CN107163172A - A kind of Joint Production system and method for Corvic - Google Patents
A kind of Joint Production system and method for Corvic Download PDFInfo
- Publication number
- CN107163172A CN107163172A CN201710355299.6A CN201710355299A CN107163172A CN 107163172 A CN107163172 A CN 107163172A CN 201710355299 A CN201710355299 A CN 201710355299A CN 107163172 A CN107163172 A CN 107163172A
- Authority
- CN
- China
- Prior art keywords
- production
- polyvinyl chloride
- ethylene
- chlorine
- corvic
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 249
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 242
- 229920000915 polyvinyl chloride Polymers 0.000 claims abstract description 209
- 239000004800 polyvinyl chloride Substances 0.000 claims abstract description 208
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 187
- 239000005977 Ethylene Substances 0.000 claims abstract description 158
- 230000008569 process Effects 0.000 claims abstract description 129
- 238000005660 chlorination reaction Methods 0.000 claims abstract description 111
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 98
- 239000000460 chlorine Substances 0.000 claims abstract description 98
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 97
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims abstract description 90
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims abstract description 88
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 claims abstract description 80
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 70
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 70
- 239000011347 resin Substances 0.000 claims abstract description 50
- 229920005989 resin Polymers 0.000 claims abstract description 50
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 45
- 239000005997 Calcium carbide Substances 0.000 claims abstract description 15
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 claims abstract description 15
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 14
- 239000006227 byproduct Substances 0.000 claims abstract description 13
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical group ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 claims description 64
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 60
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 57
- 239000011591 potassium Substances 0.000 claims description 57
- 229910052700 potassium Inorganic materials 0.000 claims description 57
- 239000007789 gas Substances 0.000 claims description 53
- 239000004743 Polypropylene Substances 0.000 claims description 52
- -1 polypropylene Polymers 0.000 claims description 48
- 229920001155 polypropylene Polymers 0.000 claims description 46
- 238000006243 chemical reaction Methods 0.000 claims description 41
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 36
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 34
- 239000000126 substance Substances 0.000 claims description 33
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 27
- 239000003054 catalyst Substances 0.000 claims description 27
- 239000011777 magnesium Substances 0.000 claims description 25
- 229910052749 magnesium Inorganic materials 0.000 claims description 25
- 238000009835 boiling Methods 0.000 claims description 23
- 229910052739 hydrogen Inorganic materials 0.000 claims description 16
- 239000001257 hydrogen Substances 0.000 claims description 16
- 238000006116 polymerization reaction Methods 0.000 claims description 16
- 238000001035 drying Methods 0.000 claims description 14
- 238000005336 cracking Methods 0.000 claims description 13
- SCYULBFZEHDVBN-UHFFFAOYSA-N 1,1-Dichloroethane Chemical class CC(Cl)Cl SCYULBFZEHDVBN-UHFFFAOYSA-N 0.000 claims description 12
- 230000008859 change Effects 0.000 claims description 10
- 238000004523 catalytic cracking Methods 0.000 claims description 8
- 238000000354 decomposition reaction Methods 0.000 claims description 8
- 239000000843 powder Substances 0.000 claims description 8
- 229920000178 Acrylic resin Polymers 0.000 claims description 7
- 239000004925 Acrylic resin Substances 0.000 claims description 7
- 230000002779 inactivation Effects 0.000 claims description 5
- 229920001596 poly (chlorostyrenes) Polymers 0.000 claims description 5
- 238000007872 degassing Methods 0.000 claims description 4
- 239000008187 granular material Substances 0.000 claims description 3
- 230000007613 environmental effect Effects 0.000 abstract description 4
- 238000004880 explosion Methods 0.000 abstract 1
- 239000002994 raw material Substances 0.000 description 23
- 239000000047 product Substances 0.000 description 21
- 239000007788 liquid Substances 0.000 description 18
- 239000007791 liquid phase Substances 0.000 description 17
- 238000012545 processing Methods 0.000 description 17
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 15
- 239000012071 phase Substances 0.000 description 15
- 239000000463 material Substances 0.000 description 14
- 238000000197 pyrolysis Methods 0.000 description 14
- 238000005516 engineering process Methods 0.000 description 11
- 239000002351 wastewater Substances 0.000 description 11
- 238000000926 separation method Methods 0.000 description 10
- 238000005265 energy consumption Methods 0.000 description 9
- 230000008016 vaporization Effects 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 239000003245 coal Substances 0.000 description 8
- 230000000694 effects Effects 0.000 description 8
- 238000011084 recovery Methods 0.000 description 8
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 7
- 150000001336 alkenes Chemical class 0.000 description 7
- 239000012535 impurity Substances 0.000 description 7
- 239000000178 monomer Substances 0.000 description 7
- 239000012452 mother liquor Substances 0.000 description 7
- 229920000642 polymer Polymers 0.000 description 7
- 239000002002 slurry Substances 0.000 description 7
- 238000009834 vaporization Methods 0.000 description 7
- 230000015572 biosynthetic process Effects 0.000 description 6
- 238000001816 cooling Methods 0.000 description 6
- 238000010992 reflux Methods 0.000 description 6
- 238000003786 synthesis reaction Methods 0.000 description 6
- 239000002912 waste gas Substances 0.000 description 6
- 239000003513 alkali Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 5
- 230000006835 compression Effects 0.000 description 5
- 238000007906 compression Methods 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- DHRRIBDTHFBPNG-UHFFFAOYSA-L magnesium dichloride hexahydrate Chemical compound O.O.O.O.O.O.[Mg+2].[Cl-].[Cl-] DHRRIBDTHFBPNG-UHFFFAOYSA-L 0.000 description 5
- 150000003839 salts Chemical class 0.000 description 5
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 description 4
- 239000002253 acid Substances 0.000 description 4
- DIWKDXFZXXCDLF-UHFFFAOYSA-N chloroethyne Chemical group ClC#C DIWKDXFZXXCDLF-UHFFFAOYSA-N 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 238000005260 corrosion Methods 0.000 description 4
- 238000005868 electrolysis reaction Methods 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 239000001103 potassium chloride Substances 0.000 description 4
- 235000011164 potassium chloride Nutrition 0.000 description 4
- 239000012495 reaction gas Substances 0.000 description 4
- 238000005201 scrubbing Methods 0.000 description 4
- 239000000243 solution Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000007334 copolymerization reaction Methods 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- 239000012530 fluid Substances 0.000 description 3
- 230000036541 health Effects 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000012423 maintenance Methods 0.000 description 3
- 229910052751 metal Inorganic materials 0.000 description 3
- 239000002184 metal Substances 0.000 description 3
- 229920003023 plastic Polymers 0.000 description 3
- 239000004033 plastic Substances 0.000 description 3
- 229940072033 potash Drugs 0.000 description 3
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 3
- 235000015320 potassium carbonate Nutrition 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 238000005057 refrigeration Methods 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 description 2
- 229910000975 Carbon steel Inorganic materials 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- GZETWZZNDACBTQ-UHFFFAOYSA-N [Cl].C=C Chemical compound [Cl].C=C GZETWZZNDACBTQ-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000010962 carbon steel Substances 0.000 description 2
