阅读说明：本技术 一种化妆品级白油生产工艺 (Production process of cosmetic-grade white oil ) 是由 刘业宽 解金国 杨栋 谭秀宝 于 2020-05-15 设计创作，主要内容包括：本发明公开了一种化妆品级白油生产工艺,属于化妆品级白油生产领域,一种化妆品级白油生产工艺,其特征在于：依次包括以下步骤：A、原料处理：A1、采购原油以及氢气材料；A2、进料检查,检查步骤A1中的原油的品质是否达标,从而选择是否使用原油进行加氢精制；A3、对原油中质量检验合格且暂不加工的材料进行储存；B、一段加氢处理：B1、将第一尾油和第二尾油以质量百分比为(15～35)：(85～65)比例混合；通过本方案以第一尾油与第二尾油以质量百分比(15～35)：(85～65)比例混合,从而通过加氢制的白油品质高于单一尾油加氢直的白油品质,进而达到节约了成本,简化了生产工艺的效果,使生产工艺能够长期稳定的运行。(The invention discloses a production process of cosmetic-grade white oil, which belongs to the field of production of cosmetic-grade white oil and is characterized in that: the method sequentially comprises the following steps: A. raw material treatment: a1, crude oil and hydrogen materials are purchased; a2, checking the feeding, checking whether the quality of the crude oil in the step A1 reaches the standard, and selecting whether the crude oil is used for hydrofining; a3, storing the materials which are qualified in quality inspection and are not processed temporarily in the crude oil; B. first-stage hydrotreatment: b1, mixing the first tail oil and the second tail oil according to the mass percentage of (15-35): (85-65) mixing in proportion; according to the scheme, the first tail oil and the second tail oil are mixed according to the mass percentage (15-35): (85-65) mixing in proportion, so that the quality of the white oil prepared by hydrogenation is higher than that of the white oil prepared by single tail oil hydrogenation, the cost is saved, the production process is simplified, and the production process can run stably for a long time.)

1. A production process of cosmetic white oil is characterized by comprising the following steps: the method sequentially comprises the following steps:

A. raw material treatment:

a1, crude oil and hydrogen materials are purchased;

a2, checking the feeding, checking whether the quality of the crude oil in the step A1 reaches the standard, and selecting whether the crude oil is used for hydrofining;

a3, storing the materials which are qualified in quality inspection and are not processed temporarily in the crude oil;

B. first-stage hydrotreatment:

b1, mixing the first tail oil and the second tail oil according to the mass percentage of (15-35): (85-65) mixing in proportion;

b2, mixing the mixed raw oil with hydrogen, introducing the mixture into a hydrotreating reactor, and reacting under the action of a hydrotreating catalyst at a pressure of 10-20 MPa, a reaction temperature of 300-400 ℃, an airspeed of 0.5-1.5 (volume fraction)/h, wherein the volume ratio of hydrogen is 1: 500-1000, carrying out impurity and aromatic saturation reactions such as hydrodesulfurization, denitrification and the like;

b3, obtaining a hydrogenation treatment product;

the initial boiling point of the first tail oil is 330-360 ℃, the final boiling point is 485-505 ℃, the density at 20 ℃ is 845-855 kg/m3, the viscosity at 40 ℃ is 20-35 mm2/s, and the condensation point is-10 ℃;

the initial boiling point of the second tail oil is 305-325 ℃, the final boiling point is 510-540 ℃, the density at 20 ℃ is 825-840 kg/m3, the viscosity at 100 ℃ is 5.0-6.0 mm2/s, and the condensation point is + 20-45 ℃.

C. The processing technology comprises the following steps:

c1, introducing the hydrotreated product obtained from the B3 into an isomeric pour point depressing reactor after steam stripping, and performing isomeric pour point depressing reaction through an isomeric pour point depressing catalyst under the conditions that the hydrogen partial pressure is 16-20/MPa and the reaction temperature is 300-410/° C to obtain an isomeric pour point depressing product;

c2, introducing the isomeric pour point depression product obtained in C1 into a complementary refining reactor after steam stripping, and performing a complementary refining reaction through a complementary refining catalyst under the conditions of hydrogen partial pressure of 16-20/MPa, reaction temperature of 300-410/DEG C and volume space velocity of 0.18-1.0/h < -1 > to obtain a complementary refining reaction effluent;

and C3, respectively carrying out gas-liquid separation on the supplementary refining reaction effluent in a high-pressure separator and a buffer pipe, distilling the separated liquid phase by a reduced pressure distillation tower, collecting and fractionating the liquid phase at the inlet temperature of 320-350 ℃ and the vacuum degree of more than 5-20 pa, and thus obtaining the cosmetic white oil.

