CN110396425B

CN110396425B - Device and method for micro-interface reinforced liquid-phase circulating hydrogenation

Info

Publication number: CN110396425B
Application number: CN201910768245.1A
Authority: CN
Inventors: 陈强; 蔡连波; 李治; 盛维武; 李小婷; 赵晓青; 刘茂增; 陈险峰
Original assignee: China Petroleum and Chemical Corp; Sinopec Engineering Group Co Ltd
Current assignee: China Petroleum and Chemical Corp; Sinopec Engineering Group Co Ltd
Priority date: 2019-08-20
Filing date: 2019-08-20
Publication date: 2021-08-31
Anticipated expiration: 2039-08-20
Also published as: CN110396425A

Abstract

The invention relates to the technical field of petroleum refining and petrochemical industry, in particular to a device and a method for micro-interface reinforced liquid phase circulating hydrogenation. The device comprises: the device comprises a raw material tank, a heating furnace, a micro-bubble generator, a hydrogenation unit, a hydrogenation reactor and a separator; the discharge end of the raw material tank is connected to the microbubble generator through a heating furnace, and the hydrogenation unit is connected to the microbubble generator; the discharge end of the microbubble generator is connected to the hydrogenation reactor, and the discharge end of the hydrogenation reactor is connected to the separator. The method comprises the following steps: carrying out hydrogenation reaction on the micro-bubble flow in a hydrogenation reactor, and collecting a hydrogenation product through a separator; the microbubble flow is mainly obtained by gas-liquid mixing of preheated raw oil and hydrogen in a microbubble generator. The invention can greatly improve the space utilization rate of the reactor by about 10-20%; meanwhile, the pressure in the device system can be reduced, and the device cost is greatly reduced.

Description

Device and method for micro-interface reinforced liquid-phase circulating hydrogenation

Technical Field

The invention relates to the technical field of petroleum refining and petrochemical industry, in particular to a device and a method for micro-interface reinforced liquid phase circulating hydrogenation.

Background

At present, the deep hydrofining of aviation kerosene and diesel oil mainly adopts the process technology of hydrogen circulation and liquid phase circulation, and also has a tubular liquid phase hydrogenation process.

When a conventional trickle-bed reactor with hydrogen recycle is operated, the excess recycle hydrogen is 10 times the amount of hydrogen required for chemical consumption. The gas and the liquid are mixed and flow downwards through the inner member and the catalyst bed layer, and the gas-liquid equilibrium state is kept in the catalyst bed layer. On the surface of the catalyst, chemical reaction occurs between the dissolved hydrogen and the reactant in the feed, and the hydrogen in the liquid phase is gradually reduced, so that the gas phase hydrogen is gradually dissolved into the liquid phase for replenishment. It can be seen from this that: the reaction rate in a conventional trickle-bed reactor is mainly influenced by the mass transfer rate, which is generally much slower than the kinetic reaction rate.

By adopting a liquid phase circulating hydrogenation technology, deep hydrogenation can be realized, and the sulfur content in the oil product can be ensured to be lower. The hydrogen flow in the whole hydrotreating process is reduced, a hydrogen circulation system and a recycle hydrogen compressor are omitted, the device construction investment of enterprises can be saved, and the production cost of clean fuel is reduced.

The current situation of liquid phase circulating hydrogenation is as follows: (1) the liquid phase hydrogenation pressure is higher than that of gas phase hydrogenation, and particularly for oil products (diesel oil or wax oil) with higher hydrogen consumption, the pressure grade of accessory facilities such as process pipelines and the like is improved, and the investment cost is not much more advantageous; (2) the hydrogen supplement among the multiple bed layers needs to arrange a plurality of gas-liquid mixers in the reactor, so that the operation is complex and the space utilization rate of the reactor is low.

In view of the above, the present invention is particularly proposed.

Disclosure of Invention

The invention aims to provide a device for micro-interface reinforced liquid-phase circulating hydrogenation, which aims to solve the technical problems of unstable operation and low space utilization rate of a reactor in the prior art.

The second purpose of the invention is to provide a method for micro-interface reinforced liquid phase circulating hydrogenation, which has good stability and high reliability.

