Multi-burner self-heating type conversion furnace, conversion system and conversion method

Abstract

The invention relates to a multi-burner self-heating reformer, a reformer system and a reformer method.The multi-burner self-heating reformer comprises a reformer body and at least two burners, a catalyst bed layer is arranged in the reformer body, a feed gas inlet is formed in the side wall of the upper portion of the reformer body, and a reformed gas outlet is formed in the side wall of the lower portion of the reformer body; the at least two burners are uniformly distributed in a circumferential shape and are fixed at the top of the furnace body in a penetrating manner, the lower ends of the burners are close to each other, the central axes of all the burners and the central axis of the furnace body are intersected at the same point, the included angle between the central axis of each burner and the central axis of the furnace body is 1-10 degrees, and the included angle between the central axis of each burner and the central axis of the furnace body is 1-10 degrees. And the distance between the lower end of the burner and the catalyst bed layer is 4-6m. The multi-burner self-heating type reformer has the advantages of being large in single-furnace processing capacity, high in material mixing uniformity, uniform in hearth temperature distribution, flexible in load adjustment, long in service life of the burners and the like, and the related technical problem of large-scale ATR reformer can be effectively solved.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of reformer, in particular to a multi-burner self-heating reformer, a reforming system and a reforming method. BACKGROUND

[0002] ATR is the abbreviation of Autothermal Reformer, and in recent years, ATR technology has been widely used in large-scale methanol, ammonia and hydrogen production devices, and is suitable for producing effective gas CO and H2 from natural gas, coke oven gas, rich methane gas and other gaseous hydrocarbons (methane content from 10% to 100%).

[0003] Under certain temperature and pressure conditions, gaseous hydrocarbons and pure oxygen sprayed through the burner mainly occur combustion exothermic reaction in the upper part of the reformer to provide heat for the catalytic conversion of methane; the lower part of the reformer is equipped with a catalyst, and the methane and water vapor in the raw material gas occur self-heating conversion reaction under the action of the catalyst.

[0004] The partial oxidation reaction occurring in the upper part of the reformer is as follows: CH4+ 2O2 CO + 2H2 △H=﹣35.7KJ / mol; H2+ 1 / 2O2 H2O △H=﹣241.6KJ / mol. The catalytic conversion reaction occurring in the lower part of the reformer is as follows: CH4+ H2O

[0005] CO + 3H2 △H=206.3KJ / mol; CO + H2O CO2+ H2 △H=﹣41.3KJ / mol. The burner has a huge impact on the reaction effect in the reformer and is one of the core equipment. The existing ATR reformer is only provided with a single top burner, and the processing capacity is limited. When processing a large amount of raw material gas, problems such as uneven mixing of raw material gas and oxygen, uneven distribution of furnace temperature, local overheating of the burner causing ablation, and the like may occur, and the long flame also seriously affects the working life of the catalyst.

[0006] The burner has a huge impact on the reaction effect in the reformer and is one of the core equipment. The existing ATR reformer is only provided with a single top burner, and the processing capacity is limited. When processing a large amount of raw material gas, problems such as uneven mixing of raw material gas and oxygen, uneven distribution of furnace temperature, local overheating of the burner causing ablation, and the like may occur, and the long flame also seriously affects the working life of the catalyst.

[0007] ​In order to improve the processing capacity of the converter, using multiple burners is an ideal technical direction. The working condition of the multi-burner converter is different from that of the single-burner, and the technical problems to be solved are: 1. After using multiple burners, the diameter of the flame is increased, the working temperature of the furnace wall of the conversion furnace reaction section is increased greatly, and the refractory bricks cannot withstand high temperature and crack. 2. In order to improve the service life of the refractory bricks, the diameter of the furnace is increased while the aluminum content of the refractory bricks is increased, so that the actual working temperature of the furnace wall is reduced by reducing the distance between the flame surface and the furnace wall. But this design brings new problems, because the diameter of the furnace is increased, the flow rate of the raw material gas in the furnace is reduced, the mixing efficiency of the raw material gas and oxygen is reduced, the flame is lengthened, and the temperature distribution of the conversion gas entering the catalyst bed is very uneven, which seriously affects the service life of the catalyst and the catalytic conversion efficiency. SUMMARY

[0008] In order to solve one or several technical problems existing in the prior art, a multi-burner self-heating converter, a conversion system and a conversion method are provided, which can reasonably determine the technical characteristics between the furnace diameter, the number of burners, the burner flow rate and the raw material gas processing capacity, thereby guiding the design work of the converter and maximizing the production cost of the equipment.

