JPH07501310A - Dehydrocyclization of polyalphaolefin lubricants - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

[Detailed description of the invention] Dehydrogenation and cyclization technology for polyalphaolefin lubricated cutting The present invention provides aromatic structures useful as lubricant raw materials and lubricant additives. New polyalphaolefin (PAO) containing compositions, and means of their production. More particularly, the present invention provides high Vl and By dehydrocyclization of polyalphaolefin oligomers exhibiting A novel lubricant family with high viscosity index (VI) and increased thermal stability is produced. Regarding products.

Background technology Oligomeric hydrocarbons with improved performance over those of mineral oil-based lubricants Synthesis of elementary fluids has long been an important research and development challenge in the petroleum industry; and is mainly based on the oligomerization of alpha olefins or 1-alkenes.

A number of superior polyalphaolefin synthetic lubricants have been introduced to the market relatively recently. The progress of industrial research efforts into synthetic lubricants has shown that they are equal to or better than mineral oils. It exhibits good lubricity, thermal and oxidative stability, and pour point, and has a wide range of Useful dryness over temperatures of 100 to 100% is directed toward fluids that exhibit an improved viscosity index. child These new synthetic lubricants reduce friction and therefore have a wider range of applications than mineral oil lubricants. Increases mechanical efficiency over operating conditions.

Despite their generally superior properties, PAO lubricants are Additives or cases of additives are often used to increase these properties. Prescribed by Ji. The more commonly used additives are oxidation inhibitors and rust inhibitors. Metal-based delivery, anti-wear agents, (pressure-resistant additives, fluidity reducers, cleaning agents - dispersants, viscosity This park of lubricant technology, including VL improvers, foaming inhibitors, etc. ir-OtbmerrEncyclopedia of Chemical Especially described in Tect+nologyJ 3rd edition, volume 14, pages 477-526 has been done.

Lubricating oil additive packages are complex and expensive materials. Therefore, it is significantly superior The new lubricant is characterized by the properties imparted to lubricant mixtures by well-known additives. New lubricant molecules that successfully avoid or at least reduce the need for is specific to the structure of As a result, improvements in lubricant technology pursued by those skilled in the art. Benefits include the development of new additives that address shortcomings in lubricant oligomers, as well as Both the development of new oligomers with inherently good properties to replace additives arises from Increasing the aromaticity of lubricant mixtures improves thermal stability and wear resistance. known to improve. However, from the viewpoint of PAO lubricant paraffin properties, , aromatic additives to PAOs pose solubility problems that limit their usefulness. Often difficult or requires the use of expensive dispersants.

Alkylated aromatics are described in U.S. Pat. 91 and 47147944, their wear resistance, thermal and known to those skilled in the art as lubricant additives with respect to oxidative stability. Archi The wear resistance of lunaphthalene lubricating fluids was determined by Khimiya i Teknol.

giya Topliv I Masel, No. 8.28-29 pages, 19 Shown in August 1986.

Recently, novel lubricant compositions containing polyalphaolefins115 (here H VI-PAO) and reduced chromium on a silica support as a catalyst. Methods for their manufacture are described in U.S. Pat. Disclosed in the issue. The method uses C6C20+-alkene raw materials and porous silica support. chromium oxide catalyst in the reduced valence state on the body under oligomerization conditions. contact in the merization zone, thereby achieving a branching ratio of less than 0.19 and temperatures as low as -15°C. A liquid hydrocarbon lubricant with low flow, high viscosity and high Vl is obtained. Including. Lubricants produced by this method cover the entire range of lubricant viscosities. - and exhibits significantly higher VT and lower pour point even at high viscosities, -The molecular structure of PAO is novel and essentially regular for alpha olefins. contains the products of head-to-tail polymerization and therefore large pendants on repeating polymer units. An oligomer having a toalkyl group is provided.

Dehydrocyclization is performed using Royals rAdvanced Organic Chem istryJ Preut 1ce-Hal l, Inc, pages 145-147 Conversion of linear and technical alkanes to aromatic compounds as described in One reaction, which is well known in the art of organic chemistry, is the catalytic action of a dehydrogenation catalyst. and proceeds by ring closure and dehydrogenation to provide the aromatic structure.

The dehydrocyclization reaction is characterized as a type of 5-aromatization reaction, and has many uses. The words are used interchangeably here.

