Process and plant for obtaining an ethylene product in a supercritical state

Patent metadata

Field	Value
Publication number	US-10457617-B2
Application number	US-201715999757-A
Country	US
Kind code	B2
Filing date	Feb 20, 2017
Priority date	Feb 19, 2016
Publication date	Oct 29, 2019
Grant date	Oct 29, 2019

Abstract

A method for obtaining an ethylene product in a supercritical state is proposed, in which method a gas mixture containing predominantly or exclusively ethylene and ethane is separated in a distillation column ( 1 ), which is operated at a distillation pressure level of from 5 to 15 bar, into an overhead product containing predominantly or exclusively ethylene and a bottom product containing predominantly or exclusively ethane, the overhead product being withdrawn in the gaseous state from the head of the distillation column ( 1 ) and a first portion thereof being liquefied and returned as reflux to the distillation column ( 1 ) and a second portion thereof being converted into a supercritical state and being used as the ethylene product. Provision is made that, for converting the second portion into the supercritical state, multi-stage compression from the distillation pressure level via a plurality of intermediate pressure levels to a supercritical pressure level is carried out, the second portion in the multi-stage compression being converted predominantly or exclusively from the gaseous into the supercritical state. A corresponding installation is likewise a subject of the invention.

First claim

The invention claimed is:

1. A method for obtaining an ethylene product in a supercritical state, in which a gas mixture containing predominantly or exclusively ethylene and ethane is separated in a distillation column, which is operated at a distillation pressure level of from 5 to 15 bar, into an overhead product containing predominantly or exclusively ethylene and a bottom product containing predominantly or exclusively ethane, the overhead product being withdrawn in the gaseous state from the head of the distillation column and a first portion thereof being liquefied and returned as reflux to the distillation column and a second portion thereof being converted into a supercritical state and being used as the ethylene product, characterised in that, for converting the second portion into the supercritical state, multi-stage compression from the distillation pressure level via a plurality of intermediate pressure levels to a supercritical pressure level is carried out, the second portion in the multi-stage compression being converted predominantly or exclusively directly from the gaseous into the supercritical state.

2. The method according to claim 1 , in which the intermediate pressure levels comprise a first intermediate pressure level which is from 18 to 25 bar.

3. The method according to claim 2 , in which the first portion is compressed in the multi-stage compression from the distillation pressure level to the first intermediate pressure level, is then liquefied and used as the reflux.

4. The method according to claim 3 , in which the distillation column is operated by a bottom evaporator which is heated using the first portion which is compressed to the first intermediate pressure level.

5. The method according to claim 2 , in which furthermore a refrigerant containing predominantly or exclusively ethylene is compressed in the multi-stage compression from a plurality of starting pressure levels which lie below the distillation pressure level, and also from the distillation pressure level to the first intermediate pressure level.

6. The method according to claim 5 , in which the starting pressure levels comprise a first starting pressure level, which is from 0.5 to 1.5 bar, and a second starting pressure level, which is from 2 to 4 bar.

7. The method according to claim 6 , in which the intermediate pressure levels further comprise a second intermediate pressure level, which is from 35 to 45 bar.

8. The method according to claim 7 , in which a first (I) compressor stage is used for compressing from the first to the second starting pressure level, a second (II) compressor stage is used for compressing from the second starting pressure level to the distillation pressure level, a third (III) compressor stage is used for compressing from the distillation pressure level to the first intermediate pressure level, and a fourth (IV) compressor stage is used for compressing from the first intermediate pressure level to the second intermediate pressure level, the first to fourth compressor stages (I-IV) being driven at the same speed by means of a first common shaft.

9. The method according to claim 8 , in which the intermediate pressure levels further comprise a third intermediate pressure level, which is from 60 to 80 bar, and in which the supercritical pressure level is from 100 to 150 bar.

10. The method according to claim 9 , in which, a fifth (V) compressor stage is used for compressing from the second to the third intermediate pressure level, and a sixth (VI) compressor stage is used for compressing from the third intermediate pressure level to the supercritical pressure level, the fifth and the sixth compressor stages (V, VI) being driven at the same speed by means of a second common shaft.

11. The method according to claim 10 , in which the first and the second common shaft are coupled together by means of a gear mechanism.

12. The method according to claim 1 , in which the gas mixture containing predominantly or exclusively ethylene and ethane is formed using a cracked gas from a steam cracking process.

Assignees

• Linde Ag

Inventors

• Hofel Torben
• Kamann Martin
• Scholch Michael
• Mccracken Sean
• Kunkel Josef
• Kracker-Semler Gunther

Classifications

• C07C11/04 Primary

  Ethene · CPC title

• B01J3/008

  Processes carried out under supercritical conditions · CPC title

• C07C7/04 Primary

  by distillation · CPC title

• B01D2256/24

  Hydrocarbons · CPC title

• B01D3/143

  by two or more of a fractionation, separation or rectification step · CPC title