Isothermal-adiabatic coupled shift reactor

Abstract

The isothermal-adiabatic coupled shift reactor comprises a furnace body, the top of the furnace body is provided with a crude synthesis gas main inlet, a crude synthesis gas preheating outlet and a high-pressure saturated steam outlet, and the bottom of the furnace body is provided with a shift gas outlet; the furnace body is sequentially divided into an isothermal section and a heat insulation section from top to bottom, and a crude synthesis gas side inlet is formed between the isothermal section and the heat insulation section of the furnace body; 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; the gap forms a gas channel communicated with the heat insulation section; a central pipe I is sleeved in the catalyst cylinder, the upper port of the central pipe I is communicated with the crude synthesis gas main inlet, and the lower port of the central pipe I is closed; a reaction zone is arranged between the catalyst cylinder and the central pipe I; the conversion reactor disclosed by the utility model can cope with different driving working conditions, load change and other conditions, can flexibly adjust the working conditions, is short in flow and low in total investment of equipment, can produce high-pressure superheated steam as a byproduct, and improves the energy utilization rate.

Description

Technical Field

[0001] The utility model relates to the technical field of carbon monoxide conversion, and particularly relates to an isothermal-adiabatic coupling conversion reactor. Background Technique

[0002] With the progress of technology and the increasing demand for energy year by year, coal chemical technology has developed rapidly. The carbon monoxide conversion process plays an important role in coal chemical industry. Up to now, CO conversion reactors are mainly divided into the following types:

[0003] Axial reactors, with simple internal structures, belong to adiabatic reactors. The raw syngas enters the catalyst bed axially for adiabatic reaction. Such a reaction mode is likely to increase the pressure drop at the inlet and outlet of the raw synthesis; meanwhile, the conversion reaction is a strongly exothermic reaction, so it is easy to cause over-temperature inside the adiabatic reaction during the conversion process, resulting in the reaction equilibrium being restricted by thermodynamics.

[0004] Axial-radial reactors, the biggest difference from axial reactors is that the raw syngas passes through the catalyst bed radially and then flows out of the reactor through the gas collecting pipe; compared with the axial feeding mode, radial feeding can largely avoid the pressure drop of the raw syngas. However, since this reactor also belongs to an adiabatic reactor, there is also an over-temperature phenomenon inside the reactor.

[0005] Isothermal reactors. In order to avoid the over-temperature phenomenon in axial and axial-radial reactors, in the past, processes of multi-stage reaction and multi-stage cooling were mostly adopted, but the processes had problems such as too long flow path and large pressure drop. Therefore, corresponding improvements were made for these shortcomings, and isothermal reactors were obtained. For example: Chinese invention patent CN 20201600008167.1 proposed "an axial-radial isothermal reactor". The internal structure of this device distributes plate-type cooling units in a central radial form in the reaction zone for immediate heat extraction. The reaction gas enters the gas distributor through the gas inlet. After being evenly distributed, the reaction gas enters the upper head. Most of the reaction gas enters the gas flow channel and enters the reaction zone through each gas inlet hole. The heat generated during the reaction is taken away by multiple plate-type cooling units in time. The converted gas generated by the reaction enters the central tube through the gas collecting hole and flows out from the outlet at the bottom of the central tube. This technology has well solved the problem of over-temperature in axial and axial-radial reactors. However, there are also some disadvantages. For example, the saturated steam by-produced during the conversion process usually has a large surplus and nowhere to be utilized, and its utilization range is not as wide as that of superheated steam. At the same time, condensate will appear when the subsequent temperature drops, and it cannot be transported through the pipeline network. In addition, when in special situations such as different startup conditions and upstream load changes, it is necessary to continuously adjust the circulation amount of the refrigerant medium, resulting in difficult temperature control inside the reactor.

