CN213556925U - System for shortening charging time of MTP (methanol to propylene) reactor in process of preparing propylene from coal-based methanol - Google Patents
System for shortening charging time of MTP (methanol to propylene) reactor in process of preparing propylene from coal-based methanol Download PDFInfo
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- CN213556925U CN213556925U CN202021623012.7U CN202021623012U CN213556925U CN 213556925 U CN213556925 U CN 213556925U CN 202021623012 U CN202021623012 U CN 202021623012U CN 213556925 U CN213556925 U CN 213556925U
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Abstract
The utility model discloses a system for shortening the charging time of an MTP reactor in the process of preparing propylene from coal-based methanol, which comprises a circulating hydrocarbon storage tank, a dehexadecane tower, a cooler, a reflux tank, a heater, a superheater and an MTP reactor; a feeding hole I is formed in the de-hexanizer, the feeding hole I is connected with a pipeline for conveying materials of C5/C6 circulating hydrocarbon, a discharging hole is formed in the tower top of the de-hexanizer and communicated with an inlet of a cooler, an outlet of the cooler is connected to an inlet of a reflux tank, an outlet of the reflux tank is connected to an inlet of a pump, and an outlet of the pump is respectively connected to a feeding hole III of the de-hexanizer, an inlet of a circulating hydrocarbon storage tank and an inlet of a heater; the outlet of the circulating hydrocarbon storage tank is connected to a feed inlet II of the dehexanizer; the outlet of the heater is connected to the inlet of the superheater, and the outlet of the superheater is connected with the inlet of the MTP reactor. The system provided by the utility model shortens the material feeding time of the MTP reactor in the process of preparing propylene from coal-based methanol and prolongs the service life of the catalyst in the MTP reactor.
Description
Technical Field
The utility model relates to a technical field of coal-based methyl alcohol system propylene especially relates to a system for shorten MTP reactor in coal-based methyl alcohol system propylene technology and throw the material time.
Background
With the continuous rising of the price of crude oil and the rapid development of domestic economy, the demand of low-carbon olefins, particularly propylene and ethylene, is rising day by day, and the traditional petrochemical industry can not meet the market demand.
Shenhua group Ning coal company adopts a device for preparing propylene (MTP) from methanol and adopts German Lurgi technology, which prepares dimethyl ether (DME) from refined methanol, and the DME generates a gaseous hydrocarbon mixture mainly containing propylene under the action of an MTP catalyst. The mixture is quenched and then sent to a compression and rectification unit, and polymerization-grade propylene is separated out and supplied to a downstream device; meanwhile, a certain amount of LPG, mixed aromatic hydrocarbon and ethylene are produced as byproducts. Of these by-products, C5/C6 was returned to the MTP reactor primarily as recycle hydrocarbons to control the bed temperature.
The C5/C6 circulating hydrocarbon is a material fed into the MTP reactor, can improve the space velocity of the MTP reactor and control the bed temperature of the reactor; meanwhile, the C5/C6 circulating hydrocarbon is advantageous in producing a propylene precursor or suppressing the progress of side reactions in the reaction. However, when the MTP reactor is initially charged, the airspeed of the reactor is low, the temperature fluctuation of a bed layer is large, the overtemperature phenomenon is easy to occur, the catalyst is damaged, the charging time is long, the time for discharging the material from a torch is long, and the loss is large. The charging time of the MTP reactor is about 25 hours, the load of the device during charging is about 120t/h methanol, and the energy consumption is large.
Therefore, a system capable of saving energy and shortening the charging time of the MTP reactor in the process of preparing propylene from coal-based methanol is needed.
SUMMERY OF THE UTILITY MODEL
To the technical problem who exists among the prior art, the utility model provides a shorten the MTP reactor in the coal-based methyl alcohol system propylene technology and throw the material time, each bed temperature's in even, the stable MTP reactor system utilizes this system to be favorable to prolonging the life of catalyst in the MTP reactor.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a system for shortening the charging time of an MTP reactor in a process of preparing propylene from coal-based methanol comprises a circulating hydrocarbon storage tank, a dehexanizer, a cooler, a reflux tank, a heater, a superheater and an MTP reactor;
the de-hexanizer is provided with a feed inlet I, the feed inlet I is connected with a pipeline for conveying materials of C5/C6 circulating hydrocarbon, the top of the de-hexanizer is provided with a discharge outlet for discharging the materials of C5/C6 circulating hydrocarbon processed by the de-hexanizer out of the de-hexanizer, the discharge outlet is communicated with an inlet of the cooler, an outlet of the cooler is connected to an inlet of the reflux tank, an outlet of the reflux tank is connected to an inlet of a pump, and an outlet of the pump is respectively connected to a feed inlet III of the de-hexanizer, an inlet of the circulating hydrocarbon storage tank and an inlet of the heater through pipelines;
the outlet of the circulating hydrocarbon storage tank is connected to a feed inlet II of the dehexanizer;
the outlet of the heater is connected to the inlet of the superheater, and the outlet of the superheater is connected with the inlet of the MTP reactor.
