A process for preparing high carbon internal olefins from a feed of fischer-tropsch oil

Abstract

The application discloses a process for preparing high-carbon internal olefins from Fischer-Tropsch oil as raw material, which comprises the following steps: a, Fischer-Tropsch oil is subjected to vacuum rectification in a vacuum tower to obtain a first gas phase and a first oil phase; b, the first gas phase is output from the top of the vacuum tower and enters an extraction tower, an extractant is introduced into the extraction tower from the middle and upper part of the extraction tower, mixed with the first gas phase and extracted to obtain a second gas phase and a second oil phase; c, the second gas phase is output from the top of the extraction tower and subjected to rectification in a first rectification tower to obtain a third gas phase and a third oil phase; and d, the third oil phase is output from the bottom of the first rectification tower and subjected to reaction in an isomerization reactor to obtain a target product. The process for preparing high-carbon internal olefins from Fischer-Tropsch oil as raw material can effectively avoid the loss of alpha olefins, has the advantages of low energy consumption, high efficiency, economy and environmental protection, and the obtained high-carbon internal olefin product has good sizing performance.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of chemical synthesis, in particular to a process for preparing high-carbon internal olefins from Fischer-Tropsch oil. BACKGROUND

[0002] Fischer-Tropsch (F-T) synthesis technology refers to a reaction in which hydrocarbons are produced by chain growth under the action of a catalyst using synthesis gas (CO and H2) as raw materials, which is an important way to synthesize clean fuels and chemical products through non-petroleum routes, and the raw materials are mainly derived from the conversion of coal, natural gas and biomass. The products obtained by Fischer-Tropsch synthesis are cleaner than traditional petroleum-based products and better meet the current global environmental protection requirements, especially in the production of high-grade lubricating oil base oil and high-melting-point paraffin wax.

[0003] However, the oxygen-containing compounds in the products of Fischer-Tropsch synthesis will affect the subsequent development and utilization of the products, and it is necessary to deoxidize and refine the Fischer-Tropsch synthesis products to improve the quality of the oil products and better exert the advantages of Fischer-Tropsch synthesis oil products. In the prior art, the method for removing oxygen-containing compounds has problems such as high cost, high energy consumption, low efficiency and environmental pollution. SUMMARY

[0004] The present application provides a process for preparing high-carbon internal olefins from Fischer-Tropsch oil.

[0005] The present application provides a process for preparing high-carbon internal olefins from Fischer-Tropsch oil, which comprises the following steps:

[0006] Step a: Fischer-Tropsch oil is subjected to vacuum distillation to obtain a first gas phase and a first oil phase, wherein the first gas phase is a mixed gas containing C16-C18, and the first oil phase is a mixed oil body containing compounds with carbon number of 19 or more;

[0007] Step b: the first gas phase is output from the top of the extraction tower, and an extractant is introduced into the extraction tower through the upper part of the extraction tower to mix and extract with the first gas phase, thereby obtaining a second gas phase and a second oil phase, wherein the second gas phase is a mixed gas containing C16-18, oxygen-containing compounds and extractant;

[0008] Step c: the second gas phase is output from the top of the extraction tower and subjected to rectification in a first rectification tower to obtain a third gas phase and a third oil phase, wherein the third gas phase is a mixed gas containing the extractant, and the third oil phase is a mixed oil body containing C16-18 and oxygen-containing compounds, and the concentration of oxygen-containing compounds in the mixed oil body is less than or equal to 500 ppm;

[0009] Step d: the third oil phase is output from the bottom of the first rectification tower and subjected to reaction in an isomerization reactor to obtain a target product.

[0010] In one embodiment of the present application, the second oil phase is output from the bottom of the extraction column and enters a flash tank for flash treatment to obtain a fourth gas phase and a fourth oil phase, wherein the fourth gas phase is configured to be recycled to the extraction column.

[0011] In one embodiment of the present application, the second oil phase is heated by a heater before entering the flash tank.

[0012] In one embodiment of the present application, the fourth oil phase is output from the bottom of the flash tank and enters a second rectifying column for rectification to obtain a fifth gas phase and a fifth oil phase, wherein the fifth gas phase is configured to be recycled to the extraction column.

[0013] In one embodiment of the present application, the Fischer-Tropsch oil is a mixed oil body containing C4-C30.

