Cryogenic air separation method for producing oxygen at high pressures

Patent metadata

Field	Value
Publication number	US-10746461-B2
Application number	US-201715689532-A
Country	US
Kind code	B2
Filing date	Aug 29, 2017
Priority date	Aug 30, 2016
Publication date	Aug 18, 2020
Grant date	Aug 18, 2020

Abstract

The present invention relates to a cryogenic air separation process that provides high pressure oxygen for an oxy-fired combustion of a fuel (e.g., a carbonaceous fuel). The air separation process can be directly integrated into a closed cycle power production process utilizing a working fluid, such as CO2. Beneficially, the air separation process can eliminate the need for inter-cooling between air compression stages and rather provide for recycling the adiabatic heat of compression into a process step in further methods wherein an additional heat supply is beneficial.

First claim

The invention claimed is:

1. A method of producing power, the method comprising:
combusting a fuel with a stream of substantially pure high pressure oxygen gas in a combustor in the presence of a recycle CO 2 working fluid stream to form a combustion product stream including CO 2 at a pressure of greater than 150 bar;
expanding the combustion product stream including CO 2 across a turbine to form a turbine exhaust stream and generate power;
removing heat from the turbine exhaust stream in a recuperator heat exchanger;
separating CO 2 from the turbine exhaust stream to form the recycle CO 2 working fluid stream;
compressing the recycle CO 2 working fluid stream;
heating at least a first portion of the recycle CO 2 working fluid stream using the heat removed from the turbine exhaust stream in the recuperator heat exchanger and also heating at least a second portion of the recycle CO 2 working fluid stream using added heating in a second heat exchanger, the heated, second portion of the recycle CO 2 working fluid stream being passed through the recuperator heat exchanger to further heat the first portion of the recycle CO 2 working fluid stream;
passing the first portion of the recycle CO 2 working fluid stream from the recuperator heat exchanger to the combustor; and
forming the stream of substantially pure high pressure oxygen gas by a method wherein:
an inlet air stream is compressed in a first compressor to form a compressed inlet air stream with a pressure of at least 3.5 bar and a temperature of greater than 150° C.;
heat from the compressed inlet air stream is used as the added heating for heating at least the second portion of the recycle CO 2 working fluid stream so that the compressed inlet air stream is cooled;
the compressed inlet air stream is purified to form a purified inlet air stream;
the purified inlet air stream is divided into a first portion and a second portion;
the first portion of the purified inlet air stream is compressed to form an intermediate pressure, purified air stream having a pressure of 20 bar to 90 bar and a high pressure, purified air stream having a pressure of 70 bar to 150 bar, the high pressure, purified air stream having a pressure that is greater than the pressure of the intermediate pressure, purified air stream;
the intermediate pressure, purified air stream and the high pressure, purified air stream are cooled in a high pressure heat exchanger;
the second portion of the purified inlet air stream is cooled in a low pressure heat exchanger;
a first fraction of the high pressure, purified air stream is expanded in a first power producing turbine to form a first expanded, purified air stream;
a second fraction of the high pressure, purified air stream is expanded in a second power producing turbine to form a second, expanded, purified air stream;
the intermediate pressure, purified air stream is expanded in a third power producing turbine to form a third expanded, purified air stream;
the first expanded, purified air stream, the second, expanded, purified air stream, the third, expanded, purified air stream, and the second portion of the purified inlet air stream are passed through a distillation column and to form an exit stream of substantially pure liquid oxygen and a waste stream comprising nitrogen;
the exit stream of substantially pure liquid oxygen is compressed to a pressure of greater than 150 bar; and
the exit stream of substantially pure liquid oxygen is heated to a temperature of greater than −10° C. in the high pressure heat exchanger against the intermediate pressure, purified air stream and the high pressure, purified air stream to form the substantially pure high pressure oxygen gas.

2. A method for producing oxygen, the method comprising:
compressing an inlet air stream in a first compressor to form a compressed inlet air stream with a pressure of at least 3.5 bar and a temperature of greater than 150° C.;
cooling the compressed inlet air stream to a temperature of less than 25° C.;
purifying the compressed inlet air stream by removing at least 90 mol % of any carbon dioxide and water present in the compressed inlet air stream and thus forming a purified inlet air stream;
dividing the purified inlet air stream into a first portion and a second portion;
further compressing the first portion of the purified inlet air stream to form an intermediate pressure, purified air stream having a pressure of 20 bar to 90 bar and a high pressure, purified air stream having a pressure of 70 bar to 150 bar, the high pressure, purified air stream having a pressure that is greater than the pressure of the intermediate pressure, purified air stream;
cooling the intermediate pressure, purified air stream and the high pressure, purified air stream in a high pressure heat exchanger;
cooling the second portion of the purified inlet air stream in a low pressure heat exchanger;
expanding a first fraction of the high pressure, purified air stream in a first power producing turbine to form a first expanded, purified air stream;
expanding a second fraction of the high pressure, purified air stream in a second power producing turbine to form a second, expanded, purified air stream;
expanding the intermediate pressure, purified air stream in a third power producing turbine to form a third expanded, purified air stream;
passing the first expanded, purified air stream, the second, expanded, purified air stream, the third, expanded, purified air stream, and the second portion of the purified inlet air stream through a distillation column and to form an exit stream of substantially pure liquid oxygen and a waste stream comprising nitrogen;
compressing the exit stream of substantially pure liquid oxygen to a pressure of greater than 150 bar; and
heating the exit stream of substantially pure liquid oxygen to a temperature of greater than −10° C. in the high pressure heat exchanger against the intermediate pressure, purified air stream and the high pressure, purified air stream to form an exit stream of substantially pure high pressure oxygen gas.

3. The method of claim 2 , wherein the purifying comprises passing the compressed inlet air stream through a dual bed adsorption system.

4. The method of claim 2 , wherein the first portion of the purified inlet air stream comprises 25 mol % to 75 mol % of the purified inlet air stream.

5. The method of claim 2 , wherein the intermediate pressure, purified air stream comprises 30 mol % to 50 mol % of the first portion of the purified inlet air stream, and the high pressure, purified air stream comprises 70 mol % to 50 mol % of the first portion of the purified inlet air stream.

6. The method of claim 2 , comprising cooling the second portion of the purified inlet air stream against a portion of the waste stream comprising nitrogen before passing the second portion of the purified inlet air stream through the distillation column.

7. The method of claim 2 , wherein the first fraction of the high pressure, purified air stream to be expanded in the first power producing turbine is withdrawn from the high pressure heat exchanger at a temperature range of −20 to −40° C.

8. The method of claim 2 , wherein the second fraction of the high pressure, purified air stream to be expanded in the second power producing turbine is withdrawn from the high pressure heat exchanger at a temperature range of −160 to −170° C.

9. The method of claim 2 , wherein the intermediate pressure, purified air stream to be expanded in the third power producing turbine is withdrawn from the heat exchanger at a temperature range of −80 to −120° C.

10. The method of claim 2 , wherein the distillation column comprises a double column distillati

Assignees

• 8 Rivers Capital Llc

Inventors

• Allam Rodney John

Classifications

• F25J3/04533

  for the direct combustion of fuels in a power plant, so-called "oxyfuel combustion" · CPC title

• F25J3/04412

  in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column · CPC title

• F25J3/04303

  Lachmann expansion, i.e. expanded into oxygen producing or low pressure column · CPC title

• F25J3/04145

  Mechanically coupling of different compressors of the air fractionation process to the same driver(s) · CPC title

• F23L7/007

  Supplying oxygen or oxygen-enriched air · CPC title