EP-4735559-A1 - PROCESS FOR CONVERTING OLEFINS TO JET FUEL WITH PARALLEL REACTORS

Abstract

A process for oligomerizing an olefin stream comprising charging a light olefin vapor stream comprising ethylene to a first oligomerization reactor containing a first oligomerization catalyst to produce a first oligomerized stream. A heavy olefin liquid stream comprising C3- C8 olefin liquids stream is charged to a second oligomerization reactor containing a second oligomerization catalyst to produce a second oligomerized stream. The two oligomerized streams can be processed to recover fuel streams together.

Inventors

• MATHUR, ASHISH
• CHAKRABARTI, Debanjan
• PAUSTIAN, JOEL S.
• BLOMMEL, JEANNIE MEE
• HOEHN, RICHARD K.

Assignees

• UOP LLC

Dates

Publication Date

20260506

Application Date

20240815

Claims (10)

1. 1. A process for oligomerizing an olefin stream comprising: charging a light olefin stream comprising a vaporous C2 olefin stream to a first oligomerization reactor containing a first oligomerization catalyst to produce a light oligomerized stream; and charging a heavy olefin stream comprising a liquid C3+ olefins stream to a second oligomerization reactor containing a second oligomerization catalyst to produce a heavy oligomerized stream.
2. 2. The process of claim 1 wherein said light olefin stream is expanded to provide an expanded light olefin stream and a light liquid stream is separated from said expanded light olefin stream to provide a dry light olefin stream and said light liquid stream is added to said heavy olefin stream to provide a supplemented heavy olefin stream.
3. 3. The process of claim 1 wherein said light olefin stream is compressed to provide a compressed light olefin stream before it is charged to said first oligomerization reactor.
4. 4. The process of claim 1 wherein said light olefin stream is split into a first light olefin stream and a second light olefin stream; and the first light olefin stream is charged to a first catalyst bed in said first oligomerization reactor and the second light olefin stream is charged to a second catalyst bed in said first oligomerization reactor.
5. 5. The process of claim 4 wherein a paraffinic diluent stream is added to said first light olefin stream to provide a dilute first light olefin stream and charging said dilute first light olefin stream to said first oligomerization reactor.
6. 6. The process of claim 5 wherein said first light olefin stream contacts said first oligomerization catalyst in said first catalyst bed in said first oligomerization reactor and produces a first light oligomerized stream; the first light oligomerized stream mixes with the second light olefin stream to provide a dilute second light olefin stream and said dilute second light olefin stream is charged to said second catalyst bed in said first oligomerization reactor.
7. 7. The process of claim 2 wherein said supplemented second stream is charged to said second oligomerization reactor.
8. 8. The process of claim 1 wherein said heavy olefin stream is split into a first heavy olefin stream and a second heavy olefin stream; and the first heavy olefin stream is charged to a first catalyst bed in said second oligomerization reactor and the second heavy olefin stream is charged to a second catalyst bed in said second oligomerization reactor.
9. 9. The process of claim 7 wherein a paraffinic diluent stream is added to said supplemented heavy olefin stream to provide a diluted heavy olefin stream and charging said diluted heavy olefin stream to said second oligomerization reactor.
10. 10. The process of claim 9 comprising recycling a first unreacted olefin stream to said first heavy olefin stream to provide an augmented first heavy olefin stream and charging said augmented first heavy olefin stream to said first catalyst bed in said second oligomerization reactor and recycling a second unreacted olefin stream to said second heavy olefin stream to provide an augmented second heavy olefin stream and charging said augmented second heavy olefin stream to said second catalyst bed in said second oligomerization reactor.

