Novel conversion furnace

Abstract

The invention discloses a novel shift converter, which comprises an internal heat exchanger (1), a catalyst basket (2), an inner shell (3), a central tube (4), an outer shell (8) and a cover (11), and is characterized in that the center of the internal heat exchanger (1) is inserted into the central tube (4), the catalyst basket (2) is arranged outside the internal heat exchanger (1), the catalyst basket (2) is arranged in the inner shell (3), the inner shell (3) is placed in the outer shell (8) and covered with the cover (11), and the top end of the internal heat exchanger (1) is connected with the top end of the inner shell (3). The shift converter has the advantages of long connection time between the process gas and the catalyst, large contact area, complete conversion, high catalyst utilization rate, low manufacturing and mounting cost, small temperature difference and difficulty in damage of the shift converter.

Description

Technical Field

[0001] The invention belongs to the technical field of chemical industry, and in particular relates to a novel conversion furnace. Background Art

[0002] The shift furnace is an indispensable core device in current chemical production. Its main working purpose is to produce hydrogen from carbon monoxide, and it is the core equipment for producing hydrogen at present. Since the direct reaction speed of carbon monoxide and water vapor is very slow, if a catalyst is used, the reaction speed can be accelerated, which is conducive to the shift reaction. In the prior art, since the reaction is an exothermic reaction with constant volume, the pressure has little effect on the reaction balance, but the temperature during the reaction process has a great influence on whether the reaction is a rightward reaction and the service life of the catalyst (mainly divided into the following points). The latest cobalt (C0) and molybdenum (Mo) catalysts have Mo as the active ingredient, and the component M0 has a use temperature range of 200℃~470℃. Excessive temperature will cause permanent damage to the catalyst sintering, and form side reaction products in the process. The main carriers are: ALOs, AbOs / MgO, and magnesium and aluminum crystals are carriers. Alkali metal potassium is often added to the catalyst as a promoter to improve its low-temperature activity. When selecting a specific catalyst, it is necessary not only to pay attention to the properties of the catalyst, but also to pay attention to its strength. The activity of the catalyst itself should not be a problem. However, the activity and strength of the catalyst are generally inversely proportional, that is, the better the activity, the relatively poorer the strength of the catalyst itself. Of course, as a catalyst manufacturer, in the process of manufacturing the catalyst, the relationship between the two has been taken into account and a certain balance point has been found, but this balance point is not suitable for any working condition. Therefore, when selecting a catalyst, it is also necessary to find a balance point for its operation to prevent the catalyst bed from being too resistant due to its poor strength, which affects the production of the entire system. In order to make the conversion catalyst have good activity at a wider temperature, a large amount of K2CO3 promoter will be added, and it can be operated at 160-500℃, but potassium is easily lost in actual use. In addition, the catalyst carrier is also easily damaged, the strength is reduced, and it is damaged. Especially in the traditional conversion furnace that is currently widely used, the catalyst is subject to high pressure difference, the temperature distribution in the catalyst bed is uneven, and the catalyst is easily damaged under local high temperature conditions. As a kind of low-transformation catalyst, in the selection of cobalt-molybdenum catalysts, try to use catalysts with small particle size to improve the effective activity of the catalyst per unit volume. But also pay attention to the pressure drop allowed by the bed. In addition, when using oxygen-containing semi-water gas to produce hydrogen, an anti-toxic agent with good anti-toxic performance should be selected to prevent oxygen from affecting the service life of the catalyst. The methanation reaction is a highly exothermic reaction, which will cause the catalyst to rise rapidly, causing the catalyst to overheat, sinter the catalyst, and grow the micropores of the catalyst, resulting in a decrease in catalyst activity. The treatment method is to quickly stop the system, cut off the gas, and release the pressure. The methanation reaction equation is: CO+3H2=CH4+H2O, CO2+4H2=CH4+2H2O, both of which are reversible reactions.Therefore, increasing the CO concentration can promote the methanation reaction, and increasing the water vapor ratio can inhibit the methanation reaction. The carbon monoxide shift reaction is a reversible exothermic reaction. The reaction proceeds very slowly under normal conditions and is far from meeting the needs of industrial production. Under the action of the shift catalyst, the speed of the shift reaction can be significantly increased, and side reactions can be prevented and reduced. According to the principle of chemical equilibrium, the higher the reaction temperature, the lower the equilibrium conversion rate of the shift reaction. In an adiabatic shift reactor, in order to obtain a higher CO conversion rate, it is necessary to reduce the catalyst bed inlet temperature as much as possible to make the bed outlet temperature as low as possible, which requires the catalyst to have good low-temperature activity. The higher the temperature during the use of the catalyst, the higher the steam-gas ratio used. If a catalyst with good low-temperature activity is used, the entire catalyst bed can be operated at a lower temperature, which can reduce the operating steam-gas ratio of the shift system and save steam consumption. Catalyst loading: The loading of the catalyst in the traditional shift furnace is very important, which will directly affect the pressure drop and airflow