[0009] The technical scheme for solving the above technical problems is as follows: the present application provides a multi-burner self-heating converter, comprising a furnace body and at least two burners, the furnace body is provided with a catalyst bed, the upper side wall of the furnace body is provided with a raw material gas inlet, and the lower side wall of the furnace body is provided with a conversion gas outlet; at least two burners are uniformly arranged in a circular manner and fixed on the top of the furnace body, the lower ends of the burners are close to each other, the center axes of all burners and the center axis of the furnace body intersect at the same point, the included angle between the center axis of the burner and the center axis of the furnace body is 1°-10°, and the distance between the lower end of the burner and the catalyst bed is 4-6m.

[0010] The multi-burner self-heating converter of the present application has the advantages of large single furnace processing capacity, high material mixing uniformity, uniform furnace temperature distribution, flexible load adjustment, long service life of the burner, etc., and can effectively solve the related technical problems of large-scale ATR converter.

[0011] On the basis of the above technical scheme, the present application can also be improved as follows.

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

[0013] The beneficial effect of the further scheme is that the raw material gas can be uniformly distributed in the axial and radial directions of the hearth of the furnace body by arranging the horizontally arranged distributor in the furnace body.

[0014] Further, the distributor is a cylindrical shell structure, and the two ends of the distributor in the axial direction are respectively provided with a first plate body and a second plate body, the first plate body and the second plate body are arranged in a spaced manner, a plurality of first through holes are formed in the first plate body, a plurality of second through holes are formed in the second plate body, and the plurality of first through holes and the plurality of second through holes are arranged in a staggered manner in the axial direction of the distributor. The diameter of the first through hole is 5mm-20mm, and the diameter of the second through hole is 5mm-20mm.

[0015] The beneficial effect of the further scheme is that the burner is provided with a distributor, the distributor adopts a cylindrical hollow structure, a plurality of through holes are arranged at the upper end and the lower end of the distributor, the through holes at the upper end and the lower end are staggered at a certain angle, this structure can make the raw material gas enter the reformer first pass through the upper end of the distributor for rectification, then pass through the lower end of the distributor for rectification again after entering the inner cavity of the distributor, and the raw material gas can be uniformly distributed in the axial and radial directions of the hearth, and the temperature distribution of the process gas entering the catalyst bed is very uniform.

[0016] Further, when the number of the burners is not more than 3, the distance between the lower end of the burner and the catalyst bed is 4-5m; when the number of the burners is more than 3, the distance between the lower end of the burner and the catalyst bed is 5-6m.

[0017] The beneficial effect of the further scheme is that according to the raw material gas treatment capacity, the number of burners, the distance between the burners and the catalyst bed and other parameters are reasonably determined, which can ensure that the combustion and mixing space of the combustion section of the reformer is sufficient, avoid the damage of the catalyst caused by the flame licking, ensure the efficient working of the reformer, and reasonably control the production cost of the equipment.

[0018] Further, a water cooling jacket is arranged on the outer side wall of the furnace body, and a cooling water inlet and a steam discharge port are arranged on the water cooling jacket; a refractory lining is arranged on the inner side wall of the furnace body.

[0019] The application further provides a conversion system, comprising a multi-burner self-heating converter as described above, and further comprising a raw material gas pipeline, a conversion gas pipeline, a protective steam main pipeline, an oxygen main pipeline, a protective steam branch pipeline and an oxygen branch pipeline, the oxygen main pipeline being connected and communicated with the upper ends of the at least two burners through the at least two oxygen branch pipelines, the protective steam main pipeline being connected and communicated with the at least two protective steam branch pipelines respectively, and the at least two protective steam branch pipelines being connected and communicated with the at least two oxygen branch pipelines one by one; the raw material gas pipeline being connected and communicated with the raw material gas inlet, and the conversion gas pipeline being connected and communicated with the conversion gas outlet.

