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; a crude synthesis gas side inlet is formed between the isothermal section and the heat insulation section of the furnace body; a high-pressure boiler water inlet and a crude synthesis gas preheating inlet are formed in the furnace body, close to the crude synthesis gas side inlet, of the isothermal section; the high-pressure boiler water inlet is communicated with the high-pressure saturated steam outlet after passing through the isothermal section; and the crude synthesis gas preheating inlet is communicated with the crude synthesis gas preheating outlet after passing through the isothermal section. 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 a conversion reactor with isothermal and adiabatic coupling. Background Art

[0002] The purpose of CO conversion is to adjust the concentrations of H 2 and CO in the syngas to meet the requirements of downstream users. According to the characteristic that the CO reaction is a strong exothermic reaction, there are usually the following several types of reactors:

[0003] (1) Axial reactor. The inside of the axial reactor is filled with catalysts, and the conversion gas passes through the catalyst bed layer axially to carry out an adiabatic conversion reaction. The characteristics of this reactor are simple structure and large catalyst loading. However, since all the conversion gas needs to pass through the entire catalyst bed layer, the pressure drop of the conversion gas is relatively large. Especially in the case of catalyst fragmentation at the end stage, the pressure drop caused by the conversion furnace is very large, resulting in an increase in the pressure drop of the entire conversion system. In the case of the reaction of medium water-gas ratio and high-CO raw syngas, it is extremely easy to cause overheating. Therefore, the axial reactor is only suitable for places such as low-temperature conversion where the adiabatic temperature rise is small and there are strict requirements for the water-gas ratio.

[0004] (2) Axial-radial reactor. Different from 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 layer, and then flows out of the reaction furnace after entering the central tube. The gas distribution of this type of reactor is stable, not affected by the catalyst packing density, and the bed layer pressure drop is small; compared with the axial conversion furnace under the same working conditions, the cylinder temperature is lower, the equipment diameter and wall thickness are smaller, and the equipment investment is lower.

[0005] The above two types of conversion furnaces both adopt adiabatic reactors. Since the conversion reaction is a strong exothermic reaction and a thermodynamically controlled process, the conversion process adopts a multi-stage and multi-time heat exchange reaction method in the process setting. This has caused a series of problems such as relatively complex conversion process, high heat loss, high steam consumption, and high equipment cost in the traditional process.

[0006] (3) Fully isothermal reactor. The isothermal reactor can immediately remove the reaction heat by the physical method of "heat transfer by water", so as to maintain the catalyst bed layer operating at a stable low temperature and ensure a high CO conversion rate. The advantages of the isothermal conversion technology compared with the traditional adiabatic conversion are as follows: First, the isothermal conversion immediately removes the reaction heat and maintains the catalyst bed layer operating stably at a lower temperature. Second, the by-product steam greatly reduces the energy consumption. Third, the process flow is simplified, and the system pressure drop and device investment are reduced.

[0007] However, the currently applied isothermal conversion technology has the following problems: ① The steam by-produced in the steam drum of the isothermal conversion furnace is saturated steam, and it is impossible to 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 prone to produce condensate when the temperature drops and cannot enter the pipe network. The outlet temperature of the traditional adiabatic conversion furnace is relatively high, usually above 400 °C, and can be used for superheating saturated steam. However, since most of the reaction heat of the isothermal conversion furnace is carried away by the water circulation system, the outlet temperature is only about 300 °C, and it cannot provide a superheating source. It can only be achieved by setting up a heating furnace separately or performing heat integration with other devices, which increases the process complexity and equipment investment. ② It is difficult to adjust the temperature of the isothermal conversion furnace. Due to the influence of factors such as upstream load changes, water-gas ratio fluctuations, and temperature increase at the end of the catalyst, the outlet temperature of the conversion furnace needs to be adjusted frequently. Since the water circulation between the steam drum and the heat exchange tubes is a natural circulation, that is, a water-vapor circulation formed by the driving force generated by the hydrostatic head of water and the density difference of the two-phase flow in the heat exchange tubes, it is difficult to control the removal of reaction heat to a certain extent. Utility Model Content

[0008] The utility model aims at the problems in the prior art and provides an isothermal-adiabatic dual-conversion coupling reactor that can cope with different start-up conditions and load changes, etc., and can flexibly adjust the working conditions, has a short process flow, less total equipment investment, and can by-produce high-pressure superheated steam.

