Multi-burner autothermal reformer and reforming system

Abstract

The utility model relates to a kind of multi-burner self-heating reformer and conversion system, multi-burner self-heating reformer includes furnace body and at least two burners, the catalyst bed is equipped in the furnace body, raw material gas inlet is equipped on the upper portion lateral wall of furnace body, conversion gas outlet is equipped on the lower portion lateral wall of furnace body;At least two the burner is evenly arranged and is fixed in the top of furnace body, the lower end of burner is close to each other, the central axis of all burners and the central axis of furnace body converge in the same point, the included angle between the central axis of burner and the central axis of furnace body is 1 °~10 °, the distance between the lower end of burner and the catalyst bed is 4~6m.The utility model has the advantages of large single furnace processing capacity, high material mixing uniformity, uniform hearth temperature distribution, flexible load regulation, long service life of burner, etc., and the utility model can effectively solve the related technical problems of ATR reformer large-scale.

Description

Technical Field

[0001] This utility model relates to the technical field of converters, specifically to a multi-burner self-heating converter and conversion system. Background Technology

[0002] ATR is an abbreviation for Autothermal Reformer. In recent years, ATR technology has been widely used in large-scale methanol, synthetic ammonia and hydrogen production plants. It is suitable for producing effective gases CO and H2 from various gaseous hydrocarbons (methane content from 10% to 100%), such as natural gas, coke oven gas and methane-rich gas.

[0003] Under certain temperature and pressure conditions, gaseous hydrocarbons and pure oxygen injected through the burner mainly undergo an exothermic combustion reaction in the upper part of the converter, providing heat for the catalytic conversion of methane; the lower part of the converter is equipped with a catalyst, and methane and water vapor in the feed gas undergo an autothermal conversion reaction under the action of the catalyst.

[0004] Partial oxidation reaction occurring in the upper part of the converter: CH4+ O2 CO + 2H₂ ΔH = -35.7 kJ / mol; H2+ O2 H2O ΔH = -241.6 kJ / mol.

[0005] Catalytic conversion reaction occurring in the lower part of the converter: CH4+H2O CO + 3H₂ ΔH = 206.3 kJ / mol; CO + H₂O CO2 + H2 ΔH = -41.3 KJ / mol.

[0006] The burner has a significant impact on the reaction effect in the converter and is one of the core pieces of equipment. The existing ATR converter is only equipped with a single top burner, which has limited processing capacity. When processing a large amount of feed gas, problems such as uneven mixing of feed gas and oxygen, uneven temperature distribution in the furnace, and local overheating of the burner causing erosion will occur. The excessively long flame also seriously affects the working life of the catalyst.

[0007] To improve the processing capacity of converters, using multiple burners is an ideal technical direction. The operating conditions of a multi-burner converter differ from a single-burner converter, and the technical problems that need to be solved include: 1. With multiple burners, the increased flame diameter leads to a significant increase in the operating temperature of the furnace wall in the combustion reaction section, causing the refractory bricks to crack due to the high temperature. 2. To improve the service life of the refractory bricks, the aluminum content of the refractory bricks is increased, and the furnace diameter is also increased. This reduces the actual operating temperature of the furnace wall by decreasing the distance between the flame front and the furnace wall. However, this design introduces new problems. Due to the increased furnace diameter, the flow rate of the feed gas in the furnace decreases, the mixing efficiency of the feed gas and oxygen decreases, and the flame lengthens, resulting in a very uneven temperature distribution of the converted gas entering the catalyst bed, seriously affecting the catalyst life and catalytic conversion efficiency. Utility Model Content

[0008] This utility model addresses one or more technical problems existing in the prior art by providing a multi-burner self-heating converter and conversion system. It can rationally determine the technical characteristics between furnace diameter, number of burners, burner flow rate and feed gas processing capacity, thereby guiding the design of the converter and controlling the production and manufacturing costs of the equipment to the greatest extent.

