Preparation system of synthesis gas

Abstract

The utility model discloses a preparation system of synthesis gas. The synthesis gas preparation system comprises a non-return mixer, a converter, a waste heat boiler and a steam superheater which are connected in sequence; the non-return mixer comprises a T-shaped pipe and a spraying assembly, and the spraying assembly comprises an L-shaped spraying pipe formed by communicating a first spraying pipe section and a second spraying pipe section perpendicular to the first spraying pipe section; the second spray pipe section faces the converter; the converter comprises a reaction chamber and a nozzle chamber which are coaxially arranged, the nozzle chamber is arranged at the top of the reaction chamber, and a mixed gas inlet is formed in the side face of the nozzle chamber; a nozzle is arranged in the nozzle chamber, and the axis of the nozzle coincides with the axis of the nozzle chamber. The nozzle includes a first tube and a second tube. By adopting the system, the conversion rate of methane, tar and fly ash can be improved, and meanwhile, high-quality superheated steam can be produced as a byproduct.

Description

Technical Field

[0001] The utility model relates to a synthesis gas preparation system. Background Art

[0002] Biomass and urban garbage are important carbon-containing resources. They can be used as raw materials to produce synthesis gas through processes such as gasification and pyrolysis, and further processed into bulk chemicals such as ammonia, methanol, olefins, and liquid fuels, or converted into clean secondary energy such as hydrogen. However, due to the low volume energy density of wastes such as biomass and garbage, it is generally believed that it is technically feasible and economically reasonable to produce synthesis gas using fixed bed or fluidized bed gasification technology for biomass and garbage that have undergone certain pretreatment. However, when fixed bed or fluidized bed gasification is used, the crude synthesis gas produced usually contains methane, tar and fly ash, which not only affects the full recovery and utilization of the sensible heat of the high-temperature crude synthesis gas, but also causes blockage of downstream devices if tar and fly ash are not handled properly.

[0003] The disadvantages of traditional tar and fly ash treatment methods are: (1) they cannot solve the problem of further conversion of methane; (2) the further processing and utilization of the separated tar are complicated; and (3) a large amount of difficult-to-treat phenol-containing wastewater is generated, causing environmental pollution.

[0004] In industry, hydrocarbon gas containing methane can be processed by steam reforming, non-catalytic partial oxidation and catalytic partial oxidation. However, the crude synthesis gas produced by fixed bed or fluidized bed gasification and pyrolysis contains methane, tar, fly ash, and harmful impurities such as sulfur and Cl, which are harmful to steam reforming and catalytic partial oxidation catalysts, so steam reforming and catalytic partial oxidation cannot be used directly. Non-catalytic partial oxidation is a more suitable method for treating methane, tar and fly ash.

[0005] The non-catalytic partial oxidation process is to fully mix the gas containing methane, tar and fly ash with oxygen at a stoichiometric ratio through a nozzle, and produce synthesis gas through partial oxidation reaction in a device cavity with a refractory lining. Specifically, there are the following reactions:

[0006]

[0007]

[0008] The carbon in fly ash will react as follows:

[0009]

[0010] Various organic sulfurs in the high-temperature gas entering the furnace are mainly converted into H2S and a small amount of COS.

[0011] The reaction temperature of this process mainly depends on the ratio of oxygen to methane, tar and carbon in fly ash. In order to fully convert methane, tar and fly ash, the temperature is generally maintained at 1200-1400℃.