distribution of the bed, thereby affecting the normal performance of the catalyst. When the catalyst water vapor ratio (the ratio of added water vapor to the process gas participating in the reaction) is high, a reverse sulfidation reaction will occur: MoS2+2H2O=MoO2+2H2S. In principle, the catalyst has no upper limit requirement for the H2S content in the raw gas, but has a lower limit requirement for the H2S content in the raw gas. When the H2S content in the process gas is low, reverse sulfidation will occur and the catalyst will be deactivated. The metal sulfide, the active component of the conversion catalyst, is converted into a metal oxide under certain conditions and releases hydrogen sulfide, thereby making the conversion catalyst inactive. This phenomenon is called the reverse sulfidation reaction of the sulfur-resistant conversion catalyst. Among them, the oxidation and sulfur release of MoS2 are the main phenomena. The reaction formula is: MoS2+2H2O=MoO2+2H2S reverse sulfidation reaction occurs. It has been mentioned above that Mo is the main catalyst and Co is the co-catalyst. Therefore, for the sulfidation of cobalt-molybdenum catalysts, it mainly completes the sulfidation of Mo during use. Mo generally exists in three valence states during sulfidation: Mo+6, Mo+5, and Mo+4. Mo+5 is related to the conversion activity in the conversion reaction. However, in practice, Mo+5 and Mo+4 exist at the same time, so Mo cannot be completely reduced. In order to ensure the safety and thoroughness of its sulfidation, pay attention to the following points during sulfidation. The so-called desulfurization is that the active components of the catalyst, CoS and MoS2, undergo the reverse reaction of sulfidation under certain temperature, steam, and HS conditions. They are transformed into inactive COO and MoO2 again, mainly the desulfurization of MoO. Generally speaking, higher bed temperature, higher steam-gas ratio, and lower HS content are the three major reasons for desulfurization. Only when these three reasons are met at the same time will desulfurization occur. Therefore, in the actual operation of traditional catalysts, it is necessary to try to avoid these three conditions being met at the same time. The main reason is caused by abnormal process operating conditions, such as too high inlet temperature, too low hydrogen sulfide content in the gas, and too high steam-gas ratio.Desulfurization is most likely to occur when the conversion system is just started. At this time, the gas volume is small, which is most likely to cause desulfurization due to a high steam-gas ratio. In daily production operations, it is found that steam cannot be used to cool down when the catalyst bed temperature rises sharply. When the cold secondary line is opened in normal production, a small steam-gas ratio is used and the inlet temperature of the imported H2S is within the index and not too high, which is higher than the dew point temperature of the gas. The desulfurization reaction will also make the catalyst inactive. Moreover, when the water-gas ratio is too high, it will also destroy the catalytic strength, causing the catalyst to pulverize, which will also make the catalyst inactive and cause problems such as increased pressure difference in the conversion furnace and impurities in the process gas. When the water-gas ratio is low and the catalyst reaction temperature is too high (>450℃\500℃), methanation reaction will occur. This reaction is a strong exothermic reaction: 3H2+CO=CH4+H2O+Q. The methanation reaction will not only not convert into hydrogen, but also consume hydrogen to generate useless CH4. CH4 increases the trouble of handling subsequent processes and increases the load of the gas purification system. At the same time, it will cause the original temperature of the catalyst to rise sharply and burn the catalyst. The current converter structure is axial, and the flow direction of the process gas is axial, which limits the diameter of the converter equipment and increases the manufacturing and installation costs. If the diameter of the axial converter is too large, it will cause the process gas to flow sideways. In order to prevent gas flow sideways, the height of each bed section of the traditional converter should not be less than Im. The bed height-to-diameter ratio is 0.5-1.0. When the catalyst is loaded, wire mesh should be laid on the top and bottom of the catalyst. Two layers are laid below to prevent catalyst leakage: one layer is laid on the top, and then 50-100mm high refractory balls or aluminum balls are placed on the mesh to prevent condensed water from directly contacting the catalyst. Corrosion often occurs. The cause of the corrosion phenomenon is the dew point when the gas is mixed, which produces dew point corrosion. Generally, in this process configuration, the corrosion that occurs is basically dew point corrosion and cavitation corrosion, supplemented by H2S corrosion. Of course, when condensed water appears, there is a large amount of H2S in the gas, and there is a dead zone for gas flow, H2S corrosion is also relatively serious. The large temperature difference of the bed in the same plane causes damage to the converter. In addition, due to the influence of the axial design, the current conversion furnace has a high pressure difference, a fast air velocity, a short contact time between the process gas and the catalyst, and a small contact area, which is incomplete. The current conversion system is an incomplete conversion, which means that CO cannot be 100% converted into hydrogen in the conversion system. The catalyst utilization rate is low under the same catalyst filling amount, and the conversion furnace is exposed to highly corrosive substances such as hydrogen and hydrogen sulfide. A single material is prone to corrosion and cracking. In such a complex environment, coupled with the increasing pressure of the current coal chemical production system, the current ordinary conversion furnace has a high manufacturing cost and is not safe during operation. It is not as safe and reliable as the double-layer design. Summary of the invention

