Two-channel fixed bed reactor and radial adiabatic coupling shift reactor
By using a semi-isothermal conversion furnace and a radial adiabatic coupled conversion reactor in the transformation reactor, combining gas-cooled and water-cooled dual heat exchange channels, the problem of difficulty in adjusting the temperature of the change gas in the prior art is solved, and the effects of reducing energy consumption, extending the catalyst life and superheated steam production are achieved.
Patent Information
- Application Number
- CN202421933065.7
- Authority / Receiving Office
- CN · China
- Patent Type
- Utility models(China)
- Current Assignee / Owner
- Filing Date
- 2024-08-09
- Publication Date
- 2025-06-03
- Estimated Expiration
- 2034-08-09
AI Technical Summary
When existing transformation reactors process coarse syngas with different loads and water-gas ratios, it is difficult to adjust the outlet transformation gas temperature, and isothermal transformation furnaces cannot produce higher quality superheated steam, which increases process complexity and equipment investment.
A semi-isothermal conversion furnace is used to set up dual heat exchange channels of air-cooled and water-cooled through segmented feed and radially adiabatic coupling of the transformation reactor to achieve flexible adjustment of the change gas temperature, and the water-gas ratio and CO content are adjusted through the air conduit and gas distributor.
It realizes effective control of the changing gas temperature, reduces the reactor pressure drop, saves energy consumption, improves the temperature equalization of the catalyst bed, extends the catalyst life, and can produce superheated steam, reducing equipment investment and operating costs.
Smart Images
Figure CN222930788U_ABST
Abstract
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 a radial adiabatic coupling conversion reactor. Background Art
[0002] The conversion reaction refers to the reaction in which CO and water vapor generate CO 2 and H 2 under certain conditions, which belongs to a strongly exothermic reaction and is a thermodynamically controlled process. In the existing process, the conversion device adopts an adiabatic reactor or an isothermal reactor.
[0003] On the one hand, the limitation of the adiabatic reactor is that due to the large adiabatic temperature rise, in order to avoid overheating of the reactor and promote the reaction to proceed in the positive direction, the existing conversion process flow is multi-stage reaction and multi-stage cooling, but there are problems of too long process flow and too large pressure drop.
[0004] On the other hand, the limitations of the isothermal reactor are as follows:
[0005] (1) In the prior art, the temperature of the isothermal conversion furnace is difficult to adjust. In order to keep a certain degree of superheat for the converted gas at the outlet of the isothermal conversion furnace, it is usually required to be stable above a certain temperature. However, when the load of the raw synthesis gas changes or the activity of the catalyst decreases at the end stage, there is a lack of effective means to adjust the outlet temperature. Therefore, the controllability and adjustability are poor. Due to the influence of factors such as upstream load changes, water-gas ratio fluctuations, and temperature increase at the end stage of the catalyst, the outlet temperature of the conversion furnace needs to be adjusted frequently.
[0006] (2) The steam by-produced by the steam drum of the isothermal conversion furnace is saturated steam and cannot produce higher-quality superheated steam. The conversion device is a steam-rich device. Usually, the excess steam needs to be supplied to other users in the whole plant through the steam pipe network. However, the saturated steam is easy to produce condensate when the temperature decreases and cannot enter the pipe network. Since most of the reaction heat of the isothermal conversion furnace is taken away by the water circulation system, the outlet temperature is only about 300 °C and cannot provide a superheat source. It can only increase the process complexity and equipment investment by setting up a separate heating furnace or performing heat integration with other devices.
[0007] (3) In the prior art, the isothermal reactor is a single-channel tubular reactor, and the raw material gas flows downward along the axis for reaction. The CO content in the raw material gas is relatively high, while the CO content in the converted gas at the outlet is relatively 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 mild and releases less heat. The hot spot temperature of the reactor is concentrated at the upper end of the reactor, resulting in easy overheating at the upper end of the reactor, short catalyst life, and fast deactivation.
[0008] On the other hand, for the existing adiabatic reactor and isothermal conversion reactor, the raw synthesis gas needs to be heated above the catalyst activation temperature before entering the conversion furnace. Summary of the Invention
[0009] The technical problem to be solved by the present utility model is to provide a semi-isothermal conversion furnace with segmented feeding and controllable and adjustable temperature of the conversion gas according to the current situation of the prior art, so as to meet the requirements of the conversion reaction of the raw synthesis gas under different loads and steam-to-water ratio conditions; at the same time, it can be combined with the entire conversion heat exchange network process to flexibly adjust the temperature of the outlet conversion gas to meet the requirements of the by-product steam grade of the conversion unit.
