CN111518589A - Production process of food-grade white oil - Google Patents
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- CN111518589A CN111518589A CN202010315756.0A CN202010315756A CN111518589A CN 111518589 A CN111518589 A CN 111518589A CN 202010315756 A CN202010315756 A CN 202010315756A CN 111518589 A CN111518589 A CN 111518589A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/10—Lubricating oil
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Abstract
The invention provides a production process of food-grade white oil. The method is characterized in that lubricating oil base oil, industrial white oil, hydrocracking tail oil, hydroisomerization dewaxing tail oil and the like are used as raw material oil, a noble metal catalyst is adopted, a reaction product is obtained through one-stage serial hydrogenation, and the reaction product is subjected to high-pressure and low-pressure gas-liquid separation, reduced pressure fractionation and side steam stripping to obtain food-grade white oil products with different viscosity grades. Compared with the prior art, the method has the advantages of simple process flow and high separation precision, and the reaction system and the fractionation system are reasonably designed and optimally adjusted, so that the same device can be used, raw materials with different viscosity grades are switched to be fed for production, and food-grade white oil products with different brands can be obtained according to market demands.
Description
Technical Field
The invention belongs to the technical field of food-grade white oil, and particularly relates to a production process of food-grade white oil.
Background
The white oil is a special mineral oil product which is subjected to ultra-deep refining, and belongs to a lubricating oil component. The white oil mainly comprises saturated hydrocarbons (cycloalkane and alkane), has extremely low contents of impurities such as sulfur, nitrogen, oxygen, aromatic hydrocarbon and the like, and has good chemical inertness and excellent light and heat stability. The white oil has wide application, and can be used for textile chemical fiber production, food demoulding, dairy product processing, medicine defoaming, lipstick production, skin care oil production and the like.
The white oil is prepared through sulfonating or hydrorefining to eliminate S, N, O, arene, heavy metal and other impurities to obtain colorless, odorless and non-corrosive high quality petroleum product. The sulfonation method is gradually replaced by a hydrogenation method which has the defects of no pollution, high yield, wide raw material source and good product quality due to the defects of high sulfuric acid consumption, high production cost, large discharge of three wastes, low yield and the like. The hydrogenation method adopts one-stage hydrogenation or multi-stage hydrogenation according to different raw materials and different requirements on products, and can obtain industrial white oil or food cosmetic white oil.
The production process of the white oil is mainly a process for removing hydrogen sulfide, aromatic hydrocarbon and other impurities, the traditional hydrogenation method generally adopts multi-stage hydrogenation, has high cost, high requirements on catalysts and possible heavy metals, the production process is complex, the operation requirement of a reaction system is high, a fractionation system has limited cutting precision on fractions, and particularly, the requirements on the production process are more and more strict along with the continuous improvement of the standard of high-grade white oil.
Disclosure of Invention
Aiming at the technical problems in the prior art, the invention provides a production process of food-grade white oil, which is suitable for raw materials with higher aromatic hydrocarbon content and higher pour point, has strong hydrogenation reaction processing capacity and high separation precision, uses the same set of device, switches the feeding production of the raw materials with various viscosity grades, and can separate food-grade white oil products with different brands according to market requirements and distillation range characteristics.
The invention provides a production process of food-grade white oil, which comprises the following steps: mixing raw oil with hydrogen, heating, sequentially entering a reactor I filled with a hydrogenation catalyst, a protective agent and ceramic balls and a reactor II filled with the hydrogenation catalyst and the ceramic balls, and carrying out hydrofining reaction to obtain a reactant; the reactants enter a fractionation system after being subjected to gas-liquid separation sequentially through a high-pressure separator and a low-pressure separator; the fractionation system finely cuts a reaction product after gas-liquid separation to obtain a plurality of food-grade white oil products with different brands which meet the GB1886.215-2016 standard; wherein, the reactor I and the reactor II adopt a single-stage series connection form to form a series connection reaction zone.
Preferably, the raw oil is one of lubricating oil base oil, industrial white oil, hydrocracking tail oil and hydroisomerization dewaxing tail oil; and in the raw oil: total metal content <2.0 μ g/g; the sulfur content is not more than 5 mg/kg; no less than 26 by Saybolt color comparison (number); the nitrogen content is not more than 1 mg/L; the content of aromatic hydrocarbon is not less than 10 wt%; the pour point is not more than 0 ℃.
