GB1584620A - Creation of Inventions and Patents with Artificial Intelligence

GB1584620A – Catalyst and process for hydrofining petroleum wax
– Google Patents

GB1584620A – Catalyst and process for hydrofining petroleum wax
– Google Patents
Catalyst and process for hydrofining petroleum wax

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Publication number
GB1584620A

GB1584620A
GB38358/77A
GB3835877A
GB1584620A
GB 1584620 A
GB1584620 A
GB 1584620A
GB 38358/77 A
GB38358/77 A
GB 38358/77A
GB 3835877 A
GB3835877 A
GB 3835877A
GB 1584620 A
GB1584620 A
GB 1584620A
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Prior art keywords
catalyst
component
range
nickel
carrier
Prior art date
1976-09-14
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GB38358/77A
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Tonen General Sekiyu KK

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Toa Nenryo Kogyyo KK
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1976-09-14
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1977-09-14
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1981-02-18

1977-09-14
Application filed by Toa Nenryo Kogyyo KK
filed
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Toa Nenryo Kogyyo KK

1981-02-18
Publication of GB1584620A
publication
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patent/GB1584620A/en

Status
Expired
legal-status
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Classifications

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00

B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper

B01J23/76—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 – B01J23/36

B01J23/84—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups B01J23/02 – B01J23/36 with arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium

B01J23/85—Chromium, molybdenum or tungsten

B01J23/88—Molybdenum

B01J23/882—Molybdenum and cobalt

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium

B01J21/12—Silica and alumina

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00

B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper

B01J23/85—Chromium, molybdenum or tungsten

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00

B01J23/70—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of the iron group metals or copper

B01J23/85—Chromium, molybdenum or tungsten

B01J23/88—Molybdenum

B01J23/883—Molybdenum and nickel

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

B01J35/00—Catalysts, in general, characterised by their form or physical properties

B01J35/02—Solids

B01J35/10—Solids characterised by their surface properties or porosity

C—CHEMISTRY; METALLURGY

C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT

C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES

C10G73/00—Recovery or refining of mineral waxes, e.g. montan wax

C10G73/42—Refining of petroleum waxes

C10G73/44—Refining of petroleum waxes in the presence of hydrogen or hydrogen-generating compounds

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

B01J35/00—Catalysts, in general, characterised by their form or physical properties

B01J35/02—Solids

B01J35/10—Solids characterised by their surface properties or porosity

B01J35/1004—Surface area

B01J35/1019—100-500 m2/g

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

B01J35/00—Catalysts, in general, characterised by their form or physical properties

B01J35/02—Solids

B01J35/10—Solids characterised by their surface properties or porosity

B01J35/1033—Pore volume

B01J35/1042—0.5-1.0 ml/g

B—PERFORMING OPERATIONS; TRANSPORTING

B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL

B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS

B01J35/00—Catalysts, in general, characterised by their form or physical properties