[0003] The object of the present invention is to overcome the above-mentioned disadvantages and provide a new type of conversion furnace with slow space velocity, high catalyst utilization, low manufacturing and installation costs, small temperature difference, not easy to be damaged, and no corrosion and cracking.

[0004] A new type of conversion furnace of the present invention includes an internal heat exchanger, a catalyst basket, an inner shell, a central tube, and a cover, and is characterized in that: the central tube is inserted into the center of the internal heat exchanger, a catalyst basket is installed outside the internal heat exchanger, the catalyst basket is installed in the inner shell, the inner shell is placed in the outer shell and covered with a cover, and the top of the internal heat exchanger is connected to the top of the inner shell.

[0005] The internal heat exchanger is composed of an outer tube, an inner tube and a waste heat tube. The outer tube is installed outside the inner tube, and a plurality of waste heat tubes are installed on the outer tube. The waste heat tube connects the gap between the outer tube and the inner tube, and the top of the outer tube is connected to the top of the inner shell.

[0006] The catalyst basket is composed of an outer cover, an inner cover, a baffle, a support seat A, and a support seat B. A plurality of baffles are installed on the inner cover, and the baffles block a plurality of holes set on the inner cover. The outer cover is placed outside the baffles. Support seats A and support seats B are respectively installed on the outer cover and the inner cover. Support seat A is placed on the inner shell, and an internal heat exchanger is placed on support seat A. A plurality of through holes are respectively set on the outer cover and the inner cover.

[0007] The top of the internal heat exchanger is respectively inserted with a filler pipe A and a steam outlet pipe A, the filler pipe A is connected to the upper end of the inner shell, an annular pipe is installed on the upper end of the inner shell, and the annular pipe is connected to the filler pipe B.

[0008] The bottom end of the internal heat exchanger is connected to the downcomer, the downcomer is connected to the steam drum, and the steam drum is respectively connected to the steam outlet pipe B and the steam drum water inlet pipe.

[0009] The cover is respectively provided with a carbon monoxide detector and a thermocouple tube, and the carbon monoxide detector and the thermocouple tube are respectively inserted into the catalyst basket.

[0010] An inlet and a gas outlet are respectively arranged below the shell, and an arc-shaped baffle is arranged inside the inlet.

