Fluidized bed hydrogenation reaction system

Abstract

The fluidized bed hydrogenation reaction system comprises a catalyst filling unit, a first reaction feeding pipeline, a mixing unit, a second reaction feeding pipeline and a fluidized bed reactor, the catalyst filling unit and the first reaction feeding pipeline are respectively connected with the mixing unit; the mixing unit is connected with the fluidized bed reactor through the second reaction feeding pipeline, the fluidized bed reactor comprises a reactor main body, a reaction cavity is formed in the reactor main body, and the second reaction feeding pipeline is communicated with the bottom of the reaction cavity; the reflux cup is arranged at the upper part of the reaction cavity; and the gas rising pipe of the backflow cup is through. According to the utility model, the reaction efficiency is improved, the conversion rate is improved, the loading and unloading process of the catalyst can be simplified, and the operation cost and safety risk are reduced. The internal component structure of the fluidized bed hydrogenation reactor is optimized, the pressure drop of the reactor can be reduced, the circulation volume in the reactor can be further increased, and the forward proceeding of hydrogenation reaction is facilitated.

Description

TECHNICAL FIELD

[0001] The utility model relates to the field of oil refining chemical industry, especially relates to a ebullated bed hydrogenation reaction system. BACKGROUND

[0002] Traditional ebullated bed hydrocracking process is widely used in heavy oil (residual oil, thick oil, coal tar) treatment production, and the solid catalyst can effectively promote heavy oil cracking reaction, but there are still significant deficiencies, including:

[0003] 1. Catalyst deactivation: under the high temperature and high pressure reaction environment, the solid catalyst is easy to deactivate due to metal deposition, carbon deposition, coking and sintering and other factors. At the same time, carbon deposition and coking phenomenon also occur with the reaction, further affecting the performance of the catalyst, eventually making the cracking reaction efficiency decrease significantly.

[0004] 2. Complex catalyst online replacement: specifically, in the actual operation process, part of the catalyst needs to be removed from the reactor, and the removal process is from high temperature and high pressure to low pressure state and then cooling treatment; at the same time, fresh catalyst needs to be added to the reactor, and the addition process is from low temperature and low pressure to high temperature and high pressure in the reactor.

[0005] 3. Fluid dynamics limitation: there are gas, liquid and solid three-phase flow in the ebullated bed reactor. The traditional reactor design often affects the three-phase flow characteristics due to any disturbance, resulting in easy agglomeration of the catalyst. Catalyst agglomeration not only increases the loss of catalyst, but also makes the reaction uneven, affecting the conversion rate and product quality of the reaction.

[0006] 4. Limitation of raw material adaptability: the traditional solid catalyst has poor adaptability to metal impurities and residual carbon content in heavy oil. With the increase of metal content and residual carbon content in the raw material, the deactivation rate of the catalyst will increase significantly. This limits the range of raw materials that can be used, and the traditional catalyst cannot effectively perform catalytic reaction for some heavy oil with high metal content or high residual carbon content.

[0007] The above problems will cause the conversion rate of the ebullated bed hydrogenation reactor to decrease, which not only reduces the economic benefit, but also makes the advantages of the ebullated bed hydrogenation process lost. Therefore, how to improve the conversion rate of the ebullated bed hydrogenation reactor becomes a problem to be solved. INVENTION CONTENTS

[0008] In order to solve the technical problem of reducing the conversion rate of the ebullated bed hydrogenation reactor, the utility model provides an ebullated bed hydrogenation reaction system to solve the above problems.

[0009] The utility model provides the following specific schemes:

[0010] The application discloses a boiling bed hydrogenation reaction system, which comprises a catalyst filling unit, a first reaction feed pipeline, a mixing unit, a second reaction feed pipeline and a boiling bed reactor.

[0011] The catalyst filling unit and the first reaction feed pipeline are connected to the mixing unit respectively.

[0012] The mixing unit is connected to the boiling bed reactor through the second reaction feed pipeline.