[0010] The present utility model provides a fixed-bed reactor, which has a shell and a hollow reaction chamber. An air inlet and an air outlet are respectively provided at the top and bottom of the shell. A partition is provided in the shell. In the direction from the air inlet to the air outlet, the partition divides the hollow reaction chamber into a heat exchange reaction zone and an adiabatic reaction zone; a heat exchange reaction chamber is provided in the heat exchange reaction zone; heat exchange components are provided in the heat exchange reaction chamber; the heat exchange components exchange heat with the heat exchange reaction chamber; the heat exchange components include a liquid medium heat exchange component and a gas medium heat exchange component; the gas medium heat exchange component has a gas medium inlet and a gas medium outlet, and the gas medium outlet is communicated with the air inlet.
[0011] As a preferred technical solution, a gas guide pipe I is provided in the heat exchange reaction chamber. A plurality of gas collecting holes I are provided on the pipe wall of the gas guide pipe I. The pipe orifice at one end of the gas guide pipe I close to the first air inlet is closed, and the pipe orifice at the end far from the first air inlet is communicated with the adiabatic reaction zone; preferably, the gas guide pipe I extends axially in the heat exchange reaction chamber, and preferably is located at the center of the axis.
[0012] As a preferred technical solution, the gas medium heat exchange component is composed of a plurality of gas medium heat exchange plates; preferably, each gas medium heat exchange plate extends radially in the heat exchange reaction chamber; preferably, the plurality of gas medium heat exchange plates are arranged in a central radial pattern with the center of the axis of the heat exchange reaction chamber as the center.
[0013] The gas medium heat exchange component has a gas medium inlet and a preheated gas outlet. As a preferred technical solution, the preheated gas outlet is communicated with the air inlet.
[0014] As a preferred technical solution, the liquid medium heat exchange component is composed of a plurality of liquid medium heat exchange plates; preferably, each liquid medium heat exchange plate extends radially in the heat exchange reaction chamber; preferably, the plurality of liquid medium heat exchange plates are arranged in a central radial pattern with the center of the axis of the heat exchange reaction chamber as the center.
[0015] As a preferred technical solution, the liquid medium heat exchange plate and the gas medium heat exchange plate are integrated into one body; preferably, the gas medium heat exchange plate is close to the center of the axis of the heat exchange reaction chamber, and the liquid medium heat exchange plate is far from the center of the axis of the heat exchange reaction chamber.
[0016] As a preferred technical solution, the air inlet is composed of a first air inlet and a second air inlet.
[0017] As a preferred technical solution, there is a gap I between the side wall I of the heat exchange reaction chamber and the inner wall of the shell, and a number of ventilation holes I are provided on the side wall I; the first air inlet, the gap I, and the ventilation holes I are connected in sequence to form an air inlet passage I.
[0018] As an implementation manner, the preheated gas outlet is communicated with the gap I, that is, the preheated gas does not discharge outside the reactor but directly enters the gap I.
[0019] As a preferred technical solution, the second air inlet is communicated with the air guide pipe I; preferably, the second air inlet is communicated with the pipe orifice at the end of the air guide pipe I far from the first air inlet.
[0020] As a preferred technical solution, an adiabatic reaction chamber is provided in the adiabatic reaction zone, there is a gap II between the side wall II of the adiabatic reaction chamber and the inner wall of the shell, and a number of ventilation holes II are provided on the side wall II; the air guide pipe I, the gap II, and the ventilation holes II are connected in sequence to form an air inlet passage II.
[0021] As a preferred technical solution, an air guide pipe II is provided in the adiabatic reaction chamber, a number of air collecting holes II are provided on the pipe wall of the air guide pipe II, the pipe orifice at the end of the air guide pipe II close to the air guide pipe I is closed, and the pipe orifice at the end far from the air guide pipe I is communicated with the air outlet.
[0022] As a preferred technical solution, the air guide pipe II extends axially and is located at the center of the adiabatic reaction chamber.
[0023] As a preferred technical solution, a gas distributor is provided between the pipe orifice at the end of the air guide pipe I far from the first air inlet and the adiabatic reaction zone.
[0024] In the heat exchange reaction chamber, an isothermal reaction catalyst is filled between the side wall I and the air guide pipe I; in the adiabatic reaction chamber, an adiabatic reaction catalyst is filled between the side wall II and the air guide pipe II.
