公开(公告)号：CA513183A

公开(公告)日：1955-05-24

申请号：CA513183D

Applicant: STANDARD OIL DEV CO

Inventor： ARCHIBALD FRANCIS M ,  MOTTERN HENRY O

公开(公告)号：FR1094469A

公开(公告)日：1955-05-20

申请号：FR1094469D

申请日：1953-11-21

Applicant: STANDARD OIL DEV CO

IPC: C07C7/10

公开(公告)号：GB730223A

公开(公告)日：1955-05-18

申请号：GB2946352

申请日：1952-11-21

Applicant: STANDARD OIL DEV CO

IPC: C10G35/14

Abstract: In a process of hydroforming hydrocarbons using a fluidized catalyst, continuously withdrawing a stream of catalyst to a regeneration zone where carbon is burnt off, treating the regenerated catalyst with hydrogen-rich gas, and recycling to the hydroforming zone, the hot regenerated catalyst is cooled with a second stream of catalyst from the hydroforming zone prior to the treatment with hydrogen. The amount of said second stream is sufficient to absorb the heat of reduction and prevent a rise of temperature of the regenerated catalyst on treatment with hydrogen. The regenerated catalyst may be mixed with spent catalyst in a separate hydrogen treatment vessel or the mixture carried by a stream of hydrogen-rich gas to the main reactor. Alternatively, indirect heat exchange may be used, preferably using a reactor having at least two vertically spaced beds connected by downcomers, catalyst being taken from the upper bed to the regenerator and regenerated catalyst recycled to the lower bed. The heated reactor catalyst is recycled to the upper bed whereby a higher temperature is maintained therein, e.g. 900-950 DEG F., compared with 875-900 DEG F. in the lower bed. Regeneration may be at 1050-1200 DEG F., the regenerated catalyst then being cooled to below 1050 DEG F. prior to the hydrogen treatment. Gaseous products of the latter which contain water vapour are preferably separated from the catalyst to prevent deleterious action thereon under hydroforming conditions. For direct mixing, reactor 10, Fig. 1, is provided with conduit 18, whereby spent catalyst is taken to a stripper 19, and thence to regenerator 30. Regenerated catalyst overflows into a stripping cell formed by conduit 37 which connects with conduit 40 and transfer lines 42, 48. Catalyst from the reactor flows by conduits 43, 44 to line 42 where mixing with regenerated catalyst occurs. The hydrogen-containing gas is separated in 49, and catalyst returned by line 51. For indirect heat exchange, reactor 110, Fig. 2, is divided to contain two fluidized beds 116, 117. Catalyst withdrawn from the upper bed passes through stripper 121 and U-line 124 to regenerator 130. Regenerated catalyst is taken by line 136 to heat exchanger 145 where it is cooled by catalyst withdrawn from the reactor by line 137 and passing via stripper 138 and U-line 141 through the exchanger back to the reactor. The cooled, regenerated catalyst passes via line 147, where it is treated with hydrogen-rich gas fed by conduit 148, to the lower bed 116. The feed may be virgin, cracked or Fischer-Tropsch naphtha and is preheated either alone or with recycle gas to as high a temperature as possible, while avoiding degradation.ALSO: In a process of hydroforming hydrocarbons using a fluidized catalyst, continuously withdrawing a stream of catalyst to a regeneration zone where carbon is burnt off, treating the regenerated catalyst with hydrogen-rich gas, and recycling to the hydroforming zone, the hot regenerated catalyst is cooled with a second stream of catalyst from the hydroforming zone prior to the treatment with hydrogen. The amount of said second stream is sufficient to absorb the heat of reduction and prevent a rise of temperature of the regenerated catalyst on treatment with hydrogen. The regenerated catalyst may be mixed with spent catalyst in a separate hydrogen treatment vessel or the mixture carried by a stream of hydrogen-rich gas to the main reactor. Alternatively, indirect heat exchange may be used, preferably using a reactor having at least two vertically spaced beds connected by downcomers, catalyst being taken from the upper bed to the regenerator and regenerated catalyst recycled to the lower bed. The heated reactor catalyst is recycled to the upper bed whereby a higher temperature is maintained therein, e.g. 900-950 DEG F. compared with 875-900 DEG F. in the lower bed. Regeneration may be at 1050-1200 DEG F., the regenerated catalyst then being cooled to below 1050 DEG F., prior to the hydrogen treatment. Gaseous products of the latter which contain water vapour are preferably separated from the catalyst to prevent deleterious action thereon under hydroforming conditions. For direct mixing, reactor 10, Fig. 1, is provided with conduit 18, whereby spent catalyst is taken to a stripper 19, and thence to regenerator 30. Regenerated catalyst overflows into a stripping cell formed by conduit 37 which connects with conduit 40 and transfer lines 42, 48. Catalyst from the reactor flows by conduits 43, 44 to line 42 where mixing with regenerated catalyst occurs. The hydrogen-containing gas is separated in 49, and catalyst returned by line 51. For indirect heat exchange, reactor 110, Fig. 2, is divided to contain two fluidized beds 116, 117. Catalyst withdrawn from the upper bed passes through stripper 121 and U-line 124 to regenerator 130. Regenerated catalyst is taken by line 136 to heat exchanger 145 where it is cooled by catalyst withdrawn from the reactor by line 137 and passing via stripper 138 and U-line 141 through the exchanger back to the reactor. The cooled, regenerated catalyst passes via line 147, where it is treated with hydrogen-rich gas fed by conduit 148, to the lower bed 116. The feed may be a virgin, cracked or Fischer-Tropsch naphtha and is preheated either alone or with recycle gas to as high a temperature as possible while avoiding degradation.

