A process for removing solvent from synthetic oil with high efficiency and energy saving

Abstract

The application discloses a process method for removing solvent from synthetic oil with high efficiency and energy saving, relates to the technical field of chemical industry and medicine, and particularly relates to the production and use field of synthetic oil. The process method uses the gaseous solvent after evaporation and compression as a heat source for heating the synthetic oil and solvent mixture in the desolventizing process, and effectively reduces the energy consumption required for removing the solvent from the synthetic oil. The process operation has high flexibility, can effectively utilize the heat in the desolventizing process, reduces the energy consumption, and saves the production cost.

Description

Technical Field

[0001] This invention relates to the fields of chemical and pharmaceutical technology, and particularly to the production and use of synthetic oils. Background Technology

[0002] Lubricating oil is an indispensable material in industry, and the performance of the base oil largely determines the quality of the lubricating oil. Currently, the internationally used base oils include mineral oils (API I-API III) and synthetic oils (API IV-V). Among them, fully synthetic oils have the characteristics of wide operating temperature range, good viscosity-temperature performance, high viscosity index, low pour point, low evaporation loss, good oxidation stability, and environmental friendliness. They are a type of high-quality lubricating oil base oil and are used in many high-end fields.

[0003] The raw materials for synthetic oils can be natural gas, coal-based syngas (CO+H2), C2~C15 olefins, fatty acids and fatty alcohols, etc. Due to the low conversion rate, the synthesized oils contain unreacted monomers or solvents added during the synthesis process, and need to be separated from the product synthetic oil. The existing separation technology is mainly distillation.

[0004] Patent CN105062555A discloses a method for preparing low-viscosity metallocene PAO base oil, which involves distilling the product after removing catalyst residue metals and borides to remove mixed alkanes, without mentioning the utilization of heat.

[0005] CN202111241242.6 discloses a method for preparing saturated metallocene polyα-olefins, wherein the method for removing unreacted monomers is vacuum distillation.

[0006] CN109181811A discloses a high viscosity index, high temperature resistant pyromellitic acid synthetic ester base oil and its preparation method. After the reaction is completed, xylene solvent and a small amount of unreacted raw materials are removed by vacuum removal at 170-180℃ to obtain the desired pyromellitic acid synthetic ester base oil.

[0007] CN112745185A and CN112745179A disclose a method for the continuous production of α-olefins by ethylene oligomerization, which separates the reaction products from the solvent and catalyst system through a flash evaporation process, without mentioning the utilization of heat.

[0008] Existing processes rely on heating the mixture of synthetic oil and solvent or unreacted monomers with heat media such as steam to vaporize the solvent or unreacted monomers for separation. A large amount of solvent or unreacted monomers needs to be condensed again after being vaporized before they can be reused. This process is energy-intensive and does not effectively utilize heat. Summary of the Invention

[0009] The purpose of this invention is to provide a highly efficient and energy-saving process for removing solvents from synthetic oils, in order to solve the aforementioned problem.

[0010] The inventor's previous patents (CN112725017A, CN112725018A, CN112725028A, CN112725029A, CN112725054A, CN112725055A) disclosed a process for directly synthesizing high-performance base oils of different viscosities by low-carbon olefin polymerization, including polymerization, hydrogenation, and distillation steps; wherein the liquid-liquid separation equipment used in the solvent recovery process is a simple atmospheric / vacuum distillation or distillation equipment. In this invention, a novel process for removing solvents from synthetic oils is provided, which recycles the heat of solvent removal to achieve high efficiency and energy saving.

[0011] A first aspect of the present invention provides a synthetic oil desolventizing apparatus, characterized in that the apparatus comprises: (a) A solvent removal system for removing solvents from synthetic oils, comprising: The first heat exchanger E-1 has a mutually enclosed heat exchange channel and a liquid feed channel; the liquid feed channel has a liquid feed inlet and a gas-liquid mixing outlet, and the heat exchange channel is used to transfer heat to the liquid feed in the liquid feed channel. The first separator D-1 has a liquid inlet, a gas phase outlet and a liquid phase outlet, and is located downstream of the first heat exchanger E-1 and connected to the gas-liquid mixing outlet of the heat exchanger. The second heat exchanger E-2 has a feed liquid inlet and a gas-liquid mixing outlet, and the inlet of the second heat exchanger E-2 is connected to the liquid phase outlet of the first separator D-1. The second separator D-2 has a liquid inlet, a gas phase outlet and a liquid phase outlet, and is connected to the gas-liquid mixing outlet of the second heat exchanger E-2. (b) A recovery system for the recycling of solvents.

