CN110846071A

CN110846071A - Method for producing lubricating oil base oil from Fischer-Tropsch wax

Info

Publication number: CN110846071A
Application number: CN201810949839.8A
Authority: CN
Inventors: 毕云飞; 夏国富; 郭庆洲; 方文秀; 李洪宝
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2018-08-20
Filing date: 2018-08-20
Publication date: 2020-02-28
Anticipated expiration: 2038-08-20
Also published as: CN110846071B

Abstract

The invention relates to a method for producing lubricating oil base oil by Fischer-Tropsch wax, which comprises the following steps: injecting Fischer-Tropsch wax into a reaction device for hydrotreating, wherein the catalyst filled in the reaction device contains a combined catalyst which comprises a first catalyst and a second catalyst, the first catalyst contains a ten-membered ring molecular sieve M1, and the second catalyst contains a ten-membered ring molecular sieve M2; wherein the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 has the following characteristics: the molar ratio of silicon oxide to aluminum oxide is 120-300; contains a mesoporous structure and has a closed hysteresis loop at a low-temperature nitrogen adsorption-desorption curve P/P0-0.4-0.99, and the starting position of the closed hysteresis loop is at a position P/P0-0.4-0.7. The Fischer-Tropsch wax is adopted to produce the lubricating oil base oil, so that a good pour point depression effect can be obtained, and the lubricating oil base oil has high yield and high viscosity index.

Description

Method for producing lubricating oil base oil from Fischer-Tropsch wax

Technical Field

The invention relates to the field of hydrogenation treatment of Fischer-Tropsch wax, in particular to a method for producing lubricating oil base oil by using Fischer-Tropsch wax.

Background

The molecular sieve material has high acidity and high specific surface area, and is an excellent acidic catalyst. Meanwhile, the molecular sieve material has strong chemical stability and hydrothermal stability, and is difficult to be corroded and dissolved by reactants to be damaged. Compared with the commonly used homogeneous catalyst, the molecular sieve material catalyst can be directly recycled without separation, and simultaneously, the environmental pollution and the product pollution are avoided. The specific surface area and other pore structure parameters of the molecular sieve material have important influence on the catalytic performance of the molecular sieve, so that the preparation of the molecular sieve with special pores is an important research direction in the chemical field.

CN104353484A discloses a preparation method of a cheap strong-acid hierarchical pore Beta zeolite, relating to a preparation method of a hierarchical pore Beta zeolite. The invention aims to solve the problem of acidity weakening of the existing desilication post-treatment hierarchical pore Beta zeolite molecular sieve. The method comprises the following steps: (1) calcining Beta zeolite to obtain microporous hydrogen type Beta zeolite; (2) adding the microporous hydrogen type Beta zeolite into an alkaline solution, stirring, washing and drying to obtain sodium type desiliconized hierarchical porous Beta zeolite; (3) adding the sodium desiliconized hierarchical pore Beta zeolite into an ammonium nitrate aqueous solution for exchange, and calcining to obtain hydrogen desiliconized hierarchical pore Beta zeolite; (4) and (3) adding the hydrogen-type desiliconized hierarchical pore Beta zeolite into an acid solution, stirring, washing, drying, and then repeating the step (3) to obtain the strong-acid hierarchical pore Beta zeolite.

CN103073020A discloses a hierarchical pore zeolite molecular sieve and a preparation method and application thereof. The preparation method specifically comprises the following steps: the method for preparing the hierarchical zeolite molecular sieve by assembling silanized zeolite seed crystals under hydrothermal conditions by using a cationic surfactant as a template. The method overcomes the problem that the multistage pore zeolite cannot be prepared due to the mismatching between the conventional cationic surfactant and the zeolite template. The prepared material realizes the composition of micropores and mesopores, and is a highly crystallized multi-level pore channel zeolite molecular sieve. In the method, substantially, organosilane is grafted to a seed crystal by utilizing a specific functional group reaction, and is matched with a cationic surfactant to prepare a mesoporous molecular sieve, wherein mesopores are formed by guiding the cationic surfactant, and the mesopores with the aperture of about 2.4nm are formed by utilizing the hard template action of the organosilane. The seed crystal selected in the invention is microporous molecular sieve, which is added into a preparation system after silanization, the hydrophobic property of the seed crystal is utilized to increase the effect of the seed crystal on the hydrophobic end of a surfactant micelle so as to reduce the interaction between two guiding agents, but the formed mesopores still do not have a regular structure, and whether the addition of the seed crystal reduces the dosage of a template agent is not reported.

CN104891526A discloses a preparation method of a mesoporous molecular sieve with high hydrothermal stability. The method comprises the following steps: (1) preparing a first Y-type molecular sieve precursor: (2) and (3) crystallization: adding seed crystals into a first Y-type molecular sieve precursor, adjusting the pH value to 0.5-5, stirring at 20-50 ℃ for 10-24 h, aging at 20-50 ℃ for 2-24 h to obtain an assembled product, transferring the assembled product into a microreactor with a polytetrafluoroethylene lining, transferring the assembled product and the reactor into an autoclave, crystallizing at 100-200 ℃ for 10-48 h, filtering, washing and drying to obtain the high-stability mesoporous molecular sieve. Firstly, a precursor of the microporous molecular sieve is prepared, the mesoporous-microporous molecular sieve is used for preparing the mesoporous molecular sieve as a seed crystal, two methods of molecular sieve precursor assembly and seed crystal are combined, and the mesoporous molecular sieve with high stability is obtained under the condition of not using an organic template agent. Not only greatly reduces the preparation cost of the molecular sieve, but also saves the process of calcining the template agent and reduces the energy consumption.

