Two-channel fixed bed reactor and axial adiabatic coupling shift reactor

Abstract

The utility model relates to a two-channel fixed bed reactor, an axial adiabatic coupling shift reactor and a fixed bed reactor, the fixed bed reactor is provided with a shell and a hollow reaction cavity, and a partition plate is arranged in the shell and divides the hollow reaction cavity into an upper chamber and a lower chamber; the upper chamber is provided with an air inlet; the lower chamber is provided with an air outlet; a cylinder is sleeved in the upper chamber and serves as a first reaction cavity; a heat exchange unit is arranged in the barrel; the heat exchange unit comprises a water-cooling heat exchange assembly and an air-cooling heat exchange assembly. According to the utility model, the air cooling-water cooling double heat exchange channels are arranged in the isothermal reaction region to remove reaction heat in time, so that the temperature of shift gas in the isothermal region can be effectively controlled, the reaction is carried out in the positive direction, and crude synthesis gas can be preheated to the temperature above the catalyst activation temperature while saturated steam is produced as a byproduct.

Description

Technical Field

[0001] The utility model relates to the field of conversion reaction equipment, in particular to a dual-channel fixed-bed reactor and an axial adiabatic coupling conversion reactor. Background Art

[0002] The shift reaction refers to the reaction of CO and water vapor to produce CO2 and H2 under certain conditions. It is a highly exothermic reaction and a thermodynamically controlled process.

[0003] In the existing process, the conversion device adopts an adiabatic reactor or an isothermal reactor.

[0004] On the one hand, the limitation of adiabatic reactors is that, due to the large adiabatic temperature rise, in order to avoid overheating of the reactor and promote the reaction in the positive direction, the existing conversion process flows all involve multi-stage reactions and multiple coolings, but all of them have the problems of too long a process and too large a pressure drop.

[0005] On the other hand, the limitations of isothermal reactors are:

[0006] (1) In the prior art, the temperature of the isothermal shift furnace is determined by the catalyst loading and the reaction equilibrium and cannot be adjusted. In order to maintain a certain degree of superheat, the conversion gas at the outlet of the isothermal shift furnace is usually required to be stable above a certain temperature. However, when the crude synthesis gas load changes or the catalyst activity decreases at the end of the process, there is a lack of effective means to adjust the outlet temperature, resulting in poor controllability and adjustability. Due to factors such as upstream load changes, water-gas ratio fluctuations, and catalyst temperature increase at the end of the process, the outlet temperature of the shift furnace needs to be adjusted frequently.

[0007] (2) The steam produced as a byproduct of the isothermal converter drum is saturated steam, which cannot produce higher quality superheated steam. The converter is a steam surplus device. Usually, the excess steam is supplied to other users in the plant through the steam pipe network. However, the saturated steam temperature drops and easily produces condensate, which cannot enter the pipe network. Since most of the reaction heat of the isothermal converter is taken away by the water circulation system, the outlet temperature is only about 300℃, which cannot provide a superheat source. It can only be achieved by setting up a separate heating furnace or combining heat with other devices, which increases the complexity of the process and equipment investment.

[0008] (3) In the prior art, the warm reactor is a single-channel tubular reactor, and the feed gas flows from top to bottom along the axial direction. The CO content in the feed gas is high, while the CO content in the outlet conversion gas is low. Therefore, the reaction at the upper end of the reactor is more intense and releases more heat, while the reaction at the lower end of the reactor is milder and releases less heat. The hot spot temperature of the reactor is concentrated at the upper end of the reactor, resulting in the upper end of the reactor being easily overheated, the catalyst life being short, and deactivation being rapid.

[0009] In addition, both the existing adiabatic reactor and isothermal shift reactor require that the crude synthesis gas be heated to above the catalyst activation temperature before entering the shift furnace. Utility Model Content

[0010] The technical problem to be solved by the present invention is to provide a semi-isothermal conversion furnace with segmented feeding and controllable and adjustable conversion gas temperature in response to the current status of the existing technology, so as to meet the requirements of the crude synthesis gas conversion reaction under different load and water-gas ratio working conditions; at the same time, it can be combined with the entire conversion heat exchange network process to flexibly adjust the outlet conversion gas temperature to meet the requirements of the by-product steam level and superheat of the conversion unit.

