A separation and purification apparatus for a fischer-tropsch synthesis oil

Abstract

The utility model discloses a kind of separation and refining device of fischer-tropsch synthetic oil, including deacidification tower, first water scrubbing tower, first separation tower, second separation tower, first deoxidation tower, second water scrubbing tower, second deoxidation tower, extractant recovery tower;Alkaline liquor, fischer-tropsch oil is input into deacidification tower, deacidification tower is connected with first water scrubbing tower, first water scrubbing tower is connected with first separation tower, first separation tower is connected with second separation tower, second separation tower is connected with first deoxidation tower, first deoxidation tower is connected with second water scrubbing tower and extractant recovery tower respectively, second water scrubbing tower is connected with second deoxidation tower, second deoxidation tower exports deoxidation C 10 ‑C 13 The present application realizes efficient removal of oxygen-containing compounds in fischer-tropsch synthetic oil through scientific and reasonable structure design, while ensuring high purity of target fraction and high retention rate of olefins.

Description

Technical Field

[0001] This utility model belongs to the field of coal chemical technology, and in particular relates to a separation and refining device for Fischer-Tropsch synthetic oil. Background Technology

[0002] The Fischer-Tropsch synthesis reaction refers to the reaction in which syngas, under specific temperature and pressure conditions and with iron or cobalt as a catalyst, produces a series of alkanes, alkenes, and oxygen-containing compounds. The hydrocarbons are predominantly straight-chain hydrocarbons, typically containing a large amount of α-olefins, thus serving as raw materials for various chemicals to increase their added value. For example, hydrocarbons with 8 to 10 carbon atoms... 10 α-olefins can be used as raw materials for synthesizing high-grade lubricating oil base oils (PAOs), and can also be used to synthesize plasticizer alcohols via carbonyl synthesis. They have a carbon number of C... 11 To C 13 α-olefins can be used to produce alkylphenols, alkylbenzenes, or detergent alcohols.

[0003] However, the oxygen-containing compounds produced by the Fischer-Tropsch synthesis reaction are mainly fatty alcohols, along with small amounts of acids, aldehydes, ketones, and esters. The presence of these oxygen-containing compounds can lead to catalyst poisoning and deactivation in downstream industries, increasing processing costs and operating expenses for subsequent products. This, in turn, limits the comprehensive utilization of Fischer-Tropsch synthesis products and the extension of the industrial chain. Therefore, it is necessary to thoroughly remove oxygen-containing compounds from the Fischer-Tropsch synthesis oil.

[0004] Patent CN111718746A discloses a method for deoxygenating and refining Fischer-Tropsch synthetic oil. This method primarily involves first fractionating the Fischer-Tropsch synthetic oil under atmospheric and vacuum distillation to obtain three fractions, and then using different extractants to deoxygenate each fraction, reducing the oxide content to below 100 ppm. Extractive deoxygenation is a relatively effective method for deoxygenating Fischer-Tropsch oil, but experiments have shown that it can only reduce the oxide content to a maximum of 1000 ppm. Furthermore, this invention does not consider the deacidification treatment of the raw material, as acidic substances in the raw material can corrode the equipment.

[0005] Patents CN115612521A and CN115612522A disclose methods for removing oxygen-containing compounds from hydrocarbon streams. Both methods involve extraction deoxygenation, where the hydrocarbon stream is Fischer-Tropsch synthetic oil, and the extractant is a compounded ester compound. After deoxygenation, the oxide content is reduced to below 10 ppm. Experiments have shown that this deoxygenation effect is difficult to achieve using only extraction deoxygenation. Utility Model Content

[0006] In view of this, the present invention aims to provide a separation and refining apparatus for Fischer-Tropsch synthetic oils to solve at least one technical problem in the prior art. This application, through a scientifically sound structural design, achieves efficient removal of oxygen-containing compounds from Fischer-Tropsch synthetic oils while ensuring high purity of the target fraction and high retention of olefins.