Preferably, the heating is performed by using a heating furnace.
Preferably, the hydrogenation catalyst is a reduced noble metal catalyst; the specific surface area of the hydrogenation catalyst is 160-240m2(ii)/g; pore volume of 0.2-0.6m2(ii)/g; the carrier being TiO2/SO4 2-(ii) a The active component is Pt-Pd, wherein the Pt/Pd (wt) is 0.3-0.7.
Preferably, the protecting agent contains MoO35-10%; 2 to 5 percent of NiO; the carrier being Al2O3(ii) a Pore volume of 0.4-0.8m2(ii)/g; the specific surface area is 120-180m2/g。
Preferably, the operating conditions in the hydrofining reaction are temperature 180-320 ℃; hydrogen partial pressure is 12.0-20.0 MPa; volume space velocity of 0.3h-1-1.5h-1(ii) a Hydrogen-oil volume ratio 300-: 1.
preferably, the operating temperature of the high-pressure separator is 180-320 ℃, and the operating pressure is 12.0-20.0 MPa; the operating temperature of the low-pressure separator is 180-320 ℃, and the operating pressure is 0.50-2.50MPa (G).
Preferably, the fractionating system comprises a reduced pressure fractionating tower, a side stripper, a first-line reducing pump, a first-line reducing heat exchanger, a second-line reducing pump, a top reducing condenser, a top reducing liquid separating tank, a top reducing vacuum system, a top reducing water seal tank, a bottom reducing pump and a bottom reducing heat exchanger; and the pressure reduction fractionating tower is provided with a top reduction noncondensable gas outlet, a first reduction line reflux port, a first reduction line extraction outlet, a second reduction line reflux port, a second reduction line extraction outlet, a reaction product feed inlet, a stripping steam inlet and a bottom reduction oil outlet from top to bottom.
Preferably, the reaction product after gas-liquid separation enters the vacuum fractionating tower from a reaction product feed inlet, and stripping steam I enters the vacuum fractionating tower from a stripping steam inlet to steam strip the reaction product; the first-line-reducing distillate is extracted from the first-line-reducing extraction outlet through a first-line-reducing pump, part of the first-line-reducing distillate is output as a first-line-reducing product after being cooled by the first-line-reducing heat exchanger, and part of the first-line-reducing distillate flows back into the reduced pressure fractionating tower through the first-line-reducing reflux outlet and is used for controlling the temperature at the top of the tower; the second-line-reducing distillate is extracted from the second-line-reducing outlet through a second-line-reducing pump and enters the side stripper to be stripped by stripping steam II; the bottom liquid phase of the side stripper is taken as a second-line-reduced product outlet device, and the top gas phase of the side stripper reflows to the vacuum fractionating tower from a second-line-reduced reflux port; the non-condensable gas at the top reducing non-condensable gas outlet is cooled by a top reducing condenser and then enters the top reducing liquid separating tank, the bottom liquid of the top reducing liquid separating tank enters a top reducing water-sealed tank, the gas at the top of the top reducing liquid separating tank enters a top reducing vacuum system and is discharged to a torch system, and the water phase separated by the top reducing water-sealed tank enters a sump oil system; the heavy component white oil product is extracted from a bottom reducing oil outlet by the bottom reducing pump, and is cooled by the bottom reducing heat exchanger to be used as a product outlet device; wherein, when the high-viscosity raw oil (the kinematic viscosity at 100 ℃ is more than or equal to 10 CST) is processed, the extraction and the reflux of the first-line reduction fraction and the second-line reduction fraction are stopped.
Preferably, the operating pressure of the vacuum fractionation column is from-0.05 to-0.095 mpa (g); the operating pressure of the side stripper is from-0.05 to-0.095 MPa (G).
Compared with the prior art, the invention has the beneficial effects that:
1) the raw materials used in the invention have wide sources, and the process flow has wide application range;
2) the catalyst I and the catalyst II selected by the invention have high activity, good stability, wide application range, strong selectivity, obvious addition reaction effect on trace aromatic hydrocarbon and olefin, high mechanical strength, good hydrorefining performance and good regeneration performance, and can meet the requirement of long-period operation.