[0013] The boiling bed reactor comprises:

[0014] A reactor body, which has a reaction cavity inside, and the second reaction feed pipeline is communicated with the bottom of the reaction cavity.

[0015] A reflux cup is arranged at the upper part of the reaction cavity.

[0016] The reflux cup comprises:

[0017] A cup wall, which is funnel-shaped, and the reflux cup divides the reaction cavity into a first chamber below the cup wall and a second chamber above the cup wall, and the mixed feed is arranged in the first chamber.

[0018] A riser pipe is arranged in the second chamber, and the first end of the riser pipe is connected to the cup wall and communicated with the first chamber, and the second end of the riser pipe extends away from the cup wall.

[0019] The riser pipe is through from the first end to the second end, so that the flow path of the reaction gas in the riser pipe is linear.

[0020] Preferably, the catalyst filling unit comprises a catalyst buffer tank and a catalyst metering pump which are connected in sequence.

[0021] The inlet of the catalyst buffer tank is connected to a pipeline from the catalyst boundary line, and the outlet of the catalyst buffer tank is communicated with the inlet of the catalyst metering pump through a metering pump inlet pipeline.

[0022] The outlet of the catalyst metering pump is communicated with the mixing unit through a metering pump outlet pipeline.

[0023] Preferably, the mixing unit comprises a static mixer and a reaction feed pump.

[0024] The first inlet of the static mixer is connected to the metering pump outlet pipeline, the second inlet of the static mixer is communicated with the first reaction feed pipeline, and the outlet of the static mixer is communicated with the inlet of the reaction feed pump.

[0025] Preferably, the ebullated bed hydrogenation reaction system further comprises a heating heat exchange unit;

[0026] The inlet of the heating heat exchange unit is communicated with the outlet of the reaction feed pump, and the outlet of the heating heat exchange unit is communicated with the ebullated bed reactor through the second reaction feed pipeline.

[0027] The utility model discloses the beneficial effects are as follows:

[0028] The utility model provides a kind of ebullated bed hydrogenation reaction system, including catalyst filling unit, first reaction feed pipeline, mixing unit, second reaction feed pipeline and ebullated bed reactor;Catalyst filling unit transports oily catalyst to mixing unit, and first reaction feed pipeline is used to deliver reaction raw material to the mixing unit;Mixing unit fully mixes oily catalyst and reaction raw material, and is delivered to ebullated bed reactor, and ebullated bed reactor makes reaction raw material under the catalysis of oily catalyst hydrogenation reaction.This system uses oil-soluble nano catalyst to replace the solid catalyst of ebullated bed hydrogenation:

[0029] 1) the utility model develops new structure according to the characteristics of oil-soluble catalyst with excellent dispersion performance, can make reaction raw material and catalyst more uniform and greatly increase the contact area of reaction, can more flexibly make reactant interact, so that more raw material oil can be converted into target product, significantly improves conversion rate;

[0030] 2) under the premise that the overall structure of reactor and other process flows are not changed, reaction space is increased, equivalent to reduce space velocity, provide more abundant time for reaction, improve reaction efficiency and conversion rate;

[0031] 3) the structure of the utility model can make catalyst and reaction raw material mix uniformly, effectively avoid local overheating phenomenon, improve the safety and stability of reaction, and further improve generation efficiency.

[0032] Particularly, catalyst filling unit adopts the combination of catalyst buffer tank and catalyst metering pump, and through reaction raw material and target concentration calculation, the injection amount and injection speed of catalyst can be accurately controlled, to ensure that the concentration of catalyst remains in a suitable range during reaction;Through this low-pressure end continuous injection mode, the traditional catalyst filling process is simplified, thereby improving overall production efficiency, and the loading and unloading process is more simple and fast, reducing operating cost and safety risk.