CN102050459A discloses a method for preparing a high-silicon molecular sieve, wherein the method comprises carrying in an inert carrier gas flowUnder the belt, the molecular sieve flows with inert carrier gas and is mixed with gas phase SiCl₄Contacting molecular sieve with gas-phase SiCl in a flowing state₄The contact time of (a) is from 10 seconds to 100 minutes. The method for preparing the high-silicon molecular sieve can realize the molecular sieve and SiCl₄The contact reaction of (2) is continuously carried out, and the molecular sieve and SiCl can be controlled by controlling the flow rate of the carrier gas and the length of the tubular reactor₄The time of contact, thereby enabling the molecular sieve to be contacted with SiCl₄The contact reaction of (2) is sufficiently carried out in the tubular reactor.

CN1703490A discloses a catalyst combination process for the production of lube base stock this invention relates to a process for converting heavy component containing wax to high quality lube basestock by using a linear mesoporous molecular sieve having a near circular pore structure with an average diameter of 0.50nm to 0.65nm, wherein the difference between the maximum and minimum diameter is 0.05nm or less, followed by a molecular sieve β zeolite catalyst.

CN1803998A discloses a dewaxing catalyst containing a composite molecular sieve, which contains a molecular sieve with a one-dimensional mesoporous structure and a molecular sieve with a macroporous structure, wherein the weight ratio of the molecular sieve with the one-dimensional mesoporous structure to the molecular sieve with the macroporous structure is 80-99: 1-20, the molecular sieve with the macroporous structure contains non-framework silicon, and the content of the silicon is 1-20 wt% calculated by oxide and based on the molecular sieve.

Disclosure of Invention

The invention aims to provide a method for producing lubricating oil base oil by Fischer-Tropsch wax, which can obtain better pour point depression effect, high yield of the lubricating oil base oil and high viscosity index by adopting the combined catalyst to produce the lubricating oil base oil by Fischer-Tropsch wax.

In order to achieve the above object, the present invention provides a method for producing a lubricant base oil from fischer-tropsch wax, the method comprising: injecting Fischer-Tropsch wax into a reaction device for hydrotreating, wherein the catalyst filled in the reaction device contains a combined catalyst which comprises a first catalyst and a second catalyst, the first catalyst contains a ten-membered ring molecular sieve M1, the second catalyst contains a ten-membered ring molecular sieve M2, the first catalyst and the second catalyst respectively and independently contain an active metal component, and the first catalyst and the second catalyst are respectively filled in different reactors of the reaction device;

wherein the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 has the following characteristics: the molar ratio of silicon oxide to aluminum oxide is 120-300; contains a mesoporous structure and has a closed hysteresis loop at a low-temperature nitrogen adsorption-desorption curve P/P0-0.4-0.99, and the starting position of the closed hysteresis loop is at a position P/P0-0.4-0.7.

Optionally, in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2, the molecular sieve has a silica/alumina molar ratio of 150-.

Optionally, in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2, the mesoporous area of the molecular sieve is 50M²/g-250m²The proportion of the mesoporous area in the specific surface area is 20-70%, preferably 25-65%.

Optionally, in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2, the start position of the closed hysteresis loop is at P/P0 ═ 0.4 to 0.6.

Optionally, the amount of penta-coordinated aluminum in the precursor of the molecular sieve in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 is 4 to 30 wt%, preferably 10 to 30 wt%, calculated as oxide and based on the total alumina amount of the molecular sieve.

Optionally, in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2, the amount of penta-coordinated aluminum in the final molecular sieve is 3 wt% or less, preferably 1 wt% or less, more preferably no penta-coordinated aluminum, calculated as oxide and based on the total alumina amount of the molecular sieve.

Alternatively, the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 is prepared according to the following steps:

(1) filtering the crystallized mother liquor to form a filter cake with the dry basis content of 5-30%;

(2) directly roasting the filter cake to obtain a molecular sieve precursor;

(3) subjecting the molecular sieve precursor to a hydrothermal treatment;

(4) and filtering, washing and drying the hydrothermal treatment product.

Optionally, in step (1), the filter cake formed by the filtration has a dry content of 6-15%.

Optionally, in the step (2), the temperature of the calcination is 400-.

Optionally, in the step (3), the medium for the hydrothermal treatment is acidic water;

preferably, the acidic water contains inorganic acid and/or organic acid, and the content of the inorganic acid and/or organic acid is 0.1M-5M, preferably 0.2M-2M;

more preferably, the acidic water contains at least one of hydrochloric acid, sulfuric acid, phosphoric acid, nitric acid, citric acid, acetic acid, maleic acid, oxalic acid, nitrilotriacetic acid, 1, 2-cyclohexanediaminetetraacetic acid, tartaric acid, and malic acid.

Optionally, in the step (3), the liquid-solid volume ratio of the hydrothermal treatment is 5-200, preferably 20-100; the temperature of the hydrothermal treatment is 100-300 ℃, and preferably 100-200 ℃; the time of the hydrothermal treatment is 0.5 to 24 hours, preferably 1 to 12 hours, and more preferably 1 to 4 hours;

preferably, the hydrothermal treatment is carried out in a closed container, and the pressure of the hydrothermal treatment is the autogenous pressure of the closed container under the hydrothermal condition.

