CN107915567A - The method that polar compound is removed from the aromatic raw material containing polar compound - Google Patents
The method that polar compound is removed from the aromatic raw material containing polar compound Download PDFInfo
- Publication number
- CN107915567A CN107915567A CN201610878287.7A CN201610878287A CN107915567A CN 107915567 A CN107915567 A CN 107915567A CN 201610878287 A CN201610878287 A CN 201610878287A CN 107915567 A CN107915567 A CN 107915567A
- Authority
- CN
- China
- Prior art keywords
- polar compound
- raw material
- material containing
- aromatic raw
- logistics
- 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.)
- Pending
Links
- 239000002994 raw material Substances 0.000 title claims abstract description 77
- 150000001875 compounds Chemical class 0.000 title claims abstract description 65
- 125000003118 aryl group Chemical group 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 44
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 50
- 239000003463 adsorbent Substances 0.000 claims abstract description 33
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 25
- 238000001179 sorption measurement Methods 0.000 claims abstract description 19
- 239000010457 zeolite Substances 0.000 claims description 29
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 15
- 239000005864 Sulphur Substances 0.000 claims description 13
- 229910017464 nitrogen compound Inorganic materials 0.000 claims description 6
- 150000002830 nitrogen compounds Chemical class 0.000 claims description 6
- -1 sulphur compound Chemical class 0.000 claims description 6
- NLYAJNPCOHFWQQ-UHFFFAOYSA-N kaolin Chemical group O.O.O=[Al]O[Si](=O)O[Si](=O)O[Al]=O NLYAJNPCOHFWQQ-UHFFFAOYSA-N 0.000 claims description 4
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 238000010992 reflux Methods 0.000 claims description 2
- 239000012535 impurity Substances 0.000 abstract description 14
- 238000005804 alkylation reaction Methods 0.000 abstract description 9
- 239000007791 liquid phase Substances 0.000 abstract description 5
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 3
- 229930195733 hydrocarbon Natural products 0.000 abstract description 3
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 3
- 238000009776 industrial production Methods 0.000 abstract 1
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 204
- 238000006243 chemical reaction Methods 0.000 description 64
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 24
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 24
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 24
- 239000003054 catalyst Substances 0.000 description 16
- 229910052717 sulfur Inorganic materials 0.000 description 14
- 239000011593 sulfur Substances 0.000 description 14
- 239000005977 Ethylene Substances 0.000 description 12
- 238000000746 purification Methods 0.000 description 11
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 6
- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 5
- 125000000217 alkyl group Chemical group 0.000 description 5
- 150000001491 aromatic compounds Chemical class 0.000 description 5
- 239000008280 blood Substances 0.000 description 5
- 210000004369 blood Anatomy 0.000 description 5
- 239000004202 carbamide Substances 0.000 description 5
- 238000011049 filling Methods 0.000 description 5
- 239000002808 molecular sieve Substances 0.000 description 5
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 5
- KVNYFPKFSJIPBJ-UHFFFAOYSA-N 1,2-diethylbenzene Chemical group CCC1=CC=CC=C1CC KVNYFPKFSJIPBJ-UHFFFAOYSA-N 0.000 description 4
- PPBRXRYQALVLMV-UHFFFAOYSA-N Styrene Chemical compound C=CC1=CC=CC=C1 PPBRXRYQALVLMV-UHFFFAOYSA-N 0.000 description 4
- 229910021536 Zeolite Inorganic materials 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 description 4
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 4
- 238000009835 boiling Methods 0.000 description 4
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 4
- 239000000523 sample Substances 0.000 description 4
- ZWEHNKRNPOVVGH-UHFFFAOYSA-N 2-Butanone Chemical compound CCC(C)=O ZWEHNKRNPOVVGH-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- PFRUBEOIWWEFOL-UHFFFAOYSA-N [N].[S] Chemical compound [N].[S] PFRUBEOIWWEFOL-UHFFFAOYSA-N 0.000 description 3
- 238000004458 analytical method Methods 0.000 description 3
- OCKPCBLVNKHBMX-UHFFFAOYSA-N butylbenzene Chemical compound CCCCC1=CC=CC=C1 OCKPCBLVNKHBMX-UHFFFAOYSA-N 0.000 description 3
- 125000004432 carbon atom Chemical group C* 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000004575 stone Substances 0.000 description 3
- 238000006467 substitution reaction Methods 0.000 description 3
- GWHJZXXIDMPWGX-UHFFFAOYSA-N 1,2,4-trimethylbenzene Chemical compound CC1=CC=C(C)C(C)=C1 GWHJZXXIDMPWGX-UHFFFAOYSA-N 0.000 description 2