[0011] The utility model provides a fixed-bed reactor comprising a shell and a hollow reaction chamber. A partition is provided within the shell, dividing the hollow reaction chamber into an upper chamber and a lower chamber. The upper chamber is provided with an air inlet, and the lower chamber is provided with an air outlet. A cylinder is sleeved within the upper chamber, and the cylinder serves as a first reaction chamber. A heat exchange unit is provided within the cylinder. The heat exchange unit includes a water-cooled heat exchange component and an air-cooled heat exchange component. The water-cooled heat exchange component is composed of a plurality of water-cooled heat exchange plates, and the air-cooled heat exchange component is composed of a plurality of air-cooled heat exchange plates. The lower chamber is provided with a radially extending upper plate and a lower plate, and the upper plate, the inner wall of the shell, and the lower plate form a second reaction chamber. The upper plate is provided with a plurality of vent holes II, and the lower plate is provided with a plurality of vent holes III. Both ends of the upper plate and the lower plate are hermetically connected to the inner wall of the shell.

[0012] As a preferred technical solution, the air-cooled heat exchange component has a preheating air inlet and a preheating air outlet, and the preheating air outlet is connected to the air inlet.

[0013] As a preferred technical solution, a gap is left between the side wall of the cylinder and the inner wall of the shell as an air inlet channel; the side wall of the cylinder is provided with a plurality of air vents I; the center of the cylinder is provided with an axially extending central tube, the tube wall of the central tube is provided with a plurality of air collecting holes, the upper end of the central tube is closed, and the lower end is connected to the lower chamber.

[0014] As an embodiment, the preheating gas outlet is communicated with the air inlet channel, that is, the preheating gas does not discharge out of the reactor but directly enters the air inlet channel.

[0015] As a preferred technical solution, the air inlet includes a first air inlet and a second air inlet; the first air inlet is located at the top of the upper chamber, the second air inlet is located in the middle of the upper chamber, and the second air inlet is connected to the central tube.

[0016] As a preferred technical solution, the air outlet is located at the bottom of the lower chamber.

[0017] As a preferred technical solution, a gas distributor is provided between the lower end of the central tube and the lower chamber.

[0018] As a preferred technical solution, the heat exchange unit is inside the first reaction chamber and extends radially.

[0019] As a preferred technical solution, the single water-cooled heat exchange plate and the single air-cooled heat exchange plate are integrated into one as a single integrated heat exchange plate; preferably, several integrated heat exchange plates are arranged radially in a central radial pattern with the central tube as the center; preferably, the air-cooled heat exchange plate is close to the central tube, and the water-cooled heat exchange plate is far away from the central tube.

[0020] As a preferred technical solution, the space between the side wall and the central tube in the first reaction chamber is filled with a heat exchange reaction catalyst; and the space between the side wall and the central tube in the second reaction chamber is filled with an adiabatic reaction catalyst.

[0021] The utility model also provides a conversion reactor, using any one of the above-mentioned fixed bed reactors as the conversion reactor.

[0022] The reaction gas enters the fixed bed reactor for reaction, and the reaction gas is composed of a first air intake and a second air intake. Preferably, the air intake volume of the first air intake: the air intake volume of the second air intake = 10-80:30-100; preferably, the air intake volume of the first air intake: the air intake volume of the second air intake = 30-50:40-80, more preferably, the first air intake accounts for 40% of the raw gas: the second air intake accounts for 60% of the raw gas. The first air intake enters from the first air inlet, flows through the air inlet channel and the air vent I in sequence to enter the first reaction chamber, and after the reaction, flows through the gas collection hole I, the central tube, the distributor, and the air vent II in sequence to enter the second reaction chamber; the first air intake enters from the second air inlet, flows through the central tube, the distributor, and the air vent II in sequence to enter the second reaction chamber; after the reaction, the gas in the second reaction chamber is discharged through the air vent III and the air outlet. The reaction gas is preferably synthesis gas; the gas discharged from the air outlet is conversion gas. Preferably, the carbon monoxide content of the synthesis gas is 30% to 90% by volume on a dry basis. Preferably, the water / absolute dry gas volume ratio of the synthesis gas is 0.1 to 1.6. The temperature of the gas discharged from the gas outlet is ≥ 400°C.