[0007] To achieve the above objectives, the technical solution of this utility model is implemented as follows: A separation and refining apparatus for Fischer-Tropsch synthetic oil includes a deacidification tower, a first water washing tower, a first separation tower, a second separation tower, a first deoxygenation tower, a second water washing tower, a second deoxygenation tower, and an extractant recovery tower. Alkali solution and Fischer-Tropsch oil are fed into the deacidification tower, which is connected to the first water washing tower. The first water washing tower is connected to the first separation tower, the first separation tower is connected to the second separation tower, and the second separation tower is connected to the first deoxygenation tower. The first deoxygenation tower is connected to both the second water washing tower and the extractant recovery tower. The second water washing tower is connected to the second deoxygenation tower, and the second deoxygenation tower outputs deoxygenated C2O3. 10 -C 13 .

[0008] Furthermore, the deacidification tower is connected to the Fischer-Tropsch oil inlet pipeline via the Fischer-Tropsch oil inlet; The deacidification tower is connected to the alkali inlet pipe through the alkali inlet, and the alkali inlet pipe is connected to the alkali supply system.

[0009] Furthermore, a first discharge pipe is provided at the bottom of the deacidification tower; The top of the deacidification tower is connected to one side of the first water washing tower via a first connecting pipe.

[0010] Furthermore, a first water inlet is provided on one side of the first water washing tower, and the first water inlet is connected to the first water inlet pipe; The bottom of the first water washing tower is equipped with a second discharge pipe; The top of the first washing tower is connected to one side of the first separation tower via a second connecting pipe.

[0011] Furthermore, the top of the first separation tower is provided with a first extraction pipe for extracting C9; The bottom of the first separation tower is equipped with a C extraction station. 10+ The second extraction pipe is connected to one side of the second separation tower.

[0012] Furthermore, the top of the second separation tower is equipped with a tool for extracting C. 10 -C 13 The third extraction pipeline is connected to one side of the first deoxygenation tower; The bottom of the second separation tower is equipped with a C extraction station. 14 The fourth extraction pipeline.

[0013] Furthermore, the top of the first deoxygenation tower is equipped with a fifth extraction pipe for extracting residual phase; the fifth extraction pipe is connected to one side of the second water washing tower. The bottom of the first deoxygenation tower is equipped with a third discharge pipe for discharging the extract phase, which is connected to one side of the extractant recovery tower.

[0014] Furthermore, the top of the extractant recovery tower is provided with a sixth extraction pipe for extracting the extractant, and the sixth extraction pipe is connected to one side of the first deoxygenation tower. Oxides, hydrocarbons, and water are discharged from the bottom of the extractant recovery tower through a fourth discharge pipe.

[0015] Furthermore, the bottom of the second water washing tower is provided with a fifth discharge pipe for drainage, which is connected to one side of the first deoxygenation tower. The top of the second water washing tower is connected to the second deoxygenation tower via a third connecting pipe; The second water washing tower has a second water inlet on one side, which is connected to the second water inlet pipe.

[0016] Furthermore, the bottom of the second deoxygenation tower is equipped with a deoxygenation C outlet. 10 -C 13 The seventh extraction pipeline.

[0017] Compared with the prior art, the separation and refining apparatus for Fischer-Tropsch synthetic oil described in this utility model has the following advantages: 1. This application achieves efficient removal of oxygen-containing compounds from Fischer-Tropsch synthetic oil through a scientific and reasonable structural design, while ensuring the high purity of the target fraction and the high retention rate of olefins.

[0018] 2. This application employs a combination of a deacidification tower and a first water washing tower. The deacidification tower uses alkali solution to chemically neutralize most of the organic acids, while the first water washing tower further removes residual alkali, salt, and trace amounts of water-soluble acids through physical washing. This synergistic effect of "chemical + physical" ensures that acidic substances in the Fischer-Tropsch oil are completely removed, greatly reducing the possibility of corrosion of subsequent equipment.

[0019] 3. This application uses a first separation tower and a second separation tower for two-stage separation. This design allows for more precise fractionation, ensuring the target product (C) is achieved. 10 -C 13 It maintains the purity of hydrocarbons while effectively separating lighter and heavier hydrocarbon components, thus avoiding contamination of the main product by the lighter and heavier components.