[0009] In the reaction zone of the upper section of the reactor of the utility model, radial feeding is adopted, which solves the problem of large pressure drop in the reactor; by setting up 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 problem of over-temperature in the adiabatic reactor; by setting a raw syngas side inlet, it can cope with special situations such as different start-up conditions and 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, and then superheat the high-pressure saturated steam to improve the energy utilization rate.

[0010] According to one aspect of the utility model, there is provided an isothermal-adiabatic coupled conversion reactor, 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;

[0011] 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;

[0012] 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;

[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 channel communicating with the main inlet of the raw syngas; a plurality of outer intake annuli are arranged on the side wall of the catalyst cylinder;

[0014] A central pipe Ⅰ is sleeved inside the catalyst cylinder, the upper port of the central pipe Ⅰ is closed, and the lower port communicates with the adiabatic section; a plurality of inner intake annuli are arranged on the side wall of the central pipe Ⅰ;

[0015] The reaction zone is between the catalyst cylinder and the central pipe Ⅰ.

[0016] Optionally, the raw syngas preheating outlet communicates with the gap, that is, the raw syngas preheating outlet is located inside the reactor, and the preheated raw syngas does not discharge out of the reactor through the raw syngas 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 central pipe Ⅰ as the center; the inlet of the plate cooling unit is connected to a refrigerant input pipeline, and the outlet of the plate cooling unit is connected to a refrigerant output pipeline.

[0018] 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;

[0019] The high-pressure boiler water riser communicates with the high-pressure saturated steam riser through the high-pressure boiler water channel, and the high-pressure saturated steam riser communicates with the high-pressure saturated steam outlet; the raw syngas riser communicates with the preheated raw syngas riser through the raw syngas preheating channel, and the preheated raw syngas riser communicates with the raw syngas preheating outlet.

[0020] Optionally, the 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 collectively 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; the 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 on a high-pressure saturated steam collection ring, and the high-pressure saturated steam collection ring is connected to the high-pressure saturated steam outlet.

[0021] Optionally, the 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 annulus, and the raw syngas collection annulus is connected to the raw syngas preheating inlet. The 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.

[0022] Optionally, a plurality of protrusions are provided on the side surface of the plate type cooling unit.

[0023] Optionally, a gas distributor is connected inside the furnace body at the raw syngas side inlet.

[0024] Optionally, a gas guide plate is provided inside the furnace body in the direction of the raw syngas side inlet near the adiabatic section.

[0025] Optionally, an axial reaction catalyst bed is provided in the adiabatic section.

[0026] Optionally, the upper and lower end plates of the axial reaction catalyst bed are connected to the furnace body to form a cavity. The cavity is used to fill a high-temperature resistant catalyst, and the reaction gas sequentially passes through the upper end plate, the cavity, and the lower end plate to undergo an adiabatic reaction.

[0027] Optionally, a radial reaction catalyst bed is provided in the adiabatic section.

[0028] Optionally, the radial reaction catalyst bed is fixed to the furnace body by a bottom plate. 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 a high-temperature resistant catalyst, and the reaction gas enters the cavity through the left and right side plates to undergo an adiabatic reaction.

[0029] Optionally, the radial reaction catalyst bed is provided with a central tube II. 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 reformed gas outlet.

[0030] According to another aspect of the present invention, a process using the above-mentioned reforming reactor for reaction is provided. The raw material gas consists of a first inlet gas and a second inlet gas. The first inlet gas enters through the main raw syngas inlet after preheating, and sequentially flows through the main raw syngas inlet, the gap, the outer inlet annulus into the catalyst cylinder, and after an isothermal reforming reaction, sequentially flows through the inner inlet annulus and the central tube I into the adiabatic section. The second inlet gas enters the adiabatic section through the raw syngas side inlet.

