Co-production system of poly-alpha-olefin base oil and white oil

Abstract

The utility model provides a co-production system of poly alpha-olefin base oil and white oil, the co-production system comprises a distillation unit, a deoxidation device, a polymerization reaction unit, a catalyst separation device and a product separation unit, the distillation unit is used for cutting Fischer-Tropsch synthetic oil to obtain C9-C11 distillate oil, C9-distillate oil and C11 + distillate oil; the deoxidation device is used for removing oxygen-containing compounds in C9-C11 distillate oil to obtain a deoxidation product, the polymerization reaction unit is used for enabling the deoxidation product to be subjected to polymerization reaction under the catalysis of a catalyst to obtain a first polymerization product, and the catalyst separation device is used for separating the catalyst in the first polymerization product to obtain a recovered catalyst and a separated product; and the product separation unit is used for separating the separation product to obtain white oil and poly-alpha-olefin base oil. By adopting the co-production system, co-production of the poly-alpha-olefin base oil and the white oil can be realized, the added value of the product is improved, and meanwhile, recycling of the catalyst can also be realized.

Description

Technical Field

[0001] The utility model relates to the technical field of lubricating oil base oil, in particular to a co-production system of poly-alpha-olefin and white oil. Background Art

[0002] As a base oil with excellent performance, polyalphaolefin has the advantages of wide liquid phase range, low pour point, high viscosity index, good viscosity-temperature performance, high flash point, good low-temperature fluidity, good oxidation stability and thermal stability, and small evaporation loss. It is widely used in demanding environments such as high-viscosity industrial gear oil, extreme cold hydraulic oil, screw compressor and refrigeration oil.

[0003] The existing document (CN115678600A) discloses a method for preparing a low-viscosity poly-α-olefin lubricant, which comprises: cutting a Fischer-Tropsch heavy oil raw material to obtain a C8-C60 poly-α-olefin lubricant containing 50-60% α-olefins, 3-5% oxygen-containing compounds and the remainder normal alkanes. 12 Then, the polymerization reaction is carried out with BF3 as a catalyst, and the product is then subjected to hydrogenation treatment and atmospheric distillation in sequence to obtain C8~C 12 The mixed normal alkane and PAO (poly alpha olefin) crude products are distilled at atmospheric pressure to obtain normal alkane series products and PAO series products. However, this process cannot realize the recycling of catalysts, and its production cost is high.

[0004] In summary, it is necessary to study and develop a co-production system of poly-α-olefin base oil and white oil with simple process flow, high catalyst utilization, low cost and high product added value. Utility Model Content

[0005] The main purpose of the utility model is to provide a poly-alpha-olefin and white oil co-production system to solve the problems of difficulty in realizing catalyst recycling, high production cost and low product added value in the prior art production system of poly-alpha-olefin base oil.

[0006] In order to achieve the above-mentioned purpose, according to the utility model, a co-production system of poly-alpha-olefin base oil and white oil is provided, and the co-production system of poly-alpha-olefin and white oil comprises a distillation unit, a deoxygenation device, a polymerization reaction unit, a catalyst separation device and a product separation unit; wherein the distillation unit is used to cut the Fischer-Tropsch synthetic oil to obtain C9-C 11 Distillate, C9-distillate and C 11 + distillate oil, the distillation unit is equipped with a Fischer-Tropsch synthetic oil inlet, C9~C 11 Distillate export, C9-distillate export and C 11 + Distillate oil outlet; deoxygenation device is used to remove C9~C 11The oxygen-containing compounds in the distillate oil are used to obtain deoxygenated products. The deoxygenation device is equipped with C9~C 11 Distillate oil inlet and deoxygenated product outlet; C9~C 11 Distillate oil inlet and C9~C 11 The first catalyst inlet is connected to the first catalyst inlet; the first catalyst inlet is connected to the first catalyst inlet; the product separation unit is used to separate the catalyst in the first polymer product to obtain white oil and poly-α-olefin base oil, and the product separation unit is provided with a first separated product inlet, a first white oil outlet and a first poly-α-olefin base oil outlet; the first separated product inlet is connected to the first separated product outlet.

[0007] Furthermore, the catalyst separation device is a first atmospheric distillation tower, and a first cooler is provided at the top of the first atmospheric distillation tower.

[0008] Furthermore, the recovered catalyst outlet is connected to the first catalyst inlet via a recovered catalyst delivery pipeline, and a compressor is provided on the recovered catalyst delivery pipeline.

[0009] Further, the product separation unit includes a first distillation device and a second distillation device; wherein the first distillation device is used to distill the separation product to obtain a distillation product and naphtha, and the first distillation device is provided with a first separation product inlet, a first distillation product outlet and a first naphtha outlet; the first separation product inlet is connected to the first separation product outlet through a separation product conveying pipeline, and a first preheating device is provided on the separation product conveying pipeline; the second distillation device is provided with a first distillation product inlet, a first white oil outlet, a second poly-α-olefin base oil outlet, a third poly-α-olefin base oil outlet, a fourth poly-α-olefin base oil outlet and a fifth poly-α-olefin base oil outlet; the second poly-α-olefin base oil outlet is used to discharge PAO2 base oil, the third poly-α-olefin base oil outlet is used to discharge PAO4 base oil, the fourth poly-α-olefin base oil outlet is used to discharge PAO6 base oil, and the fifth poly-α-olefin base oil outlet is used to discharge PAO15 base oil; the first distillation product inlet is connected to the first distillation product outlet through a first distillation product conveying pipeline, and a second preheating device is provided on the first distillation product conveying pipeline.

[0010] Furthermore, the first distillation device is a second atmospheric distillation tower, the second distillation device is a vacuum distillation tower, the second poly-α-olefin base oil outlet, the third poly-α-olefin base oil outlet and the fourth poly-α-olefin base oil outlet are arranged from top to bottom on the side of the vacuum distillation tower, and the fifth poly-α-olefin base oil outlet is arranged at the bottom of the vacuum distillation tower.

[0011] Furthermore, the product separation unit also includes a second cooler and a first oil-water separation device; wherein the second cooler is provided with a first top material inlet, a second naphtha outlet and a recovery top material outlet; the first top material inlet is connected to the first naphtha outlet, and the recovery top material outlet is connected to the first separation product inlet; the first oil-water separation device is provided with a second top material inlet, a first water phase outlet and a second white oil outlet; the second top material inlet is connected to the first white oil outlet.

[0012] Furthermore, the polymerization reaction unit includes a first polymerization reaction device, a second polymerization reaction device and a detection and screening device; wherein the first polymerization reaction device is provided with a first deoxygenated product inlet, a first catalyst inlet and a second polymerization product outlet; the second polymerization reaction device is provided with a second polymerization product inlet, a second catalyst inlet and a third polymerization product outlet; the second polymerization product inlet is connected to the second polymerization product outlet; the second catalyst inlet is connected to the recovered catalyst outlet; the detection and screening device is used to detect and screen to obtain the first polymerization product and the first unqualified product, and the detection and screening device is provided with a third polymerization product inlet, a first polymerization product outlet and a first unqualified product outlet; the third polymerization product inlet is connected to the third polymerization product outlet; the first unqualified product outlet is connected to the first deoxygenated product inlet.

[0013] Furthermore, the inner cavities of the first polymerization reaction device and the second polymerization reaction device are independently provided with cooling components.

[0014] Furthermore, the outer peripheries of the first polymerization reaction device and the second polymerization reaction device are independently provided with jackets, and the inner cavities of the jackets are filled with cooling medium.

[0015] Furthermore, the first polymerization reaction device and the second polymerization reaction device are independently selected from a bubbling reactor, a loop reactor, a microreactor or a stirred tank reactor.

