A device for preparing coal-based environmentally friendly solvent oil

Abstract

A device for preparing coal-based environmentally friendly solvent oil includes a raw material tank, the outlet of the raw material tank is connected to a suspended bed feed pump and then divided into two paths, one path returns to the raw material tank, and the other path is mixed with hydrogen to a suspended bed reactor; the top of the suspended bed reactor is connected to the top of a hot high fractionator I, the top of the hot high fractionator I is connected to the top of a cold high fractionator, and the cold high fraction liquid phase component is connected to a light oil tank; the light oil tank is connected to a fixed bed feed pump; the fixed bed feed pump is connected to the top of a fixed bed hydrofining reactor, and the bottom of the fixed bed hydrofining reactor is connected to the top of a fixed bed isomerization reactor; the bottom of the fixed bed isomerization reactor is connected to a hot high fractionator II, the top of the hot high fractionator II is connected to a demister, and the bottom of the hot high fractionator II is connected to a stripping tower; the top of the stripping tower is connected to a cooler, the bottom of the stripping tower is connected to a product tank, and the product tank is connected to a distillation tower. The utility model realizes efficient utilization of raw materials and broadens the clean preparation method of products.

Description

Technical Field

[0001] The utility model belongs to the technical field of kerosene hydrogenation co-refining, and specifically relates to a device for preparing coal-based environmentally friendly solvent oil. Background Art

[0002] Coal-based derivative oil production technology can simultaneously achieve efficient and clean utilization of coal and lightweight processing of heavy and inferior oil. Compared with single coal direct liquefaction or heavy and inferior oil hydrogenation technology, it can fully utilize the synergistic effect between coal and oil. At present, coal-based derivative oil is still mainly used to produce gasoline and diesel products, with a single product structure. The field has attached great importance to the research of production technologies including aerospace fuel, aviation fuel, and military diesel, but the above-mentioned products are ultimately fuel-type products and have not been able to achieve the utilization of fuel raw materials.

[0003] Kerosene co-refining units currently mainly produce conventional fuel oils such as diesel and naphtha, which have low profits and insufficient competitiveness, and cannot effectively bring into play the characteristics of kerosene co-refining products.

[0004] The patent "A kerosene co-refining method and device" with authorization announcement number CN 106433775B describes the production of liquid fuel by co-refining kerosene. The defect is that the method and device do not expand the utilization value of the product. It is still a single technical path for conventional kerosene co-refining to produce fuel oil, and fails to realize the utilization of fuel raw materials. Summary of the invention

[0005] In order to overcome the above technical problems, the purpose of the utility model is to provide a device for preparing coal-based environmentally friendly solvent oil. The device utilizes suspended bed hydrogenation technology to hydrogenate heavy and inferior oil and coal to obtain light diesel, and then utilizes fixed bed hydrorefining and fixed bed isomerization to improve the quality and value of the oil, thereby achieving efficient utilization of raw materials and broadening the clean production path of products.

[0006] In order to achieve the above purpose, the technical solution adopted by the utility model is:

[0007] A device for preparing coal-based environmentally friendly solvent oil, comprising a raw material tank, wherein the outlet of the raw material tank is connected to a suspended bed feed pump through an inlet valve of the suspended bed feed pump, and the suspended bed feed pump is divided into two paths, one path is returned to the raw material tank through the outlet valve of the suspended bed feed pump and the return valve of the suspended bed feed pump, and the other path is mixed with hydrogen to the inlet of the suspended bed reactor;

[0008] The top outlet of the suspension bed reactor is connected to the top inlet of the hot high fractionator I, the top outlet of the hot high fractionator I is connected to the top inlet of the cold high fractionator, and the liquid phase component outlet of the cold high fractionator is connected to the inlet of the light oil tank;

[0009] The light oil tank outlet is connected to the fixed bed feed pump inlet through the fixed bed feed pump inlet valve; the fixed bed feed pump outlet is connected to the top inlet of the fixed bed hydrofining reactor through the fixed bed feed pump outlet valve, and the bottom outlet of the fixed bed hydrofining reactor is connected to the top inlet of the fixed bed isomerization reactor through the bottom discharge valve of the fixed bed hydrofining reactor;