B01J35/02—Solids

B01J35/10—Solids characterised by their surface properties or porosity

B01J35/1052—Pore diameter

B01J35/1061—2-50 nm

Description

PATENT SPECIFICATION ( 11) 1 584 620
O ( 21) Application No 38358/77 ( 22) Filed 14 Sep 1977 ( 19), > ( 31) Convention Application No 51/110501 ( 32) Filed 14 Sep 1976 in, ( 33) Japan (JP) t ( 44) Complete Specification Published 18 Feb 1981
U ( 51) INT CL ‘ B 01 J 35/10 Cl OG 73/44 ( 52) Index at Acceptance Bl E 1127 1180 1203 1285 1298 1322 1422 1462 1463 1492 1513 1616 1631 1632 1633 1634 1635 1701 1714 1724 1741 1744 CB ( 72) Inventors: SATOSHI SAKURADA SHOHEL OKANO TAKASHI OBAYASHI TAKEO TOYOIZUMI OSAMI IWATA TAKUJI ITOH ( 54) CATALYST AND PROCESS FOR HYDROFINING PETROLEUM WAX ( 71) We, TOA NENRYO KOGYO K K, a Corporation duly organised and existing under the laws of Japan, of 1-1 Hitotsubashi, 1-Chome, Chiyoda-Ku, Tokyo, Japan do hereby declare the invention for which we pray that a patent may be granted to us, and the method by which it is to be performed, to be particularly described in and by the following statement:-
This invention relates to a catalyst and process for hydrofining petroleum waxes More particularly, this invention relates to a catalyst and process for hydrofining petroleum waxes using a catalyst comprising a metal hydrogenation component supported on a porous carrier containing alkali metal compound wherein the carrier possesses a novel pore distribution.
Still more particularly, this invention relates to a process and catalyst for improving the 10 thermal, light and UV stability of petroleum waxes by contacting the wax with hydrogen in the presence of a catalyst comprising at least one metal hydrogenating component on a porous alumina/silica carrier containing minor amounts of alkali metal and having a novel pore structure defined by the volume of pores having a diameter in the range of 60 to 150 A being greater than 80 % of the volume of pores having a diameter in the range of 0 to 150 A 15 and the volume of pores having a diameter in the range of 0 to 600 A being in the range of from 0 45 to 0 60 ml/g.
Naturally occurring petroleum waxes must be refined in order to provide high quality waxes of improved thermal, light and ultra-violet stability Although treating raw wax with sulfuric acid or contacting it with absorbent clay has been used for improving the color, 20 storage stability and oxidation resistance, it is now preferred to hydrorefine or hydrofine the wax in order to improve these properties, particularly when the wax is to be used for foods and drugs which requires a very highly refined wax in order to satisfy the requirements of the United States Food and Drug Administration (FDA) Hydrofining improves the properties of the wax by removing therefrom a very small amount of polar substances and other 25 impurities and by hydrogenation or ring scission of polycyclic aromatic molecules In order to produce a highly refined, high quality wax it is necessary for the hydrofining catalyst to have a sufficient amount of activity to be technically practical.
The present invention relates to a catalyst and process for hydrofining petroleum wax which comprises contacting the wax with hydrogen in the presence of a catalyst comprising at 30 least one metal hydrogenating component on a porous alumina/ silica carrier containing from to 25 wt % of silica and 0 2 to 5 wt % of an alkali metal component, said catalyst being further characterized in that:
(a) the volume of pores having a diameter in the range of 60 to 150 A is greater than 80 % of the volume of pores having a diameter in the range of 0 to 150 A; and 35 (b) the volume of pores having a diameter in the range of 0 to 600 A is in the range of from 0 45 to 0 60 ml/g.
In a preferred embodiment, the catalyst has a specific surface area ranging from 200 to 300 m /g.