[0016] Furthermore, the polymerization reaction unit also includes a mixing device, which is provided with a second deoxygenated product inlet, a third catalyst inlet and a mixture outlet; the second deoxygenated product inlet is connected to the deoxygenated product outlet, the third catalyst inlet is connected to the recovered catalyst outlet, and the mixture outlet is connected to the first deoxygenated product inlet or the first catalyst inlet.

[0017] Furthermore, the above-mentioned co-production system provided in the present application also includes an alkali washing unit, which includes an alkali washing device, a fluorine content detection and screening device and a second oil-water separation device; wherein the alkali washing device is used to wash the separation product with alkali solution to remove fluoride ions to obtain an alkali washing product, and the alkali washing device is provided with a second separation product inlet, an alkali solution inlet and an alkali washing product outlet; the second separation product inlet is connected to the first separation product outlet; the fluorine content detection and screening device is used to detect the fluorine content in the alkali washing product and screen it to obtain a qualified product and a second unqualified product, and the fluorine content detection and screening device is provided with an alkali washing product inlet, a qualified product outlet and a second unqualified product outlet; the alkali washing product inlet is connected to the alkali washing product outlet, and the second unqualified product outlet is connected to the second separation product inlet; the second oil-water separation device is used to perform oil-water separation on the qualified product to obtain a water phase and an oil phase, and the second oil-water separation device is provided with a qualified product inlet, a second water phase outlet and a first oil phase outlet; the qualified product inlet is connected to the qualified product outlet.

[0018] Furthermore, the above-mentioned co-production system provided in the present application also includes a hydrogenation reaction unit, which includes a catalytic hydrogenation reaction device, a hydrogen separation device, a gas compression device, a liquid-liquid separation device and a third oil-water separation device; wherein the catalytic hydrogenation reaction device is used to cause hydrogen and an oil phase to undergo a catalytic hydrogenation reaction under the catalysis of a hydrogenation catalyst, and the catalytic hydrogenation reaction device is provided with an oil phase inlet, a hydrogenation catalyst inlet, a hydrogen inlet and a catalytic hydrogenation reaction product outlet; the oil phase inlet is connected to the first oil phase outlet; the hydrogen separation device is provided with a catalytic hydrogenation reaction product inlet, a recovered hydrogen outlet and a second separated product outlet, and the hydrogenation reaction product inlet is connected to the The hydrogenation reaction product outlet is connected; the recovered hydrogen outlet is connected to the hydrogen inlet; the gas compression device is provided with a recovered hydrogen inlet and a compressed hydrogen outlet; the recovered hydrogen inlet is connected to the recovered hydrogen outlet through a hydrogen delivery pipeline, and a third cooler is provided on the hydrogen delivery pipeline; the liquid-liquid separation device is provided with a third separation product inlet, a third separation product outlet and an impurity outlet; the third separation product inlet is connected to the second separation product outlet; the third oil-water separation device is provided with a fourth separation product inlet, a third water phase outlet and a second oil phase outlet; the fourth separation product inlet is connected to the third separation product outlet; the second oil phase outlet is connected to the first separation product inlet.

[0019] Furthermore, the distillation unit comprises a third atmospheric distillation apparatus and a fourth atmospheric distillation apparatus which are sequentially connected in liquid phase, the third atmospheric distillation apparatus is provided with a Fischer-Tropsch synthetic oil inlet and a C9-fraction oil outlet, and the fourth atmospheric distillation apparatus is provided with C9-C 11 Distillate export and C 11 + Distillate export.

[0020] Furthermore, the deoxygenation device is an adsorption device, an adsorbent layer is arranged inside the adsorption device, and the material of the adsorbent layer is a molecular sieve; a nitrogen purge component is arranged inside the deoxygenation device.

[0021] Furthermore, the deoxygenated product outlet is connected to the first deoxygenated product inlet through a deoxygenated product delivery pipeline, and a third preheating device is provided on the deoxygenated product delivery pipeline.

[0022] Furthermore, the above-mentioned co-production system provided in the present application also includes a cooling unit, which includes a cooling medium storage tank, a cooling water pump and a cooling unit; wherein the cooling unit is used to output the cooling medium to the cooling unit; the cooling unit is respectively connected to the distillation unit, the deoxygenation device, the polymerization reaction unit, the catalyst separation device, the alkali washing unit, the hydrogenation reaction unit and the product separation unit in a skid-mounted manner.

[0023] Applying the technical solution of the utility model, the above-mentioned poly-alpha-olefin base oil and white oil co-production system provided in the present application comprises a distillation unit, a deoxygenation device, a polymerization reaction unit, a catalyst separation device and a product separation unit. The distillation unit can distill the Fischer-Tropsch synthetic oil to obtain C9-C 11 Distillate oil; deoxygenation unit can be used for C9~C 11 The distillate oil is deoxygenated to obtain a deoxygenated product; the polymerization reaction unit can make the deoxygenated product undergo a polymerization reaction under the catalysis of the catalyst to obtain a first polymerization product; the catalyst separation device can separate the catalyst in the polymerization product to obtain a separated product, and the catalyst separation device is provided with a catalyst recovery outlet, which is connected to the first catalyst inlet provided in the polymerization reaction unit, so that the catalyst separated in the catalyst separation device is returned to the polymerization reaction unit for reuse; the product separation unit is used to separate and obtain white oil and poly-α-olefin base oil. Compared with the traditional poly-α-olefin base oil production device, the above-mentioned co-production system of the present application can not only realize the co-production of poly-α-olefin base oil and white oil, and improve the added value of the product, but also realize the recovery and utilization of the catalyst, and improve the utilization rate of the catalyst, thereby reducing the cost; for C9~C 11 Deoxygenation treatment of distillate oil can improve the purity and reaction efficiency of polymerization reaction raw materials, thereby improving the quality of white oil and poly-alpha-olefin base oil. BRIEF DESCRIPTION OF THE DRAWINGS

[0024] The drawings constituting part of the present application are used to provide a further understanding of the present invention. The exemplary embodiments of the present invention and their descriptions are used to explain the present invention and do not constitute an improper limitation on the present invention. In the drawings:

[0025] Figure 1 A schematic diagram of the structure of a co-production system of poly-alpha-olefin base oil and white oil in one embodiment of the utility model is shown;

[0026] Figure 2 The schematic diagram of the structure of the co-production system of poly-α-olefin base oil and white oil in another embodiment of the utility model is shown.

[0027] The above drawings include the following reference numerals:

[0028] 100, distillation unit; 101, Fischer-Tropsch synthetic oil inlet; 102, C9~C 11 Distillate oil export; 103, C9- distillate oil export; 104, C 11 + distillate oil outlet; 110, third atmospheric distillation unit; 120, fourth atmospheric distillation unit;

[0029] 200, deoxidation device; 201, C9~C 11 Distillate oil inlet; 202, deoxygenation product outlet;

[0030] 300, polymerization reaction unit; 301, first deoxygenation product inlet; 302, first catalyst inlet; 303, first polymerization product outlet; 310, first polymerization reaction device; 320, second polymerization reaction device; 321, second catalyst inlet; 330, detection and screening device; 340, mixing device; 341, second deoxygenation product inlet; 342, third catalyst inlet; 343, mixture outlet;

[0031] 400, catalyst separation device; 401, first polymerization product inlet; 402, catalyst recovery outlet; 403, first separation product outlet;

[0032] 500, product separation unit; 501, first separation product inlet; 502, first white oil outlet; 503, first poly-α-olefin base oil outlet; 510, first distillation device; 520, first preheating device; 530, second distillation device; 531, second poly-α-olefin base oil outlet; 532, third poly-α-olefin base oil outlet; 533, fourth poly-α-olefin base oil outlet; 534, fifth poly-α-olefin base oil outlet; 540, second preheating device; 550, second cooler; 551, second naphtha outlet; 560, first oil-water separation device; 561, first water phase outlet; 562, second white oil outlet;