公开(公告)号：GB729985A

公开(公告)日：1955-05-11

申请号：GB1908153

申请日：1953-07-09

Applicant: STANDARD OIL DEV CO

IPC: C08C19/00 ,  C08C19/06 ,  C08K5/14

Abstract: Synthetic drying oils containing a diolefin polymer, e.g polybutadiene, or copolymer, e.g. with styrene, are heated to 100 DEG to 175 DEG C. in the presence of 0.05 to 1.0 per cent of an organic peroxide, optionally in the presence of maleic anhydride or butyl acrylate as promoter. Peroxides specified are benzoyl, acetyl, methyl ethyl ketone, and t.-butyl peroxides; cumene and t.-butyl hydroperoxides; t.-butyl perbenzoate and bis-(t.-butyl peroxy) butane. The polymer may be prepared in solution in an inert hydrocarbon using metallic sodium as catalyst and specified hydrocarbons are naphtha, straight-run mineral spirits, butane, benzene, cyclohexane, xylenes, toluenes, pentanes and mixtures. Polymerization promoters such as dioxane and its methyl and ethyl homologues, diethyl ether, the diethyl ether of ethylene or diethylene glycol, methanol, isopropanol or n-amyl alcohol, may also be present. The catalyst is destroyed, e.g. with glacial acetic acid, prior to the peroxide treatment. Example 1 illustrates the improvement in drying rate of the treated drying oils plus cobalt and manganese naphthenates. Specification 704,607 is referred to.

公开(公告)号：CA512569A

公开(公告)日：1955-05-03

申请号：CA512569D

Applicant: STANDARD OIL DEV CO

Inventor： STRICKLAND BARNEY R ,  LEWIS EMIL H

公开(公告)号：GB728772A

公开(公告)日：1955-04-27

申请号：GB2826952

申请日：1952-11-10

Applicant: STANDARD OIL DEV CO

IPC: C10M169/00

Abstract: Cracked petrolatum (approximately C18H36) is sulphonated with a ClSO3H ether complex and the reaction product neutralized with NaOH solution. Isopropyl alcohol is added and the solution is desalted with Na2CO3. The supernatant layer is separated, water added and the alcoholic solution extracted with petroleum ether. The alcoholic solution is drum dried to yield a sodium sulphonate having a chlorine content of 4.91 per cent.ALSO:A lubricating grease composition comprises a lubricating oil thickened with from 5-30 per cent. by weight of a metallic soap of an aliphatic sulphonic acid having 10-20 carbon atoms in the aliphatic portion thereof, and which is prepared by the sulphonation of a C10-C20 olefin obtained by the cracking of petroleum wax or petrolatum or by the polymerization of lower olefins. Polymerized olefins from the Fischer synthesis, polyethylenes, polypropylenes and polybutenes may be sulphonated. Unsubstituted or chloro sulphonic acids may be used, and the soap may be an alkali or alkaline earth metal soap. Soaps of high molecular weight fatty acids such as hydrogenated fish oil acids, stearic acid and oleic acid, and salts of low molecular weight acids such as acetic ethoxy-propionic, acrylic and furoic acids may also be added to the composition; the sodium soap of hydrogenated fish oil acids and sodium acetate are referred to. Lubricating oils specified are mineral oils and synthetic oils such as esters of monobasic and dibasic acids, ethers, glycols, glycol ethers, glycol esters and complex esters. Petroleum resins may also be added to the composition. Specification 689,836 is referred to.

公开(公告)号：FR1092698A

公开(公告)日：1955-04-26

申请号：FR1092698D

申请日：1953-12-09

Applicant: STANDARD OIL DEV CO

IPC: C07C51/295

公开(公告)号：CA512346A

公开(公告)日：1955-04-26

申请号：CA512346D

Applicant: STANDARD OIL DEV CO

Inventor： SQUIRES WALTER JR

公开(公告)号：CA512341A

公开(公告)日：1955-04-26

申请号：CA512341D

Applicant: STANDARD OIL DEV CO

Inventor： MACK CHARLES

公开(公告)号：FR1091907A

公开(公告)日：1955-04-15

申请号：FR1091907D

申请日：1953-12-01

Applicant: STANDARD OIL DEV CO

IPC: C08F240/00