Isothermal adiabatic coupled shift reactor and process thereof
By setting up partitioned heat exchange and crude syngas side inlet in the isothermal-adiabatic double-conversion coupled reactor, the temperature regulation problem and superheated steam by-product problem in isothermal conversion technology are solved, achieving efficient energy utilization and equipment simplification.
Patent Information
- Application Number
- CN202411093751.2
- Authority / Receiving Office
- CN · China
- Patent Type
- Applications(China)
- Current Assignee / Owner
- Filing Date
- 2024-08-09
- Publication Date
- 2026-02-10
AI Technical Summary
Existing isothermal conversion technology has problems such as the inability to produce high-quality superheated steam as a byproduct, difficulty in temperature regulation, and high equipment complexity, especially the difficulty in controlling the removal of reaction heat when the load changes.
A dual-conversion coupled isothermal-adiabatic reactor is designed. By setting up partitioned heat exchange and crude syngas side inlet in the upper reaction zone, the heat of reaction can be removed in real time and the temperature can be flexibly adjusted, producing high-pressure superheated steam as a byproduct.
Stable control of reactor temperature under different operating conditions was achieved, high-pressure superheated steam was produced as a byproduct, the process was simplified, and equipment investment and energy consumption were reduced.
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Figure CN121490671A_ABST
Abstract
Description
TECHNICAL FIELD
[0001] The present application relates to the technical field of carbon monoxide conversion, in particular to an isothermal adiabatic coupled conversion reactor and a process thereof. BACKGROUND
[0002] The purpose of CO conversion is to adjust the concentration of H2 and CO in the synthesis gas to meet the needs of downstream users. According to the characteristics of the CO reaction as a strong exothermic reaction, there are currently the following types of reactors:
[0003] (1) Axial reactor. The inside of the axial reactor is filled with catalyst, and the conversion gas passes through the catalyst bed from the axial direction to carry out the adiabatic conversion reaction. The characteristic of this reactor is simple structure and large amount of catalyst loading. However, since all the conversion gas needs to pass through the entire catalyst bed, the pressure drop of the conversion gas is large, especially in the case of catalyst breakage at the end, the pressure drop caused by the conversion furnace is large, which leads to the increase of the pressure drop of the entire conversion system. In the case of reaction of crude synthesis gas with high water-gas ratio and high CO, it is easy to cause over-temperature. Therefore, the axial reactor is only suitable for low-temperature conversion with small adiabatic temperature rise and strict requirements on water-gas ratio.
[0004] (2) Axial-radial reactor. Unlike the axial reactor, the flow direction of the conversion gas in the axial-radial reactor is along the radial direction of the reactor, from the outside to the inside through the catalyst bed, and then flows out of the reactor after entering the center pipe. The gas distribution of this type of reactor is stable and is not affected by the catalyst loading density, and the bed pressure drop is small; compared with the axial conversion furnace under the same working condition, the shell temperature is lower, the equipment diameter and wall thickness are small, and the equipment investment is low.
[0005] Both of the above two types of conversion furnaces use adiabatic reactors. Since the conversion reaction is a strong exothermic reaction and a thermodynamic process, the conversion process adopts a multi-stage and multi-heat exchange reaction mode in the process setting. This results in a series of problems such as relatively complex traditional process conversion process, high heat loss, high steam consumption, and high equipment cost.
[0006] (3) Full isothermal reactor. The isothermal reactor removes the reaction heat in time through the physical method of "water heat removal", which can maintain the catalyst bed at a stable low temperature and ensure high CO conversion rate. The advantages of isothermal conversion technology compared with traditional adiabatic conversion are as follows: first, the isothermal conversion removes the reaction heat in time, and maintains the stable operation of the catalyst bed at a lower temperature. Second, the by-product steam greatly reduces the energy consumption. Third, the process flow is simplified, the system pressure drop is reduced, and the device investment is reduced.