- 238000007600 charging Methods 0.000 description 2
- QYAMPIKBANGIEM-UHFFFAOYSA-N chloroethene;hydrochloride Chemical compound Cl.ClC=C QYAMPIKBANGIEM-UHFFFAOYSA-N 0.000 description 2
- 150000001875 compounds Chemical class 0.000 description 2
- 238000002425 crystallisation Methods 0.000 description 2
- 230000008025 crystallization Effects 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 238000011010 flushing procedure Methods 0.000 description 2
- 229910052736 halogen Inorganic materials 0.000 description 2
- 150000002367 halogens Chemical class 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000010808 liquid waste Substances 0.000 description 2
- 229910001629 magnesium chloride Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 238000005453 pelletization Methods 0.000 description 2
- 238000005554 pickling Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 238000005204 segregation Methods 0.000 description 2
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical group O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- 125000001340 2-chloroethyl group Chemical class [H]C([H])(Cl)C([H])([H])* 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- NMLQNVRHVSWEGS-UHFFFAOYSA-N [Cl].[K] Chemical compound [Cl].[K] NMLQNVRHVSWEGS-UHFFFAOYSA-N 0.000 description 1
- HIVGXUNKSAJJDN-UHFFFAOYSA-N [Si].[P] Chemical compound [Si].[P] HIVGXUNKSAJJDN-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- OTUXCLKRSRDYPV-UHFFFAOYSA-N acetylene hydrochloride Chemical group Cl.C#C OTUXCLKRSRDYPV-UHFFFAOYSA-N 0.000 description 1
- 238000010306 acid treatment Methods 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 229910052783 alkali metal Inorganic materials 0.000 description 1
- 150000001340 alkali metals Chemical class 0.000 description 1
- 150000001345 alkine derivatives Chemical class 0.000 description 1
- 239000004411 aluminium Substances 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052787 antimony Inorganic materials 0.000 description 1
- WATWJIUSRGPENY-UHFFFAOYSA-N antimony atom Chemical compound [Sb] WATWJIUSRGPENY-UHFFFAOYSA-N 0.000 description 1
- 239000008346 aqueous phase Substances 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000003490 calendering Methods 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- RCTYPNKXASFOBE-UHFFFAOYSA-M chloromercury Chemical compound [Hg]Cl RCTYPNKXASFOBE-UHFFFAOYSA-M 0.000 description 1
- NEHMKBQYUWJMIP-UHFFFAOYSA-N chloromethane Chemical class ClC NEHMKBQYUWJMIP-UHFFFAOYSA-N 0.000 description 1
- 239000003426 co-catalyst Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000007033 dehydrochlorination reaction Methods 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- YNLAOSYQHBDIKW-UHFFFAOYSA-M diethylaluminium chloride Chemical compound CC[Al](Cl)CC YNLAOSYQHBDIKW-UHFFFAOYSA-M 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 239000002270 dispersing agent Substances 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229910000856 hastalloy Inorganic materials 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 238000007038 hydrochlorination reaction Methods 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 239000002649 leather substitute Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000011344 liquid material Substances 0.000 description 1
- STFVDQZWTZJIHE-UHFFFAOYSA-H magnesium;titanium(4+);hexachloride Chemical compound [Mg+2].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Cl-].[Ti+4] STFVDQZWTZJIHE-UHFFFAOYSA-H 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
- 125000002496 methyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 239000002808 molecular sieve Substances 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000004806 packaging method and process Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 229920000058 polyacrylate Polymers 0.000 description 1
- 238000007348 radical reaction Methods 0.000 description 1
- 239000012429 reaction media Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 230000001954 sterilising effect Effects 0.000 description 1
- 238000004659 sterilization and disinfection Methods 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 230000009967 tasteless effect Effects 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 229920005992 thermoplastic resin Polymers 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
- 238000004804 winding Methods 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F114/00—Homopolymers of compounds having one or more unsaturated aliphatic radicals, each having only one carbon-to-carbon double bond, and at least one being terminated by a halogen
- C08F114/02—Monomers containing chlorine
- C08F114/04—Monomers containing two carbon atoms
- C08F114/06—Vinyl chloride
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
- C08F110/04—Monomers containing three or four carbon atoms
- C08F110/06—Propene
-
- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
- C08F2/00—Processes of polymerisation
- C08F2/01—Processes of polymerisation characterised by special features of the polymerisation apparatus used
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Landscapes
- Chemical & Material Sciences (AREA)
- Health & Medical Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Medicinal Chemistry (AREA)
- Polymers & Plastics (AREA)
- Organic Chemistry (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
Abstract
The present invention discloses a kind of Joint Production system of Corvic, it includes chlorine generating means, ethylene producing device, ethylene process production Polyvinyl Chloride System and acetylene method production Polyvinyl Chloride System, the chlorine generating means, ethylene producing device are connected with ethylene process production Polyvinyl Chloride System respectively, and ethene made from chlorine made from the chlorine generating means and the ethylene producing device is supplied to the ethylene process production Polyvinyl Chloride System；The ethylene process production Polyvinyl Chloride System is connected with acetylene method production Polyvinyl Chloride System, and the byproduct hydrogen chloride of the acetylene as made from calcium carbide and water and ethylene process production Polyvinyl Chloride System is supplied to the acetylene method production Polyvinyl Chloride System.The present invention also provides the combine production method of Corvic, solves the possibility of chlorination hydrogen gas explosion, and obtained quality of PVC resin is excellent, great competitiveness, and production process environmental protection and economy.
Description
Technical field
The present invention relates to the technical field of resource comprehensive utilization of chemical products, and in particular to a kind of connection of Corvic
System and method is produced in symphysis.
Background technology
Corvic (Polyvinyl Chloride, abbreviation PVC), is by VCM (Vinyl
Chloride Monomer, abbreviation VCM) high-molecular compound that is polymerized.Polyvinyl chloride resin is to be liked, rather flowed deeply at present
Row and a kind of synthetic material being also widely used, as the second largest universal tree for being only second to polyvinyl resin in the world
Fat, accounts for the 29% of World Synthetic Resin aggregate consumption.Polyvinyl chloride resin easy processing, can by molding, laminated, injection, extrusion molding, calendering,
The blowing mode such as hollow is processed, polyvinyl chloride resin mainly for the production of the plastics soft goods such as artificial leather, film, trunking,
The plastics boardy product such as sheet material, door and window, pipeline and valve can be produced.
It is typically necessary in the preparation method of polyvinyl chloride resin using VCM as raw materials for production, then by polymerization, vapour
Obtained polyvinyl chloride resin is carried and dried, includes acetylene method production PVC in China PVC production method and ethylene process produces two kinds of PVC
Process route, because China is the present situation of " oil-poor, rich coal, few gas ", so the polyvinyl chloride resin of acetylene method production vinyl chloride manufacture is accounted for
According to leading position, produce polyvinyl chloride resin producer with this method at present and be concentrated mainly on China, account for the 70% of China's polyvinyl chloride resin total amount.
