CN106132495B - 用于从含有co2和no2的流体中分离no2的方法和装置 - Google Patents
用于从含有co2和no2的流体中分离no2的方法和装置 Download PDFInfo
- Publication number
- CN106132495B CN106132495B CN201580015837.6A CN201580015837A CN106132495B CN 106132495 B CN106132495 B CN 106132495B CN 201580015837 A CN201580015837 A CN 201580015837A CN 106132495 B CN106132495 B CN 106132495B
- Authority
- CN
- China
- Prior art keywords
- stream
- flow
- gaseous
- fluid
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000012530 fluid Substances 0.000 claims abstract description 43
- 239000007789 gas Substances 0.000 claims abstract description 35
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 28
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims abstract description 26
- 239000001301 oxygen Substances 0.000 claims abstract description 26
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 26
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 25
- 238000000034 method Methods 0.000 claims abstract description 22
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 14
- 229910052786 argon Inorganic materials 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims description 70
- 229920000570 polyether Polymers 0.000 claims description 49
- 239000003546 flue gas Substances 0.000 claims description 38
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 35
- 239000004721 Polyphenylene oxide Substances 0.000 claims description 35
- 229920001400 block copolymer Polymers 0.000 claims description 32
- 239000000047 product Substances 0.000 claims description 29
- 238000007906 compression Methods 0.000 claims description 20
- 230000006835 compression Effects 0.000 claims description 20
- -1 polysiloxanes Polymers 0.000 claims description 19
- 238000004132 cross linking Methods 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 10
- 229920001296 polysiloxane Polymers 0.000 claims description 10
- 238000010926 purge Methods 0.000 claims description 9
- 230000003204 osmotic effect Effects 0.000 claims description 8
- 239000012466 permeate Substances 0.000 claims description 8
- 238000005201 scrubbing Methods 0.000 claims description 7
- 238000001035 drying Methods 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 6
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 5
- 239000000446 fuel Substances 0.000 claims description 5
- 229910017604 nitric acid Inorganic materials 0.000 claims description 5
- 230000008595 infiltration Effects 0.000 claims description 3
- 238000001764 infiltration Methods 0.000 claims description 3
- 239000007800 oxidant agent Substances 0.000 claims description 2
- 230000001590 oxidative effect Effects 0.000 claims description 2
- 238000012661 block copolymerization Methods 0.000 claims 1
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 73
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 36
- 239000001569 carbon dioxide Substances 0.000 abstract description 8
- 238000011144 upstream manufacturing Methods 0.000 abstract description 6
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 26
- 229910052799 carbon Inorganic materials 0.000 description 17
- 239000012071 phase Substances 0.000 description 13
- 150000001721 carbon Chemical group 0.000 description 11
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 10
- 238000004064 recycling Methods 0.000 description 10
- 125000001931 aliphatic group Chemical group 0.000 description 9
- 125000003118 aryl group Chemical group 0.000 description 9
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 238000001816 cooling Methods 0.000 description 8
- 230000003252 repetitive effect Effects 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 239000002253 acid Substances 0.000 description 6
- 230000008859 change Effects 0.000 description 6
- 150000002148 esters Chemical class 0.000 description 6
- 239000012948 isocyanate Substances 0.000 description 6
- 229920000642 polymer Polymers 0.000 description 6
- 238000000746 purification Methods 0.000 description 6
- PUPZLCDOIYMWBV-UHFFFAOYSA-N (+/-)-1,3-Butanediol Chemical compound CC(O)CCO PUPZLCDOIYMWBV-UHFFFAOYSA-N 0.000 description 5
- 239000002202 Polyethylene glycol Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 5
- 229920001577 copolymer Polymers 0.000 description 5
- 239000003431 cross linking reagent Substances 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- 239000007791 liquid phase Substances 0.000 description 5
- 238000006722 reduction reaction Methods 0.000 description 5
- 238000003860 storage Methods 0.000 description 5
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 4
- 239000004202 carbamide Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 150000004985 diamines Chemical class 0.000 description 4
- 125000005442 diisocyanate group Chemical group 0.000 description 4
- 150000002513 isocyanates Chemical class 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000000178 monomer Substances 0.000 description 4
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 4
- 229920001223 polyethylene glycol Polymers 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- 239000004971 Cross linker Substances 0.000 description 3
- 229920002292 Nylon 6 Polymers 0.000 description 3
- 239000004952 Polyamide Substances 0.000 description 3
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical group [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 3
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 3
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 3
- 238000010521 absorption reaction Methods 0.000 description 3
- 150000001408 amides Chemical class 0.000 description 3
