阅读说明：本技术 一种环己烷脱氢制苯装置的催化剂再生工艺 (Catalyst regeneration process of cyclohexane dehydrogenation benzene preparation device ) 是由 沈震 于 2021-01-29 设计创作，主要内容包括：本发明属于环己烷脱氢领域,尤其是一种环己烷脱氢制苯装置的催化剂再生工艺,针对整过过程耗时长；需要进行反应器的拆装和催化剂的装卸；来回过程需要陆路运输；工厂再生单次处理量小(实际生产使用量大,工厂需多次分批再生)；工厂再生需要费用的问题,现提出如下方案,其包括进出料换热器,进出料换热器的输出端连接有空冷器,空冷器的输出端连接有水冷器,水冷器的输出端连接有气液分离罐,本发明无需对环己烷脱氢反应器进行拆装；无需对环己烷脱氢催化剂进行卸出和再次装填；无需向外运输和从外运输回装置；再生处理量大,可一次性全部再生完；大大缩短再生所需要的时间。(The invention belongs to the field of cyclohexane dehydrogenation, in particular to a catalyst regeneration process of a cyclohexane dehydrogenation benzene preparation device, which aims at long time consumption in the whole process; the disassembly and assembly of the reactor and the loading and unloading of the catalyst are required; the process of going back and forth requires land transportation; the single treatment capacity of factory regeneration is small (the actual production usage is large, and the factory needs to be regenerated in batches for many times); the invention provides a scheme for solving the problem of cost required by factory regeneration, which comprises a feeding and discharging heat exchanger, wherein the output end of the feeding and discharging heat exchanger is connected with an air cooler, the output end of the air cooler is connected with a water cooler, and the output end of the water cooler is connected with a gas-liquid separation tank; the cyclohexane dehydrogenation catalyst does not need to be discharged and refilled; without the need to transport outward and back to the device from outside; the regeneration treatment capacity is large, and the regeneration can be completed all at one time; the time required for regeneration is greatly shortened.)

1. The utility model provides a catalyst regeneration technology of cyclohexane dehydrogenation benzene manufacturing device, includes business turn over material heat exchanger (1), its characterized in that, the output of business turn over material heat exchanger (1) is connected with air cooler (2), the output of air cooler (2) is connected with water cooler (3), the output of water cooler (3) is connected with gas-liquid separation jar (4), the output of gas-liquid separation jar (4) is connected with centrifugal compressor (5), the output of centrifugal compressor (5) is connected with the on-line monitoring appearance, the output of on-line monitoring appearance (6) is connected with the input of business turn over material pipe heat exchanger, the output of business turn over material pipe is connected with five-in-one heating furnace (7) and five-in-one cyclohexane dehydrogenation ware (8).

2. The catalyst regeneration process for a cyclohexane dehydrogenation benzene production device according to claim 1, wherein the five-in-one heating furnace (7) comprises a first heating furnace (701), a second heating furnace (702), a third heating furnace (703), a fourth heating furnace (704) and an fifth heating furnace (705).

3. The catalyst regeneration process of a cyclohexane dehydrogenation benzene-making device according to claim 2, characterized in that the penta-cyclohexane dehydrogenation reactor (8) comprises a first reactor (801), a second reactor (802), a third reactor (803), a fourth reactor (804) and a fifth reactor (805).

4. The catalyst regeneration process of a cyclohexane dehydrogenation benzene-making device according to claim 3, characterized in that the output end of the first heating furnace (701) is connected with a first reactor (801), the output end of the first reactor (801) is connected with the input end of a second heating furnace (702), the output end of the second heating furnace (702) is connected with a second reactor (802), the output end of the second reactor (802) is connected with a third heating furnace (703), and the output end of the third heating furnace (703) is connected with a third reactor (803).

5. The catalyst regeneration process for the cyclohexane dehydrogenation benzene production device according to claim 4, characterized in that the output end of the third reactor (803) is connected with a fourth heating furnace (704), the output end of the fourth heating furnace (704) is connected with a fourth reactor (804), the output end of the fourth reactor (804) is connected with a fifth heating furnace (705), the output end of the fifth heating furnace (705) is connected with a fifth reactor (805), and the output end of the fifth reactor (805) is connected with the input end of the feeding and discharging heat exchanger (1).

6. The catalyst regeneration process of a cyclohexane dehydrogenation benzene production device according to claim 5, characterized in that the output end of the gas-liquid separation tank (4) is connected with a first valve (9), and a second valve (10) is connected between the centrifugal compressor (5) and the on-line detector (6).