[0009] The technical solution of this utility model to solve the above-mentioned technical problems is as follows: This utility model provides a multi-burner self-heating converter, including a furnace body and at least two burners. A catalyst bed is provided in the furnace body. A raw material gas inlet is provided on the upper side wall of the furnace body, and a conversion gas outlet is provided on the lower side wall of the furnace body. At least two burners are evenly arranged in a circular shape and fixed to the top of the furnace body. The lower ends of the burners are close to each other. The central axes of all burners intersect the central axis of the furnace body at the same point. The angle between the central axis of the burners and the central axis of the furnace body is 1°~10°. The distance between the lower end of the burner and the catalyst bed is 4~6m.

[0010] The beneficial effects of this utility model are: the multi-burner self-heating converter of this utility model has the advantages of large single furnace processing capacity, high material mixing uniformity, uniform furnace temperature distribution, flexible load adjustment, and long burner service life. This utility model can effectively solve the related technical problems of large-scale ATR converters.

[0011] Based on the above technical solution, the present invention can be further improved as follows.

[0012] Furthermore, the furnace body is provided with a horizontally arranged distributor, which is fixed on the inner side wall of the furnace body below the raw material gas inlet, and the lower end of the burner is arranged through the distributor.

[0013] The beneficial effect of adopting the above-mentioned further scheme is that by setting a horizontally arranged distributor in the furnace body, the raw material gas can be uniformly distributed in both the axial and radial directions of the furnace chamber.

[0014] Furthermore, the distributor has a cylindrical shell structure, and a first plate and a second plate are respectively provided at both ends of the distributor along the axial direction. The first plate and the second plate are arranged at intervals. The first plate has a plurality of first through holes, and the second plate has a plurality of second through holes. The plurality of first through holes and the plurality of second through holes are staggered along the axial direction of the distributor.

[0015] The beneficial effects of adopting the above-mentioned further scheme are as follows: the burner is equipped with a distributor, which adopts a cylindrical hollow structure. Several through holes are set at the upper and lower ends of the distributor, and the upper and lower through holes are offset at a certain angle. This structure allows the raw gas to be rectified at the upper end of the distributor after entering the converter, and then rectified again at the lower end of the distributor after entering the inner cavity of the distributor. The raw gas can be evenly distributed in both the axial and radial directions of the furnace, and the temperature distribution of the process gas entering the catalyst bed is very uniform.

[0016] Furthermore, the diameter of the first through hole is 5mm to 20mm, and the diameter of the second through hole is 5mm to 20mm.

[0017] Furthermore, when the number of burners is no more than 3, the distance between the lower end of the burner and the catalyst bed is 4-5m; when the number of burners is more than 3, the distance between the lower end of the burner and the catalyst bed is 5-6m.

[0018] The beneficial effects of adopting the above-mentioned further scheme are: by reasonably determining the number of burners and the distance between the burners and the catalyst bed based on the feed gas processing volume, it is possible to ensure that the combustion section of the converter has sufficient combustion and mixing space, avoid damage caused by flame licking the catalyst, ensure the efficient operation of the converter, and reasonably control the equipment manufacturing cost.

[0019] Furthermore, a water-cooled jacket is provided on the outer wall of the furnace body, and the water-cooled jacket is provided with a cooling water inlet and a steam outlet.

[0020] Furthermore, the inner wall of the furnace body is provided with a refractory lining.

[0021] This utility model also provides a conversion system, including a multi-burner self-heating converter as described above, and further including a raw material gas pipeline, a conversion gas pipeline, a protective steam main pipeline, an oxygen main pipeline, protective steam branch pipelines, and oxygen branch pipelines. The oxygen main pipeline is connected to and communicates with the upper ends of the at least two burners through at least two oxygen branch pipelines. The protective steam main pipeline is connected to and communicates with at least two protective steam branch pipelines respectively. The at least two protective steam branch pipelines are connected to and communicate with at least two oxygen branch pipelines in a one-to-one correspondence. The raw material gas pipeline is connected to and communicates with the raw material gas inlet, and the conversion gas pipeline is connected to and communicates with the conversion gas outlet.

[0022] The beneficial effects of this invention are as follows: The conversion system of this invention can rationally determine parameters such as the number of burners, burner flow rate, and distance between the burners and the catalyst bed based on the feed gas throughput. This ensures sufficient combustion and mixing space in the combustion section of the converter, avoids damage caused by flame licking the catalyst, and guarantees efficient operation of the converter while reasonably controlling equipment manufacturing costs. Furthermore, by rationally determining the technical characteristics between the furnace diameter, the number of burners, the burner flow rate, and the feed gas throughput, this conversion system guides the design of the converter, maximizing the control of equipment manufacturing costs.

