Hydrocarbon oil hydrogenation reactor and hydrocarbon oil hydrotreatment method

Abstract

The invention belongs to the technical field of hydrocarbon oil hydrogenation, and particularly relates to a hydrocarbon oil hydrogenation reactor and a hydrocarbon oil hydrotreatment method.The hydrocarbon oil hydrogenation reactor and the hydrocarbon oil hydrotreatment method comprise a reactor body, one end of the reactor body is provided with a feeding port, and the other end of the reactor body is provided with a discharging port; a gas cavity baffle and a liquid cavity baffle are arranged in the reactor body from bottom to top, the reactor body is divided into a gas cavity, a liquid cavity and a reaction area from top to bottom by the first baffle and the second baffle, and the gas cavity is communicated with the feed port; at least one compact mixing mechanism is arranged on the first baffle plate and is used for mixing hydrogen into hydrocarbon oil to be hydrogenated, the compact mixing mechanism comprises an outer layer shell, and outer layer compact holes are formed in the outer layer shell. The hydrocarbon oil hydrogenation reactor and the hydrocarbon oil hydrotreating method have the advantages of being controllable in bubble size, uniform in gas-liquid mixing and low in energy consumption.

Description

Technical Field

[0001] The invention belongs to the technical field of hydrocarbon oil hydrogenation, and in particular relates to a hydrocarbon oil hydrogenation reactor and a hydrocarbon oil hydrogenation treatment method. Background Art

[0002] In recent years, with the increasing scarcity of oil resources, the trend of heavy and inferior crude oil has become increasingly serious, and the S, N, O and metal contents of intermediate distillates obtained from crude oil distillation have also increased accordingly. However, the laws and regulations of countries around the world have increasingly stringent requirements on the S, N, O and metal contents in various fuels.

[0003] Hydrogenation is a common method to remove S, N, O and metal impurities from hydrocarbon oil and improve the quality of middle distillate oil. The hydrocarbon oil includes gasoline, reformed oil, jet fuel, diesel, wax oil, coal tar, lubricating oil, etc. The hydrogenation includes hydrodemetallization, denitrogenation, deoxygenation, deolefination, desulfurization and hydrocracking, etc.

[0004] At present, the refining hydrogenation process mainly adopts the fixed bed hydrogenation process. During the hydrogenation treatment, hydrogen needs to be injected into the liquid oil to be hydrogenated to achieve oil-gas mixing. The oil-gas mixture then contacts the catalyst for hydrogenation reaction.

[0005] Fixed bed hydrogenation reaction equipment generally includes an oil-gas mixer and a fixed bed reactor. In existing fixed bed hydrogenation reaction equipment, the oil-gas mixer is generally set separately from the fixed bed reactor. Due to the poor compatibility of oil and gas themselves, it is difficult to maintain a good mixing state. After the oil and gas are mixed, the oil-gas mixture has a long journey to reach the dense mixing mechanism. Therefore, in the reactants in contact with the catalyst, the oil-gas mixing effect is often not ideal, resulting in low hydrogenation reaction efficiency and reaction completion. In addition, in order to increase the amount of hydrogen carried by hydrocarbon oil and improve the hydrogenation effect, the existing process often adds a large amount of diluent oil circulation and / or circulates a large amount of hydrogen, which not only increases the energy consumption of the device, but also reduces the tower air velocity.

[0006] Traditionally, the mass transfer coefficient is increased by increasing the reaction temperature, and the mass transfer driving force is enhanced by pressurization, which not only increases equipment investment and process energy consumption, but also does not increase the mass transfer rate by much. Increasing the mass transfer specific surface can promote the mass transfer rate more than pressurization and temperature increase. Especially for the hydrogenation process in which the gas phase dissolves into the liquid phase, the gas phase distribution has an important influence on the mass transfer efficiency of the reactor and the efficiency of hydrogen use. If the bubble diameter is reduced from the millimeter level to the micron level, the interphase mass transfer area will increase by tens to hundreds of times under the same conditions, and the mass transfer flux and reaction rate will also be greatly improved accordingly.