- UHOVQNZJYSORNB-UHFFFAOYSA-N benzene Substances C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 230000002708 enhancing effect Effects 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 125000004430 oxygen atom Chemical group O* 0.000 description 3
- 229920002647 polyamide Polymers 0.000 description 3
- 239000002861 polymer material Substances 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 229910052710 silicon Inorganic materials 0.000 description 3
- 229920002379 silicone rubber Polymers 0.000 description 3
- 230000032258 transport Effects 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- JHWNWJKBPDFINM-UHFFFAOYSA-N Laurolactam Chemical compound O=C1CCCCCCCCCCCN1 JHWNWJKBPDFINM-UHFFFAOYSA-N 0.000 description 2
- JCXJVPUVTGWSNB-UHFFFAOYSA-N Nitrogen dioxide Chemical compound O=[N]=O JCXJVPUVTGWSNB-UHFFFAOYSA-N 0.000 description 2
- 229920003171 Poly (ethylene oxide) Polymers 0.000 description 2
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 239000000460 chlorine Substances 0.000 description 2
- 229910052801 chlorine Inorganic materials 0.000 description 2
- 150000001805 chlorine compounds Chemical class 0.000 description 2
- 239000000539 dimer Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000003628 erosive effect Effects 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 125000000524 functional group Chemical group 0.000 description 2
- XXMIOPMDWAUFGU-UHFFFAOYSA-N hexane-1,6-diol Chemical compound OCCCCCCO XXMIOPMDWAUFGU-UHFFFAOYSA-N 0.000 description 2
- 125000001841 imino group Chemical group [H]N=* 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 description 2
- 238000006068 polycondensation reaction Methods 0.000 description 2
- 238000006116 polymerization reaction Methods 0.000 description 2
- 229920001451 polypropylene glycol Polymers 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- KIDHWZJUCRJVML-UHFFFAOYSA-N putrescine Chemical compound NCCCCN KIDHWZJUCRJVML-UHFFFAOYSA-N 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 230000005514 two-phase flow Effects 0.000 description 2
- BJZYYSAMLOBSDY-QMMMGPOBSA-N (2s)-2-butoxybutan-1-ol Chemical compound CCCCO[C@@H](CC)CO BJZYYSAMLOBSDY-QMMMGPOBSA-N 0.000 description 1
- PXFBZOLANLWPMH-UHFFFAOYSA-N 16-Epiaffinine Natural products C1C(C2=CC=CC=C2N2)=C2C(=O)CC2C(=CC)CN(C)C1C2CO PXFBZOLANLWPMH-UHFFFAOYSA-N 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- GXGJIOMUZAGVEH-UHFFFAOYSA-N Chamazulene Chemical group CCC1=CC=C(C)C2=CC=C(C)C2=C1 GXGJIOMUZAGVEH-UHFFFAOYSA-N 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- PIICEJLVQHRZGT-UHFFFAOYSA-N Ethylenediamine Chemical class NCCN PIICEJLVQHRZGT-UHFFFAOYSA-N 0.000 description 1
- SJSBUCKRFUPVIG-UHFFFAOYSA-N NCC(C(=O)O)O.NC(CO)C(=O)O Chemical compound NCC(C(=O)O)O.NC(CO)C(=O)O SJSBUCKRFUPVIG-UHFFFAOYSA-N 0.000 description 1
- 239000007832 Na2SO4 Substances 0.000 description 1
- 229920000299 Nylon 12 Polymers 0.000 description 1
- 229920002614 Polyether block amide Polymers 0.000 description 1
- 235000010891 Ptelea trifoliata Nutrition 0.000 description 1
- 239000005700 Putrescine Substances 0.000 description 1
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- OUUQCZGPVNCOIJ-UHFFFAOYSA-M Superoxide Chemical compound [O-][O] OUUQCZGPVNCOIJ-UHFFFAOYSA-M 0.000 description 1
- UKLDJPRMSDWDSL-UHFFFAOYSA-L [dibutyl(dodecanoyloxy)stannyl] dodecanoate Chemical compound CCCCCCCCCCCC(=O)O[Sn](CCCC)(CCCC)OC(=O)CCCCCCCCCCC UKLDJPRMSDWDSL-UHFFFAOYSA-L 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 125000000217 alkyl group Chemical group 0.000 description 1
- 229910052925 anhydrite Inorganic materials 0.000 description 1
- 125000004429 atom Chemical group 0.000 description 1
- CDQSJQSWAWPGKG-UHFFFAOYSA-N butane-1,1-diol Chemical compound CCCC(O)O CDQSJQSWAWPGKG-UHFFFAOYSA-N 0.000 description 1
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 1
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 description 1
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 1
- 238000010531 catalytic reduction reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 235000013399 edible fruits Nutrition 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000002803 fossil fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 238000000227 grinding Methods 0.000 description 1
- RRAMGCGOFNQTLD-UHFFFAOYSA-N hexamethylene diisocyanate Chemical compound O=C=NCCCCCCN=C=O RRAMGCGOFNQTLD-UHFFFAOYSA-N 0.000 description 1
- XTBMQKZEIICCCS-UHFFFAOYSA-N hexane-1,5-diamine Chemical compound CC(N)CCCCN XTBMQKZEIICCCS-UHFFFAOYSA-N 0.000 description 1
- NAQMVNRVTILPCV-UHFFFAOYSA-N hexane-1,6-diamine Chemical compound NCCCCCCN NAQMVNRVTILPCV-UHFFFAOYSA-N 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000003999 initiator Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 229910052753 mercury Inorganic materials 0.000 description 1
- 238000005453 pelletization Methods 0.000 description 1
- 238000005373 pervaporation Methods 0.000 description 1
- DGTNSSLYPYDJGL-UHFFFAOYSA-N phenyl isocyanate Chemical compound O=C=NC1=CC=CC=C1 DGTNSSLYPYDJGL-UHFFFAOYSA-N 0.000 description 1
- 229910021420 polycrystalline silicon Inorganic materials 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 229920000909 polytetrahydrofuran Polymers 0.000 description 1
- 229920002635 polyurethane Polymers 0.000 description 1
- 239000004814 polyurethane Substances 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 229960004063 propylene glycol Drugs 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000005096 rolling process Methods 0.000 description 1
- 238000009738 saturating Methods 0.000 description 1
- 229920005573 silicon-containing polymer Polymers 0.000 description 1
- 125000004469 siloxy group Chemical group [SiH3]O* 0.000 description 1
- 235000017550 sodium carbonate Nutrition 0.000 description 1