Acetylene method production PVC raw material is coal, and calcium carbide is made with lime stone in coal at high temperature, and calcium carbide meets water generation second
Alkynes, under mercuric chleride catalyst effect, acetylene and the direct synthesis vinyl chloride thereof of hydrogen chloride addition (VCM), then aggregated obtained PVC
Resin.Its production process can be divided into acetylene and prepare and purification, VCM synthesis, product purification and chloroethylene polymerization.Wherein chlorination
Hydrogen is as main raw material, and quality requirement is higher, and chloroacetylene is also easy to produce in process of production, it may occur however that blast, therefore usually
Need to provide the processing unit of hydrogen chloride or take other measures to prevent blast, both added the complexity of system, and also carried
High production cost.
Ethylene process production PVC raw material is oil, and oil produces ethene by cracking, and ethene is anti-through superchlorination or oxychlorination
Dichloroethanes should be synthesized, repressurization heating cracking dehydrochlorination generation vinyl chloride forms polyvinyl chloride resin after polymerization.Production process
In can produce a large amount of byproduct hydrogen chlorides, it can be common that with water absorb be changed into spent acid, a large amount of spent acid process if being handled
It is more complicated, production cost is improved, if not handling and polluting the environment, is unfavorable for clean manufacturing.
So, there is production cost height, environmental pollution when preparing Corvic in existing acetylene method or ethylene process
Big the problem of, therefore be badly in need of developing a kind of new method to prepare Corvic.
The content of the invention
It is existing for solving it is an object of the invention to provide a kind of Joint Production system and method for Corvic
Production cost when Corvic is prepared with the presence of method is high, it is big for environment pollution the problem of.
To achieve these goals, the present invention provides following technical scheme：A kind of Joint Production system of Corvic
System includes chlorine generating means, ethylene producing device, ethylene process production Polyvinyl Chloride System and acetylene method production polyvinyl chloride
Device, wherein, the chlorine generating means, ethylene producing device are connected with ethylene process production Polyvinyl Chloride System respectively,
Ethene made from chlorine made from the chlorine generating means and the ethylene producing device is supplied to the ethylene process to produce
Polyvinyl Chloride System, for producing Corvic；The ethylene process production Polyvinyl Chloride System produces polychlorostyrene with acetylene method
Ethylene unit is connected, and the acetylene as made from calcium carbide and water and the ethylene process produce the side product chlorinated of Polyvinyl Chloride System
Hydrogen is supplied to the acetylene method production Polyvinyl Chloride System, for producing Corvic.
Preferably, the chlorine generating means includes electrolytic chlorination potassium device and electrolytic chlorination magnesium apparatus, the electrolytic chlorine
Change potassium device and electrolytic chlorination magnesium apparatus to be connected with ethylene process production Polyvinyl Chloride System respectively, be the ethylene process production
Polyvinyl Chloride System provides chlorine, and the electrolytic chlorination potassium device is also connected with acetylene method production Polyvinyl Chloride System, institute
Hydrogen chloride made from stating electrolytic chlorination potassium device is supplied to the acetylene method production Polyvinyl Chloride System, for producing polyvinyl chloride
Resin.
Preferably, in the ethylene process production Polyvinyl Chloride System, chlorine is provided by the electrolytic chlorination potassium device, described
The electrolytic chlorination magnesium apparatus provides a part of chlorine and supplemented when the chlorine that electrolytic chlorination potassium device is provided is not enough.
Preferably, in the acetylene method production Polyvinyl Chloride System, hydrogen chloride is filled by ethylene process production polyvinyl chloride
The accessory substance put is provided, the electrolytic chlorination potassium device when hydrogen chloride that the ethylene process production Polyvinyl Chloride System is provided is not enough
A part of hydrogen chloride is provided to be supplemented.
Preferably, the Joint Production system also include polypropylene production apparatus, the polypropylene production apparatus with it is described
Ethylene producing device is connected, and accessory substance propylene made from the ethylene producing device is supplied to the polypropylene production apparatus, is used
In production acrylic resin.
Preferably, the ethylene process production Polyvinyl Chloride System uses high/low temperature chlorination combined producing process, the chlorine
Ethene feeding low temperature direct chlorination reactor, high temperature made from chlorine made from generating means and the ethylene producing device
Direct chlorination reactor is made dichloroethanes, then through high boiling tower is refined, low pressure cracking and polymerisation, polyvinyl chloride tree is made
Fat.
The present invention also provides a kind of combine production method of Corvic, comprises the following steps that：
1) ethene and propylene is made using methanol decomposition catalytic cracking process in ethylene producing device；
2) ethene made from the ethylene producing device and chlorine are prepared through ethylene process production Polyvinyl Chloride System
Corvic, chlorine is provided by electrolytic chlorination potassium device, and the chlorine that the electrolytic chlorination potassium device is provided is electrolysed when not enough
Chlorination magnesium apparatus provides a part of chlorine and supplemented；
3) acetylene made from calcium carbide and water and hydrogen chloride prepare polychlorostyrene second through acetylene method production Polyvinyl Chloride System
Olefine resin, the accessory substance that hydrogen chloride produces Polyvinyl Chloride System by ethylene process is provided, and the ethylene process produces Polyvinyl Chloride System
The electrolytic chlorination potassium device provides a part of hydrogen chloride and supplemented during the hydrogen chloride deficiency of offer；
4) propylene made from the ethylene producing device prepares acrylic resin through polypropylene production apparatus.
Preferably, the ethylene producing device uses methanol decomposition catalytic cracking process, and methanol is with catalyst in fluid bed
Reacted in reactor, the catalyst of reaction inactivation burns laggard fluidized bed reactor cycles reaction, warp in regenerator
Dry separating treatment and ethene and propylene is made.
Preferably, in the acetylene method production Polyvinyl Chloride System, calcium carbide and the obtained acetylene of water reaction and hydrogen chloride
Vinyl chloride is made in the reactor, then becomes press-dehydrating, high low boiling tower rectifying and polymerisation through alternating temperature, polyvinyl chloride tree is made
Fat.
Preferably, the polypropylene production apparatus uses continuous fluidized bed polymerization technique, from ethylene production dress
The accessory substance propylene put enters the vertical gas-phase fluidized-bed reactor production polypropylene powder tree containing catalyst system with hydrogen
Fat, obtained polypropylene powder resin enters the life of Squeezinggranulator group after recycle gas compressor and recycle gas cooler degassing
Into polypropylene granules resin.