[0007] Conventional methods of generating microbubbles can be divided into jet method, mechanical dispersion method, microporous dispersion method, dissolved gas release method, ultrasonic cavitation method, etc. At present, microbubble technology is mainly used in the sewage treatment industry in the field of environmental protection, such as CN203890124U, CN108854823A, etc. There are few patents related to the field of hydrogenation. Chinese patent CN104874315B discloses a microbubble generator structure that uses a microporous venturi tube and an ultrasonic method to achieve microbubble generation.

[0008] However, existing technologies for generating microbubbles generally have problems such as uneven gas-liquid mixing, uncontrollable bubble size, and high energy consumption. Summary of the invention

[0009] The purpose of the present invention is to provide a hydrocarbon oil hydrogenation reactor and a hydrocarbon oil hydrogenation treatment method to solve the common technical problems of uneven gas-liquid mixing, uncontrollable bubble size and high energy consumption, so as to achieve the purpose of controllable bubble size, uniform gas-liquid mixing and low energy consumption.

[0010] In order to solve the above technical problems, the present invention provides a hydrocarbon oil hydrogenation reactor and a hydrocarbon oil hydrogenation treatment method, comprising: a reactor body, one end of the reactor body is provided with a feed inlet, and the other end of the reactor body is provided with a discharge port; The reactor body is provided with an air cavity baffle and a liquid cavity baffle from bottom to top, the first baffle and the second baffle divide the reactor body into an air cavity chamber, a liquid cavity chamber and a reaction zone from top to bottom, and the air cavity chamber is connected to the feed port; At least one dense mixing mechanism is provided on the first baffle plate, which is used to mix hydrogen into the hydrocarbon oil to be hydrogenated, and the dense mixing mechanism includes an outer shell, the outer shell is provided with outer dense holes, the diameter of the outer dense holes is 20-30 microns, the outer shell is provided with two layers of dense liner, the two layers of dense liner are provided with two layers of dense holes, the diameter of the two layers of dense holes is 40-50 microns, the two layers of dense liner are provided with an inner layer of dense liner, the inner layer of dense liner is provided with inner layer of dense holes, the diameter of the inner layer of dense holes is 60-70 microns; The bottom of the inner dense liner is connected to the air cavity baffle, and the air cavity baffle is located at the inner dense liner and is provided with a liquid flow port to allow hydrocarbon oil to enter the air cavity chamber.

[0011] Furthermore, the distance between the outer shell and the second layer of dense liner is 50-60 cm; The distance between the second-layer dense liner and the inner-layer dense liner is 30-40 cm.

[0012] Furthermore, a primary cycle pressurizing device is provided below the air cavity baffle; The primary cycle pressurizing device includes a primary pressurizing member arranged below the air cavity baffle, and the primary pressurizing member is used to pressurize the hydrocarbon oil and push it above the air cavity baffle. The outlet of the primary pressurizing member is arranged at the air cavity baffle between the outer shell and the second layer of dense inner liner.

[0013] Furthermore, the primary pressurizing member is provided with a primary flow-increasing pipe located at the air cavity baffle, and the flow-increasing pipe is in the shape of a Laval nozzle.

[0014] Furthermore, a secondary circulation pressurizing device is provided below the air cavity baffle; The secondary circulation pressurizing device includes a secondary pressurizing member arranged below the air cavity baffle, and the secondary pressurizing member is used to pressurize the hydrocarbon oil and push it above the air cavity baffle. The outlet of the secondary pressurizing member is arranged at the air cavity baffle between the second layer of dense liner and the inner layer of dense liner.

[0015] Furthermore, the secondary pressurizing member is provided with a secondary flow-increasing pipe located at the air cavity baffle, and the flow-increasing pipe is in the shape of a Laval nozzle.

[0016] Furthermore, the mesh size of the outer layer dense pores is 1200 meshes.

[0017] Furthermore, the mesh size of the second layer of dense pores is 1000 meshes.

[0018] Furthermore, the mesh size of the inner layer dense pores is 800 meshes.

[0019] Furthermore, the ratio of the sum of the cross-sectional areas of the bottom of the dense mixing mechanism to the cross-sectional area of ​​the air cavity baffle is 0.5-0.9:1.