Disclosure of invention The aromatic structure is a pendant or branched alkyl group in the repeating polymeric unit of the PAO. Dehydrocyclization reaction that converts a part of the group into an aromatic structure Hepolyalphaolefin In the molecular structure of polyalphaolefin lubricant oligomers, It was found that it can be introduced into When the feedstock to dehydrocyclization is HVI-PAO, Performing the dehydrocyclization reaction may affect the viscosity measurement properties of HVI-PAO, especially the high Produces lubricant oligomers with increased aromaticity without significantly lowering VT. It was found that As a result, increased thermal stability, abrasion resistance and dissolution P containing an aromatic structure that imparts properties to the liquid lubricant oligomer so modified. AO and HVI-PAO are generated. Improved dissolution properties provide modified lubrication It is particularly important for improving the solubility of aromatic additives in agent oligomers.

The polyalpha olefin produced by the dehydrogenation ring method is polyalpha Up to 5% by weight of aromatic structures attached as pendant groups to the backbone of olefin structures A novel composition comprising:

For more preferred HVI-PAO oligomers, the composition comprises repeatable polymeric structure (However, in the formula, X is 5-11, n is smaller than 500, and the ratio of n to m is 200- 20, and R is an aryl, aralkyl or alkyl containing x0N1fi carbon atoms. (including kill aryl) has.

More particularly, the present invention provides a method for dehydrocyclization of C6'20 polyalphaolefins. It discloses the dehydrocyclization conditions of polyalphaolefin, dehydrogenation catalyst and contact in the dehydrocyclization reaction zone under including the production of real fur olefins.

The method uses alpha olefins containing 6-20 carbon atoms. HV[ More particularly concerned with the dehydrocyclization of -PAOs. Oligomerization is an oligomerization condition Chromium catalyst on porous support with olefin at reaction temperature of 90-250 °C under contacting the catalyst at a temperature of 200-900°C in the presence of an oxidizing gas. oxidized at a temperature of It is treated by treatment with a reducing agent. Oligomerization is O, +9 Smaller branching ratio, weight average molecular weight of 420-45000, 420-18000 Number average molecular weight, molecular weight distribution of l-5, i.e. (weight average molecular weight)/(number average molecular weight) and an oligomeric liquid lubricant set containing C-C having a pour point lower than -15°C produce a product.

Figure 1 shows the relationship between the rate of hydrogen flow and aromaticity in the product of wood separation. This is Bron 1-, which shows the relationship.

Figure 2 shows the relationship between the rate of hydrogen flow and the number of bromines in the products of the invention. 1~.

Polyalpha used as a raw material in the dehydration and cyclization step of the process of the present invention Olef, in-4 oligomer is a commercially available product if prepared as described below. PAO or HVI-PAO. Conventional PAOs are linear 1-alkene Lewis Generally produced by acid or Ziegler catalyst initiated oligomerization. Even more normal city Commercially available PAOs are oligomerized by aluminum chloride catalyst of 1-decene. Manufactured by. Oligomers are C short-chain alkyl moieties of less than 8 carbon atoms. Contains many branches.

The HVI-PAO oligomer used as a raw material in the present invention has a porous support. C6’20 alpha in contact with the reduced valence state of the chromium oxide catalyst on the body Produced by oligomerization of olefins. l-11V'-PAO oligomer The method described herein produces a weight average molecular weight of 420-60,000 and Controlled to produce oligomers with number average molecular weights of 420-24,000. I found out that I can roll. The molecular weight, measured by the number of carbons, is C30'2100 ranges from C to C, with a preferred range of C30'1400. . The molecular weight distribution, defined as the ratio of weight average molecular weight to number average molecular weight, is 1.0n -5, with a preferred range of 1.0 L-3.

The I-hexene HVI-PAO oligomer of the present invention has a very uniform linear C4 fraction. 11J-like head-to-tail structure showing the following structure, which is branched and confirmed by NMR: It was shown that it contains a connection.

Oligomerization of I-decene with supported chromium in a reduced valence state also This yields HVI-PAO with a structure similar to that of l-hexene oligomers.

Lubricant products after distillation and hydrogenation, excluding light fruccidine, are Characteristic C-13 NMR spectra confirming regular head-to-tail oligomerization of 2 to produce a structure with large alkyl group branches.

Generally, the 1-TVI-PAO oligomer has a head-to-tail bond consisting of n = 3- Since T is 17, it has a head-to-tail structure.