The Joint Production system and method for the Corvic provided compared to prior art, the present invention has following excellent
Gesture：
First, the present invention provides ethylene process and acetylene method Joint Production PVC, devises a kind of PVC Joint Production works of innovation
Skill route, the byproduct hydrogen chloride of output is directly used among acetylene method production PVC when ethylene process is produced into PVC, due to ethene
The hydrogen chloride that cracking dichloroethanes is produced when method produces PVC is free of free chlorine and moisture, greatly reduces in acetylene method production PVC
The possibility that generation chloroacetylene explodes, and the corrosivity to VCM converters is greatly reduced, add making for equipment
Use the life-span；Meanwhile, the oxychlorination unit part in conventional ethylene method production PVC techniques is eliminated, corresponding investment, original is reduced
The use of material and catalyst and the labor intensity of operating personnel, effectively reduce production cost；On the other hand, hydrogen chloride can also
There is provided by electrolytic chlorination potassium device, it is ensured that sufficient raw；
2nd, two sets of PVC process units providing of the present invention both can with Joint Production, can also isolated operation, greatly carry
High operating flexibility, can accordingly be regulated and controled, more flexibility according to the situation of actual production；Utilize electrolytic chlorination simultaneously
Potassium device and electrolytic chlorination magnesium apparatus are made chlorine and are supplied to ethylene process to produce PVC, reduce production cost, reduce environment dirt
Dye, also achieves the comprehensive cyclic utilization of industrial chain；
3rd, the propylene of coproduction when preparing ethene is used to produce acrylic resin by the present invention, by ethylene producing device, poly- third
The techniques such as alkene process units combine, and form overall technique industrial chain, around polyvinyl chloride resin so that product is more polynary, enter
One step improves resource utilization, and industrial chain whole competitiveness is stronger；
4th, the present invention provides stripping retracting device, by the way of slurry stripping and wastewater stripping, in terms of liquid phase, to the greatest extent
Possible recovery raw material VCM, not only reduces consumption of raw materials, and reduce pollutions of the VCM to environment；Present invention simultaneously provides
Centrifuge mother liquor processing unit, is handled the liquid after the stripping retracting device processing, and produced part centrifugation is female
After liquid filtration treatment, for technique flushing water, the consumption of desalted water can be reduced；After another part centrifuge mother liquor in-depth processing, use
In circulating cooling make-up water, the recycling rate of waterused of water is improved；The present invention also provides exhaust gas processing device, in terms of gas phase, to return
The VCM finished up in gas, so as to reduce the norm quota of consumption of vinyl chloride, decreases pollutions of the VCM to environment, thus the present invention from
Two aspects of gas phase and liquid phase are handled waste gas and waste water, both can effectively reclaim raw material, also cause whole Joint Production
Technique is more environmentally friendly more economical.
Brief description of the drawings
By reading the detailed description of hereafter preferred embodiment, various other advantages and benefit is common for this area
Technical staff will be clear understanding.Accompanying drawing is only used for showing the purpose of preferred embodiment, and is not considered as to the present invention
Limitation.In the accompanying drawings：
Fig. 1 shows a kind of structural representation of the Joint Production system of the Corvic of preferred embodiment of the invention
Figure；
Fig. 2 shows the process chart of the Joint Production system of Corvic shown in Fig. 1.
Brief description of the drawings
10- chlorine generating means, 11- electrolytic chlorination potassium devices,
111- primary refined brine units, 112- disalt electrolysis cells,
113- hydrogen chloride synthesis devices, 12- electrolytic chlorination magnesium apparatus,
13- ethylene producing devices, 131- vaporization units,
132- fluidized-bed reactors, 133- scrubbing towers,
134- reactor compressors, 135- gas phase driers,
136- liquid phase driers, 137- dethanizers,
138- ethylene rectifying columns, 139- propylene rectification towers,
130- propylene refrigeration compressors, 14- ethylene processes production Polyvinyl Chloride System,
141- low temperature direct chlorination reactors, 142- high temperature direct chlorination reactors,
143- high boiling towers, 144- pyrolysis furnaces,
145-VCM refined units, the polymeric kettles of 146- first,
147- first strips drying unit, and 15- acetylene methods produce Polyvinyl Chloride System,
151- acetylene generators, 152-VCM reactors,
153- rectification cells, the polymeric kettles of 154- second,
The stripping drying units of 155- second, 16- polypropylene production apparatus,
161- fluidized-bed reactors, 162- recycle gas compressors,
163- recycle gas coolers, 164- extruder grain units.
Embodiment
The invention provides many applicable creative concepts, the creative concept can be reflected in a large number of on specific
Hereinafter.Specific embodiment described in following embodiments of the present invention is only as embodiment of the invention
Exemplary illustration, and be not meant to limit the scope of the invention.
It should be noted that according to national standard《The universal Corvic of GB/T 5761-2006 suspension methods》Including
In the polyvinyl chloride resin of different model, following embodiments only by taking SG5 type polyvinyl chloride resins as an example, its credit rating specification is classified such as the institute of table 1
Show.
Wherein S represents suspension polymerisation, and G represents resins for universal use, and 5 represent viscosity number classification number.
The SG5 type polyvinyl chloride resin credit ratings specification of table 1 is classified
The present invention provides following technical scheme：A kind of Joint Production system of Corvic is filled including chlorine
Put, ethylene producing device, ethylene process production Polyvinyl Chloride System and acetylene method produce Polyvinyl Chloride System, wherein, the chlorine
Gas generating means, ethylene producing device are connected with ethylene process production Polyvinyl Chloride System respectively, the chlorine generating means
Ethene made from obtained chlorine and the ethylene producing device is supplied to the ethylene process production Polyvinyl Chloride System, uses
In production Corvic；The ethylene process production Polyvinyl Chloride System is connected with acetylene method production Polyvinyl Chloride System, by
Acetylene made from calcium carbide and water and the byproduct hydrogen chloride of ethylene process production Polyvinyl Chloride System are supplied to the acetylene
Method produces Polyvinyl Chloride System, for producing Corvic.
The present invention provides ethylene process and acetylene method Joint Production PVC, devises a kind of PVC combined producing process road of innovation
Line, provides raw material, when producing PVC due to ethylene process using ethylene process production PVC byproduct hydrogen chloride for acetylene method production PVC
The hydrogen chloride for cracking dichloroethanes generation is free of free chlorine and moisture, greatly reduces in acetylene method production PVC and generates chloroacetylene
The possibility exploded, and the corrosivity to VCM converters is greatly reduced, the service life of equipment is added, is dropped
Low production cost；
It is supplied to ethylene process to produce PVC and acetylene method production PVC using chlorine made from chlorine generating means simultaneously, not only
Reduce production cost, reduce environmental pollution, also achieve the comprehensive cyclic utilization of industrial chain.
Preferably, the chlorine generating means includes electrolytic chlorination potassium device and electrolytic chlorination magnesium apparatus, the electrolytic chlorine
Change potassium device and electrolytic chlorination magnesium apparatus to be connected with ethylene process production Polyvinyl Chloride System respectively, be the ethylene process production
Polyvinyl Chloride System provides chlorine, and the electrolytic chlorination potassium device is also connected with acetylene method production Polyvinyl Chloride System, institute
Hydrogen chloride made from stating electrolytic chlorination potassium device is supplied to the acetylene method production Polyvinyl Chloride System, for producing polyvinyl chloride
Resin.