[0012] In another preferred embodiment, liquid is transported between the first separator and the second heat exchanger via a pressure difference or a height difference.

[0013] In another preferred embodiment, the recycling system includes: Compression device C-1 is connected to the gas phase outlet of the first separator D-1 and the second separator D-2.

[0014] In another preferred embodiment, the compression device C-1 is a compressor, a vacuum pump, or a fan.

[0015] In another preferred embodiment, a vacuum pump is also provided between the second separator D-2 and the compressor C-1 to reduce the amount of solvent residue in the liquid phase of the second separator D-2.

[0016] In another preferred embodiment, the first separator D-1 and the second heat exchanger E-2 further include a pump P-1, which has a liquid phase inlet and an outlet; preferably, the pump is located downstream of the separator D-1, and its inlet is connected to the liquid phase outlet of the first separator, and its outlet is connected to the inlet of the second heat exchanger.

[0017] A second aspect of the present invention provides a process for removing solvents from synthetic oils, comprising the following steps: (1) The synthetic oil product containing low-boiling-point components is passed into heat exchanger E-1 for primary vaporization to obtain a primary gas-liquid mixture; (2) The obtained primary gas-liquid mixture is fed into separator D-1 to separate the gas phase and the liquid phase. The gas phase is fed into compression device C-1 and the liquid phase is fed into heat exchanger E-2. (3) The remaining solvent in the liquid phase undergoes secondary vaporization in heat exchanger E-2 to obtain a secondary gas-liquid mixture; (4) The secondary gas-liquid mixture is fed into separator D-2 to perform secondary separation of the gas phase and the liquid phase. The resulting liquid phase is the separated synthetic oil. (5) The gas phase obtained from the secondary separation is sent to the compression device C-1. After compression, part of the combined gas phase in the compressor is sent to the heat exchanger E-1 as a heat source, and part is sent to the distillation column for processing.

[0018] In another preferred embodiment, in step (2), the liquid phase is introduced into heat exchanger E-2 via pump P-1.

[0019] In another preferred embodiment, in step (5), the combined gas phase obtained is compressed and then completely fed into heat exchanger E-1 as a heating medium.

[0020] In another preferred embodiment, a vacuum pump may be added between step (4) D-2 and compressor C-1 to reduce solvent residue in the liquid phase of D-2. In another preferred embodiment, the synthetic oil product is selected from the group consisting of: From C2~C 15 C obtained from olefin synthesis 10 ~C 5000 olefin polymers; Oil synthesized from natural gas; Oil synthesized from syngas (CO + H2); or Oils obtained by dehydration of fatty acids and fatty alcohols through esterification reaction under the action of a catalyst.

[0021] In another preferred embodiment, the synthetic oil product is a fluid product at room temperature and pressure.

[0022] In another preferred embodiment, the synthetic oil product is an octene polymer.

[0023] In another preferred embodiment, the solvent is selected from the group consisting of: acetonitrile, ethanol, diethyl ether, toluene, C4~C6456 ... 14 Alkanes, dichloromethane, DMF, or combinations thereof.

[0024] In another preferred embodiment, the solvent is dichloromethane.

[0025] In another preferred embodiment, the solvent is a polymeric monomer used to prepare the synthetic oil.

[0026] In another preferred embodiment, the solvent may be a pure solvent or a mixture of a pure solvent and other non-solvent components.

[0027] In another preferred embodiment, in step (5), the solvent introduced into the distillation column for treatment accounts for 10-50 wt% of the total solvent volume.

[0028] In another preferred embodiment, in step (5), the compressed solvent is used entirely or partially as the heating medium for heat exchanger E-1.

[0029] In another preferred embodiment, step (5) can also be passed into a distillation column without compression.

[0030] In another preferred embodiment, the solvent in step (5) to other processing facilities may be uncompressed, compressed, or a combination of both.

[0031] In another preferred embodiment, in step (5), the compression ratio is 1.1 to 10 (i.e., compressed to 1 / 1.1 to 1 / 10 of the original volume).

[0032] Compared with the prior art, the present invention discloses a highly efficient and energy-saving process for removing solvent from synthetic oil. By using the evaporated and compressed gaseous solvent as the heat source for heating the mixture of synthetic oil and solvent during the solvent removal process, the heat of the solvent after solvent removal is effectively utilized, reducing the energy consumption required to remove the volume of synthetic oil. Attached Figure Description

[0033] Figure 1 This is a schematic diagram of the process method of the present invention.

