Patent Grant
11717787
The present disclosure is directed to polymeric membranes for gas separation. More specifically, the membranes are formed from blends of glassy polymers with high free volume polymers.
Natural gas supplies 22% of the energy used worldwide, and makes up nearly a quarter of electricity generation. Further, natural gas is an important feedstock for the petrochemicals industry. According to the International Energy Agency (IEA), the worldwide consumption of natural gas is projected to increase from 120 trillion cubic feet (Tcf) in the year 2012 to 203 Tcf by the year 2040.
Raw, or unprocessed, natural gas is formed primarily of methane (CH4), however it may include significant amounts of other components, including acid gases (carbon dioxide (CO2) and hydrogen sulfide (H2S)), nitrogen, helium, water, mercaptans, and heavy hydrocarbons (C3+), among other components. These contaminants must be removed during gas processing in order to meet the standard pipeline specifications of sales gas. In particular, the removal of acid gases (CO2 and H2S) has been a significant research topic due to the problematic effects of acid gases on natural gas heating value, pipeline transportability, and pipeline corrosion in the presence of water.
Currently, the majority of gas processing plants remove CO2 and H2S from natural gas by absorption technology, such as amine adsorption. However, several drawbacks are associated with this technology, including energy usage, capital cost, maintenance requirements, and the like.
An embodiment described in examples herein provides a gas separation membrane. The gas separation membrane includes a cellulosic matrix and a polymer of intrinsic microporosity (PIM). The PIM includes chains coupled by a heat-treating under vacuum.
Another embodiment described in examples herein provides a method for forming a gas separation membrane. The method includes forming a cellulosic polymer solution, forming a polymer of intrinsic microporosity (PIM) solution, and blending the polymer solution of the cellulosic polymer with the polymer solution of the PIM to form a mixed polymer solution. A dense film is formed from the mixed polymer solution. The dense film is dried. The dense film is heat-treated under heat and vacuum to couple the PIM chains.
Another embodiment described in examples herein provides a method for removing at least a portion of an acid gas from a natural gas feedstock to form a sweetened natural gas. The method includes flowing the natural gas feedstock over a membrane, wherein the membrane includes a cellulosic matrix and a polymer of intrinsic microporosity (PIM), wherein the PIM includes chains coupled by a heat-treating under vacuum. The portion of the acid gas is isolated in a permeate from the membrane. The sweetened natural gas is produced in a retentate from the membrane.
Polymeric membranes are thin semipermeable barriers that selectively separate some gas compounds from others. These membranes do not operate as a filter, where small molecules are separated from larger ones through a medium with pores, rather they separate based on the rate of dissolution and diffusion of compounds through the material of the membrane, termed the solution-diffusion model.
The use of polymeric membrane-based technology for gas separation has gained industrial attention recently due to the potential for high energy efficiency, small footprint, e.g., ease of adaptation into different form factors, and low capital cost. There are many factors affecting the gas separation performance of a polymeric membrane. High permeation flux and gas-pair selectivity are regarded as two of the most important criteria for the selection of a membrane for industrial use. However, there exists a trade-off between permeability and selectivity, as described herein.
Numerous polymeric membranes for gas separation have been developed over the decades, but few are currently commercialized for use in sour gas separation applications. Examples of polymeric materials used to form gas separation membranes include cellulose acetate (CA), polyimides (PI), and perfluoropolymers, such as polytetrafluoroethylene (PTFE), perfluorocycloalkene (PFCA), and the like. These polymeric materials are generally amorphous polymers that form glasses, for example, having a Tg of greater than about 100° C. CA is the most commercially used glassy polymer for acid gas removal. For example, UOP LLC's Separex™ CA membrane is used extensively for CO2 removal from natural gas. However, for wider implementation, CA membranes may be improved in a number of properties, including permeability and selectivity and enhanced chemical and thermal stability under the operating conditions that are typical of gas fields, such as higher feed pressure and high acid gas concentration.