[0020] 4. This application uses an extraction deoxygenation tower and an adsorption deoxygenation tower to perform a dual deoxygenation operation on the target product, which can reduce the oxide content in the target product to below 10 ppm. Attached Figure Description

[0021] The accompanying drawings, which form part of this utility model, are used to provide a further understanding of the utility model. The illustrative embodiments of the utility model and their descriptions are used to explain the utility model and do not constitute an undue limitation of the utility model. In the drawings: Figure 1 This is a schematic diagram of a separation and refining apparatus for Fischer-Tropsch synthetic oil proposed in this utility model; Explanation of reference numerals in the attached figures: 1. Deacidification tower; 2. First water washing tower; 3. First separation tower; 4. Second separation tower; 5. First deoxygenation tower; 6. Second water washing tower; 7. Second deoxygenation tower; 8. Extractant recovery tower. Detailed Implementation

[0022] It should be noted that, unless otherwise specified, the embodiments and features described in these embodiments can be combined with each other.

[0023] The present invention will now be described in detail with reference to the accompanying drawings and embodiments.

[0024] Example 1 A separation and refining apparatus for Fischer-Tropsch synthetic oil includes a deacidification tower 1, a first water washing tower 2, a first separation tower 3, a second separation tower 4, a first deoxygenation tower 5, a second water washing tower 6, a second deoxygenation tower 7, and an extractant recovery tower 8. Alkali solution and Fischer-Tropsch oil are fed into the deacidification tower 1. The deacidification tower 1 is connected to the first water washing tower 2, the first water washing tower 2 is connected to the first separation tower 3, the first separation tower 3 is connected to the second separation tower 4, the second separation tower 4 is connected to the first deoxygenation tower 5, the first deoxygenation tower 5 is connected to both the second water washing tower 6 and the extractant recovery tower 8, the second water washing tower 6 is connected to the second deoxygenation tower 7, and the second deoxygenation tower 7 outputs deoxygenated C2O3. 10 -C 13 .

[0025] The deacidification tower 1 is connected to the Fischer-Tropsch oil inlet pipe via the Fischer-Tropsch oil inlet; the deacidification tower 1 is connected to the alkali inlet pipe via the alkali inlet pipe, which is connected to the alkali supply system. The bottom of the deacidification tower 1 is provided with a first discharge pipe; the top of the deacidification tower 1 is connected to one side of the first water washing tower 2 via a first connecting pipe.

[0026] The first water washing tower 2 has a first water inlet on one side, which is connected to the first water inlet pipe; the bottom of the first water washing tower 2 has a second discharge pipe; the top of the first water washing tower 2 is connected to one side of the first separation tower 3 through a second connecting pipe.

[0027] The top of the first separation tower 3 is equipped with a first extraction pipe for extracting C9; the bottom of the first separation tower 3 is equipped with a extraction pipe for C9. 10+ The second extraction pipe is connected to one side of the second separation tower 4.

[0028] The top of the second separation tower 4 is equipped with a tool for extracting C. 10 -C 13 The third extraction pipeline is connected to one side of the first deoxygenation tower 5; the bottom of the second separation tower 4 is equipped with extraction C. 14 The fourth extraction pipeline.

[0029] The top of the first deoxygenation tower 5 is provided with a fifth extraction pipe for extracting the residual phase; the fifth extraction pipe is connected to one side of the second water washing tower 6; the bottom of the first deoxygenation tower 5 is provided with a third discharge pipe for discharging the extract phase, and the third discharge pipe is connected to one side of the extractant recovery tower 8.

[0030] The top of the extractant recovery tower 8 is equipped with a sixth extraction pipe for extracting the extractant, which is connected to one side of the first deoxygenation tower 5; the bottom of the extractant recovery tower 8 discharges oxides, hydrocarbons and water through a fourth discharge pipe.