[0033] Particularly, the riser is through from the first end to the second end, so that the flow path of reaction gas in the riser is linear, and the optimization of the component is compared with the traditional riser (see Figure 3), cancel the lift pipe cover and the spiral plate in the trachea, the improvement improves the circulation amount, and the high circulation amount relatively reduces the single pass conversion rate of the hydrogenation reaction; the high circulation amount also increases the oil-soluble catalyst storage in the reactor, which is beneficial to the positive reaction of the hydrogenation reaction.

[0034] In particular, after canceling the structure related to the online loading and unloading of the solid catalyst in the reactor, the reaction space is increased by more than 20%, which can significantly improve the processing capacity of the ebullated bed hydrogenation device and increase economic benefits. BRIEF DESCRIPTION OF DRAWINGS

[0035] Figure 1 A structure diagram of an ebullated bed hydrogenation reaction system is provided.

[0036] Figure 2 A schematic diagram of the upper structure of the ebullated bed reactor in the ebullated bed hydrogenation reaction system is provided.

[0037] Figure 3 A schematic diagram of a traditional lift pipe structure.

[0038] Figure 4 A schematic diagram of the improved lift pipe structure is provided.

[0039] In the figure: 100-catalyst filling unit; 101-catalyst buffer tank; 102-catalyst metering pump; 103-catalyst boundary line; 104-metering pump inlet pipeline; 105-metering pump outlet pipeline; 200-first reaction feed pipeline; 201-static mixer; 202-reaction feed pump; 300-mixing unit; 400-second reaction feed pipeline; 500-and ebullated bed reactor; 501-reaction main body; 502-reaction cavity; 5021-first chamber; 5022-second chamber; 503-reflux cup; 5031-cup wall; 5032-lift pipe; 600-heating and heat exchange unit. DETAILED DESCRIPTION

[0040] The utility model will be further described below in combination with the drawings and examples.

[0041] Examples

[0042] The ebullated bed hydrogenation reaction system of the example, as shown in Figure 1 , includes: a catalyst filling unit 100, a first reaction feed pipeline 200, a mixing unit 300, a second reaction feed pipeline 400, and an ebullated bed reactor 500;

[0043] The catalyst filling unit 100 is used to deliver the oily catalyst to the mixing unit 300;

[0044] The first reaction feed pipeline 200 is used to deliver the reaction raw material to the mixing unit 300;

[0045] The mixing unit 300 is used to mix the oil-based catalyst and the reaction raw material, and deliver them to the ebullated bed reactor 500;

[0046] The ebullated bed reactor 500 is used to make the reaction raw material perform hydrogenation reaction under the catalysis of the oil-based catalyst.

[0047] The catalyst filling unit 100 comprises a catalyst buffer tank 101 and a catalyst metering pump 102;

[0048] The inlet of the catalyst buffer tank 101 is connected with a catalyst boundary line 103, and the outlet of the catalyst buffer tank 101 is communicated with the inlet of the catalyst metering pump 102 through a metering pump inlet pipeline 104, the catalyst buffer tank 101 is used to buffer and store the oil-based catalyst delivered by the catalyst boundary line 103, and deliver the oil-based catalyst to the catalyst metering pump 102 through the metering pump inlet pipeline 104;

[0049] The outlet of the catalyst metering pump 102 is communicated with the mixing unit 300 through a metering pump outlet pipeline 105, the catalyst metering pump 102 is used to meter the mass of the oil-based catalyst, so as to deliver the oil-based catalyst with a target mass to the mixing unit 300 through the metering pump outlet pipeline 105.

[0050] The mixing unit 300 comprises a static mixer 201 and a reaction feed pump 202;

[0051] The first inlet of the static mixer 201 is communicated with the catalyst metering pump 102, the second inlet of the static mixer 201 is communicated with the first reaction feed pipeline 200, and the outlet of the static mixer 201 is communicated with the inlet of the reaction feed pump 202; the static mixer 201 is used to preliminarily mix the oil-based catalyst and the reaction raw material;

[0052] The reaction feed pump 202 is used to fully mix the preliminarily mixed oil-based catalyst and reaction raw material to form a mixed feed.

