CN114471677B - Hydroisomerization catalyst and carrier thereof - Google Patents

Hydroisomerization catalyst and carrier thereof Download PDF

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Publication number
CN114471677B
CN114471677B CN202011257233.1A CN202011257233A CN114471677B CN 114471677 B CN114471677 B CN 114471677B CN 202011257233 A CN202011257233 A CN 202011257233A CN 114471677 B CN114471677 B CN 114471677B
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acid
molecular sieve
hydroisomerization catalyst
modification
modified molecular
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CN114471677A (en
Inventor
杨晓东
陆雪峰
张国甲
倪术荣
董春明
王新苗
高善彬
孙生波
徐伟池
方磊
赵檀
姜维
郭立艳
韩志波
姜丽丽
马东海
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Petrochina Co Ltd
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Petrochina Co Ltd
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    • C10M2203/1025—Aliphatic fractions used as base material

Abstract

The invention discloses a hydroisomerization catalyst carrier, which is prepared by mixing a modified molecular sieve and an amorphous inorganic porous material and then carrying out secondary modification, wherein the modification comprises metal and/or acid modification, the mass ratio of the modified molecular sieve to the inorganic porous material is 2:3-5:1, the modified molecular sieve is prepared by modifying, drying and roasting a raw material molecular sieve containing a ten-membered ring structure by metal and/or acid, wherein the modified molecular sieve is characterized by pyridine infrared, the acid content of B is 0.2-0.6 mmol/g at 150 ℃, and the acid content of B is: l acid = 6:1 to 1:1, a step of; the content of B acid is 0.05-0.4 mmol/g at 350 ℃, and B acid: l acid = 6:1 to 1:1, wherein the total acid amount at 150 ℃ is >350 ℃. The invention also discloses a hydroisomerization catalyst. The catalyst is used for solving the problem of high cloud point in the existing lubricating oil base oil production process.

Description

Hydroisomerization catalyst and carrier thereof
Technical Field
The invention relates to the field of hydroisomerization catalysts, in particular to a hydroisomerization catalyst and a carrier thereof, which are suitable for producing lubricating oil base oil.
Background
At present, the lubricating oil base oil processing technology has a traditional old three-set production process, the process can only generally produce I base oil, and the process technology can not meet the development requirement of the existing high-quality base oil; the catalytic dewaxing technology is proposed in the 70 th century, mainly utilizes the shape-selective function of the catalyst to selectively crack straight-chain normal paraffins and hydrocarbons with long chain length into small molecular hydrocarbons, wax molecules are selectively cracked and removed on the catalyst to achieve the purpose of reducing the pour point of base oil, but the cloud point reducing effect on the base oil is not obvious, and simultaneously the selective cracking of the wax molecules by the technology can lead to the reduction of the yield and viscosity index of the base oil, and the viscosity index is generally lower than that of the solvent dewaxing; the isomerization dewaxing technology is proposed by Chevron company in the 90 th century, and the base oil produced by the technology has high viscosity index, low pour point and high yield, and is considered as the most promising base oil production technology of II and III types. The paraffin-based distillate oil is used as an ideal raw material for producing the high-viscosity index lubricating oil base oil, the problem of high cloud point usually occurs in the process of processing the lubricating oil base oil by adopting an isomerization dewaxing base, the cloud point is generally above 0 ℃, and even reaches 10-20 ℃, floccules are formed in the base oil when clouding occurs, wax molecules in the base oil are separated out and intertwined at the cloud point temperature, the appearance of the base oil is affected by the occurrence of the cloud point problem, and meanwhile, a filter or a pipeline for oil transportation can be blocked when the base oil is used.