7. The catalyst regeneration process of a cyclohexane dehydrogenation benzene production device according to claim 6, characterized in that a first pipeline and a second pipeline are connected between the online detector (6) and the feed and discharge heat exchanger (1), the first pipeline is provided with a first check valve (11), a needle valve (12), a flow meter (13) and a third valve, and the second pipeline is provided with a second check valve (15) and a fourth valve (16).

Technical Field

The invention relates to the technical field of cyclohexane dehydrogenation, in particular to a catalyst regeneration process of a cyclohexane dehydrogenation benzene preparation device.

Background

The production device for preparing benzene and hydrogen by cyclohexane dehydrogenation (hereinafter referred to as "cyclohexane dehydrogenation device") is a production device which generates benzene and hydrogen under the catalytic action of a catalyst (hereinafter referred to as "cyclohexane dehydrogenation catalyst") under the conditions of high temperature and certain pressure, and respectively obtains the benzene and the hydrogen through a series of gas-liquid separation and pressurization.

The cyclohexane dehydrogenation device is only set by Fujian Yongrong scientific and technological limited company at present in China, the capacity of the cyclohexane dehydrogenation device is 18 ten thousand tons of benzene per year, the cyclohexane dehydrogenation device is used as a matching device of a caprolactam project, cyclohexane which is the only byproduct of a cyclohexanone device in a hydration method of the caprolactam project is used as a raw material to produce benzene and hydrogen, and then the benzene and the hydrogen are used as the raw material of the cyclohexanone device in the hydration method. (the chemical principle of the cyclohexanone device of the hydration method is that benzene and hydrogen are hydrogenated to generate cyclohexane and cyclohexene, the cyclohexane is separated out as a byproduct, the cyclohexene and water are hydrated to generate cyclohexanol, the cyclohexanol is dehydrogenated to generate the cyclohexanone and hydrogen, and the hydrogen is recycled)

The cyclohexane dehydrogenation device is used for converting cyclohexane which is a byproduct of a cyclohexanone device in a hydration method into benzene and hydrogen, and then the benzene and hydrogen are used in the cyclohexanone device in the hydration method, so that the outward selling of the cyclohexane is avoided, the outward purchase or self-production of the benzene and the hydrogen is reduced, the cost is saved, and the benefit is increased.

. In the cyclohexane dehydrogenation process, the cyclohexane dehydrogenation catalyst needs to be periodically regenerated and recycled to a factory from a catalyst manufacturer, and the catalyst is transported back to the device after being regenerated, and the process is as follows during the period of being put into use:

1. the device is stopped, and nitrogen replacement treatment is carried out on the process system;

2. discharging the cyclohexane dehydrogenation catalyst out of the reactor;

3. packaging and transporting the cyclohexane dehydrogenation catalyst to a factory;

4. the cyclohexane dehydrogenation catalyst is regenerated in a factory;

5. packaging and transporting the cyclohexane dehydrogenation catalyst back to a cyclohexane dehydrogenation device;

6. filling a cyclohexane dehydrogenation catalyst into the reactor;

7. replacing nitrogen in the process system and activating a cyclohexane dehydrogenation catalyst;

8. the device is used after driving.

The above process achieves the purpose of regenerating the cyclohexane dehydrogenation catalyst, improves and recovers the performance of the catalyst, belongs to an ex-situ regeneration process, and has certain defects, such as:

1. the whole process consumes long time;

2. the disassembly and assembly of the reactor and the loading and unloading of the catalyst are required;

3. the process of going back and forth requires land transportation;

4. the single treatment capacity of factory regeneration is small (the actual production usage is large, and the factory needs to be regenerated in batches for many times);

5. plant regeneration requires expense.

Therefore, a catalyst regeneration process of a cyclohexane dehydrogenation benzene preparation device is provided.

Disclosure of Invention

The invention aims to solve the defects in the prior art and provides a catalyst regeneration process of a cyclohexane dehydrogenation benzene preparation device.

In order to achieve the purpose, the invention adopts the following technical scheme:

the utility model provides a catalyst regeneration technology of cyclohexane dehydrogenation benzene manufacturing device, includes the business turn over material heat exchanger, the output of business turn over material heat exchanger is connected with the air cooler, the output of air cooler is connected with the water cooler, the output of water cooler is connected with the gas-liquid separation jar, the output of gas-liquid separation jar is connected with centrifugal compressor, centrifugal compressor's output is connected with online monitor, online monitor's output is connected with the input of business turn over material pipe heat exchanger, the output of business turn over material pipe is connected with five-in-one heating furnace and five-in-one cyclohexane dehydrogenation reactors.