[0014] In one embodiment of the present application, the extractant is aqueous methanol or aqueous ethanol, and the water content of the extractant is 0-25%wt.

[0015] In one embodiment of the present application, the extractant enters the extraction column from the middle upper part of the extraction column and moves to the bottom of the extraction column, and the first gas phase enters the extraction column from the middle lower part of the extraction column and moves to the upper part of the extraction column.

[0016] In one embodiment of the present application, a catalyst is arranged in the isomerization reactor, and the catalyst is one or more of Hβ zeolite, ZSM-5, ZSM-34, and palladium hydride.

[0017] In one embodiment of the present application, in step c, the third gas phase is configured to be recycled to the extraction column.

[0018] In one embodiment of the present application, the third oil phase contains C16-C18 alpha-olefins and alkanes, and the third oil phase is configured to react in an isomerization reactor to generate C16-C18 internal olefins.

[0019] The present application provides a process for preparing high-carbon internal olefins from Fischer-Tropsch oil, which first rectifies and cuts the target carbon number, then removes a large amount of oxygen-containing compounds using extraction to obtain qualified raw materials for double bond isomerization, and finally obtains high-carbon internal olefin products through double bond isomerization. The loss of alpha-olefins can be effectively avoided, and the process has the advantages of low energy consumption, high efficiency, economy and environmental protection, and the obtained high-carbon internal olefin product has good sizing performance.

[0020] Other features of the present application and its advantages will become apparent from the following detailed description of exemplary embodiments thereof, with reference to the drawings. BRIEF DESCRIPTION OF DRAWINGS

[0021] The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments of the application and, together with the description, serve to explain the principles of the application.

[0022] Figure 1 is a process flow diagram for preparing high-carbon internal olefins from Fischer-Tropsch oil according to an embodiment of the present disclosure;

[0023] Figure 2 is a process structure diagram for preparing high-carbon internal olefins from Fischer-Tropsch oil according to an embodiment of the present disclosure.

[0024] 1 - vacuum column; 11 - first vacuum column; 12 - second vacuum column; 2 - extraction column; 3 - first rectification column; 4 - flash tank; 5 - heater; 6 - isomerization reactor; 7 - second rectification column. DETAILED DESCRIPTION

[0025] In order to make the purposes, technical solutions and beneficial technical effects of the present application clearer, the present application will be described in detail below in combination with specific embodiments. It should be understood that the embodiments described in the specification are only for the purpose of explaining the present application and are not intended to limit the present application.

[0026] For the sake of brevity, only some numerical ranges are explicitly recited herein. However, any lower limit can be combined with any upper limit to form a range not explicitly recited; and any lower limit can be combined with any other lower limit to form a range not explicitly recited, as can any upper limit with any other upper limit to form a range not explicitly recited. Further, although a range is recited, each point or individual value within the range is included in the range. Thus, each point or individual value can be combined as a lower limit or an upper limit with any other point or individual value or with other lower or upper limits to form a range not explicitly recited.

[0027] In the description of the present application, it should be noted that, unless otherwise specified, "above", "below", "upper", "lower", "top", "bottom", "over", "under" and like terms include the number zero. "One or more" means two or more.

[0028] The above summary of the application is not intended to describe each disclosed embodiment or implementation of the present application. The example embodiments are explained in more detail in the following description. Throughout this application, guidance is provided by a series of embodiments, which can be used in various combinations. In each instance, the list is representative and should not be construed as exhaustive.

[0029] This disclosure provides a process for preparing high-carbon internal olefins from Fischer-Tropsch oil as raw material, comprising the following steps: a) Fischer-Tropsch oil enters a vacuum distillation column for vacuum distillation to obtain a first gas phase and a first oil phase; b) The first gas phase is output from the top of the vacuum distillation column and enters an extraction column, where an extractant enters the upper middle part of the extraction column and mixes with and extracts the first gas phase to obtain a second gas phase and a second oil phase; c) The second gas phase is output from the top of the extraction column and enters a first distillation column for distillation to obtain a third gas phase and a third oil phase; d) The third oil phase is output from the bottom of the first distillation column and enters an isomerization reactor for reaction to obtain the target product.

