High pressure hydrogenation unit and its functional exchanger

Abstract

The application discloses a function exchanger, which comprises: at least two tubular cavities, which are divided into two groups with the same number; a piston arranged in each tubular cavity, the piston moving along the axial direction of the tubular cavity, the piston being a dumbbell-shaped structure formed by two end plates and a connecting rod between the two end plates, the two end plates being filled with isolation gas; a check valve group connected with one end of the tubular cavity; an electronic valve group connected with the other end of the tubular cavity; and a controller in communication connection with the electronic valve group. The application also discloses a high-pressure hydrogenation device, which comprises: a function exchanger used for pressurizing raw oil by using high-pressure separated high liquid, the pressurized raw oil entering a reactor. The piston of the dumbbell-shaped structure of the function exchanger is filled with high-pressure isolation gas, liquid leakage and mutual mixing on both sides of the piston are avoided, the quality of the high-liquid oil product is ensured, and the energy recovery rate of the high-pressure hydrogenation device is improved.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of petroleum chemical hydrogenation process, in particular to a high-pressure hydrogenation device and a functional exchanger thereof. BACKGROUND

[0002] Since the 1990s, as an important process of petroleum refining, catalytic hydrogenation technology and device have been rapidly developed all over the world. In the global refining industry, the processing capacity of catalytic hydrogenation accounts for more than 57% of the primary processing capacity of crude oil, which is much higher than that of any other secondary processing device.

[0003] Generally speaking, in the overall process layout of a petroleum chemical enterprise, according to the different properties of raw materials and product requirements, from crude oil distillation to the delivery of various qualified products, various different types of hydrogenation process devices are set up, such as naphtha hydrogenation, aviation fuel hydrogenation, gasoline refining (including S-Zorb), diesel hydrogenation, wax oil hydrogenation, residual oil hydrogenation, lubricating oil hydrogenation, and hydrogenation isomerization and condensation reduction. The processes of hydrogenation process devices are generally similar, mainly including a reaction part and a separation part. The reaction part is divided into fixed bed hydrogenation, boiling bed hydrogenation, slurry bed hydrogenation and moving bed hydrogenation according to the state of the catalyst bed in the reactor; and is divided into high-pressure hydrogenation, medium-pressure hydrogenation and low-pressure hydrogenation according to the reaction pressure. Generally, as the properties of hydrogenation raw oil become heavier, the pressure required by the hydrogenation device increases; at the same time, in order to ensure the activity of the catalyst and the operation cycle of the device, the required hydrogen partial pressure also increases. For example, residual oil hydrogenation, hydrogenation cracking, wax oil hydrogenation and lubricating oil hydrogenation for producing high-quality base oil generally require high reaction pressure (12.0-20.0 MPa). The separation part generally includes a gas-liquid separator, a stripping tower and a fractionating tower. The hydrogenation reaction product is a multi-component gas-liquid mixture, which enters the separation part after coming out of the reaction part to obtain various target products.

[0004] Since this century, with the increasing demand for energy and more and more attention to energy saving, energy saving technology has developed rapidly in all walks of life. The petroleum refining and chemical industry also attaches great importance to energy saving. Especially in the catalytic hydrogenation technology under high temperature, high pressure and hydrogen environment, energy saving has been paid more attention. USP4,159,937 proposes a method for separating the hydrogenation cracking product. The gas-liquid mixture after hydrogenation cracking is separated by multi-stage separation to separate various hydrogenation cracking products. First, the hydrogenation cracking product enters the hot high-pressure separator, and the gas-liquid separation is carried out at high temperature and high pressure, and the liquid phase enters a low-pressure hot flash tank for flash evaporation to obtain gas-liquid products. The gas phase of the hot high-pressure separator is condensed and enters the cold high-pressure separator to separate the hydrogen-rich gas. The hot low-pressure gas is condensed and enters the flash tank with the liquid phase from the cold high-pressure separator at a lower pressure. This gas-liquid separation process is based on the characteristics of large heat release in the hydrogenation process and high temperature of the hydrogenation product. In order to balance the energy of the hydrogenation reaction part and the separation part, from the perspective of energy recovery, the high-temperature liquid phase is sent to the fractionation unit which needs a large amount of heat for hydrogen sulfide removal and distillation cutting, so as to realize the purpose of reducing the overall energy consumption of the hydrogenation device.