The chlorine generating means that the present invention is provided includes electrolytic chlorination potassium device and electrolytic chlorination magnesium apparatus, electrolytic chlorination potassium
Chlorine made from chlorine made from device and hydrogen chloride and electrolytic chlorination magnesium apparatus can be used for production polyvinyl chloride, electrolytic chlorine
Change magnesium metal made from potassium hydroxide made from potassium device and electrolytic chlorination magnesium apparatus, widely used, surcharge is high, because
This comprehensively utilizes a variety of devices, forms the benign cycle mutually digested, can further improve productivity effect；Especially Qinghai Area is rich
Containing a large amount of salt lakes, the industrial chain based on potash fertilizer can produce substantial amounts of potassium chloride and the old halogen (main component of waste liquid in production
For magnesium chloride, turn into bischofite after crystallization), it can be gathered materials on the spot simultaneously by electrolytic chlorination potassium device and electrolytic chlorination magnesium apparatus
The accessory substance produced using potash fertilizer carries out the preparation of chlorine, further reduces production cost
Preferably, in the ethylene process production Polyvinyl Chloride System, chlorine is provided by the electrolytic chlorination potassium device, described
The electrolytic chlorination magnesium apparatus provides a part of chlorine and supplemented when the chlorine that electrolytic chlorination potassium device is provided is not enough.
Chlorine can be supplied to ethylene process to give birth to by the electrolytic chlorination potassium device and electrolytic chlorination magnesium apparatus that the present invention is provided
Polyvinyl Chloride System is produced, both direction provides chlorine, can both ensure that the source of chlorine is sufficient, can also be advised according to actual production
Mould is adjusted.
Preferably, in the acetylene method production Polyvinyl Chloride System, hydrogen chloride is filled by ethylene process production polyvinyl chloride
The accessory substance put is provided, the electrolytic chlorination potassium device when hydrogen chloride that the ethylene process production Polyvinyl Chloride System is provided is not enough
A part of hydrogen chloride is provided to be supplemented.
The source of hydrogen chloride provides both direction when the present invention produces PVC for acetylene method, and PVC devices are produced with ethylene process
Based on the hydrogen chloride of offer, supplemented by the hydrogen chloride that electrolytic chlorination potassium device is provided, the sufficient of raw material is supplied during ensureing to produce PVC
Should, because the hydrogen chloride that ethylene process produces the offer of PVC devices is free of free chlorine and moisture, it is only necessary to electrolytic chlorination potassium device
Hydrogen chloride is handled, and can be reduced the treatment scale of hydrogen chloride, be reduced production cost.
Preferably, the Joint Production system also include polypropylene production apparatus, the polypropylene production apparatus with it is described
Ethylene producing device is connected, and accessory substance propylene made from the ethylene producing device is supplied to the polypropylene production apparatus, is used
In production acrylic resin.
The propylene of coproduction when preparing ethene is used to produce polypropylene by the present invention, and ethylene producing device, polypropylene are produced
The techniques such as device combine, and form overall technique industrial chain, around polyvinyl chloride resin so that product is more polynary, further carry
High resource utilization, industrial chain whole competitiveness is stronger.
Preferably, the ethylene process production Polyvinyl Chloride System uses high/low temperature chlorination combined producing process, the chlorine
Ethene feeding low temperature direct chlorination reactor, high temperature made from chlorine made from generating means and the ethylene producing device
Direct chlorination reactor is made dichloroethanes, then through high boiling tower is refined, low pressure cracking and polymerisation, polyvinyl chloride tree is made
Fat.
The high/low temperature chlorination combined producing process that the present invention is provided is i.e. by the liquid two of (58 DEG C) reaction generations of low temperature chlorination
Chloroethanes feeding high-temp chlorination (118 DEG C) reactor makes it enter high boiling tower after vaporizing in gaseous mode, has not only saved height
The steam that tower, reboiler need to heat is boiled, and reduces pickling, alkali cleaning in conventional ethylene method low temperature chlorination production VCM techniques
Hydrogen chloride in part, and production process is after high-temperature process, without free chlorine and moisture, meets acetylene method production PVC
When to the quality requirement of hydrogen chloride；Other low temperature pyrolyzer can be reduced by-product impurities, so as to reduce rectifier column reflux rate
Etc. energy consumption.
The present invention also provides a kind of combine production method of Corvic, comprises the following steps that：
1) ethene and propylene is made using methanol decomposition catalytic cracking process in ethylene producing device；
2) ethene made from the ethylene producing device and chlorine are prepared through ethylene process production Polyvinyl Chloride System
Corvic, chlorine is provided by electrolytic chlorination potassium device, and the chlorine that the electrolytic chlorination potassium device is provided is electrolysed when not enough
Chlorination magnesium apparatus provides a part of chlorine and supplemented；
3) acetylene made from calcium carbide and water and hydrogen chloride prepare polychlorostyrene second through acetylene method production Polyvinyl Chloride System
Olefine resin, the accessory substance that hydrogen chloride produces Polyvinyl Chloride System by ethylene process is provided, and the ethylene process produces Polyvinyl Chloride System
The electrolytic chlorination potassium device provides a part of hydrogen chloride and supplemented during the hydrogen chloride deficiency of offer；
4) propylene made from the ethylene producing device prepares acrylic resin through polypropylene production apparatus.
The combine production method for the Corvic that the present invention is provided utilizes ethylene process and acetylene method Joint Production PVC,
Hydrogen chloride made from ethylene process is supplied to acetylene method, the possibility of blast is reduced, mitigates the complexity of process units, and is respectively filled
The product or accessory substance put can mutually digest, and reduce the waste gas and waste water of discharge, both effectively reduce production cost, carry
High income, it is also more environmentally friendly more economical.The present invention combines a variety of devices and technique in addition, is recombinated and is optimized,
Qinghai-xizang Plateau Region forms the industry chain of circular economy for integrating coal chemical industry, chemical industry for making chlorine and alkali and salt chemical engineering.
Preferably, the ethylene producing device uses methanol decomposition catalytic cracking process, and methanol is with catalyst in fluid bed
Reacted in reactor, the catalyst of reaction inactivation burns laggard fluidized bed reactor cycles reaction, warp in regenerator
Dry separating treatment and ethene and propylene is made.
Ethylene producing device is preparing low carbon olefinic hydrocarbon with methanol (DMTO) technology for introducing the Dalian Chemistry and Physics Institute, and MTO is in the world
To the unified call of methanol-to-olefins, using similar to catalytic cracking (FCC) technology, i.e. methanol and DMTO special-purpose catalysts
Reacted in reactor, the catalyst of reaction inactivation enters the recirculating fluidized bed skill of reactor after being burnt in regenerator
Art, to ensure the reactivity of catalyst and the stabilization of olefine selective；The technology have the reaction time section short, high conversion,
The features such as olefine selective is high.The reaction gas separation that MTO is produced uses advanced front-end deethanization back end hydrogenation isolation technics, the technology
Being compared compared with other similar techniques has technology chain short, low power consumption and other advantages.
Preferably, in the acetylene method production Polyvinyl Chloride System, calcium carbide and the obtained acetylene of water reaction and hydrogen chloride
Vinyl chloride is made in the reactor, then becomes press-dehydrating, high low boiling tower rectifying and polymerisation through alternating temperature, polyvinyl chloride tree is made
Fat.
