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    Method and apparatus for continuous grease manufacture
    6.
    发明授权
    Method and apparatus for continuous grease manufacture 失效
    连续润滑脂制造的方法和装置

    公开(公告)号：US3475335A

    公开(公告)日：1969-10-28

    申请号：US3475335D

    申请日：1967-06-15

    Applicant: TEXACO INC

    Inventor： GREENE JOHN H ,  HENCKE WILLIAM R ,  DOWDEN CLARENCE L JR ,  PITMAN HERBERT J

    IPC: C10M117/02 ,  B01F5/10 ,  C10M169/00 ,  C10M177/00 ,  C10N10/00 ,  C10N40/00 ,  C10N50/10 ,  C10M5/16

    CPC classification number: C10M5/00 ,  C10M2201/02 ,  C10M2207/022 ,  C10M2207/121 ,  C10M2207/122 ,  C10M2207/124 ,  C10M2207/125 ,  C10M2207/128 ,  C10M2207/129 ,  C10M2207/282 ,  C10M2207/34 ,  C10N2210/00 ,  C10N2210/01 ,  C10N2210/02 ,  C10N2210/03 ,  C10N2210/04 ,  C10N2250/10 ,  C10N2270/00 ,  C10N2270/02

    Abstract: In a continuous process for manufacturing lubricating grease including soap grease, saponifiable material and metal base are reacted in a reaction zone; the reaction product is dehydrated in a dehydration zone and the mixture is recycled from the bottom to the top of the dehydration zone through a shear valve so that the soap is simultaneously conditioned. Predetermined amounts of lubricating oil are added at each stage, but a lubricating oil hydrolysable under saponification conditions would not be added at this stage. The metal base may be the oxide, hydroxide or carbonate of an alkali metal, alkaline earth metal, magnesium, zinc, cobalt, manganese, aluminium or lead; the saponifiable material may be a fatty acid having 12 to 32 carbon atoms or an ester thereof, or a mixture thereof with a fatty acid having 1 to 6 carbon atoms; the lubricating oil may be a naphthenic and/or paraffinic mineral oil, a synthetic oil obtained by cracking a polymerization or a high molecular weight ether or ester, diesters such as di-2-ethylhexyl sebacate, or a mixture of any of the foregoing. As shown, saponifiable material, optionally containing lubricating oil, is introduced from tank 15, metal base in aqueous solution or oil slurry from tank 20, and lubricating oil mainly from tank 40 and, optionally, when more than one oil is to be used, tank 60. As shown, the lubricating oil may be introduced into the system at a number of points. The mixture is recycled through tubular reaction zone 1 by means of line 7 and pump 10 at a velocity giving highly turbulent flow, reaction taking place at 10-300 p.s.i.g. at 180 DEG F. or above. The reaction product is passed via line 26 and pump 27 to dehydration zone 30, maintained therein at above 225 DEG F. and recycled from bottom to top of the zone by pump 34 through shear valve 37 having a pressure drop of 10 to 200 p.s.i.g. across it. The volume of recycled grease mixture during the average residence time in the dehydration zone is at least five times the total average volume of mixture in the zone. Lubricating oil added at this stage comprises at least 25% of the mixture. The dehydrated grease mixture is withdrawn from line 33 via line 75, and oil added at this stage, comprising up to 90% of the total oil content, is advantageously used to cool the mixture. Also added at this stage are additives, from tank 90 and, in the case of cup greases, water of stabilization. The mixture is circulated through shear valve 81 and, if necessary, cooler 85. The product grease is taken off via line 87 and a further valve 88 after final required addition of oil have been made via line 71 and pump 72.

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