[0023] Beneficial effects of the utility model:

[0024] (1) The reactor provided by the utility model has a wide range of applications and can be used for raw materials with a carbon monoxide dry volume content of 30% to 90% and a water / absolute dry gas volume ratio of 0.1 to 1.6.

[0025] (2) The isothermal section of the present invention adopts an axial radial structure, which shortens the length of the synthesis flow channel and reduces the pressure drop of the reactor, thereby saving the downstream compression power consumption, which is beneficial to reducing the energy consumption of the entire device and is an energy-saving device.

[0026] (3) The present invention promptly removes the heat of reaction by providing air-cooling and water-cooling dual heat exchange channels within the isothermal reaction zone, thereby effectively controlling the temperature of the conversion gas in the isothermal zone and allowing the reaction to proceed in the positive direction. Saturated steam is obtained at the outlet of the water-cooling channel, and preheated crude synthesis gas above the catalyst activation temperature is obtained at the outlet of the air-cooling channel, thereby maximizing energy utilization.

[0027] (4) The present invention adopts an axial-radial dual-channel reactor. Since the reactor adopts water-cooling and air-cooling channels, the principle of different heat transfer coefficients of liquid and gas is used to exchange heat on the outer side where the reaction is more intense, using liquid with a larger heat transfer coefficient, and on the inner side where the reaction is more mild, using gas with a smaller heat transfer coefficient. This better ensures the temperature balance of the entire catalyst bed, reduces the temperature gradient in different parts of the catalyst bed, and effectively avoids the occurrence of phenomena such as overheating and catalyst deactivation. In addition, the setting of the radial flow channel utilizes the principle of different heat exchange areas on the inner and outer sides. The outer side has a large heat exchange area, which corresponds to the part with intense heat release, and takes more heat. The inner side has a small heat exchange area, which corresponds to the part with heat release temperature, and takes less heat.

[0028] (5) The present invention is provided with a crude synthesis gas bypass inlet. The crude synthesis gas injected from the bypass is mixed with the crude conversion gas obtained from the outlet of the air cooling channel in the upper isothermal zone. Since the crude synthesis gas obtained from the outlet of the air cooling channel has been preheated to above the catalyst activation temperature, the crude synthesis gas entering from the bypass does not need to be separately heated to the activation temperature and can reach the activation temperature. This directly saves the equipment investment of the crude synthesis gas preheater, reduces the complexity of the process, and avoids the tube sheet leakage problem caused by the excessive temperature difference between the shell and tube sides of the crude synthesis gas preheater.

[0029] (6) The utility model adopts a staged reaction technology, setting an axial adiabatic reaction zone in the lower section of the furnace body. By adjusting the bypass crude synthesis gas intake, the water-gas ratio, CO content and the conversion gas outlet temperature of the mixed conversion gas entering the adiabatic reaction zone can be flexibly and effectively adjusted and controlled. By effectively adjusting the conversion gas outlet temperature to above 400°C, superheated steam can be produced, saving equipment investment and operating costs, ensuring the stability of the downstream heat exchange network, not only having no effect on the steam production pressure, but also solving the problem of high CO content raw gas conversion reaction easily overheating and difficult temperature control. BRIEF DESCRIPTION OF THE DRAWINGS

[0030] Figure 1 A schematic diagram of an embodiment of a fixed bed reactor;

[0031] Figure 2 A schematic cross-sectional view of an embodiment of a fixed bed reactor;

[0032] Figure 3 Partial schematic diagram of the heat exchange unit;

[0033] Figure 4 A schematic cross-sectional view of another embodiment of a fixed bed reactor;

[0034] 1 shell, 11 first air inlet, 12 second air inlet; 13 air outlet; 14 upper chamber, 141 vent I, 15 center tube, 151 air collecting hole; 50 lower chamber, 501 vent II, 502 vent III, 51 catalyst, 52 porcelain ball, 43 gas distributor; 41 heat exchange unit, 200 air-cooled heat exchange plate, 210 water-cooled heat exchange plate; 20 air-cooled air inlet, 201 air-cooled air inlet pipe, 202 air-cooled distribution ring pipe, 203 air-cooled riser pipe, 204 preheated gas riser pipe, 205 preheated gas collecting ring pipe, 206 preheated gas rising main pipe, 18 preheated gas outlet; 21 water-cooled water inlet, 211 water-cooled inlet main pipe, 212 water-cooled distribution ring, 213 water-cooled riser pipe, 214 steam riser, 215 steam collecting ring pipe, 216 steam rising main pipe, 22 steam outlet, 28 expansion joint. DETAILED DESCRIPTION

[0035] The following are only preferred implementation methods of the present invention and are not intended to limit the scope of protection of the present invention. All technical solutions based on the concept of the present invention should fall within the scope of protection of the present invention. For professional and technical personnel in this technical field, minor improvements to the present invention without departing from the principles of the present invention should also fall within the scope of protection of the present invention.