3) The invention has simple process flow, low operation requirement and flexible operation of the fractionation system, uses the same set of device, and can produce and obtain various high-quality food-grade white oil products with different brands according to the GB1886.215-2016 standard by switching the feeding of raw materials with various viscosity grades according to market demands.
Drawings
FIG. 1 is a process flow diagram of a process for producing food grade white oil according to the present invention.
In the figure, 1, a heating furnace, 2, reactors I and 3, reactors II and 4, a hot high-pressure separator, 5, a hot low-pressure separator, 6, a reduced pressure fractionating tower, 6-1, a reaction product feed inlet, 6-2, a stripping steam feed inlet, 6-3, a reduced first line extraction outlet, 6-4, a reduced first line reflux port, 6-5, a reduced second line extraction outlet, 6-6, a reduced second line reflux port, 6-7, a reduced bottom oil outlet, 6-8, a reduced top noncondensable gas outlet, 7, a reduced first line pump, 8, a reduced first line heat exchanger, 9, a reduced second line pump, 10, a side line, 11, a reduced bottom pump, 12, a reduced bottom heat exchanger, 13, a reduced top heat exchanger, 14, a reduced top separation liquid tank, 15, a reduced top vacuum system, 16 and a reduced top water seal tank.
Detailed Description
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further explained below by combining the specific drawings.
Example 1
A production process of food-grade white oil comprises the following steps:
s1, entering a reaction system: mixing raw oil with hydrogen, heating the mixture by a heating furnace 1, and then sequentially entering a reactor I2 filled with a hydrogenation catalyst, a protective agent and ceramic balls and a reactor II 3 filled with the hydrogenation catalyst and the ceramic balls for hydrofining to perform addition reaction on unsaturated hydrocarbon; the reactant enters a fractionation system after being subjected to gas-liquid separation by a high-pressure separator 4 and a low-pressure separator 5; the reactor I2 and the reactor II 3 adopt a single-stage series connection form to form a series connection reaction zone.
Wherein, the raw oil, the hydrogenation catalyst and the reaction conditions are as follows:
1) raw oil properties:
2) catalyst and filler:
the reactor I is filled with ceramic balls ∅ 3- ∅ 20 and a protective agent MoO3-NiO/Al2O3Catalyst Pt-Pd/TiO2-SO4 2-；
The reactor II is filled with ceramic balls ∅ 3- ∅ 20 and a catalyst Pt-Pd/TiO2-SO4 2-。
3) Reaction conditions are as follows:
the inlet hydrogen partial pressure is 18MPa, the average temperature of the bed layer is 230 ℃, and the volume space velocity is 0.5h-1The hydrogen-oil ratio is 500: 1.
4) Operating temperature of high-pressure separator: 235 ℃, and the operating pressure is 18 MPa; operating temperature of low-pressure separator: 235 ℃ and the operating pressure is 2.0 MPa.
S2, entering a fractionation system: and the fractionating system finely cuts the reaction product after gas-liquid separation to obtain a plurality of high-quality food-grade white oil products with different brands which meet the GB1886.215-2016 standard.
