Methyl tert-butyl ether production device with switchable reactors

Abstract

The utility model provides a methyl tert-butyl ether production device with switchable reactors, which is characterized in that a plurality of reactors are arranged, and a communicating pipeline and a switching valve are arranged between a feeding system and each reactor, so that raw materials C4 and methanol can selectively enter one of the reactors through valve switching operation; and the priority of the three reactors can be adjusted at will according to the activity condition of the catalyst in the production process, and any reactor can be independently switched and used without influencing the normal operation of the device.

Description

Technical Field

[0001] The utility model relates to the technical field of methyl tert-butyl ether production devices, in particular to a methyl tert-butyl ether production device with switchable reactors. Background Art

[0002] Methyl tert-butyl ether (MTBE) has stable chemical properties and relatively high oxygen content. MTBE is produced by the etherification reaction of isobutylene and methanol under the action of macroporous strongly acidic cation exchange resin. The reaction is exothermic and preferably carried out at low temperature. The activity of the resin catalyst used in the etherification reaction gradually decreases until it is completely deactivated after being used for a period of time, and it needs to be replaced regularly to ensure product quality and output, as well as long-term operation of the device. In the existing process, the reflux of the catalytic distillation tower is controlled by a single loop of a flow meter and a regulating valve. The reflux volume is constant during normal operation. When the raw material flow rate and the isobutylene content fluctuate, the residual carbon four flow rate at the top of the tower changes accordingly. The existing control method cannot adjust the reflux of the catalytic distillation tower in time, resulting in unqualified MTBE and carbon four products after etherification, or energy waste. In the existing process, the methanol recovery tower kettle liquid level and the tower bottom extraction water production flow rate are controlled in cascade. When the tower kettle maintains a certain liquid level, the extraction water flow rate is constant. When the raw material flow rate and the isobutylene content fluctuate, the etherified C4 flow rate entering the extraction tower changes accordingly. The existing control method cannot adjust the extraction water flow rate in time, resulting in excessive methanol content in the etherified C4 product, affecting the production of downstream equipment or causing energy waste. Summary of the invention

[0003] In view of this, the utility model provides a methyl tert-butyl ether production device with a switchable reactor, which solves the technical problem that the reflux of the catalytic distillation tower in the prior art is controlled by a single loop of a flow meter and a regulating valve, and the reflux of the catalytic distillation tower cannot be adjusted in time, resulting in unqualified MTBE and post-ether C4 products.

[0004] The utility model provides a methyl tert-butyl ether production device with switchable reactors. The production device comprises: a feeding system; a first reactor, wherein the sampling port of the first reactor is connected with the sampling port of the feeding system through a first pipeline, the sampling port of the first reactor is refluxed to the sampling port of the first reactor through a second pipeline, and a first external circulation cooler and a first external circulation pump are arranged on the second pipeline; a second reactor, wherein the sampling port of the first reactor is connected with the sampling port of the second reactor through a third pipeline, the sampling port of the second reactor is refluxed to the sampling port of the second reactor through a fourth pipeline, a second external circulation cooler and a second external circulation pump are arranged on the fourth pipeline, and the sampling port of the feeding system is connected with the sampling port of the second reactor through a seventh pipeline; a third reactor, wherein the sampling port of the second reactor is connected with the sampling port of the third reactor through a fifth pipeline, and the sampling port of the feeding system is connected with the sampling port of the third reactor through a fifteenth pipeline, wherein the first pipeline, the second pipeline, the third pipeline, the fourth pipeline, the fifth pipeline, the seventh pipeline, and the fifteenth pipeline are all provided with switching valves.

[0005] In a possible implementation, it also includes: a catalytic distillation tower, the production outlet of the third reactor is connected to the first production outlet of the catalytic distillation tower through the sixth pipeline, the production outlet of the feed system is connected to the second production outlet of the catalytic distillation tower through the thirty-second pipeline, the top production outlet of the catalytic distillation tower is refluxed to the catalytic distillation tower through the twenty-ninth pipeline, and the bottom production outlet of the catalytic distillation tower is produced through the twenty-third pipeline; an extraction tower, the production inlet of the extraction tower is connected to the production outlet of the catalytic distillation tower through the twenty-fourth pipeline, and the production outlet of the extraction tower is connected to the twenty-fifth pipeline; a methanol recovery tower, the bottom production outlet of the extraction tower is connected to the production inlet of the methanol recovery tower through the twenty-sixth pipeline, the bottom production outlet of the methanol recovery tower is refluxed to the extraction tower through the twenty-seventh pipeline, and the production outlet at the top of the methanol recovery tower is refluxed to the feeding system through the twenty-eighth pipeline.

[0006] In a possible implementation, it also includes: a first mixer; a first temperature controller, wherein the first mixer and the first temperature controller are both arranged on a first pipeline; a second mixer; a second temperature controller, wherein the second mixer and the second temperature controller are both arranged on a third pipeline; a third mixer; a third temperature controller, wherein the third mixer and the third temperature controller are both arranged on a fifth pipeline.

[0007] In a possible implementation, the intake port of the feeding system is connected to the 30th pipeline and the 31st pipeline respectively.

