CN115851303A - Multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis product - Google Patents
Multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis product Download PDFInfo
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- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 39
- 238000003672 processing method Methods 0.000 title claims abstract description 23
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- LIKMAJRDDDTEIG-UHFFFAOYSA-N 1-hexene Chemical compound CCCCC=C LIKMAJRDDDTEIG-UHFFFAOYSA-N 0.000 claims description 8
- KWKAKUADMBZCLK-UHFFFAOYSA-N 1-octene Chemical compound CCCCCCC=C KWKAKUADMBZCLK-UHFFFAOYSA-N 0.000 claims description 8
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Abstract
The invention relates to the technical field of low-temperature Fischer-Tropsch synthesis oil conversion, and discloses a low-temperature Fischer-Tropsch synthesis product multi-industrial-chain processing method.
Description
Technical Field
The invention belongs to the technical field of low-temperature Fischer-Tropsch synthesis oil conversion, and particularly relates to a multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis products.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
The main energy sources relied on for the development of human civilization and economic prosperity are coal, petroleum and natural gas respectively from the industrialized age. The synthetic gas is obtained by gasifying coal serving as a raw material, and can be efficiently converted into clean liquid fuel through Fischer-Tropsch synthesis, so that the synthetic gas can be used as a main substitute of future petrochemical industry.
In the current coal-to-oil industry, most Fischer-Tropsch synthesis crude products are subjected to hydrogenation saturation, hydrocracking and product fractionation to obtain products such as liquefied petroleum gas, diesel oil, naphtha and the like, and the products have single structures. The produced products are liquid fuels distributed according to a wider range of carbon number, finer chemicals are not produced, and the additional value is lower 。 Therefore, the liquid fuel is obtained by the technology of obtaining the liquid fuel by the current Fischer-Tropsch synthesis crude product through hydrogenation saturation, hydrocracking and product fractionation processes, the added value of the product is low, and the economic benefit is poor.
Disclosure of Invention
In order to solve the problems, the invention provides a low-temperature Fischer-Tropsch synthesis product multi-industrial-chain processing method, which can comprehensively utilize the properties of Fischer-Tropsch synthesis products, realizes the extension of the traditional coal indirect liquefaction industrial chain by taking the principle of developing high-added-value chemicals in an oiling combination mode as a product scheme, mainly uses high-quality coal-based clean oil products, coal-based alpha olefins and high-carbon alcohols, fischer-Tropsch refined wax, PAO (polyamide oil), coal-based III + lubricating oil base oil as a product, has high added value of the product, and improves the economic benefit.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect of the invention, there is provided a low temperature fischer-tropsch synthesis product multi-industrial chain processing system, comprising:
the device comprises a light component removing tower A, an extraction deoxidation unit C, a fixed bed fine deoxidation unit D and a fractionating tower E which are sequentially connected, wherein a tower bottom discharge hole of the light component removing tower A is also connected with a feed hole of a rectifying tower B, a tower top discharge hole of the fractionating tower E is connected with a feed hole of a C5-C8 olefin adsorption separation unit F, a tower bottom discharge hole of the fractionating tower E is connected with a feed hole of a C9-C12 olefin adsorption separation unit G, discharge holes of the C5-C8 olefin adsorption separation unit F and the C9-C12 olefin adsorption separation unit G and a discharge hole of the rectifying tower B are respectively connected with a buffer tank H, and a discharge hole of the buffer tank H is respectively connected with feed holes of a hydrofining reactor I and a hydrocracking reactor N;
the hydrofining reactor I, the separation unit J, the fractionating tower K and the diesel stripping tower M are sequentially connected, a discharge port at the top of the fractionating tower K is connected with a feed port of the reflux tank L, and a discharge port at the bottom of the fractionating tower K is connected with a feed port of the hydrocracking reactor N;
the hydrocracking reactor N, the separation unit O, the fractionating tower P and the diesel stripping tower R are sequentially connected, a discharge hole in the top of the fractionating tower P is connected with a feed inlet of the reflux tank Q, and a treatment hole in the bottom of the fractionating tower P is connected with a feed inlet of the isomerization dewaxing reactor S;
the isomerization dewaxing reactor S, the heat exchanger T, the complementary refining reactor U, the separation unit V and the atmospheric fractionating tower W are connected in sequence.
