CN215464287U - Low-carbon alkane dehydrogenation tube array type fixed bed reactor - Google Patents
Low-carbon alkane dehydrogenation tube array type fixed bed reactor Download PDFInfo
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Abstract
The utility model discloses a low-carbon alkane dehydrogenation tubular fixed bed reactor, wherein a shell of the low-carbon alkane dehydrogenation tubular fixed bed reactor is provided with an outer heat insulation layer; the shell is internally provided with a tube array heat exchange tube, the upper end of the tube array heat exchange tube is provided with an upper sealing plate, the lower end of the tube array heat exchange tube is provided with a lower supporting plate, and a gap is formed between adjacent heat exchange tubes and becomes a closed heat exchange cavity; the shell is provided with a high-temperature molten salt inlet and a high-temperature molten salt outlet which are respectively communicated with the heat exchange cavity; a catalyst reaction bed layer is arranged in the tube type heat exchange tube; the high-temperature molten salt inlet is connected with the discharge hole of the molten salt heating furnace, the high-temperature molten salt outlet is connected with the feed inlet of the molten salt groove, and the discharge hole of the molten salt groove is connected with the feed inlet of the molten salt heating furnace. The reactor ensures that the reaction bed layer is in the optimal reaction temperature range for a long time, is helpful to prevent the local temperature of the catalyst bed layer from being overhigh, and prevents the rapid formation and accumulation of coke. The single-stage reaction time is prolonged, and the conversion efficiency is improved, so that frequent production halt and maintenance are avoided.
Description
Technical Field
The utility model relates to the technical field of petrochemical production equipment, in particular to a tubular fixed bed reactor for dehydrogenation of low-carbon alkane, which takes high-temperature molten salt as a heat carrier to supply heat to a catalyst bed layer in a heat exchange tube.
Background
The dehydrogenation reaction of the low-carbon alkane is a process for converting a large amount of low-carbon alkane with low price into corresponding alkene with high added value which is in short supply in the market, and has important research significance and economic value.
In most of the known dehydrogenation processes and production devices, the heat required by the dehydrogenation reaction is generated by a heater of reaction raw materials and regeneration air in front of the reactor, and is introduced into the reaction gas from the heater, and then the heat is brought into the reactor.
In order to obtain the conversion rate required by industrial production, the temperature of the heater is higher than that of dehydrogenation reaction, so that the energy consumption is high, and the low-carbon alkane is easily subjected to large-scale thermal cracking in the heater, so that the efficiency of the conversion process of the dehydrogenation reaction and the efficiency of a production device are low. Therefore, it is necessary to supplement the catalyst bed with sufficient heat while avoiding excessive heater temperature; also, the production of coke in the production apparatus and the reactor is avoided as much as possible.
In the industrialized process technology and production device, the Catofin technology of Lummus corporation is very representative, and the low-carbon alkane is converted by batch reaction-regeneration by adopting a fixed bed reactor and a traditional curdly process conversion mode. Firstly, heating propane to 590-620 ℃, then introducing the propane into a reactor for conversion, and quickly reducing the temperature of a catalyst bed layer by 40-50 ℃ after reacting for ten minutes; therefore, the reaction needs to be stopped, and the catalyst bed layer needs to be regenerated by hot air; after the catalyst bed is regenerated and heated to 650 ℃ by high-temperature hot air, the reactor is deoxidized, and then propane feed gas with 590-620 ℃ is introduced into the next cycle of reaction, wherein the period of each cycle is 20-22 minutes.
In the production process of the process, the reactor in the prior art has low conversion efficiency and large equipment, and the service life is greatly shortened due to frequent opening and closing actions of a control valve. Moreover, the refractory brick material lining commonly used in the reactor is easy to have the problems of thermal shock damage, cracking, falling off and the like, so that frequent production halt maintenance is easy to cause, and the long-period operation of the device is seriously influenced.