In order to achieve the above purpose of the present invention, the following technical solutions are adopted:

the device for the liquid phase circulation hydrogenation with the strengthened micro-interface comprises: the device comprises a raw material tank, a heating furnace, a micro-bubble generator, a hydrogenation unit, a hydrogenation reactor and a separator;

the discharge end of the raw material tank is connected to the microbubble generator through a heating furnace, and the hydrogenation unit is connected to the microbubble generator; the discharge end of the microbubble generator is connected to the hydrogenation reactor, and the discharge end of the hydrogenation reactor is connected to the separator.

The device for liquid phase circulation hydrogenation is provided with the microbubble generator, hydrogen is quickly dissolved in oil in the microbubble generator, a certain amount of surplus hydrogen forms uniform microbubble flow with the oil in a large number of microbubble states, and the gas-liquid pseudo-homogeneous phase is directly brought into the hydrogenation reactor for hydrogenation reaction. The microbubble through a large amount of stable suspensions constantly supplies hydrogen to in the oil, does not only rely on the high pressure to improve the solubility of hydrogen, can suitably reduce the pressure in the device system, reduces the device cost by a wide margin, especially can make diesel oil and wax oil liquid phase circulation hydrogenation's promotion by a wide margin.

Meanwhile, the invention does not need additional hydrogen supplement and exhaust systems, so that the whole reaction process is simpler, the operation stability is better, and the reaction effect is better. And a midway hydrogen replenishing system is reduced or even cancelled in the hydrogenation reactor, so that the space utilization rate of the hydrogenation reactor is greatly improved, and the production efficiency is improved.

The relatively stable homogeneous micro-bubble flow formed by the invention enters the hydrogenation reactor to meet the basic hydrogen supply requirement, a gas-liquid mixer and an exhaust system in the existing liquid-phase circulating hydrogenation process can be eliminated or reduced, the operation of the hydrogenation reactor is more stable, the operation difficulty is reduced, and the space utilization rate is improved. Compared with a supergravity hydrogen mixing device and the like, the device has the advantages that the safety and reliability of the device are improved, meanwhile, the energy consumption is reduced, the energy utilization rate is improved, and the gas-liquid ratio can be improved.

In addition, in the micro bubble flow formed by the micro bubble generator, bubbles basically exist in a micron-scale, so that the operation process can be simplified, the system pressure is reduced, the equipment investment is saved, the use efficiency of hydrogen can be improved under lower operation pressure, and a good hydrogenation environment is provided.

In a preferred embodiment of the invention, the discharge end of the raw material tank is connected to the heating furnace by a feed pump. The feed pump can adopt a common pump or a booster pump to properly adjust the pressure of the raw oil.

Optionally, a flow regulating valve is arranged between the feeding pump and the heating furnace. Used for adjusting the quantity, the conveying speed and the like of raw oil fed into the heating furnace.

In a preferred embodiment of the invention, the heating furnace comprises at least two material tanks, a first material tank and a second material tank, wherein the first material tank is connected to the second material tank through a pump, and the discharge end of the second material tank is connected to the heating furnace through a feeding pump.

Wherein the pump between the first raw material tank and the second raw material tank is preferably a booster pump to boost the raw material oil to a suitable pressure.

Optionally, a flow regulating valve is arranged between the booster pump and the second raw material tank. For adjusting the amount and the conveying speed of the stock oil fed into the second stock tank, and the like.

The heating furnace of the invention is used for heating the raw oil, for example, the heating furnace can be heated to 320-400 ℃ to carry out reaction.

In a preferred embodiment of the present invention, the system further comprises a circulation pump, and the hydrogenation reactor is connected to the microbubble generator through the circulation pump.

After flowing out from the discharge end of the hydrogenation reactor, the reactant is divided into two streams according to conditions (the two streams are divided according to the sulfur content and the temperature of the reaction product and are separated according to the specific process condition requirements), one stream is subjected to a subsequent separator, and the other stream is returned to the microbubble generator through a circulating pump for circular hydrogenation.

Optionally, a flow regulating valve is arranged between the circulating pump and the microbubble generator. Used for adjusting the quantity, the conveying speed and the like of the oil product sent into the microbubble generator.

In one embodiment of the invention, the hydrogenation unit is a hydrogen line. The hydrogen pipeline is used for delivering fresh hydrogen to the microbubble generator.

Optionally, a flow regulating valve is arranged on the hydrogen pipeline. For adjusting the amount and delivery rate of hydrogen gas to the microbubble generator, etc.

In a specific embodiment of the present invention, the hydrogenation reactor comprises any one of a downflow reactor and an upflow reactor. The method can be selected in the conventional hydrogenation reactor according to actual requirements, and a hydrogen supplement unit does not need to be arranged in the hydrogenation reactor, so that the space utilization rate of the reactor is greatly improved.