[0030] This invention provides a process for preparing high-carbon inner-olefins from Fischer-Tropsch oil. First, distillation is used to cut the target carbon number, followed by extraction to remove a large amount of oxygen-containing compounds, yielding a qualified raw material suitable for double bond isomerization. Finally, double bond isomerization is used to obtain the high-carbon inner-olefin product. This process effectively avoids the loss of α-olefins, has the advantages of low energy consumption, high efficiency, and economic and environmental benefits, and the resulting high-carbon inner-olefin product exhibits good sizing properties.

[0031] The specific embodiments of this disclosure are described below with reference to the accompanying drawings.

[0032] like Figures 1 to 2 As shown, this disclosure provides a process for preparing high-carbon inner olefins from Fischer-Tropsch oil, comprising the following steps:

[0033] Step a: Fischer-Tropsch oil enters vacuum distillation tower 1 for vacuum distillation to obtain a first gas phase and a first oil phase. The first gas phase is a mixed gas containing C16-C18, and the first oil phase is a mixed oil containing 19 or more carbon atoms.

[0034] Specifically, in one embodiment of this disclosure, the Fischer-Tropsch oil is a mixed oil containing C4-C30 and containing oxygen-containing compounds. The Fischer-Tropsch oil enters a vacuum distillation tower 1, where it undergoes vacuum distillation to obtain a mixed gas containing C16-C18 and a mixed oil containing 19 or more carbon atoms. In this embodiment, the number of vacuum distillation towers 1 can be set according to actual needs and is not limited herein. In this embodiment, it is preferable to provide two vacuum distillation towers 1, namely a first vacuum distillation tower 11 and a second vacuum distillation tower 12.

[0035] Step b: The first gas phase is output from the top of the vacuum tower 1 and enters the extraction tower 2. The extractant enters the extraction tower 2 through the middle and upper part of the extraction tower 2 and mixes with the first gas phase and is extracted to obtain the second gas phase and the second oil phase. The second gas phase is a mixed gas containing C16-18, oxygen-containing compounds and extractant.

[0036] Specifically, due to the difference in carbon number, the boiling points of each hydrocarbon are also different. Under the control of the internal temperature of the vacuum tower 1, the first gas phase containing C16-18 is output through the top of the vacuum tower 1 and enters the extraction tower 2 from the middle-lower part of the extraction tower 2. The extractant enters from the middle-upper part of the extraction tower 2, mixes with the first gas phase, and extracts the first gas phase to obtain a second gas phase, which is a mixed gas containing C16-18, oxygen-containing compounds and extractant.

[0037] In one embodiment of the present disclosure, the extractant is selected from alcohol extractants. In this embodiment, the extractant is aqueous methanol or aqueous ethanol, and the water content of the extractant is 0-25%wt.

[0038] Considering that the density of the extractant is greater than the density of the first gas phase, in one embodiment of the present disclosure, the extractant enters the extraction tower 2 through the middle-upper part of the extraction tower 2 and moves to the bottom of the extraction tower 2, and the first gas phase enters the extraction tower 2 through the middle-lower part of the extraction tower 2 and moves to the upper part of the extraction tower 2.

[0039] Specifically, the extractant and the first gas phase enter the extraction tower 2 through the middle-upper part and the middle-lower part of the extraction tower 2, respectively. Due to the fact that the density of the extractant is greater than the density of the first gas phase, the extractant moves to the bottom of the extraction tower 2, and the first gas phase moves to the upper part of the extraction tower 2. During the movement, the extractant and the first gas phase are mixed and extracted.

[0040] Step c: The second gas phase is output from the top of the extraction tower 2 and enters the first rectification tower 3 for rectification to obtain a third gas phase and a third oil phase. The third gas phase is a mixed gas containing the extractant, and the third oil phase is a mixed oil body containing C16-18 and oxygen-containing compounds, wherein the concentration of oxygen-containing compounds in the mixed oil body is less than or equal to 500 ppm.

[0041] Specifically, in the industrial continuous refining process, the second gas is output from the top of the extraction tower 2. The second gas phase mainly contains the extractant that is not fully dissolved in the oil phase during the extraction process and other light components. In order to further recover and purify these substances, the second gas phase enters the first rectification tower 3 for rectification treatment. In the first rectification tower 3, by accurately controlling the temperature and pressure conditions, efficient separation of each component in the second gas phase is achieved. After rectification treatment, a third gas phase and a third oil phase are obtained. The third gas phase is mainly composed of a mixed gas of extractant and other lighter components, while the third oil phase is a mixed oil body mainly containing C16-18 hydrocarbons and oxygen-containing compounds. After the rectification treatment of the first rectification tower 3, the concentration of oxygen-containing compounds in the mixed oil body is significantly reduced and strictly controlled at a level less than or equal to 500 ppm. Such treatment results not only improve the purity and quality of the final product, but also meet the strict requirements of application fields for the content of oxygen-containing compounds, ensuring the safety and stability of the product in subsequent processing and use.