Olefins suitable for use as feedstock in the production of HVI-PAO include 2-20 Olefins containing carbon atoms such as ethylene, propylene, 1-butene, I- Pentene, l-hexene, 1-octene, l-decene, l-dodecene tail 1-tet Contains and uses rhadecene as well as branched chain isomers such as 4-methyl-1-pentene Suitable for this purpose are olefin-containing refined feedstocks or effluents. But used The olefin is preferably an alpha olefin such as ■-heptene to I- xadecene, more preferably l-octene to l-tetradecene, or It is a mixture of these olefins.

HVI-PAO oligomers of alpha olefins have low o, less than 19 with branching ratios, and even high branching ratios as produced by all known industrial methods It has superior lubricity compared to alpha olefin oligomers.

HVI-PAO alpha olefin oligomer is an alpha olefin oligomer. It is produced by oligomerization reactions in which the main proportion of heavy bonds is not isomerized. these The reaction is carried out using supported metal oxide catalysts such as Cr compounds on silica or other supports. Alpha olefin oligomers according to I UPAC table VIBII compound The most preferred catalysts, including gomerization, are low valence Group VIB catalysts on an inert support. It is a metal oxide. Preferred supports are silica, alumina, titania, and silica. Contains alumina, magnesia, etc.

The branching ratio used to characterize the HVI-PAO is rAnalytical Published in CbemistryJ Volume 25, Issue 10, Page 1466 (+953) Calculated from the weight fraction of methyl groups obtained by infrared method as Supported metal oxide catalysts include metal salts, preferably in water or an organic solvent, on a support. It is manufactured by impregnating it with Any suitable organic solvent known to those skilled in the art may be 1 For example, ethanol, methanol or 1! ￥There is acid. solid catalyst precursor The cer is then dried and heated to 200-900 ml with air or other oxygen-containing gas. The catalyst, which is calcined with C, can be prepared using any of a variety of well-known reducing agents, e.g. C01H2, NH3H2S, C52, CH3SCH3, CH3SSCH3, gold Alkyl-containing compounds of the genus R3A1. R2H, R2Mg, RLi, R2Zn (wherein R is alkyl, alkoxy, aryl, etc.).

Preferably, it is CO or (2) or a metal alkyl-containing compound.

On the other hand, group VIB metals can be applied to substrates in reduced form, e.g. CI.11 compounds. Wear. 1! The prepared catalyst has a pressure of 1O-34580kPa (0.1 atm-5000 Olefins are oligomerized in the temperature range from room temperature to 500°C at a pressure of ps I). It is very active in Preferably, oligomerization is carried out at a temperature of 90-250'C. It will be carried out at the same time.

The contact time of both olefin and catalyst varies from 1 second to 24 hours. 10- The very low catalyst concentration based on 0.01% by weight of feedstock is very low to form oligomers. used for. The catalyst can be used in hatch type reactors or in fixed bed, continuous flow reactors. Can be used.

Example The following examples illustrate the preparation and oligomerization process of HV I-PAO catalysts. indicated for.

Example l Catalyst production and activation method 1.9 g of chromium(II) acetate (Cr (OCOCH3)42H20) (5°5 8 mmol) (commercially available) in 50 mL of hot acetic acid. - 12 mm size, surface area of 300 m2/g and pore volume of 1 mL/g. Also add 50g of lyca gel. Most of the solution is absorbed by the silica gel. last The mixture is mixed for 30 min in a rotor pub at room temperature and dried in an open I at room temperature. .

First, the dry solid (20 g) is purged with N2 in a tube furnace at 250°C. furnace The temperature is then increased to 400°C for 2vf. Temperature then dry air bar between 16FR The temperature is set to 600°C by the camera. At this time, the catalyst was heated to a temperature of 300″C under N2. Cooling.

A stream of purified Co (99.99% from Matheson) is then introduced for 1 hour. .

Finally, the catalyst is cooled to room temperature under N2 and ready for use.

Example 2 Commercial chromium/silica catalyst containing 1% Cr on large pore volume synthetic silica gel use. The catalyst was first calcined in air at 800° C. for 16 hours and 1.　 9 Next, 3.5 g of catalyst was reduced with CO at 300 °C for 5 h in a tube reactor. Pack and heat to 100°C under N2 atmosphere. 18 purified I-decene Pump into the reactor at 30-2310 kPa (250-320 psi) . The product was collected PiIltlI and heated to 343°C (650°F). High Vl as shown in the table below, excluding light products with lower boiling points. A high quality HV I-PAO lubricating oil is obtained.