[0020] The conversion system of the application can reasonably determine the number of burners, the flow rate of burners, the distance between burners and catalyst bed and other parameters according to the raw material gas processing capacity, can ensure sufficient combustion and mixing space in the combustion section of the converter, avoid damage caused by flame licking the catalyst, ensure efficient operation of the converter and reasonably control the production and manufacturing cost of the equipment.

[0021] Further, the oxygen main pipeline is sequentially provided with a cold oxygen cut-off valve, a cold oxygen vent pipeline, a cold oxygen regulating valve, an oxygen preheater, a first hot oxygen vent pipeline, a first hot oxygen cut-off valve and a second hot oxygen vent pipeline along the oxygen conveying direction, the cold oxygen vent pipeline is provided with a cold oxygen vent valve, the first hot oxygen vent pipeline is provided with a first hot oxygen vent valve, and the second hot oxygen vent pipeline is provided with a second hot oxygen vent valve; each of the oxygen branch pipelines is provided with a second hot oxygen cut-off valve, and each of the protective steam branch pipelines is provided with a protective steam regulating valve.

[0022] The above further scheme has the beneficial effect that not only can the pure oxygen conveying amount be conveniently and accurately adjusted, but also the oxygen can be timely cut off and vented when the converter is interlocked and stopped, thereby ensuring the safety and reliability during operation of the converter.

[0023] Further, the raw material gas flow rate in the combustion reaction section furnace of the furnace body is 2-4 m / s, and the oxygen flow rate in the burners is 60-150 m / s.

[0024] Further, when the raw material gas in the raw material gas pipeline is coke oven gas or carbon-rich gas, the raw material gas flow rate in the combustion reaction section furnace of the furnace body is 2.5-3.5 m / s; when the raw material gas in the raw material gas pipeline is natural gas, the raw material gas flow rate in the combustion reaction section furnace of the furnace body is 3-4 m / s. When the number of the burners is not more than 3, the oxygen flow rate in the burners is 100-140 m / s; when the number of the burners is more than 3, the oxygen flow rate in the burners is 80-100 m / s.

[0025] The beneficial effect of the further scheme is that the number of burners, the flow rate of the burners and other parameters can be reasonably determined according to the raw gas processing capacity, the combustion and mixing space of the conversion furnace combustion section can be ensured, the catalyst damage caused by flame licking can be avoided, the efficient working of the conversion furnace can be ensured, and the production cost of the equipment is reasonably controlled.

[0026] The application further provides a conversion method, which is realized by using the conversion system. S1, feeding raw gas into the furnace body through a raw gas pipeline; S2, before oxygen feeding, protection steam is fed through a protection steam main pipeline and protection steam branch pipelines to ensure that the protection steam flow rate in each protection steam branch pipeline is above 500 kg / h, and the burners are purged; S3, preparing for oxygen feeding operation, oxygen is fed into the furnace body through an oxygen main pipeline and oxygen branch pipelines, and the oxygen flow rate is controlled to be 8%-12% of the preset flow rate; S4, observing the temperature change at the conversion gas outlet of the furnace body, and when the temperature slowly rises, it indicates that the ignition in the furnace body is successful; S5, after a preset time of successful ignition, the protection steam flow rate in each protection steam branch pipeline is reduced to 10% of the initial flow rate; S6, according to the set operation process of the conversion furnace, the raw gas flow rate and the oxygen flow rate are increased to perform load increasing operation.