Quasi-homogeneous gas-liquid mixture output by the micro-bubble generator is immersed in a hydrogenation reactor and contacted with a catalyst to form gas, solid and liquid phases, wherein the liquid phase is a continuous phase, and the gas phase is a micron-sized uniform dispersion phase, so that efficient hydrogenation reaction is carried out; once the amount of hydrogen in the liquid phase gradually decreases as the reaction proceeds, micron-sized bubbles are rapidly dissolved in the liquid phase, and the hydrogen in the liquid phase is always in a dynamic saturated state.

In a specific embodiment of the present invention, a microbubble flow distributor may be disposed in the hydrogenation reactor, and the microbubble flow distributor is connected to the microbubble generator. As said micro bubble flow distributor may be positioned between catalyst beds of said hydrogenation reactor, preferably between the first catalyst bed.

In actual operation, if hydrogen is needed to be supplemented midway, the micro bubble flow meeting the temperature condition can be directly injected into the hydrogenation reactor through the micro bubble flow distributor in the hydrogenation reactor.

The structure of the micro-bubble flow distributor is the same as that of the gas distributor, and the difference is that the micro-bubble flow distributor is used for injecting micro-bubble flow into the hydrogenation reactor.

In an embodiment of the present invention, the microbubble generator may be a swirl-type microbubble generator. Raw oil rotates at a high speed in the hollow shaft, low pressure is formed at the hollow shaft, hydrogen is pumped, and under the effect of the rotational flow in the micro-bubble generator, the hydrogen is torn and divided into a large number of bubbles by the high-speed liquid phase material. On one hand, hydrogen is quickly dissolved into raw oil, and on the other hand, the surplus hydrogen forms pseudo-homogeneous gas-liquid mixture flow with oil products in a micron-sized bubble form.

In a preferred embodiment of the present invention, the micro-bubble generator comprises two or more micro-bubble generators, and each of the micro-bubble generators is connected in series or in parallel. Each of the microbubble generators may be connected to the hydrogenation reactor, the heating furnace, and the circulation pump.

In practical operation, if a plurality of microbubble generators are included, the amount of gas liquid and the gas-liquid ratio in each microbubble generator may be the same or different.

In one embodiment of the invention, the separator is a hot low pressure separator.

Preferably, a back pressure valve is arranged between the hydrogenation reactor and the separator. For adjusting the flow of oil, etc.

The invention also provides a micro-interface reinforced liquid phase circulating hydrogenation method, which comprises the following steps:

carrying out hydrogenation reaction on the micro-bubble flow in a hydrogenation reactor, and collecting a hydrogenation product through a separator;

the microbubble flow is mainly obtained by gas-liquid mixing of preheated raw oil and hydrogen in a microbubble generator.

Optionally, the temperature of the preheated raw oil is 320-400 ℃.

Optionally, the conditions for mixing gas and liquid in the microbubble generator are as follows: the temperature is 100-380 deg.C and the pressure is 2-10 MPa. Wherein the temperature is preferably 120 ℃ to 320 ℃, and the pressure is 2-9 MPa.

Optionally, in a standard state, the gas-liquid ratio in the microbubble generator is 1: 1-80: 1.

Optionally, the obtained circulating oil obtained by the reactor is sent to a microbubble generator for a circulating hydrogenation reaction.

Optionally, the volume ratio of the circulating oil to the raw oil is 1: 1-10: 1.

In practice, the raw oil comprises any one or more of aviation kerosene, diesel oil and wax oil.

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

(1) in the device, hydrogen supplement units can be reduced or even cancelled, the space utilization rate of the reactor is greatly improved by about 10-20%; meanwhile, the whole device runs more stably, linkage among multiple bed layers does not exist, and the reaction effect is better;

(2) in the microbubble generator, hydrogen is quickly dissolved in an oil product, a certain amount of surplus hydrogen forms uniform microbubble flow with the oil product in a large number of microbubble states, the hydrogen is continuously supplemented into the oil product through a large number of stably suspended microbubbles, the solubility of the hydrogen is improved by only depending on high pressure, the pressure in a device system can be properly reduced, the cost of the device is greatly reduced, and particularly, the economic benefit of liquid-phase cyclic hydrogenation of diesel oil and wax oil is greatly improved;

(3) in the circulating hydrogenation method, the system pressure is relatively low, and the system stability and safety are better.