[0006] At present, although the isothermal reactor has solved the problem of overheating inside the reactor, during the process of heat removal from the reaction, a large amount of saturated steam generated is usually in surplus and has nowhere to be utilized. Its scope of use is not as wide as that of superheated steam. At the same time, condensate is likely to precipitate when the temperature drops, making it impossible to be transported through the steam pipe network. In addition, when in different startup conditions and special situations such as upstream load changes, it is necessary to indirectly control the reaction temperature by adjusting the refrigerant circulation rate, resulting in difficult temperature control inside the reactor. Summary of the Invention

[0007] In view of the problems existing in the prior art, the present invention provides an isothermal-adiabatic double conversion coupling reactor that can cope with different startup conditions and load changes, etc., and can flexibly adjust the working conditions, has a short process flow, low total equipment investment, and can by-produce high-pressure superheated steam.

[0008] In the upper reaction zone of the reactor of the present invention, radial feeding is adopted to solve the problem of large pressure drop inside the reactor; by setting a partition heat exchange method in the upper reaction zone, the excess heat generated by the reaction is removed in time to achieve the maximum utilization of energy and solve the overheating phenomenon inside the adiabatic reactor; by setting a raw syngas side inlet, it can cope with different startup conditions and special situations such as load changes; by adding an adiabatic reaction section at the lower part of the reactor, the outlet temperature of the reactor can be maintained above 400 °C, thereby superheating high-pressure saturated steam and improving the steam quality and energy utilization rate.

[0009] According to one aspect of the present invention, there is provided a conversion reactor with isothermal-adiabatic coupling, including a furnace body. The top of the furnace body is provided with a main raw syngas inlet, a raw syngas preheating outlet, and a high-pressure saturated steam outlet, and the bottom is provided with a converted gas outlet;

[0010] The furnace body is sequentially divided into an isothermal section and an adiabatic section from top to bottom; a raw syngas side inlet is provided between the furnace bodies of the isothermal section and the adiabatic section; a high-pressure boiler water inlet and a raw syngas preheating inlet are provided on the furnace body of the isothermal section close to the raw syngas side inlet direction;

[0011] The high-pressure boiler water inlet is communicated with the high-pressure saturated steam outlet after passing through the isothermal section; the raw syngas preheating inlet is communicated with the raw syngas preheating outlet after passing through the isothermal section;

[0012] The isothermal section is provided with a catalyst cylinder, which is sleeved inside the furnace body and forms a gap with the inner wall of the furnace body, and the gap forms a gas channel communicating with the adiabatic section; a plurality of inner intake annuli are arranged on the side wall of the catalyst cylinder;

[0013] A central tube Ⅰ is sleeved inside the catalyst cylinder. The upper port of the central tube Ⅰ is communicated with the main raw syngas inlet, and the lower port is closed; a plurality of outer intake annuli are arranged on the side wall of the central tube Ⅰ;

[0014] The area between the catalyst cylinder and the central pipe I is the reaction zone.

[0015] Optionally, a plurality of plate cooling units are independently provided in the reaction zone I, and the plate cooling units are radially arranged with the central pipe I as the center; an inlet of the plate cooling unit is connected to a refrigerant input pipeline, and an outlet of the plate cooling unit is connected to a refrigerant output pipeline.

[0016] Optionally, the plate cooling unit includes a high-pressure boiler water channel and a raw syngas preheating channel; the refrigerant input pipeline includes a high-pressure boiler water riser and a raw syngas riser; the refrigerant output pipeline includes a high-pressure saturated steam riser and a preheated raw syngas riser;

[0017] The high-pressure boiler water riser is communicated with the high-pressure saturated steam riser through the high-pressure boiler water channel, and the high-pressure saturated steam riser is communicated with the high-pressure saturated steam outlet; the raw syngas riser is communicated with the preheated raw syngas riser through the raw syngas preheating channel, and the preheated raw syngas riser is communicated with the raw syngas preheating outlet.

[0018] Optionally, an inlet of the high-pressure boiler water channel is connected to a plurality of high-pressure boiler water risers, the plurality of high-pressure boiler water risers are convergently connected to a high-pressure boiler water collection sphere, and the high-pressure boiler water collection sphere is connected to the high-pressure boiler water inlet; an outlet of the high-pressure boiler water channel is connected to a plurality of high-pressure saturated steam risers, the plurality of high-pressure saturated steam risers converge at a high-pressure saturated steam collection ring, and the high-pressure saturated steam collection ring is connected to the high-pressure saturated steam outlet.