[0005] In order to further comprehensively utilize energy and save energy, CN101003748A proposes a hydrogenation reaction effluent separation process. The hydrogenation reaction effluent enters the hot high-pressure separator, the gas phase separated is cooled and enters the medium-temperature high-pressure separator, the gas phase separated from the medium-temperature high-pressure separator is cooled and enters the cold high-pressure separator, and the gas phase separated from the cold high-pressure separator is used as the circulating hydrogen. A heat exchange tower is provided, and the liquid phases separated from the hot high-pressure separator, the medium-temperature high-pressure separator and the cold high-pressure separator enter the lower, middle and upper parts of the heat exchange tower respectively, the liquid phase of the heat exchange tower is sent to the stripping tower for treatment, and the gas phase of the heat exchange tower is cooled and then enters the gas-liquid separator for separation. The existing gas-liquid separation process only starts from the perspective of energy balance and comprehensive utilization, and needs to set up heat exchange equipment to recover heat at different temperature levels.

[0006] In the initial hydrogenation process, the liquid phase of the high-pressure separator is generally reduced in pressure by a pressure reducing valve and then enters the low-pressure separator. In order to recover the pressure energy of the liquid phase of the high-pressure separator from high pressure to low pressure, since the 1990s, some hydrogenation processes have set up a hydraulic turbine between the high-pressure separator and the low-pressure separator to recover the pressure energy. However, in actual application, there are problems such as serious leakage and low energy recovery efficiency, and some have been idle.

[0007] The information disclosed in this BACKGROUND section is only intended to increase an understanding of the general context in which the present application can be practiced. It should not be taken as an acknowledgement or any form of suggestion that this information forms a prior art that is already known to those skilled in the art. SUMMARY

[0008] One of the purposes of the present application is to provide a high-pressure hydrogenation device and a function exchanger thereof, so as to improve the problems of liquid medium leakage and the like in the process of pressure energy recovery.

[0009] Another purpose of the present application is to provide a high-pressure hydrogenation device and a function exchanger thereof, so as to improve the problems of low energy recovery rate and the like in the high-pressure hydrogenation device.

[0010] To achieve the above-mentioned purposes, according to a first aspect of the present application, the present application provides a function exchanger, comprising: at least two tubular cavities, which are divided into two groups with the same number; a piston arranged in each tubular cavity, the piston moving along the axial direction of the tubular cavity, the piston being a dumbbell-shaped structure formed by two end plates and a connecting rod between the two end plates, and the two end plates being filled with isolation gas; a check valve group connected to one end of the tubular cavity; an electronic valve group connected to the other end of the tubular cavity; and a controller in communication connection with the electronic valve group.

[0011] Further, in the above technical solution, the piston is provided with a gas filling assembly, the gas filling assembly comprising: a conical valve hole opened in one end plate of the piston; a check valve ball accommodated in the conical valve hole, the check valve ball sealing the conical valve hole under the action of the isolation gas; and a lock valve arranged outside the conical valve hole, the conical valve hole forming a gas filling channel when the lock valve is opened, and the conical valve hole being sealed when the lock valve is closed.

[0012] Further, in the above technical solution, the isolation gas is hydrogen, nitrogen or light hydrocarbon.

[0013] Further, in the above technical solution, the pressure of the isolation gas is 1.1-1.2 times the maximum pressure of the media on both sides of the piston.

[0014] Further, in the above technical solution, a threaded groove is arranged on the outer periphery of the end plate of the piston, and a sealing band is arranged in the threaded groove.

[0015] Further, in the above technical solution, the thickness of the end plate of the piston is 1 / 6-1 / 2 times the inner diameter of the tubular cavity, and the length of the connecting rod is 1 / 100-1 / 10 times the length of the tubular cavity.