- QNLZIZAQLLYXTC-UHFFFAOYSA-N 1,2-dimethylnaphthalene Chemical compound C1=CC=CC2=C(C)C(C)=CC=C21 QNLZIZAQLLYXTC-UHFFFAOYSA-N 0.000 description 2
- QPUYECUOLPXSFR-UHFFFAOYSA-N 1-methylnaphthalene Chemical compound C1=CC=C2C(C)=CC=CC2=C1 QPUYECUOLPXSFR-UHFFFAOYSA-N 0.000 description 2
- GYMFBYTZOGMSQJ-UHFFFAOYSA-N 2-methylanthracene Chemical compound C1=CC=CC2=CC3=CC(C)=CC=C3C=C21 GYMFBYTZOGMSQJ-UHFFFAOYSA-N 0.000 description 2
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 2
- PWATWSYOIIXYMA-UHFFFAOYSA-N Pentylbenzene Chemical compound CCCCCC1=CC=CC=C1 PWATWSYOIIXYMA-UHFFFAOYSA-N 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- JUJWROOIHBZHMG-UHFFFAOYSA-N Pyridine Chemical compound C1=CC=NC=C1 JUJWROOIHBZHMG-UHFFFAOYSA-N 0.000 description 2
- SMWDFEZZVXVKRB-UHFFFAOYSA-N Quinoline Chemical compound N1=CC=CC2=CC=CC=C21 SMWDFEZZVXVKRB-UHFFFAOYSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 2
- 150000004996 alkyl benzenes Chemical class 0.000 description 2
- 230000029936 alkylation Effects 0.000 description 2
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium chloride Substances Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- VPUGDVKSAQVFFS-UHFFFAOYSA-N coronene Chemical compound C1=C(C2=C34)C=CC3=CC=C(C=C3)C4=C4C3=CC=C(C=C3)C4=C2C3=C1 VPUGDVKSAQVFFS-UHFFFAOYSA-N 0.000 description 2
- UZILCZKGXMQEQR-UHFFFAOYSA-N decyl-Benzene Chemical compound CCCCCCCCCCC1=CC=CC=C1 UZILCZKGXMQEQR-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 2
- JIRNEODMTPGRGV-UHFFFAOYSA-N pentadecylbenzene Chemical compound CCCCCCCCCCCCCCCC1=CC=CC=C1 JIRNEODMTPGRGV-UHFFFAOYSA-N 0.000 description 2
- YNPNZTXNASCQKK-UHFFFAOYSA-N phenanthrene Chemical compound C1=CC=C2C3=CC=CC=C3C=CC2=C1 YNPNZTXNASCQKK-UHFFFAOYSA-N 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 230000000607 poisoning effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- JREJWHNDQOGSQT-UHFFFAOYSA-N 1,2,3,4,5-pentaethylbenzene Chemical compound CCC1=CC(CC)=C(CC)C(CC)=C1CC JREJWHNDQOGSQT-UHFFFAOYSA-N 0.000 description 1
- FEWANSQOXSIFOK-UHFFFAOYSA-N 1,2,3,4-tetraethylbenzene Chemical class CCC1=CC=C(CC)C(CC)=C1CC FEWANSQOXSIFOK-UHFFFAOYSA-N 0.000 description 1
- 150000005200 1,2,3-trimethylbenzenes Chemical class 0.000 description 1
- WNLWIOJSURYFIB-UHFFFAOYSA-N 1,2,4-triethylbenzene Chemical class CCC1=CC=C(CC)C(CC)=C1 WNLWIOJSURYFIB-UHFFFAOYSA-N 0.000 description 1
- IVSZLXZYQVIEFR-UHFFFAOYSA-N 1,3-Dimethylbenzene Natural products CC1=CC=CC(C)=C1 IVSZLXZYQVIEFR-UHFFFAOYSA-N 0.000 description 1
- HILAULICMJUOLK-UHFFFAOYSA-N 1,3-diethyl-5-methylbenzene Chemical class CCC1=CC(C)=CC(CC)=C1 HILAULICMJUOLK-UHFFFAOYSA-N 0.000 description 1
- HYFLWBNQFMXCPA-UHFFFAOYSA-N 1-ethyl-2-methylbenzene Chemical compound CCC1=CC=CC=C1C HYFLWBNQFMXCPA-UHFFFAOYSA-N 0.000 description 1
- ZMXIYERNXPIYFR-UHFFFAOYSA-N 1-ethylnaphthalene Chemical compound C1=CC=C2C(CC)=CC=CC2=C1 ZMXIYERNXPIYFR-UHFFFAOYSA-N 0.000 description 1
- KZNJSFHJUQDYHE-UHFFFAOYSA-N 1-methylanthracene Chemical group C1=CC=C2C=C3C(C)=CC=CC3=CC2=C1 KZNJSFHJUQDYHE-UHFFFAOYSA-N 0.000 description 1
- OGVRJXPGSVLDRD-UHFFFAOYSA-N 2,3-dimethylanthracene Chemical class C1=CC=C2C=C(C=C(C(C)=C3)C)C3=CC2=C1 OGVRJXPGSVLDRD-UHFFFAOYSA-N 0.000 description 1
- XNXIYYFOYIUJIW-UHFFFAOYSA-N 3-methylbutylbenzene Chemical compound CC(C)CCC1=CC=CC=C1 XNXIYYFOYIUJIW-UHFFFAOYSA-N 0.000 description 1
- GKYWZUBZZBHZKU-UHFFFAOYSA-N 3-methylphenanthrene Chemical group C1=CC=C2C3=CC(C)=CC=C3C=CC2=C1 GKYWZUBZZBHZKU-UHFFFAOYSA-N 0.000 description 1
- JUEORGSHIXFSSI-UHFFFAOYSA-N 9,10-dimethylphenanthrene Chemical group C1=CC=C2C(C)=C(C)C3=CC=CC=C3C2=C1 JUEORGSHIXFSSI-UHFFFAOYSA-N 0.000 description 1
- 239000005995 Aluminium silicate Substances 0.000 description 1
- SNRUBQQJIBEYMU-UHFFFAOYSA-N Dodecane Natural products CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 description 1
- 239000004793 Polystyrene Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000004913 activation Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 125000003545 alkoxy group Chemical group 0.000 description 1
- 125000002877 alkyl aryl group Chemical group 0.000 description 1
- 235000012211 aluminium silicate Nutrition 0.000 description 1
- 125000004104 aryloxy group Chemical group 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 239000000440 bentonite Substances 0.000 description 1
- 229910000278 bentonite Inorganic materials 0.000 description 1
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 1
- RJTJVVYSTUQWNI-UHFFFAOYSA-N beta-ethyl naphthalene Natural products C1=CC=CC2=CC(CC)=CC=C21 RJTJVVYSTUQWNI-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000000753 cycloalkyl group Chemical group 0.000 description 1
- 239000003599 detergent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 125000003438 dodecyl group Chemical group [H]C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])C([H])([H])* 0.000 description 1