The STAR process of Phillips company and the Linde process of Linde AG company are also representative low-carbon alkane production process technologies, a tubular fixed bed reactor is adopted, a catalyst is filled in a tube array in the reactor, and the tube array is heated by using a heat carrier such as flue gas; however, the heat loss in the whole process of the process is large, so that the energy consumption in the conversion process is high, and the cost of the reactor is high.
Although the fixed bed reactor has the advantage of relatively simple structure, the common outstanding problems are that a local high-temperature region is easy to appear, so that the carbon deposition of the catalyst is serious, the conversion efficiency and the yield are reduced, the production cost is improved, the operation condition tends to be harsh, and the difficulty in the large-scale industrial production process is increased.
SUMMERY OF THE UTILITY MODEL
Aiming at the problems in the prior art, the utility model aims to provide a reactor which can improve the conversion performance and efficiency of the dehydrogenation reaction of low-carbon alkane, prolong the single-stage conversion reaction time and prolong the long-period operation of the device.
In order to solve the technical problems, the utility model adopts the following technical scheme:
a low-carbon alkane dehydrogenation tubular fixed bed reactor comprises a shell, wherein the upper end of the shell is provided with a material inlet, and the lower end of the shell is provided with a material outlet; the shell is a hollow metal structure made of stainless steel materials and is provided with an outer heat insulation layer; the shell, the upper sealing plate and the lower supporting plate enable the gaps among the tube type heat exchange tubes to be closed heat exchange cavities; the shell is provided with a high-temperature molten salt inlet and a high-temperature molten salt outlet which are respectively communicated with the heat exchange cavity; a catalyst reaction bed layer is arranged in the tube array type heat exchange tube; the high-temperature molten salt inlet is connected with a discharge hole of the molten salt heating furnace, the high-temperature molten salt outlet is connected with a feed inlet of the molten salt groove, and the discharge hole of the molten salt groove is connected with the feed inlet of the molten salt heating furnace.
The high-temperature molten salt inlet is located at the lower section of the tube type heat exchange tube, the high-temperature molten salt outlet is located at the upper section of the tube type heat exchange tube, the high-temperature molten salt inlet is located below the catalyst reaction bed layer, and the high-temperature molten salt outlet is located above the catalyst reaction bed layer.
The molten salt tank is connected with the molten salt heating furnace through a connecting pipe, and a molten salt pump is arranged on the connecting pipe.
Inert ceramic balls are filled in the heat exchange tubes and are positioned below the catalyst bed layer.
The material inlet comprises a low-carbon alkane raw material inlet, a high-temperature hot air inlet and a high-temperature steam/process gas/reducing gas inlet which are mutually independent; the high-temperature steam/process gas/reducing gas inlet is connected above the reactor and then connected to a material inlet pipeline connected with the reactor; the lower end of the material inlet pipeline is connected with a distributor for distributing materials.
The material outlet comprises a hydrocarbon product outlet, a waste heat air outlet and an evacuation/emergency outlet which are independent of each other.
The shell is provided with at least two thermocouple interfaces, thermocouples are inserted into the shell, and the temperature of the upper end and the lower end of the shell-and-tube heat exchange tube is monitored.
According to the low-carbon alkane dehydrogenation tubular fixed bed reactor provided by the utility model, the heat required by dehydrogenation reaction is continuously provided by high-temperature molten salt through the heat exchange tube, so that the temperature distribution of a catalyst bed layer is more uniform, the conversion rate at each part of the bed layer is more uniform, the conversion efficiency is improved, and the severe temperature difference of the bed layer caused by factors such as strong heat absorption in the reaction process is avoided; the high temperature molten salt inlet flow is determined by the load of the reactor.
The reactor shell is of a hollow metal structure and is made of stainless steel, and the outside of the reactor shell is coated with a heat-insulating material to prevent heat dissipation.