- 235000011121 sodium hydroxide Nutrition 0.000 description 1
- 229910052938 sodium sulfate Inorganic materials 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- PJANXHGTPQOBST-VAWYXSNFSA-N trans-stilbene Chemical group C=1C=CC=CC=1/C=C/C1=CC=CC=C1 PJANXHGTPQOBST-VAWYXSNFSA-N 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
- 238000004804 winding Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D19/00—Degasification of liquids
- B01D19/0031—Degasification of liquids by filtration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/145—One step being separation by permeation
-
- 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
- B01D53/002—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 condensation
-
- 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
- B01D53/22—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 diffusion
-
- 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
- B01D53/22—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 diffusion
- B01D53/229—Integrated processes (Diffusion and at least one other process, e.g. adsorption, absorption)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/362—Pervaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/48—Polyesters
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/52—Polyethers
- B01D71/521—Aliphatic polyethers
- B01D71/5211—Polyethylene glycol or polyethyleneoxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0266—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of carbon dioxide
-
- 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
- B01D2256/22—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/40—Nitrogen compounds
- B01D2257/404—Nitrogen oxides other than dinitrogen oxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/45—Gas separation or purification devices adapted for specific applications
- B01D2259/4516—Gas separation or purification devices adapted for specific applications for fuel vapour recovery systems
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/08—Specific process operations in the concentrate stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/13—Use of sweep gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2669—Distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2323/00—Details relating to membrane preparation
- B01D2323/30—Cross-linking
-
- 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
- B01D53/22—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 diffusion
- B01D53/228—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 diffusion characterised by specific membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/56—Polyamides, e.g. polyester-amides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
- B01D71/06—Organic material
- B01D71/76—Macromolecular material not specifically provided for in a single one of groups B01D71/08 - B01D71/74
- B01D71/80—Block polymers
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/40—Features relating to the provision of boil-up in the bottom of a column
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/80—Processes or apparatus using other separation and/or other processing means using membrane, i.e. including a permeation step
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/04—Mixing or blending of fluids with the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/70—Flue or combustion exhaust gas
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/80—Carbon dioxide
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/82—Separating low boiling, i.e. more volatile components, e.g. He, H2, CO, Air gases, CH4
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/80—Separating impurities from carbon dioxide, e.g. H2O or water-soluble contaminants
- F25J2220/84—Separating high boiling, i.e. less volatile components, e.g. NOx, SOx, H2S
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/30—Compression of the feed stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/80—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being carbon dioxide
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/80—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being carbon dioxide
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/02—Internal refrigeration with liquid vaporising loop
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/04—Internal refrigeration with work-producing gas expansion loop
-
- 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
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
-
- 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
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Water Supply & Treatment (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Inorganic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Carbon And Carbon Compounds (AREA)
Abstract
一种用于从含有二氧化碳,NO2,以及氧气、氩气、和氮气中的至少一种的流体中分离二氧化碳的方法,包括以下步骤:将该流体的至少一部分分离成富二氧化碳流,包含CO2以及氧气、氩气、和氮气中的至少一种的贫二氧化碳流,以及富NO2流,并且在该分离步骤的上游再循环所述富NO2流。
Description
相关申请的交叉引用
本申请根据35U.S.C.§119(e)要求于2014年3月28提交的美国临时专利申请号61/971,840以及2014年4月30日提交的美国专利申请号14/265,710 的优先权的权益,这些申请的全部内容通过引用结合在此。
背景
发明领域
本发明涉及一种用于分离气态混合物的方法和装置,该气态混合物包含二氧化碳作为主要成分。本发明特别涉及用于纯化例如来自如发生在氧燃烧化石燃料或生物质电厂中的含碳燃料的燃烧的二氧化碳的方法和装置。
相关技术
含碳燃料的燃烧产生CO2和气体例如SO2、SO3、和NOx,这些气体污染大气并且是温室效应的主要贡献者-尤其是CO2。这些CO2排放集中在四个主要领域:发电、工业过程、运输、以及住宅和商业建筑。目前来自发电和工业领域的到大气中的大部分CO2的排放是处于来自燃烧的烟道气的形式,其中CO2浓度典型地是按体积计4%-14%(对于空气点火的燃烧)或者按体积计最高达60%-70%(对于氧燃烧),尽管通过几种工业过程产生了高浓度的CO2。
原则上,该烟道气可能被纯化并且存储,在这种情况下该烟道气将必须被压缩到典型地大于100巴绝对值的压力,一个将消耗过多量的能量的压力。用于从烟道气中回收并且纯化CO2的系统有时候被称为CO2纯化单元或CPU。由于这些原因,优选的是生产较高纯度的CO2流用于运输、现场消耗、或存储。此二氧化碳可用于增强的油回收或仅仅注入贫气田和油田或含水层中。
在现今CO2捕获面临的众多问题之中,被送到地下存储(EOR或地质封存)的CO2的纯度是有待解决的更棘手问题之一。这是由于清楚地理解并且模拟在地下元件与注入的气体以及管道腐蚀之间的相互作用的巨大困难。