[0034] The correspondences of the various symbols are as follows: E-1 represents the first heat exchanger, E-2 represents the second heat exchanger, D-1 represents the first separator, D-2 represents the second separator, C-1 represents the compressor, and P-1 represents the pump. Detailed Implementation

[0035] Through long-term and in-depth research, the inventors discovered that after performing a two-stage continuous desolventizing operation on synthetic oil products, the removed solvent can be reused as a heat source in the first-stage desolventizing operation, which can effectively save the heat energy consumed by the system. Furthermore, by controlling the amount of the rectification section, the system can be kept running smoothly, and the quality of the separated solvent can be kept stable. Based on the above findings, the inventors completed this invention.

[0036] the term As used in this article, the term "C2~C" 15 "Olefins" refers to straight-chain or branched olefins having 2 to 15 carbon atoms, including, but not limited to, ethylene, propylene, butene, and similar groups.

[0037] As used in this article, the term "C4~C" 14 "Alkanes" refers to straight-chain or branched alkanes with 4 to 14 carbon atoms, including, but not limited to, n-butane, pentane, hexane, and similar groups.

[0038] As used in this article, the term "C" 10 ~C 5000 "Olefin polymers" refers to straight-chain or branched olefin polymers with 10-5000 carbon atoms, including, but not limited to: hyperbranched polyethylene synthetic base oil, polyalphaolefins, etc.

[0039] As used in this article, the term "esterification" refers to the process by which an acid and an alcohol react to produce an ester and water.

[0040] Process methods for removing solvents from synthetic oils This invention provides a process for removing solvents from synthetic oils, comprising the following steps: (1) The synthetic oil product containing low-boiling-point components is passed into heat exchanger E-1 for primary vaporization to obtain a primary gas-liquid mixture; (2) The obtained primary gas-liquid mixture is fed into separator D-1 to separate the gas phase and the liquid phase. The gas phase is fed into compressor C-1 and the liquid phase is fed into heat exchanger E-2. (3) The remaining solvent in the liquid phase undergoes secondary vaporization in heat exchanger E-2 to obtain a secondary gas-liquid mixture; (4) The secondary gas-liquid mixture is fed into separator D-2 to perform secondary separation of the gas phase and the liquid phase. The resulting liquid phase is the separated synthetic oil. (5) The gas phase obtained from the secondary separation is sent to the compression device C-1. The combined gas phase in the compression device is compressed and then passed into E-1 as a heat source. After condensation, it is reused, and part of it is sent to other facilities for processing.

[0041] See appendix Figure 1 The synthesis liquid to be desolventized is passed into heat exchanger E-1 for primary vaporization, thereby obtaining a primary gas-liquid mixture. The gas phase is the removed solvent, and the liquid phase is the polymerization product in the synthesis liquid. In a preferred embodiment, the liquid is an mPAO liquid, with polyoctene as the main component, and includes low-boiling-point solvents such as dichloromethane. After primary vaporization, the solvent is separated from the main component liquid to form a gas phase, while the main component, polyoctene, remains in the liquid.

[0042] The temperature of the primary vaporization is usually chosen to be slightly higher than that of the solvent. For example, when dichloromethane is used as the solvent, a range of 40-50°C can be selected to ensure that the solvent can be completely separated without causing the loss of polyoctene.

[0043] The primary gas-liquid mixture is fed into separator D-1 for gas-liquid separation. The resulting gas phase is fed into compressor C-1, and the pressurized gas enters the hot side of E-1 as a heat source. The condensed liquid solvent is collected and reused, and part of the compressed gas solvent is subjected to distillation treatment. The liquid phase obtained from D-1 is fed into heat exchanger E-2 through a pump or differential pressure for secondary vaporization to obtain a secondary gas-liquid mixture, wherein the gas phase is the removed residual solvent and the liquid phase is the polymerization product.

[0044] The temperature of the secondary vaporization is typically chosen to be slightly higher than that of the primary vaporization. For example, when dichloromethane is used as the solvent, the primary vaporization temperature is selected in the range of 40-50°C, and the secondary vaporization temperature is selected in the range of 60-80°C or higher to ensure that the residual solvent can be completely separated. The secondary gas-liquid mixture is fed into separator D-2 for gas-liquid separation. The resulting gas phase is treated in the same way as the gas phase separated in the primary gas-liquid mixture, and is then pressurized in compressor C-1 and condensed in E-1 for recycling. The liquid phase obtained from D-2 is the final desolventized product, synthetic oil.

