A carbon four hydrogenation catalyst regeneration system and method

Abstract

The present application belongs to the field of catalyst regeneration, and discloses a carbon four hydrogenation catalyst regeneration system and method. The system comprises a regeneration gas inlet-outlet heat exchanger, a regeneration gas electric heater, a carbon four hydrogenation reactor, a nitrogen pipeline, a hydrogen pipeline, a steam pipeline, an air pipeline, a regeneration gas adapter, a regeneration tail gas adapter, a first tail gas discharge pipeline and a waste stream treatment subsystem. The present application can perform hot hydrogen stripping and coking regeneration according to the heavy component content of carbon four raw materials and the coking degree of carbon four hydrogenation catalyst, can be suitable for different catalysts used in carbon four fraction hydrogenation technology, increases economic benefits, and at the same time guarantees the safety and environmental protection of the process flow.

Description

TECHNICAL FIELD

[0001] The present application belongs to the field of catalyst regeneration, more particularly, to a carbon four hydrogenation catalyst regeneration system and method. BACKGROUND

[0002] Currently, there are various types of carbon four fraction hydrogenation technologies, such as ethylene cracking carbon four hydrogenation, butadiene device carbon four alkyne tail gas hydrogenation to produce butadiene or butene-1, etc. Among them, due to the existence of olefins and alkynes and a small amount of heavy components in the carbon four fraction, the hydrogenation process will produce polymers and gum components, thereby affecting the activity of the catalyst. With the increasing maturity of hydrogenation catalysts, especially for carbon four fraction selective hydrogenation technology, noble metal palladium-based catalysts and non-noble metal nickel-based catalysts have become the most commonly used two catalysts for carbon four unsaturated fraction hydrogenation. Traditional devices mostly use noble metal catalysts. With the continuous improvement of the selectivity and conversion rate of non-noble metal nickel-based catalysts by domestic research institutions, the adoption rate of non-noble metal nickel-based catalysts in newly built carbon four fraction hydrogenation projects has increased year by year.

[0003] The current hydrogenation catalyst regeneration technology includes two types: (1) In general, for catalysts with short running time and little or no coke on the surface, hot hydrogen stripping method is used for catalyst regeneration. For example, CN101376115A discloses a regeneration method for noble metal hydrogenation catalyst, which is regenerated by passing pure hydrogen. The process is simple. However, the use of pure hydrogen not only has high economic cost, but also is difficult to stabilize the temperature control. (2) For catalysts with long running time, the activity is reduced due to coking and carbon deposition, and water vapor-air method is used for coke burning regeneration to restore the activity of the catalyst. For example, CN111822059A discloses a hydrogenation catalyst regeneration method, which realizes the regeneration of the reactor catalyst of the cracking gasoline (C5-C14) hydrogenation device by using different stages and different proportions of nitrogen, steam and air. This process realizes coke burning regeneration, and the tail gas is environmentally friendly and sealed. However, this process is more suitable for the regeneration of heavy component hydrogenation and noble metal catalysts.

[0004] At present, the regeneration system is simple, and is mainly used for coking regeneration of catalysts in carbon five and above component reaction devices. There is no device and method for carbon four hydrogenation catalyst regeneration. Therefore, it is necessary to provide a regeneration system to adapt to the above-mentioned carbon four fraction hydrogenation technology and different catalysts used in carbon four fraction hydrogenation technology, and at the same time ensure the safety and reliability of the regeneration system during use (since the hydrogen used in hot hydrogen stripping and the air used in coke burning regeneration cannot coexist). SUMMARY

[0005] The present application aims at the different of prior art, and provides a carbon four hydrogenation catalyst regeneration system and method.

[0006] In order to achieve the above-mentioned purpose, the present application provides a carbon four hydrogenation catalyst regeneration system, which comprises a regeneration gas in-out heat exchanger, a regeneration gas electric heater, a carbon four hydrogenation reactor, a nitrogen gas pipeline, a hydrogen gas pipeline, a steam pipeline, an air pipeline, a regeneration gas transfer joint, a regeneration tail gas transfer joint, a first tail gas discharge pipeline and a waste stream treatment subsystem.