[0023] Furthermore, the oxygen main pipeline is provided with a cold oxygen shut-off valve, a cold oxygen venting pipeline, a cold oxygen regulating valve, an oxygen preheater, a first hot oxygen venting pipeline, a first hot oxygen shut-off valve, and a second hot oxygen venting pipeline in sequence along the oxygen delivery direction. The cold oxygen venting pipeline is provided with a cold oxygen venting valve, the first hot oxygen venting pipeline is provided with a first hot oxygen venting valve, and the second hot oxygen venting pipeline is provided with a second hot oxygen venting valve.

[0024] The advantages of adopting the above-mentioned further scheme are: not only can the pure oxygen supply be adjusted conveniently and accurately, but also the oxygen can be cut off and vented in time when the converter is shut down by interlock, ensuring the safety and reliability of the converter operation.

[0025] Furthermore, each of the oxygen branch lines is equipped with a second hot oxygen shut-off valve, and each of the protective steam branch lines is equipped with a protective steam regulating valve. Attached Figure Description

[0026] Figure 1 This is a schematic diagram of the internal structure of the multi-burner self-heating converter of this utility model; Figure 2 for Figure 1 Enlarged structural diagram of section A in the middle; Figure 3 This is a top view of the multi-burner self-heating converter of this utility model. Figure 4This is a top view of the distributor of this utility model; Figure 5 This is a cross-sectional view of the distributor of this utility model; Figure 6 This is a schematic diagram of the conversion system of this utility model; Figure 7 This is a cloud map showing the flame shape and temperature distribution of Test Example 1 of this utility model; Figure 8 This is a cloud map showing the flame shape and temperature distribution of Test Example 2 of this utility model; Figure 9 This is a cloud map showing the flame shape and temperature distribution of Test Example 3 of this utility model.

[0027] The attached diagram lists the components represented by each number as follows: 1. Furnace body; 11. Raw material gas inlet; 12. Converted gas outlet; 13. Water-cooled jacket; 14. Cooling water inlet; 15. Steam exhaust port; 16. Refractory lining; 17. Catalyst bed; 2. Burner; 3. Distributor; 31. First plate; 32. Second plate; 33. First through hole; 34. Second through hole; 35. Third through hole; 4. Raw material gas pipeline; 5. Converter gas pipeline; 6. Protect the main steam pipeline; 61. Protect the branch steam pipelines; 62. Protect the steam regulating valves; 7. Main oxygen pipeline; 71. Branch oxygen pipeline; 72. Cold oxygen shut-off valve; 73. Cold oxygen vent pipeline; 74. Cold oxygen regulating valve; 75. Oxygen preheater; 76. First hot oxygen vent pipeline; 77. First hot oxygen shut-off valve; 78. Second hot oxygen vent pipeline; 79. Cold oxygen vent valve; 790. First hot oxygen vent valve; 791. Second hot oxygen vent valve; 792. Second hot oxygen shut-off valve; 8. Cooling water pipeline; 81. Cooling water regulating valve. Detailed Implementation

[0028] The principles and features of this utility model are described below. The examples given are only for explaining this utility model and are not intended to limit the scope of this utility model.

[0029] Example 1 like Figures 1-3As shown, this embodiment of a multi-burner self-heating converter includes a furnace body 1 and at least two burners 2. The furnace body 1 contains a catalyst bed 17. A raw material gas inlet 11 is located on the upper side wall of the furnace body 1, and a conversion gas outlet 12 is located on the lower side wall of the furnace body 1. At least two burners 2 are evenly arranged in a circular pattern and fixed to the top of the furnace body 1. The lower ends of the burners 2 are close together, and the central axes of all burners 2 intersect the central axis of the furnace body 1 at the same point. The angle between the central axes of the burners 2 and the central axis of the furnace body 1 is 1° to 10°. The distance between the lower end of each burner 2 and the catalyst bed 17 is 4 to 6 meters. The central axes of all burners intersect the central axis of the furnace body at a single point, and the angle of the burners 2 is set to ensure a compact furnace flame that does not lick the furnace wall. By rationally determining the distance between the burner and the catalyst bed based on the feed gas throughput, sufficient combustion and mixing space can be ensured in the combustion section of the converter, avoiding damage caused by flame licking the catalyst. This ensures efficient operation of the converter while reasonably controlling equipment manufacturing costs.