[0031] The gas in the adiabatic section undergoes an adiabatic reforming reaction and is discharged through the reformed gas outlet.

[0032] Optionally, after the first intake air undergoes an isothermal shift reaction, it flows successively through the inner intake annulus, central pipe I, gas distributor, and gas deflector plate and enters the adiabatic section; the second intake air enters from the raw syngas side inlet, flows through the gas distributor and gas deflector plate and enters the adiabatic section.

[0033] 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, and after the adiabatic shift reaction, it enters the central pipe II through the vent holes and is discharged through the shift gas outlet.

[0034] Optionally, the intake air volume of the first intake air: the intake air volume of the second intake air = 10 - 80: 30 - 100; preferably, the intake air volume of the first intake air: the intake air volume of the second intake air = 30 - 50: 40 - 80; more preferably, the intake air volume of the first intake air: the intake air volume of the second intake air = 40: 60.

[0035] Optionally, in the raw syngas, the dry - basis volume content of carbon monoxide is 30% - 90%.

[0036] Optionally, in the raw syngas, the volume ratio of water to dry gas is 0.1 - 1.6.

[0037] Optionally, the gas temperature at the shift gas outlet is ≥400 °C.

[0038] Compared with the prior art, the present utility model has the following beneficial effects:

[0039] (1) By providing a raw syngas side inlet, the temperature of the shift gas at the outlet of the adiabatic section can be flexibly adjusted according to the heat exchange requirements of subsequent process media, better coping with special situations such as different startup conditions and load changes.

[0040] (2) The raw syngas needs to be preheated to the catalyst activation temperature before entering the reactor. The isothermal - adiabatic dual - shift coupling technology of the present utility model sets up partition heat exchange in the upper - stage 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 over - temperature, 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 on the shell - side of the previous raw syngas preheater, and directly removing the preheater can also reduce the process complexity and equipment investment. The latter by - production of high - pressure saturated steam realizes the maximum utilization of energy.

[0041] (3) An adiabatic reaction section is provided at the lower part of the reactor. Under the regulation of the inlet on the raw syngas side, the outlet temperature of the adiabatic section can reach above 400 °C, which can superheat high-pressure saturated steam, enabling the excess high-pressure superheated steam to be stably transported through the pipeline network without generating condensate, ensuring the stability of the downstream heat exchange network. Description of the Drawings

[0042] Figure 1 Schematic diagram of the external furnace body structure of the reactor of the present utility model;

[0043] Figure 2 Schematic diagram of the internal structure of the reactor in Example 1;

[0044] Figure 3 Schematic diagram of the internal structure of the reactor in Example 2;

[0045] Figure 4 Schematic diagram of the plate cooling unit with dual-channel heat exchange of the present utility model (collection ring);

[0046] Figure 5 Schematic diagram of the plate cooling unit with dual-channel heat exchange of the present utility model (collection ball);

[0047] Among them, 1 - furnace body; 2 - high-pressure boiler water inlet; 3 - high-pressure saturated steam outlet; 4 - preheated raw syngas outlet; 5 - main raw syngas inlet; 6 - preheated raw syngas inlet; 7 - main maintenance port; 8 - catalyst upper discharge port; 9 - raw syngas side inlet; 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; 16 - central pipe I; 17 - high-pressure boiler water riser; 18 - high-pressure boiler water collection ball; 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 ball 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 ball; 36 - central pipe II. Detailed Embodiments

[0048] 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.