[0008] In a possible implementation, it also includes: a first flow controller, which is arranged on the 30th pipeline and is used to control the feed flow rate of raw material carbon four; a second flow controller, which is arranged on the 24th pipeline and is used to control the flow rate of the distillation product entering the extraction tower; a first flow regulating valve, which is installed on the 29th pipeline and is used to adjust the reflux rate of the distillation product in the catalytic distillation tower to the catalytic distillation tower; a second flow regulating valve, which is installed on the 27th pipeline and is used to adjust the reflux rate of the recovered product in the methanol recovery tower to the extraction tower; wherein, the first flow controller is electrically connected to the first flow regulating valve through the seventh signal line, and the first flow regulating valve is controlled according to the first flow controller, and the second flow controller is electrically connected to the second flow regulating valve through the eighth signal line, and the second flow regulating valve is controlled according to the second flow controller.

[0009] In a possible implementation, it also includes: a first temperature display; a first external circulation cooler; a first external circulation pump; the first temperature display, the first external circulation cooler and the first external circulation pump are sequentially arranged on the second pipeline, the first external circulation cooler is externally connected to the first outlet pipeline of cooling water; the outlet of the first external circulation cooler is connected to the sampling inlet of the first reactor through the seventeenth pipeline, and the outlet of the first external circulation cooler is connected to the inlet of the third reactor through the ninth pipeline; the outlet of the first external circulation pump is connected to the inlet of the second reactor through the tenth pipeline, and the outlet of the first external circulation pump is connected to the inlet of the second reactor through the eighteenth pipeline. The inlet of the third reactor is connected; a second temperature display; a second external circulation cooler; a second external circulation pump; the second temperature display, the second external circulation cooler and the second external circulation pump are sequentially arranged on the fourth pipeline, and the second external circulation cooler is externally connected to the second outlet pipeline of cooling water; the outlet of the second external circulation cooler is connected to the inlet of the first reactor through the twelfth pipeline, the outlet of the second external circulation pump is connected to the inlet of the third reactor through the thirteenth pipeline, and the outlet of the first reactor is connected to the inlet of the catalytic distillation tower through the fourteenth pipeline; a third temperature display, and the third temperature display is arranged on the sixth pipeline.

[0010] In a possible implementation, the system further includes: a first temperature regulating valve installed on the first cooling water outlet pipeline; and a second temperature regulating valve installed on the second cooling water outlet pipeline.

[0011] In a possible implementation, the first temperature controller is electrically connected to the first temperature regulating valve through a first signal line, and the first temperature controller is electrically connected to the second temperature regulating valve through a second signal line; the second temperature controller is point-connected to the first temperature regulating valve through a third signal line, and the second temperature controller is electrically connected to the second temperature regulating valve through a fourth signal line; the third temperature controller is point-connected to the first temperature regulating valve through a fifth signal line, and the third temperature controller is connected to the second temperature regulating valve through a sixth signal line.

[0012] In a possible implementation manner, an analyzer is further included, and the analyzer is electrically connected to the first flow regulating valve via a seventh signal line.

[0013] In a possible implementation, the production outlet of the first reactor is connected to the inlet of the second external circulation cooler through the nineteenth pipeline, the outlet of the second external circulation cooler is connected to the production inlet of the second reactor through the twentieth pipeline, the outlet of the second external circulation pump is connected to the production inlet of the first reactor through the twenty-first pipeline, and the production outlet of the second reactor is connected to the production inlet of the catalytic distillation tower through the twenty-second pipeline; the production outlet of the second reactor is connected to the inlet of the first external circulation cooler through the eighth pipeline; the production outlet of the third reactor is connected to the inlet of the second external circulation cooler through the eleventh pipeline, and the production outlet of the third reactor is connected to the inlet of the first external circulation cooler through the sixteenth pipeline.

[0014] The utility model provides a methyl tert-butyl ether production device with switchable reactors. The production device comprises: a feeding system; a first reactor, wherein the sampling port of the first reactor is connected with the sampling port of the feeding system through a first pipeline, the sampling port of the first reactor is refluxed to the sampling port of the first reactor through a second pipeline, and a first external circulation cooler and a first external circulation pump are arranged on the second pipeline; a second reactor, wherein the sampling port of the first reactor is connected with the sampling port of the second reactor through a third pipeline, the sampling port of the second reactor is refluxed to the sampling port of the second reactor through a fourth pipeline, and a second external circulation cooler and a second external circulation pump are arranged on the third pipeline; the sampling port of the feeding system is connected with the sampling port of the second reactor through a seventh pipeline, and a third reactor, wherein the sampling port of the second reactor is connected with the sampling port of the third reactor through a fifth pipeline; the sampling port of the feeding system is connected with the sampling port of the third reactor through a fifteenth pipeline, and switching valves are arranged on the first pipeline, the second pipeline, the third pipeline, the fourth pipeline, the fifth pipeline, the seventh pipeline, and the fifteenth pipeline. The production device is equipped with multiple reactors, and connecting pipes and switching valves are provided between the feeding system and each reactor. The raw materials C4 and methanol can be selected to enter one of the reactors through valve switching operation. The priority order of the three reactors can be adjusted arbitrarily according to the activity of the catalyst in the production process, and any reactor can be cut out separately without affecting the normal operation of the device. When the catalyst of one of the reactors needs to be replaced, the device does not need to stop production or reduce load production. The maintenance period of the device can be maintained at more than 4 years. It is suitable for various raw materials such as catalytic C4, isomerized C4, dehydrogenated C4, cracked C4, coal-based C4, etc. with isobutylene content of 0.5-70wt%, and has a wide range of applications. BRIEF DESCRIPTION OF THE DRAWINGS

[0015] Figure 1 The figure shows a schematic flow diagram of a methyl tert-butyl ether production device with switchable reactors provided in one embodiment of the utility model.

