Method and installation for hydrogenation of paraffin oil
Patent Information
- Authority / Receiving Office
- KZ · KZ
- Patent Type
- Utility models
- Current Assignee / Owner
- CHINA PETROLEUM & CHEMICAL CORP
- Filing Date
- 2018-12-29
- Publication Date
- 2020-07-03
AI Technical Summary
Existing methods for paraffin oil hydration are inefficient and lack specificity in controlling the hydration process, leading to inconsistent product quality and high energy consumption.
A method involving a hydration reactor system with controlled temperature and pressure conditions, combined with a catalyst to optimize the hydration of paraffin oil, ensuring precise control over the hydration process.
Enhances the efficiency and consistency of paraffin oil hydration, reducing energy consumption and improving product quality by achieving precise control over the hydration process.
Abstract
Description
The description text is provided in facsimile form.
Claims
1. A method for hydrogenating paraffinic oil, comprising the following steps: (1) bringing paraffinic oil as a feedstock and a hydrogen-containing gas into contact with a first hydroprocessing catalyst under first hydroprocessing conditions, dividing the first hydroprocessed stream obtained as a result of the contact into two parts, i.e.a first hydrotreated stream A and a first hydrotreated stream B, and performing gas-liquid separation of the first hydrotreated stream A to obtain a first hydrotreated gas-phase stream and a first hydrotreated liquid-phase stream; (2) contacting the first hydrotreated stream B, the first hydrotreated liquid-phase stream and the hydrogen-containing gas with a second hydrotreating catalyst under second hydrotreating conditions to obtain a finished hydrotreated stream, and (3) contacting the first hydrotreated gas-phase stream and light catalytic cracking cycle oil with a hydrotreating catalyst to carry out a hydrotreating reaction under hydrotreating conditions to obtain a finished hydrotreated stream.
2. The method according to claim 1, wherein the initial boiling point of the paraffinic oil is 100-400°C, and the final boiling point of the paraffinic oil is 405-650°C; preferably, the paraffinic oil is selected from at least one material from vacuum gas oil (VGO), heavy catalytic cracking gas oil (HCCO), deasphalted oil (DAO), coal tar, direct coal liquefaction distillation product (DCDP), indirect coal liquefaction distillation product (ICDP), synthetic oil, and oil from bituminous shale.
3. The method according to claim 1, wherein the initial boiling point of the light catalytic cracking cycle oil is 100-200°C, and the final boiling point of the light catalytic cracking cycle oil is 320-400°C; preferably, the weight ratio of the light catalytic cracking cycle oil to the paraffinic oil is 0.1-3:1, more preferably 0.3-1.1:
1.
4. The method according to claim 1, in which the first hydroprocessing catalyst and the second hydroprocessing catalyst comprise a carrier and an active component, respectively and independently, wherein the active component is selected from at least one metallic element of groups VIB and / or VIII, and the carrier is aluminum oxide and / or silicon-containing aluminum oxide;preferably, based on the total weight of the first hydroprocessing catalyst and in terms of oxide, the content of the metallic element of group VIB is 10-35 wt.%, and the content of the metallic element of group VIII is 3-15 wt.%;preferably, based on the total weight of the second hydroprocessing catalyst and in terms of oxide, the content of the metallic element of group VIB is 10-35 wt.%, and the content of the metallic element of group VIII is 3-15 wt.%; preferably, the specific surface area of the first hydroprocessing catalyst is 100-650 m2 / g, and the pore volume of the first hydroprocessing catalyst is 0.15-0.6 ml / g; preferably, the specific surface area of the second hydroprocessing catalyst is 100-650 m2 / g, and the pore volume of the second hydroprocessing catalyst is 0.15-0.6 ml / g.
5. The method according to claim 1, in which the first hydroprocessing conditions and the second hydroprocessing conditions, respectively and independently, comprise: a reaction pressure of 3-19 MPa, a reaction temperature of 300-450°C, a liquid hourly space velocity of 0.2-6 h-1, and a hydrogen to oil volume ratio of 100-2000:1; preferably, the first hydroprocessing conditions and the second hydroprocessing conditions, respectively and independently, comprise: a reaction pressure of 4-17 MPa; a reaction temperature of 320-420°C, a liquid hourly space velocity of 0.4-4 h-1, and a hydrogen to oil volume ratio of 400-1500:1 6. The method according to any one of paragraphs 1-5, in which the hydrotreated gas phase stream constitutes 5-95 vol.% of the hydrogen-containing gas in step (1), preferably 10-80 vol.%.
7. The method according to any one of paragraphs 1-5, in which the first hydrotreated stream A constitutes 5-95 wt.% of the total weight of the first hydrotreated stream A and the first hydrotreated stream B, preferably 10-80 wt.%.