[0007] But the isothermal shift technology applied at present has the following problems: ① The steam produced by the isothermal shift converter drum is saturated steam, which cannot produce higher quality superheated steam. The shift device is a steam surplus device, and usually the surplus steam is used by other users in the plant through the steam pipe network. However, the saturated steam is prone to produce condensate due to the decrease in temperature, and cannot enter the pipe network. The outlet temperature of the traditional adiabatic shift converter is usually above 400 DEG C, which can superheat the saturated steam. However, the outlet temperature of the isothermal shift converter is only about 300 DEG C due to the fact that most of the reaction heat is taken away by the water circulation system, and thus the isothermal shift converter cannot provide a superheating source, and can only set a heating furnace or be combined with other devices, which increases the complexity of the process and the equipment investment. ② The temperature of the isothermal shift converter is difficult to adjust. Due to the influence of factors such as upstream load variation, water-gas ratio fluctuation and catalyst temperature increase at the end of the period, the outlet temperature of the shift converter needs to be adjusted frequently. Since the water circulation between the drum and the heat exchange pipe is a natural circulation, that is, the water vapor circulation is formed by using the static pressure head of water and the driving force generated by the density difference of the two-phase flow in the heat exchange pipe, and thus it is difficult to control the removal of the reaction heat. SUMMARY
[0008] The isothermal-adiabatic dual shift coupled reactor and process provided by the present application can cope with different start-up conditions and load changes, can flexibly adjust the working conditions, has a short process, has less total equipment investment, can produce high-pressure superheated steam as a byproduct, and the like.
[0009] The upper reaction zone of the reactor of the present application adopts radial feeding, which solves the problem of large pressure drop in the reactor. By setting a partitioned heat exchange mode in the upper reaction zone, the excess heat generated by the reaction can be removed in time, energy is maximally utilized, and the over-temperature phenomenon in the adiabatic reactor is solved. By setting a crude synthesis gas side inlet, different start-up conditions and load changes and other special conditions can be coped with. By increasing an adiabatic reaction section at the lower part of the reactor, the outlet temperature of the reactor can be maintained above 400 DEG C, and then high-pressure saturated steam is superheated, and the energy utilization rate is improved.
[0010] According to one aspect of the present application, an isothermal-adiabatic coupled shift reactor is provided, comprising a furnace body, a crude synthesis gas main inlet, a crude synthesis gas preheating outlet and a high-pressure saturated steam outlet being arranged at the top of the furnace body, and a shift gas outlet being arranged at the bottom of the furnace body.
[0011] The furnace body is sequentially divided into an isothermal section and an adiabatic section from top to bottom. A crude synthesis gas side inlet is arranged between the furnace bodies of the isothermal section and the adiabatic section. A high-pressure boiler water inlet and a crude synthesis gas preheating inlet are arranged on the furnace body of the isothermal section close to the direction of the crude synthesis gas side inlet.
[0012] The high-pressure boiler water inlet is communicated with the high-pressure saturated steam outlet after passing through the isothermal section. The crude synthesis gas preheating inlet is communicated with the crude synthesis gas preheating outlet after passing through the isothermal section.
[0013] The isothermal section is provided with a catalyst cylinder which is sleeved in the furnace body and forms a gap with the inner wall of the furnace body, and the gap forms a gas passage which communicates with the main inlet of the crude synthetic gas;
[0014] The catalyst cylinder is sleeved with a center pipe I, the upper end of the center pipe I is closed, and the lower end communicates with the adiabatic section; the side wall of the center pipe I is provided with a plurality of inner gas inlet annular gaps;
[0015] The reaction zone is between the catalyst cylinder and the center pipe I.
[0016] Optionally, the crude synthetic gas preheating outlet communicates with the gap, that is, the crude synthetic gas preheating outlet is located inside the reactor, and the preheated crude synthetic gas does not discharge out of the reactor through the crude synthetic gas preheating outlet, but directly enters the gap.
[0017] Optionally, a plurality of plate cooling units are arranged in the reaction zone, and the plate cooling units are arranged radially with the center pipe I as the center; the inlet of the plate cooling unit is connected with a refrigerant input pipeline, and the outlet of the plate cooling unit is connected with a refrigerant output pipeline.