[0011] Compared with the prior art, the present invention has obvious beneficial effects; it can be seen from the above technical scheme: by inserting a central tube in the center of the internal heat exchanger, a catalyst basket is installed on the outside of the internal heat exchanger, the catalyst basket is installed in the inner shell, the inner shell is placed in the outer shell and covered with a lid, and the top of the internal heat exchanger is connected to the top of the inner shell. Through the use of heat-insulating and corrosion-proof designs for the inner and outer shells, the annular gap temperatures of the inner and outer shells are always kept within the inlet process gas temperature range. The outer shell is made of a material that can withstand high pressure, but does not need to withstand the high temperature in the furnace body and damage under the complex corrosion environment of high-temperature corrosive gas. The main process gas line enters along the annular gap between the inner and outer shells to make the pressure outside the inner shell equal to the pressure inside, so the inner shell does not bear pressure. The material of the inner shell withstands high temperature but not high pressure. In this way, the material used in the equipment manufacturing process is single and does not need to use expensive and difficult-to-process alloy materials; the use of axial and radial design also avoids the inner shell of the conversion furnace from being easily damaged and having a small pressure-resistant area; because it is an inner and outer shell design, the process gas is in the middle, and the gas is the best insulation material, while reducing the temperature loss between the beds after the system is stopped, reducing the catalyst heating time, and no longer needing to use insulation materials to insulate the conversion furnace. The axial and radial design of the present invention is not limited by the diameter of the equipment, the flow direction of the material is axial and radial, and heat can be exchanged by itself. The heat between the beds can be exchanged by itself, which is more uniform than the heat absorption of the landfill-type shell-and-tube heat exchanger and does not occupy the space for filling the catalyst. The axial and radial design reduces the overall pressure drop of the conversion tower. Catalysts with smaller particle sizes can be selected. This is mainly to increase the bulk density of the catalyst, reduce the air velocity, and increase the contact time between the process gas and the catalyst. The axial and radial design can increase the contact area between the catalyst and the process gas. The process gas after the reaction is sent out of the catalyst bed because of the material flow direction formed under the special structure of this conversion furnace. The process gas after the reaction does not enter the catalyst bed again after being sent out of the catalyst bed. The original conversion system material only enters from the surface of the upper catalyst. As the process gas enters the deeper layer of the catalyst, the process gas has already reacted when it contacts the catalyst. At this time, as the process gas flows deeper into the catalyst, the more products will be converted, that is, the concentration of the substances participating in the reaction will be reduced, which is not conducive to the reaction. Another thing is that the higher the concentration of the participating reactants, the more intense the reaction, and the higher the heat released. Therefore, the upper catalyst of the ordinary conversion furnace is prone to overheating. At present, the filling amount of the conversion furnace catalyst is certain. The mixing of the reaction products in the participating reactants does not reduce the concentration of the participating reactants. The amount of catalyst is certain, which also reduces the contact amount between the catalyst and the participating reactants. The axial and radial flow of materials reduces the concentration of products, thereby increasing the concentration of reactants, promoting the reaction to the right, and increasing the efficiency of the conversion furnace. Moreover, the layer temperature is uniform, which is not easy to burn the catalyst and methanation reaction.The built-in internal heat exchanger design is adopted. When the process gas leaves each catalyst bed layer, the high-temperature process gas after leaving the catalyst bed layer is baffled by the baffle plate and then exchanges heat with the waste heat pipe, so that the high-temperature process gas of the previous catalyst layer enters the next bed layer at a certain temperature to continue the reaction. The high-temperature process gas after the baffle plate increases the heat exchange area and time with the waste heat pipe and avoids the scouring of the waste heat pipe by the high-temperature process gas, which also increases the heat recovery