8. The method according to any one of paragraphs 1-5, in which the hydrotreating catalyst comprises a carrier and an active component, wherein the active component is selected from at least one of the metal elements of group VIB and / or VIII, and the carrier is aluminum oxide and / or silicon-containing aluminum oxide; preferably, based on the total weight of the hydrotreating catalyst and in terms of oxide, the content of the metal element of group VIB is 10-35 wt.%, and the content of the metal element of group VIII is 3-15 wt.%; preferably, the specific surface area of the hydrotreating catalyst is 100-650 m2 / g, and the pore volume of the hydrotreating catalyst is 0.15-0.6 ml / g; preferably, the hydrotreating conditions include: a reaction pressure of 3-19 MPa, a reaction temperature of 260-450 °C, a liquid hourly space velocity of 0.2-6 h-1, a volume ratio of hydrogen to oil 100-2000:1, more preferably the reaction temperature is 280-410°C.
9. The method according to any one of paragraphs 1-8, further comprising separating the light catalytic cracking cycle gas oil to obtain a light fraction and a heavy fraction, wherein the cutoff temperature is 245-300 °C; step (3) includes contacting the first hydrotreated gas phase stream, the heavy fraction and the hydrogen-containing gas with a first hydrotreating catalyst to carry out a first hydrotreating reaction under first hydrotreating conditions to obtain a first hydrotreated stream; then contacting the first hydrotreated stream, the light fraction and the hydrogen-containing gas with a second hydrotreating catalyst to carry out a second hydrotreating reaction under second hydrotreating conditions; preferably, the temperature of the second hydrotreating reaction is less than the temperature of the first hydrotreating reaction; even more preferably, the temperature of the second hydrotreating reaction is less than the temperature of the first hydrotreating reaction by 5-20 °C.
10. The method according to any one of paragraphs 1-9, in which step (2) further comprises processing the resulting hydrotreated stream by separation and fractionation to obtain a hydrotreated hydrogen-rich gas, a hydrotreated gas, a hydrotreated naphtha, a hydrotreated diesel fuel and a hydrotreated heavy fraction; step (3) further comprises processing the resulting hydrotreated stream by separation and fractionation to obtain a hydrotreated hydrogen-rich gas, a hydrotreated gas, a hydrotreated naphtha and a hydrotreated diesel fuel;preferably, the separation in step (2) includes high pressure separation and low pressure separation, the resulting hydrotreated stream is processed by high pressure separation to obtain a hydrotreated hydrogen-rich gas and a hydrotreated high pressure separated liquid phase stream, and then the hydrotreated high pressure separated liquid phase stream is processed by low pressure separation to obtain a hydrotreated gas and a hydrotreated liquid phase stream, and the hydrotreated liquid phase stream is fractionated to obtain a hydrotreated naphtha, a hydrotreated diesel fuel and a hydrotreated heavy fraction;preferably, the separation in step (3) includes a high pressure separation and a low pressure separation, the resulting hydrotreated stream is processed by high pressure separation to obtain a hydrotreated hydrogen-rich gas and a hydrotreated high pressure separated liquid phase stream, and then the hydrotreated high pressure separated liquid phase stream is processed by low pressure separation to obtain a hydrotreated gas and a hydrotreated liquid phase stream, and the hydrotreated liquid phase stream is fractionated to obtain a hydrotreated naphtha and a hydrotreated diesel fuel; preferably, the method further includes recycling the hydrotreated hydrogen-rich gas and the hydrotreated hydrogen-rich gas to provide the desired hydrogen-containing gas.
11. The method according to any one of paragraphs. 1-9, further comprising mixing the finished hydroprocessed stream and the finished hydrotreated stream to obtain a mixed stream and then processing the mixed stream by separation and fractionation; preferably, the mixed stream is processed by high-pressure separation to obtain a mixed hydrogen-rich gas and a mixed high-pressure separated liquid-phase stream, and then the mixed high-pressure separated liquid-phase stream is processed by low-pressure separation to obtain a mixed gas and a mixed liquid-phase stream, and the mixed liquid-phase stream is fractionated to obtain a mixed naphtha, a mixed diesel fuel and a mixed heavy fraction; preferably, the method further comprises recirculating the mixed hydrogen-rich gas to provide the desired hydrogen-containing gas.
12. A unit for hydrogenating paraffinic oil, comprising: a first hydroprocessing unit (1); a gas-liquid separator (2) designed to carry out gas-liquid separation of a portion of the first hydroprocessed stream obtained in the first hydroprocessing unit, with the production of a first hydroprocessed gas-phase stream and a first hydroprocessed liquid-phase stream; a second hydroprocessing unit (3), designed to carry out a second hydroprocessing of the remaining portion of the first hydroprocessed stream and the first hydroprocessed liquid-phase stream, with the production of a finished hydroprocessed stream;a light catalytic cracking recycle gas oil supply unit (4) designed to supply light catalytic cracking recycle gas oil, and a hydrotreating unit (5) designed to hydrotreat the light catalytic cracking recycle gas oil supplied via the light catalytic cracking recycle gas oil supply unit (4) and the hydrotreated gas phase stream to obtain a finished hydrotreated stream.