[0016] Further, in the above technical solution, the electronic valve group is a three-way valve, and the three-way valve is connected to high-pressure liquid inlet and high-pressure liquid outlet.

[0017] Further, in the above technical solution, the check valve group comprises an inlet check valve and an outlet check valve arranged in parallel, the inlet check valve being connected to low-pressure liquid inlet, and the outlet check valve being connected to low-pressure liquid outlet.

[0018] Furthermore, in the above technical solution, the functional exchanger also includes: a low-pressure end feed chamber and a low-pressure end outlet chamber, which are connected to one end of the two sets of tubular cavities through the check valve assembly; and a high-pressure end feed chamber and a high-pressure end outlet chamber, which are connected to the other end of the two sets of tubular cavities through the electronic valve assembly.

[0019] Furthermore, in the above technical solution, the controller controls the opening and closing of the electronic valve group, so that the two sets of tubular cavities alternately perform the pressurization process and the depressurization process.

[0020] Furthermore, in the above technical solution, when there is more than one tubular cavity in each group, the two ends of each tubular cavity are connected to the check valve group and the electronic valve group respectively.

[0021] Furthermore, in the above technical solution, the tubular cavity is equipped with a positioning element, which limits the movement of the piston, and the positioning element is communicatively connected to the controller.

[0022] According to a second aspect of the present invention, a high-pressure hydrogenation apparatus is provided, comprising: a reactor for a hydrogenation reaction; a high-pressure separator for separating the reaction products of the reactor; a functional exchanger as described in any of the above technical solutions for pressurizing the feed oil using the high-pressure separated liquid, the pressurized feed oil entering the reactor; and a low-pressure separator for separating the high-pressure separated liquid after depressurization by the functional exchanger.

[0023] Furthermore, in the above technical solution, the high-pressure hydrogenation device also includes: a compressor, which is used to recycle the hydrogen separated by the high-pressure separator back to the reactor; and a heater, which is used to heat the feed to the reactor.

[0024] Furthermore, in the above technical solution, the raw material oil enters and exits the tubular cavity via a check valve assembly; the high-separation liquid enters and exits the tubular cavity via an electronic valve assembly.

[0025] Furthermore, in the above technical solution, the pressure of the high-pressure separator is 10.0 to 20.0 MPa; the pressure of the low-pressure separator is 0.8 to 2.5 MPa.

[0026] Furthermore, in the above technical solutions, the hydrogenation reaction is wax oil hydrogenation, residue oil hydrogenation, hydrocracking, catalytic diesel hydrotreating, lubricating oil hydrogenation, or hydrodewaxing.

[0027] Compared with the prior art, the present invention has one or more of the following beneficial effects:

[0028] 1. The dumbbell-shaped piston design of the functional exchanger allows for the filling of the piston with high-pressure isolation gas, preventing liquid leakage and mixing on both sides of the piston and ensuring the quality of high-separation oil.

[0029] 2. By setting the inflation assembly on the piston, the high pressure gas is filled into the piston during the maintenance process, so as to maintain the pressure of the gas in the piston and ensure the isolation of the piston to the liquid on both sides.

[0030] 3. The application reduces the number of electromagnetic valves, reduces the cost, reduces the accident rate of electromagnetic valves, and ensures long-period operation.

[0031] 4. The high-pressure hydrogenation device has high energy recovery rate, the recovery rate is up to 90% or more, the power consumption of the raw oil booster is greatly reduced, and the device is safe and reliable, small in size, low in reconstruction investment and low in cost.

[0032] The above description is only a summary of the technical solutions of the application. In order to more clearly understand the technical means of the application and can be implemented according to the content of the specification, at the same time, in order to make the above and other purposes, technical features and advantages of the application more easy to understand, one or more preferred embodiments are listed below, and the details are described as follows with reference to the drawings. BRIEF DESCRIPTION OF DRAWINGS

[0033] Figure 1 is a structural schematic diagram of a function exchanger according to an embodiment of the application.