Optionally, in the step (4), the washing process is water washing with deionized water, and the water washing is completed until the pH value of the filtrate is 6-8, preferably 6-7.

Optionally, the reactor filled with the first catalyst is located upstream or downstream of the reactor filled with the second catalyst, according to the flow direction of the reaction mass.

Optionally, the ten-membered ring molecular sieve M1 and the ten-membered ring molecular sieve M2 are each independently selected from at least one of a ZSM-22 molecular sieve, a ZSM-23 molecular sieve, a ZSM-48 molecular sieve, a ZSM-5 molecular sieve, an SSZ-32 molecular sieve and a Eu-1 molecular sieve.

Optionally, the loading weight ratio of the first catalyst to the second catalyst is 1: 0.1 to 10;

the active metal component is Pt and/or Pd;

the first catalyst also comprises a refractory inorganic oxide, wherein the content of the ten-membered ring molecular sieve M1 is 20-80 wt%, preferably 25-55 wt%, and the content of the active metal component is 0.1-5 wt%, preferably 0.2-3 wt%, more preferably 0.4-1 wt%, based on the weight of the first catalyst;

the second catalyst also comprises a refractory inorganic oxide, the ten-membered ring molecular sieve M2 is present in an amount of 20 to 80 wt%, preferably 25 to 55 wt%, and the active metal component is present in an amount of 0.1 to 5 wt%, preferably 0.2 to 3 wt%, more preferably 0.4 to 1 wt%, based on the weight of the second catalyst.

Optionally, the distillation range of the Fischer-Tropsch wax is 200-800 ℃;

the hydrotreating conditions for the different reactors independently comprise: the temperature is 200-500 ℃, preferably 250-400 ℃, and more preferably 300-350 ℃; the pressure is 1-30MPa, preferably 2-20MPa, more preferably 5-20 MPa; the volume space velocity is 0.1-5h^-1Preferably 0.1 to 3h^-1More preferably 0.5 to 2 hours^-1(ii) a The volume ratio of the hydrogen to the oil is 50-3000, preferably 300-3000, more preferably 400-600.

According to the method for producing the lubricating oil base oil by the Fischer-Tropsch wax, two catalysts containing the molecular sieve with special physicochemical properties are combined and used in different reactors, so that a good isomerization pour point depression effect can be obtained, and the yield of the lubricating oil base oil can be improved.

Additional features and advantages of the invention will be set forth in the detailed description which follows.

Drawings

The accompanying drawings, which are included to provide a further understanding of the invention and are incorporated in and constitute a part of this specification, illustrate embodiments of the invention and together with the description serve to explain the principles of the invention and not to limit the invention. In the drawings:

FIG. 1 is a schematic structural view of one embodiment of a reaction apparatus used in the method of the present invention.

Description of the reference numerals

1 first reactor 2 second reactor

Detailed Description

The following describes in detail specific embodiments of the present invention. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.

The combined catalyst comprises a first catalyst and a second catalyst, wherein the first catalyst contains a ten-membered ring molecular sieve M1, and the second catalyst contains a ten-membered ring molecular sieve M2.

In the combined catalyst, at least one of the ten-membered ring molecular sieve M1 and the ten-membered ring molecular sieve M2 is high in silicon and contains mesopores. Preferably, both the ten-membered ring molecular sieve M1 and the ten-membered ring molecular sieve M2 have the characteristics of being high in silicon and containing mesopores.

Preferably, the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 has a high silicon content. Ten-membered ring molecular sieves prepared according to methods conventional in the art typically have a silica to alumina mole ratio of less than 100. The mole ratio of silica/alumina of the molecular sieve M1 and/or the ten-membered ring molecular sieve M2 in the present invention is 120-300, and specifically, it may be, for example, 120, 130, 140, 150, 160, 170, 180, 190, 200, 210, 220, 230, 240, 250, 260, 270, 280, 290, 300 or any value in the range of any two of these values. Preferably, the molecular sieve M1 and/or the ten-membered ring molecular sieve M2 have a silica/alumina molar ratio of 150-200.

Preferably, the molecular sieve M1 and/or the ten-membered ring molecular sieve M2 according to the present invention have a mesoporous structure. Molecular sieves prepared according to conventional methods in the art are typically microporous molecular sieves, which do not contain a mesoporous structure. On the low temperature nitrogen adsorption-desorption curves of the molecular sieves M1 and/or M2 of the present invention, the adsorption branch and desorption branch show a closed hysteresis loop at P/P0 of 0.4 to 0.99 and the start of the closed hysteresis loop is at P/P0 of 0.4 to 0.7, whereas the prior art molecular sieves do not have this feature, i.e., no hysteresis loop or the start of the hysteresis loop occurs at higher partial pressures in this interval (typically at P/P0> 0.7). Preferably, the start position of the closed hysteresis loop is at P/P0-0.4-0.6.

Preferably, the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 are/is characterized by a nitrogen adsorption BET (Brunner-Emmet-Teller) method, and the mesoporous area in the molecular sieve can be 50M²/g-250m²The specific surface area of the molecular sieve can be 150m²/g-400m²The proportion of the mesoporous area to the specific surface area can be 20-70%, preferably 25-65%.

