CN110627935B - Purification device and purification method for poly alpha-olefin reaction product - Google Patents
Purification device and purification method for poly alpha-olefin reaction product Download PDFInfo
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- CN110627935B CN110627935B CN201810663379.2A CN201810663379A CN110627935B CN 110627935 B CN110627935 B CN 110627935B CN 201810663379 A CN201810663379 A CN 201810663379A CN 110627935 B CN110627935 B CN 110627935B
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Abstract
The invention relates to the field of purification of poly-alpha-olefin reaction products, and particularly discloses a purification device and a purification method of poly-alpha-olefin reaction products. The purification method of the polyalpha-olefin reaction product comprises the steps of carrying out alkaline washing on the polyalpha-olefin reaction product, carrying out primary oil-water separation on materials after the alkaline washing, carrying out secondary oil-water separation on an oil phase obtained by the primary oil-water separation, carrying out primary water washing on the oil phase obtained by the secondary oil-water separation, carrying out primary layering on the materials after the primary water washing, carrying out secondary layering on the oil phase obtained by the primary layering, and independently setting the temperatures of the alkaline washing and the primary water washing to be 60-100 ℃. By adopting the purification device and the purification method provided by the invention, the content of water-soluble organic impurities in the obtained purified product is less than 1000mg/L, the content of water-soluble inorganic impurities is less than 2mg/L, and the content of sodium ions is less than 1mg/L, so that the requirements of downstream process flow and final product quality can be completely met.
Description
Technical Field
The invention belongs to the field of purification of poly-alpha-olefin reaction products, and particularly relates to a purification device and a purification method of poly-alpha-olefin reaction products.
Background
Poly Alpha Olefin (PAO) synthetic oils are polymers obtained by polymerizing linear alpha olefins, usually 1-decene, and are the most important group IV synthetic lubricant base oils. The IV synthetic lubricating oil base oil has the characteristics of high viscosity index, low pour point, high flash point, good thermal oxidation stability, excellent high and low temperature performance, long service life and the like, and is particularly suitable for the industries of aerospace, military, transportation, cosmetics and the like.
One of the methods for producing PAO synthetic oil is that it is made by cationic polymerization of 1-decene using lewis acid (usually boron trifluoride) as initiator, and the synthesized PAO contains residual catalyst and cocatalyst which are water-soluble organic or inorganic, and in order to meet the quality requirements of the subsequent process and product, it is necessary to remove the residual catalyst and cocatalyst from the PAO. However, no device and method for PAO purification has been reported.
Disclosure of Invention
The invention aims to provide a novel purification device and a purification method for poly alpha-olefin reaction products.
Specifically, the invention provides a purification device for poly alpha-olefin reaction products, wherein the purification device comprises an alkali washing area A and a first-section water washing area B, the alkali washing area A comprises an alkali washing mixing tank 11, an alkali washing settling tank 12 and an alkali washing coalescer 13 which are sequentially connected in series, and the first-section water washing area B comprises a first-section water washing mixing tank 21, a first-section water washing settling tank 22 and a first-section water washing coalescer 23 which are sequentially connected in series;
introducing the poly alpha-olefin reaction product into the alkaline washing mixing tank 11 for alkaline washing, introducing the material subjected to alkaline washing into the alkaline washing precipitation tank 12 for primary oil-water separation, introducing the oil phase obtained by the primary oil-water separation into the alkaline washing coalescer 13 for secondary oil-water separation, introducing the oil phase obtained by the secondary oil-water separation into the first-stage water washing mixing tank 21 for primary water washing, introducing the material subjected to the primary water washing into the first-stage water washing precipitation tank 22 for primary layering, and introducing the oil phase obtained by the primary layering into the first-stage water washing coalescer 23 for secondary layering.
The invention also provides a purification method of the polyalphaolefin reaction product, wherein the purification method comprises the steps of carrying out alkali washing on the polyalphaolefin reaction product, carrying out primary oil-water separation on the material subjected to alkali washing, carrying out secondary oil-water separation on an oil phase obtained by the primary oil-water separation, carrying out primary water washing on the oil phase obtained by the secondary oil-water separation, carrying out primary layering on the material subjected to primary water washing, carrying out secondary layering on the oil phase obtained by the primary layering, and independently setting the temperatures of the alkali washing and the primary water washing to be 60-100 ℃.