efficiency. In addition, the bed temperature can be accurately adjusted through the temperature adjustment sub-line of the first bed layer and the second bed layer to truly achieve the advantages of isothermal conversion and temperature precision adjustment. The inlet between each catalyst bed is designed with a steam supply pipe to increase the water vapor ratio. The water vapor ratio between each bed can be controlled separately. The steam supply pipe uses self-produced steam, which avoids the preheater process before use. It is in hot standby state at any time and can flexibly adjust the water vapor ratio of the process gas of each catalyst bed according to actual conditions; the steam supply device can also be completely closed according to actual production needs, and no preheating and heating operations are required when it is put into use again; the steam drum is an existing technology, and the steam supply device with a water vapor ratio enters the catalyst bed after reverse contact with the process gas, reducing the impact of the process gas and water vapor on the catalyst. The use of steam to adjust the water vapor ratio increases the contact area between gas and water, and the atomization effect and spraying area are not affected by the flow rate and the constraints of the fixed test nozzle; it will not cause water droplet quenching to the catalyst and equipment, causing damage to the catalyst, and whether the second bed will pass through the central tube heat exchanger for heat exchange after water vapor supplementation, even if the upstream process gas temperature is low, there will be a certain water vapor ratio. It adopts a three-bed catalytic, two temperature-adjusting sub-lines, and a built-in internal heat exchanger design, and the process gas can be used to adjust the temperature of each bed according to actual conditions. Both temperature-adjusting secondary lines adopt isothermal cooling after heat exchange with the internal heat exchanger, which can ensure that the catalyst bed temperature is lowered rather than cooled by a quenching method. This design further ensures the reaction rate of the catalyst and the service life of the catalyst, while reducing the installation of heat exchangers and other equipment when changing the overall design, reducing the cost of engineering construction. The three-bed, axial-radial, isothermal change, isothermal temperature adjustment, and steam supply pipe design of the variable tower furnace can expand the selection range of catalysts. Reduce the bottleneck of using high-quality catalysts; adopt the design of using and protecting at the same time to increase the use time of the catalyst; reduce the land area and equipment for the construction of the variable section, which is only 1 / 3 of the current land area for the conversion, reducing the maintenance cost and overhaul cost of the equipment.The new conversion furnace adopts a three-bed design, but each process gas, including the process gas of the two temperature-adjusting cold lines, will enter the catalyst bed at one time in the order of 1, 2, and 3 beds, which increases the utilization rate of the catalyst and the reaction efficiency. The new conversion furnace can be freely matched with heat exchangers, waste heat boilers and other equipment according to actual production needs without restrictions. The waste heat pipe of the built-in internal heat exchanger adopts a corrugated pipe design; the waste heat pipe adopts a serpentine pipe design. These two designs can effectively ensure that the free expansion of the pipeline releases stress and will not cause damage to the components of the equipment due to stress. The bottom of the bed adopts the arch design with the best load-bearing capacity in architecture, which provides good support for catalysts, inter-bed heat exchangers and other equipment. In short, the present invention has high pressure difference, fast air velocity, long contact time between process gas and catalyst, large contact area, complete conversion, high catalyst utilization, low manufacturing and installation costs, and small temperature difference. The conversion furnace is not easy to be damaged. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] Figure 1 It is a schematic diagram of the structure of the present invention; Figure 2 is a schematic structural diagram of an internal heat exchanger of the present invention; Figure 3 yes Figure 2 A cross-sectional view of Figure 4 It is a structural schematic diagram of the dense catalyst basket of the present invention; Figure 5 yes Figure 4 A cross-sectional view of Figure 6 It is a schematic diagram of the structure of the inner cover and the baffle of the present invention; Figure 7 It is a schematic structural diagram of the inner cover of the present invention; Figure 8 It is a structural schematic diagram of the baffle of the present invention; Fig. 9 It is a usage state diagram of the present invention.