[0012] In the field of non-catalytic partial oxidation, Chinese patent CN94193847.6 discloses a partial oxidation method for power generation, in which the raw materials involve liquid hydrocarbons and gaseous hydrocarbons. Practice shows that the interchange of raw materials cannot be achieved without replacing the core equipment. When a certain factory changed the residual oil raw material to natural gas raw material, the dome of the converter was overheated, and the dome temperature reached up to 400°C, exceeding the safety interlock alarm value, and the device could not operate normally. Chinese patent CN03115819.6 discloses a device and method for producing synthesis gas by partial oxidation of gaseous hydrocarbon raw materials, but the patent does not involve high-temperature gas containing methane, tar and fly ash, and cannot be used for non-catalytic partial oxidation reactions of such gases. In addition, a jacket cooling section is provided on the upper part of the device of the patent, which is complicated to operate and prone to safety accidents in industrial practice. Chinese patent CN201210462084.1 discloses a gaseous hydrocarbon non-catalytic partial oxidation converter and its application, but the patent is provided with multiple nozzles on the top of the converter. Industrial practice has proved that this type of furnace cannot be used for non-catalytic conversion of high-temperature gas rich in tar and fly ash. Chinese patent CN201610017699.1 discloses a method for preparing synthesis gas from high-temperature hydrocarbon-containing gas, in which gas distribution holes are set in the hydrocarbon gas channel. Practice has shown that this will cause tar blockage and affect stable feeding. Therefore, this method cannot be applied to the non-catalytic conversion of high-temperature gas containing methane, tar and fly ash. Chinese patent CN201210462283.2 discloses a method for preparing synthesis gas by non-catalytic partial oxidation of quenched gaseous or liquid hydrocarbons, but does not involve high-temperature gas containing methane, tar and fly ash, does not make major changes in the equipment structure, and cannot be applied to the process of preparing synthesis gas by non-catalytic partial oxidation of such gas.

[0013] Chinese patent CN201210462013.1 discloses a method for producing synthesis gas by non-catalytic partial oxidation of gaseous hydrocarbons with heat recovery, but the patent can only process gaseous hydrocarbons without tar and fly ash. If it is used to process high-temperature gas containing tar and fly ash, it may cause blockage, affect stable feeding, cause the device to be unable to operate, and affect the conversion rate; at the same time, there may be a backflow of oxygen in the reformer into the preceding gasification furnace, causing safety problems. And after the heat is recovered, only saturated steam is generated, which cannot meet the system's demand for superheated steam.

[0014] The clean, efficient and stable conversion of high-temperature gas containing methane, tar and fly ash to produce high-quality synthesis gas has always been a problem that has troubled the industry. The industry is in urgent need of a clean, efficient and large-scale industrial application of a non-catalytic conversion device and method for high-temperature gas containing methane, tar and fly ash. Utility Model Content

[0015] In order to solve the above defects in the prior art, the utility model provides a system and method for preparing synthesis gas, which can improve the conversion rate of methane, tar and fly ash, and can also produce high-quality superheated steam as a by-product.

[0016] The utility model solves the above technical problems through the following technical solutions:

[0017] The utility model also provides a synthesis gas preparation system, which includes a non-return mixer, a reformer, a waste heat boiler and a steam superheater connected in sequence;

[0018] The non-return mixer comprises a T-shaped pipe and an injection assembly, wherein the T-shaped pipe comprises a first straight pipe section with openings at both ends and a second straight pipe section with an opening at one end, wherein the open end of the second straight pipe section is vertically connected to the middle of the first straight pipe section; the injection assembly comprises an L-shaped nozzle formed by connecting a first nozzle section and a second nozzle section perpendicular to the first nozzle section; the first nozzle section is fixedly connected to the closed end of the second straight pipe section, so that the second nozzle section is placed in parallel in the first straight pipe section and faces the reformer;

[0019] The reformer comprises a coaxially arranged reaction chamber and a nozzle chamber, wherein the nozzle chamber is arranged at the top of the reaction chamber, and a mixed gas inlet is provided on the side of the nozzle chamber;

[0020] A nozzle is provided inside the nozzle chamber, and the axis of the nozzle coincides with the axis of the nozzle chamber;

[0021] The nozzle includes a first tube and a second tube, the axes of the first tube and the second tube coincide, the diameter of the second tube is larger than the diameter of the first tube and smaller than the diameter of the nozzle chamber; the first tube is used to introduce oxygen, the first annular flow channel formed between the second tube and the first tube is used to introduce a gasifying agent, and the second annular flow channel formed between the second tube and the nozzle chamber is used to introduce a mixed gas into the reaction chamber; one end of the second nozzle section arranged on the first straight pipe section is connected to the second annular flow channel through the mixed gas inlet.