[0007] The upstream joint of the regeneration gas transfer joint is divided into two routes, and the hydrogen gas pipeline is connected to one of the upstream joints of the regeneration gas transfer joint; the air pipeline and the steam pipeline are combined and then connected to the other upstream joint of the regeneration gas transfer joint.

[0008] The downstream joint of the regeneration gas transfer joint is connected to the regeneration gas inlet of the regeneration gas in-out heat exchanger through a downstream pipeline, and the nitrogen gas pipeline is combined to the downstream pipeline.

[0009] The regeneration gas outlet of the regeneration gas in-out heat exchanger, the regeneration gas electric heater, the carbon four hydrogenation reactor and the regeneration tail gas inlet of the regeneration gas in-out heat exchanger are sequentially connected.

[0010] The regeneration tail gas outlet of the regeneration gas in-out heat exchanger is connected to the upstream joint of the regeneration tail gas transfer joint; the downstream joint of the regeneration tail gas transfer joint is divided into two routes, one of which is connected to the waste stream treatment subsystem, and the other of which is connected to the first tail gas discharge pipeline.

[0011] The waste stream treatment subsystem is provided with a second tail gas discharge pipeline; tail gas analyzers are arranged on the first tail gas discharge pipeline and the second tail gas discharge pipeline.

[0012] According to the present application, preferably, the waste stream treatment subsystem is further provided with a regeneration gas cooler and a regeneration gas separator tank, and optionally an activated carbon adsorption tank.

[0013] One of the downstream joints of the regeneration tail gas transfer joint is sequentially connected to the regeneration gas cooler and the regeneration gas separator tank.

[0014] The regeneration gas separation tank comprises a waste water outlet and a gas phase tail gas outlet; the waste water outlet is connected to a waste water discharge device; the gas phase tail gas outlet is connected to a incinerator through the second tail gas discharge pipeline, and / or connected to the bottom of the activated carbon adsorption tank, and the top of the activated carbon adsorption tank is connected to the outside atmosphere.

[0015] According to the present application, preferably, the first tail gas discharge pipeline is connected to a flare system.

[0016] According to the present application, preferably, the catalyst is at least one of a nickel-based catalyst, a palladium-based catalyst and a copper-based catalyst.

[0017] According to the present application, preferably, the C4 is at least one of unsaturated C4 light hydrocarbon, refinery C4, oilfield C4, ethylene by-product C4 of refining and chemical industry and butadiene device by-product C4 alkene tail gas.

[0018] In the present application, the waste water discharge device is a sewage pool or a sewage treatment plant.

[0019] The second aspect of the present application provides a C4 hydrogenation catalyst regeneration method, which uses the C4 hydrogenation catalyst regeneration system, and comprises the following steps:

[0020] S1: nitrogen is sequentially heated by the regeneration gas in-out heat exchanger and the regeneration gas electric heater, and then enters the C4 hydrogenation reactor as feed, so that the catalyst bed in the C4 hydrogenation reactor is warmed to a first temperature threshold; the hydrocarbon concentration is monitored by a tail gas analyzer arranged on the second tail gas discharge pipeline, and when the hydrocarbon concentration is less than a hydrocarbon concentration threshold, the nitrogen stops entering the system;

[0021] S2: steam is sequentially heated by the regeneration gas in-out heat exchanger and the regeneration gas electric heater, and then enters the C4 hydrogenation reactor as feed, so that the catalyst bed is warmed to a second temperature threshold;

[0022] S3: the first steam-air mixture is sequentially heated by the regeneration gas in-out heat exchanger and the regeneration gas electric heater, and then enters the C4 hydrogenation reactor as feed, so that the catalyst bed is warmed to a third temperature threshold;

[0023] S4: when the catalyst bed in step S3 has no temperature rise, the second steam-air mixture is sequentially heated by the regeneration gas in-out heat exchanger and the regeneration gas electric heater, and then enters the C4 hydrogenation reactor as feed, so that the catalyst bed is further warmed but not more than the third temperature threshold;

[0024] S5: When the catalyst bed in step S4 has no temperature rise, the third steam-air mixture is heated by the regeneration gas in-out heat exchanger and the regeneration gas electric heater in turn, and then enters the carbon four hydrogenation reactor as feed, and the catalyst bed is coked but the temperature does not exceed the third temperature threshold value;

[0025] S6: The CO2 concentration is monitored by the tail gas analyzer arranged on the second tail gas discharge pipeline. When the CO2 concentration is less than the CO2 concentration threshold value and the catalyst bed in step S5 has no temperature rise, the regeneration reaction is completed.