[0034] Figure 2 is a structural schematic diagram of a piston according to an embodiment of the application.

[0035] Figure 3 is a structural schematic diagram of a high-pressure hydrogenation device according to an embodiment of the application.

[0036] MAIN REFERENCE NUMERALS EXPLANATION:

[0037] 10-first tubular cavity, 111-first inlet check valve, 112-first outlet check valve, 12-first three-way valve, 20-second tubular cavity, 211-second inlet check valve, 212-second outlet check valve, 22-second three-way valve, 30-piston, 31-end plate, 32-connecting rod, 33-inflation assembly, 331-conical valve hole, 332-check valve ball, 333-locking valve, 34-thread groove, 41-low pressure end feeding cabin, 42-low pressure end outlet cabin, 51-high pressure end feeding cabin, 52-high pressure end outlet cabin;

[0038] 100-reactor, 200-high pressure separator, 300-function exchanger, 400-low pressure separator, 500-circulating hydrogen compressor, 600-heating furnace, 700-high pressure heat exchanger. DETAILED DESCRIPTION

[0039] The specific embodiments of the application will be described in detail below with reference to the drawings, but it should be understood that the protection scope of the application is not limited by the specific embodiments.

[0040] Unless otherwise expressly stated, throughout the specification and claims, the term "comprising" or its variations such as "including" or "comprises" shall be understood to include the stated elements or components without excluding other elements or other components.

[0041] In this document, for ease of description, spatial relative terms such as “below,” “under,” “down,” “above,” “above,” “up,” etc., are used to describe the relationship of one element or feature to another element or feature in the accompanying drawings. It should be understood that spatial relative terms are intended to encompass different orientations of an object in use or operation, in addition to those depicted in the figures. For example, if an object in the figure is flipped, an element described as “below” or “under” another element or feature would be oriented “above” that element or feature. Thus, the exemplary term “below” can encompass both the downward and upward orientations. An object may also have other orientations (rotated 90 degrees or other orientations), and the spatial relative terms used herein should be interpreted accordingly.

[0042] In this document, the terms "first," "second," etc., are used to distinguish two different elements or parts, and are not used to define specific positions or relative relationships. In other words, in some embodiments, the terms "first," "second," etc., can also be used interchangeably.

[0043] like Figures 1 to 2 As shown, the functional exchanger 300 according to a specific embodiment of the present invention includes a first tubular cavity 10 and a second tubular cavity 20, each tubular cavity having a piston 30 capable of moving along its axial direction. The piston 30 has a dumbbell-shaped structure formed by two end plates 31 and a connecting rod 32 between them, with a gas separator between the two end plates 31. One end of the first tubular cavity 10 and the second tubular cavity 20 is provided with a check valve assembly, and the other end is provided with an electronic valve assembly, which is communicatively connected to a controller (not shown). The number of tubular cavities is at least two, and the at least two tubular cavities are divided into two groups of the same number. Figure 1 In the example shown, there are two tubular cavities. The first tubular cavity 10 is one group, and the second tubular cavity 20 is another group. It should be understood that the present invention is not limited thereto. Those skilled in the art can set the number of tubular cavities according to actual needs (such as the unit flow rate of the fluid to be processed). For example, four tubular cavities can be set, divided into two groups, with two tubular cavities in each group.

[0044] Further, in one or more exemplary embodiments of the present application, the check valve group comprises a first inlet check valve 111 and a first outlet check valve 112 connected to the first tubular cavity 10 in parallel with each other, and a second inlet check valve 211 and a second outlet check valve 212 connected to the second tubular cavity 20 in parallel with each other. The first inlet check valve 111 and the second inlet check valve 211 are connected to the low-pressure liquid inlet, and the first outlet check valve 112 and the second outlet check valve 212 are connected to the low-pressure liquid outlet. The electronic valve group can be a three-way valve, and exemplarily, the electronic valve group comprises a first three-way valve 12 connected to the first tubular cavity 10, and a second three-way valve 22 connected to the second tubular cavity 20. The first three-way valve 12 and the second three-way valve 22 are connected to the high-pressure liquid inlet and the high-pressure liquid outlet, respectively.

