Process to prepare a haze free base oil

Abstract

Process to prepare a haze free base oil having a kinematic viscosity at 100° C. of greater than 10 cSt from a Fischer-Tropsch wax feed by performing the following steps, (a) reducing the wax content of the feed by contacting the feed with a hydroisomerisation catalyst under hydroisomerisation conditions at a remote location, (b) transporting an intermediate product having a reduced wax content as obtained in step (a) from one location to another location, and (c) solvent dewaxing the transported intermediate product to obtain the haze free base oil at the location closer to the end-user.

1 . A process to prepare a haze free base oil having a kinematic viscosity at 100° C. of greater than 10 cSt from a Fischer-Tropsch wax feed comprising the following steps: 
 (a) reducing the wax content of a Fischer-Tropsch wax feed by contacting the feed with a hydroisomerisation catalyst under hydroisomerisation conditions at a remote location to form an intermediate product;    (b) transporting the intermediate product having the reduced wax content as obtained in step (a) from the remote location to another location closer to the end-user; and    (c) solvent dewaxing the transported intermediate product to obtain the a haze free base oil at the location closer to the end-user.    
     
     
         2 . The process according to  claim 1 , wherein the feed to step (a) has a 10 wt % recovery boiling point of above 500° C. and a wax content of greater than 50 wt %.  
     
     
         3 . The process according to  claim 2 , wherein the wax content in the feed is between 60 and 95 wt %.  
     
     
         4 . The process according to  claim 2 , wherein the 10 wt % recovery boiling point of the feed is between 500 and 550° C.  
     
     
         5 . The process according to  claim 1 , wherein the wax content in the intermediate product is between 10 and 35 wt %.  
     
     
         6 . The process according to  claim 1 , wherein the intermediate product has a congealing point of between 20 and 60° C.  
     
     
         7 . The process according to  claim 1 , wherein more than 50 wt % of the intermediate product boils above the 10 wt % recovery point of the feed used in step (a).  
     
     
         8 . The process according to  claim 7 , wherein more than 70 wt % of the intermediate product boils above the 10 wt % recovery point of the feed used in step (a).  
     
     
         9 . The process according to  claim 1 , wherein the hydroisomerisation catalyst used in step (a) is a substantially amorphous based catalyst comprising a silica-alumina carrier and a noble or non-noble Group VIII metal.  
     
     
         10 . The process according to  claim 1 , wherein the hydroisomerisation catalyst used in step (a) is a molecular sieve based catalyst and a noble or non-noble Group VIII metal.  
     
     
         11 . The process according to  claim 1 , wherein step (b) is performed by means of a ship and wherein containers on the ship are first purged with nitrogen before loading and wherein the nitrogen is obtained in an air-separation unit which unit also isolates oxygen for use to make syngas which in turn is used as feedstock to prepare the Fischer-Tropsch wax feed.  
     
     
         12 . A process to prepare a lubricant composition not containing a viscosity modifier additive by blending a low viscosity base oil with a haze free base oil having a kinematic viscosity at 100° C. of greater than 10 cSt from a Fischer-Tropsch wax feed prepared by a process comprising the following steps: 
 (a) reducing the wax content of a Fischer-Tropsch wax feed by contacting the feed with a hydroisomerisation catalyst under hydroisomerisation conditions at a remote location to form an intermediate product;    (b) transporting the intermediate product having the reduced wax content as obtained in step (a) from the remote location to another location closer to the end-user; and    (c) solvent dewaxing the transported intermediate product to obtain a haze free base oil at the location closer to the end-user.    
     
     
         13 . The process according to  claim 12 , wherein the feed to step (a) has a 10 wt % recovery boiling point of above 500° C. and a wax content of greater than 50 wt %.  
     
     
         14 . The process according to  claim 12 , wherein the wax content in the feed is between 60 and 95 wt %.  
     
     
         15 . The process according to  claim 12 , wherein the 10 wt % recovery boiling point of the feed is between 500 and 550° C.  
     
     
         16 . The process according to  claim 12 , wherein the wax content in the intermediate product is between 10 and 35 wt %.  
     
     
         17 . The process according to  claim 12 , wherein the intermediate product has a congealing point of between 20 and 60° C.  
     
     
         18 . The process according to  claim 12 , wherein more than 50 wt % of the intermediate product boils above the 10 wt % recovery point of the feed used in step (a).  
     
     
         19 . The process according to  claim 12 , wherein more than 70 wt % of the intermediate product boils above the 10 wt % recovery point of the feed used in step (a).  
     
     
         20 . The process according to  claim 12 , wherein the hydroisomerisation catalyst used in step (a) is a substantially amorphous based catalyst comprising a silica-alumina carrier and a noble or non-noble Group VIII metal.  
     
     
         21 . The process according to  claim 12 , wherein the hydroisomerisation catalyst used in step (a) is a molecular sieve based catalyst and a noble or non-noble Group VIII metal.  
     
     
         22 . The process according to  claim 12 , wherein step (b) is performed by means of a ship and wherein containers on the ship are first purged with nitrogen before loading and wherein the nitrogen is obtained in an air-separation unit which unit also isolates oxygen for use to make syngas which in turn is used as feedstock to prepare the Fischer-Tropsch wax feed.