The purification device and the purification method provided by the invention comprise a primary alkali washing process and at least a primary water washing process, wherein the alkali washing process adopts alkali liquor (such as sodium hydroxide) for washing so as to neutralize residual catalyst and cocatalyst in the poly alpha-olefin reaction product, the water washing process adopts desalted water (such as deionized water) for washing, and through the synergistic effect of the two processes, water-soluble organic impurities (residual catalyst) and water-soluble inorganic impurities contained in the poly alpha-olefin reaction product enter into and are removed from the water phase, the content of the water-soluble organic impurities in the final purification product is usually less than 1000mg/L, the content of the water-soluble inorganic impurities is usually less than 2mg/L, the content of sodium ions is usually less than 1mg/L, and the requirements of downstream process flow and the quality of the final product can be completely met, has great industrial application prospect.
Additional features and advantages of the invention will be set forth in the detailed description which follows.
Drawings
The above and other objects, features and advantages of the present invention will become more apparent by describing in more detail exemplary embodiments thereof with reference to the attached drawings, in which like reference numerals generally represent like parts throughout.
Fig. 1 shows a schematic block diagram of a purification apparatus for poly alpha olefin reaction products provided in accordance with one embodiment of the present invention.
Description of the reference numerals
A-an alkaline washing zone; b-a first water washing zone; c-a second-stage water washing zone; 11-an alkaline washing mixing tank; 12-alkali washing a precipitation tank; 13-caustic wash coalescer; 16-an alkali liquor heater; 17-an alkaline washing circulating pump; 18-caustic wash coalescer circulation pump; 21-first-stage water washing mixing tank; 22-first-stage washing of the precipitation tank with water; 23-a stage water washing coalescer; 24-first-stage water washing circulating pump; 25-first stage water wash coalescer circulation pump; 31-two-section water washing mixing tank; 32-two-stage washing and precipitating tank; 33-two-stage water washing coalescer; 34-two-stage water washing circulating pump; 35-two-stage water washing coalescer circulating pump; 36-desalted water heater.
Detailed Description
Preferred embodiments of the present invention will be described in more detail below. While the following describes preferred embodiments of the present invention, it should be understood that the present invention may be embodied in various forms and should not be limited by the embodiments set forth herein.
As shown in fig. 1, the purification device for poly α -olefin reaction products provided by the present invention comprises an alkali washing area a and a first water washing area B, wherein the alkali washing area a comprises an alkali washing mixing tank 11, an alkali washing precipitation tank 12 and an alkali washing coalescer 13 which are sequentially connected in series, and the first water washing area B comprises a first water washing mixing tank 21, a first water washing precipitation tank 22 and a first water washing coalescer 23 which are sequentially connected in series;
introducing the poly alpha-olefin reaction product into the alkaline washing mixing tank 11 for alkaline washing, introducing the material subjected to alkaline washing into the alkaline washing precipitation tank 12 for primary oil-water separation, introducing the oil phase obtained by the primary oil-water separation into the alkaline washing coalescer 13 for secondary oil-water separation, introducing the oil phase obtained by the secondary oil-water separation into the first-stage water washing mixing tank 21 for primary water washing, introducing the material subjected to the primary water washing into the first-stage water washing precipitation tank 22 for primary layering, and introducing the oil phase obtained by the primary layering into the first-stage water washing coalescer 23 for secondary layering. Wherein, a heater is arranged in the alkali washing mixing tank 11 to maintain the alkali washing process at a specific temperature (60-100 ℃).
According to a preferred embodiment of the present invention, the caustic washing zone a further comprises a caustic heater 16, a caustic washing circulation pump 17 and a caustic washing coalescer circulation pump 18, wherein the caustic heater 16 is used for heating the caustic liquor introduced into the caustic washing zone a, the caustic washing circulation pump 17 is used for pumping the aqueous phase in the caustic washing precipitation tank 12 and the caustic washing coalescer 13 into the caustic washing mixing tank 11 for circulation, and the caustic washing coalescer circulation pump 18 is used for pumping the aqueous phase in the caustic washing coalescer 13 into the inlet of the caustic washing circulation pump 17 or directly into the caustic washing mixing tank 11 for circulation.