In order to reduce the cloud point of the base oil, researchers have sought to reduce the cloud point of the base oil using different methods. As described in US6468417 and US6468418, the base oils are treated in specific vessels with acid clay or alumina as adsorbent, but with limited reduction in cloud point; US7674363 describes the use of an isodewaxing process followed by solvent dewaxing of a fischer-tropsch synthetic oil, which is relatively effective in reducing the pour point of the base oil, but which still contains more than 30% of the base oil wax after treatment at-20 ℃ and therefore does not effectively reduce the cloud point of the base oil; CN1524929a discloses a method for reducing cloud point of lubricating base oil, which comprises the steps of dewaxing a lubricating oil raw material by a solvent, then carrying out hydrotreatment, and then carrying out isodewaxing to produce base oil with pour point of-24 to-27, wherein the base oil has good low-temperature flow property, but the cloud point of the base oil can only reach-1, and the use requirement of the cloud point of not more than-5 ℃ can not be met.
Disclosure of Invention
The invention provides a hydroisomerization carrier, which is used for reducing the cloud point of lubricating oil base oil to solve the problem of high cloud point in the existing lubricating oil base oil production process, has high macromolecular conversion capability on lubricating oil base oil, and can effectively isomerize wax molecules so as to reduce the cloud point of the base oil, and the cloud point of the produced base oil is not more than-5 ℃.
In order to solve the technical problems, the invention provides a hydroisomerization catalyst carrier, which is prepared by mixing a modified molecular sieve and an amorphous inorganic porous material and then carrying out secondary modification, wherein the modification comprises metal and/or acid modification, the mass ratio of the modified molecular sieve to the inorganic porous material is 2:3-5:1, the modified molecular sieve is prepared by modifying a raw material molecular sieve containing a ten-membered ring structure by metal and/or acid, drying and roasting,
Wherein the modified molecular sieve is characterized by pyridine infrared, the content of B acid is 0.1-0.6 mmol/g at 150 ℃, and the B acid is as follows: l acid = 6:1 to 1:1, a step of; the content of B acid is 0.05-0.4 mmol/g at 350 ℃, and B acid: l acid = 6:1 to 1:1, wherein the total acid amount at 150 ℃ is >350 ℃.
The hydroisomerization catalyst carrier according to the present invention, wherein preferably the feedstock molecular sieve is selected from at least one of ZSM-5, SAPO-11, EU-1, ITQ-13, ZSM-22, MCM-22, NU-87, ZSM-23, ZSM-35 and ZSM-48.
The hydroisomerization catalyst carrier according to the present invention, wherein preferably the feedstock molecular sieve has a straight-through pore structure.
The hydroisomerization catalyst carrier according to the present invention is preferably one in which the molar ratio of Si/Al 2O3 of the raw material molecular sieve is 30 to 120 and the average particle diameter is 50 to 100nm.
The hydroisomerization catalyst carrier according to the present invention, wherein preferably the metal is selected from one or more of group IA, IIA, IIIA, IB and group IIB metals.
The hydroisomerization catalyst carrier according to the present invention, wherein preferably the metal is selected from one or more of potassium, magnesium, calcium, strontium, barium, copper, zinc, gallium and tin.
The hydroisomerization catalyst carrier according to the present invention, wherein preferably the acid is one or more selected from the group consisting of nitric acid, phosphoric acid, acetic acid, tartaric acid and citric acid.
The hydroisomerization catalyst carrier according to the present invention, wherein preferably the modification is: preparing the metal into a metal salt solution with the concentration of 0.1-0.5 mol/L, or preparing the acid into an acid solution with the concentration of 0.1-0.5 mol/L, and then immersing the raw material molecular sieve into the metal salt solution or the acid solution.
The hydroisomerization catalyst carrier according to the present invention, wherein preferably the amorphous inorganic porous material is selected from one or more of Al2O3、SiO2、Al2O3-SiO2、TiO2、Al2O3-TiO2、ZrO2 and Al 2O3-ZrO2.
The invention also provides a hydroisomerization catalyst, which takes the hydroisomerization catalyst carrier as a carrier and noble metal as an active component, wherein the active component accounts for 0.3-1.0% of the total mass of the hydroisomerization catalyst.
The hydroisomerization catalyst according to the present invention, wherein preferably the noble metal is selected from one or both of Pt, pd, ru, rh, re and Ir compounds.