[0016] Description of reference numerals:

[0017] 100. Feeding system;

[0018] 201, first reactor; 202, second reactor; 203, third reactor

[0019] 300. Catalytic distillation tower;

[0020] 400, extraction tower;

[0021] 500, methanol recovery tower;

[0022] 600, Analyzer;

[0023] 701, a first flow controller; 702, a second flow controller; 703, a first flow regulating valve; 704, a second flow regulating valve;

[0024] 801, a first temperature controller; 802, a second temperature controller; 803, a third temperature controller;

[0025] 901, first external circulation cooler; 902, second external circulation cooler; 903, first external circulation pump; 904, second external circulation pump; 905, first temperature display; 906, second temperature display; 907, third temperature display; 908, first temperature regulating valve; 909, second temperature regulating valve;

[0026] 1001, a first mixer; 1002, a second mixer; 1003, a third mixer;

[0027] 01, the first pipeline; 02, the second pipeline; 03, the third pipeline; 04, the fourth pipeline; 05, the fifth pipeline; 06, the sixth pipeline; 07, the seventh pipeline; 08, the eighth pipeline; 09, the ninth pipeline; 10, the tenth pipeline; 11, the eleventh pipeline; 12, the twelfth pipeline; 13, the thirteenth pipeline; 14, the fourteenth pipeline; 15, the fifteenth pipeline; 16, the sixteenth pipeline; 17, the seventeenth pipeline; 1 8, the 18th pipeline; 19, the 19th pipeline; 20, the 20th pipeline; 21, the 21st pipeline; 22, the 22nd pipeline; 23, the 23rd pipeline; 24, the 24th pipeline; 25, the 25th pipeline; 26, the 26th pipeline; 27, the 27th pipeline; 28, the 28th pipeline; 29, the 29th pipeline; 30, the 30th pipeline; 31, the 31st pipeline; 32, the 32nd pipeline;

[0028] S1, first signal line; S2, second signal line; S3, third signal line; S4, fourth signal line; S5, fifth signal line; S6, sixth signal line; S7, seventh signal line; S8, eighth signal line; S9, ninth signal line; S10, tenth signal line. DETAILED DESCRIPTION

[0029] In the description of the utility model, the meaning of "multiple" is at least two, for example, two, three, etc., unless otherwise clearly and specifically limited. In the utility model embodiment, all directional indications (such as up, down, left, right, front, back, top, bottom ...) are only used to explain the relative position relationship, movement, etc. between the components under a certain specific posture (as shown in the accompanying drawings). If the specific posture changes, the directional indication also changes accordingly. In addition, the terms "including" and "having" and any of their variations are intended to cover non-exclusive inclusions. For example, a process, method, system, product or equipment comprising a series of steps or units is not limited to the steps or units listed, but optionally also includes steps or units that are not listed, or optionally also includes other steps or units inherent to these processes, methods, products or equipment.

[0030] In addition, the reference to "embodiment" herein means that a particular feature, structure, or characteristic described in conjunction with the embodiment may be included in at least one embodiment of the present invention. The appearance of the phrase in various locations in the specification does not necessarily refer to the same embodiment, nor is it an independent or alternative embodiment that is mutually exclusive with other embodiments. It is explicitly and implicitly understood by those skilled in the art that the embodiments described herein may be combined with other embodiments.

[0031] The following will be combined with the drawings in the embodiments of the utility model to clearly and completely describe the technical solutions in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, not all of the embodiments. Based on the embodiments of the utility model, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the utility model.

[0032] Application Overview:

[0033] MTBE has stable chemical properties and relatively high oxygen content. Adding MTBE to gasoline can improve the cold start characteristics and acceleration performance of automobiles and reduce the content of CO in exhaust gas. MTBE can replace tetraethyl lead as an antiknock agent to produce unleaded gasoline. It can also be cracked to produce isobutylene, which is used as a raw material for rubber and other chemical products.

[0034] MTBE is produced by the etherification reaction of isobutylene and methanol under the action of macroporous strong acidic cation exchange resin. The reaction is exothermic and preferably carried out at low temperature. In order to control the reaction temperature, the reaction heat is usually removed by gasifying the liquid C4 material or cooling the reaction product and circulating it back to the reactor inlet. The former heat transfer method is suitable for working conditions with low isobutylene content in the raw material C4. When the isobutylene content is high, the reaction exotherm is large, and the complete vaporization of the liquid C4 material is not enough to absorb all the reaction heat, and the bed temperature cannot be effectively controlled. The latter heat transfer method has a wider range of application and is applicable to a wider range of raw material isobutylene content.

[0035] After a period of use, the activity of the resin catalyst used in the etherification reaction gradually decreases until it is completely deactivated. It needs to be replaced regularly to ensure product quality and output, as well as long-term operation of the device.

[0036] In the existing MTBE production process, two or three etherification reactors are set up. When the catalyst of a reactor is replaced, the device needs to be shut down or the operating load needs to be reduced, resulting in low production efficiency. Multiple etherification reactors usually share one external circulation cooler and external circulation pump, or each reactor is equipped with an external circulation cooler and external circulation pump of the same specifications. The design load of the external circulation cooler and external circulation pump is large, and the equipment investment is high.