Compared with the prior art, the utility model has at least the following beneficial effects:
according to the utility model, a large number of heat exchange tubes are arranged in the reactor shell, the catalyst bed layers are arranged in the heat exchange tubes, the catalyst bed layer in each heat exchange tube is a micro reaction unit, and the high-temperature molten salt provides heat for dehydrogenation reaction through heat exchange of the heat exchange tubes, so that the temperature distribution of the reaction bed layer in each micro reaction unit is more uniform.
In the dehydrogenation and conversion process of the low-carbon alkane, the high-temperature molten salt continuously supplies heat to the catalyst reaction bed layer through the heat exchange tube, so that heat required by dehydrogenation endothermic reaction is provided, the temperature drop of the catalyst bed layer in the dehydrogenation reaction with strong heat absorption is reduced, the reaction bed layer is in an optimal reaction temperature range for a long time, the single-stage reaction time is prolonged, and the conversion efficiency is improved.
The characteristics of good heat exchange and heat conduction performance, uniform temperature distribution and the like of the heat exchange tubes are utilized, the bed temperature of the catalyst is indirectly controlled by controlling the flow of the high-temperature molten salt, the local over-high temperature of the catalyst bed is favorably prevented, and the rapid formation and accumulation of coke are prevented. And the high-temperature molten salt heating also reduces the heat load of a heater in front of the reactor, reduces the thermal cracking of the low-carbon alkane in the heater, and ensures that the process is more economic as a whole and the operation is simpler and controllable.
Because the heat exchange temperature of the tubular heat exchange tubes is uniform, the tubular heat exchange tubes are beneficial to preventing the local temperature of a catalyst bed layer from being too high, preventing coke from being rapidly formed and accumulated, prolonging the single-section reaction time and simultaneously improving the conversion efficiency, thereby avoiding frequent production halt and maintenance, being beneficial to the long-period stable operation of the device and being more beneficial to heat preservation.
Drawings
FIG. 1 is a schematic view of the structure of a tubular fixed bed reactor for dehydrogenation of light alkanes in example 1.
FIG. 2 is a schematic view of the structure of a tubular fixed bed reactor for dehydrogenation of light alkanes in example 2.
FIG. 3 is a calandria diagram of a low-carbon alkane dehydrogenation tubular fixed bed reactor.
In the figure, each number represents: the system comprises a 1-light alkane raw material inlet, a 2-high temperature hot air inlet, a 3-high temperature steam/process gas/reducing gas inlet, a 4-high temperature molten salt outlet, a 5-high temperature molten salt inlet, a 6-waste heat air outlet, a 7-evacuation/emergency outlet, an 8-hydrocarbon product outlet, a 9-catalyst reaction bed layer, a 10-shell, 11-thermocouple interfaces, 12-heat exchange tubes, 13-lower support plates, 14-upper sealing plates, 15-molten salt heating furnaces, 16-molten salt tanks and 17-molten salt pumps.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the utility model and are not intended to limit the utility model.
Example 1
As shown in fig. 1, the low-carbon alkane dehydrogenation tubular fixed bed reactor (hereinafter referred to as reactor) has a shell 10 of stainless steel hollow metal structure, and the shell forms a closed reaction tank structure. The upper end of the shell is provided with a material inlet, and the lower end of the shell is provided with a material outlet. The material inlet comprises a low-carbon alkane raw material inlet 1, a high-temperature hot air inlet 2 and a high-temperature steam/process gas/reducing gas inlet 3 which are mutually independent, namely, the low-carbon alkane raw material enters the reactor from the low-carbon alkane raw material inlet 1, the high-temperature hot air enters the reactor from the high-temperature hot air inlet 2, the high-temperature steam, the process gas and the reducing gas all enter the reactor from the high-temperature steam/process gas/reducing gas inlet 3, and the high-temperature steam, the process gas and the reducing gas share the same inlet. The high-temperature steam/process gas/reducing gas inlet is connected above the reactor and then connected to a material inlet pipeline connected with the reactor; the lower end of the material inlet pipeline is connected with a distributor for distributing materials. The material outlet comprises a hydrocarbon product outlet 8, a waste heat air outlet 6 and an evacuation/emergency outlet 7 which are independent of each other.