[0049] Example 1

[0050] As Figure 1 、 Figure 2As shown in the figure, a radial isothermal - axial adiabatic dual - conversion coupling reactor includes: a furnace body 1, a high - pressure boiler water inlet 2, a high - pressure saturated steam outlet 3, a pre - heated outlet of raw syngas 4, a main inlet of raw syngas 5, a pre - heated inlet of raw syngas 6, a main maintenance port 7, a catalyst upper discharge port 8, a side inlet of raw syngas 9, a catalyst lower discharge port 10, a converted gas outlet 11, a high - pressure saturated steam collection ring 12, a pre - heated raw syngas collection ring 13, a pre - heated raw syngas riser 14, a heat transfer module (i.e., a plate - type cooling unit) 15, a central pipe I 16, a high - pressure boiler water riser 17, a high - pressure boiler water collection sphere 18, a raw syngas riser 19, a raw syngas collection annulus 20, an isothermal section maintenance port 21, a gas deflector 22, a high - temperature resistant catalyst 23, an adiabatic section maintenance port 24, a collection sphere maintenance port 25, a gas distributor 26, a pressure grid 27, a high - pressure saturated steam riser 28, a catalyst cylinder 29, porcelain balls 30, an expansion joint 31.

[0051] 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 forms a gap with the furnace body, and the gap communicates with the main inlet of raw syngas to form a syngas inlet channel. At the central position inside the catalyst cylinder, there is a central pipe I. The upper end of the central pipe I is closed, and the lower end is connected to the adiabatic section. Inner and outer intake annuli are respectively provided on the central pipe I and the side wall of the catalyst cylinder. The area between the catalyst cylinder and the central pipe I is called the reaction zone, and partitioned 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. To keep the upper - section reaction zone in an isothermal state, while pre - heating the raw syngas to the catalyst activation temperature and producing by - product high - pressure saturated steam, the present invention sets partitioned heat exchange in the reaction zone. The raw syngas is pre - heated in the second - level partition of the catalyst, and high - pressure saturated steam is generated in the first - level partition of the catalyst. Therefore, a plurality of plate - type cooling units are provided in the two partitions of the upper - section reaction zone of the reactor of the present invention.

[0052] In the reaction zone, the plate-type cooling unit is arranged in a central radial pattern with the central pipe Ⅰ as the axis. There are multiple raised positions on the side of the plate-type cooling unit. Such an arrangement can increase the turbulence degree of the fluid, thereby improving the heat transfer coefficient. Moreover, under the same heat transfer amount, the required heat exchange area is smaller, greatly reducing the equipment investment. The inlet of the plate-type cooling unit in the first-stage catalyst partition is connected to the high-pressure boiler water riser. Multiple high-pressure boiler water risers converge and are connected to the high-pressure boiler water collecting sphere, and the high-pressure boiler water inlet is connected below the high-pressure boiler water collecting sphere; the inlet of the plate-type cooling unit in the second catalyst zone is connected to the raw syngas riser. Multiple raw syngas risers converge and are connected to the raw syngas collecting annulus, and the lower part of the raw syngas collecting annulus is connected to the raw syngas preheating inlet. In addition, a maintenance opening is provided below the collecting sphere for maintenance use. The outlets of the plate-type cooling units in the first-stage catalyst partition are all connected to the high-pressure saturated steam riser. Multiple high-pressure saturated steam risers converge at the high-pressure saturated steam collecting ring. At the same time, the upper part of the high-pressure saturated steam collecting ring is connected to the high-pressure saturated steam outlet to send out the steam; the outlets of the plate-type cooling units in the second catalyst zone are all connected to the preheated raw syngas riser. Multiple preheated raw syngas risers converge at the preheated raw syngas collecting ring. At the same time, the upper part of the preheated raw syngas collecting ring is connected to the raw syngas preheating outlet to send out the preheated raw syngas.

[0053] A raw syngas side inlet is provided between the upper and lower sections of the furnace body. The syngas from the bypass can directly mix fully with the converted gas flowing out of the central pipe Ⅰ in the upper section, and then pass through the gas distributor and the gas guide plate in sequence to enter the lower adiabatic reaction section. By means of bypass adjustment, different start-up conditions and load changes can be dealt with, and the outlet temperature of the lower converted gas can be better controlled.

[0054] This radial isothermal - axial adiabatic dual conversion coupling reactor involves two systems, namely a two-stage radial - axial dual conversion reaction system and a steam generation - raw syngas preheating system.