[0010] The bottom outlet of the fixed bed isomerization reactor is connected to the inlet of the thermal high fractionator II, the top outlet of the thermal high fractionator II is connected to the inlet of the demister, and the bottom outlet of the thermal high fractionator II is connected to the stripping tower;

[0011] The top outlet of the stripping tower is connected to the cooler, the bottom outlet of the stripping tower is connected to the inlet of the product tank, and the outlet of the product tank is connected to the inlet of the distillation tower.

[0012] The top outlet of the cold high pressure separator is connected to the inlet of the light oil tank through the first and second cold high pressure separator bottom pressure reducing valves;

[0013] The bottom outlet of the thermal high fractionator II is connected to the stripping tower through the bottom outlet valve 1 of the thermal high fractionator II, the bottom outlet valve 2 of the thermal high fractionator II, and the bottom outlet valve 3 of the thermal high fractionator II.

[0014] Pressure reducing valve three and pressure reducing valve four are arranged on the liquid phase discharge pipeline at the bottom of the thermal high separation I.

[0015] The gas phase output end of the top of the cold high fractionator is divided into two paths, one path returns to the inlet of the suspended bed reactor for recycling, and the other path goes to the flare network through the second check valve, the first pipeline valve, and the second pipeline valve.

[0016] The gas phase in the demister passes through vent valve 1, vent valve 2, and vent valve 3 to the torch, and the condensate enters the cooler through the condensate cut-off valve and the one-way valve 1.

[0017] The outlet of the suspended bed feed pump and the outlet of the fixed bed feed pump are both provided with return lines.

[0018] The thermal high separation I is provided with a thermal high separation I liquid level display, and the thermal high separation I liquid level display and the thermal high separation I bottom pressure reducing valve are in three cascade stages;

[0019] A cold high separation level display is arranged on the cold high separation, and the cold high separation level display is in series with the cold high separation bottom pressure reducing valve;

[0020] A heat high separation II liquid level display is arranged on the heat high separation II, and the heat high separation II liquid level display is connected in series with the pressure reducing valve at the bottom of the heat high separation II; a stripping tower liquid level display is arranged on the stripping tower, and the stripping tower liquid level display is connected in series with the outlet valve at the bottom of the stripping tower.

[0021] Beneficial effects of the utility model:

[0022] The utility model utilizes the suspended bed hydrogenation technology to hydrogenate and co-refine heavy low-quality oil and coal to obtain light diesel, and then utilizes the fixed bed hydrogenation refining and fixed bed isomerization to improve the quality and value of the oil products, which not only solves the problem of efficient utilization of raw materials, but also broadens the way to cleanly produce products. It realizes the use of coal-based derivative oil as fuel raw material and broadens the utilization value of coal-based derivative oil;

[0023] The device uses three core devices: suspended bed, fixed bed and distillation tower, to combine heavy and low-quality oil and coal, realize hydrogenation co-refining to produce environmentally friendly solvent oil, break the traditional idea of ​​kerosene co-refining to produce liquid fuel, improve the economic benefits of the device, and provide technical support for kerosene co-refining.

[0024] The device connects the light oil tank and the fixed-bed hydrotreating reactor through a fixed-bed feed pump, couples the suspended-bed hydrogenation process with the fixed-bed hydrogenation process, and realizes the entire process from raw materials to final products.

[0025] The device is not only equipped with a fixed-bed hydrorefining reactor to remove impurities such as S\N\O from the raw materials, but also with a product stripping tower to further improve the quality of the product, thereby achieving the quality requirements of environmentally friendly solvent oil. BRIEF DESCRIPTION OF THE DRAWINGS

[0026] Figure 1 It is a schematic diagram of the structure of the utility model.