The carrier used for the catalyst of this invention is alumina or an alumina-containing 40 2 1,584,620 2 material containing from 5 to 25 wt % of silica and 0 2 to 5 wt % (as oxide) of an alkali metal component It is preferred that the alumina be gamma-alumina, alphaalumina, eta-alumina or mixture thereof having the pore distribution characteristics of this invention However, the alumina may be in the form of an alumina-containing material comprising alumina combined with one or more other refractory inorganic materials such as magnesia, calcium oxide, 5 zirconia, titania, boria, hafnia, and a crystalline zeolite These refractory inorganic oxides and zeolite may be present in the catalyst in an amount ranging from 1 to 10 wt % based on the alumina/silica content of the catalyst As hereinbefore described, supra, the silica content of the catalyst will range from 5 to 25 wt % and more preferably from 8 to 20 wt % of the carrier.
If the silica content is outside of this broad range, it has been found that the activity of the 10 catalyst is reduced or the wax decomposes to an excessive extent to form oils.
The alkali metal component of the catalyst may be one or more metals selected from lithium, potassium and sodium supported on the carrier as oxides The amount of alkali metal component will be in the range of from 0 2 to 5 wt % and preferably from 0 3 to 1 wt % of the carrier 15 In preparing the catalyst carrier or base, conditions such as temperature and time in the steps of precipitating hydrates and aging of the hydrates are controlled so as to obtain a catalyst having the desired pore distribution and characteristics One may start with watersoluble acidic aluminum compounds or water-soluble alkaline aluminum compounds such as aluminum sulfates, chlorides and nitrates, alkali metal aluminates, aluminum alkoxides and 20 other inorganic or organic salts Water-soluble silicon compounds such as alkali metal silicates (preferably Na 2 O:Si O 2 = 1:2-1:4), tetraalkoxysilanes and orthosilicic acid esters are suitable These aluminum and silicon compounds can be used as aqueous solutions The concentration of these aqueous solutions in the case of an aluminum compound solution should be within the range of about 0 1 to 4 0 moles In a preferred process for preparing an 25 alumina/silica carrier suitable in the use of this invention, the alumina and silica are coprecipitated However, other precipitation processes or gel mixing processes can also be employed.
The metal hydrogenation components of the catalyst may comprise one or more metals selected from the metals of Group VI and VIII of the Periodic Table such as chromium, 30 molybdenum, tungsten of Group VI and iron, cobalt, nickel, palladium, platinum, osmium, iridium, ruthenium and rhodium of Group VIII Combinations of metals of Groups VI and VIII may also be used Preferred combinations are molybdenum-cobalt, molybdenumnickel, tungsten-nickel, molybdenum-cobalt-nickel and tungsten-cobaltnickel Particularly preferred hydrogenating components are those which contain nickel Further, metals of 35 Group VII such as manganese and metals of Group IV such as tin and germanium may also be incorporated into the catalyst The metal hydrogenation components will preferably be in the oxide and/or sulfide form.
The catalyst can be used in the form of a fixed bed, fluidized or moving bed system in the hydrofining reaction However, a fixed or solid bed system is preferred from the viewpoint of 40 operability Also, two or more reactors can be combined together for achieving the hydrofining in two steps to attain a highly purified wax.
