytic reformer is 963℃, the working pressure of the catalytic reformer is 2MPag, and the hydrogen-to-carbon ratio of the syngas is 2.3.

[0036] Experimental Example 2 The heater outlet temperature is 600℃, and the hot oxygen temperature is 230℃; the water-to-carbon ratio is 0.2, and the oxygen-to-carbon ratio is 0.56. All the recycled CO2 separated from the syngas re-enters the catalytic reformer to participate in the reaction, while CO2 is supplemented from outside the unit. The CO2 to hydrocarbon ratio of the feed gas is 0.4. The catalytic reformer outlet temperature is 945℃, the operating pressure is 2 MPa, and the hydrogen-to-carbon ratio of the syngas is 1.4.

[0037] Experimental Example 3 The heater outlet temperature is 280℃, and the hot oxygen temperature is 230℃; the water-to-carbon ratio is 0.08, and the oxygen-to-carbon ratio is 0.62. All the recycled CO2 separated from the syngas re-enters the catalytic reformer to participate in the reaction, while CO2 is supplemented from outside the unit. The CO2 to hydrocarbon ratio of the feed gas is 0.7. The catalytic reformer outlet temperature is 907℃, the operating pressure is 2 MPa, and the hydrogen-to-carbon ratio of the syngas is 1.1.

[0038] Through the above three experimental examples, by adjusting the molar ratio of CO2 to the raw material hydrocarbons and combining different water-to-carbon ratios, syngas with different hydrogen-to-carbon ratios can be obtained.

[0039] The gaseous hydrocarbon autothermal reforming method of this embodiment can not only flexibly adjust the hydrogen-carbon ratio of the synthesis gas to meet the production needs of various chemical products, such as methanol, ethanol, ethylene glycol, acetic acid and Fischer-Tropsch synthesis products, but also reduce CO2 emissions, achieving the goal of energy conservation and emission reduction.

[0040] In the description of this invention, it should be understood that the terms "top", "bottom", "inner", "outer", etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are only for the convenience of describing this invention and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this invention.

[0041] Furthermore, the terms "first" and "second" are used for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the number of technical features indicated. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this invention, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0042] In this invention, unless otherwise explicitly specified and limited, the terms "installation," "connection," "linking," and "fixing," etc., should be interpreted broadly. For example, they can refer to a fixed connection, a detachable connection, or an integral part; they can refer to a direct connection or an indirect connection through an intermediate medium; they can refer to the internal communication of two components or the interaction between two components, unless otherwise explicitly limited. Those skilled in the art can understand the specific meaning of the above terms in this invention according to the specific circumstances.

[0043] In this invention, unless otherwise explicitly specified and limited, "above" or "below" the second feature can mean that the first feature is in direct contact with the second feature, or that the first feature is in indirect contact with the second feature through an intermediate medium. Furthermore, "above," "over," and "on top" of the second feature can mean that the first feature is directly above or diagonally above the second feature, or simply that the first feature is at a higher horizontal level than the second feature. "Below," "below," and "under" the second feature can mean that the first feature is directly below or diagonally below the second feature, or simply that the first feature is at a lower horizontal level than the second feature.

[0044] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the present invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. Moreover, without contradiction, those skilled in the art can combine and integrate the different embodiments or examples described in this specification, as well as the features of different embodiments or examples.

[0045] Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention. Those skilled in the art can make changes, modifications, substitutions and variations to the above embodiments within the scope of the present invention.

Claims

1. A gaseous hydrocarbon autothermal reforming device, characterized in that, The system includes a gaseous hydrocarbon heating mechanism, a desulfurization tank, a mixer, a catalytic reformer, an oxygen heater, a waste heat recovery mechanism, and a carbon dioxide separator. The desulfurization tank is connected to a gaseous hydrocarbon input pipeline, on which a gaseous hydrocarbon heating mechanism is installed. The mixer is connected to a medium-pressure steam input pipeline and a carbon dioxide input pipeline. The desulfurization tank is connected to and communicates with the medium-pressure steam input pipeline via the desulfurization pipeline. The mixer is connected to and communicates with the first inlet of the catalytic reformer via a mixing output pipeline. The second inlet of the catalytic reformer is connected to an oxygen input pipeline, on which an oxygen heater is installed. The third inlet of the catalytic reformer is connected to a boiler water input pipeline. The outlet of the catalytic reformer is connected to a syngas pipeline. A waste heat recovery mechanism and a carbon dioxide separator are sequentially installed along the syngas delivery direction on the syngas pipeline. The carbon dioxide separator is connected to and communicates with the mixer via a carbon dioxide circulation pipeline.