Preferably, the ten-membered ring molecular sieve M1 and/or M2 of the present invention is characterized by high silicon content, mesoporous content, and closed hysteresis, and the precursor is enriched in penta-coordinated aluminum, while the final molecular sieve contains little or no penta-coordinated aluminum. Specifically, the content of penta-coordinated aluminum in the precursor of the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 is 4 to 30% by weight, preferably 10 to 30% by weight; and the content of penta-coordinated aluminum in the finished molecular sieve is 3 wt% or less, preferably 2.5 wt% or less, more preferably 2 wt% or less, even more preferably 1 wt% or less, even more preferably 0.5 wt% or less, and most preferably no penta-coordinated aluminum is contained.

Generally, the preparation of the aluminum-containing molecular sieve can be divided into steps of colloid formation, crystallization, post-treatment and the like. In order to obtain the high-silicon mesoporous ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2, a post-treatment step in the synthesis process of the aluminum-containing molecular sieve is required to be specially treated. Preferably, the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 is prepared according to the following steps:

(1) filtering the crystallized mother liquor to form a filter cake with the dry basis content of 5-30 wt%;

(2) directly roasting the filter cake to obtain a molecular sieve precursor;

(3) subjecting the molecular sieve precursor to a hydrothermal treatment;

(4) and filtering, washing and drying the hydrothermal treatment product.

In the step (1), the mother liquor after crystallization is filtered for the purpose of removing the synthesis mother liquor. The invention is particularly limited with respect to the dry content of the filter cake formed by filtration. In particular, the filter cake has a dry content of 5 to 30% by weight, preferably 6 to 15% by weight. When the dry basis content in the filter cake is out of the above range, the physicochemical properties of the prepared molecular sieve are out of the range defined by the present invention. In the present invention, "dry basis" is defined as: the mass percentage of the material after roasting at 600 ℃ for 4 hours to the mass of the material before roasting.

In the step (2), the filter cake formed in the step (1) is directly roasted at a high temperature without being dried. In the present invention, the temperature of the calcination may be 400-600 ℃, preferably 450-550 ℃. The heating rate during the calcination can be 10-100 deg.C/min, preferably 20-50 deg.C/min. The calcination time may be 1 hour to 12 hours, preferably 2 hours to 6 hours. The roasting environment can be a natural environment, namely oxygen-containing gas is not required to be specially introduced during roasting. Even if the calcination is carried out in the natural environment, the water in the filter cake can oxidize the template agent and can react with the aluminum in the molecular sieve to form non-framework aluminum. In particular, the product treated by step (2) in the present invention (i.e., the molecular sieve precursor) contains a significant amount of penta-coordinated non-framework aluminum (i.e., penta-coordinated aluminum). Penta-coordinated non-framework aluminum is defined as²⁷Chemical shift б in the Al NMR spectrum is a peak of 15-40 ppm.²⁷Al NMR spectroscopic measurement conditions can be found in publications such as Guoliang Zhaoet Al, Applied Catalysis A: General 299(2006) 167-.

In the present invention, the amount of penta-coordinated aluminum in the product treated in step (2) (i.e., the molecular sieve precursor) is 4 to 30% by weight, preferably 10 to 30% by weight; in the step (2), the sample after the roasting treatment can be naturally cooled, and the target temperature is preferably room temperature.

In step (3), the medium for the hydrothermal treatment is preferably acidic water. In the present invention, the acidic water means containing H⁺H of (A) to (B)₂And (4) O solution. Wherein H₂O is a conventional process to obtain a liquid material called "water". H⁺Is the ion released by the dissociation of organic acid and/or inorganic acid. To obtain the acidic water, at least one of hydrochloric acid, sulfuric acid, phosphoric acid, nitric acid, citric acid, acetic acid, maleic acid, oxalic acid, nitrilotriacetic acid, 1, 2-cyclohexanediaminetetraacetic acid, tartaric acid and malic acid, preferably hydrochloric acid and/or citric acid, may be added to the "water". The content of the inorganic acid and/or the organic acid in the acidic water can be 0.1M-5M, preferably 0.2M-2M.

In step (3), the liquid-solid volume ratio of the hydrothermal treatment may be 5 to 200, preferably 20 to 100; in the step (3), the temperature of the hydrothermal treatment may be 100 to 300 ℃, preferably 100 to 200 ℃; in step (3), the time of the hydrothermal treatment may be 0.5 to 24 hours, preferably 1 to 12 hours, more preferably 1 to 4 hours; in step (3), the hydrothermal treatment is preferably performed in a closed vessel, and the pressure of the hydrothermal treatment is preferably the autogenous pressure of the closed vessel under the hydrothermal conditions.

In the step (4), the molecular sieve is required to be filtered and washed after being treated in the step (3). Among them, the filtration method may be a method known to those skilled in the art. The washing process can be water washing with deionized water, and the water washing is finished until the pH value of the filtrate is 6-8, preferably 6-7. The pH measurement of the solution may be performed using pH paper or a pH meter, and the measurement method is well known to those skilled in the art.

In the step (4), the drying treatment of the molecular sieve is not particularly limited, and may be carried out, for example, by drying at 120 ℃ for 6 hours in accordance with a conventional method.