[0033] 600, compressor;

[0034] 700, alkali washing unit; 710, alkali washing device; 711, second separated product inlet; 712, alkali solution inlet; 720, fluorine content detection and screening device; 730, second oil-water separation device; 731, second water phase outlet; 732, first oil phase outlet;

[0035] 800, hydrogenation reaction unit; 810, catalytic hydrogenation reaction device; 811, oil phase inlet; 812, hydrogenation catalyst inlet; 813, hydrogen inlet; 820, hydrogen separation device; 830, gas compression device; 840, third cooler; 850, liquid-liquid separation device; 851, impurity outlet; 860, third oil-water separation device; 861, third water phase outlet; 862, second oil phase outlet;

[0036] 900. A third preheating device. DETAILED DESCRIPTION

[0037] It should be noted that, in the absence of conflict, the embodiments and features in the embodiments of the present application can be combined with each other. The present utility model will be described in detail below in conjunction with the embodiments.

[0038] As described in the background technology, the production of poly-alpha-olefin base oil in the prior art has the problems of difficult catalyst recycling, high production cost and low product added value. In order to solve the above technical problems, the present application provides a co-production system of poly-alpha-olefin base oil and white oil, such as Figure 1 or Figure 2 As shown in FIG. 1 , the cogeneration system includes a distillation unit 100, a deoxygenation device 200, a polymerization reaction unit 300, a catalyst separation device 400 and a product separation unit 500. The distillation unit 100 is used to cut the Fischer-Tropsch synthetic oil to obtain C9-C 11 Distillate, C9-distillate and C 11 + distillate oil, the distillation unit 100 is provided with a Fischer-Tropsch synthetic oil inlet 101, C9~C 11 Distillate oil outlet 102, C9-distillate oil outlet 103 and C 11 + Distillate oil outlet 104; deoxygenation device 200 is used to remove C9~C 11 The oxygen-containing compounds in the distillate oil are used to obtain the deoxygenated product. The deoxygenation device 200 is provided with C9~C 11 Distillate oil inlet 201 and deoxygenated product outlet 202; C9~C 11 Distillate oil inlet 201 and C9~C 11The polymerization reaction unit 300 is used to make the deoxygenated product undergo polymerization reaction under the catalysis of the catalyst to obtain a first polymerization product. The polymerization reaction unit 300 is provided with a first deoxygenated product inlet 301, a first catalyst inlet 302 and a first polymerization product outlet 303. The first deoxygenated product inlet 301 is connected to the deoxygenated product outlet 202, and the first catalyst inlet 302 is used to introduce the catalyst. The catalyst separation device 400 is used to separate the catalyst in the polymerization product to obtain a recovered catalyst and a separated product. The catalyst separation device 400 is provided with a first A polymerization product inlet 401, a catalyst recovery outlet 402 and a first separation product outlet 403; the first polymerization product inlet 401 is connected to the first polymerization product outlet 303; the catalyst recovery outlet 402 is connected to the first catalyst inlet 302; the product separation unit 500 is used to separate the above separation products to obtain white oil and poly-α-olefin base oil, and the product separation unit 500 is provided with a first separation product inlet 501, a first white oil outlet 502 and a first poly-α-olefin base oil outlet 503; the first separation product inlet 501 is connected to the first separation product outlet 403.

[0039] The above-mentioned poly-alpha-olefin base oil and white oil co-production system provided in the present application comprises a distillation unit 100, a deoxygenation device 200, a polymerization reaction unit 300, a catalyst separation device 400 and a product separation unit 500. The distillation unit 100 can distill the Fischer-Tropsch synthetic oil to obtain C9-C 11 Distillate oil; deoxygenation device 200 can be used for C9~C 11 The distillate oil is deoxygenated to obtain a deoxygenated product; the polymerization reaction unit 300 can make the deoxygenated product undergo a polymerization reaction under the catalysis of the catalyst to obtain a first polymerization product; the catalyst separation device 400 can separate the catalyst in the first polymerization product to obtain a separated product, and the catalyst separation device 400 is provided with a catalyst recovery outlet 402, and the catalyst recovery outlet 402 is connected to the first catalyst inlet 302 set in the polymerization reaction unit 300, so that the catalyst separated in the catalyst separation device 400 is returned to the polymerization reaction unit 300 for reuse; the product separation unit 500 is used to separate and obtain white oil and poly-α-olefin base oil. Compared with the traditional poly-α-olefin base oil production device, the above-mentioned co-production system of the present application can not only realize the co-production of poly-α-olefin base oil and white oil, improve the added value of the product, but also realize the recovery and utilization of the catalyst, improve the utilization rate of the catalyst, and thus reduce the cost; the setting of the deoxygenation device 200 can remove C9~C 11 The oxygen-containing compounds in the distillate oil can improve the purity of the polymerization reaction raw materials and the reaction efficiency, thereby improving the quality of white oil and poly-alpha-olefin base oil.

[0040] In a preferred embodiment, the catalyst separation device 400 is a first atmospheric distillation tower, and a first cooler is provided at the top of the first atmospheric distillation tower. Compared with other types of distillation towers, the atmospheric distillation tower has a lower cost and is easier to operate. It only needs simple heating and cooling to separate the catalyst from the first polymer product, and has a high separation efficiency. At the same time, the use of the atmospheric distillation tower is also conducive to reducing production costs.

[0041] In order to improve the reaction efficiency of the polymerization reaction, thereby increasing the recovery rate of the catalyst and reducing the cost, preferably, the catalyst is BF3.

[0042] In a preferred embodiment, the recovered catalyst outlet 402 is connected to the first catalyst inlet 302 through a recovered catalyst delivery pipeline, and a compressor 600 is provided on the recovered catalyst delivery pipeline. The compressor 600 is used to pressurize the recovered catalyst to facilitate the delivery of the recovered catalyst back to the polymerization reaction unit 300 for reuse, which is beneficial to improve the recovery rate of the catalyst, thereby helping to reduce costs.

[0043] In a preferred embodiment, the product separation unit 500 includes a first distillation device 510, which is used to distill the separation product to obtain a distillation product and naphtha. The first distillation device 510 is provided with a first separation product inlet 501, a first distillation product outlet and a first naphtha outlet; the first separation product inlet 501 is connected to the first separation product outlet 403 through a separation product delivery pipeline, and a first preheating device 520 is provided on the separation product delivery pipeline. The setting of the first distillation device 510 can distill the first separation product to obtain naphtha and distillation products, which is conducive to improving the added value of the product. The setting of the first preheating device 520 facilitates the preheating of the separation product, which is conducive to improving the separation efficiency of naphtha and distillation products, thereby facilitating the improvement of the added value of the product.

[0044] In a preferred embodiment, the product separation unit 500 includes a second distillation device 530, which is provided with a first distillation product inlet, a first white oil outlet 502, a second polyα-olefin base oil outlet 531, a third polyα-olefin base oil outlet 532, a fourth polyα-olefin base oil outlet 533 and a fifth polyα-olefin base oil outlet 534; the second polyα-olefin base oil outlet 531 is used to discharge PAO2 base oil, the third polyα-olefin base oil outlet 532 is used to discharge PAO4 base oil, the fourth polyα-olefin base oil outlet 533 is used to discharge PAO6 base oil, and the fifth polyα-olefin base oil outlet 534 is used to discharge PAO15 base oil; the first distillation product inlet is connected to the first distillation product outlet through a first distillation product conveying pipeline, and a second preheating device 540 is provided on the first distillation product conveying pipeline. The setting of the second distillation device 530 facilitates the distillation of the distillation product to obtain white oil, PAO2 base oil, PAO4 base oil, PAO6 base oil and PAO15 base oil, which is beneficial to increasing the added value of the product. The second preheating device 540 can preheat the distillation product, which is beneficial to improving the separation efficiency of the second distillation device 530, thereby facilitating increasing the yield of the above-mentioned products.