[0031] The bottom of the second water washing tower 6 is provided with a fifth discharge pipe for drainage, which is connected to one side of the first deoxygenation tower 5; the top of the second water washing tower 6 is connected to the second deoxygenation tower 7 through a third connecting pipe; a second water inlet is provided on one side of the second water washing tower 6, which is connected to the second water inlet pipe.

[0032] The bottom of the second deoxygenation tower 7 is equipped with a deoxygenation outlet C. 10 -C 13 The seventh extraction pipeline.

[0033] Example 2 A separation and refining apparatus for Fischer-Tropsch synthetic oil includes a deacidification tower 1 with a Fischer-Tropsch oil inlet, an alkali inlet, a top outlet, and a bottom outlet; a first water washing tower 2 with a Fischer-Tropsch oil inlet, a water inlet, a top outlet, and a bottom outlet; a first separation tower 3 with a Fischer-Tropsch oil inlet, a top outlet, and a bottom outlet; a second separation tower 4 with a Fischer-Tropsch oil inlet, a top outlet, and a bottom outlet; a first deoxygenation tower 5 with a Fischer-Tropsch oil inlet, an extractant inlet, a top outlet, and a bottom outlet; a second water washing tower 6 with a Fischer-Tropsch oil inlet, a water inlet, a top outlet, and a bottom outlet; a second deoxygenation tower 7 with a Fischer-Tropsch oil top inlet and a bottom outlet; and an extractant recovery tower 8 with an extractant inlet, a top inlet, and a bottom outlet.

[0034] The Fischer-Tropsch synthetic oil feedstock enters through the Fischer-Tropsch oil inlet of deacidification tower 1, while the alkali solution enters through the alkali solution inlet of deacidification tower 1. The Fischer-Tropsch oil and alkali solution come into countercurrent contact for deacidification. The deacidified Fischer-Tropsch oil is collected from the top outlet of deacidification tower 1 and enters the first water washing tower 2. Water enters through the water inlet of the first water washing tower 2 and comes into countercurrent contact with the Fischer-Tropsch oil to remove residual alkali solution. The water-washed Fischer-Tropsch oil is collected from the top outlet of the first water washing tower 2 and enters the first separation tower 3 for splitting and separation. The middle fraction is collected from the bottom outlet of the first separation tower and enters the second separation tower 4 for splitting and separation. The target fraction is collected from the top of the second separation tower and enters the first deoxygenation tower 5. The extractant enters through the extractant inlet of the first deoxygenation tower 5, and the target fraction comes into countercurrent contact with the extractant in the first deoxygenation tower 5 for extraction and deoxygenation. The raffinate is collected from the top outlet of the first deoxygenation tower 5 and enters the second water washing tower 6. Water enters from the water inlet of the second water washing tower 6 and comes into countercurrent contact with the target fraction to remove residual extractant. The target fraction is collected from the top of the second deoxygenation tower and enters the second deoxygenation tower 7, and is finally collected from the bottom outlet of the second deoxygenation tower 7. The extractant is collected from the bottom outlet of the first deoxygenation tower 5 and enters the extractant recovery tower 8. Fresh extractant is collected from the top of the tower and returned to the first deoxygenation tower 5.

[0035] Example 3 Using the apparatus described in Example 1 or Example 2 of this application, Fischer-Tropsch oil is separated and refined. The raw material is Fischer-Tropsch synthetic oil from a domestic coal chemical enterprise, mainly composed of C4 to C64. 16 It has a hydrocarbon composition and an acid value of 2 mg KOH / g.

[0036] After alkali washing and water washing, the acid value of Fischer-Tropsch oil is less than 0.05 mg KOH / g.

[0037] The deacidified Fischer-Tropsch oil enters the first separation tower and is then split in the second separation tower. The target fraction, C, is collected from the top of the second separation tower. 10 -C 13 The fraction had a purity of 98%. It contained 60% α-olefins and 8.5% oxygen-containing compounds.