[0020] The beneficial effects of the present invention are: 1. The hydrogen is preliminarily dispersed through the inner dense holes of the outer shell to form larger hydrogen bubbles, which preliminarily improves the mixing degree between the hydrocarbon oil to be hydrogenated and the hydrogen; the hydrogen passes through the second dense holes of the second dense liner again to disperse the hydrogen again to form smaller hydrogen bubbles, which again improves the mixing degree between the hydrocarbon oil to be hydrogenated and the hydrogen; the hydrogen finally passes through the inner dense holes of the inner dense liner to disperse the tiny bubbles, thereby increasing the contact area between the hydrogen and the hydrocarbon oil per unit area and improving the fusion degree of the hydrocarbon oil and the hydrogen.

[0021] 2. Through the three-layer structure of the outer shell, the second layer of dense liner and the inner layer of dense liner, a filtering structure can also be formed to improve the cleanliness of the product.

[0022] 3. The internal flow rate can be increased and the degree of fusion between hydrogen and hydrocarbon oil can be improved through the primary circulation pressurization device and the secondary circulation pressurization device.

[0023] Another object of the present invention is to provide a method for hydrotreating hydrocarbon oil. Including as mentioned above, the operation steps are: Step 1: Input hydrocarbon oil through the feed port; Step 2: driving the primary pressure member and the secondary pressure member; Step 3: Drive the primary circulation pressurizing device and the secondary circulation pressurizing device.

[0024] In order to make the above-mentioned objects, features and advantages of the present invention more obvious and easy to understand, preferred embodiments are given below and described in detail with reference to the accompanying drawings. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] In order to more clearly illustrate the specific implementation methods of the present invention or the technical solutions in the prior art, the drawings required for use in the specific implementation methods or the description of the prior art will be briefly introduced below. Obviously, the drawings described below are some implementation methods of the present invention. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying creative work.

[0026] Figure 1 It is a structural schematic diagram of a hydrocarbon oil hydrogenation reactor and a hydrocarbon oil hydrogenation treatment method of the present invention; Figure 2 The present invention Figure 1 Enlarged view of point A in the middle.

[0027] In the figure: 1. Reactor body; 11. Feed inlet; 12. Discharge outlet; 13. Reaction zone; 2. air cavity baffle; 21. air cavity chamber; 3. Liquid chamber baffle; 31. Liquid chamber; 4. dense mixing mechanism; 41. outer shell; 42. outer dense holes; 43. second dense liner; 44. second dense holes; 45. inner dense liner; 46. inner dense holes; 5. Liquid flow port; 6. primary cycle pressurizing device; 61. primary pressurizing member; 62. primary flow increasing pipe; 7. Secondary circulation pressurizing device; 71. Secondary pressurizing member; 72. Secondary flow increasing pipe. DETAILED DESCRIPTION

[0028] In order to make the purpose, technical solution and advantages of the embodiments of the present invention clearer, the technical solution of the present invention will be clearly and completely described below in conjunction with the accompanying drawings. Obviously, the described embodiments are part of the embodiments of the present invention, rather than all the embodiments. Based on the embodiments of the present invention, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of the present invention. Example

[0029] like Figure 1 to Figure 2 As shown, a hydrocarbon oil hydrogenation reactor and a hydrocarbon oil hydrogenation treatment method include: a reactor body 1, one end of the reactor body 1 is provided with a feed port 11, and the other end of the reactor body 1 is provided with a discharge port 12. The staff feeds the material into the feed port 11 and discharges the material at the discharge port 12.

[0030] like Figure 1 to Figure 2 As shown, the reactor body 1 is provided with an air cavity baffle 2 and a liquid cavity baffle 3 from bottom to top. The first baffle and the second baffle separate the reactor body 1 into an air cavity chamber 21, a liquid cavity chamber 31 and a reaction zone 13 from top to bottom. The air cavity chamber 21 is connected to the feed port 11.