[0018] Optionally, the plate cooling unit includes a high-pressure boiler water passage and a crude synthetic gas preheating passage; the refrigerant input pipeline includes a high-pressure boiler water rising pipe and a crude synthetic gas rising pipe; the refrigerant output pipeline includes a high-pressure saturated steam rising pipe and a preheated crude synthetic gas rising pipe;
[0019] The high-pressure boiler water rising pipe communicates with the high-pressure saturated steam rising pipe through the high-pressure boiler water passage, and the high-pressure saturated steam rising pipe communicates with the high-pressure saturated steam outlet; the crude synthetic gas rising pipe communicates with the preheated crude synthetic gas rising pipe through the crude synthetic gas preheating passage, and the preheated crude synthetic gas rising pipe communicates with the crude synthetic gas preheating outlet.
[0020] Optionally, the inlet of the high-pressure boiler water passage is connected with a plurality of high-pressure boiler water rising pipes, the plurality of high-pressure boiler water rising pipes are connected to a high-pressure boiler water collecting ball, and the high-pressure boiler water collecting ball is connected to the high-pressure boiler water inlet; the outlet of the high-pressure boiler water passage is connected with a plurality of high-pressure saturated steam rising pipes, the plurality of high-pressure saturated steam rising pipes are connected to a high-pressure saturated steam collecting ring, and the high-pressure saturated steam collecting ring is connected to the high-pressure saturated steam outlet.
[0021] Optionally, the inlet of the crude synthesis gas preheating channel is connected with a plurality of crude synthesis gas risers, which are connected to a crude synthesis gas collection annulus, which is connected to the crude synthesis gas preheating inlet; the outlet of the crude synthesis gas preheating channel is connected with a plurality of preheated crude synthesis gas risers, which are connected to a preheated crude synthesis gas collection ring, which is connected to the crude synthesis gas preheating outlet.
[0022] Optionally, a plurality of protrusions are arranged on the side of the plate cooling unit.
[0023] Optionally, a gas distributor is arranged inside the furnace body and connected with the crude synthesis gas side inlet.
[0024] Optionally, a gas flow guide plate is arranged inside the furnace body and close to the crude synthesis gas side inlet.
[0025] Optionally, an axial reaction catalyst bed is arranged in the adiabatic section.
[0026] Optionally, a radial reaction catalyst bed is arranged in the adiabatic section.
[0027] Optionally, the radial reaction catalyst bed is provided with a center tube II, which is coaxially arranged with the center tube I; a plurality of air holes are arranged on the side wall of the center tube II; the upper end of the center tube II is closed, and the lower end is connected with the shift gas outlet.
[0028] According to another aspect of the present application, a process for reaction using the above-mentioned shift reactor is provided, in which the raw gas is composed of a first gas and a second gas; the first gas enters the furnace body through the preheating and then enters the catalyst cylinder through the crude synthesis gas main inlet, the gap and the outer gas inlet annulus in sequence, and then enters the adiabatic section through the inner gas inlet annulus and the center tube I after isothermal shift reaction; the second gas enters the adiabatic section through the crude synthesis gas side inlet.
[0029] The gas in the adiabatic section is discharged through the shift gas outlet after adiabatic shift reaction.
[0030] Optionally, the first gas enters the adiabatic section through the inner gas inlet annulus, the center tube I, the gas distributor and the gas flow guide plate in sequence after isothermal shift reaction; the second gas enters the adiabatic section through the crude synthesis gas side inlet and then flows through the gas distributor and the gas flow guide plate.
[0031] Optionally, when the adiabatic section is a radial reaction catalyst bed, the gas in the adiabatic section enters the radial reaction catalyst bed from the two sides of the furnace body in the radial direction, and then is discharged through the center tube II and the shift gas outlet after adiabatic shift reaction.
[0032] Optionally, the intake amount of the first intake gas: the intake amount of the second intake gas = 10-80: 30-100; preferably, the intake amount of the first intake gas: the intake amount of the second intake gas = 30-50: 40-80; further preferably, the intake amount of the first intake gas: the intake amount of the second intake gas = 40: 60.
[0033] Optionally, in the crude synthesis gas, the dry basis volume content of carbon monoxide is 30%-90%.
[0034] Optionally, in the crude synthesis gas, the water / absolute dry gas volume ratio is 0.1-1.6.
[0035] Optionally, the gas temperature at the outlet of the shift gas is ≥ 400℃.