[0030] In this embodiment, at least two burners 2 are evenly arranged in a circular pattern on the top of the furnace body 1, which can effectively improve the processing capacity of a single furnace body, and the load adjustment is also very flexible. The number of burners 2 can be determined according to the raw material processing volume, and can be set from 2 to 6; for example, if the raw material gas is coke oven gas, each burner can process 30,000 to 40,000 cubic meters of raw material gas; if the raw material gas is natural gas, the converter in this embodiment can be used as a two-stage furnace, and each burner can process 10,000 to 15,000 cubic meters of raw material gas.

[0031] like Figure 1 As shown, the outer wall of the furnace body 1 in this embodiment is provided with a water-cooled jacket 13, and the water-cooled jacket 13 is provided with a cooling water inlet 14 and a steam outlet 15; the inner wall of the furnace body 1 is provided with a refractory lining 16.

[0032] The multi-burner self-heating converter of this embodiment has the advantages of large single furnace processing capacity, high material mixing uniformity, uniform furnace temperature distribution, flexible load adjustment, and long burner service life. This embodiment can effectively solve the related technical problems of large-scale ATR converter.

[0033] Example 2 Based on Example 1, this example provides a preferred structure for the furnace body 1. For example... Figure 1 , Figure 2 , Figure 4 and Figure 5As shown, in this embodiment, a horizontally arranged distributor 3 is provided inside the furnace body 1. The distributor 3 is fixed on the inner wall of the furnace body 1 below the raw material gas inlet 11, and the lower end of the burner 2 passes through the distributor 3. By setting a horizontally arranged distributor inside the furnace body, the raw material gas can be uniformly distributed in both the axial and radial directions of the furnace chamber.

[0034] like Figure 4 and Figure 5 As shown, in a further preferred embodiment, the distributor 3 is a cylindrical shell structure. A first plate 31 and a second plate 32 are respectively provided at both ends of the distributor 3 along its axial direction. The first plate 31 and the second plate 32 are arranged at intervals. The first plate 31 has multiple first through holes 33, and the second plate 32 has multiple second through holes 34. The multiple first through holes 33 and the multiple second through holes 34 are staggered along the axial direction of the distributor 3. The diameter of the first through holes 33 is 5mm to 20mm, and the diameter of the second through holes 34 is 5mm to 20mm. The distributor 3 also has multiple third through holes 35 for the burner 2 to pass through.

[0035] The burner is equipped with a distributor, which adopts a hollow cylindrical structure. Several through holes are set at the upper and lower ends of the distributor, and the upper and lower through holes are offset at a certain angle. This structure allows the feed gas to be rectified at the upper end of the distributor after entering the converter, and then rectified again at the lower end of the distributor after entering the inner cavity of the distributor. The feed gas can be evenly distributed in both the axial and radial directions of the furnace, and the temperature distribution of the process gas entering the catalyst bed is very uniform.

[0036] Example 3 Based on Example 1 or Example 2, this embodiment provides a preferred setting for the distance between the burner 2 and the catalyst bed 17. When the number of burners 2 is no more than 3, the distance between the lower end of the burner 2 and the catalyst bed 17 is 4-5 m; when the number of burners 2 is greater than 3, the distance between the lower end of the burner 2 and the catalyst bed 17 is 5-6 m. By rationally determining the number of burners and the distance between the burners and the catalyst bed according to the feed gas processing volume, sufficient combustion and mixing space in the combustion section of the converter can be ensured, preventing damage caused by flame licking the catalyst. This ensures efficient operation of the converter while reasonably controlling equipment manufacturing costs.