The reactor shell is of a hollow metal structure and is made of stainless steel, and the outside of the reactor shell is coated with a heat-insulating material to prevent heat dissipation.
The shell is internally provided with a tube array heat exchange tube, the upper end of the tube array heat exchange tube is provided with an upper sealing plate 14, the lower end of the tube array heat exchange tube is provided with a lower supporting plate 13, a gap is formed between the adjacent heat exchange tubes 12, and the shell 10, the upper sealing plate 14 and the lower supporting plate 13 enable the gap between the tube array heat exchange tubes to be a closed heat exchange cavity; a high-temperature molten salt inlet 5 and a high-temperature molten salt outlet 4 are arranged on the shell and are respectively communicated with the heat exchange cavity; a catalyst reaction bed layer 9 is arranged in the tube type heat exchange tube, namely, the catalyst is arranged in the tube cavity of the heat exchange tube. Inert ceramic balls are also filled in the heat exchange tubes and are positioned below the catalyst. The upper sealing plate 14 and the lower supporting plate 13 are both structural members with mesh structures, which allow the low-carbon alkane raw material to enter a catalyst reaction bed layer, allow the product after reaction to be discharged from a hydrocarbon product outlet at the bottom of the reactor, and when the product is discharged from the hydrocarbon product outlet, the waste heat air outlet and the evacuation/emergency outlet are both closed. All inlets and all outlets of the reactor are respectively provided with valves, and the valves are opened or closed according to requirements to control the circulation direction of the pipeline.
As shown in FIG. 3, the tube array heat exchange tube is formed by vertically and uniformly arranging a plurality of heat exchange tubes 12 in a reactor, inert ceramic balls and catalysts are filled in the tube cavity of each heat exchange tube, the inert ceramic balls and the catalysts are filled in all the heat exchange tubes in the same amount, and the catalysts are positioned at the same height to form a catalyst reaction bed layer.
The high-temperature molten salt inlet is located at the lower section of the tube type heat exchange tube, the high-temperature molten salt outlet is located at the upper section of the tube type heat exchange tube, the high-temperature molten salt inlet is located below the catalyst reaction bed layer, and the high-temperature molten salt outlet is located above the catalyst reaction bed layer. The shell is provided with at least two thermocouple interfaces 11, thermocouples are inserted into the shell, and the temperature of the upper end and the lower end of the shell-and-tube heat exchange tube is monitored.
In the dehydrogenation reaction stage, the low-carbon alkane raw materials such as propane and/or isobutane and the process gas enter the reactor from an inlet at the upper end of the reactor after being preheated, contact with the catalyst in the catalyst reaction bed layer to perform dehydrogenation reaction, and then hydrocarbon products are obtained and discharged from an outlet at the lower end of the reactor. During the dehydrogenation reaction, high-temperature molten salt enters the reactor from an inlet on the side surface of the reactor, circulates in the gaps between the heat exchange tubes and is discharged from an outlet on the side surface of the reactor. The high-temperature molten salt carries high heat, the temperature of the catalytic reaction bed layer is reduced in the reaction, and the high-temperature molten salt and the heat exchange tube continuously carry out heat exchange to improve the temperature of the catalytic reaction bed layer. The temperature of the catalytic bed can be monitored by thermocouples at the upper and lower ends of the catalytic bed.
In the regeneration stage, after feeding is stopped, high-temperature steam is introduced from the top of the reactor through an inlet for purging, and high-temperature hot air is introduced from the inlet at the top of the reactor after purging to regenerate the catalyst reaction bed layer, so that coke formed after the catalyst is coked is mainly burned off and a certain heating effect is exerted on the bed layer; the waste heat air is discharged from the outlet at the bottom of the reactor, and enters the next cycle reaction-regeneration period after the reactor is pumped out through the evacuation/emergency outlet.
