Carbon molecular sieve membrane and its use in separation processes

Patent metadata

Field	Value
Publication number	US-12280340-B2
Application number	US-202017784580-A
Country	US
Kind code	B2
Filing date	Dec 10, 2020
Priority date	Dec 11, 2019
Publication date	Apr 22, 2025
Grant date	Apr 22, 2025

Abstract

It is provided a water-saturated carbon molecular sieve membrane obtainable by a) providing a hydrophilic carbon molecular sieve membrane (CMSM) comprising pores of a pore size from 0.25 nm to 0.55 nm for molecular sieving, pores of a pore size from 0.55 nm to 0.90 nm for adsorption diffusion and a negligible amount of pores larger than 0.90 nm such that a plot of N 2 permeance versus pressure of permeation at room temperature and at a pressure from 1 to 4 bar has zero or negative slope; and b) humidifying the membrane until obtaining a water-saturated carbon molecular sieve membrane. It is also provided a process for the separation of a gas from a gas mixture with such a water-saturated membrane, and its use for solvent dehydration, and as a membrane reactor.

First claim

The invention claimed is:

1. A water-saturated carbon molecular sieve membrane obtainable by a process comprising:
i) providing a hydrophilic carbon molecular sieve membrane (CMSM) comprising pores of a pore size as defined herein from 0.25 nm to 0.55 nm for molecular sieving, and of a pore size from higher than 0.55 nm to 0.90 nm for adsorption diffusion and a negligible amount of pores larger than 0.90 nm, such that a plot of N 2 permeance as defined herein versus pressure of permeation at room temperature and at a pressure from 1 to 4 bar has zero or negative slope; and
ii) humidifying the CMSM obtained in step i) to obtain a water-saturated CMSM by:
treating it with water vapor at a temperature from 5° C. to 180° C. and at atmospheric pressure and a relative humidity higher than 95% during a period of time such that after further treatment with water vapor, the permeation flux of a non-adsorbable gas at 4 bar at the temperature at which the CMSM has been treated with water vapor is constant during a particular period of time; or
alternatively, by exposing the CMSM to a N 2 or He gas stream saturated with water by bubbling the gas at a temperature from 5° C. to 180° C. into a tank filled with water such that after further exposure to the N 2 or He gas stream saturated with water, the permeation flux of a non-adsorbable gas at 4 bar and at the mentioned temperature is constant during a particular period of time.

2. The water-saturated carbon molecular sieve membrane of claim 1 , wherein the CMSM is a composite alumina-carbon molecular sieve membrane (Al-CMSM).

3. The water-saturated carbon molecular sieve membrane of claim 2 , wherein the Al-CMSM has a nitrogen content from 0.1 wt % to 4.0 wt %, an alumina content from 2.5% to 50% and a carbon content from 50 wt % to 95 wt %, with respect to the total weight of the membrane.

4. A process for the preparation of water-saturated composite alumina-carbon molecular sieve membrane (water-saturated Al-CMSM) comprising:
i) preparing a hydrophilic Al-CMSM by:
providing a porous α-Al 2 O 3 support;
preparing a solution containing from 5 to 20 wt % of phenol formaldehyde resin, from 0.5 to 5 wt % of formaldehyde, from 0.1 to 2 wt % of ethylenediamine, from 0.1 to 5 wt % of boehmite in N-methyl-2-pyrrolidone, and heating the solution to carry out a pre-polymerization process in order to obtain a coating solution;
dip-coating the porous α-Al 2 O 3 support in the coating solution in order to obtain a coated support;
drying the coated support at a temperature from 70 to 120° C. in order to complete the polymerization process; and
carbonizing the dried coated support at a carbonization temperature from 450° C. to 750° C. in order to obtain the hydrophilic Al-CMSM; and

ii) humidifying the hydrophilic Al-CMSM prepared in step i) to obtain a water-saturated Al-CMSM by:
treating the hydrophilic Al-CMSM with water vapor at a temperature from 5° C. to 180° C. and at atmospheric pressure and a relative humidity higher than 95% during a period of time such that, after further treatment with water vapor, the permeation flux of a non-adsorbable gas at 4 bar at the temperature at which the hydrophilic Al-CMSM has been treated with water vapor is constant during a particular period of time; or
alternatively, by exposing the hydrophilic Al-CMSM to a N 2 or He gas stream saturated with water by bubbling the gas at a temperature from 5° C. to 180° C. into a tank filled with water such that after further exposure to the N 2 or He gas stream saturated with water, the permeation flux of a non-adsorbable gas at 4 bar and at the mentioned temperature is constant during a particular period of time.