- SQNZJJAZBFDUTD-UHFFFAOYSA-N durene Chemical compound CC1=CC(C)=C(C)C=C1C SQNZJJAZBFDUTD-UHFFFAOYSA-N 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 125000001495 ethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000007792 gaseous phase Substances 0.000 description 1
- 125000001475 halogen functional group Chemical group 0.000 description 1
- DEQLTFPCJRGSHW-UHFFFAOYSA-N hexadecylbenzene Chemical compound CCCCCCCCCCCCCCCCC1=CC=CC=C1 DEQLTFPCJRGSHW-UHFFFAOYSA-N 0.000 description 1
- 125000004435 hydrogen atom Chemical group [H]* 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 150000002732 mesitylenes Chemical class 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000007935 neutral effect Effects 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- LIXVMPBOGDCSRM-UHFFFAOYSA-N nonylbenzene Chemical compound CCCCCCCCCC1=CC=CC=C1 LIXVMPBOGDCSRM-UHFFFAOYSA-N 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- HFPZCAJZSCWRBC-UHFFFAOYSA-N p-cymene Chemical compound CC(C)C1=CC=C(C)C=C1 HFPZCAJZSCWRBC-UHFFFAOYSA-N 0.000 description 1
- BEZDDPMMPIDMGJ-UHFFFAOYSA-N pentamethylbenzene Chemical compound CC1=CC(C)=C(C)C(C)=C1C BEZDDPMMPIDMGJ-UHFFFAOYSA-N 0.000 description 1
- 125000002080 perylenyl group Chemical group C1(=CC=C2C=CC=C3C4=CC=CC5=CC=CC(C1=C23)=C45)* 0.000 description 1
- CSHWQDPOILHKBI-UHFFFAOYSA-N peryrene Natural products C1=CC(C2=CC=CC=3C2=C2C=CC=3)=C3C2=CC=CC3=C1 CSHWQDPOILHKBI-UHFFFAOYSA-N 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 229920002223 polystyrene Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000002203 pretreatment Methods 0.000 description 1
- UMJSCPRVCHMLSP-UHFFFAOYSA-N pyridine Natural products COC1=CC=CN=C1 UMJSCPRVCHMLSP-UHFFFAOYSA-N 0.000 description 1
- ZJMWRROPUADPEA-UHFFFAOYSA-N sec-butylbenzene Chemical compound CCC(C)C1=CC=CC=C1 ZJMWRROPUADPEA-UHFFFAOYSA-N 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000011973 solid acid Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 125000001424 substituent group Chemical group 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 239000000271 synthetic detergent Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 238000004073 vulcanization Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/005—Processes comprising at least two steps in series
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/12—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
- C07C7/13—Purification; Separation; Use of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers by molecular-sieve technique
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/70—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of types characterised by their specific structure not provided for in groups C07C2529/08 - C07C2529/65
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The present invention relates to a kind of method that polar compound is removed from the aromatic raw material containing polar compound, the prior art is mainly solved there are adsorbent adsorption efficiency is low, makes the problem of still ability is limited in terms of the basic nitrogen impurities in aromatic raw material are reduced to for the low content required by liquid-phase alkylation process.The present invention enters rectifying column by using a) aromatic raw material containing polar compound, and tower reactor obtains the first logistics, and tower top obtains the second logistics；B) first logistics enters adsorption zone, and after being contacted with adsorbent, the technical solution for obtaining being substantially free of the aromatic raw material of polar compound preferably solves the problems, such as this, available in the deimpurity industrial production of aroamtic hydrocarbon raw material.
Description
Technical field
The present invention relates to a kind of method that polar compound is removed from the aromatic raw material containing polar compound.
Background technology
Alkylbenzene is a kind of important Organic Chemicals, and industrially tool has been widely used, such as：Ethylbenzene is mainly used for
The production of styrene, and styrene then carrys out the manufacture of high molecular material for polystyrene on a large scale；Isopropylbenzene is mainly used for benzene
The production of phenol and acetone；Sec-butylbenzene is used for the production of phenol and methyl ethyl ketone.Long-chain olefin and the long alkane of benzene alkylation synthesis
Base benzene is widely used in the manufacture of synthetic detergent.The production of early stage alkylbenzene mainly uses AlCl3It is catalyst with HF, due to
AlCl3With HF there is serious pollution, burn into and safety problem, and gradually substituted by solid acid zeolite catalyst, so
It is expensive and acid zeolite acid content is low, therefore be easily poisoned by raw material neutral and alkali compound, make catalyst inactivation and make
Into massive losses.