[0036] Compared with the prior art, the present application has the following beneficial effects:
[0037] (1) The crude synthesis gas side inlet is arranged, which can flexibly adjust the adiabatic section shift gas outlet temperature according to the subsequent process medium heat exchange needs, and better cope with different start-up conditions and load changes and other special situations.
[0038] (2) The crude synthesis gas needs to be preheated to the catalyst activation temperature before entering the reactor. The isothermal-adiabatic dual shift coupling technology of the present application can remove the excess heat generated by the shift reaction in time, avoid overheating, preheat the crude synthesis gas to the catalyst activation temperature, and produce high-pressure saturated steam by arranging the partition heat exchange in the upper isothermal reaction zone, the crude synthesis gas preheating in the catalyst secondary partition, and the high-pressure saturated steam generation in the catalyst primary partition (or the high-pressure saturated steam generation in the catalyst secondary partition, and the crude synthesis gas preheating in the catalyst primary partition). The former avoids the problem of tube sheet leakage caused by excessive temperature difference on the shell side of the previous crude synthesis gas preheater, and directly removing the preheater can reduce the complexity of the process and equipment investment. The latter produces high-pressure saturated steam to maximize energy utilization.
[0039] (3) The adiabatic reaction section is arranged at the lower part of the reactor, and the outlet temperature of the adiabatic section can reach more than 400℃ under the adjustment of the crude synthesis gas side inlet, which can superheat the high-pressure saturated steam, so that the excess high-pressure superheated steam can be transported stably in the pipe network without producing condensate, ensuring the stability of the downstream heat exchange network. BRIEF DESCRIPTION OF DRAWINGS
[0040] Figure 1 It is a schematic diagram of the reactor external furnace structure of the present application;
[0041] Figure 2 It is a schematic diagram of the reactor internal structure of Example 1;
[0042] Figure 3This is a schematic diagram of the internal structure of the reactor in Example 2;
[0043] Figure 4 This is a schematic diagram (collection ring) of a plate cooling unit (including dual-channel heat exchange) according to the present invention;
[0044] Figure 5 This is a schematic diagram (collecting ball) of a plate cooling unit (including dual-channel heat exchange) according to the present invention;
[0045] Among them, 1-furnace body; 2-high-pressure boiler water inlet; 3-high-pressure saturated steam outlet; 4-crude syngas preheating outlet; 5-crude syngas main inlet; 6-crude syngas preheating inlet; 7-main maintenance port; 8-catalyst top discharge port; 9-crude syngas side inlet; 10-catalyst bottom discharge port; 11-shift gas outlet; 12-high-pressure saturated steam collection ring; 13-preheated crude syngas collection ring; 14-preheated crude syngas riser pipe; 15-heat transfer module; 16-center pipe I; 17-high-pressure boiler water riser pipe; 18-pressure boiler 19- Boiler water collecting ball; 20- Crude syngas riser pipe; 21- Crude syngas collecting annular gap; 22- Isothermal section inspection port; 23- Gas guide plate; 24- High temperature resistant catalyst; 25- Insulation section inspection port; 26- Collector ball inspection port; 27- Gas distributor; 28- Pressure grid; 29- High pressure saturated steam riser pipe; 30- Catalyst cylinder; 31- Ceramic ball; 32- Expansion joint; 33- High pressure boiler water channel; 34- Crude syngas preheating channel; 35- High pressure boiler water collecting ring; 36- Crude syngas collecting ball; 37- Central tube II. Detailed Implementation
[0046] The present invention will be further described below with reference to specific embodiments, but this does not constitute any limitation on the present invention.
[0047] Example 1
[0048] like Figure 1 , Figure 2As shown, a radial isothermal-axial adiabatic dual-conversion coupled reactor includes: furnace body 1, high-pressure boiler water inlet 2, high-pressure saturated steam outlet 3, crude syngas preheating outlet 4, crude syngas main inlet 5, crude syngas preheating inlet 6, main inspection port 7, catalyst upper discharge port 8, crude syngas side inlet 9, catalyst lower discharge port 10, conversion gas outlet 11, high-pressure saturated steam collection ring 12, preheated crude syngas collection ring 13, preheated crude syngas riser pipe 14, heat transfer module (i.e., plate cooling unit) 15, central pipe I 16, high-pressure boiler water riser pipe 17, high-pressure boiler water collection ball 18, crude syngas riser pipe 19, crude syngas collection ring gap 20, isothermal section inspection port 21, gas guide plate 22, high-temperature resistant catalyst 23, adiabatic section inspection port 24, collection ball inspection port 25, gas distributor 26, pressure grid 27, high-pressure saturated steam riser pipe 28, catalyst cylinder 29, ceramic ball 30, and expansion joint 31.