[0027] The conversion method has the advantages that the technical problems of ATR conversion furnace large-scale can be effectively solved, the material mixing uniformity is high, the furnace temperature distribution is uniform, the load regulation is flexible, the service life of the burners is long and the like. BRIEF DESCRIPTION OF DRAWINGS

[0028] Figure 1 Fig. 1 is a schematic view of the internal structure of the multi-burner self-heating conversion furnace of the application; Figure 2 Fig. 3 is a schematic view of the enlarged structure of the A part in Fig. 2; Figure 1 Figure 3 Fig. 5 is a schematic view of the top structure of the multi-burner self-heating conversion furnace of the application; Figure 4 Fig. 7 is a schematic view of the top structure of the distributor of the application; Figure 5 Fig. 9 is a schematic view of the sectional structure of the distributor of the application; Figure 6 ​A structural schematic diagram of the conversion system of the present application; Figure 7 A flame shape and temperature distribution nephogram of Test Example 1 of the present application; Figure 8 A flame shape and temperature distribution nephogram of Test Example 2 of the present application; Figure 9 A flame shape and temperature distribution nephogram of Test Example 3 of the present application.

[0029] In the drawings, the components represented by the respective reference numerals are listed as follows: 1, furnace body; 11, raw material gas inlet; 12, conversion gas outlet; 13, water cooling jacket; 14, cooling water inlet; 15, steam discharge port; 16, refractory lining; 17, catalyst bed; 2, burner; 3, distributor; 31, first plate body; 32, second plate body; 33, first through hole; 34, second through hole; 35, third through hole; 4, raw material gas pipeline; 5, conversion gas pipeline; 6, protective steam main pipeline; 61, protective steam branch pipeline; 62, protective steam regulating valve; 7, oxygen main pipeline; 71, oxygen branch pipeline; 72, cold oxygen cut-off valve; 73, cold oxygen venting pipeline; 74, cold oxygen regulating valve; 75, oxygen preheater; 76, first hot oxygen venting pipeline; 77, first hot oxygen cut-off valve; 78, second hot oxygen venting pipeline; 79, cold oxygen venting valve; 790, first hot oxygen venting valve; 791, second hot oxygen venting valve; 792, second hot oxygen cut-off valve; 8, cooling water pipeline; 81, cooling water regulating valve. DETAILED DESCRIPTION

[0030] The principles and features of the present application are described below, and the examples are only used to explain the present application and are not intended to limit the scope of the present application.

[0031] Example 1 As Figures 1-3As shown, the multi-burner self-heating reformer of the embodiment comprises a furnace body 1 and at least two burners 2, the furnace body 1 is internally provided with a catalyst bed 17, the furnace body 1 is provided with a raw material gas inlet 11 on the upper side wall, and is provided with a reforming gas outlet 12 on the lower side wall; the at least two burners 2 are uniformly arranged in a circular manner and are fixedly arranged on the top of the furnace body 1, the lower ends of the burners 2 are close to each other, the central axes of all the burners 2 and the central axis of the furnace body 1 intersect at the same point, the included angle between the central axes of the burners 2 and the central axis of the furnace body 1 is 1°-10°, and the distance between the lower ends of the burners 2 and the catalyst bed 17 is 4-6 m. The central axes of all the burners and the central axis of the furnace body intersect at a point, and the angle of the burners 2 is set, which can ensure that the furnace flame is compact and does not lick the furnace wall. According to the raw material gas treatment capacity, the distance between the burners and the catalyst bed is reasonably determined, which can ensure that the combustion and mixing space of the reformer combustion section is sufficient, avoid the damage of the flame licking the catalyst, ensure the efficient working of the reformer, and reasonably control the equipment production cost.

[0032] The at least two burners 2 of the embodiment are uniformly arranged in a circular manner on the top of the furnace body 1, which can effectively improve the treatment 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 treatment capacity, and can be 2-6; for example, if the raw material gas is coke oven gas, the raw material gas treatment capacity of each burner is 30000-40000 m3; if the raw material gas is natural gas, the reformer of the embodiment can be used as a two-stage furnace, and the raw material gas treatment capacity of each burner is 10000-15000 m3.

[0033] As shown in Figure 1 , the outer side wall of the furnace body 1 is provided with a water cooling jacket 13, the water cooling jacket 13 is provided with a cooling water inlet 14 and a steam discharge port 15; the inner side wall of the furnace body 1 is provided with a refractory lining 16.

[0034] The multi-burner self-heating reformer of the embodiment has the advantages of large single furnace treatment capacity, high material mixing uniformity, uniform furnace temperature distribution, flexible load adjustment, long service life of the burner, etc., and can effectively solve the related technical problems of the large-scale ATR reformer.