[0045] The atmospheric distillation tower has low cost and is easy to operate. It only needs simple heating and cooling to separate substances. In a preferred embodiment, the first distillation device 510 is a second atmospheric distillation tower. Compared with other types of distillation towers, the atmospheric distillation tower is convenient for extracting naphtha from the top of the tower, discharging the distillation product from the bottom of the tower and passing it into the second distillation device 530 for further separation, which is beneficial to increase the added value of the product and also beneficial to reduce production costs.

[0046] In a preferred embodiment, the second distillation device 530 is a vacuum distillation tower, and the second polyalphaolefin base oil outlet 531, the third polyalphaolefin base oil outlet 532 and the fourth polyalphaolefin base oil outlet 533 are arranged from top to bottom on the side of the vacuum distillation tower, and the fifth polyalphaolefin base oil outlet 534 is arranged at the bottom of the vacuum distillation tower. Compared with other types of distillation towers, the second distillation device 530 is a vacuum distillation tower, which can reduce the boiling point of the distillation product by reducing the pressure, which is beneficial to reduce the occurrence of thermal decomposition and improve the separation efficiency of the distillation product; by controlling the temperature and pressure of the vacuum distillation tower, it is beneficial to separate products of different distillation ranges, and multiple product outlets are arranged from top to bottom and at the bottom of the vacuum distillation tower, which is beneficial to discharge the above-mentioned various base oils obtained in the vacuum distillation process, thereby facilitating the added value of the product.

[0047] In a preferred embodiment, the product separation unit 500 further includes a second cooler 550, which is provided with a first tower top material inlet, a second naphtha outlet 551 and a recovery tower top material outlet; the first tower top material inlet is connected to the first naphtha outlet, and the recovery tower top material outlet is connected to the first separated product inlet 501. The second cooler 550 is used to cool the naphtha produced from the top of the atmospheric distillation tower, and a part of the cooled naphtha is returned to the first distillation device 510 as the recovery tower top material, and the other part is discharged through the second naphtha outlet 551 and sold as a finished product; returning this part of naphtha to the atmospheric distillation tower as the recovery tower top stream is conducive to controlling the temperature of the atmospheric distillation tower, thereby facilitating the improvement of the separation efficiency of naphtha and distillation products, and further facilitating the improvement of product added value.

[0048] In a preferred embodiment, the product separation unit 500 further includes a first oil-water separation device 560, which is provided with a second tower top material inlet, a first water phase outlet 561 and a second white oil outlet 562; the second tower top material inlet is connected to the first white oil outlet 502. The first oil-water separation device 560 is used to separate the first white oil produced from the top of the vacuum distillation tower, separate and remove the water phase in the first white oil to obtain a white oil product. The provision of the first oil-water separation device 560 is conducive to improving the purity of the white oil, and selling the obtained white oil as a finished product is conducive to increasing the added value of the product.

[0049] In order to store the obtained products and to reduce the damage to the equipment caused by the heat carried by the products when discharged, thereby reducing the cost of equipment maintenance and servicing, in a preferred embodiment, the product separation unit 500 also includes a naphtha storage device, a white oil storage device, a second poly-α-olefin base oil storage device, a third poly-α-olefin base oil storage device, a fourth poly-α-olefin base oil storage device and a fifth poly-α-olefin base oil storage device; wherein the naphtha storage device is provided with a naphtha inlet, which is connected to the naphtha outlet; the white oil storage device is provided with a white oil inlet, which is connected to the third white oil outlet; the second poly-α-olefin base oil storage device is provided with a second poly-α-olefin base oil inlet, which is connected to the second poly-α-olefin base oil outlet through a second poly-α-olefin base oil transportation pipeline, and preferably the second poly-α-olefin base oil transportation pipeline is provided with a a fourth cooler; the third poly-α-olefin base oil storage device is provided with a third poly-α-olefin base oil inlet, the third poly-α-olefin base oil inlet is connected to the third poly-α-olefin base oil outlet through a third poly-α-olefin base oil delivery pipeline, and preferably a fifth cooler is provided on the third poly-α-olefin base oil delivery pipeline; the fourth poly-α-olefin base oil storage device is provided with a fourth poly-α-olefin base oil inlet, the fourth poly-α-olefin base oil inlet is connected to the fourth poly-α-olefin base oil outlet through a fourth poly-α-olefin base oil delivery pipeline, and preferably a sixth cooler is provided on the fourth poly-α-olefin base oil delivery pipeline; the fifth poly-α-olefin base oil storage device is provided with a fifth poly-α-olefin base oil inlet, the fifth poly-α-olefin base oil inlet is connected to the fifth poly-α-olefin base oil outlet through a fifth poly-α-olefin base oil delivery pipeline, and preferably a seventh cooler is provided on the fifth poly-α-olefin base oil delivery pipeline.

[0050] In a preferred embodiment, the polymerization reaction unit 300 includes a first polymerization reaction device 310, a second polymerization reaction device 320 and a detection and screening device 330, wherein the first polymerization reaction device 310 is provided with a first deoxygenated product inlet 301, a first catalyst inlet 302 and a second polymerization product outlet; the second polymerization reaction device 320 is provided with a second polymerization product inlet, a second catalyst inlet 321 and a third polymerization product outlet; the second polymerization product inlet is connected to the second polymerization product outlet; the second catalyst inlet 321 is connected to the recovered catalyst outlet 402; the detection and screening device 330 is used to detect and screen to obtain a first polymerization product and a first unqualified product, and the detection and screening device 330 is provided with a third polymerization product inlet, a first polymerization product outlet 303 and a first unqualified product outlet; the third polymerization product inlet is connected to the third polymerization product outlet; the first unqualified product outlet is connected to the first deoxygenated product inlet 301.

[0051] The first polymerization reaction device 310 and the second polymerization reaction device 320 are connected in a liquid phase series manner. When the conversion rate of the product in the first polymerization reaction device 310 reaches 50-80%, it is sent to the second polymerization reaction device 320 for polymerization reaction. Compared with a single polymerization reaction device, the use of two liquid phase series polymerization reaction devices for polymerization reaction is conducive to dispersing the reaction heat released by the polymerization reaction, thereby facilitating the improvement of the conversion rate of the polymerization reaction. Compared with other ranges, limiting the conversion rate of the polymerization reaction in the first polymerization reaction device 310 to the above range is conducive to reducing the reaction heat released by the polymerization reaction. The second polymerization reaction device 320 is used to make the product obtained by the first polymerization reaction device 310 further undergo polymerization reaction under the action of a catalyst, which is conducive to dispersing the reaction heat released by the polymerization reaction while improving the conversion rate of the polymerization reaction, thereby facilitating the improvement of the added value of the product.

[0052] The setting of the detection and screening device 330 can detect and screen the conversion rate of the third polymerization product obtained in the second polymerization reaction device 320. When its conversion rate is ≥90%, it is a qualified product, and the qualified product is discharged through the first polymerization product outlet 303. When its conversion rate is <90%, it is an unqualified product, and the unqualified product returns to the first polymerization reaction device 310 through the first unqualified product outlet to participate in the polymerization reaction again. The setting of the detection and screening device 330 is conducive to better controlling the conversion rate of the polymerization reaction, thereby helping to increase the added value of the product.