In the method of the present invention, HVI-PAO oligomers undergo dehydrocyclization of HVl-PAO. Oligomers containing aromaticity in the structure of the oligomer molecule by treatment with converted into. In the method, some of the pendant alkyl groups of the oligomer are ring-closed. and dehydrogenated to form an aromatic ring structure. Depending on the dehydrocyclization used, 5 It was found that up to % by weight of aromatic structures were introduced into the HVr-PAO molecular structure. . Preferably, the dehydrocyclization reaction is performed with an alpha olefin, most preferably 1-decene. HVI-PA produced from C8'14 alpha olefin O oligomer to produce poly-1-decene oligomer.

C-C-13N analysis of the product of the dehydrocyclization method of the present invention shows that the product is repeatedly polymerized. somatic structure (where X is 5-1], 1) is less than 500, and the ratio of n to m is 200- 20 and R contains x+1 carbon atoms, aryl, aralkyl or alkyl Confirm that the product is a liquid lubricant containing hydrocarbons (including aryls) Ru.

Special case of dehydrocyclization of poly-needecene produced by HVI-PAO method Now, the C-C-13N analysis supports the conclusion of the above structure where X is equal to 7. Po The dehydrocyclization product of Li-1-decene has a viscosity of at least 2C3 and and a viscosity index of at least 130.

Influence on the dehydrocyclization reaction of poly-alphaolefin oligomers in the present invention The catalysts used to dehydrogenate alkanes are well known to those skilled in the art of organic chemistry. These include those commonly and conventionally used to affect cyclization.

Metals of Group VIII of the CAS version of the Periodic Table of the Elements, including especially platinum and palladium .

These catalysts are made from materials such as alumina, silica, clay, charcoal and zeolites. In the present invention, the zeolite and further contained on the solid support structure taken Especially large pore zeolites have been found to be useful. These zeolites are 2 Beta, Z, with the following constraint index and alpha value of l-100 Contains SM-12 and Y.

Zeolites provide controlled access to molecules of different sizes to their internal structure. A convenient guide to the degree to which this is done is the aforementioned constraint index of the zeolite. . The method by which the constraint index is determined is detailed in U.S. Pat. No. 4,016,218. The method is described in detail and is referred to for details of the method.

The zeolites selected for use herein are generally at least 1, preferably at least 10 and more preferably at least 50 It has a value. "Alpha number" or [alpha number 4] is the acidic value of zeolite. No. 4,016,218, jJ, CatalyS isJ6. pages 278-287 (+966) and rJ, CatalysisJ 61, pages 390-396 (1980), with details of its measurements. is described in detail. Zeola with low acidity (alpha number less than 200) (a) synthesis of zeolite with high silica/alumina ratio; (b) steaming, (c) dealumination to the steaming ring and (d) basic aluminization. This can be achieved by a variety of techniques, including the replacement of aluminum by other materials, e.g. 5 For steaming, one or more zeolites are heated at 260-650°C (500°C -1200°F) and preferably 39L-538°C (750-+000° exposed to water vapor at high temperatures up to F). This process is performed in a 100% water vapor atmosphere. or in an atmosphere consisting of a gas and water vapor that is substantially inert to Ze4lite. can. A similar treatment uses high pressure and low temperature, e.g. 101O-20 177-371'C (350-700°) at 200kPa (10-200 atm) F) can be achieved. Specific details of Uni's steaming method can be found in U.S. Patent No. 432 5994.4374296 and 4418235.

A particularly useful catalyst for the process binds about 35% alumina by weight and has 0.16% white The catalyst, which contains gold-bearing zeolite beta, is steamed to produce 50 alkaline It yields an effective catalyst for dehydrocyclization with hydrocarbons.

The process of the present invention is performed under aromatization conditions involving a feed or stream of hydrogen to the reactor? Tewa It will be done. Hydrogen is produced at a rate of 0=900v/v (0-500O5CF/BBL) It will also be introduced. However, as shown in Figure 2, the hydrogen flow rate is Affects the degree of Kozoku 1hi. The highest aromatic content is hydrogen, as shown in Figure 1. The flow rate of 6 hydrogen found when the flow rate of affects the degree of residual unsaturation. The raw material I(Vl-PAO) is generally an oligo Containing at least one olefinic group per mer molecule, this unsaturation is up to 1 & The degree of product loss is influenced by the hydrogen flow rate, as shown in FIG.