In a second aspect of the invention, a multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis products is provided, which comprises the following steps:
(1) Performing light and heavy removal treatment on a mixture of light naphtha and low-temperature condensate to obtain C5-C12 fractions, and extracting crude deoxidizer to 3000ppm or below;
(2) Carrying out fixed bed adsorption and fine deoxidation on the C5-C12 mixture subjected to coarse deoxidation in the step (1) until the content is 5ppm or below, carrying out alkane-alkene separation through simulated moving bed adsorption, separating and cutting the mixture by a fractionating device to obtain a component rich in alpha-alkene and a residual raffinate mainly containing alkane;
(3) Downstream processing of the alpha olefin-rich component obtained in the step (2) with n-hexanol, n-octanol, n-C12 alcohol, n-C13 alcohol, PAO base oil and fine separation to obtain 1-hexene and 1-octene;
(4) Mixing the raffinate mainly containing alkane in the step (2) and the heavy C13+ component removed in the step (1), and then adding the mixture, fischer-Tropsch synthesis high-temperature condensate and paraffin products into a hydrofining reactor for hydrogenation, saturation and quality improvement;
(5) Fractionating the oil phase subjected to hydrogenation saturation in the step (4) to obtain crude naphtha, light diesel component oil and tower bottom 1# soft wax;
(6) Extracting the 1# soft wax part in the step (5) for thin film distillation cutting to extract different grades of refined wax products, and continuously feeding the rest most of the refined wax products into a hydrocracking reactor for cracking the components and performing supplementary refining after cracking;
(7) Fractionating the oil phase in the hydrocracking section in the step (6) to obtain crude naphtha, heavy diesel component oil and fractionation tower bottom circulating No. 2 soft wax;
(8) The 2# soft wax extraction part in the step (7) enters an isomerization dewaxing reactor and a supplementary refining reaction part;
(9) And (4) carrying out atmospheric and vacuum fractionation on the oil phase subjected to isodewaxing in the step (8) to obtain light white oil, drilling fluid and lubricating oil base oil.
The invention has the advantages of
Compared with the existing processing method, the processing method provided by the invention can convert more subdivided products through separation production, can comprehensively utilize the properties of Fischer-Tropsch synthesis products, realizes extension of the traditional coal indirect liquefaction industrial chain, and has the advantages that the products mainly comprise high-quality coal-based clean oil products, coal-based alpha olefins and high-carbon alcohols, fischer-Tropsch refined wax, PAO (polyamide-olefin) and coal-based III + lubricating oil base oil, and the economic benefit is improved.
1. The step (1) and the step (2) are divided into two steps of extraction and fixed bed adsorption to remove the oxygen-containing compounds, so that the energy consumption and the equipment cost can be greatly reduced, and higher economic benefit is created.
2. And (3) the adsorption unit for realizing the separation of the alkane and the alkene in the step (2) adopts a simulated moving bed process, and realizes periodic adsorption and desorption by utilizing the difference of the adsorption capacities of the alkene and the alkane on the adsorbent, thereby realizing the high-efficiency separation of the alkene and the alkane.
3. The fractionation in the steps (5) and (7) is atmospheric fractionation, wherein the atmospheric fractionation is carried out in an atmospheric tower with a side stripper; the stripping agent is steam stripping, and the heat source of the reboiler is respectively taken from the materials of No. 1 soft wax and No. 2 soft wax at the bottom of the fractionating tower. Thus, the atmospheric tower with the side stripper can control the flash point of the light diesel component oil.
4. And (3) an atmospheric and vacuum distillation process is adopted in the step (9), so that the key components have higher product yield and quality, and the method is environment-friendly, energy-saving and higher in equipment level.