To improve separation performance and stability, new membrane materials, including new polymeric materials and modifications of existing polymeric materials have been studied. However, some barriers, such as trade-offs in selectivity versus permeability, may prevent the deployment of these materials in industrial processes. Among various approaches, the use of polymer blends to form membranes has been recognized as one of the most promising routes as it combines the advantages of different materials into a new compound with unique and synergetic properties that are difficult to be obtained by synthetic means.
Embodiments described herein provide a method to produce a membrane from a polymer blend that has high permeability and selectivity. The matrix of the membrane is a cellulosic polymer, such as cellulose acetate (CA). A polymer of intrinsic microporosity (termed PIM herein) is a highly permeable polymer that is blended into the cellulosic matrix. Membranes formed from these blends are thermally treated in a high temperature vacuum oven to increase free volume (or pore) space by coupling PIM chains through a triazine ring formed during the heating. The heat-treated membranes have been tested for sour gas separations, and exhibit significant improvements in the removal of CO2 and H2S from a raw natural gas under a high-pressure gas feed when compared to neat CA membranes.
The CA/PIM-1 membrane 302 is thermally treated in a high temperature vacuum oven, for example, at about 100° C. to 250° C., or about 150° C. to about 180° C., or about 165° C., to form a thermally treated membrane comprising the coupled PIM-1 structures 204, termed a T-CA/PIM-1 membrane 304, herein. The coupling of the PIM-1 chains 100 to form the coupled PIM-1 structures 204 modifies the sizes of the pores 308 in the CA/PIM-1 membrane 302. In the T-CA/PIM-1 membrane 304, some pores 310 are decreased in size and other pores 312 are increased in size in comparison to the pores 308 in the CA/PIM-1 membrane 302.
In tests described with respect to the examples, the T-CA/PIM-1 membrane 304 showed improved permeability, such as to CO2 and H2S, and selectivity, for example, between CO2/CH4 and between H2S/CH4, compared to a neat CA membrane. This is likely due to chain relaxation from the coupling of the PIM-1 chains 100 creating a favorable morphology for enhancement of permeability and separation.
After the neat CA solution is prepared, a neat PIM-1 solution is prepared. To prepare the neat PIM-1 solution, a dried PIM-1 polymer 406 was added to THF at different loadings, for example, from about 2.5 wt. % to about 95 wt. % of the amount of the CA used to form the neat CA solution. The neat PIM-1 solution is rolled to completely dissolve 408 at room temperature.
The neat CA solution and the neat PIM-1 solution were then mixed 410 to form a CA/PIM-1 solution. The CA/PIM-1 solution was then stirred for 60 minutes to ensure homogeneity. The CA/PIM-1 solution was then left unstirred for 30 minutes to release any air bubbles, and filtered to remove any solids.
After the CA/PIM-1 solution was prepared, a casting procedure 412 was used to prepare the CA/PIM-1 membrane 414. For the casting procedure 412, the CA/PIM-1 solution was poured into PTFE flat-bottomed Petri dishes. The Petri dishes were covered to slow solvent evaporation and allowed to dry overnight at room temperature to prepare a dense film. The dense film was then dried in a vacuum oven at 80° C. for 48 hr to form the CA/PIM-1 membrane 414.
Once the CA/PIM-1 membrane 414 is formed, the T-CA/PIM-1 membrane 416 is fabricated. To fabricate the T-CA/PIM-1 membrane 416, the CA/PIM-1 membrane 414 is heated 418 in a high temperature vacuum oven at a temperature in the range of about 150° C. to about 180° C. under a vacuum pressure of less than about 10 mbar, with a heating rate of about 10° C./min. The vacuum oven was held for a period of 72 hr at the maximum temperature. After the thermal treatment process was completed, the T-CA/PIM-1 membrane 416 was allowed to cool to room temperature in the vacuum oven and stored in a drybox.
As described further with respect to the specific examples below, the T-CA/PIM-1 membrane 416 exhibited an increase over a neat CA membrane in membrane permeability (CO2 and H2S) and selectivity (CO2/CH4 and H2S/CH4). The increases were maintained under different feed gases, for example, pure, binary, and sour mixed gas, and testing conditions, for example, feed pressures up to 800 psi.