[0035] Embodiment 2 On the basis of embodiment 1, the embodiment provides a preferred structure of the furnace body 1. As shown in Figure 1 , Figure 2 , Figure 4 and Figure 5As shown, the furnace body 1 of the embodiment is provided with a horizontally arranged distributor 3 fixed on the inner side wall of the furnace body 1 below the raw material gas inlet 11, and the lower end of the burner 2 is arranged through the distributor 3. By arranging the horizontally arranged distributor in the furnace body, the raw material gas can be uniformly distributed in the furnace hearth in the axial and radial directions.

[0036] As shown in Figure 4 and Figure 5 Further preferably, the distributor 3 is a cylindrical shell structure, the two ends of the distributor 3 are respectively provided with a first plate body 31 and a second plate body 32, the first plate body 31 and the second plate body 32 are arranged in a spaced manner, a plurality of first through holes 33 are formed on the first plate body 31, a plurality of second through holes 34 are formed on the second plate body 32, and the plurality of first through holes 33 and the plurality of second through holes 34 are arranged in a staggered manner in the axial direction of the distributor 3; the diameter of the first through hole 33 is 5mm-20mm, and the diameter of the second through hole 34 is 5mm-20mm. A plurality of third through holes 35 for the burner 2 to pass through are formed on the distributor 3.

[0037] The burner is provided with a distributor, the distributor adopts a cylindrical hollow structure, a plurality of through holes are arranged on the upper end and the lower end of the distributor, and the through holes on the upper end and the lower end are staggered at a certain angle. This structure can make the raw material gas enter the reformer first pass through the upper end of the distributor for rectification, and then pass through the lower end of the distributor for rectification again after entering the inner cavity of the distributor. The raw material gas can be uniformly distributed in the axial and radial directions of the furnace hearth, and the temperature distribution of the process gas entering the catalyst bed is very uniform.

[0038] Embodiment 3 On the basis of embodiment 1 or embodiment 2, the embodiment provides a preferred setting mode of the distance between the burner 2 and the catalyst bed 17. When the number of the burners 2 is not more than 3, the distance between the lower end of the burner 2 and the catalyst bed 17 is 4-5m; when the number of the burners 2 is more than 3, the distance between the lower end of the burner 2 and the catalyst bed 17 is 5-6m. According to the raw material gas treatment capacity, the number of burners, the distance between the burners and the catalyst bed, and other parameters are reasonably determined, which can ensure that the combustion and mixing space of the reformer combustion section is sufficient, avoid the damage of the catalyst caused by flame licking, and ensure the efficient work of the reformer while reasonably controlling the equipment production cost.

[0039] Embodiment 4 The embodiment provides a reforming system, as shown in 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.

[0040] 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.

[0041] Optionally, the raw material gas flow velocity in the combustion reaction section of the furnace body 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 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 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.

[0042] 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.

[0043] 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.

[0044] Example 5 This embodiment provides a conversion method, implemented using a conversion system as described in Embodiment 4, including 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 injection, protective steam is first injected 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 to oxygen injection operation, confirm that the vent valve on the oxygen main pipeline 7 is fully closed, the cut-off valve is fully opened, oxygen is introduced into the furnace body 1 through the oxygen main pipeline 7 and the oxygen branch pipeline 71, the cold oxygen regulating valve on the oxygen main pipeline 7 is manually adjusted, and the oxygen flow is controlled to be 8% to 12% of the preset flow, and 10% is selected; S4, observe the temperature change at the conversion gas outlet of the furnace body 1, and when the temperature slowly rises, it indicates that the ignition in the furnace body 1 is successful; S5, after the ignition is successful for a preset time (for example, 8 to 12 minutes, preferably 10 minutes), the protection steam regulating valve position is adjusted, and the protection steam flow in each protection steam branch pipeline 61 is reduced to 10% of the initial flow; S6, according to the set operation process of the conversion furnace, the raw material gas flow and the oxygen flow are increased, and the load operation is performed.