The invention has the following beneficial effects:
the hydroisomerization catalyst carrier provided by the invention and the hydroisomerization catalyst comprising the carrier. The hydroisomerization catalyst is suitable for producing low-cloud-point lubricating oil base oil from high-condensation-point waxy oil by an isomerization dewaxing technical method. The hydroisomerization catalyst has stronger aromatic hydrocarbon saturation and excellent hydroisomerization performance, can effectively reduce the condensation point and pour point of base oil, has better cloud point performance of base oil products, has lower temperature, and particularly has higher production viscosity and viscosity index, less viscosity index loss and high yield of the base oil.
Detailed Description
The following describes embodiments of the present invention in detail: the present example is implemented on the premise of the technical scheme of the present invention, and detailed implementation modes and processes are given, but the protection scope of the present invention is not limited to the following examples, and experimental methods without specific conditions are not noted in the following examples, and generally according to conventional conditions.
Preparation of modified molecular sieves
The examples below, ZSM-5, SAPO-11, EU-1, ITQ-13, ZSM-22, MCM-22, NU-87, ZSM-23, ZSM-35 and ZSM-48 for the molecular sieves of the raw materials were commercially available industrial application molecular sieves, the Si/Al 2O3 molar ratio was 0.5 to 120, and the average grain size was 50 to 100nm. The raw material molecular sieve is modified by alkali metal solution and/or acid solution, wherein the alkali metal is selected from one or more of IA, IIA, IIIA, IB or IIB group metals, and the alkali metal is preferably one or more of potassium, magnesium, calcium, strontium, barium, copper, zinc, gallium and tin.
The modifying process is to dip IA, IIA, IIIA, IB or IIB metal salt solution or the acid solution concentration controlled to 0.1-0.5 mol/L onto molecular sieve, wherein the acid is one or more selected from nitric acid, phosphoric acid, acetic acid, tartaric acid and citric acid, the modified molecular sieve-containing carrier is dried and baked at 550 ℃ for pyridine infrared (Py-IR) adsorption-desorption characterization and catalyst preparation, wherein 100g of molecular sieve raw powder is taken as an example for illustration in table 1.
Example 1-1
The molecular sieve ZSM-5 of the raw material has a Si/Al 2O3 molar ratio of 53 and an average grain size of 87nm. 100g of raw material molecular sieve ZSM-5 is immersed in 70ml of 0.3mol/LCu (NO 3)2 solution for modification, after 12 hours, the modified molecular sieve ZSM-5 is dried (110 ℃ C., 10 hours), and baked at 550 ℃ C. For 8 hours, thus obtaining modified molecular sieve ZSM-5, which is denoted as A1.
The properties and the modifying reagent of the raw material molecular sieve are shown in table 1, a sample prepared by the modified molecular sieve is subjected to vacuumizing pretreatment in a pyridine sample cell, adsorption saturation is carried out in the pyridine sample cell in an ice bath at 0 ℃, pyridine desorption characterization is carried out at 150 ℃ and 350 ℃, the amounts of B acid and L acid of the sample are calculated, and the characterization results are shown in table 2.
Examples 1 to 2
The difference from example 1-1 is shown in Table 1, and the pyridine desorption characterization results of the modified molecular sieve B1 at 150℃and 350℃are shown in Table 2.
Examples 1 to 3
The difference from example 1-1 is shown in Table 1, and the pyridine desorption characterization results of the modified molecular sieve C1 at 150℃and 350℃are shown in Table 2.
Examples 1 to 4
The difference from example 1-1 is shown in Table 1, and the pyridine desorption characterization results of the modified molecular sieve D1 at 150℃and 350℃are shown in Table 2.
Examples 1 to 5
The difference from example 1-1 is shown in Table 1, and the pyridine desorption characterization results of the modified molecular sieve E1 at 150℃and 350℃are shown in Table 2.
Examples 1 to 6
The difference from example 1-1 is shown in Table 1, and the pyridine desorption characterization results of the modified molecular sieve F1 at 150℃and 350℃are shown in Table 2.