[0031] like Figure 1 to Figure 2 As shown, at least one dense mixing mechanism 4 is provided on the first baffle plate for mixing hydrogen into the hydrocarbon oil to be hydrogenated. In this embodiment, the ratio of the sum of the bottom cross-sectional areas of the dense mixing mechanism 4 to the cross-sectional area of ​​the air cavity baffle 2 is 0.5-0.9:1, so that the dense mixing mechanism 4 can fully mix hydrogen with the entire hydrocarbon oil.

[0032] The dense mixing mechanism 4 includes an outer shell 41, on which an outer dense hole 42 is opened, the diameter of the outer dense hole 42 is 20-30 microns, and the mesh of the outer dense hole 42 is 1200 mesh; the hydrogen is finally dispersed in the outermost layer to form hydrogen bubbles as small as 20-30 microns in diameter in the air chamber 21, which greatly improves the mixing degree between the hydrocarbon oil to be hydrogenated and the hydrogen, allowing the hydrogen to be better integrated into the hydrocarbon oil.

[0033] The outer shell 41 is provided with a second layer of dense inner liner 43, and the second layer of dense inner liner 43 is provided with a second layer of dense holes 44, the diameter of the second layer of dense holes 44 is 40-50 microns, the mesh of the second layer of dense holes 44 is 1000 mesh, and the distance between the outer shell 41 and the second layer of dense inner liner 43 is 50-60 cm. The hydrogen is dispersed in the middle, and hydrogen bubbles as small as 40-50 microns in diameter are formed in the space between the outer shell 41 and the second layer of dense inner liner 43, which greatly improves the mixing degree between the hydrocarbon oil to be hydrogenated and the hydrogen, so that the hydrogen can be better integrated into the hydrocarbon oil.

[0034] The inner layer dense liner 45 is arranged in the second layer dense liner 43, and the inner layer dense liner 45 is provided with inner layer dense holes 46, and the diameter of the inner layer dense holes 46 is 60-70 microns, and the mesh of the inner layer dense holes 46 is 800 meshes; the distance between the second layer dense liner 43 and the inner layer dense liner 45 is 30-40 cm. The hydrogen is preliminarily dispersed inside, and hydrogen bubbles with a diameter of 60-70 microns are formed in the space between the second layer dense liner 43 and the inner layer dense liner 45, and the hydrocarbon oil to be hydrogenated is preliminarily mixed with the hydrogen, and the hydrogen is preliminarily integrated into the hydrocarbon oil.

[0035] The bottom of the inner dense liner 45 is connected to the air cavity baffle 2 , and the air cavity baffle 2 is located at the inner dense liner 45 and has a liquid flow port 5 to allow hydrocarbon oil to enter the air cavity chamber 21 .

[0036] like Figure 1 to Figure 2 As shown, a primary circulation pressurizing device 6 is provided below the air cavity baffle 2; the primary circulation pressurizing device 6 includes a primary pressurizing member 61 provided below the air cavity baffle 2, the primary pressurizing member 61 is used to pressurize the hydrocarbon oil and push it above the air cavity baffle 2, and the outlet of the primary pressurizing member 61 is provided at the air cavity baffle 2 between the outer shell 41 and the second layer of dense liner 43. Among them, the primary pressurizing member 61 is provided with a primary flow-increasing pipe 62 at the air cavity baffle 2, and the flow-increasing pipe is in the shape of a Laval nozzle, and the pressurized fluid of the primary pressurizing member 61 enters the primary flow-increasing pipe 62, and is accelerated once through the narrow part in the middle of the primary flow-increasing pipe 62, thereby increasing the flow velocity in the primary flow-increasing pipe 62.

[0037] The space between the outer shell 41 and the second dense inner liner 43 is sprayed with hydrocarbon oil fluid through the primary pressurizing part 61 of the primary circulation pressurizing device 6, thereby accelerating the flow rate between the hydrocarbon oil and hydrogen between the outer shell 41 and the second dense inner liner 43, thereby accelerating the contact between the hydrocarbon oil and hydrogen and enhancing the fusion between the hydrocarbon oil and hydrogen.

