Method for recovering a stream of C2+ hydrocarbons in a residual refinery gas and associated installation

Patent metadata

Field	Value
Publication number	US-11629108-B2
Application number	US-201816614799-A
Country	US
Kind code	B2
Filing date	May 17, 2018
Priority date	May 18, 2017
Publication date	Apr 18, 2023
Grant date	Apr 18, 2023

Abstract

This method comprises passing a residual stream into a flash drum to form a gaseous overhead flow and liquid bottom flow, and feeding the bottom flow into a distillation column,
It comprises cooling the overhead flow in a heat exchanger to form a cooled overhead flow.
It comprises the extraction of a gaseous overhead stream at the head of the distillation column, and the formation of at least one effluent stream from the overhead stream and/or from the top stream.
The separation of the cooled overhead flow comprises passing the cooled overhead flow into an absorber, and injecting a methane-rich stream into the absorber to place the cooled overhead flow in contact with the methane-rich stream.

First claim

The invention claimed is:

1. Method for recovering a C2+ hydrocarbons stream in a residual refinery gas, comprising:
forming a residual stream from the residual refinery gas;
feeding the residual stream into a flash drum to form a gaseous overhead flow and a liquid bottom flow;
feeding the liquid bottom flow into a distillation column via an inlet;
cooling the gaseous overhead flow in a heat exchanger to form a cooled overhead flow;
separating the cooled overhead flow into a liquid lower stream and into a gaseous top stream;
feeding the liquid lower stream into the distillation column via an upper inlet positioned above the inlet for feeding the liquid bottom flow;
recovering the C2+ hydrocarbons stream at a bottom of the distillation column;
extracting a gaseous overhead stream at a head of the distillation column;
forming at least one effluent stream from the gaseous overhead stream and/or from the gaseous top stream;
heating the at least one effluent stream in a heat exchanger via heat exchange with the gaseous overhead flow;

wherein separating the cooled overhead flow comprises feeding the cooled overhead flow into an absorber, and injecting a methane-rich stream into the absorber to place the cooled overhead flow in contact with the methane-rich stream, wherein the molar content of methane in the methane-rich stream is higher than 90 mole %.

2. The method according to claim 1 , wherein the methane-rich stream is a liquid stream.

3. The method according to claim 1 , wherein the methane-rich stream is formed from a thermal steam cracker, without passing through the distillation column or through the flash drum.

4. The method according to claim 1 , wherein the temperature of the residual stream before entering the flash drum is lower than −80° C.

5. The method according to claim 4 , wherein the temperature of the residual stream before entering the flash drum is between −90° C. and −100° C.

6. The method according to claim 1 , wherein the overhead flow circulates from the flash drum through the heat exchanger as far as the absorber without static or dynamic expansion in an expansion valve or dynamic expansion turbine.

7. The method according to claim 1 , wherein the heat exchanger is a two-flow heat exchanger, the method comprising mixing the overhead stream and the top stream to form the effluent stream, the overhead flow being cooled exclusively by the effluent stream between the flash drum and the absorber.

8. The method according to claim 1 , wherein the heat exchanger is a three-flow heat exchanger, the method comprising forming a first effluent stream from the overhead stream and a second effluent stream from the top stream, the overhead flow being cooled exclusively by the first effluent stream and by the second effluent stream between the flash drum and the absorber.

9. The method according to claim 1 , wherein a temperature difference between the cooled overhead flow and the overhead flow is greater than 2° C. in absolute value.

10. The method according to claim 1 , wherein the C2+ hydrocarbons stream contains more than 90 mole % of the C2 hydrocarbons contained in the residual stream.

11. The method according to claim 1 comprising a prior purification and/or successive cooling and separating of the residual refinery gas.

Assignees

• Technip France
• Technip Energies France

Inventors

• Simon Yvon
• Destour Bruno
• Valente Marco

Classifications

• F25J3/0233

  separation of CnHm with 1 carbon atom or more · CPC title

• C07C7/11

  by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids · CPC title

• B01D53/00 Primary

  Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols, (recovery of volatile solvents by condensation B01D5/00; sublimation B01D7/00; cold traps, cold baffles B01D8/00; working-up undefined gaseous mixtures obtained by cracking hydrocarbon oils C10G70/00; cleaning coal gas C10K; working-up of natural gas, or synthetic natural gas, C10L3/10; separation of difficult-to-condense gases or air by liquefaction F25J; for investigating materials G01N30/00) · CPC title

• F25J2200/02

  in a single pressure main column system · CPC title

• F25J2210/12

  Refinery or petrochemical off-gas · CPC title