The petroleum waxes to be hydrofined in the process of this invention include raw paraffin waxes and raw microcrystalline waxes These waxes contain polycyclic aromatic compounds and impurities such as sulfur compounds and nitrogen compounds These waxes may be 45 separated from vacuum distillates from residua or combinations thereof Wax containing vacuum distillates generally comprise hydrocarbons boiling in the range of from 300 to 400 C or higher whereas residual materials comprise hydrocarbons boiling within the range from 400 to 5000 C or higher As is well known in the art, waxes may be separated from wax bearing hydrocarbon oils by a variety of solvent dewaxing processes employing autorefriger 50 ants, mixtures of autorefrigerants and ketones mixtures of ketones and aromatic solvents, inter alia Still further, adsorption dewaxing processes employing adsorbents such as natural or synthetic zeolites can be used as well as urea dewaxing processes In any event, it is preferred to deoil the wax before it is used in the process of this invention.
Reaction conditions in the hydrofining process of this invention comprise temperatures 55 within the broad range of from 1 80 to 330 WC and preferably from 200 to 300 C, pressures within the range of from 30 to 200 kg/cm 2 and preferably from 50 to 100 kg/cm 2, a hydrogen-containing gas rate within the range of from 50 to 1500 1/1 (liters per liter), preferably 200 to 1000 1 / 1 and a liquid hourly space velocity within the range of from 0 2 to 2 0 V/H/V (volumes per hour per volume), preferably from 0 5 to 1 5 V/H/V The 60 hydrogen-containing gas will contain from 60 to 100 % of hydrogen When the hydrofining is carried out in two stages, the reaction conditions selected for the respective stages may either be the same or different When different reaction conditions are to be used in the respective stages, it is preferred that more severe conditions be used in the second stage than in the first stage It should be noted that with the catalyst of this invention it has been found that a 65 1,584,620 3 1,584,620 relatively high hydrofining rate can be attained even when the reaction conditions are not relatively severe, particularly with lower pressures, without suffering much deterioration in the activity of the catalyst.
The invention will be more apparent from the preferred embodiment and working examples set forth below wherein catalysts A and F are in accordance with the invention and the 5 other catalysts are for comparison.
Catalyst Preparation In a preferred embodiment of preparing a catalyst useful in this invention, an aqueous solution of an alkali hydroxide or an alkali aluminate and an alkali silicate is added to an acidic aqueous aluminum solution (preferably in the range of 0 2 to 2 moles) to form an 10 alumina/silica hydrogel or hydrosol at room temperature and at a p H in the range of from 6 0 to 11 0, preferably from 8 0 to 10 5 Aqueous ammonia, acetic acid or another suitable reagent for p H-control is then added to the hydrogel to control the p H The suspension is then heated to a temperature of from 50 to 980 C and kept there for at least two hours to precipitate the alumina/silica The resulting precipitates are filtered, washed with ammonium acetate 15 and water, dried at a temperature in the range of from room temperature to 200 C and then calcined by heating to a temperature in the range of from 200 to 800 C in the presence of oxygen.
The alkali metal component of the carrier may be incorporated therein merely by immersing the carrier in a solution of alkali metal component and then calcining the carrier The 20 metal hydrogenation components may be impregnated onto the carrier by immersing the carrier in a solution of soluble salt of said metal or via a coprecipitation method wherein the metal hydrogenation component is coprecipitated in the preparation of the carrier However, the impregnation method is preferred It is to be understood of course that the quantity and concentration of the impregnation solution is controlled in order to deposit the desired 25 amount of metal on the carrier When two or more metal components are to be impregnated on the carrier, they may either be impregnated together using a mixture of two or more metal components in solution or each one may be impregnated separately In any event, the impregnation solution is separated from the carrier which is then washed with water, dried and calcined The drying and calcination may be carried out under the same conditions used 30 in the preparation of the carrier described, supra The amount of metal deposited on the carrier may range from 0 1 to 20 wt % for metals of Group VIII and from 5 to 20 wt % for metals of Group VI, based on the total catalyst weight.