[0022] The non-return mixer with the special structure provided in the utility model is conducive to preventing the gas in the converter from flowing back and causing safety problems. The use of conventional industrial valves and other devices with non-return functions in the field is prone to blockage, resulting in the inability of the device to operate stably. The non-return mixer used in the utility model has the following advantages: (1) It is conducive to guiding the direction of the gas flow, (2) When the pressure of the treated gas is low, the L-shaped nozzle is more conducive to the extraction effect and the non-return effect is better, and (3) It is conducive to preventing the gasification agent from flowing back into the front-end equipment.

[0023] In the present invention, preferably, the second nozzle section is perpendicular to the axis of the nozzle chamber.

[0024] In the present invention, preferably, the axis of the second nozzle section is arranged to coincide with the axis of the first straight pipe section.

[0025] In the present invention, preferably, the diameter ratio of the first tube to the second tube is (0.5-0.8):1, for example, 0.7:1.

[0026] In the present invention, preferably, the diameter ratio of the first tube and the nozzle chamber is (0.3-0.5):1, for example, 0.4:1.

[0027] In the present invention, preferably, the ratio of the height to the diameter of the nozzle chamber is (2-5):1, for example, 3:1.

[0028] In the utility model, the inner wall of the reaction chamber is preferably also provided with a refractory lining.

[0029] Wherein, the refractory lining preferably includes insulating bricks, backing bricks and fire surface refractory bricks which are arranged in sequence in the axial direction.

[0030] Wherein, the inner wall of the reaction chamber is made of metal, for example.

[0031] Preferably, a brick support frame is provided on the inner wall of the reaction chamber along the axial direction of the reformer. The number of brick supports is not limited in the utility model, and can be selected according to actual conditions. The brick support frame provided in the utility model can divide the refractory lining into multiple parts along the axial direction of the reformer, which is conducive to eliminating the expansion deformation of the refractory lining.

[0032] In the present invention, the ratio of the height to the diameter of the reaction chamber is preferably (3-10):1, for example, 8:1 or 6:1.

[0033] In the present invention, preferably, the ratio of the diameter of the nozzle chamber to the diameter of the reaction chamber is 1:(4-12), more preferably 1:(4-6), further more preferably 1:(4-5), for example 1:4.5.

[0034] In a specific implementation of the present invention, the nozzle chamber and the nozzle are connected via a flange.

[0035] In the present invention, preferably, the ratio of the diameter of the nozzle chamber to the height of the nozzle chamber is 1:(2-5), for example, 1:3 or 1:4.

[0036] In the present invention, preferably, a contraction section is provided at one end of the first tube close to the nozzle chamber, and an angle formed between a side wall of the contraction section and the axis of the first tube is 10-18°, for example, 15°.

[0037] In the present invention, preferably, a cooling water channel is provided inside the outer wall of the second tube.

[0038] Wherein, the cooling water channel is provided with a cooling water inlet and a cooling water outlet, for example.

[0039] In the present invention, preferably, positioning blocks are symmetrically arranged in the first annular flow channel. The positioning blocks can maintain the coaxiality between the second tube and the first tube.

[0040] Wherein, the number of the positioning blocks is preferably 4.

[0041] In the present invention, preferably, positioning blocks are symmetrically arranged in the second annular flow channel. The positioning blocks can maintain the coaxiality between the second tube and the nozzle chamber.

[0042] Wherein, the number of the positioning blocks is preferably 4.

[0043] In a specific implementation of the present invention, the fixed connection is through a flange connection.

[0044] In a specific embodiment of the present invention, the non-return mixer and the nozzle chamber are connected via a flange.