5. A series of traditional liquid fuel products such as crude naphtha, diesel component oil and the like, high-quality coal-based clean oil products, coal-based alpha olefin, high-carbon alcohol, fischer-Tropsch refined wax, PAO, coal-based III + lubricating oil base oil and other high-added-value products are obtained in the steps (3), (5), (6), (7), (8) and (9), and the products are rich in structure; production can be adjusted according to market conditions, market risk resistance is enhanced, and economic benefits are improved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention, and together with the description, serve to explain the invention and not to limit the invention.
FIG. 1 is a schematic diagram of a process flow of a low-temperature Fischer-Tropsch synthesis product processing method according to an embodiment of the invention, wherein the A light component removal tower, the B rectifying tower, the C extractive deoxygenation unit, the D fixed bed fine deoxygenation unit, the E fractionating tower, the F C5-C8 olefin adsorption separation unit, the G C9-C12 olefin adsorption separation unit, the H buffer tank, the I hydrofining reactor, the J first separation unit, the K first fractionating tower, the M diesel oil stripping tower, the L reflux tank, the N hydrocracking reactor, the O second separation unit, the P fractionating tower, the Q reflux tank, the R diesel oil stripping tower, the S isodewaxing reactor, the T heat exchanger, the U complementary refining reactor, the V separation unit and the W normal-pressure fractionating tower are arranged.
Detailed Description
It is to be understood that the following detailed description is exemplary and is intended to provide further explanation of the invention as claimed. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this invention belongs.
A multi-industrial-chain processing method of low-temperature Fischer-Tropsch synthesis products comprises the following steps:
(1) Removing light and heavy components from the mixture of light naphtha and low-temperature condensate to obtain C5-C12 fractions, and extracting crude deoxidizer to 3000ppm or below;
(2) Carrying out fixed bed adsorption refining deoxidation on the C5-C12 mixture subjected to coarse deoxidation in the step (1) until the content is 5ppm or below, carrying out simulated moving bed adsorption to realize alkane-alkene separation, separating and cutting by a fractionating device to obtain a component rich in alpha-alkene and a raffinate mainly containing alkane;
(3) Downstream processing of the alpha olefin-rich component obtained in the step (2) with n-hexanol, n-octanol, n-C12 alcohol, n-C13 alcohol, PAO base oil and fine separation to obtain 1-hexene and 1-octene;
(4) Mixing the raffinate mainly containing alkane in the step (2) and the heavy C13+ component removed in the step (1), and then adding the mixture, fischer-Tropsch synthesis high-temperature condensate and paraffin products into a hydrofining reactor for hydrogenation, saturation and quality improvement;
(5) Fractionating the oil phase subjected to hydrogenation saturation in the step (4) to obtain crude naphtha, light diesel component oil and tower bottom 1# soft wax;
(6) Extracting the 1# soft wax part in the step (5) for thin film distillation cutting to extract different grades of refined wax products, and continuously feeding the rest most of the refined wax products into a hydrocracking reactor for cracking the components and performing supplementary refining after cracking;
(7) Fractionating the oil phase of the hydrocracking section in the step (6) to obtain crude naphtha, heavy diesel component oil and circulating No. 2 soft wax at the bottom of the fractionating tower;
(8) The part of the 2# soft wax extracted in the step (7) enters an isomerization dewaxing reactor and a part of a complementary refining reaction;
(9) And (4) carrying out atmospheric and vacuum fractionation on the oil phase subjected to isodewaxing in the step (8) to obtain light white oil, drilling fluid and lubricating oil base oil.
In some embodiments, the specific steps of step (1) comprise: filtering the light naphtha 1, and then entering a light component removal tower A to remove a C4 component 3, and obtaining C5-C8 stable naphtha 2 at the tower bottom; and filtering the low-temperature Fischer-Tropsch condensate 4, and then feeding the low-temperature Fischer-Tropsch condensate into a rectifying tower B for removing the heavy components, so as to obtain C13+ heavy components 6 at the tower bottom and obtain C5-C12 light oil 5 at the tower top. The components of C5-C12 obtained by the two towers are mixed and then enter an extraction deoxidation unit C for coarse deoxidation.