[0026] According to the present application, preferably, the regeneration tail gas in steps S1-S5 is discharged from the system by the waste stream treatment subsystem; further preferably, the regeneration tail gas in steps S1-S5 is cooled by the regeneration gas in-out heat exchanger and the regeneration gas cooler in turn, and then enters the regeneration gas separation tank, waste water and gas phase tail gas are obtained at the bottom of the regeneration gas separation tank, the waste water is discharged to the waste water discharge device, the gas phase tail gas is discharged to the incinerator, and / or is discharged to the atmosphere after being adsorbed by the activated carbon adsorption tank.

[0027] According to the present application, preferably:

[0028] The temperature rise speed of the regeneration gas electric heater is 25-35℃ / hour;

[0029] The first temperature threshold value is 100-140℃;

[0030] The second temperature threshold value is 340-360℃;

[0031] The third temperature threshold value is 410-450℃;

[0032] The hydrocarbon concentration threshold value is less than or equal to 0.1wt%;

[0033] The CO2 concentration threshold value is less than or equal to 0.3wt%;

[0034] The amount of steam in step S2 is 450-550kg / m 3 Catalyst / h, and the operating pressure in the carbon four hydrogenation reactor in step S2 is 0.1-1.0MPaG;

[0035] In step S3, when the temperature of the catalyst bed rises to exceed the third temperature threshold value: the first steam-air mixture stops entering the system, and when the temperature of the catalyst bed drops below the third temperature threshold value, the first steam-air mixture enters the system again;

[0036] the air content in the first steam-air mixture is 0.8-1.2wt%, and the steam content is 98.8-99.2wt% based on the total weight of the first steam-air mixture;

[0037] the air content in the second steam-air mixture is 4.5-5.5wt%, and the steam content is 94.5-95.5wt% based on the total weight of the second steam-air mixture;

[0038] the air content in the third steam-air mixture is 8-12wt%, and the steam content is 88-92wt% based on the total weight of the third steam-air mixture;

[0039] the time for the steps S3-S5 is 12-48h.

[0040] The third aspect of the present application provides a regeneration method of a carbon four hydrogenation catalyst, which uses the regeneration system of the carbon four hydrogenation catalyst, and comprises the following steps:

[0041] (1) the nitrogen-hydrogen mixture is sequentially heated by the regeneration gas in-out heat exchanger and the regeneration gas electric heater, and then enters the carbon four hydrogenation reactor as feed, so that the inlet temperature of the carbon four hydrogenation reactor is raised to the fourth temperature threshold value, the outlet temperature reaches the fifth temperature threshold value, and the temperature is kept constant for a first preset time period;

[0042] (2) the feed temperature is adjusted, the catalyst bed in the carbon four hydrogenation reactor is heated to the sixth temperature threshold value, and the temperature is kept constant for a second preset time period;

[0043] (3) the hydrocarbon concentration is monitored by the tail gas analyzer arranged on the first tail gas discharge pipeline, and when the hydrocarbon concentration is less than the hydrocarbon concentration threshold value, the regeneration reaction is ended.

[0044] According to the present application, preferably:

[0045] the temperature rising speed of the regeneration gas electric heater is 25-35℃ / h;

[0046] the fourth temperature threshold value is 220-240℃;

[0047] the fifth temperature threshold value is 190-210℃;

[0048] the sixth temperature threshold value is 100-450℃;

[0049] the hydrocarbon concentration threshold value is less than or equal to 0.1wt%;

[0050] the total amount of the nitrogen-hydrogen mixture is 450-550kg / m 3Catalyst / h, wherein the hydrogen is used in an amount of 190-210 kg / m 3 Catalyst / h;

[0051] The operating pressure in the carbon four hydrogenation reactor is 0.1-1.0 MPaG;

[0052] The first preset time period is 7.5-8.5 h;

[0053] The second preset time period is 12-48 h.