[0036] In the preparation examples, embodiments and comparative examples of the present invention, unless otherwise specified, the components and pipe fittings used are commercially available products.

[0037] Example 1 Fixed bed reactor

[0038] like Figure 1 As shown, a fixed bed reactor comprises a shell (with an insulation layer on the periphery) and a hollow reaction chamber, wherein a partition is provided in the shell 1, dividing the hollow reaction chamber into an upper chamber and a lower chamber; the upper chamber is provided with an air inlet; the lower chamber is provided with an air outlet 13; a cylinder is sleeved in the upper chamber, and the cylinder serves as a first reaction chamber; a heat exchange unit is provided in the cylinder for timely removing the reaction heat in the first reaction chamber, and the heat exchange unit comprises a water-cooled heat exchange component and an air-cooled heat exchange component; the water-cooled heat exchange component is composed of a plurality of water-cooled heat exchange plates; the air-cooled heat exchange component is composed of a plurality of air-cooled heat exchange plates; in the lower chamber, an upper plate and a lower plate extending radially are respectively provided from top to bottom, and the edges of the upper plate and the lower plate are sealed and fixedly connected to the shell, and the second reaction chamber is constituted by the upper plate, the inner wall of the shell and the lower plate; the upper plate is provided with a plurality of air vents II, and the lower plate is provided with a plurality of air vents III.

[0039] Example 2 Fixed bed reactor

[0040] like Figure 1 、 Figure 2 As shown, the fixed-bed reactor comprises a shell (with an insulation layer around its periphery) and a hollow reaction chamber. A partition is provided within the shell 1, dividing the hollow reaction chamber into an upper chamber 14 (where the isothermal reaction occurs) and a lower chamber 50 (where the adiabatic reaction occurs). The upper chamber 14 is provided with a first air inlet 11 at its top and a second air inlet 12 in its middle. The lower chamber 50 is provided with an air outlet 13. A cylindrical body (catalyst cylinder) is nestled within the upper chamber 14, serving as the first reaction chamber. The sidewalls of the cylindrical body are provided with a plurality of air vents 1141, with a gap (external air inlet annular gap) remaining between the sidewalls and the inner wall of the shell. The first air inlet 11, the gap, and the air vents 1141 are sequentially connected to form an annular air inlet channel. An axially extending central tube 15 is provided at the center of the cylindrical body. The tube wall of the central tube 15 is provided with a plurality of air collection holes 151 (internal air inlet annular gap). The upper end of the central tube is sealed, while the lower end is connected to the lower chamber 50. A heat exchange unit 41 is provided in the cylinder for promptly removing the reaction heat in the first reaction chamber. The heat exchange unit includes a water-cooled heat exchange component and an air-cooled heat exchange component. The water-cooled heat exchange component is composed of a plurality of water-cooled heat exchange plates. The air-cooled heat exchange component is composed of a plurality of air-cooled heat exchange plates. The lower chamber 50 is provided with an upper plate and a lower plate extending radially from top to bottom in the axial direction. The edges of the upper plate and the lower plate are sealed and fixedly connected to the shell, and the second reaction chamber is formed by the upper plate and the lower plate. The upper plate is provided with a plurality of vent holes II 501, and the lower plate is provided with a plurality of vent holes III 502.