Examples 1 to 7
The difference from example 1-1 is shown in Table 1, and the pyridine desorption characterization results of the modified molecular sieve G1 at 150℃and 350℃are shown in Table 2.
Examples 1 to 8
The difference from example 1-1 is shown in Table 1, and the pyridine desorption characterization results of the modified molecular sieve H1 at 150℃and 350℃are shown in Table 2.
Examples 1 to 9
The difference from example 1-1 is shown in Table 1, and the pyridine desorption characterization results of the modified molecular sieve I1 at 150℃and 350℃are shown in Table 2.
Examples 1 to 10
The difference from example 1-1 is shown in Table 1, and the pyridine desorption characterization results of the modified molecular sieve J1 at 150℃and 350℃are shown in Table 2.
TABLE 1 molecular sieve Properties and modifying Agents
TABLE 2 Py-IR characterization results for molecular sieves
Example 2
The modified ZSM-5 molecular sieve A1 prepared in example 1-1 was weighed 70g (dry basis weight), kneaded with 40g of alumina powder, extruded into a bar-shaped carrier, dried at 200℃for 5 hours in wet bars, modified with 80ml of 0.1mol/L Mg (NO 3)2 alkali metal solution, dried at 100℃for 10 hours and calcined at 550℃for 12 hours to prepare a catalyst carrier.
The catalyst was prepared by an isovolumetric impregnation method. The solution containing PtCl 2 and PdCl 2 was impregnated on a catalyst carrier, and the wet strip was dried at 120℃for 10 hours and calcined at 550℃for 12 hours to prepare a catalyst A having Pt and Pd contents of 0.3wt% and 0.2wt%, respectively (based on the mass of the catalyst).
Example 3
The difference from the example 2 is that: the modified SAPO-11B1 prepared in example 1-2 was used, the modified alkali metal solution was 0.2mol/L ZnCl 2 solution of the same volume, and the rest was the same, to prepare catalyst B.
Example 4
The difference from the example 2 is that: catalyst C was prepared using the modified EU-1C1 prepared in examples 1-3, using the same volume of 0.3mol/L SnCl 2 solution as the modifying solution, and the remainder being the same.
Example 5
The difference from the example 2 is that: catalyst D was prepared using the modified ITQ-13D1 prepared in examples 1-4, and the same volume of the mixed solution of 0.1mol/L Ga (NO 3) 3 and 0.5mol/L citric acid as the modified solution, and the remainder was the same.
Example 6
The difference from the example 2 is that: the modified ZSM-22E1 prepared in examples 1-5 was used, and the modified solution was prepared as catalyst E using the same volume of a mixed solution containing 0.5mol/L ZnCl 2 and 0.2mol/L acetic acid, and the remainder was the same.
Example 7
The difference from the example 2 is that: the modified MCM-22F1 prepared in examples 1-6 was used, and the modified solution was prepared as catalyst F using the same volume of a mixed solution containing 0.3mol/L Ba (NO 3)2 and 0.1mol/L nitric acid), the remainder being the same.
Example 8
The difference from the example 2 is that: catalyst G was prepared using the modified NU-87G1 prepared in examples 1-7, using the same volume of a mixed solution containing 0.3mol/L Ba (NO 3)2 and 0.1mol/L nitric acid), and the remainder was the same.
Example 9
The difference from the example 2 is that: the modified ZSM-23H1 prepared in examples 1-8 was used, and the modified solution was the same volume of a mixed solution containing 0.5mol/L CuCl 2 and 0.2mol/L phosphoric acid, and the rest was the same, to prepare catalyst H.
Example 10
The difference from the example 2 is that: the modified ZSM-35I1 prepared in examples 1-9 was used, and the modified solution was prepared as catalyst I using the same volume of a mixed solution containing 0.2mol/L MgCl 2 and 0.3mol/L tartaric acid, and the remainder was the same.
Example 11
The difference from the example 2 is that: the modified ZSM-48J1 prepared in examples 1-10 was used, and the modified solution was prepared as catalyst J using the same volume of a mixed solution containing 0.3mol/L BaCl 2 and 0.4mol/L citric acid, the remainder being the same.