Drawings

In order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, and it is obvious that the drawings in the following description are some embodiments of the present invention, and other drawings can be obtained by those skilled in the art without creative efforts.

FIG. 1 is a schematic structural diagram of a micro-interface enhanced liquid-phase circulating hydrogenation apparatus according to an embodiment of the present invention;

fig. 2 is a schematic structural diagram of a micro-interface enhanced liquid-phase circulating hydrogenation apparatus according to another embodiment of the present invention.

Reference numerals:

1-a first feedstock tank; 2, a booster pump; 3-a second feed tank;

4-a feed pump; 5, heating a furnace; 6-circulating pump;

7-a hydrogen line; 8-a microbubble generator; 9-a hydrogenation reactor;

10-a separator; 11-micro bubble flow distributor.

Detailed Description

The technical solutions of the present invention will be clearly and completely described below with reference to the accompanying drawings and the detailed description, but those skilled in the art will understand that the following described embodiments are some, not all, of the embodiments of the present invention, and are only used for illustrating the present invention, and should not be construed as limiting the scope of the present invention. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention. The examples, in which specific conditions are not specified, were conducted under conventional conditions or conditions recommended by the manufacturer. The reagents or instruments used are not indicated by the manufacturer, and are all conventional products available commercially.

In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicate orientations or positional relationships based on the orientations or positional relationships shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the device or element being referred to must have a particular orientation, be constructed and operated in a particular orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.

In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.

Fig. 1 is a schematic structural diagram of a micro-interface enhanced liquid-phase circulating hydrogenation apparatus according to an embodiment of the present invention. The micro-interface enhanced liquid-phase circulating hydrogenation apparatus provided by the embodiment comprises a raw material tank, a heating furnace 5, a micro-bubble generator 8, a hydrogenation unit, a hydrogenation reactor 9 and a separator 10. The discharge end of the raw material tank is connected to the microbubble generator 8 through a heating furnace 5, and the hydrogenation unit is connected to the microbubble generator 8; the discharge end of the microbubble generator 8 is connected to the hydrogenation reactor 9, and the discharge end of the hydrogenation reactor 9 is connected to the separator 10.

In particular, the hydrogenation unit may be a hydrogen line 7. The hydrogen line 7 is used to deliver fresh hydrogen gas to the microbubble generator 8. Further, a flow regulating valve is provided on the hydrogen line 7 for regulating the amount and the delivery rate of the hydrogen gas fed into the microbubble generator 8. The pressure of the hydrogen in the hydrogen line 7 can be adjusted according to the actual demand.

It can be understood that the hydrogenation reactor 9 may be any one of a downflow reactor or an upflow reactor, and is not limited thereto, and may be selected from conventional hydrogenation reactors according to actual needs, and a hydrogen supplement unit may not be required to be arranged in the hydrogenation reactor, so that the space utilization rate of the reactor is greatly improved.

Alternatively, the apparatus comprises more than one feedstock tank, and may for example comprise two feedstock tanks, a first feedstock tank 1 and a second feedstock tank 3.

Specifically, the first raw material tank 1 is connected to the second raw material tank 3 through a pump, and the discharge end of the second raw material tank 3 is connected to the heating furnace 5 through a feed pump 4.

Optionally, the first material tank 1 is connected to the second material tank 3 by a booster pump 2. After the fresh raw oil is uniformly mixed in the first raw material tank 1, the raw oil is increased to a proper pressure by a booster pump 2 and then is sent into a second raw material tank 3.

Further, a flow rate adjusting valve is provided between the booster pump 2 and the second raw material tank 3 to adjust the amount and the conveying speed of the raw material oil fed into the second raw material tank 3.

It is understood that the feed pump 4 may be a general pump or a booster pump to appropriately adjust the pressure of the feed oil.

Optionally, a flow regulating valve is arranged between the feed pump 4 and the heating furnace 5, and is used for regulating the amount of raw oil sent into the heating furnace 5 and the speed of the conveying pipe.

Optionally, the apparatus further includes a circulation pump 6, and a discharge end of the hydrogenation reactor 9 is connected to the microbubble generator 8 through the circulation pump 6. Further, a flow regulating valve is arranged between the circulating pump 6 and the microbubble generator 8 and used for regulating the amount, conveying speed and the like of oil products sent into the microbubble generator 8.