[0053] The ebullated bed hydrogenation reaction system further comprises a heating heat exchange unit 600;

[0054] The inlet of the heating heat exchange unit 600 is communicated with the outlet of the reaction feed pump 202, and the outlet of the heating heat exchange unit 600 is communicated with the ebullated bed reactor 500 through the second reaction feed pipeline 400; the heating heat exchange unit 600 is used for heating the mixed feed delivered by the reaction feed pump 202, and delivering the heated mixed feed to the ebullated bed reactor 500 through the second reaction feed pipeline 400.

[0055] As shown in Figure 2 and Figure 4 The ebullated bed reactor 500 comprises:

[0056] A reactor body 501, which has a reaction cavity 502 inside, and the second reaction feed pipeline 400 is communicated with the bottom of the reaction cavity;

[0057] A reflux cup 503 arranged at the upper part of the reaction cavity;

[0058] The reflux cup 503 comprises:

[0059] A cup wall 5031 in the shape of a funnel; the reflux cup 503 divides the reaction cavity 502 into a first chamber 5021 below the cup wall and a second chamber 5022 above the cup wall, and the mixed feed is located in the first chamber 5021;

[0060] A riser 5032 located in the second chamber 5022; the first end of the riser 5032 is connected with the cup wall 5031 and communicated with the first chamber 5021, and the second end of the riser 5032 extends away from the cup wall 5031;

[0061] The riser 5032 is through from the first end to the second end, so that the flow path of the reaction gas in the riser 5032 is linear.

[0062] The following specific experiments are carried out:

[0063] (1) A heavy oil with high metal content and carbon residue, which is equivalent to the ebullated bed hydrogenation, is selected as the raw material for a continuous reaction of 1000 hours. In this application, a mature oil-soluble nano catalyst (active metal is molybdenum and nickel, and the particle size is controlled in the range of 1-100 nanometers after sulfidation) is mixed with the heavy oil at a concentration of 200 ppm, the reaction temperature is set to 440℃, the pressure is 20 MPa, and the hydrogen to oil ratio is ensured to be > 250:1.

[0064] After application, the conversion rate of heavy oil is stabilized at more than 80%, and the fluctuation rate of overall temperature, temperature rise, density, temperature difference and other parameters in the reactor is obviously lower than that of the traditional solid catalyst, ensuring the high efficiency and stability of the reaction.

[0065] (2) Higher metal content heavy oil which cannot be processed by ebullated bed hydrogenation is selected as raw material, and continuous reaction for 1000 hours is carried out. In the application, the oil-soluble nanocatalyst is mixed with heavy oil at a concentration of 200 ppm, the reaction temperature is set to 440 DEG C, the pressure is 20 MPa, and the hydrogen oil ratio is ensured to be > 250:1.

[0066] After application, the conversion rate of heavy oil is still stabilized at 78%, and the fluctuation rate of overall temperature, temperature rise, density, temperature difference and other parameters in the reactor is obviously lower than that of the traditional solid catalyst, which proves that the structure of the patent is well matched with the oil-soluble catalyst and has stronger adaptability to raw materials.

[0067] Economic analysis:

[0068] 1. Reduced operation cost: In addition to the reduced cost of oil-soluble catalyst itself, the traditional catalyst has a complex loading and unloading process, which requires a lot of manpower and material resources. The low-pressure continuous injection system greatly simplifies the operation process. This reduces the time and labor intensity of manual operation, and also reduces the maintenance cost of the equipment, because the simplified operation process also has relatively small damage to the equipment.

[0069] 2. Increase product yield: The improvement of reaction efficiency directly leads to the increase of product yield, thereby enhancing the overall economic benefit. For example, under the same raw material and reaction conditions, more products can be obtained by using the method of the present application, thereby improving the production capacity and market competitiveness of the enterprise.