Using guard bed come to remove the method for trace impurity in aromatic raw material be known in the art.To petrochemical industry and
The special chemical operational process of craft that product purity strictly limits is even more important.Under normal circumstances, similar bentonite, white is used
Soil, kaolin or the alumina material of special activation, are placed on the upstream of the reaction vessel containing catalyst, by raw material
Impurity captures, to meet product purity specification requirement and reduce catalyst poisoning phenomenon.However, will environmental protection, economy, efficient solution
Certainly this problem is not easy.Such as, it has been found that in existing ethylbenzene, isopropylbenzene, the acid even generally used in aromatic hydrocarbons technology
Property carclazyte purification benzene technique, be not only difficult to thoroughly removing and be present in basic nitrogen compound in benzene, and adsorbent absorption effect
Rate is low, causes a large amount of carclazyte solid waste to discharge and cause new problem of environmental pollution.
Document US5744686 and US5942650 are disclosed by the way that hydrocarbon feed and one kind are included silica alumina ratio more than 100
And the selective absorbent of non-acidic molecular sieve of the average grain diameter less than 5.5 angstroms is contacted and nitridation is removed from aroamtic hydrocarbon raw material
The method of compound.Wherein, selective absorbent is selected from closed pore molecular sieve 4A, molecular sieve 4A, silicalite, F- silicalite, ZSM-5
Molecular sieve and their mixture.Document ZL01105848.x discloses the side that impurity in benzene feedstock is removed using h-type zeolite
Method.Document ZL01105849.8 discloses a kind of acid zeolite using carried metal and removes sulphur nitrogen impurity in benzene raw materials as inorganic agent
Method.Document WO2002014240A1 discloses a kind of method that polar impurity is removed from aromatic raw material, and adsorbent includes
The cross sectional dimensions of a kind of hole and/or surface crater is more than 5.6 angstroms of molecular sieve, and the temperature of adsorption zone is less than or equal to 130 DEG C.
But the prior art is reduced to for required by liquid-phase alkylation process in the basic nitrogen impurities in making aromatic raw material
Low content in terms of still ability it is limited.
The content of the invention
The technical problems to be solved by the invention are the prior arts there are adsorbent adsorption efficiency is low, are made in aromatic raw material
The problem of still ability is limited in terms of basic nitrogen impurities are reduced to for the low content required by liquid-phase alkylation process, there is provided one
The new method that polar compound is removed from the aromatic raw material containing polar compound of kind.This method can greatly improve adsorbent
Adsorption capacity, so as to meet the low impurity content required by liquid-phase alkylation process.
In order to solve the above technical problems, the technical solution adopted by the present invention is as follows：It is a kind of from the aromatics containing polar compound
The method that polar compound is removed in raw material, comprises the following steps：
A) aromatic raw material containing polar compound enters rectifying column, and tower reactor obtains the first logistics, and tower top obtains the second logistics；
B) first logistics enters adsorption zone, after being contacted with adsorbent, obtains being substantially free of the aromatics of polar compound
Raw material.
In above-mentioned technical proposal, the polar compound includes water, nitrogen compound or sulphur compound.
In above-mentioned technical proposal, the aromatic raw material containing polar compound contains the water of 1~1000ppm, preferably comprises
The water of 10~500ppm.
In above-mentioned technical proposal, the aromatic raw material containing polar compound contains the nitrification of 0.1~10ppm in terms of nitrogen
Thing.
In above-mentioned technical proposal, the vulcanization that the aromatic raw material containing polar compound contains 0.1~10ppm in terms of sulphur is closed
Thing.
In above-mentioned technical proposal, the temperature that the aromatic raw material containing polar compound enters rectifying column is 40~120 DEG C.
In above-mentioned technical proposal, the operating condition of the rectifying column includes：60~180 DEG C of tower top temperature, bottom temperature 70
~200 DEG C.Preferably include：70~160 DEG C of tower top temperature, 80~180 DEG C of bottom temperature.
In above-mentioned technical proposal, the operating condition of the adsorption zone includes：70~180 DEG C of temperature, pressure in terms of gauge pressure 0~
6.0MPa, when aromatic raw material feed weight air speed 0.1~100 is small-1.Preferably include：80~160 DEG C of temperature, pressure is in terms of gauge pressure
0.1~5.0MPa, when aromatic raw material feed weight air speed 0.2~50 is small-1。
In above-mentioned technical proposal, the adsorbent is Emathlite, Y zeolites, X zeolites, 13X zeolites, modenite, Beta
Zeolite, MWW structural zeolites.
In above-mentioned technical proposal, second logistics is divided into third―party logistics and the 4th logistics, and third―party logistics are back to rectifying
Tower, the 4th logistics are discharged out-of-bounds.
In above-mentioned technical proposal, the rectifying column tower top is configured with condenser and return tank, and second logistics is condensed
Return tank is introduced into after device condensation, is further divided into third―party logistics and the 4th logistics.