[0037] Example 4 This embodiment provides a conversion system, such as Figure 6As shown, the multi-burner self-heating converter, as described above, also includes a raw material gas pipeline 4, a converter gas pipeline 5, a protective steam main pipeline 6, an oxygen main pipeline 7, protective steam branch pipelines 61, and oxygen branch pipelines 71. The oxygen main pipeline 7 is connected to and communicates with the upper ends of at least two burners 2 through at least two oxygen branch pipelines 71. The protective steam main pipeline 6 is connected to and communicates with at least two protective steam branch pipelines 61 respectively. The at least two protective steam branch pipelines 61 are connected to and communicate with at least two oxygen branch pipelines 71 in a one-to-one correspondence. The raw material gas pipeline 4 is connected to and communicates with the raw material gas inlet 11, and the converter gas pipeline 5 is connected to and communicates with the converter gas outlet 12.

[0038] Specifically, such as Figure 6 As shown, the main oxygen pipeline 7 is sequentially equipped with a cold oxygen shut-off valve 72, a cold oxygen venting pipeline 73, a cold oxygen regulating valve 74, an oxygen preheater 75, a first hot oxygen venting pipeline 76, a first hot oxygen shut-off valve 77, and a second hot oxygen venting pipeline 78 along the oxygen delivery direction. The cold oxygen venting pipeline 73 is equipped with a cold oxygen venting valve 79, the first hot oxygen venting pipeline 76 is equipped with a first hot oxygen venting valve 790, and the second hot oxygen venting pipeline 78 is equipped with a second hot oxygen venting valve 791. Each oxygen branch pipeline 71 is equipped with a second hot oxygen shut-off valve 792, and each protective steam branch pipeline 61 is equipped with a protective steam regulating valve 62. By setting up these pipelines and valves, not only can the pure oxygen delivery rate be conveniently and accurately adjusted, but also, in the event of a converter interlock shutdown, the oxygen can be promptly shut off and vented, ensuring the safety and reliability of the converter operation.

[0039] Optionally, the raw material flow velocity in the combustion reaction section of the furnace body 1 is 2~4m / s, and the oxygen flow velocity in the burner 2 is 60~150m / s. Preferably, when the raw gas in the raw gas pipeline 4 is coke oven gas or carbon-rich gas, the flow velocity of the raw gas in the combustion reaction section of the furnace body 1 is 2.5~3.5 m / s; when the raw gas in the raw gas pipeline 4 is natural gas, the flow velocity of the raw gas in the combustion reaction section of the furnace body 1 is 3~4 m / s; when the number of burners 2 is no more than 3, the oxygen flow velocity in the burners 2 is 100~140 m / s, for example 100 m / s, 105 m / s, 110 m / s, 115 m / s, 120 m / s, 125 m / s, 130 m / s, 135 m / s, 140 m / s; when the number of burners 2 is more than 3, the oxygen flow velocity in the burners 2 is 80~100 m / s, for example 80 m / s, 85 m / s, 90 m / s, 95 m / s, 100 m / s. Based on the amount of raw gas processed, parameters such as the number of burners and burner flow rate can be reasonably determined, which can ensure that the combustion section of the converter has sufficient combustion and mixing space, avoid damage caused by flame licking the catalyst, ensure the converter works efficiently, and at the same time, the equipment manufacturing cost can be reasonably controlled.

[0040] Specifically, such as Figure 6 As shown, in this embodiment, the cooling water inlet 14 on the water-cooled jacket 13 is connected to and communicates with the cooling water pipeline 8, and the cooling water pipeline 8 is provided with a cooling water regulating valve 81.

[0041] The conversion system in this embodiment can rationally determine parameters such as the number of burners, burner flow rate, and distance between the burners and the catalyst bed based on the feed gas throughput. This ensures sufficient combustion and mixing space in the combustion section of the converter, preventing damage caused by flame licking at the catalyst. This guarantees efficient operation of the converter while effectively controlling equipment manufacturing costs. By rationally determining the technical characteristics between the furnace diameter, number of burners, burner flow rate, and feed gas throughput, the conversion system in this embodiment guides the converter design process and minimizes equipment manufacturing costs.