[0054] The beneficial effects of the technical solution of the present application are as follows:

[0055] 1) The regeneration system of the present application is highly adaptable, and can be simultaneously applied to the regeneration of both noble metal palladium-based and non-noble metal nickel-based and copper-based catalysts for carbon four unsaturated fraction hydrogenation reaction.

[0056] 2) The present application can perform two catalyst regeneration modes of hot hydrogen stripping and coking regeneration according to the heavy component content of carbon four raw materials and the coking degree of carbon four hydrogenation catalyst.

[0057] 3) The present application can save energy consumption by more than 15% by reasonably setting the regeneration gas in-out heat exchanger.

[0058] 4) The regeneration tail gas of the present application can be discharged to a flue incinerator or discharged to the atmosphere through an activated carbon adsorption tank, and the waste gas discharge meets the environmental protection requirements, and can be flexibly selected according to the actual situation of the factory.

[0059] 5) The present application reasonably determines the regeneration end time through tail gas analysis by a tail gas analyzer.

[0060] 6) The coking regeneration working condition process of the present application adopts the steam, air coking mode after nitrogen preheating, which effectively protects the catalyst activity and avoids causing economic losses.

[0061] 7) The present application realizes the intrinsic safety switching of two regeneration working conditions by setting the regeneration gas adapter and the regeneration tail gas adapter.

[0062] Other features and advantages of the present application will be described in detail in the subsequent specific embodiments. BRIEF DESCRIPTION OF DRAWINGS

[0063] The above and other objects, features and advantages of the present application will become more apparent from the following detailed description when taken in conjunction with the accompanying drawings in which similar reference characters refer to similar features throughout the several views.

[0064] Figure 1 A structure schematic diagram of a carbon four hydrogenation catalyst regeneration system provided by embodiment 1 of the present application is shown.

[0065] Figure 2 A part of the structure of the system of Example 1 used in a carbon four hydrogenation catalyst regeneration method provided by the embodiment 2 of the present application is shown.

[0066] Figure 3 A part of the structure of the system of Example 1 used in a carbon four hydrogenation catalyst regeneration method provided by the embodiment 3 of the present application is shown.

[0067] The reference signs are explained as follows:

[0068] 1 - Regeneration gas in-out heat exchanger; 2 - Regeneration gas electric heater; 3 - Carbon four hydrogenation reactor; 4 - Regeneration gas cooler; 5 - Regeneration gas liquid separator; 6 - Activated carbon adsorption tank; 7 - Regeneration gas transfer joint; 8 - Regeneration tail gas transfer joint; 9 - Tail gas analyzer; 10 - Nitrogen pipeline; 11 - Hydrogen pipeline; 12 - Steam pipeline; 13 - Air pipeline; 14 - Cooling water pipeline; 15 - External atmospheric environment; 16 - Incinerator; 17 - Waste water discharge equipment; 18 - Flare system; 19 - First tail gas discharge pipeline; 20 - Second tail gas discharge pipeline. DETAILED DESCRIPTION

[0069] The preferred embodiments of the present application will be described in more detail below. Although the preferred embodiments of the present application are described below, it is understood that the present application can be implemented in various forms and should not be limited by the embodiments set forth herein. Rather, these embodiments are provided so that the present application will be thorough and complete, and will fully convey the scope of the present application to those skilled in the art.

[0070] Example 1

[0071] The present embodiment provides a carbon four hydrogenation catalyst regeneration system, as shown in the figure, which comprises: a regeneration gas in-out heat exchanger 1, a regeneration gas electric heater 2, a carbon four hydrogenation reactor 3, a nitrogen pipeline 10, a hydrogen pipeline 11, a steam pipeline 12, an air pipeline 13, a regeneration gas transfer joint 7, a regeneration tail gas transfer joint 8, a first tail gas discharge pipeline 19, and a waste stream processing subsystem. Figure 1 The upstream joint of the regeneration gas transfer joint 7 is divided into two routes, and the hydrogen pipeline 11 is connected to one of the upstream joints of the regeneration gas transfer joint 7; the air pipeline 13 is combined with the steam pipeline 12 and then connected to the other upstream joint of the regeneration gas transfer joint 7;

