FCC process for the maximization of medium distillates

Abstract

A FCC process for the maximization of medium distillates from feedstocks of different sources, by the contact of the feedstock which circulates in a riser reactor together with a fine particulate catalyst from a regenerator ( 6 ), under FCC conditions of maximum LCO, at temperatures between about 480° C. and about 520° C., in the absence of added hydrogen, and with injection of coolant or quench to a riser ascendant R, and where the process consists of the injection of a coolant proportion between about 200 and about 50 kg/m 3 of feedstock, preferably between about 100 and about 50 kg/m 3 of feedstock, in a zone ( 3 ) of the riser ascendant R in a position located between about 25% and about 50% of the height of said riser R above the feedstock inlet mouths ( 2 ), the injection in this position resulting in the increase of the catalyst circulation and the temperature increase in the starting segment of the riser, yielding the production of medium distillates with low aromatic compounds content and bottoms conversion lower than when the coolant injection is employed in the base of the riser R as it is handled in the prior art processes.

1 . A FCC process for the maximization of medium distillates from feedstocks of different sources, in the absence of added hydrogen, using operation conditions for maximum LCO and with introduction of coolant or quench in a riser ascendant reactor R, by the contact of said feedstock which circulates in said riser with a fine particulate catalyst, at temperatures of between about 480° C. and about 520° C. and catalyst-to-oil ratio between about 4 and about 10, yielding lower molecular weight cracking products and coked catalyst, said catalyst after contacting the feedstock being rectified and directed to a regenerator ( 6 ) for coke burning with air ( 8 ), regenerating the catalyst and releasing heat to supply the reaction thermal claim, said process being characterized by the injection of said coolant carried out in a point ( 3 ) of said ascendant reactor R located in a position between about 25% and about 50% of the height of said riser R above the feedstock mouths ( 2 ), the injection at this position bringing about a catalyst circulation increase between about 5% and about 20% and temperature increase in the riser starting segment between about 10° C. and about 30° C., thereby yielding a production of medium distillates of lower aromatic compounds content and where the bottoms conversion is lower than when the injection of said coolant is carried out in the base of said riser R.  
   
   
       2 . Process according to  claim 1 , wherein the feedstocks from different sources consist of petroleum with an °API inferior to 20.  
   
   
       3 . Process according to  claim 2 , wherein the feedstocks consist of vacuum gasoleum, residues or their mixtures in any proportion.  
   
   
       4 . Process according to  claim 1 , wherein the coolant or quench is water or water vapor.  
   
   
       5 . Process according to  claim 1 , wherein the coolant is light naphtha, with a final boiling point of 200° C.-205° C., and a 20w % to 25w % aromatic compounds content.  
   
   
       6 . Process according to  claim 1 , wherein the proportion of coolant in relation to the feedstock lies between about 200 kg/m 3  and about 50 kg/m 3  of feedstock, preferably between about 100 kg/m 3  and about 50 kg/m 3  of feedstock.  
   
   
       7 . Process according to  claim 1 , wherein the catalyst is a cracking catalyst of low acidity and reduced hydrogen transference.  
   
   
       8 . Process according to  claim 1 , wherein it leads to a bottoms conversion increase, but keeping the same aromatic compounds content of the LCO, regarding the prior art processes.  
   
   
       9 . Process according to  claim 1 , wherein it reaches temperature levels from about 670° C. to about 710° C. in the mixture zone, in low severity operations, with reaction temperature in the range from about 480° C. to about 520° C.  
   
   
       10 . A FCC process for the maximization of medium distillates from feedstocks of different sources comprising: 
 introducing a coolant or quench in a riser ascendant reactor,    contacting said feedstocks, which are introduced into said riser through feedstock mouths and which circulate in said riser, with a fine particulate catalyst, at temperatures of between about 480° C. and about 520° C. and catalyst-to-oil ratio between about 4 and about 10,    producing lower molecular weight cracking products and coked catalyst, and said catalyst after contacting the feedstock being rectified and directed to a regenerator for coke burning with air,    regenerating the catalyst and releasing heat to supply a reaction thermal claim, and    wherein the coolant or quench is injected in a point of said riser ascendant reactor located in a position between about 25% and about 50% of the height of said riser above the feedstock mouths, the injection at this position bringing about a catalyst circulation increase between about 5% and about 20% and temperature increase in the riser starting segment between about 10° C. and about 30° C., thereby yielding a production of medium distillates of lower aromatic compounds content and where the bottoms conversion is lower than when the injection of said coolant is carried out in a base of said riser.    
   
   
       11 . Process according to  claim 10  wherein the feedstocks from different sources consist of petroleum with an °API inferior to 20.  
   
   
       12 . Process according to  claim 11 , wherein the feedstocks consist of vacuum gasoleum, residues or their mixtures in any proportion.  
   
   
       13 . Process according to  claim 10 , wherein the coolant or quench is water or water vapor.  
   
   
       14 . Process according to  claim 10 , wherein the coolant is light naphtha, with a final boiling point of 200° C.-205° C., and a 20w % to 25w % aromatic compounds content.  
   
   
       15 . Process according to  claim 10 , wherein the proportion of coolant in relation to the feedstock lies between about 200 kg/m 3  and about 50 kg/m 3  of feedstock, preferably between about 100 kg/m 3  and about 50 kg/m 3  of feedstock.  
   
   
       16 . Process according to  claim 10 , wherein the catalyst is a cracking catalyst of low acidity and reduced hydrogen transference.  
   
   
       17 . Process according to  claim 10 , wherein it reaches temperature levels from about 670° C. to about 710° C. in the mixture zone, in low severity operations, with reaction temperature in the range from about 480° C. to about 520° C.  
   
   
       18 . A FCC process for the maximization of medium distillates from feedstock comprising: 
 introducing a coolant or quench in a riser ascendant reactor,    contacting said feedstock, which are introduced into said riser through a feedstock mouth and which circulate in said riser, with a fine particulate catalyst, and    wherein the coolant or quench is injected in a point of said riser ascendant reactor located in a position between about 25% and about 50% of the height of said riser above the feedstock mouths, the injection at this position bringing about a catalyst circulation increase between about 5% and about 20% and temperature increase in the riser starting segment between about 10° C. and about 30° C., thereby yielding a production of medium distillates of lower aromatic compounds content and where the bottoms conversion is lower than when the injection of said coolant is carried out in a base of said riser.    
   
   
       19 . Process according to  claim 18 , wherein the feedstocks from different sources consist of petroleum with an °API inferior to 20.  
   
   
       20 . Process according to  claim 19 , wherein the feedstocks consist of vacuum gasoleum, residues or their mixtures in any proportion.  
   
   
       21 . Process according to  claim 18 , wherein the coolant or quench is water or water vapor.  
   
   
       22 . Process according to  claim 18 , wherein the coolant is light naphtha, with a final boiling point of 200° C.-205° C., and a 20w % to 25w % aromatic compounds content.  
   
   
       23 . Process according to  claim 18 , wherein the proportion of coolant in relation to the feedstock lies between about 200 kg/m 3  and about 50 kg/m 3  of feedstock, preferably between about 100 kg/m 3  and about 50 kg/m 3  of feedstock.  
   
   
       24 . Process according to  claim 18 , wherein the catalyst is a cracking catalyst of low acidity and reduced hydrogen transference.  
   
   
       25 . Process according to  claim 18 , wherein it reaches temperature levels from about 670° C. to about 710° C. in the mixture zone, in low severity operations, with reaction temperature in the range from about 480° C. to about 520° C.