In some embodiments, the specific steps of step (2) include: the material 7 after extraction and deoxidation enters a fixed bed fine deoxidation unit D; after fine deoxidation, the C5-C12 components 8 enter a fractionating tower E for cutting, the C5-C8 components 9 obtained at the tower top are sent to a C5-C8 olefin adsorption separation unit F for separation to obtain C5-C8 olefin components 11 and C5-C8 alkane components 12; C9-C12 alkane components 10 are obtained at the bottom of the tower and sent to a C9-C12 alkene adsorption separation unit G for separation to obtain C9-C12 alkene components 13 and C9-C12 alkane components 14; the component 12 and the component 14 are mixed to obtain the raffinate mainly containing alkane.
In some embodiments, the specific steps of step (4) include: after the raffinate mainly containing alkane obtained by mixing the component 12 and the component 14 and the C13+ heavy component 6 are mixed with the Fischer-Tropsch synthesis high-temperature condensate 15 and the paraffin product 16, the mixture 17 and the hydrogen 18 are mixed and enter a hydrofining reactor I for hydrogenation saturation, the mixture enters a separation unit J for separating hydrogen 20, and the oil phase component 21 enters a fractionation system.
In some embodiments, the specific steps of step (5) include: after the oil phase component 21 enters a fractionating system fractionating tower K, crude naphtha 21 at the top of the fractionating tower enters a reflux tank L; the side line extraction 22 of the fractionating tower enters a diesel stripping tower M, the light components 26 at the top of the tower return to a fractionating tower K, and the light diesel component oil 25 obtained at the bottom of the tower is extracted to a finished product tank area; the No. 1 soft wax is obtained at the bottom of the fractionating tower K.
In some embodiments, the # 1 soft wax fraction draw 23 goes to a 10Wt/a unit for thin film distillation cutting to extract different grades of refined wax product; the rest most of the 24 continuously enters a hydrocracking reactor N to crack and supplement and refine the heavy components after cracking, the oil phase 28 after reaction enters a separation unit O to separate hydrogen 29, and the oil phase component 30 enters a fractionation system.
In some embodiments, the oil phase component 30 enters the fractionation system fractionation column P and then enters the reflux drum Q via the fractionation column overhead raw naphtha 31; a side line extraction 32 of the fractionating tower enters a diesel oil stripping tower R, a light component 36 at the top of the tower returns to a fractionating tower K, and a light diesel oil component oil 35 obtained at the bottom of the tower is extracted to a finished product tank area; and obtaining the No. 2 soft wax at the bottom of the fractionating tower K.
In some embodiments, the # 2 soft wax extraction part 33 is mixed with hydrogen 37, and then enters the isomerization dewaxing reactor S to react, the obtained reaction product 38 enters the heat exchanger T to exchange heat, 39 enters the complementary refining reactor U to carry out hydrofining reaction, the obtained reaction product 40 enters the separation unit V to separate hydrogen 41, and the oil phase component 42 enters the fractionation system.
The reaction system in the process adopts an isomerization dewaxing and complementary refining technology, the isomerization reaction temperature is 310-380 ℃, and the complementary refining reaction temperature is 220-280 ℃.
In some embodiments, the oil phase component 42 obtained in step (8) is fed to the atmospheric fractionation tower W of the fractionation system, and the gasoline type aromatic-free white oil 43 is extracted from the tower top; the atmospheric fractionating tower W is provided with two side stripping towers, coal oil type aromatic hydrocarbon-free white oil 44 is produced in the first line, and drilling fluid 45 is produced in the second line; and the atmospheric tower bottom material atmospheric bottom oil 46 enters a reduced pressure fractionating tower X for further separation, the reduced pressure fractionating tower X is provided with three side draws, wherein a first-line drawn product is a No. 2 base oil product 47, a second-line drawn product is a No. 4 base oil product 48, a third-line drawn product is a No. 8 base oil product 49, and a bottom product of the reduced pressure fractionating tower is bright stock 50.