[0045] In this invention, in order to ensure stable operation of the device, the amount of solvent in the distillation column and the amount of recycled solvent can be adjusted. For example, in a preferred embodiment, during the operation of the device, the gas phase components in the system are detected. When the impurity content in the gas phase components is detected to be too high, the amount of solvent in the distillation section is increased, thereby ensuring that the composition of the circulating gas phase components in the device is stable and the device operates smoothly.

[0046] The process provided by this invention performs secondary separation of synthetic oil, which can effectively remove the solvent from the synthetic oil. In step 1, the feed liquid undergoes primary vaporization in the first heat exchanger, where most of the solvent is converted into the gas phase, and then gas-liquid separation occurs in the first separator; subsequently, secondary vaporization occurs in the second heat exchanger, where the remaining small amount of solvent is converted into the gas phase, and gas-liquid separation occurs again in the second separator; the final liquid phase obtained from the two separations is the synthetic oil product, and the solvent converted into the gas phase is returned to the heat exchange channel of the first heat exchanger via a compressor.

[0047] The first heat exchanger has a heat exchange channel and a feed liquid channel. The vaporized solvent can enter the heat exchange channel through the compressor to provide heat for the mixture of solvent and oil, thereby realizing the recycling of heat.

[0048] To make the objectives, technical solutions, and advantages of the present invention clearer, the present invention will be further described in detail below with reference to the accompanying drawings and specific embodiments. It should be understood that the specific embodiments described herein are for illustrative purposes only and are not intended to limit the present invention. Other systems, methods, and / or features of this embodiment will become apparent to those skilled in the art after reviewing the following detailed description. All such additional systems, methods, features, and advantages are intended to be included within this specification, within the scope of the invention, and protected by the appended claims. Further features of the disclosed embodiments are described in the following detailed description, and these features will become apparent from the following detailed description.

[0049] In the accompanying drawings of the embodiments of the present invention, the same or similar reference numerals correspond to the same or similar components. In the description of the present invention, it should be understood that the positional relationships are based on the orientation shown in the drawings and are only for the convenience of describing the present invention and simplifying the description, and are not intended to indicate or imply that the device or component referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, the terms used to describe positional relationships in the drawings are only for illustrative purposes and should not be construed as limiting the present patent. For those skilled in the art, the specific meaning of the above terms can be understood according to the specific circumstances.

[0050] Example 1 (1) A mixture of synthetic oil at 100,000 kg / h, 35°C, and 2 bar and solvent CH2Cl2 is fed into heat exchanger E-1. Part of the solvent is vaporized, and the gas-liquid two-phase flow at 100,000 kg / h, 95°C, and 1 barA enters separator D-1; (2) The gas phase of separator D-1 with a flow rate of 82000 kg / h, 95℃, and 1 barA is sent to compressor C-1, and the liquid phase with a flow rate of 18000 kg / h, 93℃, and 1 barA is sent to heat exchanger E-2 via pump P-1. (3) Heat exchanger E-2 vaporizes most of the remaining solvent, and the gas-liquid two-phase flow of 18000 kg / h, 100℃, and 0.5 barA enters separator D-2; (4) The gas phase of separator D-2 at 300 kg / h, 100℃, and 1 barA is sent to compressor C-1, and the liquid phase at 17700 kg / h, 100℃, and 1 barA is the separated synthetic oil. (5) The 95°C gaseous solvent entering the compressor is compressed and then pressurized to 2 barA. 70000 kg / h of the gaseous solvent is used as the heating medium for heat exchanger E-1. After being condensed to 45°C, it is reused. 12300 kg / h of the gaseous solvent is fed into the rectification section for rectification treatment.

[0051] The process method described in the above embodiment saves 7.5MW of energy by using the evaporated and compressed gaseous solvent as a heat source for heating the synthetic oil and solvent mixture during the solvent removal process, thus significantly reducing energy consumption.