在从烟道气捕获的CO2中通常发现的一种类型的酸性气体是NOx。NOx,意思是一种或多种氮的氧化物,包括NO、N2O、N2O4、和NO2以及 N2O3。低于158℃,NO2与其聚合物/二聚物N2O4相平衡,其中温度越低,与NO2相比的N2O4浓度越高。在此文件中,词语NO2用于指不仅是NO2而且是处于平衡的其聚合物/二聚物N2O4。
在该CPU过程中不一定去除NOx化合物。然而,一些应用要求无NOx的CO2。
有些人已经提出了使用脱NOx塔通过从CO2中分离NO2来从烟道气中去除NOx,因为NO2的临界温度高于CO2的临界温度。使用脱NOx塔仍然呈现处理该液体底部的富NO2流体的挑战。例如,US 7,708,804提出了使用脱NOx塔,其中以三种方式之一处理来自该脱NOx塔的底部的富NO2液体。首先,可以将该富NO2液体再循环到该压缩机的入口。第二,可以将该富NO2液体送到洗涤塔中。第三,可以将该富NO2液体在与锅炉(其本身可以是该烟道气的来源)相关联的燃烧器处燃烧,试图将NO2还原为N2。
关于第一技术,将该富NO2流体再循环到该压缩机的入口是不利的。因为该再循环流可以占该压缩机下游的被压缩且被处理的总流量的约 5%-10%,所以该压缩机和下游设备必须被确定尺寸为比如果该富NO2流另外不被再循环将必须是的尺寸大5%-10%。在所要求的压缩能量上还将存在5%至10%的增加。此外,被压缩的烟道气的相对较高的酸性气体含量将在这些压缩机内产生较大量的酸性气体冷凝物。因此,与不存在NO2再循环流相比,这些压缩机和干燥器将经受更严重的酸性侵蚀。这种更酸性的侵蚀将导致这些压缩机的减少的使用寿命或者要求该压缩机由更昂贵的材料构成,该材料足够抵抗此类酸流体。由于酸性气体的存在,将预期发生对这些干燥器的类似负面影响。最后,为了减少被再循环到该压缩机的 NO2量,可以降低到该脱NOx塔的回流液体流量。然而,到该脱NOx塔的回流液体流量的减少可能很快导致该塔超过其润湿性极限。这将导致不令人满意的蒸馏效率降低。
因此,本发明的一个目的是提供一种从烟道气纯化CO2的方法和系统,该方法和系统不要求将富NO2流体再循环到该纯化方法的上游的点处。
关于第二技术,不在该CPU入口处再循环经洗涤的流的情况下,洗涤塔的使用将导致显著的CO2损失。如果相反在CPU入口处再循环经洗涤的流,可以避免显著的CO2损失。然而,这遭受了增加该压缩机和下游设备的尺寸以容纳增加的流量的相同的以上缺点。
因此,本发明的另一个目的是提供一种从烟道气纯化CO2的方法和系统,该方法和系统不要求使用洗涤塔用于从脱NOx塔的底部去除NO2。
关于第三技术,以来自脱NOx塔的富NO2流的规模在燃烧器的火焰中的NO2还原呈现了技术上非常有挑战性的问题。无论此种方法的相对发展状况如何,在该燃烧器火焰中的NOx还原仍然导致显著的CO2损失。
因此,本发明的一个目的是提供一种从含有令人满意的低量NOx的烟道气的纯化来生产CO2产物的更可靠的方式。
发明内容
披露了一种用于从含有CO2和NO2的流体中分离NO2的方法。该方法包括以下步骤。将包含CO2,NO2,以及氧气、氩气、和氮气中的至少一种的流体进料到精馏蒸馏塔中。从该精馏塔中抽取出第一气态流,相对于包含CO2,NO2,以及氧气、氩气、和氮气中的至少一种的该流体,该第一气态流富含CO2并且缺乏NO2。从该精馏塔中抽取出液体流,相对于包含 CO2,NO2,以及氧气、氩气、和氮气中的至少一种的该流体,该液体流富含NO2。将该富含NO2的液体流进料到流体分离膜中。从该膜中抽取出包含渗透气体的第二气态流,相对于被进料到该膜中的液体流,该第二气态流富含NO2并且缺乏CO2。从该膜中抽取出非渗透液体流,相对于被进料到该膜中的液体流,该非渗透液体流缺乏NO2并且富含CO2。将该非渗透液体流再循环到该精馏塔中。
还披露了一种用于从含有CO2和NO2的流体中分离NO2的装置,该装置包括:包含NO2和CO2的流体的源;接收该源流体的精馏蒸馏塔;流体分离膜,该流体分离膜接收来自该精馏塔的液体流并且产生液体非渗透流和气态渗透流;以及泵,该泵将来自该膜的该非渗透液体进料到该精馏塔中。
该方法和装置的任何一者或两者可包括以下方面中的一项或多项:
-通过以下方式生产包含CO2,NO2,以及氧气、氩气、和氮气中的至少一种的该流体:在压缩机处压缩烟道气,接着是在热交换器处干燥并且至少部分冷凝该压缩的烟道气。
-在热交换器处至少部分地冷凝该第一气态流;在相分离器处分离该至少部分冷凝的流以产生相对于该第一气态流富含氧气、氩气和氮气中的至少一种的第三气态流以及相对于该第一气态流富含CO2的液体流;将该富含CO2的液体流进料到汽提塔中;将从该汽提塔中抽取出的第四气态流进料到该压缩机的吸入口中;并且从该汽提塔中抽取出液体产物CO2流。
-使该液体产物CO2流膨胀以提供两相产物CO2流;在热交换器处蒸发该两相产物CO2流中的任何液体组分以提供完全气态的产物CO2流;并且压缩并且加热该完全气态的产物CO2流以提供超临界产物CO2流。
-将吹扫气体进料到该流体分离膜中,其中该第二气态流进一步包含该吹扫气体。
-将该第二气态流进料到洗涤塔中以溶解存在于该第二气态流中的该NO2的至少一些并且形成硝酸。
-在锅炉中用氧化剂燃烧燃料以产生该燃料气体,其中该烟道气具有大于300ppm的NOx含量。
-该流体分离膜的分离层包括选自下组的材料,该组由以下各项组成:交联的聚硅氧烷共聚醚、聚氨酯-聚醚嵌段共聚物、聚(脲)-聚(醚)嵌段共聚物、聚(酯)-聚(醚)嵌段共聚物、以及聚(酰胺)-聚(醚)嵌段共聚物。
-热交换器至少部分地冷凝来自该精馏塔的气态流;相分离器接收来自该热交换器的该至少部分冷凝的流并且产生包含大部分N2、O2、和/ 或Ar的气态流以及包含大部分CO2的液体流;汽提蒸馏塔接收来自该相分离器的该包含大部分CO2的液体流,该汽提塔被适配并且配置成将该包含大部分CO2的液体流的内容物分离成气态流和液体CO2产物流。
-压缩机和干燥单元被适配并且配置成压缩并且干燥该源流体,其中该热交换器还被适配并且配置成至少部分地冷凝在被进料到该精馏塔中之前的该压缩的且干燥的源流体。
-该流体源是被适配并且配置成产生烟道气的锅炉并且该烟道气是包含NO2和CO2的流体。
-该压缩机还接收该来自汽提塔的气态流。
-压缩机和加热器压缩并且加热该完全气态的CO2产物流以提供超临界产物CO2流。
-该膜还在该膜的渗透侧接收该吹扫气体。
-洗涤塔接收该气态渗透流并且溶解存在于气态渗透流中的该NO2的至少一些以形成硝酸。
-该膜包括分离层,该分离层包括选自下组的材料,该组由以下各项组成:交联的聚硅氧烷共聚醚、聚氨酯-聚醚嵌段共聚物、聚(脲)-聚(醚) 嵌段共聚物、聚(酯)-聚(醚)嵌段共聚物、以及聚(酰胺)-聚(醚)嵌段共聚物。
附图简要说明
图1是氧燃烧设备的示意图。
图2是压缩和纯化单元的示意图。
图3示出了低温纯化单元。
发明详细说明
现在将参考附图进一步详细说明本发明。
图1是氧燃烧设备的示意图。空气分离单元2产生了95-98mol.%的典型纯度的氧气流10和废氮气流13。氧气流10被分成两个子流11和12。初级烟道气再循环流15穿过磨煤机3,在该磨煤机中煤14被粉碎。子流11与磨煤机3的下游的该再循环流混合,并且将该混合物引入到锅炉1的燃烧器中。子流12与次级烟道气再循环流16混合,该次级烟道气再循环流将附加的压载物提供给这些燃烧器以保持该炉内的温度在可接受水平下。将一个或多个水流引入锅炉1中以便产生一个或多个蒸汽流18,该一个或多个蒸汽流在蒸汽轮机8中膨胀。
本领域普通技术人员将认识到,根据本发明的有待被处理的烟道气可代替地来源于不同于图1中示出的那种的熟知的任何氧燃烧方案。
富含CO2(典型地含有基于干基的大于70mol.%)的烟道气流19通过若干处理以去除一些杂质。单元4是NOx去除系统,如选择性催化还原单元(SCR)。单元5是除尘系统,如静电除尘器和/或袋式过滤器。单元6是被适配并且配置成去除SO2和/或SO3的脱硫系统。取决于CO2产品规格,单元4和6可以不是必要的。然后将烟道气流24引入压缩和纯化单元7中以便产生适合于运输、注入管道内、用于增强的油回收中、和/或封存于地质地层中的高CO2纯度的流25。单元7还产生了废物流26。
虽然图1的烟道气来源于氧燃烧,本领域普通技术人员将认识到,降低的NOx CO2产物还可从来源于空气点火的燃烧或富氧气燃烧的烟道气产生。
图2是压缩和纯化单元的示意图,该压缩和纯化单元可用作图1中的单元7。烟道气流110(对应于图1的流24)进入低压预处理单元101,在该低压预处理单元中使该烟道气流准备用于压缩单元102。此单元可包括,例如,除其他步骤外,
-在湿式洗涤器中的除尘步骤和/或干燥过程,或者动态的(例如脉冲喷射筒)或静态的(如袋和筒);
-用水和/或苏打灰或苛性钠喷射在湿式洗涤器中的(另外的)脱硫步骤;以及
-冷却步骤,以便既通过水冷凝使流量最小化,又由于流量和温度的降低使压缩单元的功率最小化。
一个或多个废流111可包括冷凝水、灰尘和溶解的物种,像H2SO4、 HNO3、Na2SO4、CaSO4、Na2CO3、和CaCO。
压缩单元102将流112从接近于大气压的压力压缩至典型地在15与60 巴绝对值之间、优选地约30巴绝对值的高压。这种压缩可在具有中间冷却的若干阶段中完成。在这种情况下,可以产生某一或一些冷凝物113。此一种或多种冷凝物113典型地包括由NO2和水的反应形成的HNO3。压缩热可以在中间冷却步骤中例如在预加热锅炉给水中有效地被回收。热流114 离开压缩单元102并进入高压预处理单元103。
高压预处理单元103至少包括:
-一个或若干个冷却步骤,以便降低温度并且减少水含量;以及
-干燥步骤,以去除大部分水,例如通过吸附。
高压预处理单元103还可以包括,但不限于:
-用于冷却和/或纯化的高压洗涤塔;以及
-除汞步骤。
来自单元103的流出物包括气态流115(该干燥步骤的再生流)并且可以包括一个或多个液体流116/117(来自该冷却步骤和/或该高压洗涤塔)。
流114可能含有NO2。在这种情况下,有时优选的是通过单元104上游的吸附去除NO2。在这种情况下,流114可以通过吸附进行处理,并且用于使吸附剂再生的再生气体被去除,该再生气体与流114相比具有富含NO2的含量。气态流115可任选地至少部分地在压缩单元102的上游、预处理单元101的上游再循环或再循环到燃烧单元的锅炉1中。
单元104是低温纯化单元。在这种情况下,低温是指在用于该烟道气的纯化的方法循环中的最低温度,该温度低于0℃、并且优选地低于-20℃、尽可能接近于纯CO2的三相点温度(-56.6℃)。在此单元中,在一个(或若干个步骤)中冷却并且部分冷凝流118。富含CO2的一个(或若干个)液相流被回收、膨胀且蒸发以便具有富含CO2的产物119。可以在现场使用此种气态CO2产物。可替代地,该一个或多个富含CO2的回收的液相流可以被保持为液体形式并且根据已知技术调节压力和温度以提供适合于存储、现场消耗、或通过长管拖车运输的液体产物CO2流。作为另一种替代方案,根据已知技术可以调节该一个或多个富含CO2的回收的液相流的压力和温度以提供适合于注入管道内或封存于地质地层中的超临界产物CO2流。一个(或若干个)不可冷凝的高压流120被回收并且能够在膨胀器中膨胀。
单元104包括精馏蒸馏塔,该精馏蒸馏塔使含有NO2和CO2的进料流体分离成富CO2气态流和富NO2液体流(相对于在该进料流体中的NO2和CO2的浓度)。该进料流体可以由流118组成或者在进一步处理流118之后可以来源于流118。
单元104还包括流体分离膜(在渗透蒸发条件下操作的),该流体分离膜使来自该精馏塔的富NO2液体流分离成富NO2气态渗透流和液体非渗透流。将该液体非渗透流再循环到该精馏塔中。
单元104还包括相分离器,该相分离器使来自该精馏塔的富CO2气态流膨胀并且将其分离成气态流(用于最终排放)和用于进料到汽提蒸馏塔(其还接收来源于该液体非渗透流的至少一部分的蒸发的汽提流体)中的液体流。该蒸馏塔将来自该汽提流体和该液体流(来自该相分离器)的组合的内容物的不可冷凝的组分(O2、N2、和Ar)汽提成气态流和该一个或多个富含CO2的液相流。可以将来自该汽提塔的气态流与被进料到该精馏塔中的进料流体组合。
可以进一步处理富CO2产物119以便以所希望的任何形式(气态的、液体、超临界的、固体)和压力/温度提供其。在封存的情况下,富CO2产物 119可以被进一步压缩冷凝并且然后进一步用泵压缩以便在高压(典型地 100至200巴绝对值)下被递送用于注入至通向封存地点的管道内。
图3示出了低温纯化单元,该低温纯化单元可用作图2中的单元104。在此种单元中运行根据本发明的至少一个过程。
包含在约30巴下并且在15℃与43℃之间的温度下的烟道气的流118主要含有二氧化碳而且还包括较少量的NO2、氧气、氩气和氮气。NOx的实际量将取决于已经在这些干燥器中吸附多少NOx随时间的推移而变化。典型地,该入口NOx将在0ppm与500ppm之间变化。NOx的实际量还将取决于产生该烟道气的燃烧器的类型。流118可以通过单元103已经在所希望的压力条件下产生或者可以使用任选的压缩机124使该流达到所希望的压力水平。交替地将压缩的烟道气流127引导至两个干燥器129、131之一中。当正在操作这些干燥器129、131之一以干燥流127时,再生这些干燥器中的另一个。
在多流体热交换器135处冷却并且至少部分地冷凝干燥的、压缩的烟道气流133。