[0053] In a preferred embodiment, the inner cavities of the first polymerization reaction device 310 and the second polymerization reaction device 320 are independently provided with cooling components, respectively; the cooling components are used to cool the first polymerization reaction device 310 and the second polymerization reaction device 320, which is beneficial to reduce the damage to the equipment caused by the strong heat release in the polymerization reaction, thereby reducing the maintenance of the equipment, and further helping to reduce production costs.

[0054] In order to improve the cooling effect of the cooling component on the first polymerization reaction device 310 and the second polymerization reaction device 320, preferably, the cooling component is a cooling coil.

[0055] In a preferred embodiment, jackets are independently configured on the peripheries of the first polymerization reaction device 310 and the second polymerization reaction device 320, and the inner cavities of the jackets are filled with cooling medium. The jackets filled with cooling medium in the inner cavities can be used to cool the first polymerization reaction device 310 and the second polymerization reaction device 320, which is conducive to reducing the damage to the equipment caused by strong heat release in the polymerization reaction, thereby reducing the maintenance of the equipment, and further helping to reduce production costs.

[0056] In order to improve the cooling effect on the first polymerization reaction device 310 and the second polymerization reaction device 320, preferably, the material of the cooling medium includes but is not limited to ethylene glycol and / or water.

[0057] In a preferred embodiment, the first polymerization reaction device 310 and the second polymerization reaction device 320 are independently selected from a bubbling reactor, a loop reactor, a microreactor or a stirred tank reactor. Compared with other types of reactors, the use of the above reactors is conducive to improving the reaction efficiency and conversion rate of the polymerization reaction, thereby helping to increase the added value of the product.

[0058] In a preferred embodiment, the polymerization reaction unit 300 further includes a mixing device 340, which is provided with a second deoxygenated product inlet 341, a third catalyst inlet 342 and a mixture outlet 343; the second deoxygenated product inlet 341 is connected to the deoxygenated product outlet 202, the third catalyst inlet 342 is connected to the recovered catalyst outlet 402, and the mixture outlet 343 is connected to the first deoxygenated product inlet 301 or the first catalyst inlet 302. The setting of the mixing device 340 can make the deoxygenated product and the catalyst mix to obtain a mixture, which is conducive to improving the dispersibility of the two, thereby facilitating the reaction efficiency of the polymerization reaction. The mixture outlet 343 is connected to the first deoxygenated product inlet 301 or the first catalyst inlet 302, which can pass the mixture into the first polymerization reaction device 310 for polymerization reaction, thereby saving the mixing time during the polymerization reaction, and further facilitating the improvement of production efficiency. The third catalyst inlet 342 is connected to the recovered catalyst outlet 402 so that the catalyst separated in the catalyst separation device 400 can be returned to the mixing device 340 for reuse, which is beneficial to improving the recovery rate of the catalyst and thus beneficial to reducing costs.

[0059] In a preferred embodiment, the above-mentioned co-production system provided in the present application also includes an alkali washing unit 700, which includes an alkali washing device 710, a fluorine content detection and screening device 720 and a second oil-water separation device 730, wherein the alkali washing device 710 is provided with a second separation product inlet 711, an alkali solution inlet 712 and an alkali washing product outlet; the second separation product inlet 711 is connected to the first separation product outlet 403; the fluorine content detection and screening device 720 is provided with an alkali washing product inlet, a qualified product outlet and a second unqualified product outlet; the alkali washing product inlet is connected to the alkali washing product outlet, and the second unqualified product outlet is connected to the second separation product inlet 711; the second oil-water separation device 730 is provided with a qualified product inlet, a second water phase outlet 731 and a first oil phase outlet 732; the qualified product inlet is connected to the qualified product outlet.

[0060] The alkali washing device 710 is used to wash the separated product with alkali solution to remove fluoride ions to obtain an alkali washed product, which is beneficial to improving the purity of the alkali washed product and thus beneficial to increasing the added value of the product.

[0061] The fluorine content detection and screening device 720 is used to detect the free fluorine ion content in the alkali-washed product and screen out qualified products and second unqualified products. The free fluorine ion content of the alkali-washed product is detected. When the free fluorine ion content is less than 10ppm, it is a qualified product. The qualified product is passed through the qualified product outlet to the second oil-water separation device 730 for further separation; when the free fluorine ion content is ≥10ppm, it is a second unqualified product. The second unqualified product is returned to the alkali-washing device 710 through the second unqualified product outlet for alkali washing again. The setting of the fluorine content detection and screening device 720 is conducive to controlling the purity of the alkali-washed product, facilitating the screening of qualified products, and thus conducive to improving the added value of the product.

[0062] The second oil-water separation device 730 is used to separate the oil and water of the qualified product into a water phase and an oil phase. The provision of the second oil-water separation device 730 is beneficial to improving the purity of the oil phase, thereby helping to increase the added value of the product.

[0063] In a preferred embodiment, the second oil-water separation device 730 is an adsorption device, which is provided with an adsorbent layer inside. The material of the adsorbent layer includes but is not limited to one or two of the group consisting of activated clay, diatomaceous earth and activated silica gel. Compared with other types of adsorbent layer materials, the use of the above materials is conducive to improving the adsorption efficiency of the adsorbent layer on impurities and water in qualified products, thereby helping to improve the purity of qualified products, and further helping to increase the added value of products.

[0064] In a preferred embodiment, the above-mentioned co-production system provided in the present application also includes a hydrogenation reaction unit 800, and the hydrogenation reaction unit 800 includes a catalytic hydrogenation reaction device 810, a hydrogen separation device 820, a gas compression device 830, a liquid-liquid separation device 850 and a third oil-water separation device 860, wherein the catalytic hydrogenation reaction device 810 is provided with an oil phase inlet 811, a hydrogenation catalyst inlet 812, a hydrogen inlet 813 and a catalytic hydrogenation reaction product outlet; the oil phase inlet 811 is connected to the first oil phase outlet 732; the hydrogen separation device 820 is provided with a catalytic hydrogenation reaction product inlet, a recovered hydrogen outlet and a second separated product outlet, and the hydrogenation reaction product inlet is connected to the hydrogenation reaction product outlet The gas compression device 830 is provided with a recovered hydrogen inlet and a compressed hydrogen outlet; the recovered hydrogen inlet is connected to the recovered hydrogen outlet through a hydrogen delivery pipeline, and a third cooler 840 is provided on the hydrogen delivery pipeline; the liquid-liquid separation device 850 is provided with a third separation product inlet, a third separation product outlet and an impurity outlet 851; the third separation product inlet is connected to the second separation product outlet; the third oil-water separation device 860 is provided with a fourth separation product inlet, a third water phase outlet 861 and a second oil phase outlet 862; the fourth separation product inlet is connected to the third separation product outlet; the second oil phase outlet 862 is connected to the first separation product inlet 501.

[0065] The catalytic hydrogenation reaction device 810 is used to cause hydrogen to react with the oil phase under the catalysis of a hydrogenation catalyst to undergo a catalytic hydrogenation reaction to obtain a catalytic hydrogenation reaction product. The setting of the catalytic hydrogenation reaction device 810 is conducive to the conversion and removal of olefins and oxygen-containing compounds in the oil phase, thereby facilitating the improvement of the purity of the catalytic hydrogenation reaction product, and further facilitating the improvement of the added value of the product.

[0066] The hydrogen separation device 820 is used to separate and recover hydrogen. The provision of the hydrogen separation device 820 is beneficial to improving the recovery rate of hydrogen, thereby helping to reduce costs.

[0067] The gas compression device 830 is used to pressurize the recovered hydrogen, and the third cooler 840 is used to cool the recovered hydrogen. The arrangement of the gas compression device 830 and the third cooler 840 facilitates the transportation of the recovered hydrogen back to the catalytic hydrogenation reaction device 810 for reuse, which is beneficial to improving the recovery rate of hydrogen and thus helping to reduce costs.