[0045] In this embodiment, if the conversion furnace is interlocked to stop during start-up or operation, all the cut-off valves on the oxygen main pipeline and the oxygen branch pipeline are simultaneously and quickly closed to ensure rapid isolation of oxygen; the vent valve on the oxygen main pipeline is simultaneously and quickly opened to ensure rapid venting of residual oxygen; and the protection steam regulating valve automatically adjusts the valve opening degree to ensure that the steam flow in each branch is not less than 500 kg / h.

[0046] The conversion method of the embodiment can effectively solve the related technical problems of the large-scale ATR conversion furnace, and has the advantages of high material mixing uniformity, uniform furnace temperature distribution, flexible load adjustment, long service life of the burner, etc.

[0047] Test Example 1 The conversion method of Example 5 is used for testing in this test example. The raw material gas used in this test example is coke oven gas, and the raw material gas components are shown in Table 1, and the generated conversion gas components are shown in Table 2.

[0048] Table 1 Raw material gas component table Table 2 Conversion gas component table In this test example, the raw material gas flow is 60000 Nm 3 / h, the inner diameter of the combustion reaction section of the furnace body is 1200 mm, the distance from the burner to the catalyst bed is 4.5 m, and the number of burners is 2.

[0049] As Figure 7 shown, the actual working conditions are simulated by CFD, and from the furnace temperature distribution cloud picture, it can be seen that the furnace flame is compact, the furnace wall temperature is about 1600K, which meets the design requirements of the refractory lining. The gas temperature distribution entering the catalyst bed is uniform, which ensures the service life of the catalyst and the conversion efficiency.

[0050] Test Example 2 The test example was tested by using the conversion method of Example 5. The raw gas components and the generated conversion gas components of the test example are the same as Table 1 and Table 2 of Test Example 1.

[0051] In the test example, the raw gas flow rate was 100000 Nm 3 / h, the combustion reaction section inner diameter of the furnace body was 1330 mm, the burner to catalyst bed distance was 4.8 m, and the number of burners was 3.

[0052] As shown in Figure 8 , by simulating the actual working condition by CFD, it can be known from the furnace temperature distribution cloud picture that the furnace flame is compact, the furnace wall temperature is about 1600 K, which meets the design requirements of the refractory lining. The gas temperature distribution entering the catalyst bed is uniform, which ensures the service life of the catalyst and the conversion efficiency.

[0053] Test Example 3 The test example was tested by using the conversion method of Example 5. The raw gas of the test example was coke oven gas, the raw gas components were shown in Table 3, and the generated conversion gas components were shown in Table 4.

[0054] Table 3 Raw gas component table Table 4 Conversion gas component table In the test example, the raw gas flow rate was 35000 Nm 3 / h, the combustion reaction section inner diameter of the furnace body was 1500 mm, the burner to catalyst bed distance was 5 m, and the number of burners was 3.

[0055] As shown in Figure 9 , by simulating the actual working condition by CFD, it can be known from the furnace temperature distribution cloud picture that the furnace flame is compact, the furnace wall temperature is about 1700 K, which meets the design requirements of the refractory lining. The gas temperature distribution entering the catalyst bed is uniform, which ensures the service life of the catalyst and the conversion efficiency.

[0056] In the description of the present application, it should be understood that the orientation or positional relationship indicated by the terms "center", "upper", "lower", "horizontal", "top", "bottom", "inner", "outer", "axial", "radial" and the like is based on the orientation or positional relationship shown in the drawings, and is only for the convenience of describing the present application and simplifying the description, and therefore cannot be understood as indicating or implying that the device or element referred to must have a particular orientation, be constructed and operated in a particular orientation, and therefore cannot be understood as limiting the present application.

[0057] In addition, the terms "first", "second", etc. are used only for the purpose of description and do not imply or imply relative importance or imply the number of the technical features indicated. Therefore, the features defined as "first", "second" can explicitly or implicitly include at least one of the features. In the description of the present application, the meaning of "a plurality of" is at least two, such as two, three, etc., unless otherwise explicitly specified.