Vinyl chloride be at normal temperatures and pressures be heavier than air one times, be slightly soluble in the colourless gas of water, inflammable, band narcoticness fragrance
Smell.VCM requires it very strict, trace impurity (such as low-boiling-point substance, high-boiling components and water) as primary raw material
Presence the quality of polymerization process and polyvinyl chloride resin is suffered from significantly affecting.If there is low-boiling-point substance impurity in VCM, gather
Low-boiling-point substance impurity energy and radical reaction when closing reaction, the internal double bonds of generation have bad shadow for the heat endurance of polyvinyl chloride resin
Ring, can also slow down the speed of polymerisation, so that the degree of polymerization of polyvinyl chloride resin declines；If there are high-boiling components in VCM
Impurity, will increase the degree of branching of polyvinyl chloride macromolecular, influence the stability of polymerization system and the particle shape of polyvinyl chloride resin；
If containing water in VCM, acidity can be produced, the pH value of polymerization system is influenceed, the stability of dispersant is destroyed, PVC is reduced
The heat endurance of resin.In the acetylene method production Polyvinyl Chloride System that the present invention is provided, using pressure-variable adsorption dewatering type, can have
Effect reduction VCM water content, it is ensured that VCM water content ＜ 100ppm, is more beneficial for polymerisation, the PVC trees for obtaining its polymerization
Fat better quality.
Preferably, the polypropylene production apparatus uses continuous fluidized bed polymerization technique, from ethylene production dress
The accessory substance propylene put enters the vertical gas-phase fluidized-bed reactor production polypropylene powder tree containing catalyst system with hydrogen
Fat, obtained polypropylene powder resin enters the life of Squeezinggranulator group after recycle gas compressor and recycle gas cooler degassing
Into polypropylene granules resin.
Polypropylene (Polypropylene, abbreviation PP) be by propylene polymerization prepared by a kind of thermoplastic resin.By methyl
Arrangement position is divided into isotactic polypropylene (isotactic polypropylene), random polypropylene (atactic
) and three kinds of syndiotactic polypropylene (syndiotactic polypropylene) polypropylene.PP is used as a kind of nontoxic, nothing
The highly crystalline polymer of smelly, tasteless milky, density only has 0.90~0.91g/cm3, it is most light in current all plastics
One of kind.It is particularly stable to water, and the water absorption rate in water is only 0.01%, molecular weight about 80,000~150,000, heat-resisting, corrosion resistant
Erosion, product can be its outstanding advantages with moise-heat sterilization, and application value is higher.
The polypropylene production apparatus that the present invention is provided uses the UNIPOLTM PP techniques of Dow Chemical.The technique is
A kind of continuous fluidized bed polymerization technique, using effective catalyst system, in addition to pelletizing water overflow water, without liquid waste row
Go out, the hydro carbons for being discharged into air is also seldom, therefore the influence to environment is very small, compared with other techniques, the technique is easier
Reach that requirement is strictly regulated in environmental protection, the various of health and safety.
The invention will be further described with specific embodiment below in conjunction with the accompanying drawings.
Embodiment 1
As shown in figure 1, the present embodiment provides a kind of Joint Production system of Corvic, it includes chlorine and filled
Put 10, ethylene producing device 13, ethylene process production Polyvinyl Chloride System 14, acetylene method production Polyvinyl Chloride System 15, polypropylene
Process units 16.
The chlorine generating means 10 includes electrolytic chlorination potassium device 11 and electrolytic chlorination magnesium apparatus 12；The electrolytic chlorination
Potassium device 11 is connected with ethylene process production Polyvinyl Chloride System 14, acetylene method production Polyvinyl Chloride System 15 respectively；
The electrolytic chlorination magnesium apparatus 12 is connected with ethylene process production PVC devices 14.
The ethylene producing device 13, ethylene process production PVC devices 14, acetylene method production PVC devices 15 are suitable
Sequence is connected, and the ethylene producing device 13 is also connected with the polypropylene production apparatus 16.
As shown in Fig. 2 the combine production method of the Corvic comprises the following steps：
Step 1: production ethene and propylene：Ethylene producing device using methanol decomposition catalytic cracking process be made ethene and
Propylene；
The ethylene producing device 13 includes vaporization unit 131, reaction member, drying unit and the separation being linked in sequence
Unit.Fluidized-bed reactor 132 that the reaction member includes being connected with vaporization unit 131, it is connected with fluidized-bed reactor 132
Regenerator；The drying unit includes scrubbing tower 133, the reaction pressure being connected with the fluidized-bed reactor 132 of reaction member
Contracting machine 134, gas phase drier 135 and liquid phase drier 136, the scrubbing tower 133 and the order of reaction gas compressor 134
Connection, the reaction gas compressor 134 connects the gas phase drier 135 and the liquid phase drier 136 respectively；Described point
From unit include dethanizer 137, ethylene rectifying column 138, propylene rectification tower 139, the gas phase drier 135 of drying unit and
Liquid phase drier 136 is connected with dethanizer 137 respectively, and dethanizer 137 connects ethylene rectifying column 138, propylene rectifying respectively
Tower 139.
Specifically, the methanol containing 5% water (250 DEG C) after the heating vaporization of vaporization unit 131 enters reaction list with gaseous state
Member, occurs cracking reaction in fluidized-bed reactor 132 in the presence of DMTO special-purpose catalysts, and the products such as ethene, propylene are made,
The DMTO special-purpose catalysts of reaction inactivation burn the laggard circular response of fluidized bed reactor 132, obtained second in regenerator
Alkene, propylene enter drying unit by fluidized-bed reactor 132, enter reaction gas after first passing through the cooling of the multiple wash of scrubbing tower 133
Compressor 134, reacted air compressor 134 enters gas phase drier 135, liquid phase drier 136 after compressing and carries out gas phase respectively
Dry and liquid phase is dried, enter back into separative element, dethanizer 137 separates carbon with the component of carbon more than 3 below 2, through ethene essence
Polymer grade ethylene and polymerization-grade propylene are prepared respectively after evaporating tower 138 and the separation of propylene rectification tower 139.Meanwhile, separative element
It is configured with propylene refrigeration compressor 130 and provides cryogen for ethene, propylene separation.
In the present embodiment, ethene made from the ethylene producing device 13 is supplied to the ethylene process production PVC devices
14, for producing PVC, obtained accessory substance propylene is supplied to the polypropylene production apparatus 16, for producing polypropylene.
Wherein, the supporting equipment propylene refrigeration compressor 130 of separative element employs back pressure turbine and three sections of compressions,
Low energy consumption is embodied in lectotype selection, it is energy-saving and emission-reduction, simple, convenient the advantages of safeguard, while back pressure 0.5MPa low pressure
Steam is incorporated to garden supervisor's net, alleviates the steam burden of garden.The unit assume responsibility for the whole alkene of ethylene producing device 13 point
From the low-temperature receiver of the Three Estate of system, tower top cryogen and tower reactor thermal source are provided for the tower separation of cold-zone, cold and hot friendship is realized
The purpose changed, the low transition of cold separating energy consumption in realizing from conventional ethylene cryogenic separation to coal-to-olefin.