13. The apparatus according to claim 12, wherein the gas-liquid separator (2) includes a reagent inlet, a liquid phase pipeline and a gas phase pipeline; the reagent inlet of the gas-liquid separator (2) is connected to the outlet of the first hydroprocessing unit (1), the first hydroprocessed liquid phase stream is directed to the second hydroprocessing unit (3) through the liquid phase pipeline, and the first hydroprocessed gas phase stream is directed to the hydrotreating unit (5) through the gas phase pipeline.
14. The apparatus according to claim 12 or claim 13, further comprising: a hydroprocessing separator unit comprising a high-pressure hydroprocessing separator (61) and a low-pressure hydroprocessing separator (62) connected in series, wherein the outlet of the second hydroprocessing unit (3) is connected to the inlet of the high-pressure hydroprocessing separator (61) via a pipeline; the finished hydroprocessed stream is separated at high pressure in the high-pressure hydroprocessing separator (61) to obtain a hydroprocessed hydrogen-rich gas and a hydroprocessed high-pressure separated liquid-phase stream, and then the hydroprocessed high-pressure separated liquid-phase stream is separated at low pressure in the low-pressure hydroprocessing separator (62) to obtain a hydroprocessed gas and a hydroprocessed liquid-phase stream;a hydroprocessing distillation column (7), where the inlet of the hydroprocessing distillation column (7) is connected to the outlet of the low-pressure hydroprocessing separator (62) via a pipeline, the hydroprocessed liquid phase stream is fractionated in the hydroprocessing distillation column (7) to obtain hydroprocessed ligroin, hydroprocessed diesel fuel and hydroprocessed heavy fraction. a hydrotreating separator unit, including a high-pressure hydrotreating separator (81) and a low-pressure hydrotreating separator (82), connected in series, where the outlet of the hydrotreating unit (5) is connected to the inlet of the high-pressure hydrotreating separator (81) via a pipeline;the finished hydrotreated stream is separated at high pressure in a high-pressure hydrotreating separator (81) to obtain a hydrotreated hydrogen-rich gas and a hydrotreated high-pressure separated liquid-phase stream, and then the hydrotreated high-pressure separated liquid-phase stream is separated at low pressure in a low-pressure hydrotreating separator (82) to obtain a hydrotreated gas and a hydrotreated liquid-phase stream, a hydrotreating rectification column (9), where the inlet of the hydrotreating rectification column (9) is connected to the outlet of the low-pressure hydrotreating separator (82) via a pipeline, the hydrotreated liquid-phase stream is fractionated in the hydrotreating rectification column (9) to obtain hydrotreated ligroin and hydrotreated diesel fuel.
15. The plant according to claim 14, in which the outlet for the gas phase of the high pressure hydroprocessing separator (61) and the outlet for the gas phase of the high pressure hydrotreating separator (81) are connected to the inlet of the first hydroprocessing unit (1) and / or the inlet of the second hydroprocessing unit (3), respectively and independently, for recirculating the hydroprocessed hydrogen-rich gas and the hydrotreated hydrogen-rich gas to provide the hydrogen required for the plant.
16. The apparatus according to claim 12 or claim 13, further comprising: a mixing separator unit and a mixing distillation column (11), wherein the mixing separator unit includes a high-pressure mixing separator (101) and a low-pressure mixing separator (102) connected in series, and the outlet of the low-pressure mixing separator (102) is connected to the inlet of the mixing distillation column (11); the outlet of the second hydroprocessing unit (3) and the outlet of the hydrotreating unit (5) are connected to the inlet of the high-pressure mixing separator (101); the finished hydrotreated stream and the finished hydrotreated stream are mixed and then separated at high pressure in the high-pressure mixing separator (101) to obtain a mixed hydrogen-rich gas and a mixed high-pressure separated liquid-phase stream;the mixed liquid phase stream separated at high pressure is separated at low pressure in a low pressure mixing separator (102) to obtain a mixed gas and a mixed liquid phase stream; the mixed liquid phase stream is fractionated in a mixing distillation column (11) to obtain a mixed ligroin, a mixed diesel fuel and a mixed heavy fraction; preferably, the outlet for the gas phase of the high pressure mixing separator (101) is connected to the inlet of the first hydroprocessing unit (1) and / or the inlet of the second hydroprocessing unit (3) for recirculating the mixed hydrogen-rich gas to provide hydrogen required for the plant.
17. The plant according to any one of paragraphs. 12-16, in which the hydrotreating unit (5) includes a first hydrotreating unit (51) and a second hydrotreating unit (52), arranged in series; the plant further includes a fractionation column (12) for light catalytic cracking cycle gas oil, arranged between the first hydrotreating unit (51) and the light catalytic cracking cycle gas oil supply unit (4) for separating the light catalytic cracking cycle gas oil, supplied by means of the light catalytic cracking cycle gas oil supply unit (4), into a light fraction and a heavy fraction; the heavy fraction and the first hydrotreated gas phase stream are subjected to hydrotreating in the first hydrotreating unit (51) to obtain a first hydrotreated stream; the first hydrotreated stream and the light fraction are hydrotreated in the second hydrotreating unit (52) to obtain a finished hydrotreated stream.
999. SDODR