According to another preferred embodiment of the present invention, the first-stage water washing zone B further comprises a first-stage water washing circulating pump 24 and a first-stage water washing coalescer circulating pump 25, the first-stage water washing circulating pump 24 is used for pumping the aqueous phases in the first-stage water washing settling tank 22 and the first-stage water washing coalescer 23 to the first-stage water washing mixing tank 21 and the alkaline washing process a for circulation, and the first-stage water washing coalescer circulating pump 25 is used for pumping the aqueous phases in the first-stage water washing coalescer 23 to the inlet of the first-stage water washing circulating pump 24 or directly to the first-stage water washing mixing tank 21 and the alkaline washing process a for circulation.
According to the invention, the water washing area can be one section or more than two sections, and the water washing area is reasonably selected according to actual conditions, wherein the content of water-soluble organic impurities in the final purified product is controlled to be less than 1000mg/L, the content of water-soluble inorganic impurities is controlled to be less than 2mg/L, and the content of sodium ions is controlled to be less than 1 mg/L. According to an embodiment of the present invention, as shown in fig. 1, the purification apparatus further includes a two-stage water washing zone C, and the two-stage water washing zone C includes a two-stage water washing mixing tank 31, a two-stage water washing precipitation tank 32, and a two-stage water washing coalescer 33 connected in series, that is, the purification apparatus includes a one-stage alkali washing zone and a two-stage water washing zone. And introducing the oil phase obtained by re-layering in the first-stage washing coalescer 23 into the second-stage washing mixing tank 31 for secondary washing, introducing the material subjected to secondary washing into the second-stage washing settling tank 32 for primary separation, and introducing the oil phase obtained by primary separation into the second-stage washing coalescer 33 for re-separation. At this time, preferably, the second water washing zone C further includes a second water washing circulation pump 34, a second water washing coalescer circulation pump 35, and a desalted water heater 36, the second water washing circulation pump 34 is configured to pump the water phase in the second water washing settling tank 32 and the second water washing coalescer 33 to the second water washing mixing tank 31 and the alkaline washing process a for circulation, the second water washing coalescer circulation pump 35 is configured to pump the water phase in the second water washing coalescer 33 to an inlet of the second water washing circulation pump 34 or directly to the second water washing mixing tank 31 and the alkaline washing process a for circulation, and the desalted water heater 36 is configured to heat the desalted water introduced into the first water washing zone B and the second water washing zone C.
The residual catalyst and cocatalyst in the poly alpha-olefin reaction product are subjected to neutralization reaction with alkali liquor in an alkali washing mixing tank 11, and in order to ensure that the neutralization reaction is complete, the alkali washing process in the alkali washing mixing tank 11 is preferably carried out under stirring. In addition, the water washing processes in the first-stage water-washing mixing tank 21 and the second-stage water-washing mixing tank 31 are also preferably performed under stirring to ensure sufficient water washing.
The purification method of the polyalpha-olefin reaction product comprises the steps of carrying out alkali washing on the polyalpha-olefin reaction product, carrying out primary oil-water separation on a material subjected to alkali washing, carrying out secondary oil-water separation on an oil phase obtained by the primary oil-water separation, carrying out primary water washing on the oil phase obtained by the secondary oil-water separation, carrying out primary layering on the material subjected to the primary water washing, carrying out secondary layering on the oil phase obtained by the primary layering, and independently setting the temperatures of the alkali washing and the primary water washing to be 60-100 ℃. Wherein the purpose of independently controlling the temperature of the alkaline washing and the primary water washing at 60-100 ℃ is to make the poly alpha-olefin reaction product have certain compatibility with alkaline liquor and aqueous solution, thereby ensuring the alkaline washing and water washing effects, so as to control the content of water-soluble organic impurities and water-soluble inorganic impurities in the poly alpha-olefin reaction product at a sufficiently low level.
According to the invention, the purification method of the poly alpha-olefin reaction product preferably further comprises heating alkali liquor to 60-100 ℃ before alkali washing, recycling the water phase part obtained by the primary oil-water separation and the secondary oil-water separation as the alkali liquor, and sending the rest part out (entering a wastewater treatment unit for treatment), wherein the weight ratio of the recycled water phase to the sent-out water phase can be (1-2): 1; and/or, the method also comprises the step of recycling an aqueous phase obtained after the material after the primary water washing is subjected to primary layering and secondary layering as desalted water of the primary water washing and alkali liquor of the alkali washing, wherein the weight ratio of the aqueous phase of the desalted water subjected to the primary water washing to the aqueous phase of the alkali liquor can be (1-2): 1.