2. A process according to claim 1 for the production of a cosmetic grade white oil, characterized in that: b3, wherein the aromatic content of the hydrotreated product is less than 5%.

3. A process according to claim 1 for the production of a cosmetic grade white oil, characterized in that: after the first tail oil and the second tail oil are mixed, the concentration of sulfur is less than 10 mu g/g, and the concentration of nitrogen is less than 10 mu g/g.

4. A process according to claim 1 for the production of a cosmetic grade white oil, characterized in that: b2, the volume ratio of the hydrogen to the mixed oil of the first tail oil and the second tail oil is 800: 1.

5. A process according to claim 1 for the production of a cosmetic grade white oil, characterized in that: the pressure of the hydroisomerization dewaxing is 15 MPa-16 MPa.

6. A process according to claim 1 for the production of a cosmetic grade white oil, characterized in that: the pressure of the hydroisomerization dewaxing is 14MPa to 16.8 MPa.

7. A process according to claim 1 for the production of a cosmetic grade white oil, characterized in that: the temperature of the hydroisomerization dewaxing is 320-360 ℃.

8. A process according to claim 1 for the production of a cosmetic grade white oil, characterized in that: the temperature of the hydroisomerization dewaxing is 340-380 ℃.

Technical Field

The invention relates to the field of cosmetic-grade white oil production, and particularly relates to a process for producing cosmetic-grade white oil.

Background

As is well known, white oil is classified into three types according to purposes, namely industrial white oil, cosmetic white oil and pharmaceutical white oil, wherein the industrial white oil occupies an important position in consumption and solely occupies a chelate in a proportion of 37% of the total domestic consumption, and downstream demand industries mainly relate to industries such as printing ink, textile, chemical fiber, plastic, adhesive and the like. However, in recent two years, the domestic entity economy is obviously accelerated and slowed down, and the downstream demand industry encounters a severe excess production period after the high-speed development of the last few years, so that the domestic white oil demand is seriously atrophied.

The raw material for producing the white oil by the hydrogenation method mainly comprises hydrocracking tail oil, and producing the white oil by solvent dewaxing or isodewaxing and high-pressure hydrogenation saturation of a reduction catalyst. In order to improve the quality of white oil in actual production, catalysts in the production process are often required to be optimized, and the cost of the catalysts is high, so that the cost of producing the white oil is greatly increased, and therefore a cosmetic-grade white oil production process is provided to solve the problems.

Disclosure of Invention

1. Technical problem to be solved

Aiming at the problems in the prior art, the invention aims to provide a production process of cosmetic-grade white oil, which can be blended by tail oil with different proportions, reduce the requirements on the quality of the tail oil, avoid the problem that the production method of a catalyst needs to be changed due to different tail oil, further achieve the effect of saving cost, simplify the production process, and solve the problem that the cost of producing the white oil is greatly increased due to the fact that the catalyst in the production process is often required to be optimized for improving the quality of the white oil and the cost of the catalyst is higher.

2. Technical scheme

In order to solve the above problems, the present invention adopts the following technical solutions.

A production process of cosmetic white oil sequentially comprises the following steps:

A. raw material treatment:

a1, crude oil and hydrogen materials are purchased;

a2, checking the feeding, checking whether the quality of the crude oil in the step A1 reaches the standard, and selecting whether the crude oil is used for hydrofining;

a3, storing the materials which are qualified in quality inspection and are not processed temporarily in the crude oil;

B. first-stage hydrotreatment:

b1, mixing the first tail oil and the second tail oil according to the mass percentage of (15-35): (85-65) mixing in proportion;

b2, mixing the mixed raw oil with hydrogen, introducing the mixture into a hydrotreating reactor, and reacting under the action of a hydrotreating catalyst at a pressure of 10-20 MPa, a reaction temperature of 300-400 ℃, an airspeed of 0.5-1.5 (volume fraction)/h, wherein the volume ratio of hydrogen is 1: 500-1000, carrying out impurity and aromatic saturation reactions such as hydrodesulfurization, denitrification and the like;

b3, obtaining a hydrogenation treatment product;

the initial boiling point of the first tail oil is 330-360 ℃, the final boiling point is 485-505 ℃, the density at 20 ℃ is 845-855 kg/m3, the viscosity at 40 ℃ is 20-35 mm2/s, and the condensation point is-10 ℃;

the initial boiling point of the second tail oil is 305-325 ℃, the final boiling point is 510-540 ℃, the density at 20 ℃ is 825-840 kg/m3, the viscosity at 100 ℃ is 5.0-6.0 mm2/s, and the condensation point is + 20-45 ℃.