Under single gas testing, for example, at a feed temperature of 25° C. and a feed pressure of 100 psi, T-CA/PIM-1 membranes with a PIM-1 content of less than or about 40 wt. % show an increase over neat CA membranes in CO2/CH4 selectivity of about 27% to about 33% and an increase in CO2 permeability of about 81% to about 139%. In one example, a T-CA/PIM-1 membrane had a CO2/CH4 single gas selectivity and a CO2 permeability of 44.28 and 1.07 Barrer, respectively, compared to a neat CA membrane, which had 33.21 and 4.64 Barrer, respectively.
When tested under a binary gas mixture testing (20% CO2/80% CH4) at 800 psi, T-CA/PIM-1 blended membranes with addition of PIM-1 at less than or about 40 wt. % showed significant improvements over neat CA membranes in CO2/CH4 mixed selectivity (41%-50%) and CO2 permeability (140%-630%) under industrially-relevant testing conditions, e.g., feed pressure up to 800 psi. In one example, a T-CA/PIM-1 membrane had a CO2/CH4 mixed gas selectivity and a CO2 permeability of 45.23 and 21.12 Barrer, respectively, compared to a neat CA membrane, which had 30.42 and 2.89 Barrer, respectively.
The addition of the PIM-1 in the CA membrane matrix improved the sour gas separation performance under industrially relevant feed stream and testing conditions, such as using a 3-component sour gas mixture containing 3% CO2, 5% H2S and 92% CH4 and a feed pressure up to 800 psi. Under these conditions, T-CA/PIM-1 blended membranes show improvements over neat CA membranes in membrane permeability (82%-328% and 95%-353% increase in CO2 and H2S, respectively) and selectivity (3% and 8% increase in CO2/CH4 and H2S/CH4 mixed gas selectivity, respectively).
The PIM-1 was prepared by dissolving equimolar amounts of purified monomers, 2,3,5,6-tetra-fluoroterephthalonetrile (TFTPN, 44.063 mmol) and 5,5′,6,6′-tetrahydroxy-3,3,3′,3′-tetramethyl-1,1′-spirobisindane (TTSBI, 44.063 mmol), in anhydrous DMAc/Toluene (90 mL/45 mL). A polycondensation reaction to form the PIM-1 was catalyzed by K2CO3 under nitrogen atmosphere at 165° C. for 40 min. The polymer was precipitated into stirring methanol (1600 mL) overnight and washed with methanol several times. Finally, yellow powder was obtained after drying at 80° C. in vacuum oven overnight.
CA/PIM-1 membranes were prepared by the techniques described with respect to
Different amounts of PIM-1, for example, at a number of ratios between 1 wt. % and 95 wt. % of the amount of CA used to form the CA solution, were each dissolved in 10 mL THF. The PIM-1 solutions formed were rolled to dissolve completely at room temperature.
Each of the PIM-1 solutions was mixed with a CA solution, and stirred overnight. The resulting CA/PIM-1 solutions included PIM-1 concentrations of 2.5 wt. %, 5 wt. %, 10 wt. %, 20 wt. %, 30 wt. %, 40 wt. %, 60 wt. %, 80 wt. %, 90 wt. %, and 95 wt. % of the amount of the CA.
Each of the CA/PIM-1 solutions were filtered through a 1 μm pore size PTFE filter to remove impurities, and were then left unstirred for 30 min to release air bubbles. The CA/PIM-1 solutions were then poured into PTFE flat-bottomed Petri dishes to prepare dense films. The Petri dishes were covered to slow solvent evaporation and the CA/PIM-1 solutions were allowed to dry at room temperature overnight to form the dense films. The Petri dishes with the dense films were then dried in a vacuum oven at 80° C. for 48 hr. The resulting CA/PIM-1 membranes were allowed to cool to room temperature in the vacuum oven and stored in a drybox for further studies. The CA/PIM-1 membranes obtained had thicknesses in the range of 10 to 90 μm, as determined by scanning electron microscopy (SEM) images of membrane cross sections, taken on a JEOL 7100F SEM.