In the present embodiment, the DMTO special-purpose catalysts are acidic catalyst SAPO-34, a kind of silicon phosphorus of aperture very little
Aluminium non-zeolite molecular sieve, the similar chabasie of its structure, with excellent heat endurance and hydrothermal stability.
DMTO technologies are higher to the quality requirement of methanol, so in the present embodiment, the methanol containing 5% water includes mutually mixing
The MTO level methanol and refined methanol of conjunction.Basicity, alkali metal and the total metal contents in soil of MTO grades of methanol are less than certain value, will to water content
Aspire for stability, refined methanol is the highly finished product of methanol.
Step 2: ethylene process produces polyvinyl chloride：
The polymer grade ethylene as made from ethylene producing device described in step one 13 and chlorine are produced through the ethylene process
PVC devices 14 prepare polyvinyl chloride resin, and chlorine is provided by the electrolytic chlorination potassium device 11, the electrolytic chlorination potassium device 11
The electrolytic chlorination magnesium apparatus 12 provides a part of chlorine and supplemented when the chlorine of offer is not enough；
The electrolytic chlorination potassium device 11 includes primary refined brine unit 111, the disalt electrolysis cells being linked in sequence
112 and hydrogen chloride synthesis device 113, the electrolytic chlorination potassium device 11 using potassium chloride as raw material, pass sequentially through it is described once
Potassium hydroxide, chlorine and hydrogen is made in salt refining unit 111 and disalt electrolysis cells 112 after being electrolysed, chlorine supplies the second
Alkene method production PVC devices 14 are used, and for producing PVC, hydrogen and chlorine pass through the hydrogen chloride synthesis device 113 when needed
Synthesize hydrogen chloride to use for acetylene method production PVC devices 15, for producing PVC；Obtained potassium hydroxide is after evaporation
Piece alkali (solid-state potassium hydroxide) is obtained, piece alkali may be used as raw material, drier, absorbent, medical daily use chemicals of sylvite production etc. and change
Work base stock, widely used, surcharge is high.
The electrolytic chlorination magnesium apparatus 12 is using bischofite as raw material, and especially Qinghai Area is rich in a large amount of salt lakes, with potash fertilizer
Based on industrial chain can be produced in production substantial amounts of potassium chloride and the old halogen of waste liquid (main component is magnesium chloride, after crystallization into
For bischofite), it is easy to gather materials on the spot using bischofite as raw material, magnesium metal and chlorine, metal is made after bischofite electrolysis
Magnesium belongs to light metal, and added value is high, application is wider, and obtained accessory substance chlorine produces PVC devices for the ethylene process
14 use, for producing PVC, certainly, and chlorine can also be incorporated to the chlorine of the electrolytic chlorination potassium device 11 when needed, pass through
The synthesising hydrogen of hydrogen chloride synthesis device 113 produces PVC devices 15 for the acetylene method and used.
In the present embodiment, chlorine made from the electrolytic chlorination potassium device 11 is supplied to the ethylene process production polychlorostyrene second
Alkene device 14, and with the electrolytic chlorination potassium device 11 provide chlorine based on, it is necessary to when, the electrolytic chlorination potassium device 11 can
The acetylene method production Polyvinyl Chloride System 15 is supplied to synthesising hydrogen, if therefore the electrolytic chlorination potassium device 11 is provided
The chlorine for producing Polyvinyl Chloride System 14 to the ethylene process is not enough, then the electrolytic chlorination magnesium apparatus 12 is made chlorine and is supplied to
The ethylene process production PVC devices 14, to be supplemented.
The ethylene process production PVC devices 14 include low temperature direct chlorination reactor 141, the direct chlorine of high temperature being linked in sequence
Change reactor 142, high boiling tower 143, pyrolysis furnace 144, VCM refined units 145, the first polymeric kettle 146 and the first stripping drying
Unit 147.
Specifically, the polymer grade ethylene as made from ethylene producing device described in step one 13 and chlorine send into the second
In alkene method production PVC devices 14, high/low temperature direct chlorination reactor is first fed into, is containing dichloroethanes
Low temperature (58 DEG C) the direct chlorination reactor 141 and high temperature (118 DEG C) of (Dichloroethane, abbreviation EDC) solution directly chlorine
Change chlorine and ethene in reactor 142 and occur the blistering reaction thick EDC of generation, will by high-temperature chlorination itself liberated heat
Essence EDC, smart EDC is made after progress EDC subtractive processes after thick EDC vaporizations, feeding high boiling tower 143, removing high-boiling components and passes through steam
EDC cracking process is carried out after vaporization, pyrolysis furnace 144 is sent into, EDC cracking reactions are carried out at a temperature of 480 DEG C, vinyl chloride is generated
Monomer (Vinyl Chloride Monomer, abbreviation VCM) and HCl, then after the VCM refined units 145 such as HCl towers, VCM towers
The VCM of polymer grade is made and the HCl gases of acetylene method PVC production are met, the VCM of polymer grade is carried out by the first polymeric kettle 146
Polymerisation, then by the first stripping drying unit 147 carry out that qualified ethylene process polyvinyl chloride resin is made after stripping drying, packaging.
In the present embodiment, byproduct hydrogen chloride made from the ethylene process production PVC devices 14 is supplied to the acetylene
Method production PVC devices 15.Because the reaction temperature of pyrolysis furnace 144 is up to 480 DEG C, and after VCM refined units 145 are refined
Impurity is can remove, so obtained hydrogen chloride is free of free chlorine and moisture, the quality requirement that acetylene method produces PVC is met.
The high temperature direct chlorination reactor 142 that the ethylene process production PVC devices 14 are used is by Occidental Chemical Corp of the U.S.
(OXY) patent is provided, and equipment is made up of reaction member, vapor-liquid separation unit and liquid-phase reflux unit.In vapor-liquid separation unit
Top reacts generation ferric trichloride as catalysis provided with the sacrifice for being filled with an iron Raschig ring bed for iron and chlorine
Agent, the reactor of reaction member is vertical row tubular reactor, and reaction medium therein is based on dichloroethanes, and material is by row
Enter reactor after bottom of the tube is scattered, reactor top extends to the vapor-liquid separation unit being relatively large in diameter, and liquid phase flows through extension
Downflow weir, stable liquid phase layer and stable difference liter can be so kept between material dispersion pipe and top liquid layer
Drop motion.After liquid phase flows into vapor-liquid separation unit, vapour phase can just be separated from liquid phase and leave reactor, and liquid phase is then
Because gravity by liquid-phase reflux pipe is back to reactor.The heat that chlorine and ethylene reaction are produced becomes product dichloroethanes
Gaseous state leaves at the top of gas-liquid separator.Because the heat produced by reaction can vaporize five times of dichloroethanes product, institute
To want maintenance reaction to carry out, it is necessary to which the part gaseous state dichloroethanes and circulating reflux at the top of condensing are into reactor, and circulation
Flowing back, some react obtained liquid material from low temperature direct chlorination, the operation of whole reactor it is final by high boiling tower bottom liquid phase Lai
Control.The reaction heat 100% of high temperature direct chlorination reaction is fully effective to be recycled.The EDC of evaporation is directly entered high boiling tower,
For EDC all in rectifier unit so that EDC rectifying removing heavy component does not need steam, it is possible to achieve load, which is down to, to be set
30% operation of meter ability.Simple iron catalyst system, it is not necessary to add special catalyst, reduce reaction cost.Instead
Answering the high velocity projector of device to design ensures effective decomposition of ethene and chlorine, and reaction efficiency is high, only need to once be tieed up in every 2-3
Shield maintenance.