[0052] Example 2 (1) A mixture of synthetic oil at 5000 kg / h, 50 °C, and 2 barA and solvent C7H8 is fed into heat exchanger E-1. Part of the solvent is vaporized, and the gas-liquid two-phase flow at 5000 kg / h, 110 °C, and 0.8 barA enters separator D1; (2) The gas phase of separator D-1 at 4200 kg / h, 110℃, and 0.8 barA is sent to fan C-1, and the liquid phase at 800 kg / h, 110℃, and 0.8 barA is sent to heat exchanger E-2 via pump P-1; (3) Heat exchanger E-2 vaporizes most of the remaining solvent, and the gas-liquid two-phase mixture at 800 kg / h, 150 °C, and 0.8 bar enters separator D-2; (4) The gas phase of separator D-2 at 50 kg / h, 120℃, and 0.8 barA is fed into blower C-1, and the liquid phase at 750 kg / h, 120℃, and 0.8 barA is the separated synthetic oil; (5) The mixed gaseous solvent of 4250 kg / h and 120℃ entering the blower is compressed and then pressurized to 1.5 barA. 3000 kg / h is used as the heating medium of heat exchanger E-1. After being condensed to 65℃, it is reused. 1250 kg / h is passed into the rectification section for rectification treatment.

[0053] The process method described in the above embodiment saves 400kW of energy by using the evaporated and compressed gaseous solvent as a heat source for heating the synthetic oil and solvent mixture during the solvent removal process, thus significantly reducing energy consumption.

[0054] Example 3 (1) A mixture of synthetic oil at 30,000 kg / h, 20°C, and 1.5 barA and solvent C2H5OH is fed into heat exchanger E-1. Part of the solvent is vaporized, and the gas-liquid two-phase flow at 30,000 kg / h, 85°C, and 1 barA enters separator D-1; (2) The gas phase of separator D-1 at 21000 kg / h, 85℃, and 1 barA is sent to compressor C-1, and the liquid phase at 9000 kg / h, 85℃, and 1 barA is sent to heat exchanger E-2 via pump P-1. (3) Heat exchanger E-2 vaporizes most of the remaining solvent, and the gas-liquid two-phase mixture at 9000 kg / h, 100℃, and 6 barA enters separator D-2. (4) The gas phase of separator D-2 at 3500 kg / h, 100℃, and 0.6 barA is fed into a vacuum pump to be pressurized to 1 barA. After mixing with the gas phase of D-1, it enters compressor C-1. The liquid phase at 5500 kg / h, 100℃, and 0.6 barA is the separated synthetic oil. (5) The gaseous solvent with a flow rate of 24,500 kg / h, 90°C and 1 barA that enters the compressor is compressed and then pressurized to 2.5 barA. It is used as the heating medium for heat exchanger E-1 and is condensed to 75°C before being reused.

[0055] The process method described in the above embodiment saves 6.3 kWh by using the evaporated and compressed gaseous solvent as the heat source for heating the synthetic oil and solvent mixture during the solvent removal process. W's energy significantly reduces energy consumption.

[0056] In summary, existing processes use heat transfer media such as steam to heat a mixture of synthetic oil and solvent or unreacted monomers, causing the solvent or unreacted monomers to vaporize for separation, which wastes a lot of heat and costs. The process of this invention constructs a complete synthetic oil desolventizing system, and uses the evaporated and compressed gaseous solvent as a heat source to heat the synthetic oil and solvent mixture during the desolventizing process to recycle the heat, thereby reducing energy consumption and showing good prospects for industrial applications.

[0057] While the present invention has been described above with reference to embodiments, it should be understood that the above are merely preferred embodiments of the invention and are not intended to limit the invention. Many changes and modifications can be made without departing from the scope of the invention. That is, the methods, systems, and devices discussed above are examples. Various configurations can be appropriately omitted, substituted, or added to various processes or components. For example, in alternative configurations, methods can be performed in a different order than described, and / or various components can be added, omitted, and / or combined. Moreover, features described with respect to certain configurations can be combined in various other configurations, such as different aspects and elements of the configuration can be combined in a similar manner. Furthermore, the elements therein can be updated as the technology develops; that is, many elements are examples and do not limit the scope of this disclosure or the claims.

[0058] In summary, the above detailed description is intended to be illustrative rather than restrictive, and it should be understood that the following claims (including all equivalents) are intended to define the spirit and scope of the invention. These embodiments should be understood as illustrative only and not as limiting the scope of protection of the invention. After reading the description of this invention, those skilled in the art can make various alterations or modifications to the invention, and these equivalent changes and modifications also fall within the scope defined by the claims of this invention.