according to the present invention, in order to reduce the content of impurities in the polyalphaolefin reaction product to a lower level, it is preferable that the purification method of the polyalphaolefin reaction product further comprises subjecting the oil phase obtained by the re-stratification to a secondary water washing, subjecting the material after the secondary water washing to a primary separation, and subjecting the oil phase obtained by the primary stratification to a secondary separation. At this time, the purification method of the polyalphaolefin reaction product preferably further comprises heating desalted water to 60 to 100 ℃ before the primary and secondary water washing, and recycling an aqueous phase obtained after the primary and secondary water washing, as desalted water for the secondary water washing and a lye for the alkaline washing, wherein a weight ratio of the aqueous phase as desalted water for the secondary water washing to the aqueous phase as lye may be (1 to 2): 1.
the method of the primary oil-water separation, the secondary oil-water separation, the primary layering, the secondary layering, the primary separation and the secondary separation is not particularly limited as long as the oil-water separation can be realized, and for example, the primary oil-water separation, the secondary oil-water separation, the primary layering, the secondary layering, the primary separation and the secondary separation can be still standing precipitation. Wherein, the conditions of the preliminary oil-water separation usually comprise that the temperature can be 60-100 ℃ and the time can be 10-40 min. The conditions for oil-water separation again usually include temperature of 60-100 deg.C and time of 10-40 min. The conditions for the preliminary stratification may generally include a temperature which may be 60-100 ℃ and a time which may be 10-40 min. The conditions for said re-stratification generally comprise a temperature which may be between 60 ℃ and 100 ℃ and a time which may be between 10 and 40 min. The conditions for the preliminary separation may generally include a temperature which may be in the range of 60 to 100 ℃ and a time which may be in the range of 10 to 40 min. The conditions for said re-separation generally include that the temperature may be 60-100 ℃ and the time may be 10-40 min.
The amount of the alkali solution used in the alkali washing process, the desalted water used in the primary water washing and the secondary water washing is not particularly limited as long as the content of the water-soluble organic impurities and the water-soluble inorganic impurities in the polyalphaolefin reaction product can be controlled to a sufficiently low level. For example, the alkali solution used in the alkali washing process may be used in an amount of 100-300 parts by weight, the desalted water used in the primary water washing process may be used in an amount of 30-90 parts by weight, and the desalted water used in the secondary water washing process may be used in an amount of 30-90 parts by weight, relative to 100 parts by weight of the polyalphaolefin reaction product. The time of the alkaline washing is preferably 10-40min, and the time of the primary water washing is preferably 10-40 min. The temperature of the secondary water washing is preferably 60-100 ℃, and the time is preferably 10-40 min. In addition, the alkali solution used in the alkali washing process may be any of various alkali substances, and specific examples thereof include, but are not limited to, at least one of sodium hydroxide, potassium hydroxide, sodium bicarbonate, potassium bicarbonate and ammonia water. The concentration of the lye is generally from 0.5mol/L to its saturation concentration. The desalinated water may be, for example, deionized water. The alkali washing, the primary water washing, and the secondary water washing may be performed in various existing mixing devices (e.g., a static mixer, a stirrer, etc.).
The present invention will be described in detail below by way of examples.
In the following examples and comparative examples, the poly α -olefin reaction product to be purified had a water-soluble organic impurity content of 14650mg/L, a water-soluble inorganic impurity content of 15500mg/L and a sodium ion content of 11200 mg/L.
Examples 1 to 3
Examples 1 to 3 are provided to illustrate the purification apparatus and purification method of poly-alpha-olefin reaction product provided by the present invention.
As shown in fig. 1, the purification apparatus used in embodiments 1 to 3 includes an alkaline washing area a, a first-stage water washing area B, and a second-stage water washing area C, where the alkaline washing area a includes an alkaline washing mixing tank 11, an alkaline washing precipitation tank 12, an alkaline washing coalescer 13, an alkaline heater 16, an alkaline washing circulation pump 17, and an alkaline washing coalescer circulation pump 18, the first-stage water washing area B includes a first-stage water washing mixing tank 21, a first-stage water washing precipitation tank 22, a first-stage water washing coalescer 23, a first-stage water washing circulation pump 24, and a first-stage water washing coalescer circulation pump 25, and the second-stage water washing area C includes a second-stage water washing mixing tank 31, a second-stage water washing precipitation tank 32, a second-stage water washing coalescer 33, a second-stage water washing circulation pump 34, a second-stage water washing coalescer circulation pump 35, and a desalted water heater 36.