[0038] C 10 -C 13 The distillate enters the first deoxygenation tower, where it undergoes multi-stage countercurrent extraction deoxygenation with a 90% methanol-water solution at a volume ratio of 4:1 and an operating temperature of 40°C. The bottom extract phase is sent to the extractant recovery tower for extractant recovery; the top raffinate phase is sent to the second water washing tower for countercurrent contact with water to remove the extractant. The C fraction after water washing... 10 -C 13 The fraction, after chromatographic analysis, has an oxide content of 2200 ppm and is sent to the second deoxygenation tower; the wash water is mixed with the recovered extractant and sent to the first deoxygenation tower.

[0039] C 10 -C 13The fraction undergoes adsorption deoxygenation in a second deoxygenation tower using silica gel as the adsorbent. The operating conditions for adsorption deoxygenation are: temperature 50℃; pressure 0.5 MPa. After adsorption deoxygenation, C... 10 -C 13 Chromatographic analysis of the fraction showed an oxide content of 6 ppm. The α-olefin retention rate was greater than 99%.

[0040] Example 4 Using the apparatus described in Example 1 or Example 2 of this application, Fischer-Tropsch oil is separated and refined. The raw material is Fischer-Tropsch synthetic oil from a domestic coal chemical enterprise, mainly composed of C4 to C64. 16 It has a hydrocarbon composition and an acid value of 2 mg KOH / g.

[0041] After alkali washing and water washing, the acid value of Fischer-Tropsch oil is less than 0.05 mg KOH / g.

[0042] The deacidified Fischer-Tropsch oil enters the first separation tower and is then split in the second separation tower. The target fraction, C, is collected from the top of the second separation tower. 10 -C 13 The fraction had a purity of 98%. It contained 60% α-olefins and 8.5% oxygen-containing compounds.

[0043] C 10 -C 13 The distillate enters the first deoxygenation tower, where it undergoes multi-stage countercurrent extraction deoxygenation with a 90% ethanol-water solution at a volume ratio of 4:1 and an operating temperature of 40°C. The bottom extract phase is sent to the extractant recovery tower for extractant recovery; the top raffinate phase is sent to the second water washing tower for countercurrent contact with water to remove the extractant. The C fraction after water washing... 10 -C 13 The fraction, after chromatographic analysis, has an oxide content of 2400 ppm and is sent to the second deoxygenation tower; the wash water is mixed with the recovered extractant and sent to the first deoxygenation tower.

[0044] C 10 -C 13 The fraction undergoes adsorption deoxygenation in a second deoxygenation tower using silica gel as the adsorbent. The operating conditions for adsorption deoxygenation are: temperature 50℃; pressure 0.5 MPa. After adsorption deoxygenation, C... 10 -C 13 Chromatographic analysis of the fraction showed an oxide content of 6 ppm. The α-olefin retention rate was greater than 99%.

[0045] Example 5 Using the apparatus described in Example 1 or Example 2 of this application, Fischer-Tropsch oil is separated and refined. The raw material is Fischer-Tropsch synthetic oil from a domestic coal chemical enterprise, mainly composed of C4 to C64. 16 It has a hydrocarbon composition and an acid value of 2 mg KOH / g.

[0046] After alkali washing and water washing, the acid value of Fischer-Tropsch oil is less than 0.05 mg KOH / g.

[0047] The deacidified Fischer-Tropsch oil enters the first separation tower and is then split in the second separation tower. The target fraction is collected from the top of the second separation tower. The target fraction is a C10-C13 fraction with a purity of 98%. The mass fraction of α-olefins is 60%, and the mass fraction of oxygen-containing compounds is 8.5%.

[0048] C 10 -C 13 The distillate enters the first deoxygenation tower, where it undergoes multi-stage countercurrent extraction deoxygenation with a 90% methanol-water solution at a volume ratio of 4:1 and an operating temperature of 40°C. The bottom extract phase is sent to the extractant recovery tower for extractant recovery; the top raffinate phase is sent to the second water washing tower for countercurrent contact with water to remove the extractant. The C fraction after water washing... 10 -C 13 The fraction, after chromatographic analysis, has an oxide content of 2200 ppm and is sent to the second deoxygenation tower; the wash water is mixed with the recovered extractant and sent to the first deoxygenation tower.