The catalyst may be molded into any desired shape such as cylinders, granules, tablets, 35 inter alia, by extrusion molding, granulation molding or other shaping procedure Preferably the catalyst will be molded into particles having a diameter within the range of from 0 5 to 3 0 mm The finished catalyst will preferably have a total pore volume of from 0 5 to 1 0 ml/g, a bulk density of 0 5 to 1 0 g/ml and a side crushing strength of 0 8 to 3 0 kg/ml in addition to the other characteristics mentioned supra 40 It is preferable to sulfide the catalyst before using it in the hydrofining reaction of this invention The catalyst can thus be sulfided during the manufacture thereof or after being charged into the reactor If the catalyst is to be sulfided after being charged into the reactor If the catalyst is to be sulfided after being charged to the reactor, it may be contacted with a sulfur-containing petroleum distillate at a temperature ranging from 150 to 400 C under a 45 pressure (total pressure) of 20 to 100 kg/cm 2 and at a liquid hourly space velocity of from 0 3 to 2 0 V/H/V in the presence of 50 to 1500 1/1 of a hydrogen-containing gas After the catalyst has been sulfided, the sulfur-containing distillate is replaced with the untreated or raw wax and conditions in the reactor are changed to those suitable for the hydrorefining process of this invention Alternatively, the catalyst can be sulfided by contacting same 50 directly with a sulfur compound such as hydrogen sulfide or by adding hydrogen sulfide or C 52 to a suitable distillate and then contacting the sulfur-containing distillate with the catalyst.
Determination of the Catalyst Pore Structure It is known in the art that a gas adsorption method such as the nitrogen adsorption method 55 is advised for determining pores having a diameter within the range of from 0 to 600 A, while a mercury porosimeter method is used for the larger pores whose diameter is greater than 600 A These methods are disclosed in P H Emmett, et al, “Catalysis” 1, 123 ( 1959) (published by Reinhold Publishing Co) and “Shokubai Kogaku Koza (Lectures on catalyst Engineering)” 4 69-78 ( 1964) (published by Chijin Shokan Co (Japan) In this invention the nitrogen 60 adsorption method was used to determine the pore volume of pores having a diameter of from 0 to 600 A while the mercury porosimeter method was used for determining the pore volume of pores having a diameter greater than 600 A.
In the mercury porosimeter method, contact angle between mercury and the catalyst was 1400, surface tension was 480 dyne/cm and all pores were considered to be cylindrical For 65 1,584,620 1,584,620 the nitrogen adsorption method, various correction methods have been proposed Among them, BJH method lE P Barrett, L G Joyner and P P Hallend, “J Amer Chem Soc ” 73, 373 ( 1951)l and CI method lR W Cranston and F A Inkley, “Advances in Catalysis” lX, 143 ( 1957) (New York Academic Press)l are employed generally Data relating to the pore structure and volumes in this invention were obtained by making calculations according to 5 the DH method lD Dollimore and G R Heal, “J Appl Chem ” 14, 109 ( 1964)l from adsorption data of adsorption isotherms.
All of these methods and references are known in the art and are discussed in U S Patent 3,994,503, in column 5, lines 32-68 and in column 6, lines 10-36.
Example 1 10
An alumina hydrogel was prepared from aluminum sulfate, sodium hydroxide and water glass No 3 (Japanese Industrial Standard K-1408) as starting materials The alumina hydrogel was washed and then subjected to an aging treatment at 75 C for two hours.