In the system provided by the utility model, the system further comprises a reboiler, the reboiler is connected with the dehexanizer and is used for heating the material at the bottom of the dehexanizer;
and the outlet of the tower bottom of the dehexanizer is communicated with the inlet of the reboiler, and the outlet of the reboiler is connected to a feed inlet II of the dehexanizer.
In the system provided by the utility model, be provided with switching device on the pump.
The utility model provides an in the system, feed inlet I with feed inlet III sets up the upper portion of dehexanizer, feed inlet II sets up the lower part of dehexanizer.
In the system provided by the utility model, the export of circulation hydrocarbon storage tank with through pipeline IV intercommunication between the feed inlet II of dehexanizer.
The utility model provides an in the system, be equipped with the circulation hydrocarbon delivery pump on the pipeline IV, be used for with the material of circulation hydrocarbon storage tank export is carried extremely the feed inlet II of de-Hexane tower.
The utility model provides an in the system, the export of pump with through I intercommunication of pipeline between the feed inlet III of dehexanizer.
In the system provided by the utility model, through II intercommunications of pipeline between the export of pump and the import of heater.
In the system provided by the utility model, the export of pump with through pipeline III intercommunication between the import of circulation hydrocarbon storage tank.
By adopting the technical scheme, the method has the following technical effects:
the utility model provides a system is through being connected the backward flow jar with circulation hydrocarbon storage tank for the system can be in advance with C5C 6 circulation hydrocarbon in the dehexadecane tower through the pump sending to storage in the circulation hydrocarbon storage tank when stopping, can send this part material back to the dehexadecane tower in when waiting that the system is driven, can reduce methyl alcohol partial pressure in the reactor after the MTP reactor possesses the feeding condition, increase the airspeed, and then establish C5C 6 circulation fast, prevent that the MTP reactor bed from overtemperature, accelerate the progress of opening a work.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention;
the system comprises a circulating hydrocarbon storage tank 1, a dehexanizer 2, a dehexanizer 3, a cooler 4, a reflux tank 5, a heater 6, a superheater 7, a pump 8, a reboiler 9, a circulating hydrocarbon delivery pump 10, pipelines I and 11, pipelines II and 12, pipelines III and 13 and a pipeline IV.
Detailed Description
For a better understanding of the present invention, reference will now be made to the following description taken in conjunction with the accompanying drawings.
As is well known to those skilled in the art, the reaction process of Methanol To Propylene (MTP) is to prepare dimethyl ether from refined methanol, and the dimethyl ether is reacted with an MTP catalyst to form a gaseous hydrocarbon mixture mainly containing propylene; the mixture is quenched, then compressed and rectified to separate polymerization-grade propylene. In the above-mentioned treatment process a certain quantity of liquefied petroleum gas, mixed aromatic hydrocarbon and ethylene can be by-produced. Of these by-products, C5/C6 will be returned to the MTP reactor primarily as recycle hydrocarbons to control the bed temperature.
The utility model provides a system for shortening the charging time of an MTP reactor in a process of preparing propylene from coal-based methanol, which comprises a circulating hydrocarbon storage tank 1, a dehexadecane tower 2, a cooler 3, a reflux tank 4, a heater 5, a superheater 6 and an MTP reactor;
as shown in fig. 1, the dehexanizer 2 is provided with a feed inlet i, which can be arranged at the upper part of the dehexanizer 2, and the feed inlet i is connected with a transfer pipeline of the C5/C6 recycle hydrocarbon (mainly composed of C5, C6, C7 and C8 components) obtained after the treatment by the MTP reactor. The treated material in the dehexanizer 2 is discharged outside the tower through a discharge hole arranged at the top of the tower, and the treated material of C5/C6 recycle hydrocarbon is discharged outside the tower.