[0042] In one embodiment of the present disclosure, the third gas phase is configured to be recycled into the extraction column 2.

[0043] Specifically, after the rectification treatment via step c, the third gas phase is mainly a mixed gas composed of extractant and other lighter components. After the rectification treatment, the extractant can be recycled back to the extraction column 2 to improve the economic efficiency and environmental performance of the overall process.

[0044] In one embodiment of the present disclosure, the second oil phase is output from the bottom of the extraction column 2 and enters the flash tank 4 for flash treatment to obtain a fourth gas phase and a fourth oil phase, wherein the fourth gas phase is configured to be recycled into the extraction column 2.

[0045] Specifically, in this embodiment, the second oil phase is output from the bottom of the extraction column 2 as a heavier component. In order to effectively separate and optimize resource utilization of the second oil phase, the second oil phase is transported to the flash tank 4 for flash treatment. In this embodiment, when the second oil phase enters the flash tank 4, under the condition of instantaneous pressure reduction, part of the components will rapidly change to a gaseous state to form a fourth gas phase. The fourth gas phase is mainly composed of light hydrocarbons, extractant and other components. Since it has high recycling value and potential for reuse, it can be reconfigured and recycled back to the extraction column 2 through a pipeline to participate in a new round of extraction process, thereby realizing closed-loop recycling of the extractant, saving costs and reducing environmental pollution. At the same time, the fourth oil phase obtained after flash treatment mainly contains extractant and oxygen-containing compounds, which will continue to be processed by downstream devices. Due to the provision of the flash tank 4, the energy consumption of the entire process can be effectively reduced, and the economic efficiency of the entire process can be improved.

[0046] In one embodiment of the present disclosure, the fourth oil phase is output from the bottom of the flash tank 4 and enters the second rectification column 7 for rectification to obtain a fifth gas phase and a fifth oil phase, wherein the fifth gas phase is configured to be recycled into the extraction column 2.

[0047] In one embodiment of the present disclosure, the second oil phase enters the flash tank 4 after being heated by the heater 5.

[0048] Specifically, after the second oil phase is discharged from the bottom of the extraction column 2, it is first heated by the heater 5 to raise the temperature of the second oil phase, thereby preparing for the subsequent flash process. After the heating step is completed, the second oil phase is then sent to the flash tank 4. In the flash tank 4, the second oil phase at high temperature begins to flash rapidly with the sudden drop in pressure.

[0049] Step d: The third oil phase is output from the bottom of the first rectification column 3 and enters the isomerization reactor 6 for reaction to obtain a target product.

[0050] In one embodiment of the present disclosure, the third oil phase comprises C16-C18 alpha-olefins, alkanes, and the third oil phase is configured to generate C16-C18 internal olefins in the isomerization reactor 6.

[0051] Specifically, the third oil phase comprising C16-C18 alpha-olefins, alkanes, is reacted in the isomerization reactor 6, and generates C16-C18 internal olefin products. The carbon number range of the product can be flexibly adjusted, and also contains odd carbon, such as C17 internal olefin, which not only improves the sizing performance of the product, but also avoids the problem that the product is not conducive to sizing at room temperature due to the high condensation point.

[0052] In one embodiment of the present disclosure, a catalyst is internally provided in the isomerization reactor 6, and the catalyst is one or more of Hβ zeolite, ZSM-5, ZSM-34, and palladium hydride.

[0053] The present application provides a process for preparing high-carbon internal olefins from Fischer-Tropsch oil as raw material. First, the target carbon number is cut by rectification, then a large amount of oxygen-containing compounds are removed by extraction to obtain qualified raw materials for double bond isomerization, and finally high-carbon internal olefin products are obtained by double bond isomerization. The loss of alpha-olefins can be effectively avoided, and the process has the advantages of low energy consumption, high efficiency, economy and environmental protection, and the obtained high-carbon internal olefin product has good sizing performance.