[0042] The conversion method using the aforementioned conversion system includes the following steps: S1, raw gas is introduced into the furnace through raw gas pipeline 4. The introduction of raw gas is carried out in accordance with the normal operating procedure of the converter. S2, before oxygen is introduced, protective steam is introduced through the main protective steam pipeline 6 and the protective steam branch pipeline 61 to ensure that the protective steam flow rate in each protective steam branch pipeline 61 is more than 500 kg / h, and the burner 2 is purged. S3, prepare for oxygen injection operation. Confirm that the vent valve on the main oxygen pipeline 7 is fully closed and the shut-off valve is fully open. Inject oxygen into the furnace body 1 through the main oxygen pipeline 7 and the oxygen branch pipeline 71. Manually adjust the cold oxygen regulating valve on the main oxygen pipeline 7 to control the oxygen flow rate to 8%~12% of the preset flow rate, with 10% being optional. S4. Observe the temperature change at the gas outlet of furnace body 1. When the temperature rises slowly, it indicates that the ignition in furnace body 1 is successful. S5, after the preset time for successful ignition (e.g., 8~12 minutes, preferably 10 minutes), adjust the valve position of the protective steam regulating valve to reduce the protective steam flow rate in each protective steam branch pipeline 61 to 10% of the initial flow rate; S6, according to the reformer's set operating procedure, increases the flow rate of raw material gas and oxygen to perform load increase operation.

[0043] In this embodiment, if the converter is shut down by interlock during start-up or operation, all shut-off valves on the main oxygen pipeline and oxygen branch pipelines will be closed quickly and simultaneously to ensure rapid oxygen isolation; the vent valve on the main oxygen pipeline will be opened quickly and simultaneously to ensure rapid release of residual oxygen; and the protective steam regulating valve will automatically adjust the valve opening to ensure that the steam flow rate on each branch is not less than 500 kg / h.

[0044] The conversion method in this embodiment can effectively solve the related technical problems of large-scale ATR converters, and has the advantages of high material mixing uniformity, uniform furnace temperature distribution, flexible load adjustment, and long burner service life.

[0045] Experimental Example 1 This experimental example uses the conversion system and method of Example 4. The feed gas used in this experimental example is coke oven gas, and the composition of the feed gas is shown in Table 1. The composition of the generated converted gas is shown in Table 2.

[0046] Table 1. Components of the Feed Gas Table 2. Components of Converted Gas In this experimental example, the feed gas flow rate was 60000 Nm³. 3 / h, the inner diameter of the combustion reaction section of the furnace body is 1200mm, the distance from the burner to the catalyst bed is 4.5m, and the number of burners is 2.

[0047] like Figure 7 As shown in the figure, CFD simulation of actual working conditions reveals that the furnace flame is compact, and the furnace wall temperature is around 1600K, meeting the design requirements of the refractory lining. The gas entering the catalyst bed has a uniform temperature distribution, ensuring the catalyst's service life and conversion efficiency.

[0048] Experimental Example 2 This experimental example uses the conversion system and method of Example 4. The composition of the feed gas and the composition of the generated converted gas in this experimental example are the same as those in Tables 1 and 2 of Experiment 1.

[0049] In this experimental example, the feed gas flow rate was 100,000 Nm³. 3 / h, the inner diameter of the combustion reaction section of the furnace body is 1330mm, the distance from the burner to the catalyst bed is 4.8m, and the number of burners is 3.

[0050] like Figure 8 As shown in the figure, CFD simulation of actual working conditions reveals that the furnace flame is compact, and the furnace wall temperature is around 1600K, meeting the design requirements of the refractory lining. The gas entering the catalyst bed has a uniform temperature distribution, ensuring the catalyst's service life and conversion efficiency.

[0051] Experimental Example 3 This experimental example uses the conversion system and method of Example 4. The feed gas used in this experimental example is coke oven gas, and the composition of the feed gas is shown in Table 3. The composition of the generated converted gas is shown in Table 4.

[0052] Table 3. Raw material gas composition table Table 4. Components of Converted Gas In this experimental example, the feed gas flow rate was 35000 Nm³. 3 / h, the inner diameter of the combustion reaction section of the furnace body is 1500mm, the distance from the burner to the catalyst bed is 5m, and the number of burners is 3.

[0053] like Figure 9 As shown in the figure, CFD simulation of actual working conditions reveals a compact furnace flame and a furnace wall temperature of approximately 1700K, meeting the design requirements for the refractory lining. The uniform temperature distribution of the gas entering the catalyst bed ensures the catalyst's lifespan and conversion efficiency.

