Slurry reactor diesel oil processing device and method thereof

Abstract

The invention discloses a slurry reactor diesel oil processing device and method. The slurry reactor diesel oil processing device comprises a raw material buffer tank, and a feeding port of the raw material buffer tank is connected with a plurality of feeding pipelines so that various raw materials can form a mixed raw material; mixing the mixed straight-run diesel oil, normal three-line diesel oil, slurry bed diesel oil and catalytic diesel oil to form a mixed raw material; mixing the mixed raw material with hydrogen, pressurizing to 8.5 MPa, heating to 340-380 DEG C, and feeding into a hydrofining reactor to obtain a reaction product; carrying out gas-liquid separation on the obtained refined reaction product in a system consisting of a hot high-pressure separator, a hot low-pressure separator, a cold high-pressure separator and a cold low-pressure separator to obtain reaction generated oil; obtained reaction generated oil enters a stripping tower to remove hydrogen sulfide and then enters a fractionating tower; and naphtha and refined diesel oil are obtained from the top of the fractionating tower, so that the production flexibility of the device is improved, the product benefit is improved, the production cost is reduced, and the purposes of refinery operation optimization and benefit improvement are achieved.

Description

Technical Field

[0001] The present invention relates to a processing device and a method thereof, and more specifically, to a slurry bed diesel processing device and a method thereof, and belongs to the field of petrochemical industry. Background Art

[0002] Slurry bed residue oil hydrotreating units are increasingly widely used in petrochemical production processes due to their high residue oil conversion rate and high yield of value-added products. There are two main design and processing routes for existing slurry bed diesel. One is to enter the diesel hydrocracking unit to increase the production of heavy naphtha, light naphtha, liquefied gas and other ethylene raw materials; the other is to enter the diesel reforming unit to produce diesel blending components. Slurry bed diesel has a high aromatic content, and entering the diesel cracking will affect the temperature rise of the reactor bed, thereby restricting the reaction depth. After entering the diesel reforming unit, the density and viscosity of the raw materials will be greatly reduced, and the indicators of the diesel blending components will be reduced, resulting in the loss of key property indicators such as density and viscosity. Summary of the invention

[0003] In order to solve the above-mentioned problems of the prior art, the present invention provides a slurry bed diesel processing device and method thereof having the technical characteristics of simple structural design and ensuring that after the slurry bed diesel is hydrogenated, the density and viscosity loss of the hydrogenated diesel is small compared with the raw material.

[0004] In order to achieve the above object, the present invention is implemented by the following technical solutions:

[0005] A slurry bed diesel processing device comprises a raw material buffer tank, wherein a feed inlet of the raw material buffer tank is connected to a plurality of feed pipelines to form a mixed raw material from a plurality of raw materials;

[0006] The discharge port of the raw material buffer tank is connected to a feed pump, a reaction feed heating furnace, and a hydrofining reactor in sequence through pipelines. The bottom of the hydrofining reactor is connected to the middle of a hot high fractionator. The upper end of the hot high fractionator is connected to a cold high fractionator through a pipeline. The lower end of the hot high fractionator is connected to a hot low fractionator. The lower end of the hot low fractionator is connected to the middle of a stripping tower through a pipeline. The lower end of the cold high fractionator and the upper end of the hot low fractionator are connected to the upper end of the cold low fractionator. The lower end of the cold low fractionator is connected to the upper end of the stripping tower through a pipeline. The stripping tower has a bottom portion, a reboiler at the bottom of the distillation tower, a circulating pump, and a refined diesel discharge pump connected in sequence through pipelines between the 46 sections of the distillation tower. The stripping tower has a bottom portion, a reboiler at the bottom of the distillation tower, a circulating pump, and a refined diesel discharge pump connected in sequence through pipelines ...

[0007] Preferably, there are four feed pipelines, which respectively convey pipeline No. 1 for mixed straight-run diesel, pipeline No. 2 for conventional three-line diesel, pipeline No. 3 for slurry bed diesel, and pipeline No. 4 for catalytic diesel.

[0008] Preferably, the upper end of the cold high fraction is connected to the upper end of the hydrotreating reactor through a circulating hydrogen pipeline.