[0049] The reactor body is cylindrical in shape and divided into upper and lower sections. In the upper section, a catalyst cylinder is fitted inside the furnace body, forming a gap between the catalyst cylinder and the furnace body. This gap connects to the main inlet of the crude syngas, forming a syngas inlet channel. A central tube I is located at the center of the catalyst cylinder. The upper end of the central tube I is closed, and the lower end connects to the insulation section. An inner and outer air inlet annular gap are respectively provided on the side wall of the central tube I and the catalyst cylinder. The area between the catalyst cylinder and the central tube I is called the reaction zone, which is filled with partitioned catalyst. The catalyst can be discharged through the catalyst discharge port at the lower end of the reaction zone. To ensure that the upper reaction zone is in an isothermal state and to preheat the crude syngas to the catalyst activation temperature and generate high-pressure saturated steam as a byproduct, this invention incorporates partitioned heat exchange within the reaction zone. The secondary partition of the catalyst is used for crude syngas preheating, while the primary partition is used for generating high-pressure saturated steam. Therefore, multiple plate cooling units are provided in the two partitions of the upper reaction zone of this invention.
[0050] Within the reaction zone, the plate cooling units are arranged radially around the central tube I. The plate cooling units have multiple raised sections on their sides; this arrangement increases fluid turbulence, thereby improving the heat transfer coefficient. Furthermore, for the same heat transfer, a smaller heat exchange area is required, significantly reducing equipment investment. The inlet of the plate cooling unit in the first catalyst zone is connected to the high-pressure boiler water riser pipe. Multiple high-pressure boiler water riser pipes converge and connect to the high-pressure boiler water collection ball, which in turn connects to the high-pressure boiler water inlet. The inlet of the plate cooling unit in the second catalyst zone is connected to the crude syngas riser pipe. Multiple crude syngas riser pipes converge and connect to the crude syngas collection annular gap, which in turn connects to the crude syngas preheating inlet at its lower part. Additionally, a maintenance port is provided below the collection ball for maintenance purposes. The outlets of the plate cooling units in the primary catalyst zone are all connected to high-pressure saturated steam risers. Multiple high-pressure saturated steam risers converge at a high-pressure saturated steam collection ring, and the upper part of the high-pressure saturated steam collection ring is connected to a high-pressure saturated steam outlet to send out the steam. The outlets of the plate cooling units in the secondary catalyst zone are all connected to preheated crude syngas risers. Multiple preheated crude syngas risers converge at a preheated crude syngas collection ring, and the upper part of the preheated crude syngas collection ring is connected to a crude syngas preheating outlet to send out the preheated crude syngas.
[0051] A crude syngas inlet is provided between the upper and lower sections of the furnace body. Syngas from the bypass can be directly and thoroughly mixed with the shift gas flowing out of the upper section's central pipe I, and then pass through the gas distributor and gas guide plate in sequence before entering the lower adiabatic reaction section. By using bypass adjustment, different start-up conditions and load changes can be addressed, allowing for better control of the lower shift gas outlet temperature.
[0052] The radial isothermal-axial adiabatic double shift coupled reactor involves two systems: a two-stage radial-axial double shift reaction system and a steam generation-rough syngas preheating system.
