WO2010119163A1 - Uso de un material cristalino microporoso de naturaleza zeolítica con estructura rho en tratamiento de gas natural - Google Patents
Uso de un material cristalino microporoso de naturaleza zeolítica con estructura rho en tratamiento de gas natural Download PDFInfo
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- WO2010119163A1 WO2010119163A1 PCT/ES2010/070236 ES2010070236W WO2010119163A1 WO 2010119163 A1 WO2010119163 A1 WO 2010119163A1 ES 2010070236 W ES2010070236 W ES 2010070236W WO 2010119163 A1 WO2010119163 A1 WO 2010119163A1
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- Prior art keywords
- separation
- adsorbed
- methane
- rho
- preferably adsorbed
- Prior art date
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 137
- 239000003345 natural gas Substances 0.000 title claims abstract description 21
- 239000002178 crystalline material Substances 0.000 title description 2
- 238000000926 separation method Methods 0.000 claims abstract description 34
- 239000010457 zeolite Substances 0.000 claims abstract description 31
- 238000000034 method Methods 0.000 claims abstract description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 56
- 239000000463 material Substances 0.000 claims description 39
- 239000000203 mixture Substances 0.000 claims description 35
- 239000007789 gas Substances 0.000 claims description 30
- 229910052757 nitrogen Inorganic materials 0.000 claims description 28
- 229910021536 Zeolite Inorganic materials 0.000 claims description 24
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 24
- 238000000746 purification Methods 0.000 claims description 20
- 229930195733 hydrocarbon Natural products 0.000 claims description 16
- 150000002430 hydrocarbons Chemical class 0.000 claims description 16
- 239000002253 acid Substances 0.000 claims description 10
- 238000011084 recovery Methods 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 abstract description 49
- 238000005259 measurement Methods 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 4
- 239000011148 porous material Substances 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- 239000003463 adsorbent Substances 0.000 description 3
- 239000002156 adsorbate Substances 0.000 description 2
- 150000001412 amines Chemical class 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000012229 microporous material Substances 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- XEZNGIUYQVAUSS-UHFFFAOYSA-N 18-crown-6 Chemical compound C1COCCOCCOCCOCCOCCO1 XEZNGIUYQVAUSS-UHFFFAOYSA-N 0.000 description 1
- 229910004298 SiO 2 Inorganic materials 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 150000003983 crown ethers Chemical class 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000012153 distilled water Substances 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 239000012456 homogeneous solution Substances 0.000 description 1
- 239000006259 organic additive Substances 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000035699 permeability Effects 0.000 description 1
- -1 polytetrafluoroethylene Polymers 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 229910001388 sodium aluminate Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000002336 sorption--desorption measurement Methods 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 229910001868 water Inorganic materials 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/16—Alumino-silicates
- B01J20/18—Synthetic zeolitic molecular sieves
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—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
- B01D53/02—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 by adsorption, e.g. preparative gas chromatography
- B01D53/04—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 by adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B39/00—Compounds having molecular sieve and base-exchange properties, e.g. crystalline zeolites; Their preparation; After-treatment, e.g. ion-exchange or dealumination
- C01B39/02—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof; Direct preparation thereof; Preparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactants; After-treatment thereof
- C01B39/46—Other types characterised by their X-ray diffraction pattern and their defined composition
- C01B39/48—Other types characterised by their X-ray diffraction pattern and their defined composition using at least one organic template directing agent
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/102—Nitrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
Definitions
- the present invention belongs to the technical field of microporous crystalline materials of a zeolitic nature, useful in the treatment of natural gas.
- CO 2 is removed from the natural gas stream by chemical reaction with amines in the presence of suitable solvents.
- This technology is the most widely used today in the purification and separation of methane from natural gas.
- this technology suffers from numerous drawbacks.
- the cryogenic distillation for nitrogen removal is extremely demanding from a point of energy view.
- the elimination of CO 2 through capture with amines implies that natural gas must be decompressed, to be pressurized again and thus be transported through gas pipelines. This whole process implies a high energy consumption that has moved many companies to develop new technologies based on membranes or adsorption processes.
- microporous materials and particularly zeolites, has been described in the selective adsorption of CO2 in methane / C ha2 mixtures.
- microporous titanosilicates have been described as molecular doors capable of separating methane from CO2 or Nitrogen CO2 [Nature, 2001, 412, 720-723; US Pat. 6068682 (2000)] depending on the heat treatment conditions to which the adsorbent is subjected.