Precipitates thus formed were separated from the solution, dried, mixed with water and extrusion/molded into cylinders of a diameter of about 1 5 mm The molded cylinders were 15 calcined to obtain a carrier for catalyst Molybdenum and nickel from aqueous ammonium molybdate and nickel nitrate solutions were deposited on the carrier thus obtained to form catalyst A For comparative purposes a commercial Ni/Mo/A 1203 catalyst (catalyst B) was also used Compositions and physical properties of catalysts A and B are shown in Table 1.
20 TABLE 1
COMPOSITION AND PROPERTIES OF CATALYSTS A AND B 25 A B Composition Mo O 3 (wt %) 15 1 15 3 30 Ni O (wt %) 4 2 4 1 Na 2 O (wt %) 0 54 0 09 Si O 2 (wt %) 11 9 3 5 A 1203 (wt %) Balance Balance Specific surface area (m 2/g) 259 286 35 Pore volume (ml/g) 0 600 A 0 559 0 565 0 60 A 0 004 0 056 150 A 0 044 O 104 150 180 A 0 175 0 162 40 240 A 0 151 0 109 240 300 A 0 094 0 105 300 600 A 0 051 0 048 P V I(%) 91 4 65 Bulk density (g/ml) 0 69 0 680 45 PVI = ( 60 150 A/0 150 A) x 100 A raw paraffin wax was introduced together with 150 L/L (hydrogen/hydrocarbon) of hydrogen in a reactor filled with catalyst A at a reaction temperature of 250 under a 50 hydrogen pressure of 60 kg/cm 2 and at a liquid hourly space velocity of 0 5 V/H/V to effect the hydrofining reaction The properties of both the raw and hydrofined wax are shown in Table 2 The same raw paraffin wax was hydrofined with catalyst B under the same conditions as with catalyst A These results are also listed in Table 2.
1,584,620 5 TABLE 2
RESULTS OF PARAFFIN WAX HYDROFINING Raw Wax Catalyst A Catalyst B 5 Color (Saybolt) 16 30 + 30 Thermal Stability -1 30 + 28 (Saybolt) 10 C x 2 hours Light Stability -3 28 20 (Saybolt) Direct rays of 15 sun, 15 days Melting Point ( C) 58 8 Oil Content (wt %) 0 185 0 203 0 445 20 Ultraviolet Absorbance 1 65 0 018 0 081 (L/100 g cm) @ 270 m/x 25 Sulfur Content 3 0 (ppm) Nitrogen Content 2 0 30 (ppm) Note:
Thermal Stability: Wax taken in a test tube of an outside diameter of 3 cm and a depth of 10 cm and then heated in a bath at 160 C for two hours and color thereof was determined 35 Light Stability: A column of wax ( 1 inch x 1 inch x 10 cm) was placed on a horizontal surface of an experiment stand at a distance of 1 m from a window and exposed to direct rays of the sun continuously for 15 days The, the wax was molten and color thereof was determined.
Example 2 40
The same wax material as in Example 1 was subjected to hydrofining treatment under the same conditions as in Example 1 except that catalysts C, D and E having compositions and physical properties shown in Table 3 were used to obtain the results shown in Table 4.
To prepare the catalyst, a hydrogel was prepared from aluminum sulfate, sodium hydroxide and water glass No 3 as main starting materials The hydrogel was washed repeatedly 45 twice so as to sufficiently eliminate sodium hydroxide which would form Na 2 O by calcination.
The hydrogel was dried, then added with water again and molded into cylinders of a diameter of about 1 5 mm with an extrusion molding machine The carrier in the form of cylinders was calcined to obtain alumina/silica carrier Molybdenum and nickel from aqueous ammonium molybdate solution and aqueous nickel nitrate solution, respectively, were supported on the 50 carrier thus obtained to form catalyst C Conditions of washing step with water were varied to obtain catalysts D and E.
6 1 1,584,620 TABLE 3
COMPOSITION AND PROPERTIES OF CATALYSTS C, D AND E Catalyst C Catalyst D Catalyst E 5 Composition Mo O 3 (wt %o) 19 1 14 5 15 8 Ni O (wt %) 5 07 4 05 4 10 Na 20 (wt %) 0 10 0 06 0 15 10 Si O 2 (wt %) 11 9 11 9 10 4 A 1203 Balance Balance Balance Specific surface area (m 2/g) 221 294 276 Pore volume 15 (ml/g) 0 600 A 0 414 0 570 0 538 0 60 A 0 023 0 024 0 041 150 A 0 079 0 103 0 107 150 180 A 0 141 0 168 0 155 20 240 A 0 103 0 116 0 103 240 300 A 0 034 0 110 0 082 300 600 A 0 034 0 049 0 050 P V I (%e) 78 73 3 72 6 Bulk Density 0 85 0 64 0 73 25 (g/ml) PVI = ( 60 150 A/0 o 150 A) x 100 30 35 TABLE 4