Brief description of the drawings
Fig. 1 is flow diagram of the present invention.
In Fig. 1,1 is aromatic raw material, and 2 be the aromatic raw material after preheating, and 3 be rectifying tower top gaseous phase logistics (the second thing
Stream), 4 be rectifying column top return logistics (third―party logistics), and 5 produce logistics (the 4th logistics) for rectifying column tower top, and 6 be rectifying column
Tower reactor material (the first logistics), 7 be that 8 be adsorption zone, and 9 be rectifying column top return tank by the purified aromatic raw material of adsorbent,
10 be rectifying column, and 11 be rectifying column tower top condenser, and 12 be feed preheater.
In Fig. 1, the aromatic raw material 1 containing polar compound enters rectifying column 10 after the preheating of preheater 12, through rectifying point
From rear, tower reactor obtains the first heavier logistics 6, and tower top obtains the second lighter logistics 3.Second logistics, 3 condensed device 11 cools down
After be collected in return tank of top of the tower 9, the logistics of a small amount of enrichment impurity is cleared out of from the bottom of return tank of top of the tower by logistics 5 is
System, remaining is back to rectifying column tower top.The liquid phase extraction logistics 6 of tower bottom of rectifying tower contacts simultaneously into adsorption zone 8 with adsorbent
Polar compound is removed, the basic aromatic raw material for removing polar compound is flowed out from the bottom of adsorption tower.
Embodiment
The present invention relates to the method that polar impurity is removed from aromatic raw material.It is more particularly related to aromatics
Raw material carries out pre-treatment step and carrys out the method that selectively removing makes the polar impurity of aromatic alkylation catalyst poisoning.This
Class impurity includes the compound of nitrogenous, sulphur and oxygen, particularly basic nitrogen compound, as pyridine, quinoline, N- formoxyls-morpholine and
N- methyl-pyrrolidons.This method can also effectively remove the water contained in aromatic raw material.
Term " aromatic compounds " used is the substitution including that can be partially alkylated or alkylated according to this professional consensus range in the present invention
Aromatic compounds or non-substituted single or multiple core compound.
Herein " the substitution aromatic compounds that can be partially alkylated or alkylated " must at least one hydrogen atom direct key connect aromatic core.Aromatic ring
Can there are one or more alkyl, aryl, alkaryl, alkoxy, aryloxy group, cycloalkyl, halo and/or other not influence alkyl
Change the group of reaction.
Herein " non-substituted single or multiple core compound " include benzene, naphthalene, anthracene, aphthacene, perylene, coronene and
Phenanthrene, is preferably benzene.
In general, can be as alkyl existing for substituent in aromatic compounds containing a carbon atom from 1 to 22 and usually from 1
To 8 carbon atoms and most it is often a carbon atom from 1 to 4.
Suitable alkyl substitution aromatic compounds include toluene, dimethylbenzene, isopropylbenzene, n-proplbenzene, alpha-methyl-naphthalene, ethylbenzene,
1,3,5- trimethylbenzenes, durol, cymol, butylbenzene, pseudocumene, adjacent diethylbenzene, a diethylbenzene, to two
Ethylo benzene, isoamyl benzene, isohesyl benzene, pentaethyl benzene, pentamethylbenzene, 1,2,3,4- tetraethylbenzenes, 1,2,3,5- durols,
1,2,4- triethylbenzenes, 1,2,3- trimethylbenzenes, a butyl toluene, to butyl toluene, 3,5- diethyltoluenes, adjacent ethyl first
Benzene, to ethyltoluene, a propyltoluene, 4- ethyls meta-xylene, dimethylnaphthalene, ethylnaphthalene, 2,3- dimethylanthracenes, 9- ethyls
Anthracene, 2- methyl anthracene, adjacent methyl anthracene, 9,10- dimethylphenanthrenes and 3- methylphenanthrenes.It is former that the aromatic hydrocarbons of higher molecular weight also is used as starting
Material, including produced aromatic hydrocarbons is such as alkylated to aromatic hydrocarbons by using olefin oligomer.This kind of product is usual in this area
Referred to as alkylates, including own benzene, nonylbenzene, detergent alkylate, pentadecyl benzene, nonyltoluene, nonyl toluene, dodecyl first
Benzene and pentadecyl toluene.Most common alkylates is obtained with higher boiling form-separating of satisfying, and wherein alkyl is connected to from C6
To C12Different size of aromatic core on.
Include benzene suitable for the typical feedstock of the method for the present invention.It is raw materials used such as aromatics as commercial scale alkylation process
The raw material generally nitrogen compound containing 0.1~10ppm in terms of nitrogen and more typical 0.2~5ppm, and 0.1~10ppm in terms of sulphur and
The sulphur compound of more typical 0.2~5ppm.In addition, raw material can contain the water of up to saturation conditions amount, generally 1~1000ppm and
More typically 10~500ppm.