[0019] Optionally, an inlet of the raw syngas preheating channel is connected to a plurality of raw syngas risers, the plurality of raw syngas risers are convergently connected to a raw syngas collection annular gap, and the raw syngas collection annular gap is connected to the raw syngas preheating inlet; an outlet of the raw syngas preheating channel is connected to a plurality of preheated raw syngas risers, the plurality of preheated raw syngas risers converge at a preheated raw syngas collection ring, and the preheated raw syngas collection ring is connected to the raw syngas preheating outlet.

[0020] Optionally, a plurality of flow disturbance modules are provided on the side surface of the plate cooling unit.

[0021] Optionally, a gas distributor is connected inside the furnace body at the raw syngas side inlet.

[0022] Optionally, a gas deflector is provided inside the furnace body in the direction of the raw syngas side inlet near the adiabatic section.

[0023] Optionally, an axial reaction catalyst bed is provided in the adiabatic section.

[0024] Optionally, the upper and lower end plates of the axial reaction catalyst bed are connected to the furnace body to form a cavity for filling a high-temperature resistant catalyst. The reaction gas sequentially passes through the upper end plate, the cavity, and the lower end plate to undergo an adiabatic reaction.

[0025] Optionally, a radial reaction catalyst bed is provided in the adiabatic section.

[0026] Optionally, the radial reaction catalyst bed is fixed to the furnace body through a bottom plate. The bottom plate is connected to the top plate and the left and right side plates to form a cavity for filling a high-temperature resistant catalyst. The reaction gas enters the cavity through the left and right side plates to undergo an adiabatic reaction.

[0027] Optionally, a central tube II is provided in the radial reaction catalyst bed. The central tube II is coaxially arranged with the central tube I. A plurality of ventilation 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 communicates with the converted gas outlet.

[0028] According to another aspect of the present invention, a process using the above-described conversion reactor for reaction is provided. The raw material gas is composed of a first inlet gas and a second inlet gas. The first inlet gas enters through the main inlet of the raw synthesis gas after being preheated, and sequentially flows through the main inlet of the raw synthesis gas, the central tube I, and the outer inlet gas annulus into the catalyst cylinder. After undergoing an isothermal conversion reaction, it sequentially flows through the inner inlet gas annulus and the gap into the adiabatic section. The second inlet gas enters the adiabatic section through the side inlet of the raw synthesis gas.

[0029] The gas in the adiabatic section undergoes an adiabatic conversion reaction and is discharged through the converted gas outlet.

[0030] Optionally, after undergoing the isothermal conversion reaction, the first inlet gas sequentially flows through the inner inlet gas annulus, the gap, the gas distributor, and the gas guide plate into the adiabatic section. The second inlet gas enters through the side inlet of the raw synthesis gas and flows through the gas distributor and the gas guide plate into the adiabatic section.

[0031] Optionally, 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 from both sides inside the furnace body, undergoes an adiabatic conversion reaction, and then enters the central tube II through the ventilation holes to be collected and discharged through the converted gas outlet.

[0032] Optionally, the intake volume of the first inlet gas: the intake volume of the second inlet gas = 10 - 80:30 - 100; preferably, the intake volume of the first inlet gas: the intake volume of the second inlet gas = 30 - 50:40 - 80; more preferably, the intake volume of the first inlet gas: the intake volume of the second inlet gas = 40:60.

[0033] Optionally, in the raw synthesis gas, the dry volume content of carbon monoxide is 30% - 90%.

[0034] Optionally, in the raw syngas, the volume ratio of water to dry gas is 0.1 - 2.0.

[0035] Optionally, the gas temperature at the outlet of the shifted gas is ≥400 °C.

