Cyclical method of producing high-purity nitrogen and optionally a high-purity hydrocarbon from a feedstock containing nitrogen and a hydrocarbon

Patent metadata

Field	Value
Publication number	US-9844750-B2
Application number	US-201214413867-A
Country	US
Kind code	B2
Filing date	Jul 9, 2012
Priority date	Jul 9, 2012
Publication date	Dec 19, 2017
Grant date	Dec 19, 2017

Abstract

The invention relates to a cyclical method for producing a nitrogen fraction, the purity of which is greater than or equal to 95 mol %, and a hydrocarbon-enriched fraction from a filler containing nitrogen and a hydrocarbon, said method using a specific class of porous hybrid solids as an adsorbent in a pressure-swing adsorption (PSA) process. The invention also relates to equipment for implementing said method.

First claim

The invention claimed is:

1. A cyclical process for the production of a nitrogen fraction with a purity ≧95 mol %, on the one hand, and of a fraction enriched in hydrocarbon, on the other hand, from a feedstock comprising nitrogen and a hydrocarbon, each cycle comprising the following stages:
i) bringing said feedstock into contact with an adsorbent bed provided with a feed end and with a production end and containing a solid adsorbent chosen from porous hybrid solids, said contacting operation being carried out under a pressure P 1 ≧0.1 MPa and a temperature T 1 ≧0° C.;
ii) recovering, at the production end of the adsorbent bed, a first nitrogen fraction with a purity ≧95 mol % (2);
iii) depressurizing the adsorbent bed cocurrentwise down to a pressure P 2 <P 1 where P 2 ≧0.1 MPa, so as to recover, at the production end of the adsorbent bed, a second fraction of nitrogen with a purity ≧95 mol %;
iv) depressurizing the adsorbent bed countercurrentwise down to a pressure P 3 <P 2 where 0.006 MPa≦P 3 ≦0.05 MPa, so as to desorb the hydrocarbons from the bed and to recover, at the feed end of the adsorbent bed, a first fraction enriched in hydrocarbon
v) purging the adsorbent bed countercurrentwise using the nitrogen fraction with a purity ≧95 mol % under the pressure P 3 , so as to recover, at the feed end of the adsorbent bed, a second fraction enriched in hydrocarbon;
vi) repressurizing the adsorbent bed countercurrentwise using the nitrogen with a purity ≧95 mol % or with the feedstock up to the pressure P 1 ;
in which said adsorbent has a dynamic capacity with regard to the hydrocarbon of at least 3 mmol/g between 0.25 MPa and 0.05 MPa at 50° C. and a dynamic capacity with regard to the nitrogen of less than or equal to 0.50 mmol/g between 0.25 MPa and 0.05 MPa at 50° C.,
wherein the hydrocarbon is propylene and the solid adsorbent is MIL 100 (Fe).

2. The process as claimed in claim 1 , wherein stage i) of bringing the feedstock into contact with the adsorbent bed is carried out at a pressure P 1 of between 0.1 MPa and 1 MPa and at a temperature of between 0° C. and 100° C.

3. The process as claimed in claim 1 , wherein the cocurrentwise depressurization stage iii) is carried out at a pressure P 2 of between 0.2 MPa and 0.1 MPa.

4. The process as claimed in claim 1 , wherein the depressurization stage iv) is carried out under vacuum.

5. The process as claimed in claim 1 , wherein the depressurization stage iv) is carried out at a pressure P 3 of between 0.01 MPa and 0.05 MPa.

6. The process as claimed in claim 1 , wherein, before carrying out the depressurization stage iv), a portion of the fraction enriched in hydrocarbon is recycled in the adsorbent bed via the feed end, so as to saturate the bed with hydrocarbon and to recover, on conclusion of stage iv), a fraction enriched in hydrocarbon with a purity ≧90 mol %.

7. The process as claimed in claim 6 , wherein the depressurization stage iv) is carried out under a pressure P 3 of between 0.006 MPa and 0.05 MPa.