In the present invention, the mother liquid after crystallization can be prepared according to the conventional method in the art, for example, when the ten-membered ring molecular sieve is ZSM-22 molecular sieve, the mother liquid after crystallization can be prepared according to the method disclosed in the document O.Murazaet, Microporous and Mesoporous Materials 206(2015) 136-143. When the ten-membered ring molecular sieve is ZSM-48, the mother liquor after crystallization can be prepared according to the reference P.Me' riaudeau et al/journal of Catalysis,1999(185), 435-444, or U.S. Pat. No. 6,596,1951. In one embodiment, the process for preparing the crystallized mother liquor comprises: preparing silicon-containing solution, aluminum-containing solution and alkaline liquid, mixing the above-mentioned liquids, making colloid, then making crystallization at a certain temperature.

In the combined catalyst of the present invention, the arrangement of the first catalyst and the second catalyst is not particularly limited. The reactor filled with the first catalyst is located upstream or downstream of the reactor filled with the second catalyst, according to the flow direction of the reaction mass. Specifically, the first catalyst may be disposed in a first reactor and the second catalyst may be disposed in a second reactor along a flow direction of the reaction material, such that the reaction material is contacted with the first catalyst for reaction and then contacted with the second catalyst for reaction; alternatively, the second catalyst may be disposed in a first reactor, and the first catalyst may be disposed in a second reactor, such that the reaction material first contacts and reacts with the second catalyst and then contacts and reacts with the first catalyst; or the first catalyst and the second catalyst are arranged in a staggered way, so that the reaction materials are sequentially and alternately in contact reaction with the first catalyst and the second catalyst.

In the combined catalyst of the present invention, the loading weight ratio of the first catalyst to the second catalyst is preferably 1: 0.1 to 10, more preferably 1: 1-2.5, more preferably 1: 1-2.

In the present invention, the weight ratio of the first catalyst to the second catalyst means the weight ratio of the first catalyst distributed in all the reactor catalyst beds to the second catalyst distributed in all the reactor catalyst beds.

In the composite catalyst of the present invention, the ten-membered ring molecular sieve is not particularly limited in type, and may be, for example, at least one of a ZSM-22 molecular sieve, a ZSM-23 molecular sieve, a ZSM-48 molecular sieve, a ZSM-5 molecular sieve, an SSZ-32 molecular sieve and an Eu-1 molecular sieve. Preferably, the ten-membered ring molecular sieve is a ZSM-22 molecular sieve and/or a ZSM-48 molecular sieve.

In the combined catalyst of the present invention, in order to further improve the isomerization pour point depressing effect of the combined catalyst, the difference between the silica/alumina molar ratio of the ten-membered ring molecular sieve M1 and the silica/alumina molar ratio of the ten-membered ring molecular sieve M2 is preferably 5 to 60, and specifically may be, for example, 5, 10, 15, 20, 25, 30, 35, 40, 45, 50, 55, 60 or any value in the range of any two of these values. More preferably, the difference is 20-40.

In the combined catalyst of the present invention, the first catalyst may be a supported catalyst, and the preparation process may include: the ten-membered ring molecular sieve M1 is mixed with a refractory inorganic oxide, formed, and then loaded with an active metal component, for example, by impregnation, followed by activation and reduction.

In the combined catalyst of the present invention, the second catalyst may be a supported catalyst, and the preparation process may include: the ten-membered ring molecular sieve M2 is mixed with a refractory inorganic oxide, formed, and then loaded with an active metal component, for example, by impregnation, followed by activation and reduction.

In the present invention, the heat-resistant inorganic oxide is preferably alumina.

In the present invention, the first catalyst and the second catalyst optionally contain an active metal component, which may be a group VIII metal component. Group VIII metals such as Ru, Os, Rh, Ir, Pd and Pt. Preferably, the group VIII metal is selected from Pd and/or Pt.

In the present invention, the content of the molecular sieve (ten-membered ring molecular sieve M1 or ten-membered ring molecular sieve M2) in the first catalyst and the second catalyst may be 20 to 80% by weight, preferably 25 to 55% by weight, based on the total weight of the catalysts; the refractory inorganic oxide (e.g., alumina) may be present in an amount of 35 to 80 wt.%, preferably 42 to 72 wt.%; the content of the active metal component may be 0.1 to 5% by weight, preferably 0.2 to 3% by weight, more preferably 0.4 to 1% by weight.

The method for producing the lubricating oil base oil by using the Fischer-Tropsch wax comprises the step of injecting the Fischer-Tropsch wax into a reaction device for hydrotreating, wherein the catalyst filled in the reaction device is the combined catalyst provided by the invention, and the reaction device at least comprises two reactors.

In the present invention, the Fischer-Tropsch wax may typically have a distillation range of 200 ℃ to 800 ℃ (measured at atmospheric pressure using a simulated distillation method).

In the process according to the invention, the hydrotreatment is not particularly limited as long as it is sufficient to hydroisomerize the fischer-tropsch wax. Generally, the reaction conditions may include: the temperature is 200-500 ℃, preferably 250-400 ℃, and more preferably 300-350 ℃; a pressure of 1 to 30MPa, preferably 2 to 20MPa, more preferably 5 to 20MPa, the pressure referred to herein being an absolute pressure; the volume space velocity is 0.1-5h^-1Preferably 0.1 to 3h^-1More preferably 0.5 to 2 hours^-1(ii) a The volume ratio of the hydrogen to the oil is 50-3000, preferably 300-3000, more preferably 400-600. The first catalyst and the second catalyst are respectively filled in different reactors, and the reaction conditions of the different reactors can be adjusted according to the factors such as catalyst activity and the like to optimize the reaction effect, namely the hydrotreating conditions of the different reactors can be the same or different.