Description

PROCESS FOR CONVERTING OLEFINS TO JET FUEL WITH PARALLEL REACTORS [0001] The field is the conversion of olefins to distillate. The field may particularly relate to oligomerizing olefins to distillate fuels. BACKGROUND [0002] Molecular sieves such as microporous crystalline zeolite and non-zeolitic catalysts, particularly silicoaluminophosphates (SAPO), are known to promote the conversion of oxygenates such as methanol to light olefins. The highly efficient Methanol to Olefin (MTO) process may convert oxygenates to light olefins which had been typically considered for plastics production. Light olefins produced from the MTO process is highly concentrated in ethylene and propylene. [0003] The ethanol dehydration process involves dehydration of ethanol molecules to generate ethylene and water. The process of converting ethanol to ethylene is endothermic in nature and the heat of endothermicity is typically provided by fired heaters that are adiabatic in nature. Dehydration reactors are adiabatic. Adiabatic reactor systems may have drawbacks such as selectivity to undesired products, potential underutilization of catalyst, higher utility consumption and larger plot space. [0004] Ethylene can be dimerized and oligomerized into olefins such as C4, C6 and C8 olefins. Propylene can be dimerized and oligomerized into olefins such as C6, C9 and C12 olefins. Olefin oligomerization is a process that can oligomerize smaller olefins into larger olefins. More specifically, it can convert olefins including dimerized olefins into distillates including jet fuel and diesel range products. The oligomerized distillate can be saturated for use as transportation fuels. [0005] Jet fuel is one of the few petroleum fuels that cannot be replaced easily by electrical motor systems because a high energy output is required to fuel planes which cannot be supplied with electric motors. Jet fuel has an end point boiling specification of less than 300°C using ASTM D86. Large incentives are currently available for green jet fuel in certain regions. [0006] An efficient process is desired for converting renewable feeds to distillate fuels. BRIEF SUMMARY [0007] We have formulated a process for oligomerizing an olefin stream to distillate fuel. A process for oligomerizing an olefin stream comprising charging a light olefin vapor stream comprising ethylene to a first oligomerization reactor containing a first oligomerization catalyst to produce a first oligomerized stream. A heavy olefin liquid stream comprising a C3-C8 olefin liquid stream is charged to a second oligomerization reactor containing a second oligomerization catalyst to produce a second oligomerized stream. The two oligomerized streams can be processed to recover fuel streams together. BRIEF DESCRIPTION OF THE DRAWINGS [0008] FIG. 1 is a schematic drawing of an oligomerization section of a process and apparatus of the present disclosure. [0009] FIG. 2 is a schematic drawing of a hydrogenation section of a process and apparatus of the present disclosure. DEFINITIONS [0010] The term “communication” means that fluid flow is operatively permitted between enumerated components, which may be characterized as “fluid communication”. [0011] The term “downstream communication” means that at least a portion of fluid flowing to the subject in downstream communication may operatively flow from the object with which it fluidly communicates. [0012] The term “upstream communication” means that at least a portion of the fluid flowing from the subject in upstream communication may operatively flow to the object with which it fluidly communicates. [0013] The term “direct communication” means that fluid flow from the upstream component enters the downstream component without passing through any other intervening vessel. [0014] The term “indirect communication” means that fluid flow from the upstream component enters the downstream component after passing through an intervening vessel. [0015] The term “bypass” means that the object is out of downstream communication with a bypassing subject at least to the extent of bypassing. [0016] As used herein, the term “predominant” or “predominate” means greater than 50%, suitably greater than 75% and preferably greater than 90%. [0017] The term “column” means a distillation column or columns for separating one or more components of different volatilities. Unless otherwise indicated, each column includes a condenser on an overhead of the column to condense and reflux a portion of an overhead stream back to the top of the column and a reboiler at a bottom of the column to vaporize and send a portion of a bottoms stream back to the bottom of the column. Feeds to the columns may be preheated. The top pressure is the pressure of the overhead vapor at the vapor outlet of the column. The bottom temperature is the liquid bottom outlet temperature. Overhead lines and bottoms lines refer to the net lines from the column downstream of any reflux or reboil to the colum