- the zeolite ERS-7 has been described as an effective material in the separation of methane from gaseous mixtures containing nitrogen and CO 2 [WO2008 / 000380].
- This zeolite has an adsorption capacity of CO 2 approximately three times larger than methane in a pressure range between 2 and 25 bar, with a maximum adsorption capacity of approximately 175 mg of CO 2 per gram of zeolite at O 0 C. It would be desirable to have microporous materials with higher adsorption capacities and that were even more selective towards the adsorption of CO2 in CO 2 / CH 4 mixtures. On the other hand, the selectivity of this zeolite ERS-7 in separation of mixtures of N 2 / CH 4 is very low, having described that the molar ratios of the maximum adsorption capacities of N 2 and CH 4 at 1 bar and 273 K They are always less than 1.5.
- zeolites can be conveniently used in gas separation processes with technology described in the state of the art such as the so-called 'Pressure Swing Adsorption (PSA)', Thermal Swing Adsorption (TSA) 'or' Pressure Vacuum Swing Adsorption (PVSA) 'in those that alternate adsorption cycles with desorption cycles of the adsorbed gas (CO 2 in this case) by washing with a stream of a gas that is not adsorbed in the PSA process (preferably N 2 , CH 4 in the process described in this invention), by heat treatment in the TSA treatment, and by evacuation of the gas adsorbed by vacuum (PVSA).
- PSA Pressure Swing Adsorption
- TSA Thermal Swing Adsorption
- PVSA Pressure Vacuum Swing Adsorption
- the RHO zeolite which presents windows with crystallographic openings of 0.36 x 0.36 nm that give access to large 'quasi-spherical' cavities of 1.15 nm in diameter meets all these requirements, allowing access to CO2 molecules, but preventing it from methane, and therefore they can be used in processes of separation or purification of methane in natural gas streams.
- the zeolites can be classified as oversized, large, medium or small pore zeolites according to the opening of their channels. In this way, small pore zeolites will have channels with openings formed by 8 tetrahedra, while those with a medium pore will be 10 tetrahedra, the large ones of 12 and finally, the extra large ones will have channels with openings greater than 12 tetrahedra,
- the RHO zeolite is a small pore zeolite that has a three-way system of channels with openings of 0.36 x 0.36 nm that intersect forming an almost spherical supercavity of 1.15 nm in diameter and with a network density of 14.7 tetrahedra / nm 3 .
- This porous system gives this zeolite a high adsorption capacity, but only molecules of small kinetic diameter such as water, nitrogen, oxygen and linear hydrocarbons, among others, can access it.
- the present invention relates to a process of separation or purification of hydrocarbons present in a natural gas stream and its recovery, using an isostructural zeolitic material to the RHO zeolite comprising at least the following steps:
- the RHO zeolite is characterized by very different thermodynamic equilibrium adsorption capacities for CO2 and Methane among others, which allows its application in separation and purification processes of methane and other hydrocarbons present in natural gas streams.
- the equilibrium condition is reached when the amount of adsorbate does not increase over time at fixed conditions of adsorbate pressure and temperature.
- the thermodynamic efficiency of an adsorbent in separation processes is determined from the value of its adsorption capacity under equilibrium conditions of the products to be separated, R A.
- zeolites In principle, the greater the adsorption capacity of a zeolite, the lesser amount will be required to separate a given amount of methane-CO 2 mixture. Thus, in order for a certain separation process to be viable at a practical level, zeolites are required have high values of R A and high or moderate adsorption capacities.
- the process described in the present invention can be carried out at a temperature from -100 to 200 0 C, preferably between -25 and 150 0 C, more preferably between 0 and 100 0 C and a pressure between 0.1 and
- 30 bar preferably between 0.5 and 25 bar, more preferably between 1 and
- CO2 is preferably adsorbed and methane is not preferentially adsorbed.
- CO2 is preferably adsorbed and methane and nitrogen are not preferentially adsorbed.
- the mixture of gases that have not been adsorbed, methane and nitrogen can be brought into contact, again in contact with the zeolitic material, with nitrogen being the one that is preferentially adsorbed against methane.
- the CO2 is preferably adsorbed and a mixture of light hydrocarbons of four or less carbons as a component is preferably not adsorbed.
- the CO2 is preferably adsorbed and a mixture of nitrogen and light hydrocarbons of four or less carbons is preferably not adsorbed.