[0054] In the description of this utility model, it should be understood that the terms "center", "upper", "lower", "horizontal", "top", "bottom", "inner", "outer", "axial", "radial", 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 utility model 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 utility model.

[0055] 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 indicated technical features. Thus, a feature defined as "first" or "second" may explicitly or implicitly include at least one of that feature. In the description of this utility model, "a plurality of" means at least two, such as two, three, etc., unless otherwise explicitly specified.

[0056] In this utility model, unless otherwise explicitly specified and limited, the terms "installation," "connection," "joining," 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 utility model according to the specific circumstances.

[0057] In this utility model, 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," "on top of," and "over" 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.

[0058] 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.

[0059] 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 multi-burner self-heating converter, characterized in that, The furnace includes a furnace body and at least two burners. The furnace body contains a catalyst bed. The upper side wall of the furnace body has a raw material gas inlet, and the lower side wall of the furnace body has a conversion gas outlet. The at least two burners are evenly arranged in a circular pattern and fixed to the top of the furnace body. The lower ends of the burners are close to each other. The central axes of all burners intersect the central axis of the furnace body at the same point. The angle between the central axes of the burners and the central axis of the furnace body is 1° to 10°. The distance between the lower end of the burner and the catalyst bed is 4 to 6 m.

2. The multi-burner self-heating converter according to claim 1, characterized in that, The furnace body is equipped with a horizontally arranged distributor, which is fixed on the inner side wall of the furnace body below the raw material gas inlet, and the lower end of the burner is arranged through the distributor.

3. The multi-burner self-heating converter according to claim 2, characterized in that, The distributor is a cylindrical shell structure. The distributor has a first plate and a second plate at its two ends along the axial direction. The first plate and the second plate are arranged at intervals. The first plate has a plurality of first through holes and the second plate has a plurality of second through holes. The plurality of first through holes and the plurality of second through holes are staggered along the axial direction of the distributor.

4. The multi-burner self-heating converter according to claim 3, characterized in that, The diameter of the first through hole is 5mm to 20mm, and the diameter of the second through hole is 5mm to 20mm.

5. A multi-burner self-heating converter according to any one of claims 1 to 4, characterized in that, When the number of burners is no more than 3, the distance between the lower end of the burner and the catalyst bed is 4-5m; when the number of burners is more than 3, the distance between the lower end of the burner and the catalyst bed is 5-6m.

6. A multi-burner self-heating converter according to any one of claims 1 to 4, characterized in that, The outer wall of the furnace body is provided with a water-cooled jacket, and the water-cooled jacket is provided with a cooling water inlet and a steam outlet.

7. A multi-burner self-heating converter according to any one of claims 1 to 4, characterized in that, The inner wall of the furnace body is provided with a refractory lining.

8. A conversion system, characterized in that, The multi-burner self-heating converter according to any one of claims 1 to 7 further includes a raw material gas pipeline, a converter gas pipeline, a protective steam main pipeline, an oxygen main pipeline, protective steam branch pipelines, and oxygen branch pipelines. The oxygen main pipeline is connected to and communicates with the upper ends of the at least two burners through at least two oxygen branch pipelines. The protective steam main pipeline is connected to and communicates with at least two protective steam branch pipelines respectively. The at least two protective steam branch pipelines are connected to and communicate with at least two oxygen branch pipelines in a one-to-one correspondence. The raw material gas pipeline is connected to and communicates with the raw material gas inlet, and the converter gas pipeline is connected to and communicates with the converter gas outlet.

9. The conversion system according to claim 8, characterized in that, The oxygen main pipeline is provided with a cold oxygen shut-off valve, a cold oxygen venting pipeline, a cold oxygen regulating valve, an oxygen preheater, a first hot oxygen venting pipeline, a first hot oxygen shut-off valve, and a second hot oxygen venting pipeline in sequence along the oxygen delivery direction. The cold oxygen venting pipeline is equipped with a cold oxygen venting valve, the first hot oxygen venting pipeline is equipped with a first hot oxygen venting valve, and the second hot oxygen venting pipeline is equipped with a second hot oxygen venting valve.

10. The conversion system according to claim 9, characterized in that, Each of the oxygen branch lines is equipped with a second hot oxygen shut-off valve, and each of the protective steam branch lines is equipped with a protective steam regulating valve.

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