5. The process according to claim 4 , wherein the phenol formaldehyde resin is a novolac resin.

6. The process according to claim 4 , wherein the carbonization temperature is from 450° C. to 700° C.

7. A water-saturated Al-CMSM obtainable by the process defined in claim 4 .

8. A process for the separation of a gas from a gas mixture, the process comprising:
a) providing the water-saturated membrane as defined in claim 1 ;
b) providing a gas mixture comprising at least two gases; and
c) feeding the gas mixture to the water-saturated CMSM at a temperature from 5° C. to 300° C. in order to get a retentate and a permeate, wherein feeding is carried out at a pressure such that the partial pressure of the gas in the retentate is higher than the partial pressure of the gas in the permeate and such that a difference in permeation is observed compared to the same CMSM without having been subjected to an humidifying step in order to get a water saturated membrane at the feeding temperature and pressure.

9. The process according to claim 8 , wherein the at least two gases have a polarizability from 2 to 27 and at least one of the at least two gases have a kinetic diameter less than 0.55 nm, and
wherein if the at least two gases have a kinetic diameter lower than 0.55 nm, the difference of the kinetic diameter between the at least two gases is equal to or more than 0.01 nm and/or the difference of the polarizability between the at least two gases is equal to or more than 1 m 3 .

10. The process according to claim 9 , wherein the at least two gases are selected from the group consisting of He, H 2 O, Ne, H 2 , NO, Ar, NH 3 , N 2 , O 2 , CO, CO 2 , CH 4 , C 2 H 4 , C 2 H 6 , propene, propane, H 2 S, methanol, and ethanol.

11. The process according to claim 8 , wherein the gas mixture comprising at least two gases is selected from the group consisting of H 2 /CH 4 , H 2 /N 2 ; H 2 /CO 2 ; CO 2 /CH 4 , CO 2 /N 2 ; O 2 /N 2 ; and biogas.

12. The process according to claim 11 , wherein the gas mixture comprises from 5% to 20% of H 2 and from 95% to 80% of CH 4 , and wherein step c) is carried out at a hydrogen partial pressure difference equal to or higher than 3 bars and at a temperature of 40° C. or below.

13. The process according to claim 11 , wherein the at least two gases are CO 2 and N 2 and the gas mixture comprises from 10% to 20% of CO 2 and from 65% to 75% of N 2 .

14. The process according to claim 11 , wherein the at least two gases are H 2 and CO 2 and the gas mixture comprises from 55% to 65% of H 2 and from 30% to 40% of CO 2 .

15. The process according to claim 11 , wherein the gas mixture comprising at least two gases is biogas, and CO 2 is removed from biogas, wherein biogas is a gas mixture comprising methane and carbon dioxide.

16. A process for removal of water from an organic solvent, the process comprising:
applying vacuum from a permeated side of the water-saturated CMSM as defined in claim 1 .

17. A process for in situ removal of water during a catalytic reaction in which water is produced, the process comprising:
carrying out the catalytic reaction in a membrane reactor, wherein the membrane reactor is the water-saturated CMSM as defined in claim 1 .

18. A process for the separation of a gas from a gas mixture, the process comprising:
a) providing a water-saturated membrane as defined in claim 7 ;
b) providing a gas mixture comprising at least two gases; and
c) feeding the gas mixture to the water-saturated CMSM at a temperature from 5° C. to 300° C. in order to get a retentate and a permeate, wherein feeding is carried out at a pressure such that the partial pressure of the gas in the retentate is higher than the partial pressure of the gas in the permeate and such that a difference in permeation is observed compared to the same CMSM without having been subjected to an humidifying step in order to ge

Assignees

• Fundacion Tecnalia Res & Innovation
• Eindhoven Univ Of Technology

Inventors

• Pacheco Tanaka David Alfredo
• Llosa Tanco Margot Anabell
• Vittoria Nordio Maria Luisa
• Medrano Jimenez Jose Antonio
• Gallucci Fausto

Classifications

• C02F1/44

  by dialysis, osmosis or reverse osmosis {(general membrane separation processes B01D61/00, membrane modules B01D63/00, electrodialysis C02F1/4693, combination of membrane modules and bioreactors C02F3/1268)} · CPC title

• B01D2325/36

  Hydrophilic membranes · CPC title

• B01D2323/02

  Hydrophilization · CPC title

• B01D69/12

  Composite membranes; Ultra-thin membranes · CPC title

• B01D69/02

  characterised by their properties · CPC title