2. The gaseous hydrocarbon autothermal reforming apparatus according to claim 1, characterized in that, The gaseous hydrocarbon heating mechanism includes a gaseous hydrocarbon heater, and the heating temperature range of the gaseous hydrocarbon heater is 230℃~380℃.

3. The gaseous hydrocarbon autothermal reforming apparatus according to claim 1, characterized in that, The gaseous hydrocarbon heating mechanism includes a heating furnace, the gaseous hydrocarbon input pipeline is connected to and communicates with the convection section input port of the heating furnace, the convection section output port of the heating furnace is connected to and communicates with the desulfurization tank, the medium-pressure steam input pipeline is connected to and communicates with the radiation section input port of the heating furnace, and the radiation section output port of the heating furnace is connected to and communicates with the mixer.

4. The gaseous hydrocarbon autothermal reforming apparatus according to claim 3, characterized in that, The heating temperature range of the convection section is 230℃~380℃, and the heating temperature range of the radiation section is 450℃~650℃.

5. The gaseous hydrocarbon autothermal reforming apparatus according to claim 1, characterized in that, The waste heat recovery mechanism includes a waste heat boiler and a boiler water heater. The waste heat boiler, boiler water heater, and carbon dioxide separator are installed sequentially on the syngas pipeline along the syngas conveying direction. A waste heat recovery pipeline is connected to the boiler water input pipeline. The waste heat recovery pipeline connects the boiler water heater and the waste heat boiler in series. The syngas temperature passing through the waste heat boiler in the syngas pipeline is 350℃~400℃, and the syngas temperature passing through the boiler water heater in the syngas pipeline is 180℃~250℃.

6. The gaseous hydrocarbon autothermal reforming apparatus according to claim 1, characterized in that, The lower part of the catalytic reformer is equipped with a catalyst bed, which is an anti-carbon deposition catalyst bed.

7. The gaseous hydrocarbon autothermal reforming apparatus according to claim 1, characterized in that, The first inlet of the catalytic reforming furnace is located on the top side wall of the catalytic reforming furnace, the second inlet of the catalytic reforming furnace is located on the top wall of the catalytic reforming furnace, the outlet of the catalytic reforming furnace is located on the bottom wall of the catalytic reforming furnace, and the third inlet of the catalytic reforming furnace is located on the bottom side wall of the jacket of the catalytic reforming furnace.

8. The gaseous hydrocarbon autothermal reforming apparatus according to claim 1, characterized in that, The working pressure of the catalytic reforming furnace is 2MPa~3MPa, and the outlet temperature of the catalytic reforming furnace is 800℃~1000℃; the oxygen heater preheats the oxygen in the oxygen input pipeline to 200℃~230℃.

9. A method for autothermal reforming of gaseous hydrocarbons, characterized in that, The gaseous hydrocarbon autothermal reforming apparatus as described in any one of claims 1 to 8 is used to achieve this, comprising the following steps: Gaseous hydrocarbons are heated to 230℃~380℃ through a gaseous hydrocarbon heating mechanism on the gaseous hydrocarbon input pipeline, and then enter the desulfurization tank for desulfurization to form desulfurized gas. The desulfurized gas is input into the medium-pressure steam input pipeline through the desulfurization pipeline and mixed with the medium-pressure steam. It is then input into the mixer through the mixing input pipeline and mixed with the carbon dioxide input into the mixer through the carbon dioxide input pipeline to form raw material mixed gas. The oxygen supplied by the oxygen input pipeline is preheated to 200-230°C by the oxygen heater and then supplied to the catalytic reformer. The raw material mixture in the mixer is also supplied to the catalytic reformer and reacts with the preheated oxygen at high temperature. An exothermic oxidation reaction first occurs in the upper part of the catalytic reformer, and an endothermic catalytic reforming reaction occurs in the lower catalytic bed region of the catalytic reformer to generate syngas. The syngas is output through a syngas pipeline, and the waste heat recovery mechanism recovers waste heat from the syngas in the syngas pipeline.

10. The method for autothermal reforming of gaseous hydrocarbons according to claim 9, characterized in that, The molar ratio of carbon dioxide input through the carbon dioxide input pipeline to gaseous hydrocarbons input through the gaseous hydrocarbon input pipeline is 0.1 to 0.7; the molar ratio of water vapor input through the medium-pressure steam input pipeline to gaseous hydrocarbons input through the gaseous hydrocarbon input pipeline is 0.05 to 1; and the molar ratio of oxygen input through the oxygen input pipeline to gaseous hydrocarbons input through the gaseous hydrocarbon input pipeline is 0.5 to 0.65.

Images