The system comprises a vacuum fractionating tower 6, a side stripper 10, a first-line reducing pump 7, a first-line reducing heat exchanger 8, a second-line reducing pump 9, a top reducing condenser 13, a top reducing liquid separating tank 14, a top reducing vacuum system 15, a top reducing water seal tank 16, a bottom reducing pump 11 and a bottom reducing heat exchanger 12;
the vacuum fractionating tower 6 is provided with a reduced-roof noncondensable gas outlet 6-8, a reduced-first-line reflux port 6-4, a reduced-first-line extraction outlet 6-3, a reduced-second-line reflux port 6-6, a reduced-second-line extraction outlet 6-5, a reaction product feed inlet 6-1, a stripping steam inlet 6-2 and a reduced oil outlet 6-7 from top to bottom;
the reaction product after gas-liquid separation enters a reduced pressure fractionating tower 6 from a reaction product feed inlet 6-1, and stripping steam I enters the reduced pressure fractionating tower from a stripping steam inlet 6-2 to carry out steam stripping on the reaction product; a first-line-reducing distillate is extracted from a first-line-reducing extraction outlet 6-3 through a first-line-reducing pump 7, part of the first-line-reducing distillate is output as a first-line-reducing product after being cooled by a first-line-reducing heat exchanger 8, and part of the first-line-reducing distillate flows back into the reduced pressure fractionating tower 6 through a first-line-reducing reflux outlet 6-4 and is used for controlling the temperature at the top of; a second-line-reduced distillate is extracted from a second-line-reduced outlet 6-5 through a second-line-reduced pump 9 and enters a side stripper 10 to be stripped by stripping steam II; the liquid phase at the bottom of the side stripper 10 is taken as a second-line-reduced product outlet device, and the gas phase at the top of the side stripper 19 flows back to the vacuum fractionating tower 6 from a second-line-reduced return port 6-6; the non-condensable gas at the 6-8 position of the top-reducing non-condensable gas outlet is cooled by a top-reducing condenser 13 and then enters a top-reducing liquid separating tank 14, the bottom liquid of the top-reducing liquid separating tank 14 enters a top-reducing water seal tank 16, the top gas of the top-reducing liquid separating tank 14 enters a top-reducing vacuum system 15 and is discharged to a torch system, and the water phase separated by the top-reducing water seal tank 16 enters a sump oil system; and the heavy component white oil product is extracted by a bottom reducing pump 11 through a bottom reducing oil outlet 6-7, and is cooled by a bottom reducing heat exchanger 12 to be used as a product outlet device.
The operating conditions of the fractionation system were as follows: the operating pressure of the reduced pressure fractionating tower is-0.08 MPa (G), the temperature of stripping steam I is 250 ℃, and the pressure is 1.2MPa (A); the operating pressure of the side stripper is-0.082 MPa (G), the temperature of stripping steam II is 250 ℃, and the pressure is 1.2MPa (A).
The properties of the white oil product made by this example are shown in the following table:
through the detection of product oil, the oil produced in the second-cut line and the bottom oil meet the requirements of the food-grade white oil product of GB1886.215-2016 standard No. 1, and the oil produced in the second-cut line can be used as the food-grade white oil product with narrow distillation range.
Example 2
A production process of food-grade white oil comprises the following steps:
s1, entering a reaction system: mixing raw oil with hydrogen, heating the mixture by a heating furnace 1, and then sequentially entering a reactor I2 filled with a hydrogenation catalyst, a protective agent and ceramic balls and a reactor II 3 filled with the hydrogenation catalyst and the ceramic balls for hydrofining to perform addition reaction on unsaturated hydrocarbon; the reactant enters a fractionation system after being subjected to gas-liquid separation by a high-pressure separator 4 and a low-pressure separator 5; the reactor I2 and the reactor II 3 adopt a single-stage series connection form to form a series connection reaction zone.
Wherein, the raw oil, the catalyst and the reaction conditions are as follows:
1) raw oil properties:
2) catalyst and filler:
the reactor I is filled with ceramic balls ∅ 3- ∅ 20 and a protective agent MoO3-NiO/Al2O3Catalyst Pt-Pd/TiO2-SO4 2-；
The reactor II is filled with ceramic balls ∅ 3- ∅ 20 and a catalyst Pt-Pd/TiO2-SO4 2-；
3) Reaction conditions are as follows:
the inlet hydrogen partial pressure is 18MPa, the average temperature of the bed layer is 240 ℃, and the volume space velocity is 0.5h-1Hydrogen-oil ratio 500: 1;
4) operating temperature of high-pressure separator: 245 ℃ and the operating pressure of 18 MPa; operating temperature of low-pressure separator: 245 ℃ and the operating pressure of 2.0 MPa.
S2, entering a fractionation system: and the fractionating system finely cuts the reaction product after gas-liquid separation to obtain a plurality of high-quality food-grade white oil products with different brands which meet the GB1886.215-2016 standard.