[0053] The flow chart of the two-stage radial-axial double conversion reaction system is as follows: The raw material crude syngas enters the upper head of the furnace body 1 through the main crude syngas inlet 5. It then flows radially through the airflow channels on both sides, passing through the outer air inlet annular gap and sequentially through the primary and secondary catalyst zones. The crude syngas reacts with the catalyst in the reaction zone and simultaneously exchanges heat with the heat transfer module (plate cooling unit) 15. Excess heat is carried away by the high-pressure boiler water and crude syngas raw material in the heat transfer module (plate cooling unit) 15, preventing overheating in the reaction zone. The generated conversion gas is collected in the central tube I 16 through the inner air inlet annular gap on the side wall. The conversion gas flowing out from the bottom of the central tube I 16 mixes with the crude syngas entering through the crude syngas side inlet 9, and sequentially passes through the gas distributor 26 and gas guide plate 22, entering the lower adiabatic reaction zone in a uniform distribution manner. Then, it flows axially into the high-temperature resistant catalyst 23 for conversion reaction. After the reaction, the temperature of the conversion gas is above 400℃ and it is discharged from the conversion gas outlet 11.
[0054] This embodiment adopts an axially adiabatic fixed bed structure, which has a large reaction gas flow area, long residence time, high catalyst efficiency, and a smaller catalyst bed packing height, which can reduce the total length of the reactor and lower equipment investment.
[0055] The furnace body 1 is equipped with a catalyst upper discharge port 8 for loading and unloading the catalyst in the upper isothermal reaction zone; and a catalyst lower discharge port 10 for loading and unloading the catalyst in the lower adiabatic reaction zone. A main inspection port 7 allows maintenance personnel to enter the reactor interior. An isothermal section inspection port 21 and an adiabatic section inspection port 24 are used by maintenance personnel to perform maintenance on the upper and lower parts of the reactor, respectively. Ceramic balls 30 are also arranged inside the furnace body 1 to protect and support the high-temperature resistant catalyst 23 and the catalyst bed in the upper isothermal reaction zone. A pressure grid 27 is used to fix the high-temperature resistant catalyst 23 and the ceramic balls 30. Gas guide plates 22 and gas distributors 26 are used for the distribution and mixing of the reactant gas. An expansion joint 31 is provided in the middle of each high-pressure saturated steam riser pipe 28 and each preheated crude syngas riser pipe 14, effectively solving the problem of thermal expansion caused by temperature differences in the upper section of the reactor.
[0056] The process of the steam generation-crude syngas preheating system is as follows: external high-pressure boiler water is collected in the high-pressure boiler water collection ball 18 through the high-pressure boiler water inlet 2, and then enters the catalyst primary zone in the heat transfer module (plate cooling unit) 15 through the high-pressure boiler water riser pipe 17. The high-pressure boiler water absorbs excess heat in the heat transfer module (plate cooling unit) 15 to avoid overheating in the reaction zone of the catalyst primary zone. After absorbing heat, the high-pressure boiler water forms high-pressure saturated steam, which flows out from the outlet of the heat transfer module (plate cooling unit) 15 and enters the high-pressure saturated steam riser pipe 28, where it is collected in the high-pressure saturated steam collection ring 12, and then flows out from the high-pressure saturated steam outlet 3. External crude syngas is collected in the crude syngas collection annular gap 20 through the crude syngas preheating inlet 6, and then enters the catalyst secondary zone in the heat transfer module (plate cooling unit) 15 through the crude syngas riser pipe 19. The crude syngas absorbs excess heat in the heat transfer module (plate cooling unit) 15 to prevent the temperature in the reaction zone of the catalyst secondary zone from exceeding the limit. After absorbing heat, the temperature of the crude syngas reaches the catalyst activation temperature, flows out from the outlet of the heat transfer module (plate cooling unit) 15 and enters the preheated crude syngas riser pipe 14, where it is collected in the preheated crude syngas collection ring 13, and then flows out from the crude syngas preheating outlet 4.
[0057] like Figure 2 As shown, the crude syngas preheating outlet 4 is located outside the reactor. The preheated crude syngas passes through the heat transfer module 15 and exits the reactor from the crude syngas preheating outlet 4 at the top of the reactor before entering the crude syngas preheating inlet 6. This intake method allows for adjustment of the crude syngas and preheated crude syngas flow rates, providing flexibility. Alternatively, the preheated crude syngas can also exit the reactor without passing through the crude syngas preheating outlet 4 (the crude syngas preheating outlet 4 is located inside the reactor and directly connected to the gap). Figure 2 (Not shown), but instead, it enters the gap directly through the crude syngas preheating outlet 4. This gas intake method does not require the preheated crude syngas to be routed outside the reactor, but the gas volume regulation performance is poor.