At fast hydrogen flow rates, bromine numbers less than 1 are achieved, but in the absence of hydrogen flow, , the bromine number for the poly-1-decene HVI-PAO aromatization product is greater than 6. stomach.

The method of the present invention is performed at a temperature of 50-700°C and a pressure of 940-7000 kPa (20- It can be carried out at a pressure of 1000 psjgl and a liquid hourly space velocity of 0.1-10. It turns out that Preferably 1M! Dihydrogen cyclization conditions are 100-300'C) twice, 2]7O-4240kPa f300-600psig) pressure, and Contains LH5V of 0.4-1.

The following examples illustrate one dehydrocyclization process of the present invention and the properties of the products produced therefrom. Explain. The examples are presented for illustrative purposes only and are intended to limit the scope of the invention. It is not intended to limit the

The raw material used in Example 3-6 is HVI-1) AO liquid lubricant, which has been previously described. Produced in a fixed bed reactor according to the method described. produced in a fixed bed reactor Oligomerization conditions and properties of 1-decene HV I-P A O oligomer raw material is as follows. Reaction temperature 165°C1 pressure 380kPa (40ps) ig), WH5V2.5, lubricating oil yield 63.3%, viscosity at 40°C +30.4c s, viscosity at 100″C! 9.7cs, viscosity index 173.1° In Example 3-6, The dehydrocyclization process carried out on the feedstock contains 35% by weight alumina and 0.5% by weight alumina. 6 In a fixed bed reactor containing an aromatization catalyst containing zeolite beta containing wt% platinum It was conducted. The catalyst is steamed to 50 alpha whispers.

All experiments were carried out at 0.5 LH3V and 2860 kPa (400 ps+g). It is carried out under pressure. The flow rate of hydrogen into the reactor is 0-900v/v (0-500v/v) 05CF/B B L). Specific experimental conditions for the products produced The conditions and properties are listed in Table 1.

From the above data, a significant degree of aromaticity was observed in HVI-P by the two described methods. It is clear that it can be introduced into the AO3 as shown in Table 1, and as already mentioned. As shown, the formation of aromatic structures varies as a function of hydrogen flow rate, with the highest aromatic The content is achieved under conditions without hydrogen flow. Goose (preferably, aromatization 1 ( The viscosity index of Vl-PAO remains high and has little or no viscosity index compared to that of the raw material. It does not decrease at all. In addition, conditions for fast hydrogen flow rate to the Wit hydrogen cyclization zone or reactor Below, there is a significant reduction in the bromine number, leading to aromatization of the HVI-PAO oligomers. and co-current hydrogen treatment. Therefore, these products with low bromine numbers are useful as lubricants. The subsequent hydrogen treatment commonly used to stabilize the product can be avoided.

These examples contain 4-5% aromatic structures by weight, based on the weight of the total product. can be introduced into the HVI-PAO and the new composition as shown by C-C-13N These are C24-C3ooo hydrocarbons. A new liquid lubricant composition comprising: ratio, weight average molecular weight of 420-60000, number average molecular weight of 420-24000 , I-5, with a pour point lower than -+5 °C, and 0.4-4 wt% Contains aromatic structures.

Although this invention has been described in a preferred embodiment, modifications and changes will readily occur to those skilled in the art. It is understood that the invention may be made without departing from the spirit and scope of the invention. should be understood. These modifications and changes are considered to be within the scope of the claims. It will be done.

international search report Continuation of front page (51) Int, C1,' Identification symbol Office serial number // C1ON 20: 02 20:04 20:00 A 30:02 70:00 CO7B 61100 300 I

Claims (25)