The system comprises a vacuum fractionating tower 6, a side stripper 10, a first-line reducing pump 7, a first-line reducing heat exchanger 8, a second-line reducing pump 9, a top reducing condenser 13, a top reducing liquid separating tank 14, a top reducing vacuum system 15, a top reducing water seal tank 16, a bottom reducing pump 11 and a bottom reducing heat exchanger 12;
the vacuum fractionating tower 6 is provided with a reduced-roof noncondensable gas outlet 6-8, a reduced-first-line reflux port 6-4, a reduced-first-line extraction outlet 6-3, a reduced-second-line reflux port 6-6, a reduced-second-line extraction outlet 6-5, a reaction product feed inlet 6-1, a stripping steam inlet 6-2 and a reduced oil outlet 6-7 from top to bottom;
the kinematic viscosity of the raw oil at 100 ℃ is 10.73 CST (more than or equal to 10 CST), at the moment, the extraction and reflux of the first-line-reduced fraction, the extraction and reflux of the second-line-reduced fraction and the side stripper 10 are stopped;
the reaction product after gas-liquid separation enters a reduced pressure fractionating tower 6 from a reaction product feed inlet 6-1, and stripping steam I enters the reduced pressure fractionating tower from a stripping steam inlet 6-2 to carry out steam stripping on the reaction product; the non-condensable gas at the 6-8 position of the top-reducing non-condensable gas outlet is cooled by a top-reducing condenser 13 and then enters a top-reducing liquid separating tank 14, the bottom liquid of the top-reducing liquid separating tank 14 enters a top-reducing water seal tank 16, the top gas of the top-reducing liquid separating tank 14 enters a top-reducing vacuum system 15 and is discharged to a torch system, and the water phase separated by the top-reducing water seal tank 16 enters a sump oil system; and the heavy component white oil product is extracted by a bottom reducing pump 11 through a bottom reducing oil outlet 6-7, and is cooled by a bottom reducing heat exchanger 12 to be used as a product outlet device.
The operating pressure of the reduced pressure fractionating tower is-0.08 MPa (G), the temperature of stripping steam I is 250 ℃, and the pressure is 1.2MPa (A);
the properties of the white oil product made by this example are shown in the following table:
by detecting the product oil, the bottom reducing oil meets the requirements of GB1886.215-2016 standard No. 4 food-grade white oil products.
The above description is only an embodiment of the present invention, and not intended to limit the scope of the present invention, and all equivalent structures made by using the contents of the present specification and the drawings can be directly or indirectly applied to other related technical fields, and are within the scope of the present invention.
Claims (10)
1. A production process of food-grade white oil is characterized by comprising the following steps: mixing raw oil with hydrogen, heating, sequentially entering a reactor I filled with a hydrogenation catalyst, a protective agent and ceramic balls and a reactor II filled with the hydrogenation catalyst and the ceramic balls, and carrying out hydrofining reaction to obtain a reactant; the reactants enter a fractionation system after being subjected to gas-liquid separation sequentially through a high-pressure separator and a low-pressure separator; and the fractionation system finely cuts the reaction product after gas-liquid separation to obtain a food-grade white oil product.
2. The production process according to claim 1, wherein the feedstock oil is one of a lubricant base oil, an industrial white oil, a hydrocracked tail oil, a hydroisomerized dewaxed tail oil; and in the raw oil: total metal content <2.0 μ g/g; the sulfur content is not more than 5 mg/kg; no less than 26 by Saybolt color comparison (number); the nitrogen content is not more than 1 mg/L; the content of aromatic hydrocarbon is not less than 10 wt%; the pour point is not more than 0 ℃.
3. The production process according to claim 1 or 2, wherein the heating is performed using a heating furnace.
4. The production process according to claim 1 or 2, wherein the hydrogenation catalyst is a reduced noble metal catalyst; the specific surface area of the hydrogenation catalyst is 160-240m2(ii)/g; pore volume of 0.2-0.6m2(ii)/g; the carrier being TiO2/SO4 2-(ii) a The active component is Pt-Pd, wherein the Pt/Pd (wt) is 0.3-0.7.