[0068] The liquid-liquid separation device 850 is used to separate and remove impurities in the second separation product to obtain a third separation product with higher purity. The liquid-liquid separation device 850 is provided with an impurity outlet 851 for discharging impurities. The setting of the liquid-liquid separation device 850 is conducive to improving the purity of the third separation product, thereby helping to increase the added value of the product.

[0069] The third oil-water separator 860 is used to separate the water phase and the oil phase in the third separated product. The setting of the third oil-water separator 860 facilitates the separation of the water phase and the oil phase in the third separated product, thereby facilitating the improvement of product added value.

[0070] In a preferred embodiment, the distillation unit 100 comprises a third atmospheric distillation apparatus 110 and a fourth atmospheric distillation apparatus 120 which are sequentially connected in liquid phase, the third atmospheric distillation apparatus 110 is provided with a Fischer-Tropsch synthetic oil inlet 101 and a C9-fraction oil outlet 103, and the fourth atmospheric distillation apparatus 120 is provided with C9-C 11 Distillate oil outlet 102 and C 11 + distillate oil outlet 104. The Fischer-Tropsch synthesis oil is subjected to two atmospheric distillations by the third atmospheric distillation apparatus 110 and the fourth atmospheric distillation apparatus 120 which are connected in sequence in the liquid phase to obtain C9-C 11 Distillate oil is beneficial to improve C9~C 11 The olefin content in the distillate oil is beneficial to improving the polymerization efficiency of the polymerization reaction, thereby increasing the added value of the product.

[0071] In a preferred embodiment, the deoxygenation device 200 is an adsorption device, an adsorbent layer is provided inside the adsorption device, and the material of the adsorbent layer is a molecular sieve; a nitrogen purge component is provided inside the deoxygenation device 200. The deoxygenation device 200 is used to remove C9~C 11 Oxygenated compounds in distillate oil are beneficial to improve C9~C 11 The purity of the distillate oil is beneficial to improving the polymerization efficiency of the polymerization reaction, and is beneficial to increasing the production rate of the first polymerization product, thereby increasing the added value of the product.

[0072] In order to improve C9~C 11 In order to improve the removal efficiency of oxygenated compounds in distillate oil, preferably, the molecular sieve includes but is not limited to one or more of the group consisting of 3A molecular sieve, 4A molecular sieve, 5A molecular sieve, 13X molecular sieve, silica gel and activated carbon. Compared with other types, the use of the above types of molecular sieves is beneficial to improve the removal efficiency of C9-C 11 The removal efficiency of oxygenated compounds in distillate oil is beneficial to improve the C9~C 11 The purity of the distillate oil is beneficial to improving the polymerization efficiency of the polymerization reaction.

[0073] In a preferred embodiment, the deoxygenated product outlet 202 is connected to the first deoxygenated product inlet 301 through a deoxygenated product delivery pipeline, and a third preheating device 900 is provided on the deoxygenated product delivery pipeline. The third preheating device 900 is provided to facilitate preheating of the deoxygenated product, which is beneficial to improving the reaction efficiency of the polymerization reaction, thereby facilitating increasing the added value of the product.

[0074] In a preferred embodiment, the above-mentioned cogeneration system provided by the present application further includes a cooling unit, which includes a cooling medium storage tank, a cooling water pump and a cooling unit; the cooling unit is used to output cooling medium to the cooling unit; the cooling unit is respectively connected to the distillation unit 100, the deoxygenation device 200, the polymerization reaction unit 300, the catalyst separation device 400, the alkali washing unit 700, the hydrogenation reaction unit 800 and the product separation unit 500 in a skid-mounted manner. The cooling unit is used to cool the distillation unit 100, the deoxygenation device 200, the polymerization reaction unit 300, the catalyst separation device 400, the alkali washing unit 700, the hydrogenation reaction unit 800 and the product separation unit 500 connected thereto in a skid-mounted manner, which is conducive to reducing the damage to the equipment caused by heat release during the production process, thereby helping to extend the service life of the equipment, and further helping to reduce production costs.

[0075] In a preferred embodiment, the material of the cooling medium includes but is not limited to ethylene glycol and / or water. Compared with other materials, the cooling medium using the above materials is conducive to improving the cooling effect of the cooling unit.

[0076] In order to further improve the cooling effect of the cooling unit, preferably, the cooling unit is used to output a cooling medium with a temperature of 5 to 10° C. to the cooling unit.

[0077] The present application is further described in detail below in conjunction with specific embodiments. These embodiments should not be construed as limiting the scope of protection claimed in the present application.

[0078] It should be noted that the poly-α-olefin base oils prepared in all the examples and comparative examples of the present application were subjected to viscosity tests, flash point tests, pour point tests, density tests, molecular weight tests and color tests, including: (1) measuring the kinematic viscosity at 100°C and the kinematic viscosity at 40°C according to the method in GB / T 265; (2) measuring the viscosity index according to the method in GB / T 1995; (3) measuring the flash point according to the method in GB / T 3536; (4) measuring the pour point according to the method in GB / T 3535; (5) measuring the density according to the method in SH / T0604; (6) measuring the molecular weight according to the method in GB / T 27843-2011; and (7) measuring the color according to the method in ASTM D156.

[0079] The components of the Fischer-Tropsch synthetic oil used in all the examples and comparative examples of this application are shown in Table 1:

[0080] Table 1

[0081] Element <![CDATA[C6~C 20 Olefins]]> <![CDATA[C6~C 20 Alkanes]]> Oxide water Content (wt%) 55～60 35～40 3～5 0.006

[0082] Example 1

[0083] A method for co-producing polyalphaolefin base oil and white oil, using Figure 2 The co-production system of polyalphaolefin base oil and white oil shown in the figure is carried out, comprising the following steps:

[0084] (1) 500 g of Fischer-Tropsch synthetic oil was introduced into a distillation unit 100 for two fraction cuttings. The distillation unit 100 included two atmospheric distillation towers connected in sequence. C9-C 11 Distillate oil, including C9~C 11 The distillate oil includes 20wt% C9 alkanes, 60wt% C 10 Alkane, 18wt% C 11 Alkane, 2 wt% of oxide and 50 ppm of water;

[0085] (2) C9~C 11 The distillate oil was passed into an adsorption tower filled with 13X molecular sieve (Guangzhou Xinci Environmental Protection Materials Co., Ltd.) for deoxygenation, and a deoxygenated product was obtained at the bottom of the tower;

[0086] (3) BF3 catalyst and the deoxidized product heated to 40° C. in a heating furnace are introduced into a mixer to mix to obtain a mixture, and the mixture is introduced into a first reactor and a second reactor in sequence to cause a polymerization reaction, and sampling is carried out in a detection and screening tank to detect whether it is qualified. When the conversion rate is less than 90%, it is an unqualified product, and when the conversion rate is ≥90%, it is a qualified product. The unqualified product is returned to the first reactor to participate in the polymerization reaction again; wherein the temperature in the first reactor is 40° C., and the temperature in the second reactor is 40° C.;

[0087] (4) passing the qualified product detected above into a catalyst separation atmospheric distillation tower for atmospheric distillation to remove the residual catalyst, and the recovered BF3 obtained by separation is cooled by a tower top cooler and then returned to the polymerization reaction unit 300 through a compressor for reuse, and the separated product is passed from the bottom of the tower into an alkali washing unit;