Example 2
As shown in FIG. 2, the high-temperature molten salt inlet 5 is connected with the discharge port of the molten salt heating furnace 15, the high-temperature molten salt outlet 4 is connected with the feed port of the molten salt tank 16, and the discharge port of the molten salt tank is connected with the feed port of the molten salt heating furnace. The molten salt tank is connected with the molten salt heating furnace through a connecting pipe, and a molten salt pump 17 is arranged on the connecting pipe. After the high-temperature molten salt enters the reactor, the high-temperature molten salt circulates in the heat exchange cavity body, exchanges heat with the heat exchange tube, flows out from the corresponding outlet, enters the molten salt tank, is pumped into the molten salt heating furnace from the low-temperature molten salt in the molten salt tank by the molten salt pump, is heated to form high-temperature molten salt, and then enters the reactor.
The other structure is the same as embodiment 1.
The low-carbon alkane dehydrogenation tubular fixed bed reactor continuously provides heat required by dehydrogenation reaction through the heat exchange tube by using high-temperature molten salt, so that the temperature distribution of a catalyst reaction bed layer is more uniform, the conversion rate of each part of the bed layer is more uniform, the conversion efficiency is improved, and the severe temperature difference of the bed layer caused by factors such as strong heat absorption in the reaction process is avoided; the high temperature molten salt inlet flow is determined by the load of the reactor.
As the catalyst reaction bed layer is arranged in the tube type heat exchange tubes, each heat exchange tube is a micro reaction unit, and the flow and the inlet temperature of the high-temperature molten salt are determined according to the load of the reactor with a predetermined amount.
Cr-Ce-Cl/Al disclosed in ZL201911306207.0 (a method, a device and a reaction system for a low-carbon alkane dehydrogenation process) is arranged in a catalyst bed layer2O3Dehydrogenation catalyst (containing 18 m% -30 m% of Cr)2O30.1-3 m% of CeO20.1-1 m% of Cl, 67-80 m% of Al2O3) And Cu-Ca-Cl/Al2O3Thermal coupling auxiliary agent (containing 5 m% -30 m% CuO, 0.1 m% -3 m% CeO)210 m-35 m% of CaO, 0.1 m-1 m% of Cl and 50 m-80 m% of Al2O3)。
In the process of propane dehydrogenation reaction, the high-temperature molten salt controls the temperature of a catalyst bed layer to be no more than 660 ℃ under the preferable condition, and can control the temperature to be no more than 760 ℃ under wider reaction conditions; in the process of isobutane dehydrogenation reaction, the temperature of a catalyst bed layer is controlled to be not more than 640 ℃ under the preferable condition by high-temperature molten salt, and is controlled to be not more than 720 ℃ under wider reaction conditions;
compared with the conventional fixed bed reactor in the prior art, in the reaction process, the high-temperature molten salt is used for continuously providing the heat required by the dehydrogenation endothermic reaction for the catalyst reaction bed layer through the tube type heat exchange tubes, so that the temperature drop of the catalyst bed layer in the dehydrogenation reaction with strong heat absorption is reduced, and the reaction bed layer is in the optimal reaction temperature range for a long time. Because the heat exchange temperature of the tube type heat exchange tubes is uniform, the local overhigh temperature of a catalyst bed layer is favorably prevented, the rapid formation and accumulation of coke are prevented, the single-stage reaction time is prolonged, and the conversion efficiency is improved. The coke formation in the reactor is reduced by 20% by combining the dehydrogenation catalyst; the circulation time in the single-stage period is prolonged by 30-50%, and the reaction time is increased from 40% to more than 60%; because the interior of the fixed bed reactor is not provided with refractory materials, the parking maintenance site in the construction period caused by cracking, falling and damage of the refractory brick lining in the traditional fixed bed reactor is avoided, and the long-period stable operation of the device is ensured; meanwhile, the temperature of the catalyst reaction bed layer can be controlled by controlling the flow of the high-temperature molten salt according to the actual load of the reactor, the temperature can be more uniform and quicker than that of the traditional fixed bed, the corresponding heat loss is greatly reduced, and the energy consumption is reduced.