[0025] The present utility model further provides a conversion reactor, using any one of the above fixed bed reactors as the conversion reactor.
[0026] The feed gas consists of a first inlet gas and a second inlet gas; the first inlet gas enters through the first inlet, successively flows through the first inlet, gap I, ventilation hole I (inlet channel I) into the heat exchange reaction chamber, and after heat exchange reaction, successively flows through the gas collecting hole I, gas guide pipe I, gas distributor, gap II, ventilation hole II (inlet channel II) into the adiabatic reaction chamber; the second inlet gas enters through the second inlet, successively flows through the gas guide pipe I, gas distributor, gap II, ventilation hole II (inlet channel II) into the adiabatic reaction chamber; the gas in the adiabatic reaction chamber flows out through the gas collecting hole II, gas guide pipe II, and outlet after adiabatic reaction. The liquid medium flowing in the liquid medium heat exchange component is water, preferably boiler water. The gas medium flowing in the gas medium heat exchange component is the feed gas to be preheated. After being preheated in the gas medium heat exchange component, the feed gas flows into the first inlet and the second inlet respectively. The intake volume of the first inlet gas: the intake volume of the second inlet gas = (10 - 80):(30 - 100), preferably (30 - 50):(40 - 80); more preferably, the first inlet gas accounts for 40% of the feed gas: the second inlet gas accounts for 60% of the feed gas. The feed gas is preferably syngas; the gas discharged from the outlet is shifted gas. In the syngas, the dry basis volume content of carbon monoxide is 30% - 90%; and / or, in the syngas, the volume ratio of water to absolutely dry gas is 0.1 - 1.6. The temperature of the gas discharged from the outlet is ≥400°C.
[0027] Advantages of the present utility model:
[0028] (1) The reactor provided by the present utility model has a wide range of applications and can be applicable to feeds with a dry basis volume content of carbon monoxide of 30% - 90% and a volume ratio of water to absolutely dry gas of 0.1 - 1.6.
[0029] (2) The isothermal reactor of the present utility model adopts an axial-radial structure, shortening the length of the synthesis gas flow path, reducing the pressure drop of the reactor, thus saving the downstream compression power consumption and being beneficial to reducing the energy consumption of the whole device, belonging to an energy-saving device.
[0030] (3) The present utility model sets up a double heat exchange channel of air cooling and water cooling in the isothermal reaction zone to timely remove the reaction heat, thereby being able to effectively control the temperature of the shifted gas in the isothermal zone and making the reaction proceed in the positive direction. Saturated steam is obtained at the outlet of the water cooling channel, realizing the maximum utilization of energy.
[0031] (4) The present utility model adopts an axial-radial dual-channel reactor. Since the reactor has two channels of water cooling and air cooling, and utilizes the principle of different heat transfer coefficients of liquid and gas, the outer side where the reaction is relatively intense is cooled by a liquid with a larger heat transfer coefficient, and the inner side where the reaction is relatively mild is cooled by a gas with a smaller heat transfer coefficient. Thus, it better ensures the temperature uniformity 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 transfer areas on the inner and outer sides. The outer side has a larger heat transfer area, which exactly corresponds to the part where the reaction heat release is intense and takes more heat. The inner side has a smaller heat transfer area, which corresponds to the part where the reaction heat release temperature is lower and takes less heat.
[0032] (5) While producing by-product saturated steam, it can also preheat the raw syngas to above the catalyst activation temperature. The present utility model is provided with a raw syngas bypass inlet. The raw syngas injected from the bypass is mixed with the raw reformed gas obtained from the outlet of the air-cooling channel in the upper isothermal zone. Since the raw reformed gas obtained from the outlet of the air-cooling channel has been preheated to above the catalyst activation temperature, the raw syngas entering from the bypass can reach the activation temperature without being separately heated to the activation temperature, directly saving the equipment investment of the raw syngas preheater, reducing the complexity of the process, and more importantly, avoiding the leakage problem caused by the stress concentration of the tube sheet due to the too large temperature difference between the shell side and the tube side of the conventional raw syngas preheater.