C. The processing technology comprises the following steps:

c1, introducing the hydrotreated product obtained from the B3 into an isomeric pour point depressing reactor after steam stripping, and performing isomeric pour point depressing reaction through an isomeric pour point depressing catalyst under the conditions that the hydrogen partial pressure is 16-20/MPa and the reaction temperature is 300-410/° C to obtain an isomeric pour point depressing product;

c2, introducing the isomeric pour point depression product obtained in C1 into a complementary refining reactor after steam stripping, and performing a complementary refining reaction through a complementary refining catalyst under the conditions of hydrogen partial pressure of 16-20/MPa, reaction temperature of 300-410/DEG C and volume space velocity of 0.18-1.0/h < -1 > to obtain a complementary refining reaction effluent;

and C3, respectively carrying out gas-liquid separation on the supplementary refining reaction effluent in a high-pressure separator and a buffer pipe, distilling the separated liquid phase by a reduced pressure distillation tower, collecting and fractionating the liquid phase at the inlet temperature of 320-350 ℃ and the vacuum degree of more than 5-20 pa, and thus obtaining the cosmetic white oil.

Preferably, the hydrotreated product of B3 has an aromatics content of less than 5%.

Preferably, after the first tail oil and the second tail oil are mixed, the concentration of sulfur is less than 10 mu g/g, and the concentration of nitrogen is less than 10 mu g/g.

Preferably, the volume ratio of the hydrogen to the mixed oil of the first tail oil and the second tail oil is 800: 1.

Preferably, the pressure of the hydroisomerization dewaxing is 15 MPa.

Preferably, the pressure of the hydroisomerization dewaxing is 14 MPa.

Preferably, the pressure of the hydroisomerization dewaxing is 15 MPa.

Preferably, the hydroisomerization dewaxing temperature is 320 ℃.

Preferably, the hydroisomerization dewaxing temperature is 340 ℃.

Example two:

3. advantageous effects

Compared with the prior art, the invention has the advantages that:

(1) according to the scheme, the first tail oil and the second tail oil are mixed according to the mass percentage (15-35): (85-65) the mixture ratio, so that the quality of the white oil prepared by hydrogenation is higher than that of the white oil prepared by single tail oil hydrogenation.

(2) According to the scheme, the viscosity index of the first tail oil and the viscosity index of the second tail oil are as high as 107, and the condensation point is as low as-24/DEG C, so that the requirement on the quality of the tail oil is lowered, the production method of the hydrogenation reaction catalyst does not need to be changed, the cost is saved, the effect of the production process is simplified, and the production process can be stably operated for a long time.

Drawings

FIG. 1 is a flow chart of the present invention;

Detailed Description

The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

The first embodiment is as follows:

a production process of cosmetic white oil is characterized by comprising the following steps: the method sequentially comprises the following steps:

A. raw material treatment:

a1, crude oil and hydrogen materials are purchased;

a2, checking the feeding, checking whether the quality of the crude oil in the step A1 reaches the standard, and selecting whether the crude oil is used for hydrofining;

a3, storing the materials which are qualified in quality inspection and are not processed temporarily in the crude oil;

B. first-stage hydrotreatment:

b1, mixing the first tail oil and the second tail oil according to the mass percentage of (15): (85) mixing in proportion;

b2, mixing the mixed raw oil with hydrogen, introducing the mixture into a hydrotreating reactor, and introducing the mixture into the hydrotreating reactor under the action of a hydrotreating catalyst, wherein the pressure is 10MPa, the reaction temperature is 300 ℃, the space velocity is 0.5 (volume fraction)/h, and the volume ratio of hydrogen is 1: 500, carrying out impurity and aromatic saturation reactions such as hydrodesulfurization, denitrification and the like;

b3, obtaining a hydrogenation treatment product;

the initial boiling point of the first tail oil is 330 ℃, the final boiling point is 485 ℃, the density at 20 ℃ is 845kg/m3, the viscosity at 40 ℃ is 20mm2/s, and the condensation point is-10 ℃;

the initial boiling point of the second tail oil is 305 ℃, the final boiling point is 510 ℃, the density at 20 ℃ is 825kg/m3, the viscosity at 100 ℃ is 5.0mm2/s, and the condensation point is +20 ℃.

