Hydroprocessing in multiple beds with intermediate flash zones

Abstract

The instant invention comprises a hydroprocessing method having at least two stages. The first stage employs a hydroprocessing catalyst which may contain hydrotreating catalyst, hydrocracking catalyst, or a combination of both. The subsequent stage is limited to hydrocracking. Conversion in subsequent stages may be improved by the addition of multiple reaction zones for hydrocracking, with flash separation zones between the stages. Middle distillate yield is thereby increased and the volume of the recycle stream is reduced. This invention reduces the need for equipment which would normally be required for a large recycle stream.

1 . The hydroprocessing method of the instant invention, which has at least two reaction stages, comprises the following steps:
 (a) passing a hydrocarbon feed into a first reaction stage which is maintained at hydroprocessing conditions, where it is contacted with a catalyst in at least one fixed bed and at least a portion of the feed is converted;   (b) passing the effluent of step (a) to a hot high pressure separation zone;   (c) separating the stream of step (b) into an unconverted liquid effluent and a stream comprising converted products having boiling points below that of the feed, said products being subsequently passed to fractionation;   (d) passing the unconverted liquid effluent from step (c) to a second reaction stage, said stage comprising a plurality of reaction zones, wherein each zone is maintained at hydrocracking conditions and separation occurs between each zone;   (e) contacting the feed in the first reaction zone of step (d) with a catalyst in a fixed bed, thereby converting at least a portion of the feed;   (f) separating the effluent of step (e) into an unconverted liquid effluent, and a hydrogen-rich converted stream;   (g) passing the unconverted liquid effluent from step (f) to a second reaction zone of the second stage, the zone being maintained at hydrocracking conditions;   (h) contacting the feed in the second reaction zone of step (g) with a catalyst in a fixed bed, thereby converting at least a portion of the feed;   (i) fractionating the effluent of step (h) to produce one or more middle distillate product streams.   
   
   
       2 . The process of  claim 1 , wherein fresh feed may be combined with the unconverted liquid effluent of step (c) before entering the second reactor stage. 
   
   
       3 . The process of  claim 1 , wherein the second reaction stage may comprise a reactor having multiple catalyst beds. 
   
   
       4 . The process of  claim 1 , wherein the second reaction stage may comprise several small, single bed reactors in series. 
   
   
       5 . The process of  claim 1 , wherein the inlet temperature of each reaction zone in the second stage subsequent to the first reaction zone is lower than the previous one and the outlet temperature of each reaction zone subsequent to the first reaction zone is lower than the previous one. 
   
   
       6 . The process of  claim 5 , wherein the average reaction temperature of each reaction zone subsequent to the first reaction zone is at least 50 F lower than the average reaction temperature of the previous one. 
   
   
       7 . The process of  claim 1 , wherein the catalyst of each reaction zone of the second stage is a hydrocracking catalyst. 
   
   
       8 . The process of  claim 7 , in which the catalyst in each bed subsequent to the first one in the second stage reaction zone demonstrates increasing activity. 
   
   
       9 . The process of  claim 7 , wherein each of the reaction zones of the second stage is operated under hydrocracking conditions including temperatures in the range from about 400-950 F (204-510 C), reaction pressure in the range from 500 through 5000 psig (3.5-34.5 MPa), LHSV of 0.1 to 15 hr (−1), and hydrogen consumption of 500 through 2500 scf per barrel of liquid hydrocarbon feed (89.1-445 m 3  H 2  feed). 
   
   
       10 . The process of  claim 9 , wherein more preferred hydrocracking conditions include a temperature range from 650-850 F (343 C.-454 C), reaction pressure from 1500 psig through 3500 psig (10.4-24.2 MPa) and LHSV 0.25 through 2.5 hr (−1), and hydrogen consumption of 500 through 2500 scf per barrel of liquid hydrocarbon feed (89.1-445 m 3  H 2  feed). 
   
   
       11 . The process of  claim 1 , wherein the unconverted effluent comprises hydrocarbons which boil above 700 F. 
   
   
       12 . The process of  claim 1 , wherein the converted stream comprises hydrocarbons boiling below 700 F. 
   
   
       13 . The process of  claim 1 , wherein one or more side vessels comprises hydroprocessing catalyst for further upgrading. 
   
   
       14 . The process of  claim 12 , wherein the converted stream from each reaction zone may be fractionated separately or be combined, then fractionated into at least one fuel product. 
   
   
       15 . The process of  claim 1 , wherein at least two of the reaction stages operate within a single high-pressure hydrogen loop. 
   
   
       16 . The process of  claim 15 , wherein the reaction stages operate at different pressure and conversion levels. 
   
   
       17 . The process of  claim 14 , wherein the preferred fuel product is diesel. 
   
   
       18 . The process of  claim 14 , wherein the preferred fuel product is jet fuel. 
   
   
       19 . The process of  claim 14 , wherein the preferred fuel product is naphtha. 
   
   
       20 . The process of  claim 1 , wherein the feed is subjected to a preliminary hydrotreating step.