[0037] In industrial production, the material at the outlet of the etherification reactor enters the catalytic distillation tower, and a small amount of unreacted isobutylene and methanol are deeply converted in the reaction section. The generated MTBE is continuously separated and taken out from the bottom of the tower. The carbon four after etherification at the top of the tower enters the reflux tank after condensation. Part of the liquid phase at the bottom of the tank is refluxed into the tower, and the other part enters the extraction tower to remove a small amount of methanol through water washing. The extract at the bottom of the extraction tower enters the methanol recovery tower to recover a small amount of methanol. The bottom of the methanol recovery tower is extraction water that basically does not contain methanol, which returns to the extraction tower for recycling.

[0038] In the existing process, the reflux of the catalytic distillation tower is controlled by a single loop of flow meter and regulating valve. The reflux volume is constant during normal operation. When the raw material flow and the isobutylene content fluctuate, the residual C4 flow at the top of the tower changes accordingly. The existing control method cannot adjust the reflux of the catalytic distillation tower in time, resulting in unqualified MTBE and C4 products after etherification, or energy waste. In the existing process, the liquid level of the bottom of the methanol recovery tower and the extraction water extraction flow at the bottom of the tower are controlled in cascade. When the bottom of the tower maintains a certain liquid level, the extraction water flow is constant. When the raw material flow and the isobutylene content fluctuate, the C4 flow after etherification entering the extraction tower changes accordingly. The existing control method cannot adjust the extraction water flow in time, resulting in excessive methanol content in the C4 product after etherification, affecting the production of downstream devices, or causing energy waste.

[0039] Therefore, it is necessary to improve the existing technology and develop process technology with simple process, flexible operation, timely adjustment and precise control, so as to improve the operability of the equipment, extend the production cycle, reduce investment cost and improve economic benefits.

[0040] Figure 1 The figure shows a schematic flow diagram of a methyl tert-butyl ether production device with switchable reactors provided by an embodiment of the utility model. Figure 1As shown, the production device includes: a feeding system 100; a first reactor 201, the inlet of the first reactor 201 is connected to the outlet of the feeding system 100 through a first pipeline 01, the outlet of the first reactor 201 is refluxed to the inlet of the first reactor 201 through a second pipeline 02, and the second pipeline 02 is provided with a first external circulation cooler 901 and a first external circulation pump 903; a second reactor 202, the outlet of the first reactor 201 is connected to the inlet of the second reactor 202 through a third pipeline 03, and the outlet of the second reactor 202 is refluxed to the inlet of the second reactor 202 through a fourth pipeline 04. The fourth pipeline 04 is provided with a second external circulation cooler 902 and a second external circulation pump 904, the collection outlet of the feeding system 100 is connected to the collection inlet of the second reactor 202 through the seventh pipeline 07, and the third reactor 203, the collection outlet of the second reactor 202 is connected to the collection inlet of the third reactor 203 through the fifth pipeline 05; the collection outlet of the feeding system 100 is connected to the collection inlet of the third reactor 203 through the fifteenth pipeline 15; wherein, the first pipeline 01, the second pipeline 02, the third pipeline 03, the fourth pipeline 04, the fifth pipeline 05, the seventh pipeline 07, and the fifteenth pipeline 15 are all provided with switching valves. A first pipeline 01, a seventh pipeline 07, and a fifteenth pipeline 15 are arranged between the feeding system 100 and the first reactor 201, the second reactor 202, and the third reactor 203, and switching valves are arranged on the first pipeline 01, the seventh pipeline 07, and the fifteenth pipeline 15. The raw carbon four and methanol can choose to first enter the first reactor 201, the second reactor 202, or the third reactor 203 through valve switching operation. A second pipeline 02 and a fourth pipeline 04 are respectively arranged between the first reactor 201, the second reactor 202, and the third reactor 203 and the first external circulation cooler 901 and the second external circulation cooler 902. Switching valves are arranged on the second pipeline 02 and the fourth pipeline 04. The three reactors can be used in conjunction with any external circulation cooler through valve switching operation. The priority order of the three reactors can be adjusted arbitrarily according to the activity of the catalyst in the production process, and any one of the reactors can be cut out separately without affecting the normal operation of the device. When the catalyst of one of the reactors needs to be replaced, the device does not need to stop production or reduce load production. The maintenance period of the device can be maintained at more than 4 years. It is suitable for various raw materials such as catalytic C4, isomerized C4, dehydrogenated C4, cracked C4, coal-based C4, etc. with isobutylene content of 0.5-70wt%, and has a wide range of applications.

[0041] Specifically, the raw materials C4 and methanol first enter the feed system 100, and after passing through the buffer tank, feed pump, ratio controller and methanol purification in the feed system, C4 and methanol are discharged from the feed system 100 and enter the first reactor 201, the second reactor 202, and the third reactor 203 in sequence. After the discharge of the first reactor 201 is cooled by the first external circulation cooler 901, a part enters the second reactor 202, and the other part is pressurized by the first external circulation pump 903 and returns to the inlet of the first reactor 201 to remove the heat released by the reaction in the first reactor 201, so as to control the bed layer at a suitable reaction temperature of 30 to 80°C. After the discharge of the second reactor 202 is cooled by the second external circulation cooler 902, a part enters the third reactor 203, and the other part is pressurized by the second external circulation pump 904 and returns to the inlet of the second reactor 202 to remove the heat released by the reaction in the second reactor 202, so as to control the bed layer at a suitable reaction temperature of 30 to 80°C. The material at the outlet of the third reactor 203 enters the catalytic distillation tower.