[0045] In the present invention, preferably, the ratio of the height to the diameter of the waste heat boiler is (3-8):1, for example, 5:1 or 6:1.

[0046] In the utility model, preferably, a steam outlet is provided at the top of the waste heat boiler, a first synthesis gas outlet is provided at the bottom of the waste heat boiler, and a second synthesis gas outlet is provided at the side wall of the waste heat boiler; the steam inlet of the steam superheater is connected to the steam outlet; the steam superheater is also provided with a synthesis gas inlet, and the synthesis gas inlet is connected to the second synthesis gas outlet, and the steam superheater is used to recover the heat of the synthesis gas.

[0047] Preferably, the waste heat boiler is provided with a spiral reducer for flow heat transfer of the synthesis gas.

[0048] The number of the spiral reducers is preferably 2-10, for example 8.

[0049] In a specific embodiment of the present invention, the first synthesis gas outlet is connected to the synthesis gas inlet through a tube sheet.

[0050] In a specific embodiment of the utility model, an inlet head and an outlet head are respectively provided at both ends of the steam superheater along the flow direction of the synthesis gas.

[0051] The inlet head and the outlet head may be provided with heat-insulating refractory materials, for example.

[0052] In a specific embodiment of the present invention, the reformer and the waste heat boiler are connected via flanges and connecting pipes.

[0053] In the present invention, preferably, the ratio of the length to the diameter of the first straight pipe section is (6-10):1, for example, 8:1.

[0054] In the present invention, preferably, the ratio of the length to the diameter of the second straight pipe section is (4-8):1, for example, 7:1.

[0055] In the present invention, preferably, the length ratio of the second nozzle section to the first nozzle section is (1.5-4):1, for example, 3:1.

[0056] In the present invention, preferably, the ratio of the length to the diameter of the second nozzle section is (4-8):1, for example, 6:1.

[0057] The positive and progressive effects of the utility model are:

[0058] The special structure of the nozzle adopted by the utility model is conducive to further improving the mixing efficiency of oxygen, gasifying agent and mixed gas, and improving the conversion rate of methane, tar and fly ash; at the same time, the above nozzle structure can also help to prolong the life of the nozzle. The utility model combines the reformer, waste heat boiler and steam superheater with each other, and can also generate superheated steam, significantly improve the steam quality, and improve the energy utilization rate of the system.

[0059] The utility model solves the engineering problem of tar and fly ash treatment in methane-containing gas, completes the efficient conversion of methane, tar and fly ash in high-temperature gas in one set of equipment, and realizes the full recovery of reaction heat, and produces high-pressure superheated steam as a by-product. It has the advantages of compact equipment, simple process, low investment and low operating cost. BRIEF DESCRIPTION OF THE DRAWINGS

[0060] Figure 1 This is a schematic diagram of the synthesis gas preparation system of Example 1.

[0061] Figure 2 Schematic diagram of the non-return mixer of Example 1.

[0062] Figure 3 Schematic diagram of the nozzle of Example 1.

[0063] Reference numerals:

[0064] 1- non-return mixer; 2- reaction chamber; 3- nozzle chamber; 4- waste heat boiler; 5- steam superheater; 6- nozzle; 7- spiral reducer;

[0065] 101-first straight pipe section; 102-second straight pipe section; 103-first nozzle section; 104-second nozzle section;

[0066] 601 - first tube; 602 - second tube; 603 - first annular flow channel. DETAILED DESCRIPTION

[0067] The present invention is further described below by way of examples, but the present invention is not limited to the scope of the examples. The experimental methods without specific conditions in the following examples are selected according to conventional methods and conditions, or according to the product specifications.