In some embodiments, the above fractionation system wherein the atmospheric fractionation tower has an overhead temperature of 95 to 115 deg.C and a pressure of 0.1 to 0.15MPa (G), the vacuum fractionation tower has an overhead temperature of 65 to 80 deg.C and an overhead pressure of-0.1 MPa (G).
The present invention is described in further detail below with reference to specific examples, which are intended to be illustrative of the invention and not limiting.
Example 1
A method for processing a low-temperature Fischer-Tropsch synthesis product. In the present embodiment, the raw materials used are light naphtha, high-temperature condensate, low-temperature condensate and paraffin wax obtained by separating and pretreating a low-temperature fischer-tropsch synthesis product, the composition tables are shown in tables 1 to 3, and the processing method of the fischer-tropsch synthesis product of the present embodiment is shown in fig. 1.
Table 1 is a table of the feedstock composition of light naphtha, the feedstock used in the process of the low temperature fischer-tropsch synthesis product processing method according to an embodiment of the present invention;
table 1 light naphtha feedstock composition
Table 2 is a table of the composition of the feed for the low temperature condensate, which is the feed used in the process for the low temperature Fischer-Tropsch synthesis product processing method according to an embodiment of the present invention;
TABLE 2 Low temperature condensate feed composition
Table 3 is a table of the composition of the high temperature condensate and paraffin used as the raw materials for the process of the low temperature Fischer-Tropsch synthesis product processing method according to the embodiment of the invention.
TABLE 3 high temperature condensate, paraffin feedstock composition
Step (1): filtering the light naphtha 1, and then entering a light component removal tower A to remove a C4 component 3, and obtaining C5-C8 stable naphtha 2 at the tower bottom; and filtering the low-temperature Fischer-Tropsch condensate 4, and then feeding the low-temperature Fischer-Tropsch condensate into a rectifying tower B for removing the heavy components, so as to obtain C13+ heavy components 6 at the tower bottom and obtain C5-C12 light oil 5 at the tower top. The components of C5-C12 obtained by the two towers are mixed and then enter an extraction deoxidation unit C for coarse deoxidation.
Step (2): and the material 7 after extraction and deoxidation enters a fixed bed fine deoxidation unit D. After fine deoxidation, the C5-C12 components 8 enter a fractionating tower E for cutting, the C5-C8 components 9 obtained at the tower top are sent to a C5-C8 olefin adsorption separation unit F for separation to obtain C5-C8 olefin components 11 and C5-C8 alkane components 12; C9-C12 alkane components 10 are obtained at the bottom of the tower and sent to a C9-C12 alkene adsorption separation unit G for separation to obtain C9-C12 alkene components 13 and C9-C12 alkane components 14; the component 12 and the component 14 are mixed to obtain the raffinate mainly containing alkane.
And (3): and (3) carrying out downstream processing on the obtained component 11 and the component 13 rich in the olefin, producing n-hexanol, n-octanol, n-C12 alcohol, n-C13 alcohol and PAO base oil by adopting a carbonyl synthesis technology, a fine separation technology and a polymerization process, and finely separating to obtain 1-hexene and 1-octene.
And (4): after the raffinate mainly containing alkane obtained by mixing the component 12 and the component 14 and the C13+ heavy component 6 are mixed with the Fischer-Tropsch synthesis high-temperature condensate 15 and the paraffin product 16, the mixture 17 and the hydrogen 18 are mixed and enter a hydrofining reactor I for hydrogenation saturation, the mixture enters a separation unit J for separating hydrogen 20, and the oil phase component 21 enters a fractionation system.