C. The processing technology comprises the following steps:

c1, introducing the hydrotreated product obtained from the B3 into an isomeric pour point depressing reactor after steam stripping, and carrying out an isomeric pour point depressing reaction by using an isomeric pour point depressing catalyst under the conditions of hydrogen partial pressure of 16/MPa and reaction temperature of 300/DEG C to obtain an isomeric pour point depressing product;

c2, introducing the isomeric pour point depression product obtained in C1 into a complementary refining reactor after steam stripping, and performing a complementary refining reaction by using a complementary refining catalyst under the conditions of hydrogen partial pressure of 16/MPa, reaction temperature of 300/DEG C and volume space velocity of 0.18/h < -1 > to obtain a complementary refining reaction effluent;

and C3, performing gas-liquid separation on the supplementary refined reaction effluent in a high-pressure separator and a buffer pipe respectively, performing distillation treatment on the separated liquid phase by a reduced pressure distillation tower, wherein the inlet temperature of the reduced pressure distillation tower is 320 ℃, the vacuum degree is more than 5pa, and collecting and fractionating to obtain the cosmetic white oil.

Further, the B3 hydrotreated product had an aromatic content of 3%.

Further, after the first tail oil and the second tail oil were mixed, the concentration of sulfur was 5. mu.g/g, and the concentration of nitrogen was 5. mu.g/g.

Further, the volume ratio of the hydrogen gas to the mixed oil of the first tail oil and the second tail oil in B2 is 800:1

Further, the pressure of the hydroisomerization dewaxing is 15 MPa.

Further, the pressure of the hydroisomerization dewaxing is 14 MPa.

Further, the hydroisomerization dewaxing temperature was 320 ℃.

Further, the temperature of the hydroisomerization dewaxing is 340 ℃.

Example two:

a production process of cosmetic white oil is characterized by comprising the following steps: the method sequentially comprises the following steps:

A. raw material treatment:

a1, crude oil and hydrogen materials are purchased;

a2, checking the feeding, checking whether the quality of the crude oil in the step A1 reaches the standard, and selecting whether the crude oil is used for hydrofining;

a3, storing the materials which are qualified in quality inspection and are not processed temporarily in the crude oil;

B. first-stage hydrotreatment:

b1, mixing the first tail oil and the second tail oil according to the mass percentage of (25): (75) mixing in proportion;

b2, mixing the mixed raw oil with hydrogen, introducing the mixture into a hydrotreating reactor, and introducing the mixture into the hydrotreating reactor under the action of a hydrotreating catalyst, wherein the pressure is 15MPa, the reaction temperature is 350 ℃, the space velocity is 1 (volume fraction)/h, and the volume ratio of hydrogen is 1: 750, carrying out impurity such as hydrodesulfurization, denitrification and the like and aromatic hydrocarbon saturation reaction;

b3, obtaining a hydrogenation treatment product;

the initial boiling point of the first tail oil is 345 ℃, the final boiling point is 495 ℃, the density at 20 ℃ is 850kg/m3, the viscosity at 40 ℃ is 28mm2/s, and the condensation point is 3 ℃;

the initial boiling point of the second tail oil is 315 ℃, the final boiling point is 530 ℃, the density at 20 ℃ is 833kg/m3, the viscosity at 100 ℃ is 5.5mm2/s, and the condensation point is 32 ℃.

C. The processing technology comprises the following steps:

c1, introducing the hydrotreated product obtained from the B3 into an isomeric pour point depressing reactor after steam stripping, and carrying out an isomeric pour point depressing reaction by using an isomeric pour point depressing catalyst under the conditions of hydrogen partial pressure of 18/MPa and reaction temperature of 355/DEG C to obtain an isomeric pour point depressing product;

c2, introducing the isomeric pour point depression product obtained in C1 into a complementary refining reactor after steam stripping, and performing a complementary refining reaction by using a complementary refining catalyst under the conditions of hydrogen partial pressure of 18/MPa, reaction temperature of 360/DEG C and volume space velocity of 0.6/h < -1 > to obtain a complementary refining reaction effluent;

and C3, performing gas-liquid separation on the supplementary refined reaction effluent in a high-pressure separator and a buffer pipe respectively, performing distillation treatment on the separated liquid phase by a reduced pressure distillation tower, collecting and fractionating the liquid phase at the inlet temperature of the reduced pressure distillation tower of 335 ℃ and the vacuum degree of more than 13pa, and thus obtaining the cosmetic white oil.

Further, the aromatic content of the hydrotreating product of B3 is less than 4%.

Further, after the first tail oil and the second tail oil are mixed, the concentration of sulfur is less than 7 mu g/g, and the concentration of nitrogen is less than 7 mu g/g.

