Lube hydroisomerization system

Abstract

The present invention relates to a process for converting wax with a heavy component to high quality lube basestocks using a unidimensional intermediate pore molecular sieve with near circular pore structures having an average diameter of 0.50 nm to 0.65 nm wherein the difference between the maximum diameter and the minimum is ≦0.05 nm followed by a molecular sieve Zeolite Beta catalyst. Both catalysts comprise one or more Group VIII metals. For example, a cascaded two-bed catalyst system consisting of a first bed Pt/ZSM-48 catalyst followed by a second bed Pt/Beta catalyst improves processing of heavy lubes.

1 . A process for converting a wax, having hydrocarbons primarily within C 24 -C 110  with essentially no sulfur or nitrogen content, to an isoparaffinic lube basestock, comprising: 
 first, passing the wax and a hydrogen co-feed over a unidimensional molecular sieve catalyst comprising a unidimensional intermediate pore molecular sieve with near circular pore structures having an average diameter of 0.50 nm to 0.65 nm wherein the difference between a maximum diameter and a minimum diameter is ≦0.05 nm and one or more Group VIII metals to form an intermediate product; and    second, passing the intermediate product over a Beta catalyst comprising a Zeolite Beta and one or more Group VIII metals; to form the isoparaffinic lube basestock.    
     
     
         2 . A process according to  claim 1 , wherein 
 the wax comprises about 5 wt % to about 80 wt % of a 1,100° F.+ fraction, based on the total weight of the wax;    the unidimensional molecular sieve catalyst is kept at a temperature of 500 to 800° F. (260 to 427° C.);    the Beta catalyst is kept at a temperature of 400 to 700° F. (204 to 371° C.);    the wax is passed over the unidimensional molecular sieve catalyst at a feed liquid hourly space velocity of 0.1 to 10 h −1 ;    the intermediate product is passed over the Beta catalyst at a feed liquid hourly space velocity of 0.1 to 10 h −1 ; and    the process further comprises less than about 1,500 psig (102 atm) hydrogen, wherein the hydrogen is circulated at 100 to 10,000 scf/bbl (18 to 1780 n.L.L −1 ).    
     
     
         3 . A process according to  claim 2 , wherein 
 the unidimensional molecular sieve catalyst is kept at a temperature of 600-700° F. (316 to 371° C.);    the Beta catalyst is kept at a temperature of 500-600° F. (260 to 316° C.);    the wax is passed over the unidimensional molecular sieve catalyst at a feed liquid hourly space velocity of 0.5 to 2 h −1 ;    the intermediate product is passed over the Beta catalyst at a feed liquid hourly space velocity of 0.5 to 2 h −1 ; and    the process further comprises less than about 1,500 psig (102 atm) hydrogen, wherein the hydrogen is circulated at 1,000 to 6,000 scf/bbl (178 to 1068 n.L.L −1 ).    
     
     
         4 . A process according to  claim 3 , wherein the Group VIII metal on said catalysts is at least one member selected from the group consisting of Pt and Pd; and the unidimensional molecular sieve catalyst is ZSM-48 with a Alpha value of 10 to 50 prior to the metal incorporation.  
     
     
         5 . A process according to  claim 3 , wherein 
 the wax has a 1,000° F.+ high temperature tail;    the ZSM-48 is loaded with about 0.5 wt % to about 1 wt % of the Group VIII metal, based on the total weight of the ZSM-48;    the Zeolite Beta has an Alpha value less than about 15 prior to loading with the Group VIII metal;    the Zeolite Beta is loaded with about 0.5 wt % to about 1 wt % of the Group VIII metal, based on the total weight of the Zeolite Beta; and    the Group VIII metal is at least one member selected from the group consisting of Pt and Pd.    
     
     
         6 . A process according to  claim 5 , wherein 
 the Beta catalyst is Pt/Beta; and    the Pt/ZSM-48 and the Pt/Beta are in a cascaded two-bed catalyst system comprising a first bed followed by a second bed, wherein the first bed comprises the Pt/ZSM-48 catalyst and the second bed comprises the Pt/Beta catalyst.    
     
     
         7 . A process according to  claim 6 , wherein 
 the temperature of the first bed and the temperature of the second bed are controlled independently; and    the intermediate product is cascaded directly to the second bed.    
     
     
         8 . An isoparaffinic lube basestock made by the process according to  claim 1 , wherein 
 the isoparaffinic lube basestock has a viscosity index of at least 150 at a −20° C. lube pour point and a viscosity index of at least 130 at a pour point of no more than −50° C.    
     
     
         9 . An isoparaffinic lube basestock made by the process according to  claim 1 , wherein the isoparaffinic lube basestock has less than 1 wt % aromatic content.  
     
     
         10 . A lubricant with a viscosity index of at least 150 at a −20° C. lube pour point and a viscosity index of at least 130 at a pour point of no more than −50° C. made by the process according to  claim 1 .  
     
     
         11 . A lubricant with a viscosity index of at least 150 at a −20° C. lube pour point and a viscosity index of at least 130 at a pour point of no more than −50° C. made by the process according to  claim 6 .  
     
     
         12 . A process according to  claim 1 , wherein the passing of the wax and the intermediate product over said catalysts is conducted under conditions sufficient to form an isoparaffinic lube basestock with a viscosity index of at least 150 at a −20° C. lube pour point and a viscosity index of at least 130 at a pour point of no more than −50° C.  
     
     
         13 . A process according to  claim 5 , wherein the passing of the wax and the intermediate product over said catalysts is conducted under conditions sufficient to form an isoparaffinic lube basestock with a viscosity index of at least 150 at a −20° C. lube pour point and a viscosity index of at least 130 at a pour point of no more than −50° C.