[0054] Experimental Example 1

[0055] The Fischer-Tropsch oil with carbon number C4-C30 enters the first vacuum tower 11 for vacuum rectification, and the overhead product is a mixture gas with carbon number less than or equal to 15, and the tower bottom product C16-30 enters the second vacuum tower 12 for vacuum rectification, and the tower bottom product is C19-C30, and the overhead product is C16-C18 (including odd carbon).

[0056] The C16-C18 Fischer-Tropsch oil enters the extraction tower 2, is mixed with water-containing methanol, and is extracted to remove oxygen-containing compounds.

[0057] The extraction phase is heated to superheat, then enters the flash tank 4, and part of the methanol from the top of the flash tank 4 is returned to the extraction tower 2, and the remaining material enters the rectification tower, and part of the methanol from the top is returned to the extraction tower 2, and the tower bottom is the oxygen-containing compounds and a small amount of vented methanol.

[0058] The raffinate phase enters the first rectification tower, and the methanol from the top is returned to the extraction tower 2, and the tower bottom material enters the isomerization reactor 6 to generate a mixed product of high-carbon internal olefins and alkanes.

[0059] (1) The operating conditions of each device are as follows:

[0060]

[0061]

[0062] (2) The composition of Fischer-Tropsch oil feedstock is as follows:

[0063]

[0064]

[0065] (3) The mass ratio of alkene to alkane is 3:1.

[0066] (4) Methanol water content 1%wt.

[0067] (5) The product composition is as follows:

[0068] Light component oil from the top of the first vacuum distillation tower

[0069] No. Composition Content %wt 1 ≤C15 97 2 C16-C18 3

[0070] Second vacuum tower bottom refining and oil separation

[0071]

[0072] Oxygen-containing compounds and purge methanol

[0073] No. Composition Content %wt 1 Water 7 2 Methanol 3 3 Oxygenates 90

[0074] Mixed products of olefins and alkanes (carbonyl group <100ppm)

[0075] No. Composition Content %wt 1 C16-C18 alkanes 26 2 C16-C18 alpha olefins 2.25 3 C16-C18 internal olefins 71.75

[0076] Experiment Example 2

[0077] Fischer-Tropsch oil with a carbon number of C4-C30 enters the first vacuum distillation column 11 for vacuum distillation. The top product of the column is a mixed gas with a carbon number of less than or equal to 15. The bottom product, C16-30, enters the second vacuum distillation column 12 for vacuum distillation. The bottom product of the second column is C19-C30, and the top product is C16-C18 (including odd-numbered carbons).

[0078] C16-C18 Fischer-Tropsch oil enters CQ-1 extraction tower 2, where it is mixed with aqueous methanol and extracted to crudely remove oxygen-containing compounds.

[0079] The extract phase is heated to superheat and then enters flash tank 4. A portion of the methanol is recycled from the top of flash tank 4 and returned to extraction tower 2. The remaining material is distilled, and a portion of the methanol is recycled from the top of the tower and returned to extraction tower 2. The bottom of the tower contains oxygen-containing compounds and a small amount of purge methanol.

[0080] The raffinate enters the first distillation column, and methanol is recycled from the top of the column back to the extraction column 2. The bottom material isomerization reactor 6 produces a mixed product of high-carbon olefins and alkanes.

[0081] (1) The operating conditions for each piece of equipment were as follows:

[0082]

[0083]

[0084] (2) The Fischer-Tropsch oil feedstock composition was as follows:

[0085]

[0086] (3) The olefin to alkane mass ratio was 3:1

[0087] (4) The methanol water content was 5% wt

[0088] (5) The product composition was as follows:

[0089] First vacuum column overhead light ends oil

[0090] No. Composition Content %wt 1 ≤C15 99 2 C16-C18 1

[0091] Second vacuum column bottoms heavy ends oil

[0092] Oxygenates and vented methanol

[0093] No. Composition Content %wt 1 Water 6 2 Methanol 2 3 Oxygenates 92

[0094] Internal olefins and alkane mixed product (carbonyls < 100 ppm)

[0095] No. Composition Content %wt 1 C16-C18 alkanes 25 2 C16-C18 alpha olefins 1.25 3 C16-C18 internal olefins 73.75

[0096] The present application provides a process for preparing high carbon internal olefins from Fischer-Tropsch oil, which first distills and cuts the target carbon number, then uses extraction to remove a large amount of oxygen-containing compounds to obtain qualified raw materials that can be subjected to double bond isomerization, and finally obtains high carbon internal olefin products through double bond isomerization. It can effectively avoid the loss of alpha olefins, has the advantages of low energy consumption, high efficiency, economy and environmental protection, and the obtained high carbon internal olefin product has good sizing performance.