[0013] Marking in the figure 1. Internal heat exchanger, 2. Catalyst basket, 3. Inner shell, 4. Center tube, 5. Baffle, 6. Inlet, 7. Gas outlet, 8. Outer shell, 9. Filling pipe A, 10. Steam outlet pipe A, 11. Cover, 12. Carbon monoxide detector, 13. Steam drum, 14. Steam outlet pipe B, 15. Thermocouple tube, 16. Steam drum water inlet pipe, 17. Connecting pipe, 18. Filling pipe B, 19. Downcomer, 20. Annular pipe, 21. Start-up auxiliary line, 101. Outer tube, 102. Inner tube, 103. Waste heat pipe, 201. Outer cover, 202. Inner cover, 203. Baffle, 204. Support seat A, 205. Support seat B. DETAILED DESCRIPTION

[0014] The specific implementation methods, structures, features and functions of the present invention are described in detail below in conjunction with the accompanying drawings and preferred embodiments.

[0015] The purpose of the present invention and the solution of its main technical problems are achieved by adopting the following technical solutions: A novel conversion furnace of the present invention comprises an internal heat exchanger 1, a catalyst basket 2, an inner shell 3, a central tube 4, a baffle 5, an inlet 6, a gas outlet 7, an outer shell 8, a supplementary pipe A9, a steam outlet pipe A10, a cover 11, a carbon monoxide detector 12, a steam drum 13, a steam outlet pipe B14, a thermocouple tube 15, a steam drum water inlet pipe 16, a connecting pipe 17, a supplementary pipe B18, a downcomer 19, and a ring pipe 20, wherein the central tube 4 is inserted into the center of the internal heat exchanger 1, a catalyst basket 2 is installed outside the internal heat exchanger 1, and the catalyst basket 2 The inner shell 3 is installed in the inner shell 3, the inner shell 3 is placed in the outer shell 8 and covered with a cover 11, the top of the internal heat exchanger 1 is connected to the top of the inner shell 3, the internal heat exchanger 1 is composed of an outer tube 101, an inner tube 102, and a waste heat pipe 103, the outer tube 101 is installed outside the inner tube 102, and a plurality of waste heat pipes 103 are installed on the outer tube 101, and the waste heat pipe 103 communicates with the gap between the outer tube 101 and the inner tube 102, the top of the outer tube 101 is connected to the top of the inner shell 3, and the catalyst basket 2 is composed of an outer cover 201, an inner cover 202, a baffle 203, a support seat A204, The support seat B205 is composed of a plurality of baffles 203 installed on the inner cover 202, the baffles 203 block a plurality of holes set on the inner cover 202, an outer cover 201 is placed outside the baffle 203, and a support seat A204 and a support seat B205 are respectively installed on the outer cover 201 and the inner cover 202. The support seat A204 is placed on the inner shell 3, and an internal heat exchanger 1 is placed on the support seat A204. A plurality of through holes are respectively set on the outer cover 201 and the inner cover, and a filling pipe A9 and a steam outlet pipe A10 are respectively inserted into the top of the internal heat exchanger 1, and the filling pipe A9 is connected to the upper end of the inner shell 3, and an annular tube 20 is installed on the upper end of the inner shell 3, and the annular tube 20 is connected to the filler tube B18. The bottom end of the internal heat exchanger 1 is connected to the downcomer 19, and the downcomer 19 is connected to the steam drum 13. The steam drum 13 is respectively connected to the steam outlet pipe B14 and the steam drum water inlet pipe 16. The cover 11 is respectively installed with a carbon monoxide detector 12 and a thermocouple tube 15, and the carbon monoxide detector 12 and the thermocouple tube 15 are respectively inserted into the catalyst basket 2. The lower side of the outer shell 8 is respectively provided with an inlet 6 and a gas outlet 7, and the inlet 6 is provided with an arc baffle 5.