Contacting a fischer-tropsch wax with a combined catalyst according to the invention according to the process of the invention enables higher yields of isomerised products to be obtained; and the isomerized product has a lower pour point while having a higher viscosity index, and is suitable for being used as lubricating oil base oil.

The present invention will be described in detail with reference to examples, but the scope of the present invention is not limited thereto.

In the following examples and comparative examples, the content of each element in the measurement sample was analyzed and measured by a 3271E type X-ray fluorescence spectrometer commercially available from Nippon chemical and electric machines industries, and the sample was baked at 600 ℃ for 3 hours before the measurement.

In the following examples and comparative examples, the specific surface area, the external surface area and the nitrogen adsorption-desorption curve of a sample were measured by using an automatic adsorption apparatus model DIGISORB 2500 of Micromeritics, USA, and the sample was baked at 600 ℃ for 3 hours before the test, and the measurement method was performed according to the ASTM D4222-98 standard method.

In the following examples and comparative examples, dry basis means the percentage of the weight of the product obtained after calcination of a certain amount of material in a muffle furnace at 600 ℃ for 4 hours in an air atmosphere, to the weight of the material before calcination. I.e. dry basis (weight of product obtained after calcination ÷ weight of material before calcination) × 100%.

Preparation example 1

(1) Preparation of crystallized mother liquor

36.3 g of a 40% by weight SiO solution were taken₂1.77 g of analytically pure Al₂(SO₄)₃·18H₂O, 3.94 g of analytically pure KOH and 8.44 g of hexamethylenediamine are used. Mixing hexamethylenediamine with silica sol, adding KOH and Al₂(SO₄)₃·18H₂O and 89.4 g of deionized water, then mixing the two solutions, stirring for 1 hour, transferring the mixture into a reaction kettle, and crystallizing for 72 hours at 160 ℃.

(2) Preparation of the Filter cake

Filtering the crystallized mother liquor prepared in the step (1), and continuing to pump and filter for 5 minutes when no filtrate exists on a filter cake to obtain a filter cake F-1, wherein the dry content of the filter cake F-1 is 11.2 wt%, and the molar ratio of silicon oxide to aluminum oxide is 60.

(3) Preparation of molecular Sieve precursors

The filter cake F-1 was warmed from room temperature to 450 ℃ at a temperature rise rate of 25 ℃ per minute and held at that temperature for 4 hours. And in the temperature rising process, the roasting furnace is a closed roasting furnace, and the molecular sieve precursor C-1 is obtained.

(4) Preparation of molecular sieve finished product

Putting the molecular sieve precursor C-1 into a HCl solution with the concentration of 1M for closed hydrothermal treatment. Wherein, the liquid-solid volume ratio is 50, the temperature of the hydrothermal treatment is 180 ℃, the time of the hydrothermal treatment is 3 hours, after the hydrothermal treatment is finished, the product is filtered and washed until the pH value of the filtrate is 7, and after the filtrate is dried for 4 hours at 120 ℃, the product is roasted for 4 hours at 550 ℃, and the finished product H-1 of the ZSM-22 molecular sieve is obtained. As can be seen from the nitrogen adsorption-desorption curve (measured by the BET method) of the molecular sieve, the ZSM-22 molecular sieve shows a closed hysteresis loop at a low-temperature nitrogen adsorption-desorption curve P/P0 of 0.4 to 0.99, and the start position of the closed hysteresis loop is at a P/P0 of 0.4 to 0.5.

(5) Preparation of the catalyst

40g (dry basis) of molecular sieve H-1 was ground to 120 mesh and then mixed with 60g (dry basis) of alumina, shaped, calcined at 560 ℃ and loaded with 0.17 wt% of metallic Pt and 0.38 wt% of metallic Pd. Activating for 3h at 400 ℃, and reducing for 3h at 400 ℃ to prepare the catalyst, which is named as Cat-1.

Preparation of comparative example 1

A ZSM-22 molecular sieve and a catalyst were prepared according to the method of preparation example 1, except that, in the step (2), when there was no filtrate on the filter cake, the suction filtration was continued for 50 minutes to obtain a filter cake DF-1, the dry content of which filter cake DF-1 was 46.5% by weight. To prepare a ZSM-22 molecular sieve finished product DH-1 and a catalyst D-Cat-1.

Preparation of comparative example 2

The mother liquor after crystallization was prepared according to procedure (1) of preparation example 1, followed by filtration, and the filter cake obtained after filtration was dried at 120 ℃ for 6 hours and then calcined at 550 ℃ for 4 hours to obtain a solid product and NH₄Exchanging Cl for 3 times, and drying to form the ammonium molecular sieve finished product DH-2. Then, catalyst D-Cat-2 was prepared using molecular sieve DH-2 and following the procedure of preparation example 1.

Preparation example 2

(1) Preparation of crystallized mother liquor

45 g of white carbon black and 1.25 g of analytically pure Al are taken₂(SO₄)₃·18H₂O, 1.88 g of analytically pure NaOH and 39.3 g of hexamethylenediamine are used. Mixing hexanediamine, white carbon black and 200g of deionized water, and adding NaOH and Al₂(SO₄)₃·18H₂O and 272 g of deionized water, then mixing the two solutions, stirring for 1 hour, moving into a reaction kettle,crystallizing at 160 deg.C for 72 hr.