[0068] Example 1

[0069] Example 1 provides a system for preparing synthesis gas, the schematic diagram of which is as follows Figure 1 It includes a non-return mixer 1, a reformer, a waste heat boiler 4 and a steam superheater 5 which are connected in sequence;

[0070] The non-return mixer 1 includes a T-shaped pipe and an injection assembly. The schematic diagram of the non-return mixer 1 is as shown in FIG. Figure 2 As shown. The T-shaped pipe includes a first straight pipe section 101 with openings at both ends and a second straight pipe section 102 with an opening at one end, and the open end of the second straight pipe section 102 is vertically connected to the middle of the first straight pipe section 101; the injection assembly includes an L-shaped nozzle formed by connecting a first nozzle section 103 and a second nozzle section 104 perpendicular to the first nozzle section 103; the first nozzle section 103 is connected to the closed end of the second straight pipe section 102 by a flange, so that the second nozzle section 104 is placed parallel to the first straight pipe section 101 and faces the reformer; the second nozzle section 104 is arranged to coincide with the axis of the first straight pipe section 101;

[0071] Among them, the ratio of the length to the diameter of the first straight pipe section is 8:1, the ratio of the length to the diameter of the second straight pipe section is 7:1, the length ratio of the second nozzle section to the first nozzle section is 3:1, and the ratio of the length to the diameter of the second nozzle section is 6:1.

[0072] The reformer comprises a coaxially arranged reaction chamber 2 and a nozzle chamber 3, wherein the nozzle chamber 3 is arranged at the top of the reaction chamber 2, and a mixed gas inlet is provided on the side of the nozzle chamber 3; the second nozzle section 104 is perpendicular to the axis of the nozzle chamber 3;

[0073] A nozzle 6 is provided inside the nozzle chamber 3, and the axis of the nozzle 6 coincides with the axis of the nozzle chamber 3; a schematic diagram of the nozzle 6 is shown in Figure 3 shown.

[0074] The nozzle 6 includes a first tube 601 and a second tube 602, the axes of the first tube 601 and the second tube 602 coincide, the diameter of the second tube 602 is larger than the diameter of the first tube 601 and smaller than the diameter of the nozzle chamber 3; the first tube 601 is used to introduce oxygen, the first annular flow channel 603 formed between the second tube 602 and the first tube 601 is used to introduce a gasifying agent, and the second annular flow channel formed between the second tube 602 and the nozzle chamber 3 is used to introduce a mixed gas into the reaction chamber 2; one end of the second nozzle section arranged on the first straight pipe section 101 is connected to the second annular flow channel through a mixed gas inlet.

[0075] The ratio of the height to the diameter of the nozzle chamber 3 is 3:1; the ratio of the diameters of the first tube 601 and the second tube 602 is 0.7:1; the ratio of the diameters of the first tube 601 and the nozzle chamber 3 is 0.4:1;

[0076] The inner wall of the reaction chamber 2 is also provided with a refractory lining; wherein the refractory lining includes insulating bricks, backing bricks and fire surface refractory bricks arranged in sequence in the axial direction; wherein a brick support frame is provided on the inner wall of the reaction chamber 2 along the axial direction of the reformer;

[0077] The height of the reaction chamber 2 is 7900 mm, the outer diameter of the reaction chamber 2 is 1920 mm, the diameter of the reaction chamber 2 is 1320 mm, and the ratio of the height to the diameter of the reaction chamber 2 is 6:1;

[0078] The ratio of the diameter of the nozzle chamber 3 to the diameter of the reaction chamber 2 is 1:4.5; the nozzle chamber 3 and the nozzle are connected by a flange;

[0079] The outer diameter of the nozzle chamber 3 is 700 mm, the diameter is 300 mm, and the height is 900 mm. The ratio of the diameter of the nozzle chamber 3 to the height of the nozzle chamber 3 is 1:3;

[0080] A contraction section is provided at one end of the first tube 601 close to the nozzle chamber 3, and an angle formed between the side wall of the contraction section and the axis of the first tube 601 is 15°;

[0081] A cooling water channel is provided inside the outer wall of the second tube 602; a cooling water inlet and a cooling water outlet are provided on the cooling water channel respectively;