Preferably, the five-in-one heating furnace comprises a first heating furnace, a second heating furnace, a third heating furnace, a fourth heating furnace and a fifth heating furnace.

Preferably, the penta-cyclohexane dehydrogenation reactor comprises a first reactor, a second reactor, a third reactor, a fourth reactor and a fifth reactor.

Preferably, the output end of the first heating furnace is connected with a first reactor, the output end of the first reactor is connected with the input end of a second heating furnace, the output end of the second heating furnace is connected with a second reactor, the output end of the second reactor is connected with a third heating furnace, and the output end of the third heating furnace is connected with a third reactor.

Preferably, the output end of the third reactor is connected with a fourth heating furnace, the output end of the fourth heating furnace is connected with a fourth reactor, the output end of the fourth reactor is connected with a fifth heating furnace, the output end of the fifth heating furnace is connected with a fifth reactor, and the output end of the fifth reactor is connected with the input end of the feeding and discharging heat exchanger.

Preferably, the output end of the gas-liquid separation tank is connected with a first valve, and a second valve is connected between the centrifugal compressor and the online detector.

Preferably, a first pipeline and a second pipeline are connected between the online detector and the feeding and discharging heat exchanger, a first check valve, a needle valve, a flowmeter and a third valve are installed on the first pipeline, and a second check valve and a fourth valve are installed on the second pipeline.

Compared with the prior art, the invention has the beneficial effects that:

1. the cyclohexane dehydrogenation reactor does not need to be disassembled and assembled;

2. the cyclohexane dehydrogenation catalyst does not need to be discharged and refilled;

3. without the need to transport outward and back to the device from outside;

4. the regeneration treatment capacity is large, and the regeneration can be completed all at one time;

5. greatly shorten the time required by regeneration;

6. the temperature and oxygen content of any regeneration stage can be controlled;

7. the one-time regeneration of the loading amount of the cyclohexane dehydrogenation catalyst is realized, and loading, unloading and returning to a factory for regeneration are not needed;

8. the catalyst used by the cyclohexane dehydrogenation device can be completely regenerated at one time, and the catalyst of the cyclohexane dehydrogenation device can be regenerated at one time in the device (in the using environment).

Drawings

FIG. 1 is a process flow diagram of a catalyst regeneration process of a cyclohexane dehydrogenation benzene production device according to the present invention.

Reference numbers in the figures: 1 feeding and discharging heat exchanger, 2 air cooler, 3 water cooler, 4 gas-liquid separation tank, 5 centrifugal compressor, 6 on-line detector, 7 five-in-one heating furnace, 701 first heating furnace, 702 second heating furnace, 703 third heating furnace, 704 fourth heating furnace, 705 fifth heating furnace, 8 cyclohexane dehydrogenation reactor, 801 first reactor, 802 second reactor, 803 third reactor, 804 fourth reactor, 805 fifth reactor, 9 first valve, 10 second valve, 11 first check valve, 12 needle valve, 13 flowmeter, 14 third valve, 15 second check valve, 16 fourth valve.

Detailed Description

In order to make the objects, technical solutions and advantages of the embodiments of the present disclosure more clear, the technical solutions of the embodiments of the present disclosure will be described below clearly and completely with reference to the drawings of the embodiments of the present disclosure, and it is obvious that the described embodiments are some embodiments of the present disclosure, but not all embodiments, and all other embodiments obtained by a person of ordinary skill in the art without creative efforts based on the described embodiments of the present disclosure belong to the protection scope of the present disclosure.

Unless otherwise defined, technical or scientific terms used herein should be understood as having a common meaning as understood by those of ordinary skill in the art to which this disclosure belongs, and the use of "including" or "comprising" and the like in this disclosure means that the element or item appearing before the word covers the element or item listed after the word and its equivalents, but does not exclude other elements or items, that "connected" or "connected" and the like are not limited to physical or mechanical connections, and may include electrical connections, whether direct or indirect, "upper", "lower", "left", "right", and the like are used merely to indicate relative positional relationships, which may also change accordingly when the absolute position of the object being described changes.

To maintain the following description of the embodiments of the present disclosure clear and concise, a detailed description of known functions and known components have been omitted from the present disclosure.