Example 12
Taking A and B as catalysts for example, carrying out real raw material hydrogenation evaluation reaction, wherein the reaction is carried out on a 100ml hydrogenation fixed bed, the B catalyst is filled in the upper part of a hydroisomerization reactor, the A catalyst is filled in the lower part, and the filling ratio of the two catalysts is 1:1 (by weight of catalyst) is designated B/A.
Example 13
The difference from the example 12 is that: taking E and H as catalysts for example, the E catalyst is filled in the upper part of the hydroisomerization reactor, and the H catalyst is filled in the lower part, which is denoted as E/H.
Example 14
The difference from the example 12 is that: taking C, D and G as catalysts as examples, a catalyst C is filled in the upper part of the hydroisomerization reactor, a catalyst D is filled in the middle part, a catalyst G is filled in the lower part, and the filling ratio of the three catalysts is 1:1:1 (by weight of catalyst) is designated C/D/G.
Example 15
The difference from the example 12 is that: taking F and I as catalysts for example, the F catalyst is filled in the upper part of the hydroisomerization reactor, and the I catalyst is filled in the lower part, which is denoted as F/I.
Example 16
The difference from the example 12 is that: taking H and J as catalysts for example, the H catalyst is filled in the upper part of the hydroisomerization reactor, and the I catalyst is filled in the lower part, which is denoted as H/J.
Example 17
The difference from the example 12 is that: taking L and K as catalysts for example, the K catalyst is filled in the upper part of the hydroisomerization reactor, and the L catalyst is filled in the lower part, which is denoted as K/L.
Comparative example 1
The difference from example 2 is that: the ZSM-5 of example 1 was used as a molded carrier without modification, and the catalyst carrier was prepared without modification with 0.1mol/L Mg (NO 3)2 alkali metal solution, then drying at 100℃for 10 hours and baking at 550℃for 12 hours, the other steps being the same, and the catalyst prepared was catalyst A-D1.
Comparative example 2
The difference from example 3 is that: the catalyst carrier is prepared by adopting the SAPO-11 which is not modified in the embodiment 1, not carrying out the modification step of 0.2mol/L ZnCl 2 solution, then drying at 100 ℃ for 10 hours and roasting at 550 ℃ for 12 hours, and the rest steps are the same, wherein the prepared catalyst is the catalyst B-D1.
Comparative example 3
The difference from example 12 is that: catalyst B was replaced with B-D1, catalyst A was replaced with catalyst A-D1, and the remainder were identical.
Example 18
The catalysts packed in examples 12 to 17 and comparative example 3 were subjected to hydrogenation evaluation using two reactors connected in series, one of which was an isomerization dewaxing reactor and the other of which was a supplemental refining reactor, and after hydroisomerization, the resulting oil was mixed with high purity hydrogen gas and fed into the supplemental refining reactor, and subjected to aromatic saturation reaction with the supplemental refining catalyst to give a product, which was fed into a fractionation system to give a lubricating oil base oil having a low cloud point, wherein the supplemental refining reactor was packed with commercial supplemental refining catalyst PHF-301, and the metal active components were noble metals Pt and Pd, and the carrier material was a silica alumina material.
The feedstock oil was evaluated as a hydrocracked tail oil, and the feedstock properties are shown in table 3.
TABLE 3 Properties of raw oil
Density (20 ℃), g/ml 0.8380
Distillation range
HK，℃ 352
50％，℃ 435
KK，℃ 584
Sulfur, μg/g 42
Nitrogen, μg/g 19
Pour point, C 29
Wax content, omega% 58
Aromatic hydrocarbon content, omega% 38.9
Condensation point, DEG C 49
The hydrogenation evaluation conditions are shown in Table 4. The results of the hydrogenation evaluation of the product properties after cutting at a true boiling point of more than 320 ℃ are shown in Table 5.