And (5): after the oil phase component 21 enters a fractionating tower K of a fractionating system, crude naphtha 21 passing through the top of the fractionating tower enters a reflux tank L; a side line extraction 22 of the fractionating tower enters a diesel oil stripping tower M, a light component 26 at the tower top returns to a fractionating tower K, and a light diesel oil component oil 25 obtained at the tower bottom is extracted to a finished product tank area; the No. 1 soft wax is obtained at the bottom of the fractionating tower K.
And (6): 1# soft wax part is pumped out 23 to a 10Wt/a refined Fischer-Tropsch wax device for film distillation cutting and extraction of refined wax products of different brands; the rest most of the 24 continuously enters a hydrocracking reactor N to crack and supplement and refine the heavy components after cracking, the oil phase 28 after reaction enters a separation unit O to separate hydrogen 29, and the oil phase component 30 enters a fractionation system.
And (7): after the oil phase component 30 enters a fractionating tower P of a fractionating system, crude naphtha 31 at the top of the fractionating tower enters a reflux tank Q; a side line extraction 32 of the fractionating tower enters a diesel stripping tower R, a light component 36 at the top of the tower returns to a fractionating tower K, and a light diesel component oil 35 obtained at the bottom of the tower is extracted to a finished product tank area; and obtaining the No. 2 soft wax at the bottom of the fractionating tower K.
And (8): the No. 2 soft wax extraction part 33 is mixed with hydrogen 37 and then enters an isomerization dewaxing reactor S for reaction, the obtained reaction product 38 enters a heat exchanger T for heat exchange, 39 enters a complementary refining reactor U for hydrofining reaction, the obtained reaction product 40 enters a separation unit V for separating hydrogen 41, and the oil phase component 42 enters a fractionation system.
The reaction system in the process adopts an isomerization dewaxing and complementary refining technology, the isomerization reaction temperature is 310-380 ℃, and the complementary refining reaction temperature is 220-280 ℃.
And (9): the oil phase component 42 obtained in the step (8) enters a normal pressure fractionating tower W of a fractionating system, and gasoline type aromatic hydrocarbon-free white oil 43 is extracted from the top of the tower; the normal pressure fractionating tower W is provided with two side stripper towers, coal oil type aromatic hydrocarbon-free white oil 44 is produced in the first line, and drilling fluid 45 is produced in the second line; and the atmospheric tower bottom material atmospheric bottom oil 46 enters a reduced pressure fractionating tower X for further separation, the reduced pressure fractionating tower X is provided with three side draws, wherein a first-line drawn product is a No. 2 base oil product 47, a second-line drawn product is a No. 4 base oil product 48, a third-line drawn product is a No. 8 base oil product 49, and a bottom product of the reduced pressure fractionating tower is bright stock 50.
In the above fractionation system, the atmospheric fractionation tower has a top temperature of 95-115 deg.C and a pressure of 0.1-0.15MPa (G), the vacuum fractionation tower has a top temperature of 65-80 deg.C and a top pressure of-0.1 MPa (G).
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. A multi-industrial-chain processing system for low-temperature Fischer-Tropsch synthesis products is characterized by comprising:
the device comprises a light component removal tower (A), an extraction deoxidation unit (C), a fixed bed fine deoxidation unit (D) and a fractionating tower (E), wherein a tower bottom discharge hole of the light component removal tower (A) is also connected with a feed inlet of a rectifying tower (B), a tower top discharge hole of the fractionating tower (E) is connected with a feed inlet of a C5-C8 olefin adsorption separation unit (F), a tower bottom discharge hole of the fractionating tower (E) is connected with a feed inlet of a C9-C12 olefin adsorption separation unit (G), discharge holes of the C5-C8 olefin adsorption separation unit (F) and the C9-C12 olefin adsorption separation unit (G) and a discharge hole of the rectifying tower (B) are respectively connected with a buffer tank (H), and a discharge hole of the buffer tank (H) is respectively connected with feed inlets of a hydrofining reactor (I) and a hydrocracking reactor (N);
the hydrofining reactor (I), the separation unit (J), the fractionating tower (K) and the diesel stripping tower (M) are sequentially connected, a discharge hole in the top of the fractionating tower (K) is connected with a feed inlet of the reflux tank (L), and a discharge hole in the bottom of the fractionating tower (K) is connected with a feed inlet of the hydrocracking reactor (N);
the hydrocracking reactor (N), the separation unit (O), the fractionating tower (P) and the diesel stripping tower (R) are sequentially connected, a discharge hole in the top of the fractionating tower (P) is connected with a feed inlet of the reflux tank (Q), and a treatment hole in the bottom of the fractionating tower (P) is connected with a feed inlet of the isomerization dewaxing reactor (S);
the isomerization dewaxing reactor (S), the heat exchanger (T), the complementary refining reactor (U), the separation unit (V) and the atmospheric fractionating tower (W) are connected in sequence.