[0033] (6) The present utility model adopts a staged reaction technology. A radial adiabatic reaction zone is set in the lower section of the furnace body. By adjusting the intake of the raw syngas entering from the bypass inlet, the water-gas ratio, CO content, and the outlet temperature of the reformed gas of the mixed reformed gas entering the adiabatic reaction zone can be flexibly and effectively adjusted and controlled. By effectively adjusting the outlet temperature of the reformed gas 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 impact on the steam production pressure, but also solving the problems of easy overheating and difficult temperature control in the reforming reaction of raw gas with a high CO content. Description of the Drawings
[0034] Figure 1 Schematic diagram of an embodiment of a fixed-bed reactor;
[0035] Figure 2 Cross-sectional schematic diagram of an embodiment of a fixed-bed reactor;
[0036] Figure 3 Partial schematic diagram of a heat exchange component;
[0037] Figure 4 Schematic diagram of another embodiment of a fixed-bed reactor;
[0038] In the figure, 1 is the housing, 11 is the first air inlet, 12 is the second air inlet, 13 is the air outlet; 14 is the heat exchange reaction chamber, 141 is the vent hole I, 15 is the air duct I, 151 is the air collecting hole I; 50 is the adiabatic reaction chamber, 501 is the vent hole II, 51 is the catalyst, 52 is the porcelain ball, 16 is the air duct II, 161 is the air collecting hole II, and 43 is the gas distributor; 41 is the heat exchange component, 200 is the air medium plate heat exchange plate, and 210 is the liquid medium heat exchange plate; 20 is the air medium inlet, 201 is the air medium inlet pipe, 202 is the air medium distribution loop pipe, 203 is the air medium rising pipe, 204 is the preheated air rising pipe, 205 is the preheated air collecting loop pipe, 206 is the preheated air rising main pipe, and 18 is the preheated air outlet; 21 is the liquid medium inlet, 211 is the liquid medium inlet main pipe, 212 is the liquid medium distribution loop, 213 is the liquid medium rising pipe, 214 is the steam rising pipe, 215 is the steam collecting loop pipe, 216 is the steam rising main pipe, 22 is the steam outlet, and 28 is the expansion joint. Detailed implementation mode
[0039] The following are only the preferred implementation modes of the present invention, and are not intended to limit the protection scope of the present invention. All technical solutions falling within the idea of the present invention should fall within the protection scope of the present invention. For professional technicians in the technical field, minor improvements made to the present invention without departing from the principle of the present invention should also fall within the protection scope of the present invention.
[0040] Example 1 Fixed bed reactor
[0041] As Figure 1 shown, the fixed bed reactor has a housing 1 (with a heat insulation layer on the outer periphery) and a hollow reaction chamber. The top and bottom of the housing are respectively provided with an air inlet and an air outlet. A partition is provided inside the housing 1. In the direction from the air inlet to the air outlet, the partition divides the hollow reaction chamber into a heat exchange reaction zone and an adiabatic reaction zone. A heat exchange reaction chamber is provided in the heat exchange reaction zone. A heat exchange component is provided in the heat exchange reaction chamber to timely remove the reaction heat in the heat exchange reaction chamber. The heat exchange component includes a liquid medium heat exchange component and an air medium heat exchange component.
[0042] Example 2 Fixed bed reactor
[0043] The structure of the fixed bed reactor, as Figure 1 、 Figure 2 shown, has a housing 1 (with a heat insulation layer on the outer periphery) and a hollow reaction chamber. The top and bottom of the housing are respectively provided with an air inlet and an air outlet 13. The air inlet is composed of a first air inlet 11 and a second air inlet 12. A partition is provided inside the housing 1. In the direction from the air inlet to the air outlet, the partition divides the hollow reaction chamber into a heat exchange reaction zone and an adiabatic reaction zone. A heat exchange reaction chamber 14 is provided in the heat exchange reaction zone.
[0044] There is a heat exchange reaction chamber 14 in the heat exchange reaction zone. A number of ventilation holes I 141 (outer air inlet annulus) are provided on the side wall I of the heat exchange reaction chamber 14. There is a gap I (annular gap) between the side wall I and the inner wall of the housing 1. The first air inlet 11, the gap I, and the ventilation holes I 141 are connected in sequence to form an air inlet passage I. A guide pipe I 15 is provided in the heat exchange reaction chamber 14, located at the axial center of the heat exchange reaction chamber 14 and extending along its axis. A number of air collecting holes I 151 (inner air inlet annulus) are provided on the pipe wall of the guide pipe I 15. The second air inlet 12 is connected to the guide pipe I. One end of the guide pipe I 15 close to the first air inlet 11 ( Figure 2 the upper end in) has its pipe orifice closed, and one end of the guide pipe I 15 far from the first air inlet 11 ( Figure 2 the lower end in) has its pipe orifice connected to the adiabatic reaction zone through a gas distributor 43. A heat exchange component is provided in the heat exchange reaction chamber 14 for timely removing the reaction heat in the heat exchange reaction chamber 14. The heat exchange component includes a liquid medium heat exchange component and a gas medium heat exchange component; the gas medium heat exchange component is composed of a number of gas medium heat exchange plates, and the liquid medium heat exchange component is composed of a number of liquid medium heat exchange plates.