[0058] Furthermore, the high-pressure boiler water collecting ball described in this invention can also be replaced by a high-pressure boiler water collecting ring, such as... Figure 4 As shown, the upper end of the high-pressure boiler water riser pipe is connected to the high-pressure boiler water channel 32, and the lower end converges into the high-pressure boiler water collection ring 34; the upper end of the syngas riser pipe is connected to the crude syngas preheating channel 33, and the lower end converges into the crude syngas collection ring; the crude syngas collection ring can also be replaced by a crude syngas collection ball 35, such as... Figure 5 As shown.
[0059] Example 2
[0060] like Figure 3As shown, an isothermal-adiabatic coupled dual radial shift reactor differs from Embodiment 1 in that the lower end of the furnace body is a mixing-radial adiabatic reactor within the reactor cavity. The reaction gas flowing out from the lower end of the gas guide plate passes radially through the shift catalyst bed from both sides to react. The generated shift gas enters the central tube II 36 through the vent holes on the sidewall of the lower section of the reactor, collects within the central tube II 36, and then exits through the shift gas outlet. The adiabatic reaction section allows the shift gas outlet temperature to reach over 400°C, suitable for superheated high-pressure saturated steam.
[0061] This embodiment adopts a radially adiabatic fixed bed structure, in which the reactant gas enters the catalyst bed from the annular gaps on both sides. The flow channel is short and the pressure drop is low, which helps to reduce the power consumption of downstream compression, making it an energy-saving device.
[0062] Any numerical value mentioned in this invention, if there is only a two-unit interval between any minimum and any maximum value, includes all values that increase by one unit each time from the minimum to the maximum value. For example, if the amount of a component, or the value of a process variable such as temperature, pressure, or time, is stated as 50-90, in this specification it means specifically listing values such as 51-89, 52-88… and 69-71 and 70-71, etc. For non-integer values, it may be appropriately considered that a unit is 0.1, 0.01, 0.001, or 0.0001. These are merely some specifically specified examples. In this application, in a similar manner, all possible combinations of numerical values between the listed minimum and maximum values are considered to have been disclosed.
[0063] It should be noted that the embodiments described above are only for explaining the present invention and do not constitute any limitation on the present invention. The present invention has been described with reference to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory terms, not limiting terms. Modifications can be made to the present invention within the scope of the claims, and revisions can be made to the present invention without departing from the scope and spirit of the present invention. Although the present invention described herein relates to specific methods, materials, and embodiments, it does not mean that the present invention is limited to the specific examples disclosed herein; on the contrary, the present invention can be extended to all other methods and applications with the same function.
Claims
1. An isothermal adiabatic coupled shift reactor, characterized in that, The furnace body includes a main crude syngas inlet, a crude syngas preheating outlet, and a high-pressure saturated steam outlet at the top, and a shift gas outlet at the bottom. The furnace body is divided into an isothermal section and an adiabatic section from top to bottom; a crude syngas side inlet is provided between the isothermal section and the adiabatic section of the furnace body; a high-pressure boiler water inlet and a crude syngas preheating inlet are provided on the furnace body of the isothermal section near the crude syngas side inlet; the high-pressure boiler water inlet is connected to the high-pressure saturated steam outlet after passing through the isothermal section; the crude syngas preheating inlet is connected to the crude syngas preheating outlet after passing through the isothermal section. The isothermal section is equipped with a catalyst cylinder, which is fitted inside the furnace body and forms a gap with the inner wall of the furnace body; the gap forms a gas channel connecting the main inlet of the crude syngas; multiple external air inlet annular gaps are provided on the side wall of the catalyst cylinder; a central tube I is fitted inside the catalyst cylinder, the upper end of the central tube I is closed, and the lower end connects to the insulation section; multiple internal air inlet annular gaps are provided on the side wall of the central tube I. The reaction zone is located between the catalyst cylinder and the central tube I.