[0027] 1. Raw material tank; 2. Suspended bed reactor; 3. Hot high fractionator I; 4. Cold high fractionator; 5. Light oil tank; 6. Fixed bed hydrotreating reactor; 7. Fixed bed isomerization reactor; 8. Hot high fractionator II; 9. Demister; 10. Stripping tower; 11. Cooler; 12. Product tank; 13. Distillation tower; 14. Suspended bed feed pump; 15. Fixed bed feed pump 16. Agitator; 17. Hydrogen main valve; 18. Check valve; 19. Suspended bed feed Pump inlet valve; 20. Suspended bed feed pump outlet valve; 21. Suspended bed feed pump return valve; 22. Hydrogen to suspended bed reactor inlet valve; 23. Hot high separation I bottom pressure reducing valve; 24. Hot high separation I bottom pressure reducing valve; 25. Cold high separation bottom pressure reducing valve; 26. Cold high separation bottom pressure reducing valve; 27. Cold high separation top outlet circulation line cut-off valve; 28. Check valve; 29. ​​Fixed bed feed pump inlet valve; 30. Fixed bed feed pump outlet valve; 31. Fixed bed feed pump return valve; 32. Fixed bed hydrotreating reactor bottom discharge valve; 33. Thermal high separation II bottom outlet valve; 34. Thermal high separation II bottom outlet valve; 35. Thermal high separation II bottom outlet valve; 36. Stripping tower bottom outlet valve; 37. Defogger top vent valve; 38. Defogger top vent valve; 39. Defogger top vent valve; 40. Condensate shut-off valve; 41. Check valve; 42. Product tank inlet valve; 43. Product tank outlet valve Inlet valve; 44. Hot high separation I liquid level display; 45. Cold high separation liquid level display; 46. Hot high separation II liquid level display; 47. Stripping tower liquid level display; 48. Product tank liquid level display; 49. Light oil tank liquid level display; 50. One-way valve from the top outlet of cold high separation to the flare pipeline; 51. Valve from the top outlet of cold high separation to the flare pipeline; 52. Valve from the top outlet of cold high separation to the flare pipeline; 53. Pressure display one; 54. Pressure display two. DETAILED DESCRIPTION

[0028] The utility model is further described in detail below in conjunction with the accompanying drawings.

[0029] like Figure 1 As shown, a device for preparing coal-based environmentally friendly solvent oil includes a raw material tank 1, the outlet of the raw material tank 1 is connected to a suspended bed feed pump 14 through a suspended bed feed pump inlet valve 19, and the suspended bed feed pump 14 is divided into two paths, one path returns to the raw material tank 1 through a suspended bed feed pump outlet valve 20 and a suspended bed feed pump return valve 21, and the other path is mixed with hydrogen to the inlet of a suspended bed reactor 2;

[0030] The top outlet of the suspension bed reactor 2 is connected to the top inlet of the hot high fractionator I 3, the top outlet of the hot high fractionator I 3 is connected to the top inlet of the cold high fractionator 4, and the liquid component outlet of the cold high fractionator 4 is connected to the inlet of the light oil tank 5;

[0031] The outlet of the light oil tank 5 is connected to the inlet of the fixed bed feed pump 15 through the fixed bed feed pump inlet valve 29; a light oil tank liquid level display 49 is provided on the light oil tank 5;

[0032] The outlet of the fixed bed feed pump 15 is divided into two paths through the fixed bed feed pump outlet valve 30, one path is connected to the top inlet of the fixed bed hydrofining reactor 6, and the other path is connected to the light oil tank 5 through the fixed bed feed pump return valve 31. The bottom outlet of the fixed bed hydrofining reactor 6 is connected to the top inlet of the fixed bed isomerization reactor 7 through the bottom discharge valve 32 of the fixed bed hydrofining reactor;

[0033] The bottom outlet of the fixed bed isomerization reactor 7 is connected to the inlet of the thermal high fractionator II 8, the top outlet of the thermal high fractionator II 8 is connected to the inlet of the demister 9, and the bottom outlet of the thermal high fractionator II 8 is connected to the stripping tower 10;

[0034] The top outlet of the stripping tower 10 is connected to the cooler 11, the bottom outlet of the stripping tower 10 is connected to the inlet of the product tank 12, and the outlet of the product tank 12 is connected to the inlet of the distillation tower 13. The product tank 12 is provided with a product tank liquid level display 48.