5. The process according to claim 1 or 2, wherein the protecting agent comprises MoO35-10%; 2 to 5 percent of NiO; the carrier being Al2O3(ii) a Pore volume of 0.4-0.8m2(ii)/g; the specific surface area is 120-180m2/g。
6. The production process as claimed in claim 1 or 2, wherein the operating conditions in the hydrorefining reaction are temperature 180-320 ℃; hydrogen partial pressure is 12.0-20.0 MPa; volume space velocity of 0.3h-1-1.5h-1(ii) a Hydrogen-oil volume ratio 300-: 1。
7. The process according to claim 1 or 2, wherein the high pressure separator has an operating temperature of 180 ℃ and an operating pressure of 12.0 to 20.0 MPa; the operating temperature of the low-pressure separator is 180-320 ℃, and the operating pressure is 0.50-2.50MPa (G).
8. The process of claim 1 or 2, wherein the fractionation system comprises a vacuum fractionation column, a side stripper, a first-line pump, a first-line heat exchanger, a second-line pump, a reduced-head condenser, a reduced-head separation tank, a reduced-head vacuum system, a reduced-head water seal tank, a reduced-head pump, a reduced-head heat exchanger; and the pressure reduction fractionating tower is provided with a top reduction noncondensable gas outlet, a first reduction line reflux port, a first reduction line extraction outlet, a second reduction line reflux port, a second reduction line extraction outlet, a reaction product feed inlet, a stripping steam inlet and a bottom reduction oil outlet from top to bottom.
9. The production process according to claim 8, wherein the reaction product after gas-liquid separation enters the vacuum fractionating tower through a reaction product feed inlet, and stripping steam I enters the vacuum fractionating tower through a stripping steam inlet to steam strip the reaction product; the first-line-reducing distillate is extracted from the first-line-reducing extraction outlet through a first-line-reducing pump, part of the first-line-reducing distillate is output as a first-line-reducing product after being cooled by the first-line-reducing heat exchanger, and part of the first-line-reducing distillate flows back into the reduced pressure fractionating tower through the first-line-reducing reflux outlet and is used for controlling the temperature at the top of the tower; the second-line-reducing distillate is extracted from the second-line-reducing outlet through a second-line-reducing pump and enters the side stripper to be stripped by stripping steam II; the bottom liquid phase of the side stripper is taken as a second-line-reduced product outlet device, and the top gas phase of the side stripper reflows to the vacuum fractionating tower from a second-line-reduced reflux port; the non-condensable gas at the top reducing non-condensable gas outlet is cooled by a top reducing condenser and then enters the top reducing liquid separating tank, the bottom liquid of the top reducing liquid separating tank enters a top reducing water-sealed tank, the gas at the top of the top reducing liquid separating tank enters a top reducing vacuum system and is discharged to a torch system, and the water phase separated by the top reducing water-sealed tank enters a sump oil system; the heavy component white oil product is extracted from a bottom reducing oil outlet by the bottom reducing pump, and is cooled by the bottom reducing heat exchanger to be used as a product outlet device; wherein, when the high-viscosity raw oil (the kinematic viscosity at 100 ℃ is more than or equal to 10 CST) is processed, the extraction and the reflux of the first-line reduction fraction and the second-line reduction fraction are stopped.
10. The production process of claim 9, wherein the operating pressure of the vacuum fractionation column is from-0.05 to-0.095 mpa (g); the operating pressure of the side stripper is from-0.05 to-0.095 MPa (G).
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| CN113372951A (en) * | 2021-06-01 | 2021-09-10 | 宁波博汇化工科技股份有限公司 | Production method of low aromatic white oil |
| CN113372944A (en) * | 2021-06-01 | 2021-09-10 | 宁波博汇化工科技股份有限公司 | Production method of basic lubricating oil |
| CN116410783A (en) * | 2021-12-31 | 2023-07-11 | 中国石油天然气股份有限公司 | Hydrogenation method for producing food-grade white oil |
| CN115926836A (en) * | 2022-10-31 | 2023-04-07 | 东营市俊源石油技术开发有限公司 | Hydrotreating process for preparing food-grade white oil |
| CN115926836B (en) * | 2022-10-31 | 2024-02-13 | 东营市俊源石油技术开发有限公司 | Hydrotreatment process for preparing food-grade white oil |
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