[0016] When used; see Fig. 9, the process gas is divided into four routes before entering the new type of furnace, namely the main line entering from the inlet 6, the first temperature-adjusting auxiliary line supplementary pipe B18, the second temperature-adjusting auxiliary line supplementary pipe A9, and the start-up auxiliary line 21. The four-way process gas can adjust the gas flow or cut off the gas through the regulating valve. Enter the furnace main line; the process gas enters from the inlet 6 at the bottom of the outer shell 8, rises to the top through the annular gap between the outer shell 8 and the inner shell 3 and enters the central tube 4, and then enters the first, second, and third central tubes 4 of the internal heat exchanger 1 in turn. There are three layers of internal heat exchangers 1, and the central tube 4 goes all the way to the bottom of the third layer. At the same time, the process gas of the central tube 4 will bring part of the heat of the first layer into the overall heat of the second and third layers of the balanced conversion furnace, and exchange heat with the built-in waste heat pipes 103 of the first, second and third layers at one time. The temperature of the process gas after heat exchange rises, and the outer tube 101 of the internal heat exchanger 1 continues to rise, and then enters the first catalyst layer from the axial and radial directions of the catalyst layer of the catalyst basket 2 for conversion reaction; the process gas after exiting the first catalyst layer of the catalyst basket 2 enters the outer tube 101 of the first layer of the internal heat exchanger 1 to exchange heat with the inner tube 102 and the waste heat pipe 103 of the built-in internal heat exchanger 1, and then enters the second layer of the catalyst basket 2 from the bottom; the gas exiting the second catalyst layer enters the central outer tube 101 of the second bed layer of the built-in internal heat exchanger 1 to exchange heat with the inner tube 102 and the waste heat pipe 103 of the built-in internal heat exchanger 1, and then enters the third catalyst bed layer of the catalyst basket 2 for reaction. The main line gas entering the tower from the first inlet 6 can also play a role in regulating the heat exchange of the inlet temperature of the first, second and third layers. The second feed pipe B18 is a secondary line for regulating the temperature of the gas at the inlet of the first layer of the catalyst basket 2. The gas in this line merges with the main line gas entering the conversion furnace at the inlet of the catalyst layer of the first catalyst basket 2, and is used to regulate the temperature of the process gas at the inlet of the first catalyst layer of the catalyst basket 2 and the first catalyst layer of the catalyst basket 2. The third feed pipe A9 is a secondary line for regulating the temperature of the gas at the inlet of the second layer of the catalyst basket 2. The gas in this line enters the first layer of the internal heat exchanger 1 through the inner annular gap of the central waste heat pipe 103 of the internal heat exchanger 1, and mixes with the main line gas from the third and second beds of the internal heat exchanger 1 to exchange heat with the waste heat pipe 103 of the waste heat boiler built into the first catalyst layer of the catalyst basket 2, so as to regulate the process gas temperature at the outlet of the first catalyst layer of the catalyst basket 2 and the inlet of the second catalyst bed of the catalyst basket 2, and then enters the first layer of the catalyst basket 2; the fourth line is the start-up secondary line 21, which directly enters the first catalyst layer of the catalyst basket 2 after being heated by the start-up heating furnace to initially heat the catalyst. Catalyst temperature detection, inlet and outlet and plane temperature of each layer of catalyst basket 2, gas drawn out of the air capillary of carbon monoxide detector is analyzed by mass spectrometer for gas composition. Keep track of the operation status of the converter at all times. Each thermocouple tube is equipped with 12 thermocouples; 2 carbon monoxide monitoring points at the outlet of the catalyst layer; a total of 12 temperature measurement points; 2 carbon monoxide monitoring points. There are 16 temperature measurement points on the high-pressure shell 8 of the converter, and there is no fixed number of these temperature points, which are designed according to actual needs.It is used to monitor the temperature of the high-pressure shell. The temperature measuring point adopts a sleeve installation for easy disassembly and maintenance. The carbon monoxide monitoring point adopts an air bleed type to draw out the gas at the outlet of the measured catalyst bed for detection. This converter is designed according to the current common medium and high pressure. The by-product steam is 1.0MPa and 180℃, so a built-in internal heat exchanger 1 is designed between the first, second and third catalyst layers of the catalyst basket 2. The steam used for the steam supply pipe needs to be re-quoted from the steam network. It can also be designed according to the actual factory needs. For example, if the steam supply device and the by-product steam with higher by-product pressure are to be taken into account, for example, the by-product steam pressure is 4.0MPa, 250℃-5.0MPa, 264℃, a heat exchanger system is designed between the first and second catalyst layers of the catalyst basket 2, or the actual process gas temperature entering the internal heat exchanger 1 is controlled by a temperature regulating secondary line. It mainly depends on the performance parameters of the catalyst and the process requirements. The steam process flow, qualified desalted water enters the steam drum and enters the built-in internal heat exchanger 1 through the downcomer 19 and the waste heat pipe 103 Bottom; the temperature of the desalted water rises after heat exchange with the process gas from the third bed of the catalyst basket 2 through the waste heat pipe 103 inside the conversion furnace, and part of the desalted water is evaporated by the heat; the steam continues to rise along the waste heat pipe 103, exchanges heat with the process gas from the second bed through the waste heat pipe 103 of the second bed, and then the steam temperature continues to rise, exchanges heat with the process gas from the first bed through the waste heat pipe 103 of the first bed, and is sent to the multiple steam separators in the steam drum 13 through the steam pipeline for steam-water separation, and after obtaining qualified steam, it is sent to the steam network through the steam outlet pipe B14. As the steam continues to rise along the waste heat pipe 13, it will exchange heat with the process gas from the temperature-adjusting secondary line of the central pipe 4 of the converter and the second bed layer supplement pipe A9 of the internal heat exchanger 1. On the one hand, the process gas can be used to adjust the temperature of the steam to ensure the quality of the steam; on the other hand, the steam output can be increased or decreased according to the actual production needs to balance the steam network, and the production can be met according to the actual working conditions; on the other hand, the process gas from the temperature-adjusting secondary line and the process gas entering the central pipe 4 from the main line can be heat-exchanged so that the temperature difference between the temperature-adjusting secondary line and the catalyst basket 2 bed layer can be controlled to prevent quenching, thereby protecting the catalyst and the converter. In the steam-water supplement process, the steam from the steam network is divided into three routes, which are controlled by three supplementary steam control valves respectively, and distributed through the supplementary steam devices of each bed layer, with one steam outlet pipe B14 and one steam outlet pipe at each end of the connecting pipe 17. The upper part of the three-layer catalyst is in reverse contact with the process gas entering the bed layer to increase the water-vapor ratio of the process gas and ensure the process gas index out of the conversion tower. The three-way steam supplement is controlled separately through three valves according to the actual production situation; during the start-up process, if the water-gas ratio needs to be adjusted, it can be adjusted through the steam of the official website.

