Heat reduction in alkylation process

Patent metadata

Field	Value
Publication number	US-10131591-B2
Application number	US-201715857175-A
Country	US
Kind code	B2
Filing date	Dec 28, 2017
Priority date	Dec 28, 2016
Publication date	Nov 20, 2018
Grant date	Nov 20, 2018

Abstract

Processes using mid-column reboilers in at least one benzene separation columns to reduce the heat duty in alkylation processes are provided. The feed to the aromatics removal zone may exchange heat in a mid-column reboiler in the benzene separation column in the alkylbenzene separation zone followed by exchanging heat in a mid-column reboiler in the benzene separation column in the aromatics removal zone. This arrangement minimizes the hot oil duty on the reboilers in both benzene separation columns.

First claim

What is claimed is:

1. A method of heat integration in a process for producing alkylbenzene comprising:
dehydrogenating an n-paraffin rich stream in a dehydrogenation zone under dehydrogenation conditions to form a first dehydrogenated stream comprising n-paraffins, mono-olefins, di-olefins, and aromatics, the dehydrogenated stream having a first temperature;
removing heat from at least a portion of the first dehydrogenated stream in a mid-column reboiler in a first benzene separation column to form a second dehydrogenated stream, the portion of the first dehydrogenated stream having a first temperature in a range of about 150° C. to about 250° C., the second dehydrogenated stream having a second temperature lower than the first temperature, the mid-column reboiler positioned such that the second temperature is in a range of about 135° C. to about 165° C.;
removing the aromatics from the second dehydrogenated stream in an aromatics removal zone to form an aromatics stream, a mono-olefin stream, and a first benzene stream, the aromatics removal zone comprising at least one aromatics removal unit and a second benzene separation column;
alkylating benzene with the mono-olefin stream in an alkylation zone under alkylation conditions to provide an alkylation effluent stream comprising alkylbenzene, benzene, and n-paraffins; and
separating the alkylation effluent stream into an alkylbenzene stream and a second benzene stream in an alkylbenzene separation zone comprising the first benzene separation column.

2. The method of claim 1 further comprising:
removing heat from the second dehydrogenated stream in a mid-column reboiler in the second benzene separation column to form a third dehydrogenated stream having a third temperature lower than the second temperature before removing the aromatics from the second dehydrogenated stream, and wherein removing the aromatics from the second dehydrogenated stream comprises removing the aromatics from the third dehydrogenated stream, the mid-column reboiler positioned such that the third temperature is in a range of about 110° C. to about 140° C.

3. The method of claim 2 further comprising:
removing heat from the third dehydrogenated stream in a heat exchanger using the first benzene stream to form a fourth dehydrogenated stream having a fourth temperature lower than the third temperature before removing the aromatics from the second dehydrogenated stream, and wherein removing the aromatics from the second dehydrogenated stream comprises removing the aromatics from the fourth dehydrogenated stream.

4. The method of claim 1 further comprising:
selectively hydrogenating the first dehydrogenated stream to remove at least a portion of the di-olefins forming a selectively hydrogenated stream before removing heat from the portion of the first dehydrogenated stream; and
separating the selectively hydrogenated stream into a light ends stream and a bottoms stream, wherein the bottoms stream comprises the portion of the first dehydrogenated stream.

5. The method of claim 1 wherein the alkylbenzene separation zone further comprises a paraffin separation column, and wherein separating the alkylation effluent stream into the alkylbenzene stream and the second benzene stream comprises:
separating the alkylbenzene effluent into a first alkylbenzene stream and the second benzene stream in the first benzene separation column, wherein the first alkylbenzene stream comprises alkylbenzene and n-paraffins;
separating the first alkylbenzene stream into an n-paraffin stream and a second alkylbenzene stream in the paraffin separation column; and
recycling the n-paraffin stream to the dehydrogenation zone.