Aromatic raw material is typically that benzene enters rectifying column, after rectifying separates, one after preheating in the method for the present invention
Divide lighter logistics containing benzene to be vaporized and distill and be enriched in tower top, a part of heavier logistics containing benzene is enriched in tower reactor.Tower top
It is collected in after the condensed device cooling of gas-phase benzene logistics in return tank of top of the tower, the logistics containing benzene of a small amount of enrichment impurity can be from tower top
System is cleared out of in the bottom of return tank, remaining is back to rectifying column tower top.The amount for being back to the logistics of rectifying column tower top meets
The requirement of rectifying column operating reflux ratio.Temperature after the preheated device preheating of aromatic raw material is 40~120 DEG C.The behaviour of rectifying column
Include as condition：60~180 DEG C of tower top temperature, 70~200 DEG C of bottom temperature.Preferably include：70~160 DEG C of tower top temperature, tower
80~180 DEG C of kettle temperature degree.
Tower bottom of rectifying tower effluent stream is directly entered adsorption zone.The adsorbent of adsorption zone is Emathlite, Y zeolites, X boiling
Stone, 13X zeolites, modenite, Beta zeolites, MWW structural zeolites.The operating condition of adsorption zone includes：70~180 DEG C of temperature,
Pressure 0~6.0MPa in terms of gauge pressure, when aromatic raw material feed weight air speed 0.1~100 is small-1.Preferably include：Temperature 80~160
DEG C, pressure 0.1~5.0MPa in terms of gauge pressure, when aromatic raw material feed weight air speed 0.2~50 is small-1。
Adsorption zone is usually fixed bed form, and wherein aromatic feed flow direction is upper or is downward through bed.
Compared with prior art, the method for the present invention aromatic raw material first carries out pre- essence before being contacted into adsorption zone with adsorbent
Evaporate, it is surprisingly found by the inventors that the adsorption capacity of adsorbent can be substantially improved in aromatic raw material after pre- rectification process.
Below by embodiment, the invention will be further elaborated.
【Embodiment 1】
By the technological process of Fig. 1, water content 200ppm, total nitrogen content 3.0ppm, total sulfur content 0.7ppm in benzene feedstock, essence
Evaporate tower operating pressure 0.01Pa, 80 DEG C of tower top temperature, 82 DEG C of bottom temperature.Adsorbent bed filling 100g Emathlites, absorption
82 DEG C, pressure 0.5MPa of agent bed temperature, benzene weight space velocity 5.0h-1.Continuous operation 100hr, is analyzed using sulphur blood urea/nitrogen analyzer and inhaled
The total nitrogen content of attached dose of bed outlet is 0.05ppm, total sulfur content 0.06ppm.
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and propylene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity Beta zeolites, 160 DEG C, reaction pressure 3.0MPa of reaction temperature, propylene weight air speed 10.0h-1, the molar ratio 4.0 of benzene and propylene, when successive reaction 200 is small, propylene conversion reaches 99%.
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and ethene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity Beta zeolites, 205 DEG C, reaction pressure 4.5MPa of reaction temperature, weight ethylene air speed 3.0h-1,
The molar ratio 4.0 of benzene and ethene, when successive reaction 200 is small, conversion of ethylene reaches 99%.
【Embodiment 2】
By the technological process of Fig. 1, water content 500ppm, total nitrogen content 3.0ppm, total sulfur content 1.6ppm in benzene feedstock, essence
Evaporate tower operating pressure 0.6MPa, about 140 DEG C of tower top temperature, 160 DEG C of bottom temperature.Adsorbent bed filling 100g acidity Beta boilings
Stone, adsorbent bed 160 DEG C, pressure 2.0MPa of temperature, benzene weight space velocity 3.0h-1.Continuous operation 100hr, using sulphur nitrogen analysis
The total nitrogen content that instrument analyzes adsorbent bed outlet is 0.05ppm, total sulfur content 0.07ppm.
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and propylene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity Beta zeolites, 160 DEG C, reaction pressure 3.0MPa of reaction temperature, propylene weight air speed 10.0h-1, the molar ratio 4.0 of benzene and propylene, when successive reaction 200 is small, propylene conversion reaches 99%.
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and ethene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity Beta zeolites, 205 DEG C, reaction pressure 4.5MPa of reaction temperature, weight ethylene air speed 3.0h-1,
The molar ratio 4.0 of benzene and ethene, when successive reaction 200 is small, conversion of ethylene reaches 99%.
【Embodiment 3】
By the technological process of Fig. 1, water content 300ppm, total nitrogen content 10ppm, total sulfur content 1.6ppm in benzene feedstock, essence
Evaporate tower operating pressure 0.6MPa, about 140 DEG C of tower top temperature, 160 DEG C of bottom temperature.Adsorbent bed filling 100g acidity Beta boilings
Stone, adsorbent bed 160 DEG C, pressure 2.0MPa of temperature, benzene weight space velocity 3.0h-1.Continuous operation 100hr, using sulphur nitrogen analysis
The total nitrogen content that instrument analyzes adsorbent bed outlet is 0.06ppm, total sulfur content 0.07ppm.
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and propylene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity MCM-22 zeolites, 160 DEG C, reaction pressure 3.0MPa of reaction temperature, propylene weight air speed
10.0h-1, the molar ratio 4.0 of benzene and propylene, when successive reaction 200 is small, propylene conversion reaches 99%.
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and ethene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity MCM-22 zeolites, 205 DEG C, reaction pressure 4.5MPa of reaction temperature, weight ethylene air speed
3.0h-1, the molar ratio 4.0 of benzene and ethene, when successive reaction 200 is small, conversion of ethylene reaches 99%.