将液体或两相烟道气流137进料到精馏(还被称为脱NOx)塔139中作为回流并且分离成富NO2液体流141和富CO2气态流143。该脱NOx塔中的压力典型地是约25巴绝对值,其中该入口气体温度是约-19℃。
将富NO2液体流141进料到渗透蒸发分离膜147的进料气体侧。膜147 包括由以下材料构成的分离层,该材料越过CO2选择性地渗透NO2(和SO2,若存在的话)以便提供富NO2渗透物和富CO2非渗透物。被进料到膜147的渗透侧(与该进料气体侧相反)的任选的吹扫气体145将增强来自流141的 NO2从该进料气体侧到该渗透侧横穿膜147的渗透(通过降低其在该渗透侧上的分压)。从膜147中抽取出组合的吹扫气体145和富NO2渗透物作为流 149。
用泵153加压从膜147中抽取出的富CO2非渗透物作为液体流151。将加压的液体流155与流192组合并且再循环回到精馏塔139中。
在热交换器135处冷却并且至少部分地冷凝气态流143(含有在约 1-5ppm之间的NO2和约98%的CO2)以提供冷却的两相流161。然后将两相流161进料到相分离器163中以提供富N2、O2、和Ar的气态流165和富CO2液体流167。
将流165在热交换器135处升温并且将升温的流169进一步在加热器或热交换器处升温171。两次升温的流171用于使以再生模式运行的干燥器 129、131再生,并且然后随后在热交换器177处升温以增强在膨胀器179处回收的可获得的膨胀能量。在膨胀器179的下游,该流在热交换器135处升温并且将升温的膨胀的流120排放。
将富CO2液体流167的压力在膨胀阀处降低并且作为回流进料到汽提塔186中。塔186在约15巴的压力和在-27℃与-50℃之间的温度下运行以从塔186的顶部去除处于贫CO2的气态流187的形式的不可冷凝的组分(N2、 O2、和Ar)。在热交换器135处回收流187的冷能的一些,由此提供了升温的流189,该升温的流与烟道气流118在压缩机124的吸入口处组合。
还将二氧化碳液体流191从塔186的底部去除并且分成流192、流194、和流196。将流192与液体非渗透流155组合以提供被进料到精馏塔139中的流157。在膨胀阀193处减少流194的压力以提供更冷的、两相(液体/气态 CO2)流195。在热交换器135处通过蒸发两相流195的剩余液相回收流195 中的潜热以提供气态流197。
在热交换器135处以两部分将流196中的CO2升温至不同的程度。使所得到的流198过热,而流200保持在其露点下并且被进料到汽提塔186中用于提供该塔必要的热量。
然后将流197和流198在压缩机199的吸入口处组合、在压缩机199处压缩并且在热交换器201处冷却至高于CO2的临界压力的水平。然后将该加热的、压缩的流的压力升高至高于CO2的临界压力以提供对于注入管道内有用的富超临界CO2产物流119。
本领域普通技术人员将认识到,富CO2产物119可代替地以用于存储、现场消耗、和/或通过长管拖车运输的液体形式提供。另外,液体CO2流191 不必被进料到膨胀阀193中或穿过热交换器135。的确,可以根据本领域中熟知的技术调节液体CO2流191的压力和/或温度以向液体富CO2产物119提供任何所希望的压力和温度。
膜147包括选择性渗透的分离层,该分离层主要负责分离NO2(连同 SO2,若存在的话)和CO2。膜147可以完全由该分离层的聚合物材料制成。膜147可代替地具有复合结构,其中该分离层由支撑层(其目的是提供机械强度)支撑。该支撑层的材料可以是流体膜分离的本领域技术人员已知的任何材料,如具有相对高的通量和足够令人希望的机械强度。膜147可以具有流体分离膜的本领域技术人员已知的任何构型,包括螺旋卷绕的片材和中空纤维。
膜147基于溶解度选择性原理工作。溶解度通常与分子参数如Lennard-Jones亲和常数或临界温度相关。因为NO2和SO2的临界温度大于 157℃并且CO2的临界温度仅仅是30.98℃,所以我们认为预期NO2和SO2展现出通过具有柔性主链并且具有极性亲和力的聚合物的高渗透性。
若干种聚合物材料适合用于膜147的分离层中,这些聚合物材料包括聚硅氧烷共聚醚(其是交联的)、聚氨酯-聚醚嵌段共聚物、聚(脲)-聚(醚) 嵌段共聚物、聚(酯)-聚(醚)嵌段共聚物、以及聚(酰胺)-聚(醚)嵌段共聚物。
在交联的聚硅氧烷共聚醚的情况下,它包含聚硅氧烷共聚醚,包含聚合链,该聚合链包含以下重复单元:具有式(1)的分子链段、被键合到该链的一端的硅原子上的末端分子链段-O-W(其中O是氧原子)、以及被键合到该链的另一端的氧原子上的末端分子链段-W:
每个W选自下组,该组由以下各项组成:-Si(CH3)3基团、具有式(2) 的分子链段、具有式(3)的分子链段、以及具有式(4)的分子链段;
每个X包括b个具有式(5)的分子链段的重复单元以及c个具有式(6) 的分子链段的重复单元:
每个R单独地选自下组,该组由以下各项组成:苯基、C1-C6烷基、具有式(2)的分子链段、具有式(3)的分子链段、以及具有式(4)的分子链段;
为了确保在该聚硅氧烷共聚醚中的聚醚含量的存在,施加以下两种条件。首先,如果每个W是-Si(CH3)3基团或具有式(3)的分子链段,那么至少一些R是具有式(2)的分子链段或具有式(4)的分子链段。其次,如果每个R是苯基或C1-C6烷基,那么每个W是具有式(2)的分子链段或具有式(4)的分子链段。
以下整数具有以下范围:
p:1-3;
q:1-3;
b:0-400;
c:0-200。
重复单元的数目(其中R是C1-C6烷基)是1-2000。
聚醚链段与聚硅氧烷链段的比率可以变化。当W是-Si(CH3)3基团时,交联位点存在于该链的中间,并且该链中的具有式(5)或(6)的分子链段的数目与硅原子的数目的比率范围是从约0.05至约6.0。当每个R是苯基或C1-C6烷基时,交联位点存在于该链的每个末端处,并且该链中的具有式 (5)或(6)的分子链段的数目与硅原子的数目的比率范围是从约0.05至约 0.33。在这种情况下,较大含量的硅氧烷基重复单元是所希望的用于提供更大的稳健性。
潜在的交联位点是W或者R为具有式(2)、(3)、或(4)的分子链段的任何地方。在该交联位点处形成的键的类型将取决于所讨论的W或R以及交联剂或交联促进剂的类型。对于具有式(2)的分子链段的W和R,可以使用单体二异氰酸酯、单体三异氰酸酯或聚合异氰酸酯交联剂形成尿烷键。对于具有式(3)的分子链段的W和R,可以使用单体二异氰酸酯、单体三异氰酸酯或聚合异氰酸酯交联剂形成脲键。对于具有式(3)的分子链段的W和R,可代替地使用二酰基氯取代的芳香族交联剂或三酰基氯取代的芳香族交联剂形成酰胺键。对于具有式(4)的分子链段的W和R,可以使用自由基交联促进剂(如偶氮或过氧化物自由基引发剂)交联该共聚物。
合适的单体二异氰酸酯、单体三异氰酸酯或聚合异氰酸酯交联剂的非限制实例是从多种多样的来源可商购的甲苯二异氰酸酯(TDI)或者从银彩公司(Siltech)可商购的氰酸酯官能化的硅氧烷。合适的二酰基氯取代的芳香族交联剂和三酰基氯取代的芳香族交联剂的非限制实例包括1,3-苯二羰基二氯化物、1,4-苯二羰基二氯化物、和1,3,5-苯三羰基三氯化物。
该交联的聚硅氧烷共聚醚可以任选地与一种或多种硅酮弹性体一起交联。该硅酮弹性体可以衍生自具有第一反应性官能团(如乙烯基硅氧烷单元)的第一硅酮聚合物和具有第二反应性官能团(如氢硅氧烷单元)的交联剂。合适的硅酮弹性体可以在商业上从迈图公司(Momentive)在商品名RTV615下并且从道康宁公司(Dow Corning)在商品名Sylgard184、 182、或186下获得。
特别合适类型的聚硅氧烷共聚醚可以在商业上从银彩公司在商品名 D-208、Di-2510、Di-5018F、Di1010、和J-1015-O下获得。
聚氨酯-聚醚嵌段共聚物是通过以下方式产生的:在催化剂如有机锡化合物(如二月桂酸二丁基锡)存在下,使至少一种聚醚二醇与芳香族的或脂肪族的二异氰酸酯反应、接着是与至少一种脂肪族二醇反应(以形成聚氨酯-聚醚)或者与至少一种脂肪族二胺反应(以形成聚脲-聚醚),但是可以使用本领域的技术人员已知的其他催化剂。这些所得到的聚合物含有包含聚醚的具有式(Is)的软链段以及包含聚氨酯或聚脲的具有式(Ih)的硬链段。
这些所得到的聚氨酯-聚醚或聚脲-聚醚嵌段共聚物是由具有式(Is) 和(Ih)的重复单元表示:
式(Is)和(Ih)的Ri是具有至少约2-18个碳原子的脂肪族或芳香族基团。(PE)是具有范围从约600至8000、并且优选约1000至4000的数均分子量Mn(其基本上等于重复的式(Is)的Mn)的聚醚链段。(Ih)的Ra是具有至少约2-18个碳原子的直链或支链的脂肪族基团;并且,X是氧原子或-NH-。如果X是氧,该嵌段共聚物是聚氨酯-聚醚,并且如果X是-NH-,该嵌段共聚物是聚脲-聚醚。在该嵌段共聚物内,在重复单元中的碳原子数目可以变化并且在其中可以存在碳原子数目的多样化和组合。重复的式(Ih)的数均分子量优选地在约200至3000、并且更优选地约200-1000的范围内。在一种共聚物中,特别地,Ri是直链-(CH2)6-或选自下组的组成的部分,该组主要包含以下的式(S)、式(T)、式(U)、或(V)、以及其组合或混合物。
这些结构分别对应于1,6-己烷二异氰酸酯、甲代亚苯基-2,6-二异氰酸酯、甲代亚苯基-2,4-二异氰酸酯、1,3-亚二甲苯基二异氰酸酯、和4,4′-亚甲基双(异氰酸苯酯)。该聚醚链段(PE)优选地衍生自约600-8000、并且更优选地约1000-4000的数均分子量,以及优选地约0.2-0.5的氧/碳比的聚醚二醇。优选的聚醚二醇是羟基封端的聚乙二醇、羟基封端的1,2-聚丙二醇、以及羟基封端的1,4-聚丁二醇,虽然可以使用由本领域的技术人员已知或使用的其他二醇。
该聚氨酯-聚醚或聚脲-聚醚嵌段共聚物的硬链段衍生自残余的脂肪族或芳香族二异氰酸酯端基或单体与至少一种脂族二醇或至少一种脂肪族二胺的反应。优选的二醇或二胺含有至少约2-18个碳原子并且可以是直链或支链的。最优选的是含有至少约2-6个碳原子的二醇或二胺。典型的二醇和二胺是乙二醇、1,3-丙二醇、1,2-丙二醇、1,4-丁二醇、1,6-己二醇、1,2- 二氨基乙烷、1,4-二氨基丁烷、1,5-二氨基戊烷、1,5-二氨基己烷、1,6-二氨基己烷、以及dl-丝氨酸(3-氨基-2-羟基丙酸),虽然可以使用由本领域的技术人员已知或使用的其他二醇和二胺。典型地,该聚氨酯-聚醚或聚脲- 聚醚嵌段共聚物展现了在从约23,000至400,000并且优选地约 50,000-280,000的范围内的数均分子量。如从这些组分的各种各样的组合示出的,在此考虑并且披露了宽范围以及各种各样类型的聚氨酯-聚醚和聚脲 -聚醚嵌段共聚物。典型地,该软链段包含该嵌段共聚物重量的约50-90重量百分比并且更典型地约60-85百分比。
这些聚酯-聚醚嵌段共聚物是通过以下方式产生的:在催化剂存在下使至少一种羟基封端的聚醚二醇、过量的至少一种脂肪族二醇、以及至少一种芳香族或脂肪族二酸的二羧酸酯反应。这些所得到的聚合物含有包含聚醚的具有式(IIs)的软链段以及包含聚酯的具有式(IIh)的硬链段。
(IIs)和(IIh)的Ra是具有约至少2-18个碳原子的脂肪族或芳香族基团。(Hs)的(PE)是具有范围从约600至8000、并且优选约1000至4000的数均分子量Mn(其基本上等于重复的式(Hs)的Mn)的聚醚链段。(IIh)的Rd是至少一种具有约至少2-18个碳原子的直链或支链的脂肪族基团。在该聚酯-聚醚嵌段共聚物内,在重复单元中的碳原子数目可以变化并且在其中可以存在碳原子数目的多样化和组合。重复的式(IIh)的平均分子量优选地是在约200至3000、并且更优选地约200-1000的范围内。在本发明的优选的实施例中,Ra是选自下组的组成的部分,该组由以下各项组成或包含以下各项:以下式(S)、(T)、(U)、(V)、(W)、(X)、或(Y)、或其组合或混合物:
进一步地,其中存在或包括式(Y),式(Y)中的-Z-是选自下组的部分,该组包含以下各项或由以下各项组成:以下式(A)、(B)、(C)、或(D)、或其混合物或组合:
该聚酯-聚醚嵌段共聚物的聚醚链段(PE)优选地衍生自约600-8000、并且更优选地约1000-4000的数均分子量,以及优选地约0.2-0.5的氧/碳比的聚醚二醇。优选的聚醚二醇是羟基封端的聚乙二醇、羟基封端的1,2-聚丙二醇、以及羟基封端的1,4-聚丁二醇,虽然可以使用由本领域的技术人员已知或使用的其他二醇。该嵌段共聚物的硬链段衍生自至少一种芳香族或脂肪族二酸的酯与至少一种脂肪族二醇的缩聚。具有式(I h)的部分R d 是该脂肪族二醇的衍生物。优选的二醇含有至少约2-18个碳原子并且可以是直链和/或支链的。最优选的是含有在约2-6个之间的碳原子的二醇。典型的二醇是乙二醇、1,3-丙二醇、1,2-丙二醇、1,4-丁二醇、以及1,6-己二醇,虽然可以使用由本领域的技术人员已知或使用的其他二醇。典型地,本发明的聚合物展现了在从约23,000至400,000并且优选地约50,000-280,000的范围内的数均分子量。如从这些组分的各种各样的组合示出的,在此考虑并且披露了各种各样类型的聚酯-聚醚嵌段共聚物。
典型地,该聚酯-聚醚嵌段共聚物的软链段包含该共聚物重量的约 50-90重量百分比并且更典型地约60-85百分比。