Claims

1. A synthetic oil desolventizing device, characterized in that, The device includes: (a) A solvent removal system for removing solvents from synthetic oils, comprising: The first heat exchanger E-1 has a mutually enclosed heat exchange channel and a liquid feed channel; the liquid feed channel has a liquid feed inlet and a gas-liquid mixing outlet, and the heat exchange channel is used to transfer heat to the liquid feed in the liquid feed channel. The first separator D-1 has a liquid inlet, a gas phase outlet and a liquid phase outlet, and is located downstream of the first heat exchanger E-1 and connected to the gas-liquid mixing outlet of the heat exchanger. The second heat exchanger E-2 has a liquid inlet and a gas-liquid mixing outlet, and the inlet of the second heat exchanger E-2 is connected to the liquid phase outlet of the first separator D-1. The second separator D-2 has a liquid inlet, a gas phase outlet and a liquid phase outlet, and is connected to the gas-liquid mixing outlet of the second heat exchanger E-2. (b) A recovery system for the recycling of solvents; In another preferred embodiment, liquid is transported between the first separator and the second heat exchanger via a pressure difference or a height difference.

2. The apparatus as claimed in claim 1, characterized in that, The recycling system includes: Compression device C-1 is connected to the gas phase outlet of the first separator D-1 and the second separator D-2.

3. The apparatus as described in claim 1, characterized in that, The compression device C-1 is a compressor, vacuum pump, or fan; In another preferred embodiment, a vacuum pump is also provided between the second separator D-2 and the compressor C-1 to reduce the amount of solvent residue in the liquid phase of the second separator D-2.

4. The apparatus as claimed in claim 1, characterized in that, The first separator D-1 and the second heat exchanger E-2 are further comprising: a pump P-1, which has a liquid phase inlet and an outlet; preferably, the pump is located downstream of the separator D-1, and its inlet is connected to the liquid phase outlet of the first separator, and its outlet is connected to the inlet of the second heat exchanger.

5. A process for removing solvents from synthetic oil, comprising the following steps: (1) The synthetic oil product containing low-boiling-point components is passed into heat exchanger E-1 for primary vaporization to obtain a primary gas-liquid mixture; (2) The obtained primary gas-liquid mixture is fed into separator D-1 to separate the gas phase and the liquid phase. The gas phase is fed into compression device C-1 and the liquid phase is fed into heat exchanger E-2. (3) The remaining solvent in the liquid phase undergoes secondary vaporization in heat exchanger E-2 to obtain a secondary gas-liquid mixture; (4) The secondary gas-liquid mixture is fed into separator D-2 to perform secondary separation of the gas phase and the liquid phase. The resulting liquid phase is the separated synthetic oil. (5) The gas phase obtained from the secondary separation is sent to the compression device C-1. After compression, part of the combined gas phase in the compressor is sent to the heat exchanger E-1 as a heat source, and part is sent to the distillation column for processing. In another preferred embodiment, in step (2), the liquid phase is introduced into heat exchanger E-2 via pump P-1; In another preferred embodiment, in step (5), the combined gas phase obtained is compressed and then completely fed into heat exchanger E-1 as a heating medium. In another preferred embodiment, a vacuum pump can be added between separator D-2 and compressor C-1 in step (4) to reduce the amount of solvent residue in the liquid phase of D-2.

6. The process as described in claim 5, characterized in that, The synthetic oil product is selected from the following group: From C2~C 15 C obtained from olefin synthesis 10 ~C 5000 olefin polymers; Oil synthesized from natural gas; Oil synthesized from syngas (CO + H2); or Oil obtained by dehydration of fatty acids and fatty alcohols through esterification reaction under the action of a catalyst; In another preferred embodiment, the synthetic oil product is a fluid product at room temperature and pressure; In another preferred embodiment, the synthetic oil product is an octene polymer.

7. The process as described in claim 5, characterized in that, The solvent is selected from the group consisting of: acetonitrile, ethanol, diethyl ether, toluene, and C4~C4 solvents. 14 Alkanes, dichloromethane, DMF, or combinations thereof; In another preferred embodiment, the solvent is dichloromethane.

8. The process as described in claim 5, characterized in that, The solvent is a polymeric monomer used to prepare the synthetic oil; In another preferred embodiment, the solvent may be a pure solvent or a mixture of a pure solvent and other non-solvent components.

9. The process as described in claim 5, characterized in that, In step (5), the solvent introduced into the distillation column for processing accounts for 10-50 wt% of the total solvent volume; In another preferred embodiment, step (5) may also be passed into a distillation column without compression; In another preferred embodiment, the solvent in step (5) may be uncompressed, compressed, or a combination of both.

10. The process for removing solvent from synthetic oil according to claim 5, characterized in that, In step (5), the compression ratio is 1.1 to 10 (i.e., compressed to 1 / 1.1 to 1 / 10 of the original volume).

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