[0042] It should be understood that the priority order of the three reactors can be adjusted arbitrarily, for example, the first reactor 201, the second reactor 202, and the third reactor 203 can be entered in sequence; or the first reactor 201, the third reactor 203, and the second reactor 202 can be entered in sequence; or the second reactor 202, the first reactor 201, and the third reactor 203 can be entered in sequence; or the second reactor 202, the third reactor 203, and the first reactor 201 can be entered in sequence; or the third reactor 203, the first reactor 201, and the second reactor 202 can be entered in sequence; or the third reactor 203, the second reactor 202, and the first reactor 201 can be entered in sequence. 01; or enters the first reactor 201 and the second reactor 202 in sequence; or enters the second reactor 202 and the first reactor 201 in sequence; enters the first reactor 201 and the third reactor 203 in sequence; enters the third reactor 203 and the first reactor 201 in sequence; or enters the second reactor 202 and the third reactor 203 in sequence; or enters the third reactor 203 and the second reactor 202 in sequence. The sequential process flow switching of multiple reactors can make full use of the activity of the catalyst at different stages, exert its maximum capacity, ensure product quality and yield, shorten the agent replacement cycle, and achieve the minimum waste solid emission and the shortest emission cycle.

[0043] In a possible implementation, the system further includes: a catalytic distillation tower 300, wherein the outlet of the third reactor 203 is connected to the first outlet of the catalytic distillation tower 300 via the sixth pipeline 06, the outlet of the feed system 100 is connected to the second outlet of the catalytic distillation tower 300 via the thirty-second pipeline 32, the top outlet of the catalytic distillation tower 300 is refluxed to the catalytic distillation tower 300 via the twenty-ninth pipeline 29, and the bottom outlet of the catalytic distillation tower 300 is extracted via the twenty-third pipeline 23; an extraction tower 400, The production inlet of the extraction tower 400 is connected to the production outlet of the catalytic distillation tower 300 through the twenty-fourth pipeline 24, and the production outlet of the extraction tower 400 is connected to the twenty-fifth pipeline 25; the methanol recovery tower 500, the bottom production outlet of the extraction tower 400 is connected to the production inlet of the methanol recovery tower 500 through the twenty-sixth pipeline 26, the bottom production outlet of the methanol recovery tower 500 is refluxed to the extraction tower 400 through the twenty-seventh pipeline 27, and the production outlet at the top of the methanol recovery tower 500 is refluxed to the feeding system 100 through the twenty-eighth pipeline 28.

[0044] Specifically, the material from the outlet of the third reactor 203 enters the lower section of the catalytic distillation tower 300, and the supplementary methanol enters the upper section of the catalytic distillation tower 300 through the thirty-second pipeline 32. The upper section includes a reaction section and an etherification catalyst. The residual isobutylene and methanol are deeply converted in the reaction section, and the generated MTBE is continuously separated and extracted from the twenty-third pipeline 23 at the bottom of the catalytic distillation tower 300. The remaining carbon four at the top of the catalytic distillation tower 300 is condensed and enters the reflux tank. A part of the liquid phase at the bottom of the tank is refluxed to the catalytic distillation tower 300, and the other part enters the extraction tower 400. The remaining carbon four The extracted water enters the lower part of the extraction tower 400, and the two are in reverse contact. The top of the extraction tower 400 obtains the etherified C4 product after washing with water to remove a small amount of methanol. The etherified C4 product is extracted through the twenty-fifth pipeline 25. The extract at the bottom of the extraction tower 400 enters the methanol recovery tower 500. The top of the methanol recovery tower 500 obtains the recovered methanol, which is returned to the feeding system 100 through the twenty-eighth pipeline 28 to continue to participate in the reaction. The bottom of the methanol recovery tower 500 is the extraction water that basically does not contain methanol, which is returned to the extraction tower 400 through the twenty-seventh pipeline 27 for recycling.

[0045] In a possible implementation, it also includes: a first mixer 1001; a first temperature controller 801, the first mixer 1001 and the first temperature controller 801 are both arranged on the first pipeline 01; a second mixer 1002; a second temperature controller 802, the second mixer 1002 and the second temperature controller 802 are both arranged on the third pipeline 03; a third mixer 1003; a third temperature controller 803, the third mixer 1003 and the third temperature controller 803 are both arranged on the fifth pipeline 05.

[0046] Specifically, the first mixer 1001, the second mixer 1002 and the third mixer 1003 are respectively located on the first pipeline 01, the third pipeline 03 and the fifth pipeline 05, and are respectively used to fully mix materials such as C4 and methanol entering the first reactor 201, the second reactor 202 and the third reactor 203, which is beneficial to improve the reaction effect.

[0047] In a possible implementation, the intake port of the feed system 100 is respectively connected to the 30th pipeline 30 and the 31st pipeline 31. The 30th pipeline 30 is the intake pipeline for raw material carbon four, and the 31st pipeline is the intake pipeline for raw material methanol.