- the mixture of gases that have not been adsorbed, nitrogen and light hydrocarbons can be brought into contact, again in contact with the zeolitic material, with nitrogen being the one that is preferentially adsorbed against light hydrocarbons.
- the denomination of acid gases is known to refer to the set of the following components of natural gas, CO2 and SH 2 .
- the mixture contains acid gases as components that are preferably adsorbed and methane that is not preferably adsorbed.
- the mixture contains acid gases as components that are preferably adsorbed and methane and nitrogen as components that are not preferably adsorbed.
- the mixture of gases that have not been adsorbed, nitrogen and methane can be contacted again in contact with the zeolitic material with nitrogen being the one that is preferentially adsorbed against methane.
- the mixture contains acid gases as components that are preferably adsorbed and a mixture of light hydrocarbons of four or less carbons as a component that is not preferably adsorbed.
- the mixture contains acid gases as components that are preferably adsorbed and a mixture of nitrogen and light hydrocarbons of four or less carbons as a component that is not preferably adsorbed.
- the mixture of gases that have not been adsorbed, nitrogen and light hydrocarbons can be brought into contact, again in contact with the zeolitic material, with nitrogen being the one that is preferentially adsorbed against light hydrocarbons.
- the RHO zeolite has very different adsorption capacities for CO 2 and methane, with high adsorption capacities of CO 2 .
- the zeolite RHO has an adsorption capacity of CO 2 of more than 100 mg / g to 1000 mbar and in the range of temperatures between 10 and 6O 0 C and adsorption capacity of less than 10 mg / g for methane under these same conditions. Therefore, the RHO zeolite is a very suitable adsorbent to carry out methane separation or purification processes in natural gas streams.
- the separation process of this invention implies that a certain amount of RHO zeolite is contacted with a mixture of gases (natural gas) containing, among others, CO 2 and methane and in which preferably CO2 is adsorbed inside the RHO zeolite.
- the mixture of CO2 and methane and the RHO zeolite is kept in contact for a certain time to enable the adsorption process to take place and, finally, the mixture of gases that have not been adsorbed is removed.
- the gas adsorbed in the zeolite is recovered by means of techniques such as entrainment with another gas, temperature increase, evacuation or combination of the above methods.
- This separation process can also be carried out in columns, in which case different fronts of CO2 and methane are obtained as they are more or less strongly retained by the bed of zeolite RHO.
- the separation conditions will depend on the precise composition of the gas mixture containing methane and CO2 that is intended to be separated.
- the lower limit of pressure and separation temperature will correspond to the conditions in which the condensation of CO 2 occurs.
- the process of this invention can be carried out between -100 and 200 0 C, preferably between -25 and 150 0 C, more preferably between 0 and 100 0 C and a pressure between 0.1 and 30 bar, preferably between 0.5 and 25 bar, more preferably between 1 and 10 bar.
- Example 1 Preparation of the isostructural material with the RHO zeolite. 0.98 g of crown ether 18-6 are mixed, the structure of which is shown in Figure 1, 0.705 g of Cs (OH), 0.45 g of NaOH and 6.04 g of distilled water. The mixture is stirred until complete dissolution is achieved. Then, 1.32 g of sodium aluminate (54% AI2O3, 32.8% Na 2 O, 13.2% H 2 O) are added and stirred until a homogeneous solution is obtained. Finally, 10.5 g of silica suspension (Ludox AS-40) are added and the mixture is stirred for 24 hours. The composition of the gel is:
- the mixture obtained is introduced into an autoclave provided with an internal polytetrafluoroethylene sheath and introduced into a preheated oven at 125 ° C for 5 days with stirring.
- the X-ray diffractogram of the solid obtained indicates that the material has been obtained.
- the calcination at 600 0 C in air for 3 hours allows to eliminate the occluded organic species and obtain the RHO material capable of being used in adsorption and separation processes.
- the measurement of the adsorption capacity of CO 2 of the RHO material, prepared according to example 1 at 1O 0 C and 5000 mbar corresponds to 244 mg / g. Also, the value obtained after performing 20 adsorption / desorption cycles is 235 mg / g, which shows that the material
- the measurement of the adsorption capacity of CO 2 of the RHO material, prepared according to example 1 at 1O 0 C and 5000 mbar corresponds to 4 mg / g.
- Example 4 Adsorption of CO 2 at 5000 mbar in the RHO material at 25 0 C.