[0097] The above has described various embodiments of the present application, and the above description is exemplary, not exhaustive, and is not limited to the disclosed embodiments. Many modifications and changes are obvious to those skilled in the art without departing from the scope and spirit of the described embodiments. The choice of terms used herein is intended to best explain the principles, practical applications, or improvements in technology in the market of the embodiments, or to enable other ordinary skilled persons in the art to understand the embodiments disclosed herein. The scope of the present application is defined by the appended claims.

Claims

1. A process for preparing high-carbon inner olefins from Fischer-Tropsch oil, characterized in that, Includes the following steps: Step a: Fischer-Tropsch oil enters a vacuum distillation tower (1) for vacuum distillation to obtain a first gas phase and a first oil phase, wherein the first gas phase is a mixed gas containing C16-C18, and the first oil phase is a mixed oil containing 19 or more carbon atoms; Step b: The first gas phase is output through the top of the pressure reducing tower (1) and enters the extraction tower (2). The extractant enters the extraction tower (2) through the middle and upper part of the extraction tower (2) and mixes with the first gas phase and is extracted to obtain the second gas phase and the second oil phase. The second gas phase is a mixed gas containing C16-18, oxygen-containing compounds and extractant. Step c: The second gas phase is output from the top of the extraction tower (2) and enters the first distillation tower (3) for distillation to obtain a third gas phase and a third oil phase. The third gas phase is a mixed gas containing the extractant, and the third oil phase is a mixed oil containing C16-18 and oxygen-containing compounds, wherein the concentration of oxygen-containing compounds in the mixed oil is less than or equal to 500 ppm. Step d: The third oil phase is output from the bottom of the first distillation column (3) and enters the isomerization reactor (6) for reaction to obtain the target product; The third oil phase comprises C16-C18 α-olefins and alkanes, and the third oil phase is configured to react in the isomerization reactor (6) to generate C16-C18 inner olefins.

2. The process for preparing high-carbon inner olefins from Fischer-Tropsch oil according to claim 1, characterized in that, The second oil phase is output from the bottom of the extraction tower (2) and enters the flash tank for flash evaporation to obtain the fourth gas phase and the fourth oil phase, wherein the fourth gas phase is configured to be circulated back to the extraction tower (2).

3. The process for preparing high-carbon inner olefins from Fischer-Tropsch oil according to claim 2, characterized in that, The second oil phase is heated by the heater (5) and then enters the flash tank.

4. The process for preparing high-carbon inner olefins from Fischer-Tropsch oil according to claim 2, characterized in that, The fourth oil phase is output from the bottom of the flash tank and enters the second distillation column (7) for distillation to obtain the fifth gas phase and the fifth oil phase, wherein the fifth gas phase is configured to be recycled to the extraction column (2).

5. The process for preparing high-carbon inner olefins from Fischer-Tropsch oil according to claim 1, characterized in that, The Fischer-Tropsch oil is a mixture of C4-C30 oils.

6. The process for preparing high-carbon inner olefins from Fischer-Tropsch oil according to claim 1, characterized in that, The extractant is aqueous methanol or aqueous ethanol.

7. The process for preparing high-carbon inner olefins from Fischer-Tropsch oil according to claim 1, characterized in that, The extractant enters the extraction tower (2) through the middle and upper part and moves toward the bottom of the extraction tower (2), while the first gas phase enters the extraction tower (2) through the middle and lower part and moves toward the upper part of the extraction tower (2).

8. The process for preparing high-carbon inner olefins from Fischer-Tropsch oil according to claim 1, characterized in that, The isomerization reactor (6) is equipped with a catalyst, which is one or more of Hβ zeolite, ZSM-5, ZSM-34, and palladium hydride.

9. The process for preparing high-carbon inner olefins from Fischer-Tropsch oil according to claim 1, characterized in that, In step c, the third gas phase is configured to be circulated to the extraction tower (2).

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