[0088] (5) passing the separated product and a KOH solution with a mass concentration of 10% into an alkali washing tank for alkali washing to obtain an alkali washing product, passing the alkali washing product into a fluorine content detection and screening tank for sampling and detection, when the free fluorine ion content is ≥10ppm, it is an unqualified product, and when the free fluorine ion content is <10ppm, it is a qualified product. After detection, the unqualified product is passed into the alkali washing tank for alkali washing again, and the qualified product is adsorbed by a filter filled with activated clay and activated silica gel adsorbent to obtain an oil phase;

[0089] (6) The oil phase obtained by alkali washing, the hydrogenation catalyst nickel-based catalyst and H2 are introduced into a catalytic hydrogenation reactor to carry out a catalytic hydrogenation reaction at 240° C. to obtain a catalytic hydrogenation reaction product, the hydrogenation reaction product is introduced into a hot high-pressure separator to separate hydrogen, the separated hydrogen is cooled in a cooler, compressed by a compressor and returned to the catalytic hydrogenation reaction device for reuse, the second separated product extracted from the bottom of the hot high-pressure separator is introduced into a hot low-pressure separator to remove impurities such as trace water and fluoride ions contained therein, to obtain a third separated product, the third separated product is introduced into an oil-water separator for oil-water separation, and the separated oil phase is introduced into a product separation unit 500 for separation;

[0090] (7) The oil phase obtained after the hydrodeoxygenation in the catalytic hydrogenation reaction unit 800 is passed into the atmospheric distillation tower in the product separation unit 500, and naphtha is produced at the top of the tower. 35% of the naphtha is cooled in a cooler and returned to the atmospheric distillation tower as reflux material; the bottom product of the atmospheric distillation tower is passed into a vacuum distillation tower for vacuum distillation, and white oil is produced at the top of the tower, PAO2 base oil is produced at the first vacuum distillation line, PAO4 base oil is produced at the second vacuum distillation line, PAO6 base oil is produced at the third vacuum distillation line, and PAO15 base oil is produced at the bottom of the tower; wherein the distillation temperature of each product is shown in Table 2, and the test results are shown in Table 3.

[0091] Table 2

[0092]

[0093]

[0094] Example 2

[0095] The difference from Example 1 is that in step (4), the separated product obtained by separation in the catalyst separation atmospheric distillation tower is not subjected to alkali washing, but is directly introduced into the catalytic hydrogenation reactor for catalytic hydrogenation reaction. The remaining steps are the same as those in Example 1. The test results are shown in Table 4.

[0096] Example 3

[0097] The difference from Example 1 is that the catalytic hydrogenation reaction product obtained by the catalytic hydrogenation reaction in step (6) is directly introduced into a hot low-pressure separator to separate the impurities such as trace water and fluoride ions contained therein, and the remaining steps are the same as Example 1. The test results are shown in Table 5.

[0098] Example 4

[0099] The difference from Example 1 is that in step (7), the naphtha produced at the top of the atmospheric distillation tower is all passed into the naphtha finished product tank and is not returned to the atmospheric distillation tower. The remaining steps are the same as in Example 1. The test results are shown in Table 6.

[0100] Comparative Example 1

[0101] The difference from Example 1 is that the BF3 catalyst separated in step (4) is not returned to the polymerization reaction unit 300, and the remaining steps are the same as Example 1. The test results are shown in Table 7.

[0102] Table 3

[0103]

[0104] Table 4

[0105]

[0106] Table 5

[0107]

[0108] Table 6

[0109]

[0110] Table 7

[0111]

[0112] From the above description, it can be seen that the above embodiments of the utility model achieve the following technical effects: compared with the traditional poly-α-olefin base oil production device, the above co-production system of the present application can not only realize the co-production of poly-α-olefin base oil and white oil, improve the added value of the product, but also realize the recycling of the catalyst, improve the utilization rate of the catalyst, and thus reduce the cost; for C9~C 11 Deoxygenation treatment of distillate oil can improve the purity and reaction efficiency of polymerization reaction raw materials, thereby improving the quality of white oil and poly-alpha-olefin base oil.

[0113] The above description is only the preferred embodiment of the utility model, and is not intended to limit the utility model. For those skilled in the art, the utility model can have various modifications and changes. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the utility model shall be included in the protection scope of the utility model.

Claims

1. A co-production system of poly-alpha-olefin base oil and white oil, characterized in that: The poly-alpha-olefin and white oil co-production system comprises: A distillation unit (100) is used to cut the Fischer-Tropsch synthetic oil to obtain C9-C 11 Distillate, C9-distillate and C 11 + fraction oil, the distillation unit (100) is provided with a Fischer-Tropsch synthetic oil inlet (101), C9~C 11 Distillate oil outlet (102), C9-distillate oil outlet (103) and C 11 + distillate oil outlet (104); Deoxidation device (200), used to remove the C9~C 11 The oxygen-containing compounds in the distillate oil are used to obtain a deoxygenated product. The deoxygenation device (200) is provided with C9~C 11 The distillate oil inlet (201) and the deoxygenated product outlet (202); the C9-C 11 The distillate oil inlet (201) is connected to the C9-C 11 The distillate oil outlet (102) is connected; A polymerization reaction unit (300) is used to make the deoxygenated product undergo a polymerization reaction under the catalysis of a catalyst to obtain a first polymerization product. The polymerization reaction unit (300) is provided with a first deoxygenated product inlet (301), a first catalyst inlet (302) and a first polymerization product outlet (303); the first deoxygenated product inlet (301) is connected to the deoxygenated product outlet (202), and the first catalyst inlet (302) is used to introduce the catalyst; A catalyst separation device (400) is used to separate the catalyst in the first polymer product to obtain a recovered catalyst and a separated product, wherein the catalyst separation device (400) is provided with a first polymer product inlet (401), a recovered catalyst outlet (402) and a first separated product outlet (403); the first polymer product inlet (401) is connected to the first polymer product outlet (303); the recovered catalyst outlet (402) is connected to the first catalyst inlet (302); A product separation unit (500) is used to separate the separation product to obtain the white oil and the poly-α-olefin base oil, and the product separation unit (500) is provided with a first separation product inlet (501), a first white oil outlet (502) and a first poly-α-olefin base oil outlet (503); the first separation product inlet (501) is connected to the first separation product outlet (403).

2. The co-production system of poly-alpha-olefin base oil and white oil according to claim 1, characterized in that: The catalyst separation device (400) is a first atmospheric distillation tower, and a first cooler is provided at the top of the first atmospheric distillation tower; and / or, The recovered catalyst outlet (402) is connected to the first catalyst inlet (302) via a recovered catalyst delivery pipeline, and a compressor (600) is provided on the recovered catalyst delivery pipeline.

3. The co-production system of poly-α-olefin base oil and white oil according to claim 1 or 2, characterized in that: The product separation unit (500) comprises: a first distillation device (510), used for distilling the separation product to obtain a distillation product and naphtha, wherein the first distillation device (510) is provided with a first separation product inlet (501), a first distillation product outlet and a first naphtha outlet; the first separation product inlet (501) is connected to the first separation product outlet (403) via a separation product delivery pipeline, and a first preheating device (520) is provided on the separation product delivery pipeline; A second distillation device (530), wherein the second distillation device (530) is provided with a first distillation product inlet, the first white oil outlet (502), a second polyα-olefin base oil outlet (531), a third polyα-olefin base oil outlet (532), a fourth polyα-olefin base oil outlet (533) and a fifth polyα-olefin base oil outlet (534); the second polyα-olefin base oil outlet (531) is used to discharge PAO2 base oil, the third polyα-olefin base oil outlet (532) is used to discharge PAO4 base oil, the fourth polyα-olefin base oil outlet (533) is used to discharge PAO6 base oil, and the fifth polyα-olefin base oil outlet (534) is used to discharge PAO15 base oil; the first distillation product inlet is connected to the first distillation product outlet through a first distillation product conveying pipeline, and a second preheating device (540) is provided on the first distillation product conveying pipeline.