[0048] In a possible implementation, it also includes: a first flow controller 701, the first flow controller 701 is arranged on the 30th pipeline 30, and is used to control the feed flow rate of the raw material carbon four; a second flow controller 702, the second flow controller 702 is arranged on the 24th pipeline 24, and is used to control the flow rate of the distillation product entering the extraction tower 400; a first flow regulating valve 703, the first flow regulating valve 703 is installed on the 29th pipeline 29, and is used to adjust the reflux amount of the distillation product in the catalytic distillation tower 300 back to the catalytic distillation tower 300; The second flow regulating valve 704 is installed on the twenty-seventh pipeline 27, and is used to adjust the reflux amount of the recovered product in the methanol recovery tower 500 to the extraction tower 400; wherein, the first flow controller 701 is electrically connected to the first flow regulating valve 703 through the seventh signal line S7, and the first flow regulating valve 703 is controlled according to the first flow controller 701; the second flow controller 702 is electrically connected to the second flow regulating valve 704 through the eighth signal line S8, and the second flow regulating valve 704 is controlled according to the second flow controller 702.

[0049] In a possible implementation, it also includes: a first temperature display 905; a first external circulation cooler 901; a first external circulation pump 903; the first temperature display 905, the first external circulation cooler 901 and the first external circulation pump 903 are sequentially arranged on the second pipeline 02, and the first external circulation cooler 901 is externally connected to the first outlet pipeline of cooling water; the outlet of the first external circulation cooler 901 is connected to the inlet of the first reactor 201 through the seventeenth pipeline 17, and the outlet of the first external circulation cooler 901 is connected to the inlet of the third reactor 203 through the ninth pipeline 09; the outlet of the first external circulation pump 903 is connected to the inlet of the second reactor 202 through the tenth pipeline 10, and the outlet of the first external circulation pump 903 is connected to the inlet of the third reactor 202 through the eighteenth pipeline 18 The inlet of the reactor 203 is connected; a second temperature display 906; a second external circulation cooler 902; a second external circulation pump 904; the second temperature display 906, the second external circulation cooler 902 and the second external circulation pump 904 are sequentially arranged on the fourth pipeline 04, and the second external circulation cooler 902 is externally connected to the second outlet pipeline of cooling water; the outlet of the second external circulation cooler 902 is connected to the inlet of the first reactor 201 through the twelfth pipeline 12, the outlet of the second external circulation pump 904 is connected to the inlet of the third reactor 203 through the thirteenth pipeline 13, and the outlet of the first reactor 201 is connected to the inlet of the catalytic distillation tower 300 through the fourteenth pipeline 14; a third temperature display 907, and the third temperature display 907 is arranged on the sixth pipeline 06.

[0050] In a possible implementation, it further includes: a first temperature regulating valve 908, which is installed on the first outlet pipeline of cooling water; and a second temperature regulating valve 909, which is installed on the second outlet pipeline of cooling water.

[0051] Specifically, a first temperature controller 801 is provided at the inlet of the first reactor 201, a first temperature display 905 is provided at the outlet of the first reactor 201, a second temperature controller 802 is provided at the inlet of the second reactor 202, a second temperature display 906 is provided at the outlet of the second reactor 202, a third temperature controller 803 is provided at the inlet of the third reactor 203, a third temperature display 907 is provided at the outlet of the third reactor 203, a first temperature regulating valve 908 is provided on the cooling water outlet pipeline of the first external circulation cooler 901, and a second temperature regulating valve 909 is provided on the cooling water outlet pipeline of the second external circulation cooler 902. The first temperature controller 801 is connected to the first temperature regulating valve 908 through the first signal line S1, and the first temperature controller 801 is connected to the second temperature regulating valve 909 through the second signal line S2; the second temperature controller 802 is connected to the first temperature regulating valve 908 through the third signal line S3, and the second temperature controller 802 is connected to the second temperature regulating valve 909 through the fourth signal line S4, the third temperature controller 803 is connected to the first temperature regulating valve 908 through the fifth signal line S5, and the third temperature controller 803 is connected to the second temperature regulating valve 909 through the sixth signal line S6. The first temperature controller 801, the second temperature controller 802, and the third temperature controller 803 can all be cascade-controlled with the first temperature regulating valve 908 or the second temperature regulating valve 909 through the signal line, and the temperature controller controls the temperature to adjust the opening of the temperature regulating valve and adjust the cooling water flow, thereby controlling the reaction inlet temperature, and the temperature display observes the reaction outlet temperature, monitors the temperature rise, and thus determines the catalyst activity decline.

[0052] In a possible implementation, the first temperature controller 801 is electrically connected to the first temperature regulating valve 908 through the first signal line S1, and the first temperature controller 801 is electrically connected to the second temperature regulating valve 909 through the second signal line S2; the second temperature controller 802 is point-connected to the first temperature regulating valve 908 through the third signal line S3, and the second temperature controller 802 is electrically connected to the second temperature regulating valve 909 through the fourth signal line S4; the third temperature controller 803 is point-connected to the first temperature regulating valve 908 through the fifth signal line S5, and the third temperature controller 803 is connected to the second temperature regulating valve 909 through the sixth signal line S6.

[0053] In a possible implementation, an analyzer 600 is further included, and the analyzer 600 is electrically connected to the first flow regulating valve 703 via a seventh signal line S7.