PROPERTIES OF HYDROFINED WAX 40 Catalyst C Catalyst D Catalyst E Color (Saybolt) 30 + 30 + 30 Thermal Stability 29 28 28 45 C x two hrs.
Light Stability 18 19 18 Direct rays of the sun, 15 days 50 Oil Content (wt %o) 0 40 0 25 0 293 Ultraviolet 0 0453 0 060 0 0935 Absorbance 55 (L/ 100 g cm) a 270 io, 7 1,584,620 7 Example 3
The same raw wax as in Example 1 was subjected to hydrofining treatment under the same conditions as in Example 1 except that catalysts I, J and K having compositions and physical properties shown in Table 5 were used to obtain the results shown in Table 6.
5 TABLE 5
COMPOSITION AND PROPERTIES OF CATALYSTS I, J AND K 10 Catalyst I Catalyst J Catalyst K Composition Mo O 3 (wt %) 15 1 13 4 17 4 Ni O (wt %) 3 6 4 8 5 3 15 Na 2 O (wt %) 0 7 0 04 0 9 Si O 2 (wt %) 20 2 18 7 4 3 A 1203 Balance Balance Balance Specific surface 275 289 233 area (m 2/g) 20 Pore volume (ml/g) 0 600 A 0 511 0 568 0 473 0 60 A 0 037 0 022 0 017 25 150 A 0 103 0 101 0 098 180 A 0 127 0 155 0 129 240 A 0 136 0 115 0 106 240 300 A 0 030 0 099 0 077 300 600 A 0 028 0 047 0 043 30 P V I (%) 74 82 85 Bulk Density 0 721 0 724 0 773 (g/ ml) 35 TABLE 6
PROPERTIES OF HYDROFINED WAX Catalyst I Catalyst J Catalyst K 40 Color (Saybolt) 30 30 + 30 Thermal Stability (Saybolt) 45 C x 2 hours 27 29 28 C x 3 hours 18 19 18 Light Stability 18 18 17 50 (Saybolt) Direct rays of the sun, 15 days Oil Content (wt %) 0 35 0 53 0 27 55 Ultraviolet Absorbance 0 051 0 034 0 086 (L/ 100 g cm) @’ 270 m/x 60 1,584,620 1,584,620 Example 4
Catalytic hydrofining in two stages was carried out under reaction conditions shown below in the presence of a Co/Mo/A 1203-Si O 2 (catalyst F) obtained by supporting 3 5 wt % (as Co O) of cobalt instead of nickel on the catalyst carrier (catalyst A) prepared in Example 1.
Raw material was raw microcrystalline wax shown in Table 7 The results are also shown in 5 Table 8.
TABLE 7
TWO-STAGE HYDROFINING CONDITIONS 10 The first The second stage stage Temperature ( C) 320 260 15 Liquid hourly space velocity (V/H/V) 0 5 0 5 Pressure (kg/cm 2) 50 50 20 Hydrogen/hydrocarbon (L/L) 200 200 Amount of catalyst filled (ml) 300 300 9 1,584,620 9 TABLE 8
TWO-STA GE HYDROFINED WAX PROPERTIES Raw Wax Catalyst F Catalyst L 5 Color (ASTM D-1500-64) 8 + 0 4 1 7 Melting Point ( C) 83 6 85 5 83 6 10 Thermal Stability C x 5 hours Color (Union) 4 0 7 3 15 Total acid number 7 98 8 90 (mg/KOH) FDA Standard Not Satisfied Not 20 satisfied satisfied Ultraviolet Absorbance ( 1/100 g cm) 25 280/289 m 0 027 0 11 290/299 m 0 044 0 12 30 300/359 mt 0 062 0 09 360/400 m 0 013 0 018 Oil Content (wt %) 0 57 0 67 35 Ultraviolet absorbance is determined as follows according to FDA standard 121 1156.
Wave length (m/x) Absorbance ( 1/100 cm) 40 280/289 below 0 15 290/299 below 0 12 300/359 below 0 08 45 360/400 below 0 02 50 Example 5
The same raw wax as in Example 4 was subjected to hydrofining treatment under the same conditions as in Example 4 except that catalyst L shown in Table 9 was used The results are shown in above Table 8 for comparison 55 1,584,620 10 TABLE 9
COMPOSITION AND PROPERTIES OF CATALYST L Composition 5 Mo O 3 (wt %O) 12 5 Co O (wt% ) 3 5 10 Na 2 O (wt %) 0 05 Si O 2 (wt %) 0 3 A 1203 Balance 15 Specific surface area (m 2/g) 224 Pore Volume (ml/g) 20 0 600 A 0 478 0 60 A 0 025 60 150 A 0 080 25 180 A 0 106 240 A 0 128 30 240 300 A 0 047 300 600 A O 092 P V I (%) 76 5 35 Bulk Density (g/ml) 0 628 It is apparent from the foregoing examples that, according to the process of this invention, the silica and alkali metal components in the catalyst and the pore distribution thereof exhibit 40 a remarkable effect on the improvement in the color light and thermal stability of the refined wax and also on the control of side reactions such as isomerization.