Although the utility model has been described herein with reference to illustrative embodiments thereof, it should be understood that numerous other modifications and embodiments can be devised by those skilled in the art that will fall within the spirit and scope of the principles of this disclosure. More specifically, various variations and modifications may be made to the component parts and/or arrangements of the subject combination arrangement within the scope of the disclosure herein. In addition to variations and modifications in the component parts and/or arrangements, other uses will also be apparent to those skilled in the art.
Claims (7)
1. A low-carbon alkane dehydrogenation tubular fixed bed reactor comprises a shell, wherein the upper end of the shell is provided with a material inlet, and the lower end of the shell is provided with a material outlet; the heat-insulation type solar water heater is characterized in that the shell is of a hollow metal structure made of stainless steel materials and is provided with an outer heat-insulation layer; the shell, the upper sealing plate and the lower supporting plate enable the gaps among the tube type heat exchange tubes to be closed heat exchange cavities; the shell is provided with a high-temperature molten salt inlet and a high-temperature molten salt outlet which are respectively communicated with the heat exchange cavity; a catalyst reaction bed layer is arranged in the tube array type heat exchange tube; the high-temperature molten salt inlet is connected with a discharge hole of the molten salt heating furnace, the high-temperature molten salt outlet is connected with a feed inlet of the molten salt groove, and the discharge hole of the molten salt groove is connected with the feed inlet of the molten salt heating furnace.
2. The light alkane dehydrogenation tubular fixed bed reactor of claim 1, wherein the high-temperature molten salt inlet is located at the lower section of the tubular heat exchange tube, the high-temperature molten salt outlet is located at the upper section of the tubular heat exchange tube, the high-temperature molten salt inlet is located below the catalyst reaction bed layer, and the high-temperature molten salt outlet is located above the catalyst reaction bed layer.
3. The light alkane dehydrogenation shell and tube type fixed bed reactor of claim 1, wherein the molten salt tank and the molten salt heating furnace are connected through a connecting pipe, and a molten salt pump is arranged on the connecting pipe.
4. The fixed-bed reactor of claim 1, wherein inert ceramic balls are filled in the heat exchange tubes and are positioned below the catalyst bed.
5. The fixed-bed reactor of claim 1, wherein the material inlet comprises a low-carbon alkane raw material inlet, a high-temperature hot air inlet, and a high-temperature steam/process gas/reducing gas inlet which are independent of each other; the high-temperature steam/process gas/reducing gas inlet is connected above the reactor and then connected to a material inlet pipeline connected with the reactor; the lower end of the material inlet pipeline is connected with a distributor for distributing materials.
6. The lower alkane dehydrogenation shell and tube fixed bed reactor of claim 1, wherein the feed outlet comprises a hydrocarbon product outlet, a waste heat air outlet and an evacuation/emergency outlet that are independent of each other.
7. The low-carbon alkane dehydrogenation shell and tube type fixed bed reactor as claimed in claim 1, wherein the shell is provided with at least two thermocouple ports, thermocouples are inserted into the shell, and the temperature of the upper end and the lower end of the shell and tube type heat exchange tube is monitored.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115228388A (en) * | 2022-07-20 | 2022-10-25 | 武汉工程大学 | Heat pipe-tube type fixed bed propane dehydrogenation reactor with hydrogen separation mechanism |
| CN115430367A (en) * | 2022-09-28 | 2022-12-06 | 中化学科学技术研究有限公司 | Dehydrogenation system and method |
-
2021
- 2021-08-12 CN CN202121883469.6U patent/CN215464287U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115228388A (en) * | 2022-07-20 | 2022-10-25 | 武汉工程大学 | Heat pipe-tube type fixed bed propane dehydrogenation reactor with hydrogen separation mechanism |
| CN115430367A (en) * | 2022-09-28 | 2022-12-06 | 中化学科学技术研究有限公司 | Dehydrogenation system and method |
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