2. The shift reactor according to claim 1, characterized in that, The reaction zone is equipped with multiple plate cooling units, which are arranged radially around the central tube I; the inlet of each plate cooling unit is connected to a refrigerant input pipe, and the outlet of each plate cooling unit is connected to a refrigerant output pipe. Preferably, the plate cooling unit has multiple protrusions on its side.
3. The shift reactor according to claim 2, characterized in that, The plate cooling unit includes a high-pressure boiler water channel and a crude syngas preheating channel; the refrigerant input pipeline includes a high-pressure boiler water riser and a crude syngas riser; the refrigerant output pipeline includes a high-pressure saturated steam riser and a preheated crude syngas riser. The high-pressure boiler water riser pipe is connected to the high-pressure saturated steam riser pipe via the high-pressure boiler water channel, and the high-pressure saturated steam riser pipe is connected to the high-pressure saturated steam outlet; the crude syngas riser pipe is connected to the preheated crude syngas riser pipe via the crude syngas preheating channel, and the preheated crude syngas riser pipe is connected to the crude syngas preheating outlet.
4. The shift reactor according to claim 3, characterized in that, The inlet of the high-pressure boiler water channel is connected to multiple high-pressure boiler water risers, which converge and connect to a high-pressure boiler water collecting ball, which is connected to the high-pressure boiler water inlet. The outlet of the high-pressure boiler water channel is connected to multiple high-pressure saturated steam risers, which converge to a high-pressure saturated steam collecting ring, which is connected to the high-pressure saturated steam outlet.
5. The shift reactor according to claim 3 or 4, characterized in that, The inlet of the crude syngas preheating channel is connected to multiple crude syngas riser pipes, which converge and connect to a crude syngas collection annular gap. The crude syngas collection annular gap is connected to the crude syngas preheating inlet. The outlet of the crude syngas preheating channel is connected to multiple preheated crude syngas riser pipes, which converge and connect to a preheated crude syngas collection ring. The preheated crude syngas collection ring is connected to the crude syngas preheating outlet.
6. The shift reactor according to any one of claims 1-5, characterized in that, The crude syngas side inlet is connected to a gas distributor inside the furnace body; And / or, the insulation section is provided with a gas guide plate inside the furnace body near the crude syngas inlet.
7. The shift reactor according to any one of claims 1-6, characterized in that, The insulation section is equipped with an axial reaction catalyst bed; And / or, the adiabatic section is provided with a radial reaction catalyst bed; preferably, the radial reaction catalyst bed is provided with a central tube II, the central tube II being coaxially arranged with the central tube I; a plurality of vent holes are provided on the side wall of the central tube II; the upper port of the central tube II is closed, and the lower port is connected to the shift gas outlet.
8. A process for carrying out a reaction using the shift reactor according to any one of claims 1-7, characterized in that, The feed gas consists of a first inlet and a second inlet; the first inlet, after being preheated, enters through the main crude syngas inlet, flows sequentially through the main crude syngas inlet, the gap, and the outer inlet annular gap into the catalyst cylinder, and after the isothermal shift reaction, flows sequentially through the inner inlet annular gap and the central tube I into the adiabatic section; the second inlet enters the adiabatic section through the crude syngas side inlet; The gas in the adiabatic section is discharged through the transformed gas outlet after undergoing an adiabatic transformation reaction.
9. The process according to claim 8, characterized in that, After undergoing an isothermal transformation reaction, the first intake air flows sequentially through the inner intake annular gap, central tube I, gas distributor, and gas guide plate into the adiabatic section; the second intake air enters from the crude syngas side inlet, flows through the gas distributor and gas guide plate into the adiabatic section. Preferably, when the adiabatic section is a radial reaction catalyst bed, the gas in the adiabatic section enters the radial reaction catalyst bed in the radial direction through both sides inside the furnace body, and after the adiabatic transformation reaction, it enters the central pipe II through the vent and is collected, and then discharged through the transformation gas outlet.
10. The process according to claim 8 or 9, characterized in that, 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 air intake volume of the first air intake : the air intake volume of the second air intake = 40 :
60. And / or, the crude syngas contains 30% to 90% carbon monoxide by volume on a dry basis; and / or, the crude syngas contains a water to oven-dry gas volume ratio of 0.1 to 1.
6. And / or, the gas temperature at the outlet of the shift gas is ≥400℃.