An alkali liquor (an aqueous solution of sodium hydroxide with the concentration of 1.32 mol/L) is heated by an alkali liquor heater 16 and then introduced into an alkali washing mixing tank 11, and desalted water (deionized water) is heated by a desalted water heater 36 and then introduced into a first-stage water washing mixing tank 21 and a second-stage water washing mixing tank 31.
In the alkaline washing area A, poly alpha-olefin reaction products are introduced into an alkaline washing mixing tank 11, alkaline washing is carried out by adopting alkaline liquor heated by an alkaline liquor heater 16 under stirring (the using amount of the alkaline liquor is 100 parts by weight relative to 100 parts by weight of the poly alpha-olefin reaction products), and the materials after alkaline washing are introduced into an alkaline washing precipitation tank 12 to be stood so as to realize preliminary oil-water separation. The water phase is wastewater containing impurities, part of the wastewater is circulated back to the alkaline washing mixer under the action of the alkaline washing circulating pump 17, and the rest part of the wastewater is sent to the wastewater treatment unit for treatment. The oil phase is introduced into a caustic wash coalescer 13 and allowed to stand to effect oil-water separation again. The water phase is wastewater containing impurities, part of the wastewater is circulated back to the alkaline washing mixer 11 under the action of an alkaline washing circulating pump 17 and an alkaline washing coalescer circulating pump 18, and the rest part of the wastewater is sent out to a wastewater treatment unit for treatment. Wherein the weight ratio of the recycled aqueous phase to the delivered aqueous phase is 2: 1. the oil phase enters a first-stage water washing mixing tank 21.
In the first-stage water-washing zone B, the oil phase from the alkaline washing coalescer 13 is washed with water in a first-stage water-washing mixing tank 21 with desalted water heated by a desalted water heater 36 under stirring (the amount of desalted water is 60 parts by weight per 100 parts by weight of polyalphaolefin reaction product), and the washed material is introduced into a first-stage water-washing precipitation tank 22 to be left to stand for preliminary stratification. The water phase is wastewater containing impurities, part of the water phase circulates back to the first section of water washing mixing tank 21 under the action of the first section of water washing circulating pump 24, and the rest part of the water phase returns to the alkali washing process. The oil phase is introduced into a first-stage water-washing coalescer 23 to be kept stand to realize re-stratification, the water phase is wastewater containing impurities, under the action of a first-stage water-washing circulating pump 24 and a first-stage water-washing coalescer circulating pump 25, part of the oil phase is circulated back to the first-stage water-washing mixing tank 21, the rest part of the oil phase is returned to the alkali-washing process (wherein the weight ratio of the water phase returned to the first-stage water-washing mixing tank 21 to the water phase returned to the alkali-washing process is 2: 1), and the oil phase enters the second-stage water-washing mixing tank 31.
In the second-stage water washing zone B, the oil phase from the first-stage water washing coalescer 23 is subjected to second water washing in a second-stage water washing mixing tank 31 with desalted water heated by a desalted water heater 36 under stirring (the amount of the desalted water is 30 parts by weight relative to 100 parts by weight of the poly α -olefin reaction product), the material subjected to the second water washing is introduced into a second-stage water washing settling tank 32 to be left standing for primary separation, the water phase is impurity-containing wastewater, part of the water phase is circulated back to the second-stage water washing mixing tank 31 under the action of a second-stage water washing circulation pump 34, the rest is returned to the alkali washing process, the oil phase is introduced into a second-stage water washing coalescer 33 to be left standing for secondary separation, the water phase is impurity-containing wastewater, part of the water phase is circulated back to the second-stage water washing mixing tank 31 under the action of the second-stage water washing circulation pump 34 and the second-stage water washing coalescer circulation pump 35, the rest is returned to the alkali washing process (wherein, the weight ratio of the water phase returned to the two-stage water washing mixing tank 31 to the water phase returned to the alkali washing process is 2: 1) and the obtained oil phase is sent out as a purified product. The reaction conditions and results are shown in Table 1 and Table 2, respectively.
Example 4
The purification device adopted in this example does not include the two-stage water washing section C, and accordingly, the purification method does not include the two-stage water washing, and the specific settings of the alkaline washing section a and the one-stage water washing section B are the same as those in example 1, and the specific processes of the alkaline washing and the one-stage water washing are the same as those in example 1. The reaction conditions and results are shown in Table 1 and Table 2, respectively.