[0009] The present invention provides a slurry bed diesel processing method, which comprises the following steps:

[0010] Step 1: Mix straight-run diesel, conventional three-line diesel, slurry bed diesel, and catalytic diesel to form a mixed raw material; wherein the ratio of the mixed straight-run diesel, conventional three-line diesel, slurry bed diesel, and catalytic diesel is 30-50:10-30:20-40:5-15;

[0011] Step 2: After the mixed raw material is mixed with hydrogen, it is pressurized to 8.5MPa, heated to 340℃~380℃, and enters the hydrogenation refining reactor to obtain the reaction product;

[0012] Step 3: The obtained refined reaction product is subjected to gas-liquid separation in a system consisting of a hot high fraction, a hot low fraction, a cold high fraction, and a cold low fraction to obtain a reaction product oil;

[0013] Step 4: The obtained reaction product oil enters a stripping tower to remove hydrogen sulfide and then enters a fractionation tower;

[0014] Step 5: naphtha is obtained through the top of the fractionation tower and outputted by the naphtha discharge pump; refined diesel is obtained through the bottom of the fractionation tower and outputted by the refined diesel discharge pump; there is undistilled generated oil at the bottom of the fractionation tower, which is transported to the heating furnace through a circulation pump, heated to 350° C. by the heating furnace, and then enters the fractionation tower for cutting again, and the cycle operation is repeated until naphtha and refined diesel are obtained.

[0015] Preferably, the ratio of mixed straight-run diesel, conventional three-line diesel, slurry bed diesel and catalytic diesel is 40:20:30:10.

[0016] Beneficial effects: According to the material balance of the whole plant and market demand, the processing of slurry bed diesel can be flexibly switched to increase the production flexibility of the device and product benefits. It has the technical characteristics of increasing the production flexibility of the device, improving product benefits, reducing production costs, and achieving the purpose of optimizing refinery operations and improving benefits. BRIEF DESCRIPTION OF THE DRAWINGS

[0017] Figure 1 It is a schematic diagram of the overall structure of the present invention. DETAILED DESCRIPTION

[0018] The present invention will be further described below in conjunction with the accompanying drawings, but the present invention is not limited to the following embodiments.

[0019] like Figure 1 The figure shows a specific embodiment of a slurry bed diesel processing device, which is a slurry bed diesel processing device, comprising a raw material buffer tank 101, wherein a feed port of the raw material buffer tank 101 is connected to a plurality of feed pipelines to form a mixed raw material from a plurality of raw materials;

[0020] The discharge port of the raw material buffer tank 101 is connected to a feed pump, a reaction feed heating furnace 102, and a hydrotreating reactor 103 in sequence through pipelines; the bottom of the hydrocracking reactor is connected to the middle of a hot high fractionator 104; the upper end of the hot high fractionator 104 is connected to a cold high fractionator 105 through a pipeline; the lower end of the hot high fractionator 104 is connected to a hot low fractionator 106; the lower end of the hot low fractionator 106 is connected to the middle of a stripping tower 107 through a pipeline; the lower end of the cold high fractionator 105 and the upper end of the hot low fractionator 106 are connected to the upper end of a cold low fractionator 108; the lower end of the cold low fractionator 108 is connected to the upper end of the stripping tower 107 through a pipeline; the lower end of the stripping tower 107 is connected to the 31st section of a fractionating tower 109 through a pipeline; and the 46 sections of the fractionating tower 109 are connected through The pipelines are connected in sequence to the reboiler 110 at the bottom of the fractionation tower, the circulating pump, and the refined diesel discharge pump 111. The lower end of the stripping tower 107 is connected to the pipeline between the circulating pump and the discharge pump. The first section of the fractionation tower 109 is connected to a tank body through a pipeline, and the tank body is connected to a naphtha discharge pump. The outlet pipeline of the naphtha discharge pump is connected back to the first section of the fractionation tower 109 through a circulating pipeline. There are four feed pipelines, and they respectively transport the first pipeline 113 of mixed straight-run diesel, the second pipeline 114 of the three-line diesel, the third pipeline 115 of the slurry bed diesel, and the fourth pipeline 116 of the catalytic diesel. The upper end of the cold high fraction 105 is connected to the upper end of the hydrofining reactor 103 through the circulating hydrogen pipeline 112 to realize the recycling of hydrogen. From top to bottom, the fractionation tower 109 includes sections 1 to 46 marked by positive integer numbers.

[0021] The device can flexibly switch to process slurry bed diesel according to the material balance of the entire plant and market demand, thereby increasing the production flexibility and product benefits of the device.