[0045] Further, in one or more exemplary embodiments of the present application, the piston 30 is provided with an inflation assembly 33, which comprises a conical valve hole 331 formed in one end plate 31 of the piston, and a check valve ball 332 accommodated in the conical valve hole 331 and sealing the conical valve hole 331 under the isolation of the gas in the piston 30. The outer side of the conical valve hole 331 is provided with a lock valve 333, which, when opened, forms an inflation passage of the conical valve hole 331, and, when closed, seals the conical valve hole 331.

[0046] Further, in one or more exemplary embodiments of the present application, the isolation gas can be hydrogen, nitrogen, light hydrocarbon, or the like. Further, in one or more exemplary embodiments of the present application, the pressure of the isolation gas is 1.1-1.2 times the maximum pressure of the medium on both sides of the piston 30.

[0047] Further, in one or more exemplary embodiments of the present application, the outer periphery of the end plate 31 of the piston 30 is provided with a threaded groove 34, and a sealing band is arranged in the threaded groove 34. Exemplarily, the sealing band is an integral sealing band, thereby ensuring the sealing of the piston 30 with the inner wall of the tubular cavity during movement.

[0048] Further, in one or more exemplary embodiments of the present application, the thickness of the end plate 31 of the piston 30 is 1 / 6-1 / 2 times the inner diameter of the tubular cavity, and the length of the connecting rod 32 is 1 / 100-1 / 10 times the length of the tubular cavity.

[0049] Further, in one or more exemplary embodiments of the present application, the function exchanger further comprises a low-pressure end feed cabin 41 and a low-pressure end outlet cabin 42, and a high-pressure end feed cabin 51 and a high-pressure end outlet cabin 52. The low-pressure end feed cabin 41 is connected to one end of the first tubular cavity 10 through a first inlet check valve 111, and the low-pressure end feed cabin 41 is connected to one end of the second tubular cavity 20 through a second inlet check valve 211; the low-pressure end outlet cabin 42 is connected to one end of the first tubular cavity 10 through a first outlet check valve 112, and the low-pressure end outlet cabin 42 is connected to one end of the second tubular cavity 20 through a second outlet check valve 212. The first three-way valve 12 is connected to the other end of the first tubular cavity 10, the high-pressure end feed cabin 51 and the high-pressure end outlet cabin 52, respectively; the second three-way valve 22 is connected to the other end of the second tubular cavity 20, the high-pressure end feed cabin 51 and the high-pressure end outlet cabin 52, respectively.

[0050] Further, in one or more exemplary embodiments of the present application, the controller controls the opening and closing of the first three-way valve 12 and the second three-way valve 22, so that the first tubular cavity 10 and the second tubular cavity 20 (or the first group of tubular cavities and the second group of tubular cavities) alternately perform the pressurization process and the pressure relief process.

[0051] Further, in one or more exemplary embodiments of the present application, the tubular cavity can be provided with a positioning member (not shown in the figure), which limits the movement of the piston 30 and is in communication connection with the controller.

[0052] Further, in one or more exemplary embodiments of the present application, when the number of each group of tubular cavities is more than one, one end of each group of tubular cavities is connected to a set of check valves after being collected respectively, and the other end is connected to a set of electronic valves after being collected respectively. For example, when the number of each group of tubular cavities is two, one end of the two tubular cavities of the first group shares a set of inlet check valves and outlet check valves after being collected, and the other end of the two tubular cavities of the first group shares a three-way valve after being collected; one end of the two tubular cavities of the second group shares a set of inlet check valves and outlet check valves after being collected, and the other end of the two tubular cavities of the second group shares a three-way valve after being collected.