[0038] like Figure 1 to Figure 2 As shown, a secondary circulation pressurizing device 7 is provided below the air cavity baffle 2; the secondary circulation pressurizing device 7 includes a secondary pressurizing member 71 provided below the air cavity baffle 2, the secondary pressurizing member 71 is used to pressurize the hydrocarbon oil and push it above the air cavity baffle 2, and the outlet of the secondary pressurizing member 71 is provided at the air cavity baffle 2 between the second layer of dense liner 43 and the inner layer of dense liner 45. Hydrocarbon oil fluid is sprayed into the space between the second layer of dense liner 43 and the inner layer of dense liner 45 to accelerate the flow rate between the hydrocarbon oil and hydrogen between the second layer of dense liner 43 and the inner layer of dense liner 45, thereby accelerating the contact between the hydrocarbon oil and hydrogen again and enhancing the fusion between the hydrocarbon oil and hydrogen.

[0039] Among them, the secondary pressure member 71 is located at the air cavity baffle 2 and is provided with a secondary flow increaser pipe 72, which is in the shape of a Laval nozzle. The pressurized fluid of the secondary pressure member 71 enters the secondary flow increaser pipe 72 and is accelerated secondary through the narrow part in the middle of the secondary flow increaser pipe 72, thereby increasing the flow rate in the secondary flow increaser pipe 72.

[0040] In this embodiment, the primary pressurizing member 61 and the secondary pressurizing member 71 use a booster pump to output hydrocarbon oil.

[0041] In summary: hydrogen is initially dispersed through the inner dense holes 46 of the outer shell 41 to form larger hydrogen bubbles, which initially improves the mixing degree between the hydrocarbon oil to be hydrogenated and hydrogen; hydrogen passes through the second dense holes 44 of the second dense liner 43 again to disperse hydrogen again to form smaller hydrogen bubbles, which again improves the mixing degree between the hydrocarbon oil to be hydrogenated and hydrogen; hydrogen finally passes through the inner dense holes 46 of the inner dense liner 45 to disperse tiny bubbles of hydrogen, thereby increasing the contact area between hydrogen and hydrocarbon oil per unit area and improving the fusion degree of hydrocarbon oil and hydrogen. Through the three-layer structure of the outer shell 41, the second dense liner 43 and the inner dense liner 45, a filtering structure can also be formed to improve the cleanliness of the product. Through the primary circulation pressurizing device 6 and the secondary circulation pressurizing device 7, the internal flow rate can be increased, and the fusion degree between hydrogen and hydrocarbon oil can be improved.

[0042] Example 2: A hydrocarbon oil hydroprocessing method, including the hydrocarbon oil hydrogenation reactor as described above, and its operating steps are: Step 1: input hydrocarbon oil through the feed port; Step 2: drive the primary pressurizing member and the secondary pressurizing member; Step 3: drive the primary circulation pressurizing device and the secondary circulation pressurizing device.

[0043] The various devices selected in this application are all universal standard parts or parts known to those skilled in the art, and their structures and principles can be known to those skilled in the art through technical manuals or conventional experimental methods.

[0044] In the description of the embodiments of the present invention, unless otherwise clearly specified and limited, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection or an indirect connection through an intermediate medium, or it can be the internal communication of two components. For ordinary technicians in this field, the specific meanings of the above terms in the present invention can be understood according to specific circumstances.

[0045] In the description of the present invention, it should be noted that the terms "center", "upper", "lower", "left", "right", "vertical", "horizontal", "inner", "outer", etc., indicating the orientation or positional relationship, are based on the orientation or positional relationship shown in the drawings, and are only for the convenience of describing the present invention and simplifying the description, rather than indicating or implying that the device or element referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limiting the present invention. In addition, the terms "first", "second", and "third" are used for descriptive purposes only, and cannot be understood as indicating or implying relative importance.

[0046] Based on the above ideal embodiments of the present invention, the relevant staff can make various changes and modifications without departing from the technical concept of the present invention through the above description. The technical scope of the present invention is not limited to the contents of the specification, and its technical scope must be determined according to the scope of the claims.