Optionally, the microbubble generator 8 is a swirl-type microbubble generator. Raw oil rotates at a high speed in the hollow shaft, low pressure is formed at the hollow shaft, hydrogen is pumped, and under the effect of the rotational flow in the micro-bubble generator, the hydrogen is torn and divided into a large number of bubbles by the high-speed liquid phase material. On one hand, hydrogen is quickly dissolved into raw oil, and on the other hand, the surplus hydrogen forms pseudo-homogeneous gas-liquid mixture flow with oil products in a micron-sized bubble form. It is understood that the microbubble generator 8 may be other types of microbubble generators, and it is sufficient to mix hydrogen gas and the raw oil to form a pseudo-homogeneous gas-liquid mixture flow.

Optionally, the apparatus includes more than two microbubble generators, and the microbubble generators are connected in series.

Optionally, the separator 10 is a hot low pressure separator. Further, a back pressure valve is arranged between the hydrogenation reactor 9 and the separator 10 for adjusting the flow of oil products and the like.

Please refer to fig. 2, which is a schematic structural diagram of a micro-interface enhanced liquid-phase circulating hydrogenation apparatus according to another embodiment of the present invention. Specifically, a microbubble flow distributor 11 is arranged in the hydrogenation reactor 9, and the microbubble flow distributor 11 is connected to the microbubble generator 8. As said micro bubble flow distributor may be arranged between the catalyst beds of said hydrogenation reactor 9, preferably between the first catalyst bed.

In actual operation, if hydrogen is needed to be supplemented midway, the micro bubble flow with the composite temperature condition can be directly injected into the hydrogenation reactor through the micro bubble flow distributor in the hydrogenation reactor.

Specifically, the raw oil comprises any one or a mixture of a plurality of aviation kerosene, diesel oil and wax oil.

After the raw oil is sent into a heating furnace, the temperature of the raw oil is heated to 320-400 ℃. And mixing the heated raw oil with hydrogen gas in a standard state according to the gas-liquid ratio of 1: 1-80: 1 in the microbubble generator, wherein the gas-liquid mixing temperature in the microbubble generator is 100-.

The micro-bubble flow obtained from the micro-bubble generator is sent into the hydrogenation reactor from the top end of the reactor, the reaction is most violent in the front 30% of the bed layer of the hydrogenation reactor, the hydrogen consumption is large and generally exceeds 70%, a small amount of micro-bubbles are still suspended, and the micro-bubbles can meet the hydrogen consumption of the whole hydrogenation reactor. And after the hydrogenation reaction is finished, the effluent flows out of the bottom of the hydrogenation reactor and is divided into two streams, one stream enters a subsequent separator, and the other stream returns to the microbubble generator through the circulating pump for cyclic hydrogenation. Optionally, the volume ratio of the circulating oil to the fresh raw oil is 1: 1-10: 1.

Referring to the apparatus of fig. 2, if it is necessary to supply hydrogen gas halfway, the microbubble flow distributor 11 can supply the microbubble flow to ensure that there is sufficient hydrogen gas in the subsequent bed.

Example 1

The embodiment is a specific method for performing circulating hydrogenation by using the device, and the method comprises the following steps:

(1) mixing the coking diesel oil and the straight-run diesel oil in a first raw material tank according to the volume ratio of 2: 1, pressurizing the mixed fresh raw material oil to 5.0MPa by a booster pump, and conveying the fresh raw material oil to a second raw material tank;

(2) conveying the raw oil in the second raw material tank to a heating furnace through a feed pump, heating to 350 ℃, then conveying the raw oil into a microbubble generator, and simultaneously conveying hydrogen into the microbubble generator through a hydrogen pipeline, wherein the gas-liquid ratio of the hydrogen to the raw oil in the microbubble generator is 40: 1 (volume ratio);

(3) mixing hydrogen and raw oil in a microbubble generator at 350 ℃ and 5MPa to obtain a quasi-homogeneous microbubble flow;

(4) and (2) feeding the quasi-homogeneous microbubble into a downflow reactor, carrying out hydrogenation reaction at 350 ℃ and 5MPa, after the hydrogenation reaction is finished, dividing the material flowing out of the reactor into two streams, feeding one stream into a separator, and returning the other stream to the microbubble generator through a circulating pump to carry out the recycling hydrogenation reaction again.