- the measurement of the adsorption capacity of CO 2 of the RHO material, prepared according to example 1 at 25 0 C and 5000 mbar corresponds to 234 mg / g.
- the measurement of the CO2 adsorption capacity of the RHO material, prepared according to example 1 at 25 0 C and 5000 mbar corresponds to 5 mg / g.
- Example 6 Adsorption of CO 2 at 5000 mbar in the RHO material at 45 0 C.
- the measurement of the CO2 adsorption capacity of the RHO material, prepared according to example 1 at 45 0 C and 5000 mbar corresponds to 206 mg / g .
- Example 7 Adsorption of methane at 5000 mbar RHO material 45 0 C.
- the measurement of the CO2 adsorption capacity of the RHO material, prepared according to example 1 at 45 0 C and 5000 mbar corresponds to 6 mg / g.
- Example 8 Adsorption of CO 2 at 5000 mbar in the RHO material at 6O 0 C.
- the measurement of the CO2 adsorption capacity of the RHO material, prepared according to example 1 at 6O 0 C and 5000 mbar corresponds to 180 mg / g .
- Example 9 Adsorption of methane at 5000 mbar in the RHO material at 6O 0 C.
- the measurement of the CO2 adsorption capacity of the RHO material, prepared according to example 1 at 6O 0 C and 5000 mbar corresponds to 7 mg / g.
- Example 10 Adsorption of methane at 1000 mbar in the RHO material at 1O 0 C.
- the adsorption kinetics of methane on the RHO material, prepared according to example 1, indicates that in 30 minutes 0.5 mg of methane are adsorbed.
- Example 11 Adsorption of nitrogen at 1000 mbar in the RHO material at 1O 0 C.
- the adsorption kinetics of methane on the RHO material, prepared according to example 1, indicates that in 30 minutes 3 mg of nitrogen are adsorbed.
- Figure 1 the structure of the organic additive used in example 1 for the synthesis of an isostructural material to the RHO zeolite is shown.
- Figure 2 the values of the adsorption capacity in the CO2 and CH 4 equilibrium of the RHO material, prepared according to example 1, at different pressures and different temperatures are shown. It can be seen that methane isobars are indistinguishable from each other due to the low adsorption capacity of the RHO Zeolite at any temperature and / or pressure compared to those determined for CO2.
- Figure 3 The adsorption kinetics of methane and nitrogen are shown at 1O 0 C and at 1000 mbar of gas pressure in an RHO material, prepared according to Example 1. It can be seen that nitrogen diffuses more rapidly than methane under these conditions.
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Abstract
Description
Claims
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2012505194A JP5732451B2 (ja) | 2009-04-17 | 2010-04-19 | 天然ガス処理における、rho構造を備えるゼオライト特性の微孔性結晶性材料の使用 |
CN201080017196.5A CN102439123B (zh) | 2009-04-17 | 2010-04-19 | 具有rho结构的沸石性质微孔晶体材料在天然气加工过程中的应用 |
AU2010238431A AU2010238431B2 (en) | 2009-04-17 | 2010-04-19 | Use of a microporous crystalline material of zeolitic nature with RHO structure in natural gas processing |
EP10764136.7A EP2420551B1 (en) | 2009-04-17 | 2010-04-19 | Use of a microporous crystalline material of zeolitic nature with rho structure in natural gas processing |
US13/272,586 US8337594B2 (en) | 2009-04-17 | 2011-10-13 | Use of a microporous crystalline material of zeolitic nature with RHO structure in natural gas processing |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
ESP200901136 | 2009-04-17 | ||
ES200901136A ES2346627B1 (es) | 2009-04-17 | 2009-04-17 | Uso de un material cristalino microporoso de naturaleza zeolitica conestructura rho en tratamiento de gas natural. |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
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US13/272,586 Continuation US8337594B2 (en) | 2009-04-17 | 2011-10-13 | Use of a microporous crystalline material of zeolitic nature with RHO structure in natural gas processing |
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WO2010119163A1 true WO2010119163A1 (es) | 2010-10-21 |
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US8337594B2 (en) | 2012-12-25 |
EP2420551B1 (en) | 2020-11-18 |
EP2420551A4 (en) | 2013-01-30 |
ES2346627B1 (es) | 2011-08-08 |
AU2010238431B2 (en) | 2016-03-17 |
EP2420551A1 (en) | 2012-02-22 |
US20120067216A1 (en) | 2012-03-22 |
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CN102439123A (zh) | 2012-05-02 |
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