Referring to fig. 1, a catalyst regeneration process of cyclohexane dehydrogenation benzene manufacturing device, including business turn over material heat exchanger 1, the output of business turn over material heat exchanger 1 is connected with air cooler 2, the output of air cooler 2 is connected with water cooler 3, the output of water cooler 3 is connected with gas-liquid separation jar 4, the output of gas-liquid separation jar 4 is connected with centrifugal compressor 5, the output of centrifugal compressor 5 is connected with the on-line monitoring appearance, the output of on-line monitoring appearance 6 is connected with the input of business turn over material pipe heat exchanger, the output of business turn over material pipe is connected with five unification heating furnace 7 and five unification cyclohexane dehydrogenation ware 8.

The five-in-one heating furnace 7 comprises a first heating furnace 701, a second heating furnace 702, a third heating furnace 703, a fourth heating furnace 704 and a fifth heating furnace 705, and the five-in-one cyclohexane dehydrogenation reactor 8 comprises a first reactor 801, a second reactor 802, a third reactor 803, a fourth reactor 804 and a fifth reactor 805.

The output end of the first heating furnace 701 is connected with a first reactor 801, the output end of the first reactor 801 is connected with the input end of a second heating furnace 702, the output end of the second heating furnace 702 is connected with a second reactor 802, the output end of the second reactor 802 is connected with a third heating furnace 703, and the output end of the third heating furnace 703 is connected with a third reactor 803.

The output end of the third reactor 803 is connected with a fourth heating furnace 704, the output end of the fourth heating furnace 704 is connected with a fourth reactor 804, the output end of the fourth reactor 804 is connected with a fifth heating furnace 705, the output end of the fifth heating furnace 705 is connected with a fifth reactor 805, and the output end of the fifth reactor 805 is connected with the input end of the charging and discharging heat exchanger 1.

The output end of the gas-liquid separation tank 4 is connected with a first valve 9, a second valve 10 is connected between the centrifugal compressor 5 and the on-line detector 6, a first pipeline and a second pipeline are connected between the on-line detector 6 and the charging and discharging heat exchanger 1, the first pipeline is provided with a first check valve 11, a needle valve 12, a flowmeter 13 and a third valve, and the second pipeline is provided with a second check valve 15 and a fourth valve 16.

The working principle is as follows: the gas in the gas-liquid separation tank 4 enters a centrifugal compressor 5, is pressurized and sent to a feed and discharge heat exchanger 1, enters a first reactor 801 after being heated by a first heating furnace 701, enters a second reactor 802 after being heated by a second heating furnace 702, enters a third reactor 803 after being heated by a third heating furnace 703, enters a fourth reactor 804 after being heated by a fourth heating furnace 704, enters a fifth reactor 805 after being heated by a fifth heating furnace 705, the gas with a certain temperature discharged from the fifth reactor 805 exchanges heat with the gas entering the first heating furnace 701 in the feed and discharge heat exchanger 1, and is cooled to the gas-liquid separation tank 4 through the feed and discharge heat exchanger 1 and a water cooler 3. The condensate generated in the regeneration process is mainly water which is condensed and separated by gas and liquid in a water cooler 3 and a gas-liquid separation tank 4, the sewage is discharged from the bottom through a first valve 9, the system is discharged, the generated waste gas is discharged through a second valve 10, the system is discharged, the process system is pressurized to a proper pressure through 0.7MPa nitrogen during regeneration, a centrifugal compressor 5 is started, a circulating centrifugal compressor 5 under the condition of nitrogen is established, a material inlet and outlet heat exchanger 1 → a first heating furnace 701 → a first reactor 801 → a second heating furnace 702 → a second reactor 802 → a third heating furnace 703 → a third reactor 803 → a fourth heating furnace 704 → a fourth reactor 804 → a fifth heating furnace 705 → a material inlet and outlet heat exchanger 1 → an air cooler 2 → a water cooler 3 → a gas-liquid separation tank 4 → a material inlet and outlet heat exchanger 1, the temperature of a cyclohexane dehydrogenation reactor 8 is raised and controlled to be stable by stages by controlling the load of the five-in-one heating furnace 7, when the regeneration temperature is reached, the proper amount of compressed air is controlled through the third valve and the needle valve 12 to enter the process system, the temperature of the bed layer of the cyclohexane dehydrogenation reactor 8 is observed to control the introduction amount of the compressed air, the detection value of the online detector 6 is observed at regular time, the gas emptying amount is controlled through the change of the detection value and the second valve 10, and the regeneration is controlled through the temperature, the compressed air amount, the circulation amount of the centrifugal compressor 5, the detection value of the online detector 6 and the emptying amount in the whole process.

The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and the inventive concepts thereof according to the present invention should be equivalent or changed within the scope of the present invention.