[0049] C 10 -C 13 The fraction underwent adsorption deoxygenation in the second deoxygenation tower, using 13X molecular sieve as the adsorbent. The adsorption deoxygenation operating conditions were: temperature 50℃; pressure 0.5 MPa. After adsorption deoxygenation, C... 10 -C 13 Chromatographic analysis of the fraction showed an oxide content of 8 ppm. The α-olefin retention rate was greater than 99%.

[0050] Example 6 Using the apparatus described in Example 1 or Example 2 of this application, Fischer-Tropsch oil is separated and refined. The raw material is Fischer-Tropsch synthetic oil from a domestic coal chemical enterprise, mainly composed of C4 to C64. 16 It has a hydrocarbon composition and an acid value of 2 mg KOH / g.

[0051] After alkali washing and water washing, the acid value of Fischer-Tropsch oil is less than 0.05 mg KOH / g.

[0052] The deacidified Fischer-Tropsch oil enters the first separation tower and is then split in the second separation tower. The target fraction is collected from the top of the second separation tower. The target fraction is a C10-C13 fraction with a purity of 98%. The mass fraction of α-olefins is 60%, and the mass fraction of oxygen-containing compounds is 8.5%.

[0053] C 10 -C 13The distillate enters the first deoxygenation tower, where it undergoes multi-stage countercurrent extraction deoxygenation with a 90% ethanol-water solution at a volume ratio of 4:1 and an operating temperature of 40°C. The bottom extract phase is sent to the extractant recovery tower for extractant recovery; the top raffinate phase is sent to the second water washing tower for countercurrent contact with water to remove the extractant. The C fraction after water washing... 10 -C 13 The fraction, after chromatographic analysis, has an oxide content of 2400 ppm and is sent to the second deoxygenation tower; the wash water is mixed with the recovered extractant and sent to the first deoxygenation tower.

[0054] C 10 -C 13 The fraction underwent adsorption deoxygenation in the second deoxygenation tower, using 13X molecular sieve as the adsorbent. The adsorption deoxygenation operating conditions were: temperature 50℃; pressure 0.5MPa. After adsorption deoxygenation, C... 10 -C 13 Chromatographic analysis of the fraction showed an oxide content of 9 ppm. The α-olefin retention rate was greater than 99%.

[0055] Example 7 Using the apparatus described in Example 1 or Example 2 of this application, Fischer-Tropsch oil is separated and refined. The raw material is Fischer-Tropsch synthetic oil from a domestic coal chemical enterprise, mainly composed of C4 to C64. 16 It has a hydrocarbon composition and an acid value of 2 mg KOH / g.

[0056] After alkali washing and water washing, the acid value of Fischer-Tropsch oil is less than 0.05 mg KOH / g.

[0057] The deacidified Fischer-Tropsch oil enters the first separation tower and is then split in the second separation tower. The target fraction is collected from the top of the second separation tower. The target fraction is a C10-C13 fraction with a purity of 98%. The mass fraction of α-olefins is 60%, and the mass fraction of oxygen-containing compounds is 8.5%.

[0058] C 10 -C 13 The distillate enters the first deoxygenation tower, where it undergoes multi-stage countercurrent extraction deoxygenation with an 80% methanol-water solution at a volume ratio of 4:1 and an operating temperature of 40°C. The bottom extract phase is sent to the extractant recovery tower for extractant recovery; the top raffinate phase is sent to the second water washing tower for countercurrent contact with water to remove the extractant. The C fraction after water washing... 10 -C 13 The fraction, after chromatographic analysis, has an oxide content of 4500 ppm and is sent to the second deoxygenation tower; the wash water is mixed with the recovered extractant and sent to the first deoxygenation tower.

[0059] C 10 -C 13 The fraction undergoes adsorption deoxygenation in a second deoxygenation tower using silica gel as the adsorbent. The operating conditions for adsorption deoxygenation are: temperature 50℃; pressure 0.5 MPa. After adsorption deoxygenation, C...10 -C 13 Chromatographic analysis of the fraction showed an oxide content of 86 ppm. The α-olefin retention rate was greater than 99%.