这些聚酰胺-聚醚嵌段共聚物包含具有式III的部分的重复单元:
其中PA是饱和的脂肪族聚酰胺链段并且PE是聚醚链段。典型地,该饱和的脂肪族聚酰胺链段是:
-尼龙6(PA6),其是聚[亚氨基(1-氧代六亚甲基)],或者
-尼龙12(PA12),其是聚[亚氨基(1-氧代十二亚甲基)]。
典型地,该聚醚链段是:
-PEO,其是聚(氧化乙烯),或者
-PTMEO,其是聚(四氢呋喃)。
聚酰胺-聚醚嵌段共聚物的一个特别合适的组是从阿科玛公司 (Arkema)在商品名PEBAX下可商购的。这些是通过羧酸聚酰胺(PA6、 PA11、PA12)与醇封端的聚醚(例如聚(丁二醇)(PTMG)或聚乙二醇(PEG)) 的缩聚获得的。
虽然已经结合其具体的实施例描述了本发明,明显的是鉴于前述说明许多替代方案、修改、和变体对于本领域技术人员将是清楚的。因此,它旨在包含如落入所附权利要求书中的精神和宽范围内的所有此类替代方案、修改、和变体。本发明可以适当地包含所披露的要素、由所披露的要素组成或基本上由所披露的要素组成,并且可以在不存在未披露的要素下实践。此外,如果存在提及顺序的语言,例如第一和第二,它应在示例性意义上并且不在限制性意义上进行理解。例如,本领域的技术人员可以认识到可以将某些步骤组合到单个步骤内。
单数形式“一个/种”(a/an)和“该(the)”包括复数指示物,除非上下文另外清楚地指出。
权利要求中的“包含(Comprising)”是开放式过渡术语,其是指随后确定的权利要求要素是无排他性的清单,即,其他任何事物可以附加地被包括并且保持在“包含”的范围内。“包含”在此被定义为必要地涵盖更受限制的过渡术语“主要由......组成”和“由......组成”;因此“包含”可以被“主要由......组成(consisting essentially of)”或“由......组成 (consisting of)”代替并且保持在“包含”的清楚地限定的范围内。
权利要求中的“提供(Providing)”被定义为是指供给、供应、使可获得、或制备某物。该步骤可以通过任何行动者在不存在相反的该权利要求中的表达语言下进行。
任选的或任选地是指随后描述的事件或情况可能发生或可能不发生。本说明包括其中该事件或情况发生的实例以及其中该事件或情况不发生的实例。
在此范围可以表述为从约一个具体值,和/或到约另一个具体值。当表述此种范围时,应理解的是另一个实施例是从该一个具体值和/或到该另一个具体值,连同在所述范围内的所有组合。
在此确定的所有参考文件各自特此通过引用以其全文结合到本申请中,并且是为了具体的信息,各个参考文献被引用就是为了该具体信息。
Claims (16)
1.一种用于从含有CO2和NO2的流体中分离NO2的方法,所述方法包括以下步骤:
将包含CO2,NO2,以及氧气、氩气、和氮气中的至少一种的该流体进料到精馏蒸馏塔中;
从该精馏塔中抽取出第一气态流,相对于包含CO2,NO2,以及氧气、氩气、和氮气中的至少一种的该流体,该第一气态流富含CO2并且缺乏NO2;
从该精馏塔中抽取出液体流,相对于包含CO2,NO2,以及氧气、氩气、和氮气中的至少一种的该流体,该液体流富含NO2;
将该富含NO2的液体流进料到流体分离膜中;
从该膜中抽取出包含渗透气体的第二气态流,相对于被进料到该膜中的该液体流,该第二气态流富含NO2并且缺乏CO2;
从该膜中抽取出非渗透液体流,相对于被进料到该膜中的该液体流,该非渗透液体流缺乏NO2并且富含CO2;并且
将该非渗透液体流再循环到该精馏塔中。
2.如权利要求1所述的方法,其中通过以下方式产生包含CO2,NO2,以及氧气、氩气、和氮气中的至少一种的该流体:在压缩机处压缩烟道气,接着是在热交换器处干燥并且至少部分冷凝该压缩的烟道气。
3.如权利要求2所述的方法,进一步包括以下步骤:
在热交换器处至少部分地冷凝该第一气态流;
在相分离器处分离该至少部分冷凝的流以产生相对于该第一气态流富含氧气、氩气和氮气中的至少一种的第三气态流以及相对于该第一气态流富含CO2的液体流;
将该富含CO2的液体流进料到汽提塔中;
将从该汽提塔中抽取出的第四气态流进料到该压缩机的吸入口;并且
从该汽提塔中抽取出液体产物CO2流。
4.如权利要求3所述的方法,进一步包括以下步骤:
使该液体产物CO2流膨胀以提供两相产物CO2流;
在热交换器处蒸发两相产物CO2流中的任何液体组分以提供完全气态的产物CO2流;并且
压缩并且加热该完全气态的产物CO2流以提供超临界产物CO2流。
5.如权利要求1所述的方法,进一步包括将吹扫气体进料到该流体分离膜中的步骤,其中该第二气态流进一步包含该吹扫气体。
6.如权利要求1所述的方法,进一步包括将该第二气态流进料到洗涤塔中以溶解存在于该第二气态流中的该NO2的至少一些并且形成硝酸的步骤。
7.如权利要求2所述的方法,进一步包括在锅炉中用氧化剂燃烧燃料以产生该烟道气的步骤,其中该烟道气具有大于300ppm的NOx含量。
8.如权利要求1所述的方法,其中该流体分离膜的分离层包括选自下组的材料,该组由以下各项组成:交联的聚硅氧烷共聚醚、聚氨酯-聚醚嵌段共聚物、聚脲-聚醚嵌段共聚物、聚酯-聚醚嵌段共聚物、以及聚酰胺-聚醚嵌段共聚物。
9.一种用于根据权利要求1所述的方法从含有CO2和NO2的流体中分离NO2的装置,该装置包括:
包含NO2和CO2的流体的源;
接收该源流体的精馏蒸馏塔;
流体分离膜,该流体分离膜接收来自该精馏塔的液体流并且产生液体非渗透流和气态渗透流;以及
泵,该泵将来自该膜的该非渗透液体进料到该精馏塔中。
10.如权利要求9所述的装置,进一步包括:
热交换器,该热交换器至少部分地冷凝来自该精馏塔的气态流;
相分离器,该相分离器接收来自该热交换器的该至少部分冷凝的流并且产生包含大部分N2、O2、和/或Ar的气态流以及包含大部分CO2的液体流;
汽提蒸馏塔,该汽提蒸馏塔接收来自该相分离器的该包含大部分CO2的液体流,该汽提塔被适配并且配置成将该包含大部分CO2的液体流的内容物分离成气态流和液体CO2产物流。
11.如权利要求10所述的装置,进一步包括被适配并且配置成压缩并且干燥该源流体的压缩机和干燥单元,其中该热交换器还被适配并且配置成至少部分地冷凝在被进料到该精馏塔中之前的该压缩的且干燥的源流体。
12.如权利要求11所述的装置,其中该流体源是被适配并且配置成产生烟道气的锅炉并且该烟道气是该包含NO2和CO2的流体。
13.如权利要求11所述的装置,其中该压缩机还接收来自该汽提塔的该气态流。
14.如权利要求9所述的装置,进一步包括吹扫气体的源,该膜还在该膜的渗透侧接收该吹扫气体。
15.如权利要求9所述的装置,进一步包括洗涤塔,该洗涤塔接收该气态渗透流并且溶解存在于气态渗透流中的该NO2的至少一些以形成硝酸。
16.如权利要求9所述的装置,其中该膜包括分离层,该分离层包括选自下组的材料,该组由以下各项组成:交联的聚硅氧烷共聚醚、聚氨酯-聚醚嵌段共聚物、聚脲-聚醚嵌段共聚物、聚酯-聚醚嵌段共聚物、以及聚酰胺-聚醚嵌段共聚物。
Applications Claiming Priority (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US201461971840P | 2014-03-28 | 2014-03-28 | |
US61/971,840 | 2014-03-28 | ||
US14/265,710 | 2014-04-30 | ||
US14/265,710 US9458022B2 (en) | 2014-03-28 | 2014-04-30 | Process and apparatus for separating NO2 from a CO2 and NO2—containing fluid |
PCT/US2015/022999 WO2015148927A1 (en) | 2014-03-28 | 2015-03-27 | Process and apparatus for separating no2 from a co2 and no2-containing fluid |
Publications (2)
Publication Number | Publication Date |
---|---|
CN106132495A CN106132495A (zh) | 2016-11-16 |
CN106132495B true CN106132495B (zh) | 2019-03-01 |
Family
ID=54189805
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
CN201580015837.6A Active CN106132495B (zh) | 2014-03-28 | 2015-03-27 | 用于从含有co2和no2的流体中分离no2的方法和装置 |
Country Status (5)
Country | Link |
---|---|
US (2) | US9458022B2 (zh) |
EP (1) | EP3145606B1 (zh) |
CN (1) | CN106132495B (zh) |
PL (1) | PL3145606T3 (zh) |
WO (1) | WO2015148927A1 (zh) |
Families Citing this family (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9458022B2 (en) * | 2014-03-28 | 2016-10-04 | L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude | Process and apparatus for separating NO2 from a CO2 and NO2—containing fluid |
FR3045403B1 (fr) * | 2015-12-18 | 2022-02-11 | Electricite De France | Systeme de regeneration membranaire d'un solvant de captage de gaz acide |
CN106839651A (zh) * | 2017-03-27 | 2017-06-13 | 四川华亿石油天然气工程有限公司 | 一种从真空烘箱尾气中回收氮气的系统及工艺 |
CN107029546A (zh) * | 2017-04-20 | 2017-08-11 | 北京国电龙源环保工程有限公司 | 基于碱性吸收剂细小颗粒的so3脱除系统及其脱除方法 |
FR3070016B1 (fr) * | 2017-08-10 | 2019-08-23 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede et installation de purification d'un flux gazeux d'alimentation comprenant au moins 90% de co2 |
CN107485981B (zh) * | 2017-09-05 | 2020-05-12 | 北京科技大学 | 一种烟气脱硝装置和方法 |
CN107855210B (zh) * | 2017-12-08 | 2023-04-25 | 西安热工研究院有限公司 | 超临界机组中速磨煤机出口温度节能优化控制系统及方法 |
CN109289449B (zh) * | 2018-11-02 | 2021-06-11 | 辽宁新瑞碳材料科技有限公司 | 一种高温炉尾气的回收方法 |
CN109289342B (zh) * | 2018-11-02 | 2021-06-11 | 辽宁新瑞碳材料科技有限公司 | 一种分离回收高温炉尾气的系统和方法 |
CN109289486B (zh) * | 2018-11-02 | 2021-06-11 | 辽宁新瑞碳材料科技有限公司 | 一种高温尾气中氮气的分离回收方法 |
WO2020104004A1 (en) * | 2018-11-19 | 2020-05-28 | Nov Process & Flow Technologies As | Hydrate inhibitor recovery system |
US11149636B2 (en) * | 2019-03-01 | 2021-10-19 | Richard Alan Callahan | Turbine powered electricity generation |
US11149634B2 (en) * | 2019-03-01 | 2021-10-19 | Richard Alan Callahan | Turbine powered electricity generation |
US11071947B2 (en) | 2019-10-30 | 2021-07-27 | W. L. Gore & Associates, Inc. | Catalytic efficiency of flue gas filtration |