[0017] The above description is only a preferred embodiment of the present invention and does not limit the present invention in any form. Any simple modification, equivalent change and modification made to the above embodiment according to the technical essence of the present invention without departing from the technical solution of the present invention still falls within the scope of the technical solution of the present invention.

Claims

1. A novel converter, comprising an internal heat exchanger (1), a catalyst basket (2), an inner shell (3), a central tube (4), an outer shell (8), and a cover (11), characterized in that: The center of the internal heat exchanger (1) is inserted into the center tube (4), and a catalyst basket (2) is installed outside the internal heat exchanger (1). The catalyst basket (2) is installed in the inner shell (3). The inner shell (3) is placed in the outer shell (8) and covered with a cover (11). The top of the internal heat exchanger (1) is connected to the top of the inner shell (3).

2. A novel converter according to claim 1, characterized in that: The internal heat exchanger (1) is composed of an outer tube (101), an inner tube (102), and a waste heat tube (103); the outer tube (101) is installed outside the inner tube (102); a plurality of waste heat tubes (103) are installed on the outer tube (101); the waste heat tubes (103) are connected to the gap between the outer tube (101) and the inner tube (102); and the top end of the outer tube (101) is connected to the top end of the inner shell (3).

3. A novel converter according to claim 1, characterized in that: The catalyst basket (2) is composed of an outer cover (201), an inner cover (202), a baffle (203), a support seat A (204), and a support seat B (205); a plurality of baffles (203) are installed on the inner cover (202); the baffles (203) block a plurality of holes provided on the inner cover (202); an outer cover (201) is placed outside the baffles (203); a support seat A (204) and a support seat B (205) are respectively installed on the outer cover (201) and the inner cover (202); the support seat A (204) is placed on the inner shell (3); an internal heat exchanger (1) is placed on the support seat A (204); and a plurality of through holes are respectively provided on the outer cover (201) and the inner cover.

4. A novel converter according to claim 1, characterized in that: A patching pipe A (9) and a steam outlet pipe A (10) are respectively inserted into the top end of the internal heat exchanger (1); the patching pipe A (9) is connected to the upper end of the inner shell (3); an annular pipe (20) is installed at the upper end of the inner shell (3); and the annular pipe (20) is connected to the patching pipe B (18).

5. A novel converter according to claim 1, characterized in that: The bottom end of the heat exchanger (1) is connected to a downcomer (19), the downcomer (19) is connected to a steam drum (13), and the steam drum (13) is respectively connected to a steam outlet pipe B (14) and a steam drum water inlet pipe (16).

6. A novel converter according to claim 1, characterized in that: The cover (11) is respectively mounted with a carbon monoxide detector (12) and a thermocouple tube (15), and the carbon monoxide detector (12) and the thermocouple tube (15) are respectively inserted into the catalyst basket (2).

7. A novel converter according to claim 1, characterized in that: An inlet (6) and a gas outlet (7) are respectively arranged below the shell (8), and an arc-shaped baffle (5) is arranged inside the inlet (6).

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