Comparative example 1
The purification device adopted by the comparative example only comprises an alkali washing area A, correspondingly, the purification method only comprises an alkali washing process, the specific arrangement of the alkali washing area A is the same as that of the example 4, and the specific process and conditions of the alkali washing are the same as those of the example 4. The results are shown in Table 2.
Comparative example 2
The purification apparatus employed in this comparative example includes only one-stage water washing section B, and accordingly, the purification method includes only one-stage water washing process, and the specific setup of the one-stage water washing section B is the same as in example 4, and the specific process and conditions of the one-stage water washing are the same as in example 4, and in the water washing process, the poly α -olefin reaction product is directly introduced into the one-stage water washing mixing tank 21, and water washing is performed with deionized water heated by the desalted water heater 36 under stirring. The results show that the catalyst contained in the poly alpha-olefin reaction product to be purified can generate hydrofluoric acid when meeting water in the water washing process, and severe corrosion is caused to equipment.
TABLE 1
TABLE 2
From the results, the purification device and the purification method provided by the invention can be used for treating the poly-alpha-olefin reaction product, so that the content of water-soluble organic impurities and water-soluble inorganic impurities in the poly-alpha-olefin reaction product can be remarkably reduced, and the poly-alpha-olefin reaction product can completely meet the requirements of downstream process flows and the quality of final products.
The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, but the present invention is not limited to the specific details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.
It should be noted that the various features described in the above embodiments may be combined in any suitable manner without departing from the scope of the invention. The invention is not described in detail in order to avoid unnecessary repetition.
In addition, any combination of the various embodiments of the present invention can be made, and the same should be considered as the disclosure of the present invention as long as the idea of the present invention is not violated.
Claims (8)
1. A purification method of a poly alpha-olefin reaction product is characterized by comprising the steps of carrying out alkali washing on the poly alpha-olefin reaction product, carrying out primary oil-water separation on a material after the alkali washing, carrying out secondary oil-water separation on an oil phase obtained by the primary oil-water separation, carrying out primary water washing on the oil phase obtained by the secondary oil-water separation, carrying out primary layering on the material after the primary water washing, carrying out secondary layering on the oil phase obtained by the primary layering, wherein the alkali washing temperature and the primary water washing temperature are respectively and independently 60-100 ℃;
wherein, relative to 100 weight parts of the poly alpha-olefin reaction product, the dosage of the alkali liquor in the alkali washing process is 100-300 weight parts, and the dosage of the fresh desalted water in the primary water washing process is 30-90 weight parts; the alkaline washing time is 10-40min, and the primary water washing time is 10-40 min;
the modes of primary oil-water separation, secondary oil-water separation, primary layering and secondary layering are standing precipitation;
the conditions of the preliminary oil-water separation comprise that the temperature is 60-100 ℃ and the time is 10-40 min;
the conditions for oil-water separation again comprise that the temperature is 60-100 ℃ and the time is 10-40 min;
the condition of the preliminary layering comprises the temperature of 60-100 ℃ and the time of 10-40 min;
the secondary layering condition comprises that the temperature is 60-100 ℃ and the time is 10-40 min;
the purification method of the poly alpha-olefin reaction product adopts a purification device of the poly alpha-olefin reaction product, the purification device comprises an alkali washing area (A) and a first-section water washing area (B), the alkali washing area (A) comprises an alkali washing mixing tank (11), an alkali washing settling tank (12) and an alkali washing coalescer (13) which are sequentially connected in series, and the first-section water washing area (B) comprises a first-section water washing mixing tank (21), a first-section water washing settling tank (22) and a first-section water washing coalescer (23) which are sequentially connected in series;
introducing the poly alpha-olefin reaction product into the alkaline washing mixing tank (11) for alkaline washing, introducing materials subjected to alkaline washing into the alkaline washing settling tank (12) for primary oil-water separation, introducing an oil phase obtained by the primary oil-water separation into the alkaline washing coalescer (13) for secondary oil-water separation, introducing the oil phase obtained by the secondary oil-water separation into the first-stage water washing mixing tank (21) for primary water washing, introducing the materials subjected to the primary water washing into the first-stage water washing settling tank (22) for primary layering, and introducing the oil phase obtained by the primary layering into the first-stage water washing coalescer (23) for secondary layering.