US10940471B1 (en) * | 2019-10-30 | 2021-03-09 | W. L. Gore & Associates, Inc. | Catalytic efficiency of flue gas filtration |
CN113477033B (zh) * | 2021-07-20 | 2023-03-14 | 金浦新材料股份有限公司 | 一种可自乳化有机硅脱碳溶剂 |
FR3135212B1 (fr) | 2022-05-09 | 2024-03-22 | Air Liquide | Procédé et appareil de purification d’un flux gazeux contenant au moins un oxyde d’azote |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5607557A (en) * | 1994-03-28 | 1997-03-04 | Institut Francais Du Petrole | Ethyl tertio-butyl ether purification process combining a membrane method and distillation |
CN1178211A (zh) * | 1996-05-08 | 1998-04-08 | 气体产品与化学公司 | 从烯烃-氢混合物中回收烯烃 |
Family Cites Families (50)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3303105A (en) * | 1963-03-25 | 1967-02-07 | Gen Electric | Diffusion of water vapor through slicone rubber |
US3739553A (en) * | 1971-06-14 | 1973-06-19 | H Aine | Exhaust emission control means for internal combustion apparatus |
US4001279A (en) * | 1973-03-29 | 1977-01-04 | The Regents Of The University Of California | Asymmetric macrocycles containing oxygen and binaphthyl ring members |
US4425313A (en) * | 1976-08-16 | 1984-01-10 | Cooper Hal B H | Removal and recovery of nitrogen and sulfur oxides from gaseous mixtures containing them |
US4073089A (en) * | 1976-09-27 | 1978-02-14 | Canadian Patents And Development Limited | Utilization of exhaust gases for plant growth |
US4272437A (en) * | 1978-12-18 | 1981-06-09 | Bristol-Myers Company | Antibacterial agents, and 4-thio azetidinone intermediates |
IN154274B (zh) * | 1980-09-02 | 1984-10-13 | Ube Industries | |
DE3037736C2 (de) * | 1980-10-06 | 1984-01-26 | Achim Dipl.-Ing. 6650 Homburg Ballweg | Verfahren zur Entwässerung von Gemischen aus organischen Flüssigkeiten und Wasser |
US4717406A (en) | 1986-07-07 | 1988-01-05 | Liquid Air Corporation | Cryogenic liquified gas purification method and apparatus |
US4963165A (en) | 1987-04-27 | 1990-10-16 | Membrane Technology & Research, Inc. | Composite membrane, method of preparation and use |
US4774365A (en) * | 1987-11-25 | 1988-09-27 | Air Products And Chemicals, Inc. | Pervaporation process for separating alcohols from ethers |
US5352272A (en) * | 1991-01-30 | 1994-10-04 | The Dow Chemical Company | Gas separations utilizing glassy polymer membranes at sub-ambient temperatures |
US5080698A (en) * | 1991-04-25 | 1992-01-14 | E. I. Du Pont De Nemours And Company | Aromatic polyethers containing cyano groups for gas separation |
FR2688224A1 (fr) * | 1992-02-24 | 1993-09-10 | Shell Int Research | Procede de traitement des gaz de petrole liquefies acides. |
JPH06287153A (ja) * | 1993-04-02 | 1994-10-11 | Mitsubishi Petrochem Co Ltd | 無水エタノールの製造方法 |
FR2711986B1 (fr) * | 1993-11-05 | 1996-02-02 | Inst Francais Du Petrole | Procédé de séparation des composés oxygénés d'hydrocarbures, combinant une distillation et une perméation et son utilisation en éthérification. |
US5585527A (en) * | 1994-10-31 | 1996-12-17 | Uop | Continuous distillation and membrane process |
US6257018B1 (en) * | 1999-06-28 | 2001-07-10 | Praxair Technology, Inc. | PFC recovery using condensation |
US6843829B2 (en) | 2002-03-27 | 2005-01-18 | L'air Liquide-Societe Anonyme A'directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedures Georges Claude | Block polyurethane-ether and polyurea-ether gas separation membranes |
US6860920B2 (en) | 2002-03-28 | 2005-03-01 | L'air Liquide-Societe Anoyme A Directoire Et Conseil De Surveillance Pour L'etude Et L'exploitation Des Procedes George Claude | Block polyester-ether gas separation membranes |
US6899743B2 (en) * | 2002-06-12 | 2005-05-31 | Membrane Technology And Research, Inc. | Separation of organic mixtures using gas separation or pervaporation and dephlegmation |
US7124605B2 (en) * | 2003-10-30 | 2006-10-24 | National Tank Company | Membrane/distillation method and system for extracting CO2 from hydrocarbon gas |
FR2886646B1 (fr) * | 2005-06-03 | 2010-12-24 | Inst Francais Du Petrole | Procede et installation de separation de composes, dont au moins une n-paraffine, dans une charge d'hydrocarbures |
US7850763B2 (en) * | 2007-01-23 | 2010-12-14 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
US8088196B2 (en) * | 2007-01-23 | 2012-01-03 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
US8080090B2 (en) | 2007-02-16 | 2011-12-20 | Air Liquide Process & Construction, Inc. | Process for feed gas cooling in reboiler during CO2 separation |
US7842264B2 (en) * | 2007-04-12 | 2010-11-30 | Cefco, Llc | Process and apparatus for carbon capture and elimination of multi-pollutants in flue gas from hydrocarbon fuel sources and recovery of multiple by-products |
US7708804B2 (en) | 2007-07-11 | 2010-05-04 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Process and apparatus for the separation of a gaseous mixture |
US20090057128A1 (en) * | 2007-08-30 | 2009-03-05 | Leland Vane | Liquid separation by membrane assisted vapor stripping process |
JP2011516258A (ja) * | 2008-04-08 | 2011-05-26 | フジフィルム・マニュファクチュアリング・ヨーロッパ・ベスローテン・フエンノートシャップ | 複合膜 |
KR20110016434A (ko) * | 2008-04-08 | 2011-02-17 | 후지필름 매뉴팩츄어링 유럽 비.브이. | 막의 제조 공정 |
DE102008029514A1 (de) * | 2008-06-21 | 2009-12-24 | Bayer Materialscience Ag | Verfahren zur Herstellung von Diarylcarbonaten aus Dialkylcarbonaten |
US8771477B2 (en) * | 2008-09-17 | 2014-07-08 | Sylvan Source, Inc. | Large-scale water purification and desalination |
DE102009035389A1 (de) | 2009-07-30 | 2011-02-03 | Siemens Aktiengesellschaft | Verfahren zur Schadstoffentfernung aus Kohlendioxid und Vorrichtung zur dessen Durchführung |
FR2949553B1 (fr) * | 2009-09-02 | 2013-01-11 | Air Liquide | Procede de production d'au moins un gaz pauvre en co2 et d'un ou plusieurs fluides riches en co2 |