[0041] Example 3 Fixed bed reactor

[0042] like Figure 1 、 Figure 3 As shown, a fixed bed reactor comprises a shell (with an insulation layer on the periphery) and a hollow reaction chamber, wherein a partition is provided in the shell 1, dividing the hollow reaction chamber into an upper chamber 14 (where an isothermal reaction occurs) and a lower chamber 50 (where an adiabatic reaction occurs); the upper chamber is provided with an air inlet, and the lower chamber is provided with an air outlet; a cylinder is provided in the upper chamber, and the cylinder serves as a first reaction chamber; a heat exchange unit 41 is provided in the cylinder for promptly removing the reaction heat in the first reaction chamber; the heat exchange unit 41 comprises a water-cooled heat exchange component and an air-cooled heat exchange component, and the air-cooled heat exchange component has an air-cooled inlet and a preheated air outlet, and the preheated air outlet is connected to the air inlet. The water-cooled heat exchange assembly is composed of several water-cooled heat exchange plates; the air-cooled heat exchange assembly is composed of several air-cooled heat exchange plates; and the single water-cooled heat exchange plate 210 and the single air-cooled heat exchange plate 200 are integrated into one, as a single dual-channel integrated heat exchange plate; several dual-channel integrated heat exchange plates are arranged in a central radial manner, with the air-cooled heat exchange plate 200 close to the center of the axis and the water-cooled heat exchange plate 210 away from the center of the axis. The water-cooled heat exchange plate 210 circulates boiler water as a heat exchange medium, and the air-cooled heat exchange plate 200 circulates the raw gas to be preheated as a heat exchange medium.

[0043] Example 4 Shift Reactor

[0044] like Figure 1 、 Figure 2 、 Figure 3 As shown, the shift reactor comprises a shell (with an insulation layer around its periphery) and a hollow reaction chamber. A partition is provided within the shell 1, dividing the hollow reaction chamber into an upper chamber 14 (for isothermal shift reactions) and a lower chamber 50 (for adiabatic shift reactions). The top of the upper chamber 14 is provided with a first air inlet 11 (the main inlet for the crude syngas) and a second air inlet 12 (a side inlet for the crude syngas) in the middle. The lower chamber 50 is provided with an air outlet 13. A cylindrical body is nestled within the upper chamber 14, serving as the first reaction chamber. To ensure more uniform distribution of the feed gas, a gas distributor can be installed at the first air inlet 11. The sidewalls of the cylindrical body are provided with a number of vents 141, leaving an annular gap between the sidewalls and the inner wall of the shell as an annular air inlet channel. The first air inlet 11, the gap, and the vents 141 are sequentially connected. An axially extending central tube 15 is provided at the center of the cylindrical body to collect the shifted gas and deliver it to the second reaction chamber. The wall of the central tube 15 is provided with a plurality of gas collection holes 151. The upper end of the central tube is sealed, and the lower end is connected to the lower chamber 50. The second air inlet is connected to the lower end of the central tube 15. Within the lower chamber 50, from top to bottom in the axial direction, there are an upper plate and a lower plate extending radially. The edges of the upper plate and the lower plate are both sealed and fixedly connected to the shell, and the upper plate and the lower plate form a second reaction chamber. The upper plate is provided with a plurality of vent holes II 501, and the lower plate is provided with a plurality of vent holes III 502. The gas flows from the first air inlet 11, then into the annular space between the upper chamber 14 and the shell, through the vent holes I 141, into the central tube 15, and then through the gas distributor 43 into the lower chamber 50. It then passes through the vent holes II 501, the catalyst 51, the porcelain balls 52, and finally out of the gas outlet 13. A heat exchange unit 41 is provided in the cylinder for promptly removing the reaction heat in the first reaction chamber. The heat exchange unit includes a water-cooled heat exchange component and an air-cooled heat exchange component. The water-cooled heat exchange component is composed of a plurality of water-cooled heat exchange plates. The air-cooled heat exchange component is composed of a plurality of air-cooled heat exchange plates. The water-cooled heat exchange component is composed of a plurality of water-cooled heat exchange plates. The air-cooled heat exchange component is composed of a plurality of air-cooled heat exchange plates. The single water-cooled heat exchange plate 210 and the single air-cooled heat exchange plate 200 are integrated into one body to form a single dual-channel integrated heat exchange plate. The plurality of dual-channel integrated heat exchange plates are arranged in a radial manner from the center, with the air-cooled heat exchange plate 200 close to the center of the axis and the water-cooled heat exchange plate 210 away from the center of the axis. The water-cooled heat exchange plate 210 circulates boiler water as a heat exchange medium, and the air-cooled heat exchange plate 200 circulates raw synthesis gas to be preheated as a heat exchange medium. The heat exchange unit 41 is provided with an air-cooled air inlet 20, a preheated air outlet 18 (the gas is discharged after preheating), a water-cooled water inlet 21, and a steam outlet 22 (water is discharged in the form of steam), and the preheated air outlet is connected to the air inlet.