Each of the CA/PIM-1 membranes were given a further thermal treatment in a vacuum oven to prepare the T-CA/PIM-1 membranes. After a vacuum of less than about 10 mbar was achieved, the vacuum oven temperature was raised to between 150° C. and 250° C. at a rate of 10° C./min and held for a period of 72 hr. After the thermal treatment process, the membranes were allowed to cool to room temperature in the vacuum oven and stored in a drybox for further studies. The T-CA/PIM-1 membranes obtained had thicknesses in the range of 10 to 90 μm, as determined by SEM.
Comparison Membranes
The neat cellulose acetate (CA) membrane was prepared using a solution casting technique, similar to that described with respect to
The neat polymer of intrinsic microporosity (PIM-1) membrane was prepared using the solution casting technique, similar to that described with respect to
Membrane Permeation Testing
Permeation Test Procedures
The gas permeation tests were performed in triplicate using a constant-volume, variable-pressure technique. In this technique, a testing gas (upstream side or feed side) with desired pressure is fed to the permeation cell 508. In the variable-pressure method, the gas permeates through a membrane film into a closed, constant-volume chamber (downstream side, or permeate side) that is evaluated. The downstream pressure rise in the chamber is recorded as a function of time.
For testing, an epoxy masked membrane sample of 5-20 mm in diameter was inserted and sealed in the permeation cell 508. The permeation apparatus 500 was then evacuated for 1 hour before each test, using the vacuum pump 510. Pure gas permeability coefficients were measured at the temperature range of 20° C. to 50° C. and feed pressure range of 25 to 700 psi in the order of CH4 followed by CO2 to avoid swelling.
In addition to single gas tests, binary gas mixtures were used for permeation tests, including a CO2/CH4 mixture (20/80 vol/vol). Two sour gas feeds were also used for tests. The first is termed a 5% sour gas mixture and included three components, 5 vol. % H2S, 3 vol. % CO2, and 92 vol. % CH4. The second sour gas feed, referred to herein as a 20% sour gas mixture, included five components, 10 vol. % CO2, 20 vol. % H2S, 10 vol. % N2, 3 vol. % C2H6, and 57 vol. % CH4.
Steady-state permeation was verified using the time-lag method, where 10 times the diffusion time lag was taken as the effective steady state. As used herein, the time-lag method is commonly used to characterize membrane permeation properties. The intercept on the time axis of the plot of pressure rise versus time is defined as the time lag, t. The upstream (feed) pressure and the downstream (permeate) pressure were measured using Baraton absolute capacitance transducers (MKS Instruments) and recorded using LabVIEW software. The permeate pressure was maintained below 100 torr using a second vacuum pump 814. Mixed gas permeation was performed at 20° C. and feed pressure range of 200 psi to 800 psi with binary gas mixture and sour gas mixtures. A retentate stream was added for mixed gas tests and adjusted to 100 times the permeate flow rate to maintain a less than 1% stage cut. As used herein, the stage cut is a ratio of permeate flow to feed flow, and is defined as the fraction of feed gas that permeates the membrane, and is a measure of the degree of separation. The permeate gas was collected and then injected into the gas chromatograph 512, which was a Shimadzu gas chromatograph (GC-2014), to measure permeate composition. Permeate injections were performed at 95 torr. An Isco model 1000D syringe pump (TeledyneIsco) was used to control the feed pressure.
The permeability coefficients of gas i, Pi, were calculated according to Equation 1. In equation 1, dpi/dt is the slope of the steady state pressure rise in the downstream, V is the downstream volume, R is the ideal gas constant, T is the temperature of the downstream, L is the membrane thickness (as determined by SEM), A is the membrane surface area (estimated using ImageJ image processing software), and Δfi is the partial fugacity difference across the membrane calculated using the Peng-Robinson equation. Selectivity, αi/j, was calculated as the ratio of permeability coefficients as expressed in Equation 2.
Membrane Pure Gas Permeation Properties
The results shown are for the membrane permeability-selectivity trade-off (CO2/CH4 vs. CO2) comparison of neat CA membrane 602 (open square), neat PIM-1 membrane 604 (open circle), and T-CA/PIM-1 membranes 606 (solid squares). The PIM-1 loadings for the T-CA/PIM-1 membranes 606 as a weight percent (wt. %) of the CA matrix are (from left to right) 2.5 wt. %, 5 wt. %, 10 wt. %, 20 wt. %, 30 wt. %, 40 wt. %, 80 wt. %, 90 wt. %, and 95 wt. %. The tests were performed in pure gas at 25° C. and 100 psi.