[0053] In combination Figure 3 As shown, in the high-pressure hydrogenation device of one or more embodiments of the present application, the reaction product of the reactor 100 for hydrogenation reaction enters the high-pressure separator 200 for separation, the liquid phase effluent of the high-pressure separator 200 is separated into high-pressure liquid and low-pressure liquid, and the high-pressure liquid enters the function exchanger 300 for pressurization, and the low-pressure liquid enters the low-pressure separator 400 for separation. The gas phase effluent of the high-pressure separator 200 is combined with new hydrogen by the circulating hydrogen compressor 500 to form raw hydrogen, and the raw hydrogen and the raw oil pressurized by the function exchanger 300 are heated by the heating furnace 600 and then enter the reactor 100 for hydrogenation reaction.

[0054] Further, in one or more exemplary embodiments of the present application, a part of the raw oil enters the functional exchanger 300 to be pressurized, and another part is mixed with the pressurized raw oil, and the mixed raw oil exchanges heat with the reaction product of the reactor 100 in the high-pressure heat exchanger 700, and then enters the heating furnace 600, thereby increasing the temperature of the raw oil and reducing the fuel consumption of the heating furnace 600.

[0055] Exemplarily, the pressure of the high-pressure separator 200 is 10.0-20.0 MPa, preferably 11.0-15.0 MPa; and the pressure of the low-pressure separator is 0.8-2.5 MPa, preferably 1.2-2.0 MPa.

[0056] Further, in one or more exemplary embodiments of the present application, the hydrogenation reaction can be wax oil hydrogenation, residual oil hydrogenation, hydrocracking, catalytic diesel oil hydro-upgrading, lubricating oil hydrogenation, and hydrogenation pour point reduction, etc.

[0057] The working process of the functional exchanger of the present application will be described in more detail in the form of specific examples below, and it should be understood that the present application is not limited thereto.

[0058] Example 1

[0059] In combination with Figure 1 and Figure 3 It is shown that the working principle and working process of the functional exchanger 300 of the present embodiment are as follows:

[0060] The low-pressure raw oil enters the first tubular cavity 10 through the first inlet check valve 111 via the low-pressure end feed cabin 41, and the low-pressure raw oil pushes the piston 30 in the first tubular cavity 10 to the high-pressure end; the feed port of the first three-way valve 12 is opened, and the high-pressure high-liquid separated from the high-pressure separator 200 enters the first tubular cavity 10 through the first three-way valve 12 via the high-pressure end feed cabin 51, and the high-liquid pushes the piston 30 to the low-pressure end of the first tubular cavity 10; at this time, the pressure of the high-liquid in the first tubular cavity 10 is reduced, and the pressurized raw oil is discharged through the first outlet check valve 112 into the low-pressure end outlet cabin 42; when the piston 30 of the first tubular cavity 10 moves to the positioning member of the low-pressure end, the feed port of the first three-way valve 12 is closed, and the outlet is opened, the low-pressure raw oil enters the first tubular cavity 10 through the first inlet check valve 111 via the low-pressure end feed cabin 41, and the low-pressure raw oil pushes the piston 30 in the first tubular cavity 10 to the high-pressure end, and at the same time, the high-liquid in the first tubular cavity 10 after pressure relief enters the high-pressure end outlet cabin 52 through the first three-way valve 12 and is discharged.

[0061] The pressurization and pressure relief processes opposite to those of the first tubular cavity 10 are carried out in the second tubular cavity 20, thereby realizing the pressurization of the raw oil.

[0062] The foregoing description of specific exemplary embodiments of the application has been presented for the purposes of illustration and description. It is not intended to be exhaustive or to limit the application to the precise form disclosed, and various modifications and variations are possible in light of the above teachings. It is intended that the embodiments be limited only by the claims. A variety of changes and modifications can be suggested by the above description, and it is intended that the application encompass such changes and modifications as fall within the scope of the claims. Any simple modifications, equivalent changes, and modifications based on the above-described exemplary embodiments should fall within the protection scope of the application.