(2) Preparation of the Filter cake

Filtering the crystallized mother liquor prepared in the step (1), and continuing to pump and filter for 5 minutes when no filtrate exists on a filter cake to obtain a filter cake F-2, wherein the dry content of the filter cake F-2 is 11.2 weight percent, and the molar ratio of silicon oxide to aluminum oxide is 60.

(3) Preparation of molecular Sieve precursors

The filter cake F-2 was warmed from room temperature to 450 ℃ at a temperature rise rate of 25 ℃/min and held at that temperature for 4 hours. And in the temperature rising process, the roasting furnace is a closed roasting furnace, and the molecular sieve precursor C-2 is obtained.

(4) Preparation of molecular sieve finished product

And putting the molecular sieve precursor C-2 into a citric acid solution with the concentration of 1M for closed hydrothermal treatment. Wherein, the liquid-solid volume ratio is 100, the temperature of the hydrothermal treatment is 180 ℃, the time of the hydrothermal treatment is 2 hours, after the hydrothermal treatment is finished, the product is filtered and washed until the pH value of the filtrate is 7, and after the filtrate is dried for 4 hours at 120 ℃, the product is roasted for 4 hours at 550 ℃, and the finished product H-2 of the ZSM-48 molecular sieve is obtained. As can be seen from the nitrogen adsorption-desorption curve (measured by the BET method) of the molecular sieve, the ZSM-48 molecular sieve shows a closed hysteresis loop at a low-temperature nitrogen adsorption-desorption curve P/P0 of 0.4 to 0.99, and the start position of the closed hysteresis loop is at a P/P0 of 0.4 to 0.5.

(5) Preparation of the catalyst

40g (dry basis) of molecular sieve H-2 was ground to 120 mesh and then mixed with 60g (dry basis) of alumina, shaped, calcined at 560 ℃ and loaded with 0.4 wt% of metallic Pt. Activating for 3h at 400 ℃, and reducing for 3h at 400 ℃ to prepare the catalyst, which is named as Cat-2.

Test example 1

(1) The mesoporous area and the specific surface area (measured by the BET method) of the molecular sieve products prepared in the above preparation examples and preparation comparative examples were measured by using an automatic adsorption apparatus model DIGISORB 2500, Micromeritics, usa, and the ratio of the mesoporous area to the specific surface area was calculated, and the results are shown in table 1 below.

(2) The contents of the respective elements in the molecular sieve precursors and the molecular sieve finished products prepared in the above preparation examples and preparation comparative examples were analyzed and measured by a 3271E type X-ray fluorescence spectrometer commercially available from japan physical and electrical machinery industries, and the silicon-aluminum ratio and the content of penta-coordinated aluminum were determined, and the results are shown in table 1 below.

Example 1

As shown in FIG. 1, 50g of catalyst Cat-1 and 150g of catalyst Cat-2 were placed in a first reactor 1 and a second reactor 2 of a high-pressure hydrogenation reaction apparatus, respectively. Fischer-Tropsch wax (parameters shown in Table 2) was charged into the reactor from top to bottom to carry out the reaction under 2 conditions shown in Table 3 below. After the reaction is finished, the product is distilled to cut off light components at the temperature of less than 370 ℃. Pour point, viscosity index analysis and yield calculations were performed on the components above 370 c and the results are shown in table 4. The yield is defined as: yield-weight of components in product greater than 370 ℃ per weight of feed.

Comparative example 1

A lubricant base oil was produced using Fischer-Tropsch wax according to the method of example 1, except that the first reactor and the second reactor of the high-pressure hydrogenation reaction apparatus were filled with the corresponding amounts by weight of catalyst D-Cat-1 and catalyst D-Cat-2, respectively.

Comparative example 2

A lubricant base stock was produced using Fischer-Tropsch wax according to the method of example 1, except that the high pressure hydrogenation unit was charged with only 200g of catalyst D-Cat-1.

Comparative example 3

A lubricant base stock was produced using Fischer-Tropsch wax according to the method of example 1, except that the high pressure hydrogenation unit was charged with only 200g of catalyst D-Cat-2.

Example 2

A lubricant base oil was produced using Fischer-Tropsch wax according to the method of example 1, except that the first reactor of the high-pressure hydrogenation reaction apparatus was charged with a corresponding weight of catalyst D-Cat-1 in place of the catalyst Cat-1.

Example 3

A lubricant base oil was produced using Fischer-Tropsch wax according to the method of example 1, except that the second reactor of the high-pressure hydrogenation reactor was charged with a corresponding weight of catalyst D-Cat-2 instead of catalyst Cat-2.

Example 4

A lubricant base oil was produced using Fischer-Tropsch wax according to the method of example 1, except that 100g of catalyst Cat-1 and 100g of catalyst Cat-2 were installed in the first reactor and the second reactor of the high-pressure hydrogenation reaction apparatus, respectively.

Example 5

A lubricant base oil was produced using Fischer-Tropsch wax according to the method of example 1, except that 150g of catalyst Cat-1 and 50g of catalyst Cat-2 were charged in the first reactor and the second reactor of the high-pressure hydrogenation reaction apparatus, respectively.

Example 6

A lubricant base oil was produced using Fischer-Tropsch wax according to the method of example 1, except that 180g of catalyst Cat-1 and 20g of catalyst Cat-2 were charged in the first reactor and the second reactor of the high-pressure hydrogenation reaction apparatus, respectively.