[0035] The bottom outlet of the cold high pressure separator 4 is connected to the inlet of the light oil tank 5 through a cold high pressure separator bottom pressure reducing valve 1 25 and a cold high pressure separator bottom pressure reducing valve 26;

[0036] The bottom outlet of the thermal high separation II 8 is connected to the stripping tower 10 through a thermal high separation II bottom outlet valve 1 33, a thermal high separation II bottom outlet valve 2 34, and a thermal high separation II bottom outlet valve 35.

[0037] A pressure reducing valve 3 23 and a pressure reducing valve 4 24 are arranged on the liquid phase discharge pipeline at the bottom of the hot high separation I3.

[0038] The gas phase output end of the top of the cold high fractionator 4 is divided into two paths, one path returns to the entrance of the suspended bed reactor 2 for recycling, and the pipeline is provided with a cold high fractionator top outlet circulation line cut-off valve 27 and a one-way valve 28, and the other path goes to the flare network through a pressure display 1 53, a one-way valve 2 50, a pipeline valve 1 51, and a pipeline valve 2 52. The pipeline valve 1 51 is connected to a pressure display 1 53 through a pipeline.

[0039] The gas phase in the demister 9 reaches the flare through pressure indicator 2 54, vent valve 1 37, vent valve 2 38, and vent valve 3 39. Vent valve 2 38 is connected to pressure indicator 2 54, and the condensate enters the cooler 11 through the condensate cut-off valve 40 and the one-way valve 1 41.

[0040] The outlets of the suspended bed feed pump 14 and the fixed bed feed pump 15 are both provided with return lines.

[0041] The said heat high separation I 3 is provided with a heat high separation I liquid level display 44, and the heat high separation I liquid level display 44 is connected in series with the heat high separation I bottom pressure reducing valve three 23;

[0042] A cold high separation liquid level display 45 is provided on the cold high separation 4, and the cold high separation liquid level display 45 is cascaded with a cold high separation bottom pressure reducing valve 25;

[0043] A heat high separation II liquid level display 46 is provided on the heat high separation II 8, and the heat high separation II liquid level display 46 is in series with the heat high separation II bottom pressure reducing valve 34; a stripping tower liquid level display 47 is provided on the stripping tower 10, and the stripping tower liquid level display 47 is in series with the stripping tower bottom outlet valve 36.

[0044] The working principle of this utility model:

[0045] Low-metamorphosis bituminous coal, catalyst, and high-aromatic heavy oil are added to the raw material tank in proportion (mass ratio) (oil: coal = 7:3), the catalyst addition amount accounts for 1% of the raw material mass, the stirrer 16 is turned on, and after the raw materials are evenly stirred, the suspended bed feed pump 14 is started. The raw materials are mixed with hydrogen through valve 19, suspended bed feed pump 14, valve 20, and then enter the suspended bed reactor 2. After the raw materials are fully reacted in the suspended bed reactor 2, they enter the inlet of the hot high fractionator I3 at the top of the suspended bed reactor 2. After the materials are thermally separated in the hot high fractionator I3, the liquid phase is discharged through the pressure reducing valve three 23 and the pressure reducing valve four 24, and the gaseous phase components enter the cold high fractionator 4 from the top outlet of the hot high fractionator I3; the gaseous phase components after the gas-liquid separation of the cold high fractionator 4 are divided into two paths from the top outlet of the cold high fractionator 4, one path returns to the inlet of the suspended bed reactor 2 for recycling, and the other path goes to the flare network through the one-way valve two 50, the pipeline valve one 51, and the pipeline valve two 52; the liquid phase components enter the light oil tank 5 from the bottom of the cold high fractionator 4 through the pressure reducing valve one 25 and the pressure reducing valve two 26 for collection. After the liquid level of the light oil tank 5 is greater than 50%, the fixed bed feed pump 15 is started, and the light oil is mixed with hydrogen through the valve 29, the fixed bed feed pump 15, and the valve 30 and enters the fixed bed hydrofining reactor 6. After the removal of sulfur, nitrogen, oxygen, olefin saturation, aromatic saturation and other reactions in the fixed bed hydrofining reactor 6, the light oil enters the fixed bed isomerization reactor 7 for isomerization reaction. The product oil flows out from the bottom of the fixed bed isomerization reactor 7 and enters the hot high separation II 8 for gas-liquid separation. The gas phase passes through the demister 9, Vent valve 1 37, vent valve 2 38, vent valve 3 39 go to the flare (the condensate enters the cooler 11 through the condensate cut-off valve 40 and the one-way valve 1 41), the liquid phase enters the inlet end of the stripping tower 10 through valve 33, valve 34, valve 35 from the bottom of the hot high fractionator II 8, and the product oil after stripping passes through the bottom outlet of the stripping tower 10 through valve 36 and valve 42 to the product tank 12; when the liquid level in the product tank 12 is greater than 50%, open valve 43 to enter the distillation tower 13 to collect the 120-180℃ fraction oil.