[0058] In the present application, unless otherwise explicitly specified and limited, the terms "mounting", "connecting", "connecting", "fixing" and the like should be understood broadly, for example, it can be fixedly connected, or it can be detachably connected, or it can be integrated; it can be directly connected, or it can be indirectly connected through an intermediate medium, it can be the internal communication of two elements or the interaction relationship of two elements, unless otherwise explicitly limited. For those skilled in the art, the specific meaning of the above terms in the present application can be understood according to the specific circumstances.

[0059] In the present application, unless otherwise explicitly specified and limited, the first feature is "on" or "under" the second feature. The first and second features can be in direct contact, or the first and second features can be indirectly contacted through an intermediate medium. Moreover, the first feature "above", "above" and "above" the second feature can be the first feature directly above or obliquely above the second feature, or only indicates that the first feature is higher than the second feature in horizontal height. The first feature "below", "below" and "below" the second feature can be the first feature directly below or obliquely below the second feature, or only indicates that the first feature is lower than the second feature in horizontal height.

[0060] In the description of the present application, the description of the terms "one embodiment", "some embodiments", "example", "specific example", or "some examples" means that the specific features, structures, materials or characteristics described in conjunction with the embodiment or example are included in at least one embodiment or example of the present application. In the present application, the illustrative description of the above terms is not necessarily for the same embodiment or example. Moreover, the specific features, structures, materials or characteristics described can be combined in any suitable manner in any one or more embodiments or examples. In addition, those skilled in the art can combine and combine different embodiments or features of different embodiments or examples described in the present application without contradiction.

[0061] Although the embodiments of the present application have been shown and described above, it can be understood that the above embodiments are exemplary and cannot be understood as limiting the present application, and those skilled in the art can make changes, modifications, replacements and variations to the above embodiments within the scope of the present application.

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 first plate and the 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. The diameter of the first through hole is 5mm to 20mm, and the diameter of the second through hole is 5mm to 20mm.

4. A multi-burner self-heating converter according to any one of claims 1 to 3, 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.

5. A multi-burner self-heating converter according to any one of claims 1 to 3, characterized in that, The outer wall of the furnace body is provided with a water-cooled jacket, which is provided with a cooling water inlet and a steam outlet; the inner wall of the furnace body is provided with a refractory lining.

6. A conversion system, characterized in that, The multi-burner self-heating converter, as described in any one of claims 1 to 5, 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 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.

7. The conversion system according to claim 6, characterized in that, The main oxygen pipeline is sequentially equipped 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 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. Each of the oxygen branch pipelines is equipped with a second hot oxygen shut-off valve, and each of the protective steam branch pipelines is equipped with a protective steam regulating valve.

8. The conversion system according to claim 6, characterized in that, The gas flow velocity of the raw material in the combustion reaction section of the furnace body is 2~4m / s, and the oxygen flow velocity in the burner is 60~150m / s.

9. The conversion system according to claim 8, characterized in that, When the raw gas in the raw gas pipeline is coke oven gas or carbon-rich gas, the flow velocity of the raw gas in the combustion reaction section of the furnace body is 2.5~3.5m / s; when the raw gas in the raw gas pipeline is natural gas, the flow velocity of the raw gas in the combustion reaction section of the furnace body is 3~4m / s. When the number of burners is no more than 3, the oxygen flow rate inside the burners is 100~140m / s; when the number of burners is more than 3, the oxygen flow rate inside the burners is 80~100m / s.

10. A conversion method, characterized in that, This is achieved using the conversion system described in any one of claims 6 to 9. Includes the following steps: S1, raw material gas is introduced into the furnace through the raw material gas pipeline; S2. Before oxygen injection, protective steam is first injected through the main protective steam pipeline and the protective steam branch pipelines to ensure that the protective steam flow rate in each protective steam branch pipeline is more than 500 kg / h, and the burner is purged. S3, prepare for oxygen injection operation, introduce oxygen into the furnace through the main oxygen pipeline and oxygen branch pipelines, and control the oxygen flow rate to 8%~12% of the preset flow rate; S4. Observe the temperature change at the gas outlet of the furnace body. When the temperature rises slowly, it indicates that the ignition in the furnace body is successful. S5, after a preset time for successful ignition, reduce the protective steam flow rate in each protective steam branch pipeline 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.

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