[0072] The downstream joint of the regeneration gas transfer joint 7 is connected to the regeneration gas inlet of the regeneration gas in-out heat exchanger 1 through a downstream pipeline, and the nitrogen pipeline 10 is combined with the downstream pipeline;

[0073]

[0074] ​The regenerated gas outlet of the regenerated gas inlet and outlet heat exchanger 1, the regenerated gas electric heater 2, the carbon four hydrogenation reactor 3 and the regenerated tail gas inlet of the regenerated gas inlet and outlet heat exchanger 1 are connected in sequence.

[0075] The regenerated tail gas outlet of the regenerated gas inlet and outlet heat exchanger 1 is connected to the upstream joint of the regenerated tail gas adapter 8; the downstream joint of the regenerated tail gas adapter 8 is divided into two routes, one of which is connected to the waste stream treatment subsystem, and the other of which is connected to the first tail gas discharge pipeline 19; wherein the second tail gas discharge pipeline 20, the regenerated gas cooler 4 and the regenerated gas liquid-liquid separator 5, and the activated carbon adsorption tank 6 are arranged in the waste stream treatment subsystem; the downstream joint of one of the regenerated tail gas adapter 8 is connected to the regenerated gas cooler 4 and the regenerated gas liquid-liquid separator 5 in sequence.

[0076] The regenerated gas liquid-liquid separator 5 includes a waste water outlet and a gas phase tail gas outlet; the waste water outlet is connected to the waste water discharge device 17; the gas phase tail gas outlet is connected to the incinerator 16 and the bottom of the activated carbon adsorption tank 6 through the second tail gas discharge pipeline 20, and the top of the activated carbon adsorption tank 6 is connected to the external atmosphere 15.

[0077] The first tail gas discharge pipeline 19 is connected to the flare system 18.

[0078] The tail gas analyzer 9 is arranged on the first tail gas discharge pipeline 19 and the second tail gas discharge pipeline 20.

[0079] Example 2

[0080] The present embodiment provides a carbon four hydrogenation catalyst regeneration method, the carbon four is a by-product carbon four alkyne tail gas of a butadiene device, and the catalyst is a palladium-based catalyst, such as Figure 2 As shown, the coke-burning regeneration part device in the carbon four hydrogenation catalyst regeneration system of Example 1 is used, including the following steps:

[0081] S1: nitrogen is sequentially heated by the regenerated gas inlet and outlet heat exchanger and the regenerated gas electric heater, and then enters the carbon four hydrogenation reactor as feed, so that the catalyst bed in the carbon four hydrogenation reactor is warmed to a first temperature threshold value 120℃; the hydrocarbon concentration is monitored by the tail gas analyzer arranged on the second tail gas discharge pipeline, and when the hydrocarbon concentration is less than a hydrocarbon concentration threshold value 0.1wt%, the nitrogen stops entering the system;

[0082] S2: steam is sequentially heated by the regenerated gas inlet and outlet heat exchanger and the regenerated gas electric heater, and then enters the carbon four hydrogenation reactor as feed, so that the catalyst bed is warmed to a second temperature threshold value 350℃, and the operating pressure in the carbon four hydrogenation reactor is 0.3MPaG; 3 Catalyst / h is sequentially heated by the regenerated gas inlet and outlet heat exchanger and the regenerated gas electric heater, and then enters the carbon four hydrogenation reactor as feed, so that the catalyst bed is warmed to a second temperature threshold value 350℃, and the operating pressure in the carbon four hydrogenation reactor is 0.3MPaG;

[0083] S3: After the first steam-air mixture is sequentially heated by the regenerator inlet-outlet heat exchanger and the regenerator electric heater, the first steam-air mixture enters the C4 hydrocracking reactor as feed, and the catalyst bed is heated to a temperature not exceeding a third temperature threshold of 420°C;

[0084] The air content in the first steam-air mixture is 1 wt%, and the steam content is 99 wt%, based on the total weight of the first steam-air mixture;