The ideal transport properties are measured by the pure gas permeation and provide preliminary material observations and comparisons. The results show that the CO2/CH4 gas separation performance is within the Robeson upper bound lines (1991 and 2008). Some of the T-CA/PIM-1 membranes 606, for example, at a loading of PIM-1 or at 80 wt. % or greater, have separation performance that is above the 1991 upper bound. However, these membranes have lower CO2/CH4 selectivity and are not suitable for actual gas separation.
The incorporation of lower amounts of PIM-1 into the T-CA/PIM-1 membrane 606, for example, 2.5-40 wt. % in the CA matrix, not only leads to a significant increase in gas permeability, but also enhanced selectivity, which makes the membranes suitable for CO2/CH4 separation. In one example (Table 1), T-CA/PIM-1 membranes at CA/PIM-1 blend ratios of 95/5, 90/10, and 80/20 had CO2/CH4 selectivities of 42.18, 43.85 and 44.28, respectively, which are a 27% to 32% increase over the neat CA membrane 602, which had a selectivity of 33.21.
Further, the T-CA/PIM-1 blended membranes 606 also exhibited significant enhancement in permeability (81%, 88% and 139% increase in CO2 permeability for T-CA/PIM-1 (95/5), T-CA/PIM-1 (90/10) and T-CA/PIM-1 (80/20), respectively), compared to the neat CA membrane 602. By comparison, the addition of PIM-1 into other glassy polymer membranes, such as Matrimid®, Ultem®, Torlon®, PAFEK®, P84®, TB®, without thermal treatment in vacuum conditions, leads to an increase in CO2 permeability, but a decrease in CO2/CH4 selectivity.
As shown in
Membrane Permeation Properties for Binary Gas Mixture
For CO2/CH4 separation, the addition of 2.5 wt. %-40 wt. % of PIM-1 increases the CO2/CH4 mixed gas selectivity and CO2 permeability for T-CA/PIM-1 membranes 804. In one example (Table 3), T-CA/PIM-1 membranes 804 at CA/PIM-1 ratios of 97.5/2.5, 95/5, 90/10, and 80/20 had CO2/CH4 mixed gas selectivities of 42.80, 42.82, 45.64, and 45.23, respectively, at a feed pressure of 800 psi. These values are a 41%, 41%, 50%, and 49% increase, respectively, over a neat CA membrane 802, which had a CO2/CH4 mixed gas selectivity of 30.42.
A number of T-CA/PIM-1 membranes also exhibited an increase in permeability over the neat CA membrane 802. For example, for T-CA/PIM-1 at CA/PIM-1 ratios of 97.5/2.5, 95/5, 90/10, and 80/20 increases in CO2 permeability were seen over a neat CA membrane of 140%, 233%, 313% and 631% increase, respectively. Thus, T-CA/PIM-1 membranes demonstrate better overall separation performance under mixed gas testing conditions.
However, the overall mixed gas selectivity for all of the tested membranes are comparable to their ideal selectivity, but at higher CO2 permeability. For example, a T-CA/PIM-1 membrane with a loading of 80/20 CA/PIM-1, has a mixed gas CO2 permeability of 21.12 Barrer, which is 91% higher than its pure gas CO2 permeability of 11.07 Barrer. This increase in permeability may be due to the better sorption interactions of CO2 in a mixed gas and the higher affinity of PIM-1 towards CO2. Similar trends were observed under binary gas mixture tests for T-CA/PIM-1 membranes with a loading of 10%-20%, which have higher CO2/CH4 mixed gas selectivity in the range of PIM-1 loading of 10%-20%.