4. The co-production system of poly-alpha-olefin base oil and white oil according to claim 3, characterized in that: The first distillation device (510) is a second atmospheric distillation tower, the second distillation device (530) is a vacuum distillation tower, the second poly-α-olefin base oil outlet (531), the third poly-α-olefin base oil outlet (532) and the fourth poly-α-olefin base oil outlet (533) are arranged on the side of the vacuum distillation tower from top to bottom, and the fifth poly-α-olefin base oil outlet (534) is arranged at the bottom of the vacuum distillation tower; and / or, The product separation unit (500) further comprises: a second cooler (550), wherein the second cooler (550) is provided with a first tower top material inlet, a second naphtha outlet (551) and a recovery tower top material outlet; the first tower top material inlet is connected to the first naphtha outlet, and the recovery tower top material outlet is connected to the first separated product inlet (501); A first oil-water separation device (560), wherein the first oil-water separation device (560) is provided with a second tower top material inlet, a first water phase outlet (561) and a second white oil outlet (562); the second tower top material inlet is connected to the first white oil outlet (502).

5. The co-production system of poly-α-olefin base oil and white oil according to claim 1 or 2, characterized in that: The polymerization reaction unit (300) comprises: A first polymerization reaction device (310), wherein the first polymerization reaction device (310) is provided with the first deoxygenated product inlet (301), the first catalyst inlet (302) and a second polymerization product outlet; A second polymerization reaction device (320), wherein the second polymerization reaction device (320) is provided with a second polymerization product inlet, a second catalyst inlet (321) and a third polymerization product outlet; the second polymerization product inlet is connected to the second polymerization product outlet; the second catalyst inlet (321) is connected to the recovered catalyst outlet (402); The detection and screening device (330) is used for detecting and screening the first polymerization product and the first unqualified product, and the detection and screening device (330) is provided with a third polymerization product inlet, the first polymerization product outlet (303) and the first unqualified product outlet; the third polymerization product inlet is connected to the third polymerization product outlet; the first unqualified product outlet is connected to the first deoxygenated product inlet (301).

6. The co-production system of poly-alpha-olefin base oil and white oil according to claim 5, characterized in that: The inner cavities of the first polymerization reaction device (310) and the second polymerization reaction device (320) are independently provided with cooling components; and / or, The outer peripheries of the first polymerization reaction device (310) and the second polymerization reaction device (320) are independently provided with jackets, and the inner cavities of the jackets are filled with cooling medium; and / or, The first polymerization reaction device (310) and the second polymerization reaction device (320) are independently selected from a bubbling reactor, a loop reactor, a microreactor or a stirred tank reactor.

7. The co-production system of poly-alpha-olefin base oil and white oil according to claim 5, characterized in that: The polymerization reaction unit (300) further comprises a mixing device (340), wherein the mixing device (340) is provided with a second deoxygenated product inlet (341), a third catalyst inlet (342) and a mixture outlet (343); the second deoxygenated product inlet (341) is connected to the deoxygenated product outlet (202), the third catalyst inlet (342) is connected to the recovered catalyst outlet (402), and the mixture outlet (343) is connected to the first deoxygenated product inlet (301) or the first catalyst inlet (302).

8. The co-production system of poly-α-olefin base oil and white oil according to claim 1 or 2, characterized in that: The cogeneration system further comprises an alkali washing unit (700), wherein the alkali washing unit (700) comprises: an alkali washing device (710), used for washing the separated product with an alkali solution to remove fluoride ions to obtain an alkali washed product, wherein the alkali washing device (710) is provided with a second separated product inlet (711), an alkali solution inlet (712) and an alkali washed product outlet; the second separated product inlet (711) is connected to the first separated product outlet (403); a fluorine content detection and screening device (720), used for detecting the fluorine content in the alkali-washed product and screening to obtain a qualified product and a second unqualified product, wherein the fluorine content detection and screening device (720) is provided with an alkali-washed product inlet, a qualified product outlet, and a second unqualified product outlet; the alkali-washed product inlet is connected to the alkali-washed product outlet, and the second unqualified product outlet is connected to the second separated product inlet (711); The second oil-water separation device (730) is used to separate the oil and water of the qualified product into a water phase and an oil phase. The second oil-water separation device (730) is provided with a qualified product inlet, a second water phase outlet (731) and a first oil phase outlet (732); the qualified product inlet is connected to the qualified product outlet.

9. The co-production system of poly-alpha-olefin base oil and white oil according to claim 8, characterized in that: The cogeneration system further comprises a hydrogenation reaction unit (800), wherein the hydrogenation reaction unit (800) comprises: A catalytic hydrogenation reaction device (810) is used to cause hydrogen to react with the oil phase under the catalysis of a hydrogenation catalyst. The catalytic hydrogenation reaction device (810) is provided with an oil phase inlet (811), a hydrogenation catalyst inlet (812), a hydrogen inlet (813) and a catalytic hydrogenation reaction product outlet; the oil phase inlet (811) is connected to the first oil phase outlet (732); A hydrogen separation device (820), wherein the hydrogen separation device (820) is provided with a catalytic hydrogenation reaction product inlet, a recovered hydrogen outlet, and a second separation product outlet, wherein the hydrogenation reaction product inlet is connected to the hydrogenation reaction product outlet; and the recovered hydrogen outlet is connected to the hydrogen inlet (813); A gas compression device (830), wherein the gas compression device (830) is provided with a recovered hydrogen inlet and a compressed hydrogen outlet; the recovered hydrogen inlet is connected to the recovered hydrogen outlet via a hydrogen delivery pipeline, and a third cooler (840) is provided on the hydrogen delivery pipeline; A liquid-liquid separation device (850), wherein the liquid-liquid separation device (850) is provided with a third separation product inlet, a third separation product outlet and an impurity outlet (851); the third separation product inlet is connected to the second separation product outlet; A third oil-water separation device (860), wherein the third oil-water separation device (860) is provided with a fourth separation product inlet, a third water phase outlet (861) and a second oil phase outlet (862); the fourth separation product inlet is connected to the third separation product outlet; the second oil phase outlet (862) is connected to the first separation product inlet (501).

10. The co-production system of poly-alpha-olefin base oil and white oil according to claim 9, characterized in that: The distillation unit (100) comprises a third atmospheric distillation apparatus (110) and a fourth atmospheric distillation apparatus (120) which are arranged in liquid phase in sequence and connected to each other, the third atmospheric distillation apparatus (110) is provided with the Fischer-Tropsch synthetic oil inlet (101) and the C9-fraction oil outlet (103), and the fourth atmospheric distillation apparatus (120) is provided with the C9-C 11 The distillate outlet (102) and the C 11 + a distillate outlet (104); and / or, The deoxygenation device (200) is an adsorption device, an adsorbent layer is arranged inside the adsorption device, and the material of the adsorbent layer is a molecular sieve; a nitrogen purge component is arranged inside the deoxygenation device (200); and / or, The deoxygenated product outlet (202) is connected to the first deoxygenated product inlet (301) via a deoxygenated product delivery pipeline, and a third preheating device (900) is provided on the deoxygenated product delivery pipeline; and / or, The cogeneration system further comprises a cooling unit, which comprises a cooling medium storage tank, a cooling water pump and a cooling unit; the cooling unit is used to output cooling medium to the cooling unit; the cooling unit is respectively connected to the distillation unit (100), the deoxygenation device (200), the polymerization reaction unit (300), the catalyst separation device (400), the alkali washing unit (700), the hydrogenation reaction unit (800) and the product separation unit (500) in a skid-mounted manner.

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