[0082] Positioning blocks are symmetrically arranged in the first annular flow channel 603; wherein the number of the positioning blocks is 4;

[0083] Positioning blocks are symmetrically arranged in the second annular flow channel; wherein the number of the positioning blocks is 4;

[0084] The non-return mixer 1 and the nozzle chamber 3 are connected via a flange;

[0085] The height of the waste heat boiler 4 is 9000 mm, the diameter of the waste heat boiler 4 is 1800 mm, the ratio of the height to the diameter of the waste heat boiler 4 is 5:1, a steam outlet is provided at the top of the waste heat boiler 4, a first synthesis gas outlet is provided at the bottom of the waste heat boiler 4, and a second synthesis gas outlet is provided at the side wall of the waste heat boiler 4; the steam inlet of the steam superheater 5 is connected to the steam outlet; the steam superheater 5 is also provided with a synthesis gas inlet, which is connected to the second synthesis gas outlet, and the steam superheater 5 is used to recover the heat of the synthesis gas;

[0086] The waste heat boiler 4 is provided with a spiral reducer 7 for flow heat transfer of the synthesis gas; the number of the spiral reducers 7 is 8;

[0087] Wherein, the first synthesis gas outlet is connected to the synthesis gas inlet through the tube sheet;

[0088] The steam superheater 5 is provided with an inlet head and an outlet head at both ends along the flow direction of the synthesis gas; wherein the inlet head and the outlet head are provided with heat-insulating refractory materials;

[0089] The reforming furnace and the waste heat boiler 4 are connected via flanges and connecting pipes.

[0090] Example 2

[0091] Example 2 adopts the synthesis gas preparation system of Example 1.

[0092] The method for preparing synthesis gas of Example 2 comprises the following steps:

[0093] The mixed gas is mixed with the second gasifying agent after passing through the non-return mixer and enters the second annular flow channel, and forms a stable flow after being accelerated in the second annular flow channel. The stable flow is mixed with the oxygen sprayed from the first pipe and the first gasifying agent sprayed from the second pipe and then passed into the reaction chamber for partial oxidation reaction to generate synthesis gas; the synthesis gas is cooled after passing through the waste heat boiler and the steam superheater in sequence, and superheated steam is generated at the same time;

[0094] The mixed gas is a gas including methane, tar and fly ash; the flow rate of the mixed gas is 40000Nm 3 / h, the specific composition of methane and other gases in the mixed gas is (dry basis, volume):

[0095] H2: 25.80%, CO: 27.04%, CO2: 27.50%, CH4: 16.50%, H2S: 0.25%, COS: 0.03%, N2: 1.50%; NH3: 0.50%, HCN: 0.06%, HCl: 0.72%.

[0096] The fly ash content in the mixed gas is 25g / Nm 3 ; The tar content in the mixed gas is 20g / Nm 3 ;

[0097] The temperature of the mixed gas is 500℃; the converter is calculated based on 330 working days per year.

[0098] The temperature of the partial oxidation reaction is 1280°C; the pressure of the partial oxidation reaction is 5 MPa;

[0099] The composition of the synthesis gas is (dry basis, volume): H2: 34.97%, CO: 48.30%, CO2: 14.69%, CH4: 0.13%, H2S: 0.18%, COS: 0.01%, N2: 1.22%; Ar: 0.06%; HCl: 0.44%.

[0100] The flow rate of the synthesis gas in the spiral reducer is 20m / s; the flow rate of the synthesis gas entering the steam superheater is regulated by a valve; the steam pressure is 4MPa, and the temperature of the superheated steam is 400℃;

[0101] The temperature of the synthesis gas entering the steam superheater is 900°C; the mass percentage of the synthesis gas entering the steam superheater is 20% of the synthesis gas;

[0102] The first gasifying agent and the second gasifying agent are both steam;

[0103] The temperature of the second gasifying agent is 500°C; the pressure of the second gasifying agent is higher than the pressure of the mixed gas, and the pressure difference between the second gasifying agent and the mixed gas is 0.5MPa;