2. A multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis products is characterized by comprising the following steps:
(1) Performing light and heavy removal treatment on a mixture of light naphtha and low-temperature condensate to obtain C5-C12 fractions, and extracting crude deoxidizer to 3000ppm or below;
(2) Carrying out fixed bed adsorption and fine deoxidation on the C5-C12 mixture subjected to coarse deoxidation in the step (1) until the content is 5ppm or below, carrying out alkane-alkene separation through simulated moving bed adsorption, separating and cutting the mixture by a fractionating device to obtain a component rich in alpha-alkene and a residual raffinate mainly containing alkane;
(3) Downstream processing of the alpha olefin-rich component obtained in the step (2) with n-hexanol, n-octanol, n-C12 alcohol, n-C13 alcohol, PAO base oil and fine separation to obtain 1-hexene and 1-octene;
(4) Mixing the raffinate mainly containing alkane in the step (2) and the heavy C13+ component removed in the step (1), and then adding the mixture, fischer-Tropsch synthesis high-temperature condensate and paraffin products into a hydrofining reactor for hydrogenation, saturation and quality improvement;
(5) Fractionating the oil phase subjected to hydrogenation saturation in the step (4) to obtain crude naphtha, light diesel component oil and tower bottom 1# soft wax;
(6) Extracting the 1# soft wax part in the step (5) for thin film distillation cutting to extract different grades of refined wax products, and continuously feeding the rest most of the refined wax products into a hydrocracking reactor for cracking the components and performing supplementary refining after cracking;
(7) Fractionating the oil phase of the hydrocracking section in the step (6) to obtain crude naphtha, heavy diesel component oil and circulating No. 2 soft wax at the bottom of the fractionating tower;
(8) The part of the 2# soft wax extracted in the step (7) enters an isomerization dewaxing reactor and a part of a complementary refining reaction;
(9) And (4) carrying out atmospheric and vacuum fractionation on the oil phase subjected to isodewaxing in the step (8) to obtain light white oil, drilling fluid and lubricating oil base oil.
3. The multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis products according to claim 1, wherein the specific steps in step (1) include: filtering the light naphtha 1, and then entering a light component removal tower A to remove a C4 component 3, and obtaining C5-C8 stable naphtha 2 at the tower bottom; filtering the low-temperature Fischer-Tropsch condensate 4, and then entering a rectifying tower B for removing the weight, obtaining a C13+ heavy component 6 at the tower bottom, and obtaining a C5-C12 light oil product 5 at the tower top; the components of C5-C12 obtained by the two towers are mixed and then enter an extraction deoxidation unit (C) for coarse deoxidation.
4. The multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis products according to claim 1, wherein the specific steps in the step (2) include: the material 7 after extraction and deoxidation enters a fixed bed fine deoxidation unit (D); after fine deoxidation, the C5-C12 components 8 enter a fractionating tower (E) for cutting, the C5-C8 components 9 obtained at the tower top are sent to a C5-C8 olefin adsorption separation unit (F) for separation to obtain C5-C8 olefin components 11 and C5-C8 alkane components 12; C9-C12 alkane components 10 are obtained at the bottom of the tower and are sent to a C9-C12 alkene adsorption separation unit (G) for separation to obtain C9-C12 alkene components 13 and C9-C12 alkane components 14; the component 12 and the component 14 are mixed to obtain the raffinate mainly containing alkane.