Claims

1. A functional exchanger, characterized by, The application relates to a functional exchanger. The application comprises: at least two tubular cavities, which are divided into two groups with the same number; a piston arranged in each of the tubular cavities, the piston moving along the axial direction of the tubular cavity, the piston being a dumbbell-shaped structure formed by two end plates and a connecting rod between the two end plates, and the two end plates being filled with isolation gas; the piston is provided with a gas filling assembly, the gas filling assembly comprising: a conical valve hole formed in one end plate of the piston; a check valve ball accommodated in the conical valve hole, the check valve ball being sealed in the conical valve hole under the action of the isolation gas; a lock valve arranged outside the conical valve hole, the conical valve hole forming a gas filling channel when the lock valve is opened, and the conical valve hole being sealed when the lock valve is closed; a check valve group connected to one end of the tubular cavity; an electronic valve group connected to the other end of the tubular cavity; and 2. The functional exchanger of claim 1, wherein, a controller in communication connection with the electronic valve group.

3. The functional exchanger of claim 1, wherein, The isolation gas is hydrogen, nitrogen or light hydrocarbon.

4. The functional exchanger of claim 1, wherein, The pressure of the isolation gas is 1.1-1.2 times the maximum pressure of the medium on both sides of the piston.

5. The functional exchanger of claim 1, wherein, A threaded groove is arranged on the outer periphery of the end plate of the piston, and a sealing strip is arranged in the threaded groove.

6. The functional exchanger of claim 1, wherein, The thickness of the end plate of the piston is 1 / 6-1 / 2 times the inner diameter of the tubular cavity, and the length of the connecting rod is 1 / 100-1 / 10 times the length of the tubular cavity.

7. The functional swap of claim 1, wherein, The electronic valve group is a three-way valve connected to high-pressure liquid feeding and high-pressure liquid discharging.

8. The functional exchanger of claim 1, wherein, The check valve group comprises an inlet check valve and an outlet check valve arranged in parallel, the inlet check valve being connected to low-pressure liquid feeding, and the outlet check valve being connected to low-pressure liquid discharging. The application further comprises: a low-pressure end feeding cabin and a low-pressure end outlet cabin connected to one end of the two groups of tubular cavities through the check valve group; and a high-pressure end feeding cabin and a high-pressure end outlet cabin connected to the other end of the two groups of tubular cavities through the electronic valve group.

9. The functional exchanger of claim 1, wherein, The controller controls the opening and closing of the electronic valve group, so that the two groups of tubular cavities alternately perform the pressurization process and the pressure relief process.

10. The functional exchanger of claim 1, wherein, When the number of each group of tubular cavities is more than one, the two ends of each group of tubular cavities are respectively collected and connected to the check valve group and the electronic valve group.

11. The functional exchanger of claim 1, wherein, The tubular cavity is provided with a positioning member, the positioning member limiting the movement of the piston, and the positioning member being in communication connection with the controller.

12. A high pressure hydrogenation unit characterized by, The application relates to a functional exchanger. The application comprises: a reactor for hydrogenation reaction; a high-pressure separator for separating the reaction product of the reactor; the functional exchanger as claimed in any one of claims 1-11, which is used for pressurizing raw oil by using high-separation liquid separated by the high-pressure separator, and the pressurized raw oil enters the reactor; and 13. The high pressure hydrogenation unit of claim 12, wherein, a low-pressure separator for separating high-separation liquid depressurized by the functional exchanger. The application further comprises: a compressor for circulating hydrogen separated by the high-pressure separator back to the reactor; 14. The high pressure hydrogenation unit of claim 12, wherein, a heating furnace for heating the feed of the reactor. Raw oil enters and flows out of the tubular cavity through the check valve group, and high-separation liquid enters and flows out of the tubular cavity through the electronic valve group.

15. The high pressure hydrogenation unit of claim 12, wherein, The high-pressure separator has a pressure of 10.0-20.0 MPa; and the low-pressure separator has a pressure of 0.8-2.5 MPa.

16. The high pressure hydrogenation plant of claim 12, wherein, The hydrogenation reaction is wax oil hydrogenation, residual oil hydrogenation, hydrocracking, catalytic diesel oil hydro-upgrading, lubricating oil hydrogenation or hydrogenation pour point depression.

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