6. The method of claim 5 wherein the alkylbenzene separation zone further comprises an alkylbenzene separation column, further comprising:
separating the second alkylbenzene stream in the alkylbenzene separation column into a linear alkylbenzene stream and a heavy alkylate stream.

7. The method of claim 1 wherein the aromatics removal zone comprises at least two aromatics removal units.

8. The method of claim 7 wherein one aromatics removal unit is regenerated with the first benzene stream while the second aromatics removal unit removes the aromatics from the second dehydrogenated stream.

9. The method of claim 7 wherein the at least two aromatics removal units are in a swing bed arrangement.

10. The method of claim 1 wherein the at least one aromatics removal unit comprises an adsorption bed.

11. The method of claim 1 wherein the n-paraffin rich stream comprises an n-paraffin rich stream from an adsorptive separation process, or an n-paraffin rich stream produced from a renewable feedstock.

12. The process of claim 1 further comprising:
introducing a kerosene feed stream into a fractionation zone to form a fraction comprising hydrocarbons having between 10 and 13 carbon atoms;
hydrotreating the fraction; and
separating the hydrotreated fraction in an adsorptive separation zone to form the n-paraffin rich stream and an isoparaffin rich stream.

13. The method of claim 1 further comprising at least one of:
recycling the first benzene stream to the aromatics removal zone; and
recycling the second benzene stream to the alkylation zone.

14. A method of heat integration in a process for producing alkylbenzene comprising:
dehydrogenating an n-paraffin rich stream in a dehydrogenation zone under dehydrogenation conditions to form a first dehydrogenated stream comprising n-paraffins, mono-olefins, di-olefins, and aromatics, the dehydrogenated stream having a first temperature;
removing heat from at least a portion of the first dehydrogenated stream in a mid-column reboiler in a first benzene separation column to form a second dehydrogenated stream, the portion of the first dehydrogenated stream having a first temperature in a range of about 150° C. to about 250° C., the second dehydrogenated stream, the second dehydrogenated stream having a second temperature lower than the first temperature, the second temperature being in a range of about 135° C. to about 165° C.;
removing heat from the second dehydrogenated stream in a mid-column reboiler in a second benzene separation column to form a third dehydrogenated stream having a third temperature lower than the second temperature, the third temperature being in a range of about 110° C. to about 140° C.;
removing the aromatics from the third dehydrogenated stream in an aromatics removal zone to form an aromatics stream, a mono-olefin stream, and a first benzene stream, the aromatics removal zone comprising at least one aromatics removal unit and the second benzene separation column;
alkylating benzene with the mono-olefin stream in an alkylation zone under alkylation conditions to provide an alkylation effluent stream comprising alkylbenzene, benzene, and n-paraffins;
separating the alkylation effluent stream into an alkylbenzene stream and a second benzene stream in an alkylbenzene separation zone comprising the first benzene separation column;
recycling the first benzene stream to the aromatics removal zone; and
recycling the second benzene stream to the alkylation zone.

15. The method of claim 14 further comprising:
removing heat from the third dehydrogenated stream in a heat exchanger using the first benzene stream to form a fourth dehydrogenated stream having a fourth temperature lower than the third temperature before removing the aromatics from the third dehydrogenated stream, and wherein removing the aromatics from the third dehydrogenated stream comprises removing the aromatics from the fourth dehydrogenated stream.

Assignees

• Uop Llc
• Compania Espanola De Petroleos S A U
• Uop Llc

Inventors

• Siedler Nathan
• Luebke Charles P
• Zimmerman Cynthia K
• Meunier Jacques
• Alcázar Leopoldo R

Classifications

• C07C5/333

  Catalytic processes · CPC title

• C10G2300/40

  Characteristics of the process deviating from typical ways of processing · CPC title

• C10G2400/30

  Aromatics · CPC title

• C07C2/66 Primary

  Catalytic processes · CPC title

• C10G29/205

  by reaction with hydrocarbons added to the hydrocarbon oil · CPC title