A discharge hole on the top of the dehexanizer 2 is communicated with an inlet of a cooler 3, an outlet of the cooler 3 is connected to an inlet of a reflux tank 4, an outlet of the reflux tank 4 is connected to an inlet of a pump 7, outlets of the pump 7 are respectively connected to the dehexanizer 2, a heater 5 and a circulating hydrocarbon storage tank 1 in the following manner, and an outlet of the pump 7 is communicated with a feed hole III of the dehexanizer 2 through a pipeline I10 so as to return part of C5/C6 circulating hydrocarbon in the reflux tank 4 to the dehexanizer 2 for continuous reaction; wherein, the feed inlet III and the feed inlet I of the dehexanizer 2 can be both arranged at the upper part of the dehexanizer 2; the outlet of the pump 7 is connected with the inlet of the heater 5 through a pipeline II 11, and is used for conveying part of C5/C6 circulating hydrocarbon in the reflux tank 4 to the heater 5, treating the hydrocarbon in the superheater 6 and then sending the hydrocarbon into the MTP reactor; the outlet of pump 7 is connected via line III 12 to the inlet of the recycle hydrocarbon storage tank 1 to deliver a portion of the C5/C6 recycle hydrocarbon directly to the recycle hydrocarbon storage tank 1 for storage. The pump 7 is provided with a switching device for controlling the connection or disconnection of the reflux drum 4 to the dehexanizer 2, the heater 5 and the hydrocarbon circulation tank 1, and the switching device may be any structure conventional in the art, such as a manual cut-off valve or an electrically-controlled cut-off valve.
The utility model discloses an in the structure, the export of circulation hydrocarbon storage tank 1 is passed through pipeline IV 13 and is linked together with feed inlet II of dehexanizer 2 for carry the C5C 6 circulation hydrocarbon in the circulation hydrocarbon storage tank 1 to in the dehexanizer 2. A circulating hydrocarbon conveying pump 9 is arranged on the pipeline IV 13 and used for providing power for the material at the outlet of the circulating hydrocarbon storage tank 1 and conveying the material to the feed inlet II of the dehexanizer 2.
The structure of the utility model also comprises a reboiler 8, the outside of the dehexanizer 2 is connected with the reboiler 8, the outlet at the bottom of the dehexanizer 2 is connected with the inlet of the reboiler 8, and the outlet of the reboiler 8 is connected with the feed inlet II of the dehexanizer 2; specifically, the liquid phase at the bottom of the dehexanizer 2 enters the reboiler 8, where the liquid phase is re-vaporized, the vaporized two-phase streams are fed back to the dehexanizer 2, respectively, the gas phase component returning to the dehexanizer 2 passes upward through the trays, and the liquid phase component falls back to the bottom of the tower. The specific structures of the reboiler 8 and the dehexanizer 2 are conventional in the art, and are not described in detail.
In the normal operation process of the utility model, the material containing C5/C6 circulating hydrocarbon is conveyed into the dehexanizer 2 through the feed inlet I, the material is separated and rectified in the dehexanizer 2, the obtained liquid phase component enters the reboiler 8 through the outlet at the bottom of the tower, and the component gasified in the reboiler 8 returns to the dehexanizer 2; the gas phase components obtained by treatment in the dehexanizer 2 are sent into the cooler 3 through a discharge hole arranged at the top of the tower, the gas phase components are cooled in the cooler 3 to become a liquid phase, and then the liquid phase enters the reflux tank 4 from an inlet of the reflux tank 4.
In the normal operation process of the system, a switch on the pump 7 is in a state of communicating the reflux tank 4 with the dehexanizer 2 and the heater 5, namely, a part of liquid phase flowing out of an outlet of the reflux tank 4 is sent back to the dehexanizer 2 through a pipeline I10 under the action of the pump 7 for continuous reaction, and the rest part of liquid phase is conveyed to the heater 5 through a pipeline II 11 for heating. In the heater 5, the liquid phase material is heated to 160 ℃ for 150-.
The utility model discloses when the operation in-process need be parked, the switch on the pump 7 is in intercommunication backflow tank 4 and the state of dehexanizer tower 2 and circulation hydrocarbon storage tank 1, and the liquid phase that flows out from 4 exports of backflow tank passes through pipeline III 12 to be carried to circulation hydrocarbon storage tank 1 and stores under the effect of pump 7 partly liquid phase promptly, and remaining part liquid phase is sent back to in the dehexanizer tower 2 through pipeline I10. Since the MTP reaction is exothermic, the MTP reactor requires a large amount of recycle hydrocarbon, process steam to reduce the partial pressure of methanol in the reactor and increase the space velocity to start the reaction. When the system of the utility model is operated again, the materials (namely C5/C6 circulating hydrocarbon) stored in the circulating hydrocarbon storage tank 1 are conveyed into the de-hexane tower 2 through the pipeline IV 13 by utilizing the power provided by the circulating hydrocarbon conveying pump 9, and then enter the MTP reactor after being processed by the de-hexane tower 2 and passing through the cooler 3 and the reflux tank 4, so that the circulating hydrocarbon can be supplied to the MTP reactor in time at the initial stage of operation, and the reaction balance is quickly established by stabilizing and homogenizing the temperature of each bed layer in the reactor; meanwhile, the charging time of the MTP reactor is shortened, the service life of the catalyst in the MTP reactor is prolonged, and the torch discharge amount of the materials at the outlet of the reactor is greatly reduced (the loss can be reduced by about 210 ten thousand yuan due to one-time charging of the reactor).