[0085] When the catalyst bed is heated to exceed the third temperature threshold of 420°C: the first steam-air mixture stops entering the system, and when the temperature of the catalyst bed drops below the third temperature threshold, the first steam-air mixture enters the system again;

[0086] S4: After the catalyst bed in step S3 is not heated, the second steam-air mixture is sequentially heated by the regenerator inlet-outlet heat exchanger and the regenerator electric heater, and then enters the C4 hydrocracking reactor as feed, and the catalyst bed is further heated but not exceeding the third temperature threshold of 420°C;

[0087] The air content in the second steam-air mixture is 5 wt%, and the steam content is 95 wt%, based on the total weight of the second steam-air mixture;

[0088] S5: After the catalyst bed in step S4 is not heated, the third steam-air mixture is sequentially heated by the regenerator inlet-outlet heat exchanger and the regenerator electric heater, and then enters the C4 hydrocracking reactor as feed, and the catalyst bed is coked but the temperature does not exceed the third temperature threshold of 420°C;

[0089] The air content in the third steam-air mixture is 10 wt%, and the steam content is 90 wt%, based on the total weight of the third steam-air mixture;

[0090] The time for steps S3-S5 is 16 hours;

[0091] S6: The CO2 concentration is monitored by a tail gas analyzer arranged on the second tail gas discharge pipeline, and when the CO2 concentration is less than a CO2 concentration threshold of 0.3 wt% and the catalyst bed in step S5 is not heated, the regeneration reaction is completed;

[0092] Wherein: the regeneration tail gas in steps S1-S5 is sequentially heated by the regenerator inlet-outlet heat exchanger and the regenerator cooler, and then enters the regenerator liquid separation tank, waste water and gas phase tail gas are obtained at the bottom of the regenerator liquid separation tank, the waste water is discharged to a sewage treatment plant, and the gas phase tail gas is discharged to the atmosphere after being adsorbed by the activated carbon adsorption tank.

[0093] The temperature rising speed of the electric heater is 30℃ / hour.

[0094] Example 3

[0095] The present example provides a method for regenerating a carbon four hydrogenation catalyst, the carbon four being a byproduct of a butadiene device, and the catalyst being a nickel-based catalyst, such as Figure 3 As shown, the hot hydrogen stripping part of the carbon four hydrogenation catalyst regeneration system of Example 1 is used, including the following steps:

[0096] (1) The nitrogen-hydrogen mixture at 500kg / m 3 catalyst / h (wherein the hydrogen is used in an amount of 200kg / m 3 catalyst / h) is sequentially heated by the regeneration gas in-out heat exchanger and the regeneration gas electric heater, and then fed into the carbon four hydrogenation reactor, so that the inlet temperature of the carbon four hydrogenation reactor is raised to the fourth temperature threshold value 230℃, the outlet temperature reaches the fifth temperature threshold value 200℃, and the temperature is kept constant for 8 hours, and the operating pressure in the carbon four hydrogenation reactor is 0.3MPaG;

[0097] (2) The temperature of the feed is adjusted, and the catalyst bed in the carbon four hydrogenation reactor is raised to the sixth temperature threshold value 350℃, and the temperature is kept constant for 24 hours;

[0098] (3) The hydrocarbon concentration is monitored by the tail gas analyzer arranged on the first tail gas discharge pipeline, and when the hydrocarbon concentration is less than the hydrocarbon concentration threshold value 0.1wt%, the regeneration reaction is completed.

[0099] The temperature rising speed of the electric heater is 30℃ / hour.

[0100] The above has described various embodiments of the present application, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and changes are obvious to those skilled in the art without departing from the scope and spirit of the described embodiments.