[0036] Compared with the prior art, the present utility model has the following beneficial effects:

[0037] (1) A raw syngas side inlet is provided to better cope with different startup conditions and special situations such as load changes.

[0038] (2) The raw syngas needs to be preheated to the catalyst activation temperature before entering the reactor. In the isothermal-adiabatic dual shift coupling technology of the present utility model, by setting partition heat exchange in the upper isothermal reaction zone, the raw syngas is preheated in the second-stage catalyst partition, and high-pressure saturated steam is generated in the first-stage catalyst partition (high-pressure saturated steam can also be generated in the second-stage catalyst partition, and the raw syngas is preheated in the first-stage catalyst partition). In this way, not only can the excess heat generated by the shift reaction be removed in a timely manner to avoid overheating, but also the raw syngas can be preheated to the catalyst activation temperature and high-pressure saturated steam can be by-produced. The former avoids the problem of tube sheet leakage caused by too large a temperature difference between the shell side and the tube side of the previous raw syngas preheater, and directly removing the preheater can also reduce the complexity of the process and equipment investment. The latter by-produces high-pressure saturated steam to achieve the maximum utilization of energy.

[0039] (3) An adiabatic reaction section is provided at the lower part of the reactor. Under the adjustment of the raw syngas side inlet, the outlet temperature of the adiabatic section can reach above 400 °C, and high-pressure saturated steam can be superheated, so that the excess high-pressure superheated steam can be transported through the pipeline network, ensuring the stability of the downstream heat exchange network. BRIEF DESCRIPTION OF THE DRAWINGS

[0040] Figure 1 It is a schematic diagram of the external furnace body structure of the reactor of the present utility model;

[0041] Figure 2 It is a schematic diagram of the internal structure of the reactor in Example 1;

[0042] Figure 3 It is a schematic diagram of the internal structure of the reactor in Example 2;

[0043] Figure 4 It is a schematic diagram of the plate cooling unit (collection ring) with double-channel heat exchange of the present utility model;

[0044] Figure 5 It is a schematic diagram of the plate cooling unit (collection ball) with double-channel heat exchange of the present utility model;

[0045] Among them, 1 - furnace body; 2 - high-pressure boiler water inlet; 3 - high-pressure saturated steam outlet; 4 - preheated outlet of raw syngas; 5 - main inlet of raw syngas; 6 - preheated inlet of raw syngas; 7 - main maintenance port; 8 - catalyst upper discharge port; 9 - side inlet of raw syngas; 10 - catalyst lower discharge port; 11 - shifted gas outlet; 12 - high-pressure saturated steam collection ring; 13 - preheated raw syngas collection ring; 14 - preheated raw syngas riser; 15 - heat transfer module (i.e., plate cooling unit); 16 - central tube I; 17 - high-pressure boiler water riser; 18 - high-pressure boiler water collection sphere; 19 - raw syngas riser; 20 - raw syngas collection annulus; 21 - isothermal section maintenance port; 22 - gas deflector; 23 - high-temperature resistant catalyst; 24 - adiabatic section maintenance port; 25 - collection sphere maintenance port; 26 - gas distributor; 27 - pressure grid; 28 - high-pressure saturated steam riser; 29 - catalyst cylinder; 30 - porcelain ball; 31 - expansion joint; 32 - high-pressure boiler water channel; 33 - preheated raw syngas channel; 34 - high-pressure boiler water collection ring; 35 - raw syngas collection sphere; 36 - central tube II. Detailed implementation manners

[0046] The present utility model will be further described below in conjunction with specific embodiments, but it does not constitute any limitation to the present utility model.