[0045] There is an adiabatic reaction chamber 50 in the adiabatic reaction zone. There is a gap II (annular gap) between the side wall II of the adiabatic reaction chamber 50 and the inner wall of the housing. A number of ventilation holes II 501 are provided on the side wall II. One end of the guide pipe I 15 far from the first air inlet 11 ( Figure 2 the lower end in) has its pipe orifice, the gap II, and the ventilation holes II 501 connected in sequence to form an air inlet passage II. A guide pipe II 16 is provided in the adiabatic reaction chamber 50, located at the axial center of the adiabatic reaction chamber 50 and extending along its axis. A number of air collecting holes II 161 are provided on the pipe wall of the guide pipe II 16. One end of the guide pipe II 16 close to the guide pipe I 15 ( Figure 2 the upper end in) has its pipe orifice closed, and one end of the guide pipe II 16 far from the guide pipe I 15 ( Figure 2 the lower end in) has its pipe orifice connected to the air outlet 13.
[0046] Example 3 Fixed Bed Reactor
[0047] The structure of the fixed bed reactor is as Figure 1 、 Figure 3 shown, having a housing 1 (with a thermal insulation layer on the outer periphery) and a hollow reaction chamber. An air inlet and an air outlet 13 are respectively provided at the top and bottom of the housing. The air inlet is composed of a first air inlet 11 and a second air inlet 12. A partition is provided in the housing 1. In the direction from the air inlet to the air outlet, the partition divides the hollow reaction chamber into a heat exchange reaction zone and an adiabatic reaction zone. A heat exchange reaction chamber 14 is provided in the heat exchange reaction zone.
[0048] The heat exchange reaction chamber 14 is provided with a heat exchange component 41 for timely removing the reaction heat in the heat exchange reaction chamber 14. The heat exchange component 41 is composed of a number of double-channel heat exchange plates. Each double-channel heat exchange plate is formed by integrating a single liquid medium heat exchange plate and a single gas medium heat exchange plate. A number of double-channel heat exchange plates are arranged in a central radial pattern. The gas medium heat exchange plate is close to the gas guide pipe I 15, and the liquid medium heat exchange plate is far from the gas guide pipe I 15. The liquid medium heat exchange plate circulates water source as the heat exchange medium, and the gas medium heat exchange plate circulates the to-be-preheated crude synthesis gas as the heat exchange medium. The heat exchange component 41 is provided with a gas medium inlet 20, a preheated gas outlet 18 (the gas medium is discharged after being preheated), a liquid medium inlet 21, and a steam outlet 22 (the liquid medium is discharged in the form of steam). The preheated gas outlet 18 is communicated with the air inlet.
[0049] Example 4 Shift Reactor
[0050] As Figure 1 shown, the shift reactor has a shell 1 (with a heat insulation layer on the outer periphery) and a hollow reaction chamber. The top, side wall and bottom of the shell are respectively provided with a first air inlet 11 (the main inlet of the crude synthesis gas), a second air inlet 12 (the side inlet of the crude synthesis gas), and an air outlet 13 (the shift gas outlet). In order to make the raw material gas distribution more uniform, a gas distributor can be arranged at the first air inlet 11. The interior of the shift reactor is separated by a partition plate into an upper section and a lower section. The upper section is a heat exchange reaction zone (isothermal zone) for isothermal shift reaction; the lower section is a radial adiabatic zone for adiabatic shift reaction.
[0051] As Figure 2 shown, a heat exchange reaction chamber 14 is arranged in the heat exchange reaction zone, sleeved in the upper half of the furnace body 1 (shell). The side wall I of the heat exchange reaction chamber 14 is provided with a number of air vent holes I 141 (outer air inlet annulus). There is a gap I (annular gap) between the side wall I and the inner wall of the shell 1. The first air inlet 11, the gap I, and the air vent holes I 141 are sequentially communicated to form an air inlet passage I. The axial center of the heat exchange reaction chamber 14 is provided with a gas guide pipe I 15, extending along its axial direction. The pipe wall of the gas guide pipe I 15 is provided with a number of air collecting holes I151 (inner air inlet annulus). The second air inlet 12 is communicated with the lower half of the gas guide pipe I. The upper end pipe orifice of the gas guide pipe I15 is closed, and the lower end pipe orifice is communicated with the adiabatic reaction zone through a gas distributor 43.