Claims (1)

WHAT WE CLAIM IS:
1 A catalyst comprising at least one metal hydrogenating component on a porous alumina/silica carrier containing from 5 to 25 wt % silica and from 0 2 to 5 wt % of an alkali 45 metal component and being further characterized in that:
(a) the volume of pores having a diameter in the range of 60 to 150 A is greater than 80 % of the volume of pores having a diameter in the range of 0 to 150 A; and (b) the volume of pores having a diameter in the range of 0 to 600 A is in the range of from 0 45 to 0 60 ml/g 50 2 A catalyst as claimed in claim I wherein said metal hydrogenating component is selected from the metals of Group VI and Group VIII and mixtures thereof.
3 A catalyst as claimed in either of claims I or 2 wherein said metal hydrogenating component comprises nickel.
4 A catalyst as claimed in either of claims I or 2 wherein said metal hydrogenating 55 component is selected from chromium molybdenum tungsten iron cobalt nickel and mixtures thereof.
A catalyst as claimed in any one of claims 1-4 wherein the silica content ranges from 8 to 20 wt % of the carrier.
6 A catalyst as claimed in any one of claims 1-5 wherein the alkali metal component is 60 present in an amount ranging from 0 3 to I wt % of the carrier.
7 A catalyst as claimed in any of claims 1-6 wherein the total pore volume ranges from 0.5 to 1 0 ml/g.
8 A catalyst as claimed in any one of claims 1-7 wherein the catalyst has a specific surface area ranging from 200 to 300 m 2/g 65 1,584,620 1,584,620 9 A catalyst as claimed in any one of claims 1-8 wherein said alkali metal component is an oxide of one or more metals selected from lithium, potassium and sodium.
A catalyst as claimed in any one of claims 1-9 wherein the metal hydrogenating component is selected from: a mixture of molybdenum and cobalt, molybdenum and nickel, tungsten and nickel, molybdenum, cobalt and nickel and tungsten, cobalt and nickel 5 11 A process for hydrofining petroleum wax which comprises contacting the wax with hydrogen at hydrofining conditions in the presence of a catalyst as claimed in any one of claims 1-10.
12 A process as claimed in claim 11 wherein said catalyst is sulfided prior to use.
13 A process as claimed in either of claims 11 or 12 wherein said metal hydrogenating 10 component is selected from the metals of Group VI and Group VIII and mixtures thereof.
14 A process as claimed in anyone of claims 11-13 wherein said alkali metal component is selected from lithium, potassium and sodium oxides.
A process as claimed in any one of claims 11-14 wherein said alkali metal component is present in the catalyst in an amount ranging from 0 3 to 1 wt % of the carrier 15 16 A process as claimed in any one of claims 11-15 wherein said hydrorefining conditions include a temperature within the range of from 180 to 330 C, a pressure within the range of from 30 to 200 kg/cm 2, a hydrogen-containing gas rate from 50 to 1500 1/1 and a liquid hourly space velocity of from 0 2 to 2 0 V/H/V.
17 A process as claimed in any one of claims 11-16 wherein said hydrogencontaining 20 gas contains from 60 to 100 % of hydrogen.
18 A process as claimed in any one of claims 11-17 wherein the catalyst has a specific surface area ranging from 200 to 300 m 2/g.
19 A process as claimed in any one of claims 11-18 wherein the catalyst has a total pore volume ranging from 0 5 to 1 0 ml/g 25 A process as claimed in any one of claims 11-19 wherein said metal hydrogenating component is a mixture of two or more metals, one of which is molybdenum and/or tungsten and the other is cobalt and/or nickel.
21 A catalyst as claimed in any one of claims 1-10 substantially as hereinbefore described 30 22 A process as claimed in any one of claims 11-20 substantially as hereinbefore described.
23 A petroleum wax when hydrofined according to the process claimed in any of claims 11-20.
K J VERYARD 35 Suffolk Street, SW 1 Agent for the Applicants Printed for Her Majesty’s Stationery Office, by Croydon Printing Company Limited, Croydon, Surrey 1981.
Published by The Patent Office, 25 Southampton Buildings London, WC 2 A l AY, from which copies may be obtained.

GB38358/77A
1976-09-14
1977-09-14
Catalyst and process for hydrofining petroleum wax

Expired

GB1584620A
(en)

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JP11050176A

JPS5335705A
(en)

1976-09-14
1976-09-14
Hydrogenation and purification of petroleum wax

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GB1584620A
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1981-02-18

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GB1584620A
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1976-09-14
1977-09-14
Catalyst and process for hydrofining petroleum wax

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US4139494A
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1976

1976-09-14
JP
JP11050176A
patent/JPS5335705A/en
active
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1977

1977-09-12
US
US05/832,434
patent/US4139494A/en
not_active
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1977-09-14
GB
GB38358/77A
patent/GB1584620A/en
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1979-05-25
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1979-02-13

JPS5335705A
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1978-04-03

BE876546Q
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1979-09-17

JPS6240059B2
(en)

1987-08-26

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