[0047] Embodiment 1

[0048] As Figure 1 , Figure 2 shown, a radial isothermal - axial adiabatic dual shift coupling reactor includes: furnace body 1, high-pressure boiler water inlet 2, high-pressure saturated steam outlet 3, preheated outlet of raw syngas 4, main inlet of raw syngas 5, preheated inlet of raw syngas 6, main maintenance port 7, catalyst upper discharge port 8, side inlet of raw syngas 9, catalyst lower discharge port 10, shifted gas outlet 11, high-pressure saturated steam collection ring 12, preheated raw syngas collection ring 13, preheated raw syngas riser 14, heat transfer module (i.e., plate cooling unit) 15, central tube I 16, high-pressure boiler water riser 17, high-pressure boiler water collection sphere 18, raw syngas riser 19, raw syngas collection annulus 20, isothermal section maintenance port 21, gas deflector 22, high-temperature resistant catalyst 23, adiabatic section maintenance port 24, collection sphere maintenance port 25, gas distributor 26, pressure grid 27, high-pressure saturated steam riser 28, catalyst cylinder 29, porcelain ball 30, expansion joint 31.

[0049] The shape of the reactor furnace body is a vertical cylinder, which is divided into upper and lower sections inside. In the upper section, the catalyst cylinder is sleeved inside the furnace body, and a gap is formed between the catalyst cylinder and the furnace body. The gap is the synthesis gas outlet channel. The central tube is connected to the main inlet of the raw synthesis gas, runs through the catalyst cylinder from the main inlet of the raw synthesis gas until the bottom of the catalyst cylinder. An outer intake annulus and an inner intake annulus are respectively provided on the side wall of the central tube and the catalyst cylinder. The area between the catalyst cylinder and the central tube Ⅰ is called the reaction zone, and sectional catalysts are filled in this area. The catalyst can be discharged through the catalyst upper discharge port at the lower end of the reaction zone. In order to make the upper reaction zone in an isothermal state, and at the same time preheat the raw synthesis gas to the activation temperature of the catalyst and by-product high-pressure saturated steam, the present invention sets sectional heat exchange in the reaction zone. The raw synthesis gas is preheated in the second-stage catalyst section, and high-pressure saturated steam is generated in the first-stage catalyst section. Therefore, a plurality of plate cooling units are provided in the two sections of the upper reaction zone of the reactor of the present invention.

[0050] In the reaction zone, the plate cooling units are arranged in a central radial pattern with the central tube Ⅰ as the axis in the reaction zone. There are positions of a plurality of turbulence modules on the side surface of the plate cooling unit. Such an arrangement can increase the turbulence degree of the fluid, thereby improving the heat transfer coefficient. And under the same heat transfer amount, the required heat exchange area is smaller, greatly reducing the equipment investment. The inlet of the plate cooling unit in the first-stage catalyst section is connected to the high-pressure boiler water riser. A plurality of high-pressure boiler water risers are collectively connected to the high-pressure boiler water collection sphere, and the high-pressure boiler water inlet is connected under the high-pressure boiler water collection sphere; the inlet of the plate cooling unit in the second-stage catalyst section is connected to the raw synthesis gas riser. A plurality of raw synthesis gas risers are collectively connected to the raw synthesis gas collection annulus, and the lower part of the raw synthesis gas collection annulus is connected to the raw synthesis gas preheating inlet. In addition, a collection sphere inspection opening is provided below the collection sphere for maintenance use. The outlets of the plate cooling units in the first-stage catalyst section are all connected to the high-pressure saturated steam riser. A plurality of high-pressure saturated steam risers are collectively connected to the high-pressure saturated steam collection ring. At the same time, the upper part of the high-pressure saturated steam collection ring is connected to the high-pressure saturated steam outlet to send out the steam; the outlets of the plate cooling units in the second-stage catalyst section are all connected to the preheated raw synthesis gas riser. A plurality of preheated raw synthesis gas risers are collectively connected to the preheated raw synthesis gas collection ring. At the same time, the upper part of the preheated raw synthesis gas collection ring is connected to the raw synthesis gas preheating outlet to send out the preheated raw synthesis gas.

[0051] A raw synthesis gas side inlet is provided between the upper and lower sections of the furnace body. The synthesis gas from the bypass can be directly mixed fully with the converted gas flowing out of the central tube Ⅰ in the upper section, and then passes through the gas distributor and the gas deflector plate in turn and enters the lower adiabatic reaction section. By means of bypass regulation, different startup conditions and load changes and other situations can be dealt with, and the outlet temperature of the lower converted gas can be better controlled.