[0055] The process of the two-stage radial-axial dual conversion reaction system is as follows: The raw synthesis gas enters the upper head of the furnace body 1 through the main inlet 5 of the raw synthesis gas, passes through the outer gas inlet annulus in a radial flow direction through the gas flow channels on both sides, and sequentially passes through the first-stage catalyst partition and the second-stage catalyst partition. The raw synthesis gas 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 synthesis gas in the heat removal module (plate cooling unit) 15 to avoid over-temperature in the reaction zone. The generated converted gas is collected in the central pipe I 16 through the inner gas inlet annulus on the side wall of the central pipe I 16. The converted gas flowing out from the bottom of the central pipe I 16 is mixed with the raw synthesis gas entering from the side inlet 9 of the raw synthesis gas, 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 conversion reaction in an axial flow direction. The temperature of the converted gas after the reaction is above 400 °C and is discharged from the converted gas outlet 11.

[0056] In this embodiment, an axial adiabatic fixed bed structure is adopted, which has a large reaction gas flow area, a long residence time, a high catalyst efficiency, a small filling height of the catalyst bed layer, can reduce the total length of the reactor, and has a low equipment investment.

[0057] On the furnace body 1, there is 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 22 and the gas distributor 26 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 synthesis gas riser 14, effectively solving the problem of thermal expansion caused by the temperature difference in the upper section of the reactor.

[0058] 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 cooler unit) 15 through the high-pressure boiler water riser 17. The high-pressure boiler water absorbs excess heat in the heat transfer module (plate cooler 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 cooler 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 cooler unit) 15 through the raw syngas riser 19. The raw syngas absorbs excess heat in the heat transfer module (plate cooler 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 catalyst activation temperature, flows out from the outlet of the heat transfer module (plate cooler 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.

[0059] As Figure 2 shown, the raw syngas preheating outlet 4 is located outside the reactor. The preheated raw syngas passes through the heat transfer module 15 and then is discharged from the raw syngas preheating outlet 4 at the top of the reactor, and then enters the raw syngas preheating inlet 6. This intake method can adjust the amounts of raw syngas and preheated raw syngas, with flexible adjustment; the preheated raw syngas can also not be discharged from the reactor through the raw syngas preheating outlet 4 (the raw syngas preheating outlet 4 is located inside the reactor and is directly connected to the gap, Figure 2 not shown), but directly enters the gap through the raw syngas preheating outlet 4. This intake method does not require the preheated raw syngas to bypass outside the reactor, but the gas volume adjustment performance is poor.

[0060] 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.

[0061] Example 2

[0062] As Figure 3As shown, an isothermal-adiabatic coupled double-radial conversion reactor. Different from Embodiment 1, the lower end of the furnace body is a mixing-radial adiabatic reactor in the reactor cavity. The reaction gas flowing out from the lower end of the gas deflector passes through the conversion catalyst bed layer radially from both sides for reaction, and the generated conversion gas enters the central pipe II 36 through the ventilation holes on the side wall of the central pipe II 36 at the lower section of the reactor to be collected, 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.

[0063] This embodiment adopts a radial adiabatic fixed bed structure. The reaction gas enters the catalyst bed layer from the side annulus. The flow path length 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.

[0064] Regarding 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, all values increasing by one unit from the minimum value to the maximum value are included. For example, if the amount of a component, or the value of a process variable such as temperature, pressure, time, etc. is stated as 50 - 90, it means in this specification that 51 - 89, 52 - 88... as well as 69 - 71 and 70 - 71 and other numerical values are specifically listed. For non-integer values, appropriate consideration can be given with 0.1, 0.01, 0.001 or 0.0001 as a unit. These are only some specifically indicated examples. In this application, in a similar manner, all possible combinations of numerical values between the listed minimum value and the maximum value are considered to have been disclosed.

[0065] 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 revisions can be made to the present utility model 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 main inlet of the crude synthesis gas; a plurality of external air intake annular gaps are provided on the side wall of the catalyst cartridge; a central tube I is sleeved in the catalyst cartridge, the upper port of the central tube I is closed, and the lower port is connected to the adiabatic section; a plurality of internal air intake 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 protrusions are provided on the side surface 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, and the cavity 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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