[0022] The present invention provides a slurry bed diesel processing method, which comprises the following steps:

[0023] Step 1: Mix straight-run diesel, conventional three-line diesel, slurry bed diesel, and catalytic diesel to form a mixed raw material; the ratio of the mixed straight-run diesel, conventional three-line diesel, slurry bed diesel, and catalytic diesel is 30-50:10-30:20-40:5-15, and the specific ratio value can be the left endpoint value, the right endpoint value, the middle value, or other values ​​within the range;

[0024] Step 2: After the mixed raw material is mixed with hydrogen, it is pressurized to 8.5 MPa, heated to 340° C. to 380° C., and enters the hydrofining reactor 103 to obtain a reaction product;

[0025] Step 3: The obtained refined reaction product is subjected to gas-liquid separation in a system consisting of a hot high fraction 104, a hot low fraction 106, a cold high fraction 105, and a cold low fraction 108 to obtain a reaction product oil;

[0026] Step 4: The obtained reaction product oil enters the stripping tower 107 to remove hydrogen sulfide and then enters the fractionation tower 109;

[0027] Step 5: Naphtha is obtained through the top of the fractionation tower 109 and output by the naphtha discharge pump; refined diesel is obtained through the bottom of the fractionation tower 109 and output by the refined diesel discharge pump 111; there is undistilled generated oil at the bottom of the fractionation tower 109, which is transported to the heating furnace through a circulation pump, heated to 350°C by the heating furnace, and then enters the fractionation tower 109 for cutting again, and the cycle operation is repeated until naphtha and refined diesel are obtained.

[0028] This method has the technical characteristics of increasing the production flexibility of the device, improving product benefits, reducing production costs, achieving the purpose of optimizing refinery operations and improving benefits, and has good reference significance for the full process optimization of refineries of the same type. Specifically: it can effectively remove sulfur, nitrogen, chlorine and other impurities in slurry bed diesel, and at the same time ensure that the key properties of the hydrofined diesel product are close to those of the mixed raw materials, the product properties are controllable, and the hydrogen consumption and energy consumption are low. It is convenient for enterprises to produce diesel blending components with high density, high viscosity, high cetane number and other indicators, with flexible production and strong raw material adaptability.

[0029] Method Description:

[0030] 1. The existing process uses atmospheric and vacuum light diesel as raw material. The process of the present invention controls the mixing of 32% slurry bed diesel into atmospheric and vacuum straight-run diesel to form a mixed raw material, wherein the distribution ratio of each component in the mixed raw material is shown in Table 1, and the properties of the slurry bed diesel and the mixed raw material are shown in Table 2.

[0031]

[0032] Table 2 Properties of slurry bed diesel and mixed stock

[0033]

[0034]

[0035] 2. The mixed raw materials are pressurized and heat exchanged, mixed with hydrogen, heated to 340°C ~ 380°C and enter into a reactor filled with a refining catalyst for a hydrogenation refining reaction. Because the nitrogen content of slurry bed diesel is high, the temperature of the hydrogenation refining reaction is controlled to be about 10°C higher than that of the unprocessed slurry bed diesel. As the processing ratio increases to 5%, the temperature is gradually increased, and the reaction pressure is controlled to be the same as the pressure when the slurry bed diesel is not added.

[0036] 3. The obtained refined reaction product is subjected to gas-liquid separation in a hot and cold high and low separator, and the obtained reaction product oil enters the hydrogen sulfide stripping tower 107 to remove the hydrogen sulfide and then enters the fractionation tower 109 for cutting. Under the specific fractionation process operation, naphtha, diesel and other by-products are obtained respectively.

[0037] 4. The operating parameters of the distillation process remain unchanged to maintain the quality indicators of the products before processing slurry bed diesel.

[0038] 5. Compared with the existing process, the nitrogen content in the mixed raw materials of the process of the present invention is increased. In order to ensure that the product indicators are consistent with the existing process, the hydrogen consumption is slightly increased. The distribution of various products is basically the same as the existing process.

[0039] 6. If the slurry bed diesel is processed according to the material balance of the whole plant or market demand, it is only necessary to switch the existing process, and the production plan can be adjusted simply and flexibly.

[0040] Table 3 Comparison of operating parameters and material balance between the existing process and the process of the present invention

[0041]

[0042]

[0043] 1. A new type of raw material for diesel refining unit, slurry bed diesel, has been added.