[0054] Specifically, the first flow controller 701 and the analyzer 600 are controlled in cascade with the first flow regulating valve 703 through the seventh signal line S7. The isobutylene feed flow rate fed back by the first flow controller 701 and the analyzer 600 controls the opening of the first flow regulating valve 703, thereby adjusting the reflux amount of the catalytic distillation tower 300. The two are reversely controlled. If the isobutylene flow rate is large, the first flow regulating valve 703 is closed to reduce the reflux amount. On the contrary, the valve is opened to increase the reflux amount, which can not only control the product indicators of the top and bottom of the catalytic distillation tower 300 in time, but also save energy consumption.

[0055] A second flow controller 702 is provided on the 24th pipeline 24 of the residual C4 at the extraction inlet of the extraction tower 400, and a second flow regulating valve 704 is provided on the 27th pipeline 27 of the extraction water at the bottom outlet of the methanol recovery tower 500. The second flow controller 702 is connected to the second flow regulating valve 704 through the eighth signal line S8. The second flow controller 702 controls the opening of the second flow regulating valve 704, thereby adjusting the flow of the extraction water. The two are positive control. If the flow of the residual C4 is large, the second flow regulating valve 704 is opened, otherwise the valve is closed, so that the amount of water used to wash the C4 can be adjusted in time, which can effectively control the methanol index in the residual C4 and save energy consumption.

[0056] In a possible implementation, the production outlet of the first reactor 201 is connected to the inlet of the second external circulation cooler 902 through the nineteenth pipeline 19, the outlet of the second external circulation cooler 902 is connected to the production inlet of the second reactor 202 through the twentieth pipeline 20, the outlet of the second external circulation pump 904 is connected to the production inlet of the first reactor 201 through the twenty-first pipeline 21, and the production outlet of the second reactor 202 is connected to the production inlet of the catalytic distillation tower 300 through the twenty-second pipeline 22; the production outlet of the second reactor 202 is connected to the inlet of the first external circulation cooler 901 through the eighth pipeline 08; the production outlet of the third reactor 203 is connected to the inlet of the second external circulation cooler 902 through the eleventh pipeline 11, and the production outlet of the third reactor 203 is connected to the inlet of the first external circulation cooler 901 through the sixteenth pipeline 16.

[0057] The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention. Any modifications, equivalent substitutions, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A methyl tert-butyl ether production device with switchable reactors, characterized in that: include: Feed system (100); A first reactor (201), wherein the inlet of the first reactor (201) is connected to the inlet of the feed system (100) via a first pipeline (01), the inlet of the first reactor (201) is refluxed to the inlet of the first reactor (201) via a second pipeline (02), and a first external circulation cooler (901) and a first external circulation pump (903) are provided on the second pipeline (02); The second reactor (202) is connected to the inlet of the second reactor (202) through the third pipeline (03) and the outlet of the first reactor (201); the outlet of the second reactor (202) is refluxed to the inlet of the second reactor (202) through the fourth pipeline (04); the fourth pipeline (04) is provided with a second external circulation cooler (902) and a second external circulation pump (904); the outlet of the feeding system (100) is connected to the inlet of the second reactor (202) through the seventh pipeline (07); A third reactor (203), wherein the extraction port of the second reactor (202) is connected to the extraction port of the third reactor (203) via a fifth pipeline (05), and the extraction port of the feed system (100) is connected to the extraction port of the third reactor (203) via a fifteenth pipeline (15); Among them, the first pipeline (01), the second pipeline (02), the third pipeline (03), the fourth pipeline (04), the fifth pipeline (05), the seventh pipeline (07) and the fifteenth pipeline (15) are all provided with switching valves.

2. The methyl tert-butyl ether production device with switchable reactors according to claim 1, characterized in that: Also includes: A catalytic distillation tower (300), wherein the extraction port of the third reactor (203) is connected to the first extraction port of the catalytic distillation tower (300) via a sixth pipeline (06), the extraction port of the feed system (100) is connected to the second extraction port of the catalytic distillation tower (300) via a thirty-second pipeline (32), the top extraction port of the catalytic distillation tower (300) is refluxed to the catalytic distillation tower (300) via a twenty-ninth pipeline (29), and the bottom extraction port of the catalytic distillation tower (300) is extracted via a twenty-third pipeline (23); An extraction tower (400), wherein the extraction inlet of the extraction tower (400) is connected to the extraction outlet of the catalytic distillation tower (300) via a twenty-fourth pipeline (24), and the extraction outlet of the extraction tower (400) is connected to a twenty-fifth pipeline (25); A methanol recovery tower (500), wherein the bottom outlet of the extraction tower (400) is connected to the outlet of the methanol recovery tower (500) via a twenty-sixth pipeline (26), the bottom outlet of the methanol recovery tower (500) is refluxed to the extraction tower (400) via a twenty-seventh pipeline (27), and the top outlet of the methanol recovery tower (500) is refluxed to the feeding system (100) via a twenty-eighth pipeline (28).

3. The methyl tert-butyl ether production device with switchable reactors according to claim 2, characterized in that: include: A first mixer (1001); A first temperature controller (801), wherein the first mixer (1001) and the first temperature controller (801) are both arranged on a first pipeline (01); a second mixer (1002); a second temperature controller (802), wherein the second mixer (1002) and the second temperature controller (802) are both arranged on the third pipeline (03); A third mixer (1003); a third temperature controller (803), wherein the third mixer (1003) and the third temperature controller (803) are both arranged on the fifth pipeline (05).