2. The purification process of polyalphaolefin reaction product according to claim 1, wherein the caustic wash zone (a) further comprises a caustic heater (16), a caustic wash circulation pump (17) and a caustic wash coalescer circulation pump (18), the caustic heater (16) being used to heat the caustic introduced into the caustic wash zone (a), the caustic wash circulation pump (17) being used to pump the aqueous phase in the caustic wash precipitation tank (12) and the caustic wash coalescer (13) into the caustic wash mixing tank (11) for circulation, the caustic wash coalescer circulation pump (18) being used to pump the aqueous phase in the caustic wash coalescer (13) into the caustic wash circulation pump (17) inlet or directly into the caustic wash mixing tank (11) for circulation.
3. The purification method of poly alpha olefin reaction product as claimed in claim 1, wherein the first water washing section (B) further comprises a first water washing circulation pump (24) and a first water washing coalescer circulation pump (25), the first water washing circulation pump (24) is used for pumping the aqueous phase in the first water washing precipitation tank (22) and the first water washing coalescer (23) to the first water washing mixing tank (21) and the alkaline washing section (a) for circulation, and the first water washing coalescer circulation pump (25) is used for pumping the aqueous phase in the first water washing coalescer (23) to the first water washing circulation pump (24) inlet or directly to the first water washing mixing tank (21) and the alkaline washing section (a) for circulation.
4. The purification method of poly α olefin reaction product according to any one of claims 1 to 3, wherein the purification apparatus further comprises a second-stage water washing zone (C) comprising a second-stage water washing mixing tank (31), a second-stage water washing settling tank (32) and a second-stage water washing coalescer (33) connected in series in this order, the oil phase obtained by re-layering in the first-stage water washing coalescer (23) is introduced into the second-stage water washing mixing tank (31) to be subjected to secondary water washing, the material after secondary water washing is introduced into the second-stage water washing settling tank (32) to be primarily separated, and the oil phase obtained by primary separation is introduced into the second-stage water washing coalescer (33) to be re-separated.
5. The method for purifying a polyalphaolefin reaction product of claim 4, wherein, the second-stage water washing area (C) also comprises a second-stage water washing circulating pump (34), a second-stage water washing coalescer circulating pump (35) and a desalted water heater (36), the second-stage washing circulating pump (34) is used for pumping the water phases in the second-stage washing settling tank (32) and the second-stage washing coalescer (33) to the second-stage washing mixing tank (31) and the alkaline washing area (A) for circulation, the second-stage water washing coalescer circulating pump (35) is used for pumping the water phase in the second-stage water washing coalescer (33) to the inlet of the second-stage water washing circulating pump (34) or directly pumping the water phase into the second-stage water washing mixing tank (31) and the alkali washing area (A) for circulation, the desalted water heater (36) is used for heating the desalted water introduced into the first-stage water washing zone (B) and the second-stage water washing zone (C).
6. The method for purifying a polyalphaolefin reaction product of claim 1, wherein,
heating the alkali liquor to 60-100 ℃ before alkali washing, recycling the water phase part obtained by the primary oil-water separation and the secondary oil-water separation as the alkali liquor, and sending the rest part out; and/or the presence of a gas in the gas,
the method also comprises the step of recycling an aqueous phase obtained after the materials after the primary water washing are subjected to primary layering and secondary layering as the desalted water of the primary water washing and the alkali liquor of the alkali washing.
7. The method for purifying polyalphaolefin reaction product according to claim 1, further comprising subjecting the oil phase obtained by the re-stratification to a secondary water washing, subjecting the material after the secondary water washing to a primary separation, and subjecting the oil phase obtained by the primary separation to a secondary separation.
8. The method for purifying a polyalphaolefin reaction product of claim 7, wherein,
the temperature of the secondary water washing is 60-100 ℃, and the time is 10-40 min;
the amount of the desalted water used in the secondary water washing process is 30 to 90 parts by weight with respect to 100 parts by weight of the polyalphaolefin reaction product;
the conditions of the preliminary separation comprise that the temperature is 60-100 ℃ and the time is 10-40 min;
the re-separation conditions comprise that the temperature is 60-100 ℃ and the time is 10-40 min;
the method also comprises the steps of heating desalted water to 60-100 ℃ before the primary water washing and the secondary water washing, and recycling an aqueous phase obtained after the primary separation and the secondary separation of the materials after the secondary water washing as desalted water of the secondary water washing and alkali liquor of the alkali washing.
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