[0052] As Figure 2As shown in the figure, an adiabatic reaction chamber 50 is provided in the adiabatic reaction zone. There is a gap II (annular gap) between the side wall II of the adiabatic reaction chamber 50 and the inner wall of the shell. The side wall II is provided with a number of vent holes II 501. The lower end pipe orifice of the conduit I 15, the gap II, and the vent holes II 501 are connected in sequence to form an intake passage II (annular passage). A conduit II 16 is provided at the axial center of the adiabatic reaction chamber 50, which is located at the axial center of the adiabatic reaction chamber 50 and extends along its axis. The pipe wall of the conduit II 16 is provided with a number of air collecting holes II 161. The upper end pipe orifice of the conduit II 16 is closed, and the pipe orifice far from the lower end of the conduit I 15 is connected to the air outlet 13. The gas flow direction is from the first intake port 11, then enters the annular space between the heat exchange reaction chamber 14 and the shell, passes through the vent holes I 141, then enters the conduit I 15, and then enters the adiabatic reaction chamber 50 through the gas distributor 43, successively passes through the vent holes II 501, the catalyst 51, the porcelain balls 52, and finally flows out from the air outlet 13.
[0053] As Figure 3 As shown in the figure, a heat exchange component 41 is provided in the heat exchange reaction chamber 14 for timely removing the reaction heat in the heat exchange reaction chamber 14. The heat exchange component 41 is composed of a number of double-channel heat exchange plates. Each double-channel heat exchange plate is integrated by a single liquid medium heat exchange plate and a single gas medium heat exchange plate. A number of double-channel heat exchange plates are arranged in a central radial pattern. The gas medium heat exchange plate is close to the conduit I 15, and the liquid medium heat exchange plate is far from the conduit I 15. The liquid medium heat exchange plate circulates water source as the heat exchange medium, and the gas medium heat exchange plate circulates the to-be-preheated crude synthesis gas as the heat exchange medium. The heat exchange component 41 is provided with a gas medium inlet 20, a preheated gas outlet 18 (the gas medium is discharged after being preheated), a liquid medium inlet 21, and a steam outlet 22 (the liquid medium is discharged in the form of steam). The preheated gas outlet 18 is respectively connected to the first intake port 11 and the second intake port 12.
[0054] The raw syngas enters the heat exchange reaction chamber 14 through the first air inlet 11, the gap I, and the air vent I 141 (air inlet passage I). The heat exchange reaction chamber 14 is suspended, and the gas guide pipe I 15 axially extends and is sleeved in the center of the heat exchange reaction chamber for collecting the converted gas and sending it to the adiabatic reaction zone. Inside the heat exchange reaction chamber 14, a heat exchange reaction catalyst (catalyst cartridge) is filled between the side wall I and the gas guide pipe I. In the radial adiabatic zone, the adiabatic reaction chamber 50 is suspended inside the shell. Inside the adiabatic reaction chamber, a catalyst 51 and porcelain balls 52 are filled between the side wall II and the gas guide pipe II. The converted gas after heat exchange reaction enters the gas guide pipe I 15 through the gas collecting hole I 151, and successively flows through the gas distributor, the gap II, and the air vent II (air inlet passage II) and enters the adiabatic reaction chamber. The upper maintenance opening 34 is used for loading and unloading the upper isothermal section catalyst and for maintaining the heat exchange module. The middle maintenance opening 35 is used for loading the lower adiabatic section catalyst and for inspection and maintenance of the adiabatic section. The lower maintenance opening 36 is used for discharging the lower adiabatic section catalyst; the pressure grid 42 is used for fixing the catalyst bed.
[0055] The liquid medium heat exchange plate circulates water source as the heat exchange medium, and the gas medium heat exchange plate circulates the raw syngas to be preheated as the heat exchange medium. While producing by-product saturated steam, it can also preheat the raw syngas to above the catalyst activation temperature, reducing the investment cost of the preheater.