[Claims] 1. Polymers produced by oligomerization of C6-C20 polyalphaolefins An alpha olefin and a dehydrogenation catalyst are placed in a dehydrocyclization reaction zone under dehydrocyclization conditions. , thereby attaching pendant groups to the backbone of the polyalphaolefin structure. Modified polyalphaolefins containing aromatic structures bonded together are produced. The dehydrogenation of polyalphaolefins, including How to produce real fur olefins. 2. Alpha olefins containing 6-20 carbon atoms including the products of oligomerization of olefins or mixtures of these olefins; The reaction is carried out by chromatography on a porous support at a reaction temperature of 90-250°C under oligomerization conditions. contacting an olefin with a olefin, the catalyst being oxidized in the presence of oxidizing gas. 00-900°C for sufficient time to be oxidized and then reduced to the lower valence state. and temperatures of 0.19 and 0.19. Smaller branching ratio, weight average molecular weight of 420-45000, 420-18000 C30 with number average molecular weight, molecular weight distribution of 1-5 and pour point below -15°C 2. The method of claim 1 for obtaining an oligomeric liquid lubricant composition comprising -C1300. 3. 3. The method of claim 2, wherein the liquid lubricant composition has a viscosity index greater than 130. 4. The reducing agent contains CO and the oligomerization temperature is 100-180°C. Method for request 2. 5. 3. The method of claim 2, wherein the support comprises porous silica. 6. The olefin is 1-octene, 1-decene, 1-dodecene, 1-tetradecene. 3. The method of claim 2, consisting essentially of: or a mixture thereof. 7. The dehydrocyclization catalyst comprises a supported Group VIII metal of the periodic table as well as a metal. Zeolite is selected from ZSM-5, ZSM-12, Y, and Beta, and the support is The method of claim 1, wherein the material is selected from mina, silica, clay and charcoal. 8. The dehydrocyclization catalyst comprises zeolite beta on an alumina support containing platinum. The method of claim 1, wherein the catalyst has an alpha number of 50. 9. The dehydrocyclization conditions are a temperature of 50-700°C and a pressure of 240-7000kPa. , 0.1-10. 10. Supplying hydrogen together with polyalphaolefin to the dehydrogenation cyclization zone 2. The method of claim 1, further comprising: 11. 11. The method of claim 10, wherein hydrogen is co-fed at a rate of 0-900 v/v. 12. The modified polyalphaolefin has a temperature at 100°C greater than 2cs. Claim 1 comprising a liquid hydrocarbon lubricant having a viscosity and a VI greater than 130. Law. 13. The modified polyalphaolefin aromatic structure accounts for 0.4-4% by weight. 2. The method of claim 1. 14. Branching ratio less than 0.19, weight average molecular weight of 420-60000, 42 Number average molecular weight of 0-24000, molecular weight distribution of 1-5, pour point lower than -15℃ C24-C5000 hydrocarbons, containing 0.4-4% by weight of aromatic structures. A new liquid lubricant composition containing. 15. The composition of claim 14 having a VI greater than 130. 16. Hydrocarbons have a repeating polymeric structure ▲ There are mathematical formulas, chemical formulas, tables, etc. ▼ (However, in the formula, x is 5-11, n is smaller than 500, and the ratio of n to m is 200 -20 and R is aryl, aralkyl or alkyl containing x+1 carbon atoms (including lure reel) 15. The composition of claim 14. 17. When x is 7, the composition has a viscosity at 100°C of at least 2 cs and 13 17. The composition of claim 16 having a VI greater than zero. 18. C6-C20 alpha olefin feedstock or mixtures of these olefins Oligomer contacted with reduced valence VIB metal catalyst on porous support products of oligomerization under oxidation conditions (branching ratio less than 0.19, greater than 130) a lubricant with a low viscosity index and a pour point below -15°C) on a solid support. contact with the above group VIII metal-containing aromatization catalyst under aromatization conditions in the aromatization zone. high A method of introducing aromaticity into the structure of VI liquid lubricant hydrocarbons. 19. The liquid lubricant product has a viscosity index greater than 130 and 2cs at 100°C. 19. The method of claim 18 having a greater viscosity. 20. Aromatization catalysts include supported metals platinum and palladium; The zeolite is selected from ZSM-5, ZSM-12, Y, and Beta, and the support is 20. The method of claim 18, wherein the material is selected from mina, silica, clay and charcoal. 21. The aromatization catalyst includes zeolite beta on an alumina support containing platinum. 20. The method of claim 18, wherein the catalyst has an alpha number of 50. 22. The aromatization conditions were a temperature of 50-700°C and a pressure of 138-7000kPa. , 0.1-10. 23. Supplying hydrogen together with polyalphaolefin to the dehydrogenation cyclization zone 20. The method of claim 18, further comprising: 24. 24. The method of claim 23, wherein hydrogen is co-supplied at a rate of 0-900 v/v. 25. The aromatic structure of the liquid lubricant product should be comprised of 0.4-4% by weight of the product. The method of claim 18.