[0044] 2. The process of the present invention realizes the conversion of inferior slurry bed diesel into refined diesel with higher added value, making slurry bed diesel a high-quality raw material for producing high-density, high-viscosity, high-cetane number diesel blending components.

[0045] 3. It can realize online switching of slurry bed diesel production scheme and increase the processing and production flexibility of the device.

[0046] 4. The energy consumption cost is much lower than the current diesel hydrocracking and diesel hydromodification, and is competitive in the market.

[0047] Finally, it should be noted that the present invention is not limited to the above embodiments, and there are many variations. All variations that can be directly derived or associated with the content disclosed by ordinary technicians in this field should be considered as the protection scope of the present invention.

Claims

1. A slurry bed diesel processing device, characterized in that: It comprises a raw material buffer tank (101), wherein a feed port of the raw material buffer tank (101) is connected to a plurality of feed pipelines to combine a plurality of raw materials into a mixed raw material; The discharge port of the raw material buffer tank (101) is connected to a feed pump, a reaction feed heating furnace (102), and a hydrofining reactor (103) in sequence through pipelines; the bottom of the hydrofining reactor (103) is connected to the middle of a hot high fractionator (104); the upper end of the hot high fractionator (104) is connected to a cold high fractionator (105) through a pipeline; the lower end of the hot high fractionator (104) is connected to a hot low fractionator (106); the lower end of the hot low fractionator (106) is connected to the middle of a stripping tower (107) through a pipeline; the lower end of the cold high fractionator (105) and the upper end of the hot low fractionator (106) are connected to the upper end of a cold low fractionator (108); The lower end is connected to the upper end of the stripping tower (107) through a pipeline, and the lower end of the stripping tower (107) is connected to the 31st section of the fractionation tower (109) through a pipeline. The 46th sections of the fractionation tower (109) are sequentially connected to the fractionation tower bottom reboiler (110), the circulation pump, and the refined diesel discharge pump (111) through pipelines. The lower end of the stripping tower (107) is connected to the pipeline between the circulation pump and the refined diesel discharge pump (111). The first section of the fractionation tower (109) is connected to a tank body through a pipeline, and the tank body is connected to a naphtha discharge pump. The outlet pipeline of the naphtha discharge pump is connected back to the first section of the fractionation tower (109) through a circulation pipeline.

2. A slurry bed diesel processing device according to claim 1, characterized in that: There are four feed pipelines, which respectively transport mixed straight-run diesel through pipeline No. 1 (113), regular three-line diesel through pipeline No. 2 (114), slurry bed diesel through pipeline No. 3 (115), and catalytic diesel through pipeline No. 4 (116).

3. A slurry bed diesel processing device according to claim 1 or 2, characterized in that: The upper end of the cold high fraction (105) is connected to the upper end of the hydrotreating reactor (103) through a circulating hydrogen pipeline (112).

4. A slurry bed diesel processing method, characterized in that The method comprises the following steps: Step 1: Mix straight-run diesel, conventional three-line diesel, slurry bed diesel, and catalytic diesel to form a mixed raw material; wherein the ratio of the mixed straight-run diesel, conventional three-line diesel, slurry bed diesel, and catalytic diesel is 30-50:10-30:20-40:5-15; Step 2: After the mixed raw material is mixed with hydrogen, it is pressurized to 8.5 MPa, heated to 340° C. to 380° C., and enters the hydrofining reactor (103) to obtain a reaction product; Step 3: The obtained refined reaction product is subjected to gas-liquid separation in a system consisting of a hot high fraction (104), a hot low fraction (106), a cold high fraction (105), and a cold low fraction (108), and the obtained reaction product oil is obtained; Step 4: The obtained reaction product oil enters the stripping tower (107) to remove hydrogen sulfide and then enters the fractionation tower (109); Step 5: naphtha is obtained through the top of the fractionation tower (109) and discharged by the naphtha discharge pump; refined diesel is obtained through the bottom of the fractionation tower (109) and discharged by the refined diesel discharge pump (111); there is undistilled generated oil at the bottom of the fractionation tower (109), which is transported to the heating furnace through a circulation pump, heated to 350° C. by the heating furnace, and then enters the fractionation tower (109) for cutting again, and the cycle operation is repeated until naphtha and refined diesel are obtained.

5. A slurry bed diesel processing method according to claim 4, characterized in that: The ratio of mixed straight-run diesel, conventional three-line diesel, slurry bed diesel and catalytic diesel is 40:20:30:10.

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