5. The multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis products according to claim 1, wherein the specific step of step (4) includes: the raffinate mainly containing alkane obtained by mixing the component 12 and the component 14, the C13+ heavy component 6, the Fischer-Tropsch synthesis high-temperature condensate 15 and the paraffin product 16 enter a buffer tank (H), the mixture 17 and hydrogen 18 are mixed and enter a hydrofining reactor (I) for hydrogenation saturation, the mixture enters a separation unit (J) for separating hydrogen 20, and the oil phase component 21 enters a fractionation system.
6. The multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis products according to claim 1, wherein the specific steps in the step (5) include: after the oil phase component 21 enters a fractionating tower (K) of a fractionating system, crude naphtha 21 at the top of the fractionating tower enters a reflux tank (L); the side line extraction 22 of the fractionating tower enters a diesel oil stripping tower (M), the light components 26 at the top of the fractionating tower return to the fractionating tower (K), and the light diesel oil component oil 25 obtained at the bottom of the fractionating tower is extracted to a finished product tank area; and obtaining the No. 1 soft wax at the bottom of the fractionating tower (K).
7. The multi-industrial-chain processing method of low-temperature Fischer-Tropsch synthesis products according to claim 1, wherein the No. 1 soft wax part is extracted 23 to a 10Wt/a device for membrane distillation, cutting and extraction of refined wax products with different grades; the rest 24 continuously enters a hydrocracking reactor (N) to crack and supplement and refine the heavy components after cracking, the reacted oil phase 28 enters a separation unit (O) to separate hydrogen 29, and the oil phase component 30 enters a fractionation system.
8. The multi-industrial-chain processing method for low-temperature Fischer-Tropsch synthesis products according to claim 1, wherein the oil phase component 30 enters the fractionating tower (P) of the fractionating system, and then enters the reflux drum (Q) through the crude naphtha 31 at the top of the fractionating tower; a side line extraction 32 of the fractionating tower enters a diesel stripping tower (R), a light component 36 at the top of the tower returns to the fractionating tower (K), and a light diesel component oil 35 obtained at the bottom of the tower is extracted to a finished product tank area; and 2# soft wax is obtained at the bottom of the fractionating tower (K).
9. The multi-industrial-chain processing method of low-temperature Fischer-Tropsch synthesis products according to claim 1, characterized in that the 2# soft wax extraction part 33 is mixed with hydrogen 37, and then enters an isomerization dewaxing reactor (S) for reaction, the obtained reaction product 38 enters a heat exchanger (T) for heat exchange, then 39 enters a complementary refining reactor (U) for hydrorefining reaction, the obtained reaction product 40 enters a separation unit (V) for separation of hydrogen 41, and the oil phase component 42 enters a fractionation system.
10. The multi-industrial-chain processing method for the low-temperature Fischer-Tropsch synthesis product according to claim 1, wherein the oil phase component 42 obtained in the step (8) enters a fractionation system atmospheric fractionation tower (W), and the gasoline type aromatic-free white oil 43 is extracted from the top of the tower; the normal pressure fractionating tower (W) is provided with two side stripper towers, the kerosene type aromatic hydrocarbon-free white oil 44 is extracted at the first line, and the drilling fluid 45 is extracted at the second line; and the atmospheric tower bottom material atmospheric bottom oil 46 enters a reduced pressure fractionating tower (X) for further separation, three side draws are arranged on the reduced pressure fractionating tower (X), wherein a first-line drawn product is a No. 2 base oil product 47, a second-line drawn product is a No. 4 base oil product 48, a third-line drawn product is a No. 8 base oil product 49, and a bottom product of the reduced pressure fractionating tower is bright stock 50.
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