[0104] The mass ratio of the second gasifying agent to the first gasifying agent and the mixed gas is 0.5:1;

[0105] The mass of the second gasifying agent accounts for 70% of the sum of the mass of the second gasifying agent and the first gasifying agent; the mass of the first gasifying agent accounts for 30% of the sum of the mass of the second gasifying agent and the first gasifying agent;

[0106] The flow rate of the first gasifying agent leaving the second tube is 100 m / s; the flow rate of oxygen leaving the first tube is 90 m / s;

[0107] The flow rate of the steady flow is 50m / s;

[0108] The pressure of the cooling water in the cooling water channel is higher than the pressure of the partial oxidation reaction, and the difference between the pressure of the cooling water in the cooling water channel and the pressure of the partial oxidation reaction is 0.5 MPa;

[0109] The ratio of the volume of oxygen to the mass of the mixed gas is 0.8:1; the concentration of oxygen is 99.6%;

[0110] The effects achieved in Example 2 are: methane conversion rate is 99%, tar conversion rate is 100%, and fly ash conversion rate is 100%.

[0111] The utility model can simultaneously realize the integrated conversion of methane, tar and fly ash, and the processing conversion rate of the above three substances is as high as over 99%; at the same time, the utility model can also realize steam self-superheating.

Claims

1. A system for preparing synthesis gas, characterized in that: It includes a non-return mixer, a reformer, a waste heat boiler and a steam superheater connected in sequence; The non-return mixer comprises a T-shaped pipe and an injection assembly, wherein the T-shaped pipe comprises a first straight pipe section with openings at both ends and a second straight pipe section with an opening at one end, wherein the open end of the second straight pipe section is vertically connected to the middle of the first straight pipe section; the injection assembly comprises an L-shaped nozzle formed by connecting a first nozzle section and a second nozzle section perpendicular to the first nozzle section; the first nozzle section is fixedly connected to the closed end of the second straight pipe section, so that the second nozzle section is placed in parallel in the first straight pipe section and faces the reformer; The reformer comprises a coaxially arranged reaction chamber and a nozzle chamber, wherein the nozzle chamber is arranged at the top of the reaction chamber, and a mixed gas inlet is provided on the side of the nozzle chamber; A nozzle is provided inside the nozzle chamber, and the axis of the nozzle coincides with the axis of the nozzle chamber; The nozzle includes a first tube and a second tube, the axes of the first tube and the second tube coincide, the diameter of the second tube is larger than the diameter of the first tube and smaller than the diameter of the nozzle chamber; the first tube is used to introduce oxygen, the first annular flow channel formed between the second tube and the first tube is used to introduce a gasifying agent, and the second annular flow channel formed between the second tube and the nozzle chamber is used to introduce a mixed gas into the reaction chamber; one end of the second nozzle section arranged on the first straight pipe section is connected to the second annular flow channel through the mixed gas inlet.

2. The synthesis gas preparation system according to claim 1, characterized in that: The synthesis gas preparation system meets one or more of the following conditions: ① The second nozzle section is perpendicular to the axis of the nozzle chamber; ② The axis of the second nozzle section coincides with the axis of the first straight pipe section; ③The ratio of the height to the diameter of the nozzle chamber is (2-5):

1.

3. The synthesis gas preparation system according to claim 1, characterized in that: The synthesis gas preparation system meets one or more of the following conditions: ① The diameter ratio of the first tube to the second tube is (0.5-0.8):1; ② The diameter ratio of the first tube and the nozzle chamber is (0.3-0.5):1; ③ The ratio of the height to the diameter of the reaction chamber is (3-10): 1; ④ The ratio of the diameter of the nozzle chamber to the diameter of the reaction chamber is 1:(4-12); ⑤ The ratio of the diameter of the nozzle chamber to the height of the nozzle chamber is 1:(2-5); ⑥ A contraction section is provided at one end of the first tube close to the nozzle chamber, and an angle formed between the side wall of the contraction section and the axis of the first tube is 10-18°; ⑦ The ratio of the height to the diameter of the waste heat boiler is (3-8):

1.