Further, the volume ratio of the hydrogen gas to the mixed oil of the first tail oil and the second tail oil in B2 is 800:1

Further, the pressure of the hydroisomerization dewaxing is 15.5MPa

Further, the pressure of the hydroisomerization dewaxing is 15 MPa.

Further, the hydroisomerization dewaxing temperature was 345 ℃.

Further, the temperature of the hydroisomerization dewaxing is 360 ℃.

Example three:

a production process of cosmetic white oil is characterized by comprising the following steps: the method sequentially comprises the following steps:

A. raw material treatment:

a1, crude oil and hydrogen materials are purchased;

a2, checking the feeding, checking whether the quality of the crude oil in the step A1 reaches the standard, and selecting whether the crude oil is used for hydrofining;

a3, storing the materials which are qualified in quality inspection and are not processed temporarily in the crude oil;

B. first-stage hydrotreatment:

b1, mixing the first tail oil and the second tail oil according to the mass percentage of (35): (65) mixing in proportion;

b2, mixing the mixed raw oil with hydrogen, introducing the mixture into a hydrotreating reactor, and introducing the mixture into the hydrotreating reactor under the action of a hydrotreating catalyst, wherein the pressure is 20MPa, the reaction temperature is 400 ℃, the space velocity is 1.5 (volume fraction)/h, and the volume ratio of hydrogen is 1: 1000, carrying out impurity and aromatic saturation reactions such as hydrodesulfurization, denitrification and the like;

b3, obtaining a hydrogenation treatment product;

the initial boiling point of the first tail oil is 360 ℃, the final boiling point is 505 ℃, the density at 20 ℃ is 855kg/m3, the viscosity at 40 ℃ is 35mm2/s, and the condensation point is +10 ℃;

the initial boiling point of the second tail oil is 325 ℃, the final boiling point is 540 ℃, the density at 20 ℃ is 840kg/m3, the viscosity at 100 ℃ is 6.0mm2/s, and the condensation point is +45 ℃.

C. The processing technology comprises the following steps:

c1, introducing the hydrotreated product obtained from the B3 into an isomeric pour point depressing reactor after steam stripping, and carrying out an isomeric pour point depressing reaction by using an isomeric pour point depressing catalyst under the conditions of hydrogen partial pressure of 20/MPa and reaction temperature of 410/° C to obtain an isomeric pour point depressing product;

c2, introducing the isomeric pour point depression product obtained in C1 into a complementary refining reactor after steam stripping, and performing a complementary refining reaction by using a complementary refining catalyst under the conditions of hydrogen partial pressure of 20/MPa, reaction temperature of 410/DEG C and volume space velocity of 1.0/h < -1 > to obtain a complementary refining reaction effluent;

and C3, performing gas-liquid separation on the supplementary refined reaction effluent in a high-pressure separator and a buffer pipe respectively, performing distillation treatment on the separated liquid phase by a reduced pressure distillation tower, collecting and fractionating the liquid phase at the inlet temperature of the reduced pressure distillation tower of 350 ℃ and the vacuum degree of more than 20pa, and thus obtaining the cosmetic white oil.

Further, the aromatic content of the hydrotreating product of B3 is less than 5%.

Furthermore, after the first tail oil and the second tail oil are mixed, the concentration of sulfur is less than 10 mu g/g, and the concentration of nitrogen is less than 10 mu g/g.

Further, the volume ratio of the hydrogen gas to the mixed oil of the first tail oil and the second tail oil in B2 is 800: 1.

Further, the pressure of the hydroisomerization dewaxing is 16 MPa.

Further, the pressure of the hydroisomerization dewaxing is 16.8 MPa.

Further, the temperature of the hydroisomerization dewaxing is 360 ℃.

Further, the hydroisomerization dewaxing temperature was 380 ℃.

The white oil produced by the scheme meets the index requirements of cosmetic white oil, the content of aromatic hydrocarbon is lower than 0.01% w/w, the content of sulfur is lower than 1ppm, the condensation point is lower than-30 ℃, and the condensation point is far lower than the national standard requirements.

The foregoing is only a preferred embodiment of the present invention; the scope of the invention is not limited thereto. Any person skilled in the art should be able to cover the technical scope of the present invention by equivalent or modified solutions and modifications within the technical scope of the present invention.

The foregoing is only a preferred embodiment of the present invention; the scope of the invention is not limited thereto. Any person skilled in the art should be able to cover the technical scope of the present invention by equivalent or modified solutions and modifications within the technical scope of the present invention.