[0056] The liquid medium inlet 21 (boiler water inlet), the liquid medium inlet main pipe 211, the liquid medium distribution ring 212, several liquid medium riser pipes 213, the liquid medium heat exchange plate 210, several steam riser pipes 214, the steam outlet 22 (discharged in the form of steam), the steam collecting ring pipe 215, and the steam riser main pipe 216 are connected in sequence. Among them, several liquid medium riser pipes 213 are evenly distributed on the liquid medium distribution ring 212, and each liquid medium riser pipe 213 is respectively connected to 1 liquid medium heat exchange plate 210. Several steam riser pipes 214 are evenly distributed on the steam collecting ring pipe 215, and the steam collecting ring pipe 215 sends the saturated steam out of the boundary through the steam riser main pipe 216.
[0057] Gas medium inlet 20 (raw syngas preheating inlet), gas medium inlet pipeline 201, gas medium distribution loop pipe 202, several gas medium (raw syngas) riser pipes 203, gas medium heat exchange plate 200, several preheated gas (raw syngas) riser pipes 204, preheated gas outlet 18, preheated gas (raw syngas) collection loop pipe 205, and preheated gas (raw syngas) riser main pipe 206 are connected in sequence. Among them, several gas medium riser pipes 203 are evenly distributed on the gas medium distribution loop 202, and each gas medium riser pipe 203 is respectively connected to 1 gas medium heat exchange plate 200. Several preheated gas riser pipes 204 are evenly distributed on the preheated gas collection loop pipe 205. The preheated gas collection loop pipe 205 discharges the preheated raw syngas through the preheated gas riser main pipe 206 and the preheated gas outlet 18, and then enters the inlet. Preferably, 40% is introduced into the first inlet, and 60% is introduced into the second inlet.
[0058] As Figure 2 shown, the preheated gas outlet 18 is located outside the reactor. After the preheated gas passes through the heat exchange plate, it is discharged from the preheated gas outlet 18 at the top of the reactor and then enters the first inlet 11. This inlet method can adjust the amounts of raw syngas and preheated syngas, and the adjustment is flexible. An expansion joint 28 is provided in the middle of each steam riser pipe 214 and each preheated gas riser pipe 204, effectively solving the problem of thermal expansion caused by the temperature difference in the upper section of the reactor.
[0059] As Figure 4 shown, the preheated gas outlet 18 is located inside the reactor. The preheated gas may not be discharged from the reactor through the preheated gas outlet 18. The preheated gas outlet 18 is located inside the reactor and is directly connected to the gap I, that is, the preheated gas directly enters the gap I through the preheated gas outlet 18. This inlet method does not require the preheated raw syngas to bypass outside the reactor, and the heat loss is small, but the gas volume adjustability is poor. An expansion joint 28 is provided in the middle of each steam riser pipe 214, effectively solving the problem of thermal expansion caused by the temperature difference in the upper section of the reactor.
[0060] The first inlet gas enters the heat exchange reaction chamber 14 through each vent hole I 141 from the inlet passage I. During the reaction process, the heat generated by the catalyst bed is taken away by the heat exchange component 41 in a timely manner. The converted gas after the reaction is collected into the gas guide pipe I 15 through each gas collecting hole I 151 and mixed with the raw synthesis gas from the second inlet 12 to obtain the mixed converted gas. Due to the top of the adiabatic reaction zone being closed and the top of the gas guide pipe II 16 being closed, the mixed converted gas from the heat exchange reaction zone is dispersed by the gas distributor 43 and then flows along the inner wall of the housing 1. In the radial direction, it enters the adiabatic reaction chamber through the vent hole II 501. After the reaction, it is collected into the gas guide pipe II 16 through the gas collecting hole II 161, and the converted gas is discharged from the housing 1 through the outlet 13. If the activity of the catalyst decreases in the later stage of the reaction, or the temperature of the converted gas outlet is too low, the temperature of the converted gas outlet can be increased by adjusting the inlet gas volume on the synthesis gas side to 75% to ensure the temperature of the downstream heat exchange system.
[0061] The raw material gas (raw synthesis gas, with the dry - basis volume content of carbon monoxide being 30% - 90% and the volume ratio of water to absolutely dry gas being 0.1 - 1.6) is composed of the first inlet gas (40% of the total inlet gas) and the second inlet gas (60% of the total inlet gas). The first inlet 11 is located at the top of the housing 1, and the second inlet 12 is located in the middle of the housing 1. The first inlet gas enters the housing 1 through the first inlet, and the second inlet gas enters the housing 1 through the second inlet 12 as a bypass. The second inlet is communicated with the lower - end pipe orifice of the gas guide pipe I. By adjusting the inlet gas volume of the bypass synthesis gas, the water - gas ratio and the CO content of the mixed converted gas entering the adiabatic reaction zone can be controlled, thereby effectively adjusting the temperature of the converted gas outlet. The structure of the radial adiabatic reaction zone is similar to that of the heat exchange reaction zone, but there is no heat exchange channel. Therefore, the temperature of the converted gas outlet after the reaction can reach above 400 °C.