The process can be used for diesel oil liquid-phase circulating hydrodesulfurization, and can produce refined diesel oil with sulfur content below 50ppm under the process conditions of 350 ℃ and 6MPa, and the sulfur removal rate reaches 98 percent.

The device and the method greatly improve the space utilization rate of the reactor (reduce the midway hydrogen supplement link and save the space) and have better operation stability. In addition, the internal pressure of the reactor is low (the working pressure of the original liquid phase circulating hydrogenation is reduced from 9MPa to 6MPa), the investment range of the device is reduced, and the market competitiveness of the liquid phase circulating hydrogenation is improved.

Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the invention has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.

Claims

1. The device for the liquid phase circulation hydrogenation with the strengthened micro-interface is characterized by comprising the following components: the device comprises a raw material tank, a heating furnace, a micro-bubble generator, a hydrogenation unit, a hydrogenation reactor and a separator;

the discharge end of the raw material tank is connected to the microbubble generator through a heating furnace, and the hydrogenation unit is connected to the microbubble generator; the discharge end of the microbubble generator is connected to the hydrogenation reactor, and the discharge end of the hydrogenation reactor is connected to the separator;

a microbubble flow distributor is arranged in the hydrogenation reactor and connected to the microbubble generator;

the micro-bubble flow distributor is arranged between catalyst bed layers of the hydrogenation reactor;

the device for the micro-interface reinforced liquid-phase circulating hydrogenation is used for the micro-interface reinforced liquid-phase circulating hydrogenation, and the method comprises the following steps:

the microbubble flow is mainly obtained by gas-liquid mixing of preheated raw oil and hydrogen in a microbubble generator;

under a standard state, the gas-liquid ratio in the microbubble generator is 1: 1-80: 1.

2. The apparatus of claim 1, further comprising a circulation pump, wherein the hydrogenation reactor is connected to the microbubble generator via the circulation pump.

3. The device for micro-interfacial intensified liquid-phase circulation hydrogenation according to claim 2, wherein a flow control valve is disposed between the circulation pump and the micro-bubble generator.

4. The apparatus of micro-interfacial enhanced liquid phase hydrogas recycle of claim 1 wherein the hydrogenation unit is a hydrogen pipeline.

5. The apparatus of claim 4, wherein the hydrogen line is provided with a flow control valve.

6. The apparatus of micro-interfacial enhanced liquid phase cyclic hydrogenation of claims 1 or 2, wherein said hydrogenation reactor comprises any one of a downflow reactor and an upflow reactor.

7. The device for micro-interfacial intensified liquid-phase cyclic hydrogenation of claim 1 or 2, wherein the device comprises more than two micro-bubble generators, and each micro-bubble generator is connected in series or in parallel.

8. The apparatus of claim 1, wherein the separator is a hot low pressure separator.

9. The device for micro-interfacial enhanced liquid phase cycle hydrogenation according to claim 1, wherein a back pressure valve is disposed between the hydrogenation reactor and the separator.

10. The apparatus for micro-interfacial intensified liquid-phase circulation hydrogenation according to claim 1, wherein in the method for micro-interfacial intensified liquid-phase circulation hydrogenation, the gas-liquid mixing conditions in the microbubble generator are as follows: the temperature is 100-380 deg.C and the pressure is 2-10 MPa.

11. The apparatus for micro-interfacial enhanced liquid-phase hydronic hydrogenation according to claim 1, wherein in the method for micro-interfacial enhanced liquid-phase hydronic hydrogenation, the gas-liquid mixing conditions in the microbubble generator are as follows: the temperature is 120-320 ℃, and the pressure is 2-9 MPa.

12. The device for liquid-phase cyclic hydrogenation with micro-interface enhancement as claimed in claim 1, wherein the temperature of the preheated raw oil is 320-400 ℃ in the method for liquid-phase cyclic hydrogenation with micro-interface enhancement.

13. The device for micro-interface enhanced liquid-phase circulating hydrogenation according to claim 1, wherein in the method for micro-interface enhanced liquid-phase circulating hydrogenation, the circulating oil obtained from the reactor is sent to the microbubble generator for circulating hydrogenation reaction.

14. The device for the micro-interfacial enhanced liquid phase cycle hydrogenation according to claim 13, wherein the volume ratio of the cycle oil to the raw oil is 1: 1 to 10: 1.

15. The apparatus for micro-interface enhanced liquid phase recycle hydrogenation according to claim 14, wherein the raw oil comprises any one or more of aviation kerosene, diesel oil and wax oil.