4. The system for preparing synthesis gas according to claim 3, characterized in that: The synthesis gas preparation system meets one or more of the following conditions: ① The diameter ratio of the first tube to the second tube is 0.7:1; ② The diameter ratio of the first tube and the nozzle chamber is 0.4:1; ③ The ratio of the height to the diameter of the reaction chamber is 8:1 or 6:1; ④ The ratio of the diameter of the nozzle chamber to the diameter of the reaction chamber is 1:(4-6); ⑤ The ratio of the diameter of the nozzle chamber to the height of the nozzle chamber is 1:3 or 1:4; ⑥ The angle formed between the side wall of the contraction section and the axis of the first tube is 15°; ⑦ The ratio of height to diameter of the waste heat boiler is 5:1 or 6:

1.

5. The synthesis gas preparation system according to claim 1, characterized in that: The synthesis gas preparation system meets one or more of the following conditions: ① The inner wall of the reaction chamber is also provided with a refractory lining; ② The nozzle chamber and the nozzle are connected via a flange; ③ A cooling water channel is provided inside the outer wall of the second tube; ④ Positioning blocks are symmetrically arranged in the first annular flow channel; ⑤ Positioning blocks are symmetrically arranged in the second annular flow channel; ⑥ The fixed connection is through a flange connection; ⑦ The non-return mixer and the nozzle chamber are connected via a flange.

6. The system for preparing synthesis gas according to claim 5, characterized in that: The synthesis gas preparation system meets one or more of the following conditions: ① The refractory lining includes insulating bricks, backing bricks and fire surface refractory bricks arranged in sequence in the axial direction; ② A brick support frame is provided on the inner wall of the reaction chamber along the axial direction of the reformer; ③ The cooling water channel is provided with a cooling water inlet and a cooling water outlet respectively; ④The number of the positioning blocks is 4; ⑤The number of the positioning blocks is 4.

7. The synthesis gas preparation system according to claim 1, characterized in that: The waste heat boiler is provided with a steam outlet at the top, a first synthesis gas outlet at the bottom, and a second synthesis gas outlet at the side wall of the waste heat boiler; the steam inlet of the steam superheater is connected to the steam outlet; the steam superheater is also provided with a synthesis gas inlet, which is connected to the second synthesis gas outlet, and the steam superheater is used to recover the heat of the synthesis gas.

8. The system for preparing synthesis gas according to claim 7, characterized in that: The synthesis gas preparation system meets one or more of the following conditions: ① The waste heat boiler is provided with a spiral reducer for flow heat transfer of synthesis gas; ② The first synthesis gas outlet is connected to the synthesis gas inlet through a tube sheet; ③ The steam superheater is provided with an inlet head and an outlet head at both ends along the flow direction of the synthesis gas; ④ The converter and the waste heat boiler are connected via flanges and connecting pipes.

9. The system for preparing synthesis gas according to claim 1, characterized in that: The synthesis gas preparation system meets one or more of the following conditions: ① The ratio of the length to the diameter of the first straight pipe section is (6-10): 1; ② The ratio of the length to the diameter of the second straight pipe section is (4-8):1; ③ The length ratio of the second nozzle section to the first nozzle section is (1.5-4):1; ④The ratio of the length to the diameter of the second nozzle section is (4-8):

1.

10. The synthesis gas preparation system according to claim 9, characterized in that: The synthesis gas preparation system meets one or more of the following conditions: ① The ratio of the length to the diameter of the first straight pipe section is 8:1; ② The ratio of the length to the diameter of the second straight pipe section is 7:1; ③ The length ratio of the second nozzle section to the first nozzle section is 3:1; ④The ratio of the length to the diameter of the second nozzle section is 6:1.

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