Claims
1. A fixed bed reactor, comprising a shell and a hollow reaction chamber, wherein the top and bottom of the shell are provided with an air inlet and an air outlet, respectively, and characterized in that: A partition is provided in the shell, and in the direction from the air inlet to the air outlet, the partition divides the hollow reaction chamber into a heat exchange reaction zone and an adiabatic reaction zone; A heat exchange reaction chamber is provided in the heat exchange reaction zone; A heat exchange component is provided in the heat exchange reaction chamber; the heat exchange component exchanges heat with the heat exchange reaction chamber; The heat exchange component includes a liquid heat exchange component and a gas heat exchange component; The gas medium heat exchange component has a gas medium inlet and a gas medium outlet, and the gas medium outlet is communicated with the air inlet.
2. The fixed bed reactor according to claim 1, characterized in that An air duct I is provided in the heat exchange reaction chamber, and a plurality of air collecting holes I are provided on the wall of the air duct I. The pipe opening of the air duct I close to the first air inlet is closed, and the pipe opening away from the first air inlet is connected to the adiabatic reaction zone.
3. The fixed bed reactor according to claim 2, characterized in that The air guide pipe I is inside the heat exchange reaction chamber, extends axially, and is located at the center of the axis.
4. The fixed bed reactor according to claim 3, characterized in that The gas-medium heat exchange component is composed of a plurality of gas-medium heat exchange plates; each gas-medium heat exchange plate extends radially in the heat exchange reaction chamber; the plurality of gas-medium heat exchange plates are arranged in a central radial manner with the axial center of the heat exchange reaction chamber as the center; the gas-medium heat exchange component has a gas-medium inlet and a preheating gas outlet, and the preheating gas outlet is connected to the gas inlet.
5. The fixed bed reactor according to claim 4, characterized in that The liquid heat exchange assembly is composed of a plurality of liquid heat exchange plates; each liquid heat exchange plate is in the heat exchange reaction chamber and extends radially; the plurality of liquid heat exchange plates are arranged in a central radial manner with the axial center of the heat exchange reaction chamber as the center.
6. The fixed bed reactor according to claim 5, characterized in that The liquid medium heat exchange plate and the gas medium heat exchange plate are integrated into one; the gas medium heat exchange plate is close to the axial center of the heat exchange reaction chamber, and the liquid medium heat exchange plate is far away from the axial center of the heat exchange reaction chamber.
7. The fixed bed reactor according to claim 6, characterized in that The air inlet is composed of a first air inlet and a second air inlet; A gap I is left between the side wall I of the heat exchange reaction chamber and the inner wall of the shell, and the side wall I is provided with a plurality of vents I; the first air inlet, the gap I, and the vents I are connected in sequence to form an air inlet channel I; The second air inlet is connected to the air duct I; the second air inlet is connected to the pipe opening of the air duct I away from the first air inlet; And / or, the preheating gas outlet is connected to the gap I.
8. The fixed bed reactor according to claim 7, characterized in that An adiabatic reaction chamber is provided in the adiabatic reaction zone, a gap II is left between the side wall II of the adiabatic reaction chamber and the inner wall of the shell, and a plurality of vents II are provided on the side wall II; the air guide pipe I, the gap II, and the vents II are connected in sequence to form an air inlet channel II; An air guide pipe II is provided in the adiabatic reaction chamber, and a plurality of air collecting holes II are provided on the wall of the air guide pipe II. The pipe opening of the air guide pipe II close to one end of the air guide pipe I is closed, and the pipe opening away from one end of the air guide pipe I is connected to the air outlet; The air guide pipe II extends axially and is located at the center of the adiabatic reaction chamber.
9. The fixed bed reactor according to claim 8, characterized in that A gas distributor is provided between the pipe opening of the air guide pipe 1 away from the first air inlet and the adiabatic reaction zone; And / or, in the heat exchange reaction chamber, an isothermal reaction catalyst is filled between the side wall I and the air guide pipe I; And / or, in the adiabatic reaction chamber, an adiabatic reaction catalyst is filled between the side wall II and the air guide pipe II.
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.