[0045] The crude synthesis gas enters the shift reactor for the shift reaction. The catalyst (isothermal shift reaction catalyst) is filled between the side wall of the cylinder and the central tube. The second reaction chamber is filled with catalyst 51 (adiabatic shift reaction catalyst) and ceramic balls 52.

[0046] The water-cooled water inlet 21 (boiler water), water-cooled inlet manifold 211, water-cooled distribution ring 212, several water-cooled riser pipes 213, water-cooled heat exchanger plates 210, several steam riser pipes 214, steam outlet 22 (discharged in the form of steam), steam collection ring pipe 215, and steam riser manifold 216 are sequentially connected. The several water-cooled riser pipes 213 are evenly distributed throughout the water-cooled distribution ring 212, each connected to a water-cooled heat exchanger plate 210. Several steam riser pipes 214 are evenly distributed throughout the steam collection ring 215, which delivers saturated steam to the outside through the steam riser manifold 216.

[0047] The air-cooled air inlet 20 (the raw syngas preheating inlet), air-cooled air inlet pipe 201, air-cooled distribution ring pipe 202, several air-cooled riser pipes 203, air-cooled heat exchanger plates 200, several preheated gas riser pipes 204, preheated gas outlet 18, preheated gas collection ring pipe 205, and preheated gas riser main pipe 206 are sequentially connected. The several air-cooled riser pipes 203 are evenly distributed throughout the air-cooled distribution ring 202, each connected to one of the air-cooled heat exchanger plates 200. The several preheated gas riser pipes 204 are evenly distributed throughout the gaseous medium collection ring pipe 205, which delivers the preheated raw syngas to the outside through the gaseous medium riser main pipe 206.

[0048] The crude synthesis gas to be preheated enters the air-cooled air inlet 20, flows through the air-cooled air inlet pipe 201, the cold distribution loop 202, a plurality of air-cooled riser pipes 203, the air-cooled heat exchange plate 200, the preheating gas riser 204, the preheating gas outlet 18, the preheating gas collecting loop 205, the preheating gas riser main pipe 206, is discharged through the preheating gas outlet 18, and then enters the air inlet (preferably 40% is passed into the first air inlet and 60% is passed into the second air inlet). While producing saturated steam as a by-product, the crude synthesis gas can also be preheated to above the catalyst activation temperature, thereby reducing the investment cost of the preheater.

[0049] like Figure 2 As shown, the preheated gas outlet 18 is located outside the reactor. After passing through the heat exchange plates, the preheated gas exits the reactor through the preheated gas outlet 18 at the top of the reactor and then enters the first gas inlet 11. This intake method allows for flexible adjustment of the amount of crude syngas and preheated syngas. An expansion joint 28 is provided in the middle of each steam riser 214 and each preheated gas riser 204, effectively addressing thermal expansion issues caused by temperature differences in the upper section of the reactor.

[0050] like Figure 4As shown, preheated gas outlet 18 is located inside the reactor. Preheated gas can also exit the reactor without passing through preheated gas outlet 18. Instead, preheated gas outlet 18 is located inside the reactor and directly communicates with gap I. This allows preheated gas to enter gap I directly through preheated gas outlet 18. This intake method eliminates the need to route the preheated crude syngas outside the reactor, resulting in minimal heat loss but poor gas flow regulation. An expansion joint 28 is provided in the middle of each steam riser 214, effectively addressing thermal expansion issues caused by temperature differences in the upper section of the reactor.

[0051] The upper inspection port 34 is used for loading and unloading the catalyst in the upper isothermal section and for inspecting the heat exchange module. The middle inspection port 35 is used for loading the catalyst in the lower adiabatic section and for inspecting and repairing the adiabatic section. The lower inspection port 36 is used for unloading the catalyst in the lower adiabatic section. The pressure grid 42 is used to fix the catalyst bed.