[0070] Conclusion:

[0071] The utility model provides a kind of ebullated bed hydrogenation reactor based on oil-soluble nanocatalyst, can significantly improve conversion rate in heavy oil treatment, avoid catalyst deactivation, cancel catalyst loading and unloading operation, enhance the safety of system. Experimental results show that the utility model not only has higher reaction efficiency and economy, but also has good raw material adaptability, provides a new solution for heavy oil treatment technology in oil refining and chemical industry.

[0072] The above examples are only used to illustrate the technical solutions of the present application, and are not intended to limit the protection scope of the present application. Obviously, the described examples are only some of the embodiments of the present application, not all the embodiments. Based on these examples, all other embodiments obtained by those of ordinary skill in the art without creative labor fall within the scope of the present application. Although the present application has been described in detail with reference to the above examples, those of ordinary skill in the art can still combine, add or delete the features in the embodiments of the present application according to the circumstances without creative labor, so as to obtain different other technical solutions which do not deviate from the concept of the present application in essence, and these technical solutions also fall within the scope of the present application.

Claims

1. An ebullated bed hydroreaction system, characterized by The application relates to a boiling bed hydrogenation reaction system. The boiling bed hydrogenation reaction system comprises a catalyst filling unit (100), a first reaction feed pipeline (200), a mixing unit (300), a second reaction feed pipeline (400) and a boiling bed reactor (500). The catalyst filling unit (100) and the first reaction feed pipeline (200) are connected with the mixing unit (300) respectively. The mixing unit (300) is connected with the boiling bed reactor (500) through the second reaction feed pipeline. The boiling bed reactor (500) comprises a reactor main body (501) with a reaction cavity (502) inside, wherein the second reaction feed pipeline (400) is communicated with the bottom of the reaction cavity. A reflux cup (503) is arranged at the upper part of the reaction cavity. The reflux cup (503) comprises a cup wall (5031) which is funnel-shaped, and the reflux cup (503) divides the reaction cavity (502) into a first cavity (5021) below the cup wall and a second cavity (5022) above the cup wall, wherein the mixed feed is arranged in the first cavity (5021). A riser pipe (5032) is arranged in the second cavity (5022), wherein the first end of the riser pipe (5032) is connected with the cup wall (5031) and communicated with the first cavity (5021), and the second end of the riser pipe (5032) extends away from the cup wall (5031). The riser pipe (5032) is through from the first end to the second end, so that the flow path of the reaction gas in the riser pipe (5032) is linear. The catalyst filling unit (100) comprises a catalyst buffer tank (101) and a catalyst metering pump (102) which are connected in sequence. The inlet of the catalyst buffer tank (101) is connected with a pipeline which enters from a catalyst boundary line (103), the outlet of the catalyst buffer tank (101) is communicated with the inlet of the catalyst metering pump (102) through a metering pump inlet pipeline (104), and the outlet of the catalyst metering pump (102) is communicated with the mixing unit (300) through a metering pump outlet pipeline (105).

2. A fluidized bed hydroreactor system as set forth in claim 1 wherein, The mixing unit (300) comprises a static mixer (201) and a reaction feed pump (202). The first inlet of the static mixer (201) is connected with the metering pump outlet pipeline (105), the second inlet of the static mixer (201) is communicated with the first reaction feed pipeline (200), and the outlet of the static mixer (201) is communicated with the inlet of the reaction feed pump (202). The boiling bed hydrogenation reaction system further comprises a heating and heat exchange unit (600).

3. A fluidized bed hydroreactor system as set forth in claim 2 wherein, The inlet of the heating and heat exchange unit (600) is communicated with the outlet of the reaction feed pump (202), and the outlet of the heating and heat exchange unit (600) is communicated with the boiling bed reactor (500) through the second reaction feed pipeline (400). ​ 4. A fluidized bed hydroreactor system as set forth in claim 3 wherein, ​ ​

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