Claims

1. A method for regenerating a C4 hydrogenation catalyst, characterized in that, The C4 hydrogenation catalyst regeneration system used in this method includes: a regeneration gas inlet and outlet heat exchanger, a regeneration gas electric heater, a C4 hydrogenation reactor, a nitrogen pipeline, a hydrogen pipeline, a steam pipeline, an air pipeline, a regeneration gas adapter, a regeneration tail gas adapter, a first tail gas emission pipeline, and a waste logistics treatment subsystem. The upstream connector of the regeneration gas adapter is divided into two lines. The hydrogen pipeline is connected to one upstream connector of the regeneration gas adapter. The air pipeline and the steam pipeline are merged and then connected to the other upstream connector of the regeneration gas adapter. The downstream connector of the regenerated gas adapter is connected to the regenerated gas inlet of the regenerated gas heat exchanger via a downstream pipeline, and the nitrogen pipeline is merged into the downstream pipeline. The regenerated gas outlet of the regenerated gas inlet and outlet heat exchanger, the regenerated gas electric heater, the C4 hydrogenation reactor, and the regenerated tail gas inlet of the regenerated gas inlet and outlet heat exchanger are connected in sequence. The regenerated exhaust gas outlet of the heat exchanger is connected to the upstream connector of the regenerated exhaust gas adapter; the downstream connector of the regenerated exhaust gas adapter is divided into two paths, one of which is connected to the waste logistics treatment subsystem and the other of which is connected to the first exhaust gas emission pipeline. The waste logistics treatment subsystem is equipped with a second exhaust gas emission pipeline; both the first exhaust gas emission pipeline and the second exhaust gas emission pipeline are equipped with exhaust gas analyzers. The regeneration method is hot hydrogen stripping regeneration, which includes the following steps: (1) The nitrogen-hydrogen mixture is heated by the regenerated gas inlet and outlet heat exchanger and the regenerated gas electric heater in sequence, and then enters the C4 hydrogenation reactor as feed, so that the inlet temperature of the C4 hydrogenation reactor is raised to the fourth temperature threshold and the outlet temperature reaches the fifth temperature threshold, and is kept constant for a first preset time period. (2) Adjust the feed temperature to raise the catalyst bed in the C4 hydrogenation reactor to the sixth temperature threshold and keep it constant for a second preset time period; (3) The hydrocarbon concentration is monitored by the exhaust gas analyzer installed on the first exhaust gas emission pipeline. When the hydrocarbon concentration is less than the hydrocarbon concentration threshold, the regeneration reaction ends. The fourth temperature threshold is 220-240℃; The fifth temperature threshold is 190-210℃; The sixth temperature threshold is 350-450℃; The total amount of the nitrogen-hydrogen mixture used is 450-550 kg / m³. 3 Catalyst / h, wherein the amount of hydrogen used is 190-210 kg / m³. 3 catalyst / h; The operating pressure inside the C4 hydrogenation reactor is 0.1-1.0 MPaG; The first preset time period is 7.5-8.5 hours; The second preset time period is 12-48 hours; The catalyst is at least one of nickel-based catalysts, palladium-based catalysts, and copper-based catalysts; C4 is an unsaturated light hydrocarbon.

2. The method for regenerating the C4 hydrogenation catalyst according to claim 1, wherein, Alternatively, the regeneration method is coke burning regeneration, which includes the following steps: S1: Nitrogen gas is successively heated by the regenerated gas inlet and outlet heat exchanger and the regenerated gas electric heater, and then enters the C4 hydrogenation reactor as feed, so that the catalyst bed in the C4 hydrogenation reactor is heated to the first temperature threshold. The hydrocarbon concentration is monitored by the tail gas analyzer installed on the second tail gas emission pipeline. When the hydrocarbon concentration is less than the hydrocarbon concentration threshold, nitrogen gas stops entering the system. S2: After the steam is successively heated by the regenerated gas inlet and outlet heat exchanger and the regenerated gas electric heater, it enters the C4 hydrogenation reactor as feed and raises the temperature of the catalyst bed to the second temperature threshold. The second temperature threshold is 340-360℃; The amount of steam used in step S2 is 450-550 kg / m³. 3 Catalyst / h, the operating pressure in the C4 hydrogenation reactor in step S2 is 0.1-1.0 MPaG; S3: The first steam-air mixture is successively heated by the regenerated gas inlet and outlet heat exchanger and the regenerated gas electric heater, and then enters the C4 hydrogenation reactor as feed, thereby raising the temperature of the catalyst bed to no more than the third temperature threshold. S4: When the catalyst bed in step S3 has no temperature rise, the second steam-air mixture is fed into the C4 hydrogenation reactor after being heated by the regeneration gas inlet and outlet heat exchanger and the regeneration gas electric heater in sequence, and the catalyst bed is further heated but not exceeding the third temperature threshold. S5: When the catalyst bed in step S4 has no temperature rise, the third steam-air mixture is fed into the C4 hydrogenation reactor after being heated by the regeneration gas inlet and outlet heat exchanger and the regeneration gas electric heater in sequence, and the catalyst bed is charred but the temperature does not exceed the third temperature threshold. S6: The CO2 concentration is monitored by the exhaust gas analyzer installed on the second exhaust gas emission pipeline. When the CO2 concentration is less than the CO2 concentration threshold and there is no temperature rise in the catalyst bed in step S5, the regeneration reaction ends. The third temperature threshold is 410-450℃; Based on the total weight of the first steam-air mixture, the air content in the first steam-air mixture is 0.8-1.2 wt%, and the steam content is 98.8-99.2 wt%. Based on the total weight of the second steam-air mixture, the air content in the second steam-air mixture is 4.5-5.5 wt%, and the steam content is 94.5-95.5 wt%. Based on the total weight of the third steam-air mixture, the air content in the third steam-air mixture is 8-12 wt%, and the steam content is 88-92 wt%.