Claims

1. A hydrocarbon oil hydrogenation reactor comprising: A reactor body (1), wherein one end of the reactor body (1) is provided with a feed inlet (11), and the other end of the reactor body (1) is provided with a discharge outlet (12), characterized in that: The reactor body (1) is provided with an air cavity baffle (2) and a liquid cavity baffle (3) from bottom to top, wherein the first baffle and the second baffle divide the reactor body (1) into an air cavity chamber (21), a liquid cavity chamber (31) and a reaction zone (13) from top to bottom, and the air cavity chamber (21) is connected to the feed port (11); At least one dense mixing mechanism (4) is provided on the first baffle plate, and is used for mixing hydrogen into the hydrocarbon oil to be hydrogenated. The dense mixing mechanism (4) comprises an outer shell (41), and the outer shell (41) is provided with outer dense holes (42), and the diameter of the outer dense holes (42) is 20-30 microns. A two-layer dense liner (43) is provided inside the outer shell (41), and the two-layer dense liner (43) is provided with two-layer dense holes (44), and the diameter of the two-layer dense holes (44) is 40-50 microns. An inner layer dense liner (45) is provided inside the two-layer dense liner (43), and the inner layer dense liner (45) is provided with inner layer dense holes (46), and the diameter of the inner layer dense holes (46) is 60-70 microns. The bottom of the inner dense liner (45) is connected to the air cavity baffle (2), and the air cavity baffle (2) is located at the inner dense liner (45) and is provided with a liquid flow port (5) to allow hydrocarbon oil to enter the air cavity chamber (21).

2. A hydrocarbon oil hydrogenation reactor as claimed in claim 1, characterized in that: The distance between the outer shell (41) and the second layer of dense liner (43) is 50-60 cm; The distance between the second-layer dense liner (43) and the inner-layer dense liner (45) is 30-40 cm.

3. A hydrocarbon oil hydrogenation reactor as claimed in claim 2, characterized in that: A primary circulation pressurizing device (6) is provided below the air cavity baffle (2); The primary circulation pressurizing device (6) comprises a primary pressurizing member (61) disposed below the air cavity baffle (2), and the primary pressurizing member (61) is used to pressurize the hydrocarbon oil and push it above the air cavity baffle (2). The outlet of the primary pressurizing member (61) is disposed at the air cavity baffle (2) between the outer shell (41) and the second layer of dense inner liner (43).

4. A hydrocarbon oil hydrogenation reactor as claimed in claim 3, characterized in that: The primary pressurizing member (61) is provided with a primary flow increasing pipe (62) located at the air cavity baffle (2), and the flow increasing pipe is in the shape of a Laval nozzle.

5. A hydrocarbon oil hydrogenation reactor as claimed in claim 4, characterized in that: A secondary circulation pressurizing device (7) is provided below the air cavity baffle (2); The secondary circulation pressurizing device (7) comprises a secondary pressurizing member (71) disposed below the air cavity baffle (2), and the secondary pressurizing member (71) is used to pressurize the hydrocarbon oil and push it above the air cavity baffle (2). The outlet of the secondary pressurizing member (71) is disposed at the air cavity baffle (2) between the second layer of dense liner (43) and the inner layer of dense liner (45).

6. A hydrocarbon oil hydrogenation reactor as claimed in claim 5, characterized in that: The secondary pressurizing member (71) is provided with a secondary flow increasing pipe (72) located at the air cavity baffle (2), and the flow increasing pipe is in the shape of a Laval nozzle.

7. A hydrocarbon oil hydrogenation reactor as claimed in claim 6, characterized in that: The mesh size of the outer layer dense pores (42) is 1200 meshes.

8. A hydrocarbon oil hydrogenation reactor as claimed in claim 7, characterized in that: The mesh size of the second layer of dense pores (44) is 1000 meshes.

9. A hydrocarbon oil hydrogenation reactor as claimed in claim 8, characterized in that: The mesh size of the inner layer dense pores (46) is 800 meshes.

10. A method for hydrotreating hydrocarbon oil, characterized in that: comprising any one of claims 1 to 9 above; The operation steps are: Step 1: Input hydrocarbon oil through the feed port; Step 2: driving the primary pressure member and the secondary pressure member; Step 3: Drive the primary circulation pressurizing device and the secondary circulation pressurizing device.

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