[0052] The lower adiabatic reaction section of the furnace body is a mixing-axial adiabatic reactor in the reactor cavity. The reaction gas flowing out from the lower end of the gas guide plate passes through the shift catalyst bed axially for reaction, and then is discharged through the shift gas outlet. The setting of the adiabatic reaction section can make the temperature of the shift gas outlet reach above 400 °C, which can be used to superheat high-pressure saturated steam and improve the steam quality.

[0053] This radial isothermal-axial adiabatic dual shift coupling reactor involves two systems, namely a two-stage radial-axial dual shift reaction system and a steam generation-raw syngas preheating system.

[0054] The process of the two-stage radial-axial dual shift reaction system is as follows: The raw syngas enters the central pipe I 16 in the furnace body 1 through the main raw syngas inlet 5, first flows vertically downward in the central pipe I 16, and then passes through the outer intake annulus on both sides of the central pipe I 16 in a radial flow direction and sequentially passes through the catalyst secondary partition and the catalyst primary partition. The raw syngas contacts and reacts with the catalyst in the reaction zone, and at the same time exchanges heat with the heat removal module (plate cooling unit) 15. The excess heat is carried out by the high-pressure boiler water and the raw syngas in the heat removal module (plate cooling unit) 15 to avoid overheating in the reaction zone. The generated shift gas flows out through the inner intake annulus on both sides of the catalyst cylinder and enters the gas flow channel. The outflowing shift gas is mixed with the raw syngas entering from the raw syngas side inlet 9, sequentially passes through the gas distributor 26 and the gas guide plate 22, and enters the lower adiabatic reaction zone in a uniformly distributed manner, and then enters the high-temperature resistant catalyst 23 for shift reaction in an axial flow direction. The temperature of the shift gas after the reaction is above 400 °C and is discharged from the shift gas outlet 11.

[0055] In this embodiment, an axial adiabatic to fixed bed structure is adopted, with a large reaction gas flow area, a long residence time, a high catalyst efficiency, a small filling height of the catalyst bed layer, which can reduce the total length of the reactor and the equipment investment is relatively low.

[0056] The furnace body 1 is provided with a catalyst upper unloading port 8 for loading and unloading the catalyst in the upper isothermal reaction zone; a catalyst lower unloading port 10 for loading and unloading the catalyst in the lower adiabatic reaction zone. The main maintenance port 7 is used for maintenance personnel to enter the interior of the reactor, and the isothermal section maintenance port 21 and the adiabatic section maintenance port 24 are respectively used for maintenance personnel to repair the upper and lower regions of the reactor. Porcelain balls 30 are also arranged in the furnace body 1 to protect and support the high-temperature resistant catalyst 23 and the catalyst bed layer in the upper isothermal reaction zone. The pressure grid 27 is used to fix the high-temperature resistant catalyst 23 and the porcelain balls 30. The gas guide plate 26 and the gas distributor 22 are used for the distribution and mixing of the reaction gas; An expansion joint 31 is provided in the middle of each high-pressure saturated steam riser 28 and each preheated raw syngas riser 14, effectively solving the problem of thermal expansion caused by the temperature difference in the upper section of the reactor.