3. The method for regenerating a C4 hydrogenation catalyst according to claim 1, wherein, The waste logistics treatment subsystem is also equipped with a regenerated gas cooler and a regenerated gas separator, as well as, optionally, an activated carbon adsorption tank. One downstream connector of the regenerated exhaust gas adapter is sequentially connected to the regenerated gas cooler and the regenerated gas separator. The regenerated gas separator includes a wastewater outlet and a gas phase tail gas outlet; the wastewater outlet is connected to a wastewater discharge device; the gas phase tail gas outlet is connected to an incinerator through a second tail gas discharge pipeline, and / or connected to the bottom of the activated carbon adsorption tank, and the top of the activated carbon adsorption tank is connected to the external atmospheric environment.

4. The method for regenerating a C4 hydrogenation catalyst according to claim 1, wherein, The first exhaust gas pipeline is connected to the flare system.

5. The method for regenerating a C4 hydrogenation catalyst according to claim 1, wherein, The C4 is at least one of the following: oilfield C4, C4 by-product from ethylene production in the refining and chemical industry, and C4 alkyne tail gas by-product from butadiene plants.

6. The method for regenerating a C4 hydrogenation catalyst according to claim 2, wherein, The regenerated exhaust gas from steps S1-S5 is discharged from the system through the waste logistics treatment subsystem.

7. The method for regenerating a C4 hydrogenation catalyst according to claim 6, wherein, The regeneration tail gas from steps S1-S5 is cooled sequentially by the regeneration gas inlet / outlet heat exchanger and the regeneration gas cooler, and then enters the regeneration gas separator. Wastewater and gaseous tail gas are obtained at the bottom of the regeneration gas separator. The wastewater is discharged to the wastewater discharge equipment, and the gaseous tail gas is discharged to the incinerator, and / or, after being adsorbed by the activated carbon adsorption tank, it is discharged into the atmosphere.

8. The method for regenerating a C4 hydrogenation catalyst according to claim 2, wherein, In the coke recycling method: The heating rate of the regenerated gas electric heater is 25-35℃ / hour; The first temperature threshold is 100-140℃; The hydrocarbon concentration threshold is less than or equal to 0.1 wt%; The CO2 concentration threshold is less than or equal to 0.3 wt%; In step S3, when the catalyst bed temperature rises above the third temperature threshold: the first steam-air mixture stops entering the system, and when the catalyst bed temperature drops below the third temperature threshold, the first steam-air mixture re-enters the system; The time required for steps S3-S5 is 12-48 hours.

9. The method for regenerating a C4 hydrogenation catalyst according to claim 1, wherein, In the hot hydrogen stripping process: The heating rate of the regenerated gas electric heater is 25-35℃ / hour; The hydrocarbon concentration threshold is less than or equal to 0.1 wt%.

Images