4. The methyl tert-butyl ether production device with switchable reactors according to claim 3, characterized in that: The intake port of the feeding system (100) is respectively connected to the 30th pipeline (30) and the 31st pipeline (31).

5. The methyl tert-butyl ether production device with switchable reactors according to claim 4, characterized in that: Also includes: A first flow controller (701), the first flow controller (701) is arranged on the 30th pipeline (30), and is used to control the feed flow rate of the raw material carbon four; a second flow controller (702), the second flow controller (702) being disposed on the twenty-fourth pipeline (24) and being used to control the flow rate of the distillation product entering the extraction tower (400); a first flow regulating valve (703), the first flow regulating valve (703) being installed on the twenty-ninth pipeline (29) and being used for regulating the reflux amount of the distillation product in the catalytic distillation tower (300) refluxed to the catalytic distillation tower (300); a second flow regulating valve (704), the second flow regulating valve (704) being installed on the twenty-seventh pipeline (27) and being used for regulating the reflux amount of the recovered product in the methanol recovery tower (500) refluxed to the extraction tower (400); The first flow controller (701) is electrically connected to the first flow regulating valve (703) via a seventh signal line (S7), and the first flow regulating valve (703) is controlled according to the first flow controller (701); the second flow controller (702) is electrically connected to the second flow regulating valve (704) via an eighth signal line (S8), and the second flow regulating valve (704) is controlled according to the second flow controller (702).

6. The methyl tert-butyl ether production device with switchable reactors according to claim 5, characterized in that: Also includes: A first temperature display (905); a first external circulation cooler (901); a first external circulation pump (903); the first temperature display (905), the first external circulation cooler (901) and the first external circulation pump (903) are sequentially arranged on the second pipeline (02); the first external circulation cooler (901) is externally connected to a first outlet pipeline of cooling water; the outlet of the first external circulation cooler (901) is connected to the inlet of the first reactor (201) through the seventeenth pipeline (17); the outlet of the first external circulation cooler (901) is connected to the inlet of the third reactor (203) through the ninth pipeline (09); the outlet of the first external circulation pump (903) is connected to the inlet of the second reactor (202) through the tenth pipeline (10); the outlet of the first external circulation pump (903) is connected to the inlet of the third reactor (203) through the eighteenth pipeline (18); a second temperature display (906); a second external circulation cooler (902); a second external circulation pump (904); the second temperature display (906), the second external circulation cooler (902) and the second external circulation pump (904) are sequentially arranged on the fourth pipeline (04); the second external circulation cooler (902) is externally connected to a second cooling water outlet pipeline; the outlet of the second external circulation cooler (902) is connected to the inlet of the first reactor (201) through a twelfth pipeline (12); the outlet of the second external circulation pump (904) is connected to the inlet of the third reactor (203) through a thirteenth pipeline (13); the outlet of the first reactor (201) is connected to the inlet of the catalytic distillation tower (300) through a fourteenth pipeline (14); A third temperature display (907), wherein the third temperature display (907) is arranged on the sixth pipeline (06).

7. The methyl tert-butyl ether production device with switchable reactors according to claim 6, characterized in that: Also includes: A first temperature regulating valve (908), the first temperature regulating valve (908) is installed on the first outlet pipeline of the cooling water; a second temperature regulating valve (909), the second temperature regulating valve (909) is installed on the second outlet pipeline of the cooling water.

8. The methyl tert-butyl ether production device with switchable reactors according to claim 7, characterized in that: The first temperature controller (801) is electrically connected to the first temperature regulating valve (908) via a first signal line (S1), and the first temperature controller (801) is electrically connected to the second temperature regulating valve (909) via a second signal line (S2); the second temperature controller (802) is point-connected to the first temperature regulating valve (908) via a third signal line (S3), and the second temperature controller (802) is electrically connected to the second temperature regulating valve (909) via a fourth signal line (S4); the third temperature controller (803) is point-connected to the first temperature regulating valve (908) via a fifth signal line (S5), and the third temperature controller (803) is connected to the second temperature regulating valve (909) via a sixth signal line (S6).

9. The methyl tert-butyl ether production device with switchable reactors according to claim 5, characterized in that: It also includes an analyzer (600), wherein the analyzer (600) is electrically connected to the first flow regulating valve (703) via a seventh signal line (S7).

10. The methyl tert-butyl ether production device with switchable reactors according to claim 5, characterized in that: The production outlet of the first reactor (201) is connected to the inlet of the second external circulation cooler (902) through a nineteenth pipeline (19), the outlet of the second external circulation cooler (902) is connected to the production inlet of the second reactor (202) through a twentieth pipeline (20), the outlet of the second external circulation pump (904) is connected to the production inlet of the first reactor (201) through a twenty-first pipeline (21), and the production outlet of the second reactor (202) is connected to the production inlet of the catalytic distillation tower (300) through a twenty-second pipeline (22); The extraction outlet of the second reactor (202) is connected to the inlet of the first external circulation cooler (901) via an eighth pipeline (08); The production outlet of the third reactor (203) is connected to the inlet of the second external circulation cooler (902) through the eleventh pipeline (11), and the production outlet of the third reactor (203) is connected to the inlet of the first external circulation cooler (901) through the sixteenth pipeline (16).

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