[0057] The process of the steam generation - raw syngas preheating system is as follows: High-pressure boiler water from the outside world converges at the high-pressure boiler water collection sphere 18 through the high-pressure boiler water inlet 2, and then enters the first-stage catalyst partition in the heat transfer module (plate heat exchanger unit) 15 through the high-pressure boiler water riser 17. The high-pressure boiler water absorbs excess heat in the heat transfer module (plate heat exchanger unit) 15 to prevent the temperature in the reaction zone of the first-stage catalyst partition from exceeding the limit; the high-pressure boiler water after absorbing heat forms high-pressure saturated steam, which flows out from the outlet of the heat transfer module (plate heat exchanger unit) 15 and enters the high-pressure saturated steam riser 28 to converge at the high-pressure saturated steam collection ring 12, and then flows out from the high-pressure saturated steam outlet 3. Raw syngas from the outside world converges at the raw syngas collection annulus 20 through the raw syngas preheating inlet 6, and then enters the second-stage catalyst partition in the heat transfer module (plate heat exchanger unit) 15 through the raw syngas riser 19. The raw syngas absorbs excess heat in the heat transfer module (plate heat exchanger unit) 15 to prevent the temperature in the reaction zone of the second-stage catalyst partition from exceeding the limit; the temperature of the raw syngas after absorbing heat reaches the activation temperature of the catalyst, flows out from the outlet of the heat transfer module (plate heat exchanger unit) 15 and enters the preheated raw syngas riser 14 to converge at the preheated raw syngas collection ring 13, and then flows out from the raw syngas preheating outlet 4.

[0058] In addition, the high-pressure boiler water collection sphere described in the present utility model can also be replaced by a high-pressure boiler water collection ring. As Figure 4 shown, the upper end of the high-pressure boiler water riser is connected to the high-pressure boiler water channel 32, and the lower end converges at the high-pressure boiler water collection ring 34; the upper end of the syngas riser is connected to the raw syngas preheating channel 33, and the lower end converges at the raw syngas collection ring; the raw syngas collection ring can also be replaced by a raw syngas collection sphere 35, as Figure 5 shown.

[0059] Embodiment 2

[0060] As Figure 3 shown, an isothermal - adiabatic coupled double-radial conversion reactor, which is different from Embodiment 1 in that the lower end of the furnace body is a reactor cavity mixing - radial adiabatic reactor. The reaction gas flowing out from the lower end of the gas deflector plate passes through the conversion catalyst bed layer radially from both sides for reaction, and the generated conversion gas enters the inner part of the central tube II 36 through the annulus on the central tube II 36 of the lower section of the reactor to converge, and then is discharged through the conversion gas outlet. The setting of the adiabatic reaction section can make the temperature of the conversion gas outlet reach above 400°C, which can be used for superheating high-pressure saturated steam.

[0061] This embodiment adopts a radial adiabatic fixed-bed structure. The reaction gas enters the catalyst bed layer from the two-side annuli. The flow path is short and the pressure drop is low, which is beneficial to reducing the downstream compression power consumption and belongs to an energy-saving device.

[0062] Any numerical values mentioned in the present utility model, if there is only a two-unit interval between any minimum value and any maximum value, include all values increasing by one unit each time from the minimum value to the maximum value. For example, if the amount of a component is stated, or the value of a process variable such as temperature, pressure, time, etc. is 50 - 90, it means in this specification that the values 51 - 89, 52 - 88... as well as 69 - 71 and 70 - 71, etc. are specifically listed. For non-integer values, appropriate consideration can be given to taking 0.1, 0.01, 0.001 or 0.0001 as one unit. These are only some specifically indicated examples. In the present application, in a similar manner, all possible combinations of numerical values between the listed minimum value and maximum value are considered to have been disclosed.

[0063] It should be noted that the above-described embodiments are only used to explain the present utility model and do not constitute any limitation to the present utility model. The present utility model has been described by referring to typical embodiments, but it should be understood that the words used therein are descriptive and explanatory words rather than limiting words. Modifications can be made to the present utility model within the scope of the claims of the present utility model as stipulated, and the present utility model can be revised without departing from the scope and spirit of the present utility model. Although the present utility model described therein relates to specific methods, materials and embodiments, it does not mean that the present utility model is limited to the specific examples disclosed therein. On the contrary, the present utility model can be extended to all other methods and applications with the same function.