[0046] The equipment are connected by pipelines and valves.

[0047] The hydrogen is divided into two parts after passing through valve 17 and one-way valve 18. One part goes to the inlet of the suspended bed reactor 2 through valve 22; and the other part goes to the inlet of the fixed bed hydrotreating reactor 6.

[0048] The outlets of the suspended bed feed pump 14 and the fixed bed feed pump 15 are both provided with return lines, the purpose of which is to make the material mixing more uniform and to prevent the pump outlet flow rate from fluctuating.

[0049] The temperature of the raw material tank 1 is controlled at 80-90°C, the temperature of the suspended bed reactor 2 is controlled at 460-470°C, the pressure is controlled at 18-20Mpa, the air velocity is controlled at 0.5h-1, the hydrogen-oil ratio is controlled at 1500-2000NL / kg, the hot high fraction liquid level is controlled at 30%, and the cold high fraction liquid level is controlled at 30%; the fixed bed reaction temperature is controlled at 360-370°C, the pressure is controlled at 16-18Mpa, the air velocity is controlled at 0.5h-1, the hydrogen-oil ratio is controlled at 1000-1100NL / kg, the hot high fraction liquid level is controlled at 30%, and the stripping tower liquid level is controlled at 30%. The above control parameters can make the device run more smoothly, with higher product yield and better product quality.

[0050] Valve 51 controls the pressure of suspended bed reactor 2, hot high fractionator I 3, and cold high fractionator 4 at 18-20 MPa, and valve 35 controls the pressure of fixed bed hydrotreating reactor 6, fixed bed isomerization reactor 7, and hot high fractionator II 8 at 16-18 MPa.

[0051] The hot high separation I liquid level display 44 is set to 30%, and is cascaded with the hot high separation I bottom pressure reducing valve three 23; the cold high separation liquid level display 45 is set to 30%, and is cascaded with the cold high separation bottom pressure reducing valve one 25; the hot high separation II liquid level display 46 is set to 30%, and is cascaded with the hot high separation II bottom pressure reducing valve 34; the stripping tower liquid level display 47 is set to 20, and is cascaded with the stripping tower bottom outlet valve 36. The above purpose realizes the automation of the device and ensures the smooth operation of the device.

[0052] The outer walls of the raw material tank 1, suspended bed reactor 2, thermal high fractionator I 3, thermal high fractionator II 8, fixed bed hydrotreating reactor 6 and fixed bed isomerization reactor 7 are all equipped with electric heating jackets to meet the heating needs of various equipment.