[0060] The above description is only a preferred embodiment of the present utility model and is not intended to limit the present utility model. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of the present utility model should be included within the protection scope of the present utility model.

Claims

1. A separation and refining apparatus for Fischer-Tropsch synthetic oil, characterized in that: It includes a deacidification tower, a first water washing tower, a first separation tower, a second separation tower, a first deoxygenation tower, a second water washing tower, a second deoxygenation tower, and an extractant recovery tower; Alkali solution and Fischer-Tropsch oil are fed into the deacidification tower, which is connected to the first water washing tower. The first water washing tower is connected to the first separation tower, which is connected to the second separation tower. The second separation tower is connected to the first deoxygenation tower. The first deoxygenation tower is connected to both the second water washing tower and the extractant recovery tower. The second water washing tower is connected to the second deoxygenation tower, and the second deoxygenation tower outputs deoxygenated C. 10 -C 13 .

2. The separation and refining apparatus for Fischer-Tropsch synthetic oil according to claim 1, characterized in that: The deacidification tower is connected to the Fischer-Tropsch oil inlet pipeline via the Fischer-Tropsch oil inlet; The deacidification tower is connected to the alkali inlet pipe through the alkali inlet, and the alkali inlet pipe is connected to the alkali supply system.

3. The separation and refining apparatus for Fischer-Tropsch synthetic oil according to claim 1, characterized in that: The bottom of the deacidification tower is equipped with a first discharge pipe; The top of the deacidification tower is connected to one side of the first water washing tower via a first connecting pipe.

4. The separation and refining apparatus for Fischer-Tropsch synthetic oil according to claim 1, characterized in that: The first water inlet is located on one side of the first water washing tower and is connected to the first water inlet pipe; The bottom of the first water washing tower is equipped with a second discharge pipe; The top of the first washing tower is connected to one side of the first separation tower via a second connecting pipe.

5. The separation and refining apparatus for Fischer-Tropsch synthetic oil according to claim 1, characterized in that: The top of the first separation tower is equipped with a tool for extracting C. 9- The first extraction pipe; The bottom of the first separation tower is equipped with a C extraction station. 10+ The second extraction pipe is connected to one side of the second separation tower.

6. The separation and refining apparatus for Fischer-Tropsch synthetic oil according to claim 1, characterized in that: The top of the second separation tower is equipped with a tool for extracting C. 10 -C 13 The third extraction pipeline is connected to one side of the first deoxygenation tower; The bottom of the second separation tower is equipped with a C extraction station. 14+ The fourth extraction pipeline.

7. The separation and refining apparatus for Fischer-Tropsch synthetic oil according to claim 1, characterized in that: The top of the first deoxygenation tower is equipped with a fifth extraction pipe for extracting residual phase; the fifth extraction pipe is connected to one side of the second water washing tower. The bottom of the first deoxygenation tower is equipped with a third discharge pipe for discharging the extract phase, which is connected to one side of the extractant recovery tower.

8. The separation and refining apparatus for Fischer-Tropsch synthetic oil according to claim 1, characterized in that: The top of the extractant recovery tower is equipped with a sixth extraction pipe for extracting the extractant, which is connected to one side of the first deoxygenation tower. Oxides, hydrocarbons, and water are discharged from the bottom of the extractant recovery tower through a fourth discharge pipe.

9. The separation and refining apparatus for Fischer-Tropsch synthetic oil according to claim 8, characterized in that: The bottom of the second water washing tower is equipped with a fifth discharge pipe for drainage, which is connected to one side of the first deoxygenation tower. The top of the second water washing tower is connected to the second deoxygenation tower via a third connecting pipe; The second water washing tower has a second water inlet on one side, which is connected to the second water inlet pipe.

10. The separation and refining apparatus for Fischer-Tropsch synthetic oil according to claim 7, characterized in that: The bottom of the second deoxygenation tower is equipped with a deoxygenation outlet C. 10 -C 13 The seventh extraction pipeline.

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