Membrane Sour Mixed Gas Permeation Properties
However, the T-CA/PIM-1 membranes 1006 show significant improvement over a neat CA membrane in permeability (80%˜328% increase in CO2 permeability and 77%˜353% increase in H2S permeabilities), and comparable CO2/CH4 and H2S/CH4 mixed gas selectivities with the addition of amounts of PIM-1 of less than about 20 wt. %. In one example (Table 4), a T-CA/PIM-1 membrane with a PIM-1 loading of 5 wt. % had CO2/CH4 and H2S/CH4 mixed gas selectivities of 36.66 and 43.11, CO2 and H2S permeabilities of 7.50 Barrer and 8.90 Barrer, respectively, compared to neat CA membrane CO2/CH4 and H2S/CH4 mixed gas selectivities of 35.74 and 39.76, and CO2 and H2S permeabilities of 4.11 Barrer and 4.57 Barrer, respectively.
An embodiment described in examples herein provides a gas separation membrane. The gas separation membrane includes a cellulosic matrix and a polymer of intrinsic microporosity (PIM). The PIM includes chains coupled by a heat-treating under vacuum.
In an aspect, the cellulosic matrix includes cellulose acetate (CA). In an aspect, the cellulosic matrix includes cellulose acetate butyrate (CAB).
In an aspect, the PIM includes PIM-1. In an aspect, the PIM includes triazine rings coupling PIM chains.
In an aspect, the gas separation membrane includes larger free volume spaces and smaller free volume spaces formed by the heat-treating under vacuum. In an aspect, the gas separation membrane has a CO2 permeability that is at least 50% higher than the CO2 permeability of a neat CA membrane. In an aspect, the gas separation membrane has a CO2/CH4 mixed gas selectivity that is within +/−10% of a neat CA membrane. In an aspect, the gas separation membrane has an H2S permeability that is at least 50% higher than the H2S permeability of a neat CA membrane. In an aspect, the gas separation membrane has an H2S/CH4 mixed gas selectivity that is within +/−10% of a neat CA membrane.
In an aspect, the gas separation membrane includes between about 2.5 wt. % PIM and about 40 wt. % PIM. In an aspect, the gas separation membrane includes between about 5 wt. % PIM and about 20 wt. % PIM.
Another embodiment described in examples herein provides a method for forming a gas separation membrane. The method includes forming a cellulosic polymer solution, forming a polymer of intrinsic microporosity (PIM) solution, and blending the polymer solution of the cellulosic polymer with the polymer solution of the PIM to form a mixed polymer solution. A dense film is formed from the mixed polymer solution. The dense film is dried. The dense film is heat-treated under heat and vacuum to couple the PIM chains.
In an aspect, the method includes dissolving a cellulosic polymer in tetrahydrofuran (THF) to form the cellulosic polymer solution. In an aspect, the method includes forming the cellulosic polymer solution by dissolving cellulose acetate in THF.
In an aspect, the method includes dissolving the PIM in THF. In an aspect, the method includes forming the PIM polymer solution by dissolving PIM-1 in THF. In an aspect, the method includes dissolving an amount of PIM that is in a weight ratio to the cellulosic polymer of between about 2.5 wt. % and about 40 wt. %. In an aspect, the method includes dissolving an amount of PIM that is in a weight ratio to the cellulosic polymer of between about 5 wt. % and about 20 wt. %.
In an aspect, the method includes forming triazine rings during the heat treatment under vacuum, wherein the triazine rings couple the PIM chains.
Another embodiment described in examples herein provides a method for removing at least a portion of an acid gas from a natural gas feedstock to form a sweetened natural gas. The method includes flowing the natural gas feedstock over a membrane, wherein the membrane includes a cellulosic matrix and a polymer of intrinsic microporosity (PIM), wherein the PIM includes chains coupled by a heat-treating under vacuum. The portion of the acid gas is isolated in a permeate from the membrane. The sweetened natural gas is produced in a retentate from the membrane.
In an aspect, the cellulosic matrix is formed from cellulose acetate (CA). In an aspect, the PIM is formed from PIM-1. In an aspect, the PIM includes triazine rings formed by the heat-treating under vacuum. In an aspect, larger free volume spaces and smaller free volume spaces are formed by the heat-treating under vacuum.
Other implementations are also within the scope of the following claims.
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| Number | Date | Country | |
|---|---|---|---|
| 20220212139 A1 | Jul 2022 | US |