Example 7

A lubricant base oil was produced using Fischer-Tropsch wax according to the method of example 1, except that 20g of catalyst Cat-1 and 180g of catalyst Cat-2 were installed in the first reactor and the second reactor of the high-pressure hydrogenation reaction apparatus, respectively.

As can be seen from the data in Table 4, the Fischer-Tropsch wax process of producing lube base oil of the present invention provides good pour point depressing effect, and the lube base oil has high yield, low pour point and high viscosity index.

The preferred embodiments of the present invention have been described in detail, however, the present invention is not limited to the specific details of the above embodiments, and various simple modifications may be made to the technical solution of the present invention within the technical idea of the present invention, and these simple modifications are within the protective scope of the present invention.

It should be noted that the various technical features described in the above embodiments can be combined in any suitable manner without contradiction, and the invention is not described in any way for the possible combinations in order to avoid unnecessary repetition.

In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the content of the present invention as long as it does not depart from the gist of the present invention.

TABLE 1

TABLE 2

Analysis item	Analyzing data	Analytical method
			Density/(kg/m) at 20 DEG C³)	809.6	SH/T 0604-2000
Viscosity index	145	GB/T 1995-1998
			Pour point/. degree.C	+78.5	SH/T 0771-2005
Mass fraction of nitrogen/(μ g/g)	5.2	NB/SH/T 0704-2010
			Sulfur mass fraction/(μ g/g)	2.6	SH/T 0842-2010
Distillation range/. degree.C		ASTM D-1160
			Initial boiling point	222
5％	286
			10％	315
30％	381
			50％	425
70％	477
			90％	535
Dried cake	571

TABLE 3

Reaction conditions	Condition	1	Condition 2
				Pressure, MPa	12.0	12.0
Volumetric space velocity h^-1	1.0	1.0
			Reaction temperature of	320	330
Hydrogen to oil ratio, v/v	500	500

TABLE 4

Claims

1. A process for producing a lubricant base oil from fischer-tropsch wax, the process comprising: the Fischer-Tropsch wax is injected into a reaction device for hydrotreating, and the catalyst loaded in the reaction device contains a combined catalyst, the combined catalyst comprises a first catalyst and a second catalyst, the first catalyst contains a ten-membered ring molecular sieve M1, the second catalyst contains a ten-membered ring molecular sieve M2, the first catalyst and the second catalyst respectively and independently contain an active metal component, and the first catalyst and the second catalyst are respectively loaded in different reactors of the reaction device;

2. The process as claimed in claim 1, wherein the molecular sieve has a silica/alumina molar ratio of 150-200 in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2.

3. The method of claim 1, wherein the mesopore area of the molecular sieve in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 is 50M²/g-250m²The proportion of the mesoporous area in the specific surface area is 20-70%, preferably 25-65%.

4. The process of claim 1, wherein the closed hysteresis loop in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 has a starting position at P/P0 of 0.4-0.6.

5. The process of claim 1 wherein the penta-coordinated aluminum content of the precursor to molecular sieve in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 is from 4 to 30% by weight, preferably from 10 to 30% by weight, calculated as oxide and based on the total alumina content of the molecular sieve.

6. The process of claim 1 wherein the amount of penta-coordinated aluminum in the finished molecular sieve is 3 wt.% or less, preferably 1 wt.% or less, more preferably no penta-coordinated aluminum, calculated as oxide and based on total alumina amount of molecular sieve in the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2.

7. The process of any one of claims 1-6, wherein the ten-membered ring molecular sieve M1 and/or the ten-membered ring molecular sieve M2 is prepared according to the following steps:

(2) directly roasting the filter cake to obtain a molecular sieve precursor;

(3) subjecting the molecular sieve precursor to a hydrothermal treatment;

(4) and filtering, washing and drying the hydrothermal treatment product.

8. The process of claim 7, wherein in step (1), the filtration forms a filter cake having a dry content of 6-15% on a dry basis.

9. The method as claimed in claim 7, wherein, in step (2), the temperature of the roasting is 400-600 ℃, preferably 450-550 ℃.

10. The process according to claim 7, wherein, in step (3), the hydrothermally treated medium is acidic water;

11. The process according to claim 7, wherein in step (3), the liquid-solid volume ratio of the hydrothermal treatment is 5-200, preferably 20-100; the temperature of the hydrothermal treatment is 100-300 ℃, and preferably 100-200 ℃; the time of the hydrothermal treatment is 0.5 to 24 hours, preferably 1 to 12 hours, and more preferably 1 to 4 hours;

12. The method according to claim 7, wherein in step (4), the washing is performed by washing with deionized water until the filtrate has a pH value of 6-8, preferably 6-7.

13. The process of claim 1 wherein the reactor charged with the first catalyst is located upstream or downstream of the reactor charged with the second catalyst, in terms of the reactant stream direction.

14. The process of claim 1, wherein the ten-membered ring molecular sieve M1 and ten-membered ring molecular sieve M2 are each independently selected from at least one of ZSM-22 molecular sieve, ZSM-23 molecular sieve, ZSM-48 molecular sieve, ZSM-5 molecular sieve, SSZ-32 molecular sieve, and Eu-1 molecular sieve.

15. The process of claim 1, wherein the loading weight ratio of the first catalyst to the second catalyst is 1: 0.1 to 10;

the active metal component is Pt and/or Pd;

16. The process as claimed in claim 1, wherein the Fischer-Tropsch wax has a distillation range of 200-800 ℃;