8. The process as claimed in claim 1 , wherein the degree of recovery of nitrogen with a purity ≧95 mol % is greater than or equal to 80%.

9. The process as claimed in claim 6 , wherein the degree of recovery of hydrocarbon with a purity ≧90 mol % is greater than or equal to 80%.

10. The process as claimed in claim 1 , wherein the feedstock comprises at least 30 mol % of nitrogen and at most 70 mol % of hydrocarbon.

11. The process as claimed in claim 1 , wherein the feedstock originates from a plant for the production of polypropylene.

12. A process for the production of polypropylene by polymerization of propylene optionally comprising a propane fraction, in which the polypropylene resulting from the polymerization stage is separated from the propylene and propane which have not reacted during the polymerization using a gas/solid separator into which a nitrogen charge is introduced in order to purify the polypropylene, which results in the formation of a nitrogen/propylene/propane mixture, said process being characterized in that said nitrogen/propylene/propane mixture is recovered and the stages as defined in claim 1 are carried out in order to produce, on the one hand, a nitrogen fraction with a purity ≧95 mol % and, on the other hand, a fraction enriched in propylene and propane.

13. The process as claimed in claim 12 , wherein a portion of the fraction enriched in propylene and propane is recycled in the adsorbent bed via the feed end, so as to saturate the bed with hydrocarbon and to recover, on conclusion of stage iv), a fraction enriched in propylene and propane with a purity ≧90 mol %.

14. An installation for the implementation of a process as claimed in claim 12 , wherein said installation comprises:
a polymerization reactor with an inlet which makes it possible to introduce propylene as reactant, said propylene comprising a propane fraction, as well as the other ingredients necessary for the polymerization;
a gas/solid separator positioned at the outlet of the polymerization reactor which receives the solid polypropylene resulting from the polymerization reaction and also an unreacted propylene/propane mixture, said gas/solid separator additionally comprising:
an inlet which makes it possible to introduce nitrogen intended to degas the solid polypropylene,
an outlet (A) for the nitrogen/propylene/propane gas mixture; and
an outlet (B) for recovering the solid polypropylene;

at least one adsorbent column chosen from MIL 100 (Fe), said columns making it possible to receive the nitrogen/propylene/propane gas mixture so as to produce, on the one hand, a nitrogen with a purity ≧95 mol % and, on the other hand, a mixture enriched in propylene and propane.

15. The installation as claimed in claim 14 , wherein said installation comprises a line which makes it possible to recycle the mixture enriched in propylene and propane in the adsorbent column, so as to saturate the bed with hydrocarbon and to recover a fraction of propylene and propane with a purity ≧90 mol %.

Assignees

• Luck Francis
• Leroi Catherine
• Fernandez Alvaro
• Peixoto Ribeiro Ana Mafalda Almeida
• Godinho De Faria Dos Santos Joao Carlos
• Rodrigues Alirio Egidio
• Chang Jong-San
• Lee U-Hwang
• Hwang Young Kyu
• Bonne Jean-Patrick
• Total Petrochemicals France
• Univ Do Porto (Uporto) Faculdade De Engenharia
• Korea Res Inst Chemical Tech

Inventors

• Luck Francis
• Leroi Catherine
• Fernandez Alvaro
• Peixoto Ribeiro Ana Mafalda Almeida
• Godinho De Faria Dos Santos Joao Carlos
• Rodrigues Alirio Egidio
• Chang Jong-San
• Lee U-Hwang
• Hwang Young Kyu
• Bonne Jean-Patrick

Classifications

• B01J20/28066

  being more than 1000 m2/g · CPC title

• C10G2300/202

  Heteroatoms content, i.e. S, N, O, P · CPC title

• B01J2219/00006

  Large-scale industrial plants · CPC title

• C10G50/00

  Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation · CPC title

• C10G25/12

  Recovery of used adsorbent · CPC title