Claims

1. A device for preparing coal-based environmentally friendly solvent oil, characterized in that: The invention comprises a raw material tank (1), wherein the outlet of the raw material tank (1) is connected to a suspended bed feed pump (14) via a suspended bed feed pump inlet valve (19), and the suspended bed feed pump (14) is divided into two paths, one path is returned to the raw material tank (1) via a suspended bed feed pump outlet valve (20) and a suspended bed feed pump return valve (21), and the other path is mixed with hydrogen and reaches the inlet of a suspended bed reactor (2); The top outlet of the suspended bed reactor (2) is connected to the top inlet of the hot high fractionator I (3), the top outlet of the hot high fractionator I (3) is connected to the top inlet of the cold high fractionator (4), and the liquid component outlet of the cold high fractionator (4) is connected to the inlet of the light oil tank (5); The outlet of the light oil tank (5) is connected to the inlet of the fixed bed feed pump (15) via the fixed bed feed pump inlet valve (29); the outlet of the fixed bed feed pump (15) is connected to the top inlet of the fixed bed hydrotreating reactor (6) via the fixed bed feed pump outlet valve (30); the bottom outlet of the fixed bed hydrotreating reactor (6) is connected to the top inlet of the fixed bed isomerization reactor (7) via the bottom discharge valve (32) of the fixed bed hydrotreating reactor; The bottom outlet of the fixed bed isomerization reactor (7) is connected to the inlet of the thermal high fractionator II (8), the top outlet of the thermal high fractionator II (8) is connected to the inlet of the demister (9), and the bottom outlet of the thermal high fractionator II (8) is connected to the stripping tower (10); The top outlet of the stripping tower (10) is connected to the cooler (11), the bottom outlet of the stripping tower (10) is connected to the inlet of the product tank (12), and the outlet of the product tank (12) is connected to the inlet of the distillation tower (13).

2. The device for preparing coal-based environmentally friendly solvent oil according to claim 1, characterized in that: The top outlet of the cold high pressure separator (4) is connected to the inlet of the light oil tank (5) via a cold high pressure separator bottom pressure reducing valve 1 (25) and a cold high pressure separator bottom pressure reducing valve 2 (26); The bottom outlet of the thermal high fractionator II (8) is connected to the stripping tower (10) via a thermal high fractionator II bottom outlet valve 1 (33), a thermal high fractionator II bottom outlet valve 2 (34), and a thermal high fractionator II bottom outlet valve 3 (35); A pressure reducing valve 3 (23) and a pressure reducing valve 4 (24) are arranged on the liquid phase discharge pipeline at the bottom of the thermal high separation I (3).

3. The device for preparing coal-based environmentally friendly solvent oil according to claim 1, characterized in that: The gas phase output end at the top of the cold high fractionator (4) is divided into two paths, one path is returned to the inlet of the suspended bed reactor (2) for recycling, and the other path is sent to the flare network through the one-way valve 2 (50), the pipeline valve 1 (51), and the pipeline valve 2 (52).

4. The device for preparing coal-based environmentally friendly solvent oil according to claim 1, characterized in that: The gas phase in the demister (9) passes through the vent valve 1 (37), the vent valve 2 (38), and the vent valve 3 (39) to the flare, and the condensate enters the cooler (11) through the condensate cut-off valve (40) and the one-way valve 1 (41).

5. The device for preparing coal-based environmentally friendly solvent oil according to claim 1, characterized in that: The outlets of the suspended bed feed pump (14) and the fixed bed feed pump (15) are both provided with return lines.

6. The device for preparing coal-based environmentally friendly solvent oil according to claim 1, characterized in that: A heat high separation I liquid level display (44) is arranged on the heat high separation I (3), and the heat high separation I liquid level display (44) is connected in series with the heat high separation I bottom pressure reducing valve 3 (23).

7. The device for preparing coal-based environmentally friendly solvent oil according to claim 1, characterized in that: A cold high fraction liquid level display (45) is provided on the cold high fraction (4), and the cold high fraction liquid level display (45) is connected in series with a cold high fraction bottom pressure reducing valve (25); A heat high separation II liquid level display (46) is provided on the heat high separation II (8), and the heat high separation II liquid level display (46) is connected in series with the heat high separation II bottom outlet valve 2 (34); a stripping tower liquid level display (47) is provided on the stripping tower (10), and the stripping tower liquid level display (47) is connected in series with the stripping tower bottom outlet valve (36).

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