The embodiments of the present invention are described above, but the descriptions are only for the convenience of understanding the present invention, and are not intended to limit the present invention. It will be apparent to persons skilled in the relevant art that various changes in form and detail can be made therein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (9)
1. A system for shortening the charging time of an MTP reactor in a process of preparing propylene from coal-based methanol is characterized by comprising a circulating hydrocarbon storage tank (1), a dehexanizer (2), a cooler (3), a reflux tank (4), a heater (5), a superheater (6) and the MTP reactor;
the de-hexanizer (2) is provided with a feeding hole I, the feeding hole I is connected with a pipeline for conveying C5/C6 circulating hydrocarbon materials, the top of the de-hexanizer (2) is provided with a discharging hole for discharging the C5/C6 circulating hydrocarbon materials treated by the de-hexanizer (2) out of the de-hexanizer, the discharging hole is communicated with the inlet of the cooler (3), the outlet of the cooler (3) is connected to the inlet of the reflux tank (4), the outlet of the reflux tank (4) is connected to the inlet of a pump (7), and the outlet of the pump (7) is respectively connected to the feeding hole III of the de-hexanizer (2), the inlet of the circulating hydrocarbon storage tank (1) and the inlet of the heater (5) through pipelines;
the outlet of the circulating hydrocarbon storage tank (1) is connected to the feed inlet II of the dehexanizer (2); the outlet of the heater (5) is connected to the inlet of the superheater (6), and the outlet of the superheater (6) is connected with the inlet of the MTP reactor.
2. The system for shortening the MTP reactor feeding time in the coal-based methanol to propylene process according to claim 1, further comprising a reboiler (8), wherein the reboiler (8) is connected with the dehexanizer (2) and is used for heating the bottom material of the dehexanizer (2);
wherein the outlet at the bottom of the dehexanizer (2) is communicated with the inlet of the reboiler (8), and the outlet of the reboiler (8) is connected to the feed inlet II of the dehexanizer (2).
3. The system for shortening the charging time of the MTP reactor in the process of preparing propylene from coal-based methanol as claimed in claim 2, wherein a switch device is arranged on the pump (7).
4. The system for shortening the charging time of an MTP (methanol to propylene) reactor in a coal-based methanol to propylene process according to claim 3, wherein the feed inlet I and the feed inlet III are arranged at the upper part of the dehexanizer (2), and the feed inlet II is arranged at the lower part of the dehexanizer (2).
5. The system for shortening the charging time of an MTP (methanol to propylene) reactor in a coal-based methanol to propylene process as claimed in any one of claims 1 to 4, wherein the outlet of the circulating hydrocarbon storage tank (1) is communicated with the feed inlet II of the dehexanizer (2) through a line IV (13).
6. The system for shortening the feeding time of the MTP reactor in the process of preparing propylene from coal-based methanol as claimed in claim 5, wherein a circulating hydrocarbon transfer pump (9) is disposed on the pipeline IV (13) and used for transferring the material at the outlet of the circulating hydrocarbon storage tank (1) to the feeding port II of the dehexanizer (2).
7. The system for shortening the feed time of an MTP (methanol to propylene) reactor in the process of preparing propylene from coal-based methanol according to claim 6, wherein the outlet of the pump (7) is communicated with the feed inlet III of the dehexanizer (2) through a pipeline I (10).
8. The system for shortening the feed time of an MTP (methanol to propylene) reactor in a coal-based methanol to propylene process as claimed in claim 7, wherein the outlet of the pump (7) is communicated with the inlet of the heater (5) through a pipeline II (11).
9. The system for shortening the feed time of an MTP (methanol to propylene) reactor in a coal-based methanol to propylene process according to claim 8, wherein the outlet of the pump (7) is communicated with the inlet of the circulating hydrocarbon storage tank (1) through a pipeline III (12).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021623012.7U CN213556925U (en) | 2020-08-06 | 2020-08-06 | System for shortening charging time of MTP (methanol to propylene) reactor in process of preparing propylene from coal-based methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202021623012.7U CN213556925U (en) | 2020-08-06 | 2020-08-06 | System for shortening charging time of MTP (methanol to propylene) reactor in process of preparing propylene from coal-based methanol |
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| Publication Number | Publication Date |
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| CN213556925U true CN213556925U (en) | 2021-06-29 |
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| Application Number | Title | Priority Date | Filing Date |
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| CN202021623012.7U Active CN213556925U (en) | 2020-08-06 | 2020-08-06 | System for shortening charging time of MTP (methanol to propylene) reactor in process of preparing propylene from coal-based methanol |
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| CN (1) | CN213556925U (en) |
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