Claims

1. An isothermal-adiabatic coupled shift reactor, characterized in that: It comprises a furnace body, wherein the top of the furnace body is provided with a main inlet for crude synthesis gas, a preheating outlet for crude synthesis gas and a high-pressure saturated steam outlet, and the bottom of the furnace body is provided with a conversion gas outlet; The furnace body is divided into an isothermal section and an adiabatic section from top to bottom; a crude synthesis gas 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 synthesis gas preheating inlet are provided on the furnace body of the isothermal section near the crude synthesis gas 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 synthesis gas preheating inlet is connected to the crude synthesis gas preheating outlet after passing through the isothermal section; The isothermal section is provided with a catalyst cartridge, which is sleeved in the furnace body and forms a gap with the inner wall of the furnace body; the gap forms a gas channel connected to the adiabatic section; a plurality of inner air intake annular gaps are provided on the side wall of the catalyst cartridge; The catalyst cylinder is provided with a central tube I, the upper port of the central tube I is connected to the main inlet of the crude synthesis gas, and the lower port is closed; a plurality of external air inlet annular gaps are provided on the side wall of the central tube I; The reaction zone is between the catalyst cylinder and the central tube I.

2. The shift reactor according to claim 1, characterized in that A plurality of plate cooling units are provided in the reaction zone, and the plate cooling units are radially arranged with the central tube I as the center; the inlet of the plate cooling unit is connected to the refrigerant input pipeline, and the outlet of the plate cooling unit is connected to the refrigerant output pipeline.

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 synthesis gas preheating channel; the refrigerant input pipeline includes a high-pressure boiler water riser and a crude synthesis gas riser; the refrigerant output pipeline includes a high-pressure saturated steam riser and a preheated crude synthesis gas riser; The high-pressure boiler water riser is connected to the high-pressure saturated steam riser through the high-pressure boiler water channel, and the high-pressure saturated steam riser is connected to the high-pressure saturated steam outlet; the crude synthesis gas riser is connected to the preheated crude synthesis gas riser through the crude synthesis gas preheating channel, and the preheated crude synthesis gas riser is connected to the crude synthesis gas preheating outlet; And / or, a plurality of spoiler modules are provided on the side of the plate type cooling unit.

4. The shift reactor according to claim 3, characterized in that The inlet of the high-pressure boiler water channel is connected to a plurality of high-pressure boiler water riser pipes, and the plurality of high-pressure boiler water riser pipes are gathered and 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 channel is connected to a plurality of high-pressure saturated steam riser pipes, and the plurality of high-pressure saturated steam riser pipes are gathered in a high-pressure saturated steam collecting ring, and the high-pressure saturated steam collecting ring 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 synthesis gas preheating channel is connected to a plurality of crude synthesis gas riser pipes, which are gathered together in a crude synthesis gas collecting annulus, which is connected to the crude synthesis gas preheating inlet; the outlet of the crude synthesis gas preheating channel is connected to a plurality of preheated crude synthesis gas riser pipes, which are gathered together in a preheated crude synthesis gas collecting ring, which is connected to the crude synthesis gas preheating outlet.

6. The shift reactor according to claim 1, characterized in that The raw synthesis gas side inlet is connected to a gas distributor inside the furnace body.

7. The shift reactor according to claim 1, characterized in that A gas guide plate is provided inside the furnace body of the heat-insulating section close to the inlet side of the raw synthesis gas.

8. The shift reactor according to claim 1, characterized in that The adiabatic section is provided with an axial reaction catalyst bed; The upper and lower end plates of the axial reaction catalyst bed are connected to the furnace body to form a cavity, which is used to fill the high temperature resistant catalyst. The reaction gas passes through the upper end plate, the cavity and the lower end plate in sequence to produce an adiabatic reaction.

9. The shift reactor according to claim 1, characterized in that The adiabatic section is provided with a radial reaction catalyst bed; The radial reaction catalyst bed is fixed on the furnace body through a bottom plate, and the bottom plate is connected to the top plate and the left and right side plates to form a cavity. The cavity is used to fill the high temperature resistant catalyst, and the reaction gas enters the cavity through the left and right side plates to produce an adiabatic reaction.

10. The shift reactor according to claim 9, characterized in that The radial reaction catalyst bed is provided with a central tube II, which is coaxially arranged with the central tube I; a plurality of vents are arranged 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 conversion gas outlet.

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