Table 4 hydrogenation evaluation conditions
Table 5 hydrogenation evaluation results
According to the embodiment of the invention, the hydroisomerization carrier prepared by the method is used for producing the lubricating oil base oil, and has the advantages of strong aromatic hydrocarbon saturation performance, good hydroisomerization performance, capability of effectively reducing the condensation point, pour point and cloud point of the base oil, better cloud point performance, high viscosity and viscosity index of the produced base oil, less viscosity and viscosity index loss and high base oil yield.
The hydroisomerization carrier prepared by the invention is suitable for treating one or more of decompressed wax oil, decompressed dewaxed oil, hydrocracking tail oil, deasphalted oil and coked wax oil, and is especially suitable for treating the wax oil with heavy high condensation point as a raw material to produce low-cloud point high-grade lubricating oil base oil.
Of course, the present invention is capable of other various embodiments and its several details are capable of modification and variation in light of the present invention by one skilled in the art without departing from the spirit and scope of the invention.

Claims (8)

1. A hydroisomerization catalyst carrier is characterized in that the catalyst carrier is prepared by mixing a modified molecular sieve and an amorphous inorganic porous material and then carrying out secondary modification, wherein the secondary modification comprises metal and/or acid modification, the mass ratio of the modified molecular sieve to the inorganic porous material is 2:3-5:1, the modified molecular sieve is prepared by modifying a raw material molecular sieve containing a ten-membered ring structure by metal and/or acid, drying and roasting,
Wherein the modified molecular sieve is characterized by pyridine infrared, the content of B acid is 0.1-0.6 mmol/g at 150 ℃, and the B acid is as follows: l acid = 6:1 to 1:1, a step of; the content of B acid is 0.05-0.4 mmol/g at 350 ℃, and B acid: l acid = 6:1 to 1:1, wherein the total acid amount at 150 ℃ is >350 ℃ total acid amount;
the modification of the modified molecular sieve is as follows: preparing the metal into a metal salt solution with the concentration of 0.1-0.5 mol/L, and/or preparing the acid into an acid solution with the concentration of 0.1-0.5 mol/L, and then immersing a raw material molecular sieve into the metal salt solution and/or the acid solution;
The metal in the modification process and the re-modification process of the modified molecular sieve is one or more selected from IA, IIA, IIIA, IB and IIB metals respectively;
The acid in the modification process and the re-modification process of the modified molecular sieve is one or more selected from nitric acid, phosphoric acid, acetic acid, tartaric acid and citric acid respectively.
2. The hydroisomerization catalyst carrier of claim 1, wherein the feedstock molecular sieve is selected from at least one of ZSM-5, SAPO-11, EU-1, ITQ-13, ZSM-22, MCM-22, NU-87, ZSM-23, ZSM-35 and ZSM-48.
3. The hydroisomerization catalyst carrier of claim 1, wherein the feedstock molecular sieve has a straight-through pore structure.
4. The hydroisomerization catalyst carrier according to claim 1, characterized in that the raw material molecular sieve has a Si/Al 2O3 molar ratio of 30 to 120 and an average particle diameter of 50 to 100nm.
5. Hydroisomerization catalyst support according to claim 1, characterized in that the metal during the modification of the modified molecular sieve and during the re-modification is selected from one or several of potassium, magnesium, calcium, strontium, barium, copper, zinc, gallium and tin, respectively.
6. The hydroisomerization catalyst carrier according to claim 1, wherein the amorphous inorganic porous material is selected from one or more of Al2O3、SiO2、Al2O3-SiO2、TiO2、Al2O3-TiO2、ZrO2 and Al 2O3-ZrO2.
7. A hydroisomerization catalyst, characterized in that the hydroisomerization catalyst uses the hydroisomerization catalyst carrier according to any one of claims 1 to 6 as a carrier and noble metal as an active component, and the active component accounts for 0.3 to 1.0% of the total mass of the hydroisomerization catalyst.
8. Hydroisomerization catalyst according to claim 7, characterized in that the noble metal is selected from one or both of Pt, pd, ru, rh and Ir compounds.
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