【Embodiment 4】
Press【Embodiment 1】Technological process and alkylation reaction method, simply raw material water content 100ppm in benzene feedstock, always
Nitrogen content 6ppm, total sulfur content 3.0ppm.Continuous operation 100hr, the total of adsorbent bed outlet is analyzed using sulphur blood urea/nitrogen analyzer
Nitrogen content is 0.04ppm, total sulfur content 0.07ppm.
99% is maintained at the probe reaction that is alkylated to of benzene and propylene, successive reaction 200hr, propylene conversion.
99% is maintained at the probe reaction that is alkylated to of benzene and ethene, successive reaction 200hr, conversion of ethylene.
【Embodiment 5】
Press【Embodiment 1】Technological process and alkylation reaction method, simply raw material water content 50ppm in benzene feedstock, always
Nitrogen content 2ppm, total sulfur content 6.5ppm.Continuous operation 100hr, the total of adsorbent bed outlet is analyzed using sulphur blood urea/nitrogen analyzer
Nitrogen content is 0.03ppm, total sulfur content 0.1ppm.
99% is maintained at the probe reaction that is alkylated to of benzene and propylene, successive reaction 200hr, propylene conversion.
99% is maintained at the probe reaction that is alkylated to of benzene and ethene, successive reaction 200hr, conversion of ethylene.
【Comparative example 1】
According to【Embodiment 1】Method, water content 200ppm, total nitrogen content 3.0ppm, total sulfur content 0.7ppm in benzene feedstock,
Benzene feedstock is directly entered adsorbent bed, adsorbent bed filling 100g Emathlites without rectifying column, adsorbent bed
82 DEG C, pressure 0.5MPa of temperature, benzene weight space velocity 5.0h-1.Continuous operation 100hr, adsorbent bed is analyzed using sulphur blood urea/nitrogen analyzer
The total nitrogen content of layer outlet is 1.5ppm, total sulfur content 0.6ppm.
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and propylene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity Beta zeolites, 160 DEG C, reaction pressure 3.0MPa of reaction temperature, propylene weight air speed 10.0h-1, the molar ratio 4.0 of benzene and propylene, when successive reaction 160 is small, propylene conversion 65%.
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and ethene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity Beta zeolites, 205 DEG C, reaction pressure 4.5MPa of reaction temperature, weight ethylene air speed 3.0h-1,
The molar ratio 4.0 of benzene and ethene, when successive reaction 200 is small, conversion of ethylene reaches 71%.
【Comparative example 2】
According to【Embodiment 3】Method, water content 300ppm, total nitrogen content 10ppm, total sulfur content 1.6ppm in benzene feedstock,
Benzene feedstock is directly entered adsorbent bed without rectifying column, and adsorbent bed filling 100gBeta zeolites are adsorbent, inhales
Attached dose of bed loads 100g acidity Beta zeolites, adsorbent bed 160 DEG C, pressure 2.0MPa of temperature, benzene weight space velocity 3.0h-1。
Continuous operation 100hr, using the total nitrogen content of the adsorbent bed outlet of sulphur blood urea/nitrogen analyzer analysis, total sulfur content is for 1.7ppm
1.6ppm。
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and propylene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity MCM-22 zeolites, 160 DEG C, reaction pressure 3.0Mpa of reaction temperature, propylene weight air speed
10.0h-1, the molar ratio 4.0 of benzene and propylene, when successive reaction 200 is small, propylene conversion reaches 46%.
Using the above-mentioned benzene by purification as raw material, goal response is alkylated to benzene and ethene, reaction condition is：It is fixed
Bed reactor, catalyst is acidity MCM-22 zeolites, 205 DEG C, reaction pressure 4.5MPa of reaction temperature, weight ethylene air speed
3.0h-1, the molar ratio 4.0 of benzene and ethene, when successive reaction 200 is small, conversion of ethylene reaches 35%.
Claims (14)
1. a kind of method that polar compound is removed from the aromatic raw material containing polar compound, comprises the following steps：
A) aromatic raw material containing polar compound enters rectifying column, and tower reactor obtains the first logistics, and tower top obtains the second logistics；
B) first logistics enters adsorption zone, after being contacted with adsorbent, obtains being substantially free of the aromatic raw material of polar compound.
2. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, the polar compound includes water, nitrogen compound or sulphur compound.
3. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, the aromatic raw material containing polar compound contains the water of 1~1000ppm.
4. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 3
It is, the aromatic raw material containing polar compound contains the water of 10~500ppm.
5. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, the aromatic raw material containing polar compound contains the nitrogen compound of 0.1~10ppm in terms of nitrogen.
6. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, the aromatic raw material containing polar compound contains the sulphur compound of 0.1~10ppm in terms of sulphur.
7. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, the temperature that the aromatic raw material containing polar compound enters rectifying column is 40~120 DEG C.
8. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, the operating condition of the rectifying column includes：60~180 DEG C of tower top temperature, 70~200 DEG C of bottom temperature.
9. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 8
It is, the operating condition of the rectifying column includes：70~160 DEG C of tower top temperature, 80~180 DEG C of bottom temperature.
10. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, the operating condition of the adsorption zone includes：70~180 DEG C, pressure 0~6.0MPa in terms of gauge pressure of temperature, aromatic raw material into
When expecting that weight space velocity 0.1~100 is small-1。
11. removing the method for polar compound from the aromatic raw material containing polar compound according to claim 10, it is special
Sign is that the operating condition of the adsorption zone includes：80~160 DEG C, pressure 0.1~5.0MPa in terms of gauge pressure of temperature, aromatics are former
When expecting that feed weight air speed 0.2~50 is small-1。
12. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, the adsorbent is Emathlite, Y zeolites, X zeolites, 13X zeolites, modenite, Beta zeolites, MWW structural zeolites.
13. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, second logistics is divided into third―party logistics and the 4th logistics, and third―party logistics are back to rectifying column, the 4th logistics discharge circle
Outside.
14. the method for polar compound, its feature are removed from the aromatic raw material containing polar compound according to claim 1
It is, the rectifying column tower top is configured with condenser and return tank, and reflux is introduced into after the condensed device condensation of the second logistics
Tank, is further divided into third―party logistics and the 4th logistics.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610878287.7A CN107915567A (en) | 2016-10-08 | 2016-10-08 | The method that polar compound is removed from the aromatic raw material containing polar compound |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610878287.7A CN107915567A (en) | 2016-10-08 | 2016-10-08 | The method that polar compound is removed from the aromatic raw material containing polar compound |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107915567A true CN107915567A (en) | 2018-04-17 |
Family
ID=61892171
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610878287.7A Pending CN107915567A (en) | 2016-10-08 | 2016-10-08 | The method that polar compound is removed from the aromatic raw material containing polar compound |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107915567A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112755591A (en) * | 2019-10-21 | 2021-05-07 | 中国石油化工股份有限公司 | Method for removing alkaline nitrogenous substances in organic solvent, method for aromatic alkylation reaction and device for aromatic alkylation reaction |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1639089A (en) * | 2002-02-28 | 2005-07-13 | 斯东及韦伯斯特公司 | Production of alkyl aromatic compounds |
| CN102060650A (en) * | 2010-12-29 | 2011-05-18 | 天津市康科德科技有限公司 | Method for purifying chromatographic grade toluene |
| CN103030516A (en) * | 2013-01-06 | 2013-04-10 | 北京旭阳化工技术研究院有限公司 | Purification method of coking xylene |
| US20130217945A1 (en) * | 2012-02-22 | 2013-08-22 | Uop Llc | Processes and systems for treating aromatic feed including an aromatic component and nitrogen-containing impurities, and processes and systems for preparing a reaction product of the aromatic component |
| CN104936929A (en) * | 2012-11-27 | 2015-09-23 | 巴杰许可有限责任公司 | Production of styrene |
-
2016
- 2016-10-08 CN CN201610878287.7A patent/CN107915567A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1639089A (en) * | 2002-02-28 | 2005-07-13 | 斯东及韦伯斯特公司 | Production of alkyl aromatic compounds |
| CN102060650A (en) * | 2010-12-29 | 2011-05-18 | 天津市康科德科技有限公司 | Method for purifying chromatographic grade toluene |
| US20130217945A1 (en) * | 2012-02-22 | 2013-08-22 | Uop Llc | Processes and systems for treating aromatic feed including an aromatic component and nitrogen-containing impurities, and processes and systems for preparing a reaction product of the aromatic component |
| CN104936929A (en) * | 2012-11-27 | 2015-09-23 | 巴杰许可有限责任公司 | Production of styrene |
| CN103030516A (en) * | 2013-01-06 | 2013-04-10 | 北京旭阳化工技术研究院有限公司 | Purification method of coking xylene |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112755591A (en) * | 2019-10-21 | 2021-05-07 | 中国石油化工股份有限公司 | Method for removing alkaline nitrogenous substances in organic solvent, method for aromatic alkylation reaction and device for aromatic alkylation reaction |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU767622B2 (en) | Aromatic alkylation process | |
| US7517506B2 (en) | Process for the production of alkylbenzene with ethane stripping | |
| RU2322430C2 (en) | Alkylaromatic compounds production process | |
| CA2633215C (en) | Improved process for the dehydrogenation of alkyl-aromatic hydrocarbons for the production of vinyl-aromatic monomers | |
| CN107915567A (en) | The method that polar compound is removed from the aromatic raw material containing polar compound | |
| CN107915566A (en) | Produce the device of alkylaromatic | |
| KR20100123719A (en) | Process for production of ethylbenzene from toluene and methane | |
| ES2342400T3 (en) | IMPROVED PROCEDURE FOR THE PRODUCTION AND PURIFICATION OF VINYLOMATIC MONOMERS. | |
| CN107915568A (en) | The method for producing alkylaromatic | |
| US20060194991A1 (en) | Treatment of alkylation catalyst poisons | |
| CN111097369A (en) | Method for removing polar compounds | |
| TWI395620B (en) | Treatment of alkylation catalyst poisons with dehydrogenation | |
| EP2590912B1 (en) | Process for recovering monoalkylbenzene | |
| KR100683509B1 (en) | Process for the preparation of alkylaromatics using solid alkylation catalysts | |
| KR100348988B1 (en) | Process for producing diarylethane having high quality | |
| EP2516365B1 (en) | Process for recovering monoalkylbenzene | |
| MXPA01006186A (en) | Improved aromatic alkylation process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20180417 |