DE102009047351A1 (de) * | 2009-12-01 | 2011-06-09 | Evonik Goldschmidt Gmbh | Komposit-Siliconmembranen mit hoher Trennwirkung |
US8617292B2 (en) * | 2009-12-15 | 2013-12-31 | L'Air Liquide, Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude | Method of obtaining carbon dioxide from carbon dioxide-containing gas mixture |
FR2961270B1 (fr) * | 2010-06-11 | 2017-07-28 | Air Liquide | Procede et appareil de sechage et de compression d'un flux riche en co2 |
US8012446B1 (en) * | 2010-07-08 | 2011-09-06 | Air Products And Chemicals, Inc. | Recycle TSA regen gas to boiler for oxyfuel operations |
US9216390B2 (en) * | 2010-07-15 | 2015-12-22 | Ohio State Innovation Foundation | Systems, compositions, and methods for fluid purification |
DE102011014007A1 (de) * | 2011-03-15 | 2012-09-20 | Linde Aktiengesellschaft | Verfahren und Anlage zur Rauchgasentstickung |
EP2753414A1 (en) * | 2011-09-07 | 2014-07-16 | Carbon Engineering Limited Partnership | Target gas capture |
GB201211309D0 (en) * | 2012-06-26 | 2012-08-08 | Fujifilm Mfg Europe Bv | Process for preparing membranes |
CA2884012C (en) * | 2012-09-20 | 2020-09-01 | Dow Global Technologies Llc | Radiation cured membranes derived from polymers that are co-reactive with azide crosslinking agent(s) |
EP2745918A1 (en) * | 2012-12-18 | 2014-06-25 | Max-Planck-Gesellschaft zur Förderung der Wissenschaften e.V. | Method and device for transferring gas molecules from a gaseous medium into a liquid medium or vice versa |
US20160045841A1 (en) * | 2013-03-15 | 2016-02-18 | Transtar Group, Ltd. | New and improved system for processing various chemicals and materials |
US10254042B2 (en) * | 2013-10-25 | 2019-04-09 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
US9375685B2 (en) * | 2014-03-28 | 2016-06-28 | L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude | Membrane for the separation of a mixture of a polar fluid and a non-polar fluid and methods for use thereof |
US9458022B2 (en) * | 2014-03-28 | 2016-10-04 | L'Air Liquide Société Anonyme Pour L'Étude Et L'Exploitation Des Procedes Georges Claude | Process and apparatus for separating NO2 from a CO2 and NO2—containing fluid |
US9266748B1 (en) * | 2015-05-21 | 2016-02-23 | Gradiant Corporation | Transiently-operated desalination systems with heat recovery and associated methods |
-
2014
- 2014-04-30 US US14/265,710 patent/US9458022B2/en active Active
-
2015
- 2015-03-27 EP EP15716304.9A patent/EP3145606B1/en active Active
- 2015-03-27 WO PCT/US2015/022999 patent/WO2015148927A1/en active Application Filing
- 2015-03-27 CN CN201580015837.6A patent/CN106132495B/zh active Active
- 2015-03-27 PL PL15716304T patent/PL3145606T3/pl unknown
-
2016
- 2016-06-30 US US15/198,677 patent/US9816755B2/en active Active
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5607557A (en) * | 1994-03-28 | 1997-03-04 | Institut Francais Du Petrole | Ethyl tertio-butyl ether purification process combining a membrane method and distillation |
CN1178211A (zh) * | 1996-05-08 | 1998-04-08 | 气体产品与化学公司 | 从烯烃-氢混合物中回收烯烃 |
Also Published As
Publication number | Publication date |
---|---|
EP3145606A1 (en) | 2017-03-29 |
US20160313058A1 (en) | 2016-10-27 |
EP3145606B1 (en) | 2018-08-01 |
CN106132495A (zh) | 2016-11-16 |
PL3145606T3 (pl) | 2018-12-31 |
US9458022B2 (en) | 2016-10-04 |
US9816755B2 (en) | 2017-11-14 |
US20150276309A1 (en) | 2015-10-01 |
WO2015148927A1 (en) | 2015-10-01 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
CN106132495B (zh) | 用于从含有co2和no2的流体中分离no2的方法和装置 | |
RU2489197C2 (ru) | Способ разделения газов с применением мембран с продувкой пермеата для удаления co2 из продуктов сжигания | |
EP2616162B1 (en) | Process for separating carbon dioxide from flue gas using sweep-based membrane separation and absorption steps | |
US20200179868A1 (en) | Production of biomethane using multiple types of membrane | |
Lokhandwala et al. | Membrane separation of nitrogen from natural gas: A case study from membrane synthesis to commercial deployment | |
EP2616163B1 (en) | Gas separation process using membranes with permeate sweep to remove co2 from gaseous fuel combustion exhaust | |
US8025715B2 (en) | Process for separating carbon dioxide from flue gas using parallel carbon dioxide capture and sweep-based membrane separation steps | |
US10479684B2 (en) | Enhancement of claus tail gas treatment by sulfur dioxide-selective membrane technology and sulfur dioxide-selective absorption technology | |
CN110022963B (zh) | 气体分离-轮机中整合的co2 捕获方法 | |
US20180133643A1 (en) | Methods for the separation of co2 from a gas stream | |
CN109310945B (zh) | 用于从由多个燃烧源产生的排放气体中除去二氧化碳的基于吹扫的膜分离方法 | |
US9140186B2 (en) | Sweep-based membrane gas separation integrated with gas-fired power production and CO2 recovery | |
WO2010126985A1 (en) | Membrane-based process for co2 capture from flue gases generated by oxy-combustion of coal | |
Baker et al. | Gas separation process using membranes with permeate sweep to remove CO2 from combustion gases | |
RU2619313C2 (ru) | Способ разделения газов с использованием мембран на основе продувки, объединённый с выработкой энергии на газовых электростанциях и извлечением co2 | |
Ho et al. | Methods for the separation of CO 2 from a gas stream | |
Wijmans et al. | Gas separation process using membranes with permeate sweep to remove CO2 from gaseous fuel combustion exhaust | |
WO2021231591A1 (en) | A membrane co2 separation process |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
C06 | Publication | ||
PB01 | Publication | ||
SE01 | Entry into force of request for substantive examination | ||
SE01 | Entry into force of request for substantive examination | ||
GR01 | Patent grant | ||
GR01 | Patent grant |