[0052] The raw gas (crude synthesis gas, with a carbon monoxide dry volume content of 30% to 90%, and a water / absolute dry gas volume ratio of 0.1 to 1.6) is composed of a first intake air (40% of the total intake air) and a second intake air (60% of the total intake air). The first intake air enters the shell 1 through the first air inlet, and the second intake air enters the shell 1 through the second air inlet 12, serving as a bypass. By adjusting the bypass synthesis gas intake amount, the water-gas ratio and CO content of the mixed conversion gas entering the adiabatic reaction zone can be controlled, thereby effectively adjusting the conversion gas outlet temperature. The axial adiabatic reaction zone is similar in structure to the heat exchange reaction zone, but does not have a heat exchange channel, so the outlet temperature of the conversion gas after the reaction can reach above 400°C.

[0053] The first intake air enters the first reaction chamber 14 through the first air inlet 11, the annular air inlet channel, and the air vent I 141. The heat generated by the catalyst bed during the reaction is promptly taken away by the heat exchange unit 41. The converted gas after the reaction is collected into the central tube 15 through the air collecting holes I 151 and mixed with the first intake air from the second air inlet 12 to obtain a mixed converted gas.

[0054] The mixed shifted gas from the heat exchange reaction zone is dispersed by gas distributor 43 and axially enters the second chamber through vent II 501. After reaction, it exits housing 1 through vent III 502 and outlet 13. If catalyst activity decreases in the later stages of the reaction, or the shifted gas outlet temperature is too low, the shifted gas outlet temperature can be increased by adjusting the syngas inlet volume to 75% to maintain the temperature of the downstream heat exchange system.

Claims

1. A fixed bed reactor having a shell and a hollow reaction chamber, characterized in that: A partition is provided in the shell to divide the hollow reaction chamber into an upper chamber and a lower chamber; The upper chamber is provided with an air inlet; The lower chamber is provided with an air outlet; A cylinder is installed inside the upper chamber, and the cylinder serves as the first reaction chamber; A heat exchange unit is provided in the cylinder; the heat exchange unit includes a water-cooled heat exchange component and an air-cooled heat exchange component; The water-cooled heat exchange assembly is composed of a number of water-cooled heat exchange plates; The air-cooled heat exchange assembly is composed of a number of air-cooled heat exchange plates; The lower chamber is provided with a radially extending upper plate and lower plate, and the upper plate, the inner wall of the shell and the lower plate constitute a second reaction chamber; the upper plate is provided with a plurality of vent holes II, and the lower plate is provided with a plurality of vent holes III.

2. The fixed bed reactor according to claim 1, characterized in that The air-cooled heat exchange component has a preheating air inlet and a preheating air outlet, and the preheating air outlet is communicated with the air inlet.

3. The fixed bed reactor according to claim 2, characterized in that A gap is left between the side wall of the cylinder and the inner wall of the shell, serving as an air inlet channel; a plurality of vent holes I are provided on the side wall of the cylinder; an axially extending central tube is provided in the center of the cylinder, and a plurality of air collecting holes are provided on the wall of the central tube. The upper end of the central tube is closed, and the lower end is connected to the lower chamber; And / or, the preheating gas outlet is connected to the air inlet channel.

4. The fixed bed reactor according to claim 3, characterized in that The air inlet includes a first air inlet and a second air inlet; The first air inlet is located at the top of the upper chamber, the second air inlet is located in the middle of the upper chamber, and the second air inlet is communicated with the central tube.

5. The fixed bed reactor according to claim 4, characterized in that The air outlet is located at the bottom of the lower chamber.

6. The fixed bed reactor according to claim 5, characterized in that A gas distributor is provided between the lower end pipe opening of the central pipe and the lower chamber.

7. The fixed bed reactor according to claim 6, characterized in that The heat exchange unit is inside the first reaction chamber and extends radially.

8. The fixed bed reactor according to claim 7, characterized in that A single water-cooled heat exchange plate and a single air-cooled heat exchange plate are integrated into one as a single integrated heat exchange plate; a plurality of integrated heat exchange plates are arranged in a central radial pattern with the central tube as the center; the air-cooled heat exchange plate is close to the central tube, and the water-cooled heat exchange plate is far away from the central tube.

9. The fixed bed reactor according to claim 8, characterized in that In the first reaction chamber, a heat exchange reaction catalyst is filled between the side wall and the central tube; The second reaction chamber is filled with an adiabatic reaction catalyst.

10. A shift reactor, characterized in that The fixed bed reactor according to any one of claims 1 to 9 is used as the shift reactor.

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