The low temperature direct chlorination reactor 141 that the ethylene process production PVC devices 14 are used is by Occidental Chemical Corp of the U.S.
(OXY) patent is provided, and equipment is made up of conversion zone, segregation section, cooling section, including monoblock type shell-and-tube heat exchanger.Runtime
Between, conversion zone and cooling section are filled with liquid EDC, and segregation section is filled partially with EDC.Conversion zone is a straight vertical carbon steel
Pipe, length is 11390mm, and diameter has 1900mm.It is all to feed the bottom for being added to conversion zone by nickel matter distribution system.Instead
Liberated heat is answered to be removed heat with recirculated water by the heat exchanger of cooling section, chlorine and ethene are in EDC solution with trichlorine
Change iron reacts for catalyst and produces EDC.Whole reactor yield can accomplish the 30%~100% of designed capacity, without
Reduce efficiency or product purity.Raw material efficiency is high, and the efficiency of ethene and chlorine reaches more than 99.0%, and need not add catalyst.
Reactor and supporting cooler make for carbon steel material, reduce cost of investment, just need within every 2 to 3 years once to be overhauled.
In the ethylene process that the present invention is provided production PVC devices 14, high temperature direct chlorination reactor (HTDC) 142 and low
Warm direct chlorination reactor (LTDC) 141 is natural circulation reactor, it is not necessary to large-scale liquid circulation pump.
The pyrolysis furnace 144 that the ethylene process production PVC devices 14 are used is fabricated by by French conspicuous antimony patented technology, is cracked
144 points of stove is convection section and radiant section, and convection section effect is that Mist heat recovering is used for preheating EDC, and radiant section is used for splitting for EDC
Heating fuel gas is natural gas or coke-stove gas in solution reaction, burner hearth, it is possible to use multifuel firing pyrolysis furnace, burner hearth combustion
It is 480-490 DEG C to burn temperature, and the thermal efficiency that efficient pyrolysis furnace reaches is more than 90%.The low pressure operation of pyrolysis furnace 144, with vapor-phase material
Crack workshop section as entering, EDC conversion ratio is 55%, can be kept low coking rate and high on-line operation time, 1 year with
On need not devoke, while by-product impurities are reduced, so as to reduce the energy consumptions such as rectifier column reflux rate.Only can in cracking process
Produce few by-product article, such as butadiene, chloromethanes, diethylaluminum monochloride.The pyrolysis furnace 144 that the present invention is provided allows boiler tube more
It is thin so that investment is lower.The gas phase discharging of the chilling tower top of pyrolysis furnace 144 is used for preheating cracking feed EDC, and 80 are heated to from 40 DEG C
DEG C, save the use of steam and recirculated water.The EDC chargings that the flue gas at the top of pyrolysis furnace 144 is used to heat before cracking, from 80
DEG C it is warming up to 177 DEG C.The heat that the heat exchanger (TLE) of pyrolysis furnace 144 reclaims the high-temperature gas of discharge pyrolysis furnace 144 is had
The recuperation of heat of effect, VCM per ton reclaims 200,000 kilocalorie of steam and is used as 2.0MPaG high steams for equipment, accessory substance in device
Measure as 18.6t/h, folding standard coal 2.26t/h.
In the part of VCM refined units 145 of the ethylene process production PVC devices 14, the discharging of VCM bottom of towe is added by heat exchange
Heat makes the latter be warming up to 104 DEG C from 40 DEG C from dry crude EDC storage tanks to the EDC materials of the rectifying of high boiling tower 143, reclaims heat energy.
The ethylene process production PVC devices 14 use high/low temperature chlorination Joint Production VCM, by (58 DEG C) reactions of low temperature chlorination
Liquid EDC feeding high-temp chlorination (118 DEG C) reactors of generation make it enter high boiling tower 143 after vaporizing in gaseous mode, no
The steam that high boiling tower 143 needs to heat only has been saved, and has reduced acid in conventional ethylene method low temperature chlorination production VCM techniques
Wash, caustic wash section, and solve and a large amount of waste water are produced because of pickling, alkali cleaning need problem to be processed.
The ethylene process production PVC devices 14 that the present invention is provided also are configured with coke oven gas desulfurization, wastewater treatment, tail gas
Burn the production device such as high purity hydrochloric acid and steam.Wastewater stripping bottom of towe discharge (treated waste water) by heat exchanger heat from
The wastewater feed that sewage storage tank comes, 80 DEG C is warming up to from 40 DEG C, treated waste water sends out out-of-bounds further processing.For production
Raw waste gas, the incineration technology with the leading level in the world of the supporting Beijing Space Patent design of waste liquid, by the waste gas of generation, useless
Liquid is burned, and the heat of generation is used for accessory substance 2.8Mpa steam, and amount of by-products is 9t/h, not only realizes clean manufacturing,
And reached the economic effect that energy regenerating is utilized.CIU is also burnt while waste gas is disposed waste liquid using these
Heat energy accessory substance 2.5MpaG high steams, amount of by-products is 9t/h, folding standard coal 1.09t/h (24.98kg/MT.VCM), the steaming
Vapour is incorporated to garden high steam pipe network.
Step 3: acetylene method produces polyvinyl chloride：
Hydrogen chloride made from acetylene made from calcium carbide and water and step 2 produces PVC devices 15 through the acetylene method and is prepared into
To Corvic, the accessory substance that hydrogen chloride produces PVC devices 14 by the ethylene process is provided, the hydrogen chloride of insufficient section by
The accessory substance of the electrolytic chlorination potassium device 11 is provided；
The acetylene method production PVC devices 15 include the acetylene generator 151, VCM reactors 152, rectifying being linked in sequence
Unit 153, the second polymeric kettle 154, second stripping drying unit 155.The rectification cell 153 includes the compression being linked in sequence
Section, dewatering period and high low boiling tower, compression section are connected with VCM reactors 152, and high low boiling tower is connected with the second polymeric kettle 154.
Specifically, calcium carbide and water react generation acetylene in acetylene generator 151, it is obtained in step 2 with coming from
After hydrogen chloride mixing, reaction generation thick VCM, thick VCM pass through rectification cell in the VCM reactors 152 that coal is touched containing mercury chloride
153 compression section compression, dewatering period alternating temperature become press-dehydrating, removes after the rectifying of high low boiling tower and is made after moisture and high-boiling and low-boiling components
The VCM monomers of polymer grade, VCM monomers occur polymerisation, the second stripping drying unit 155 by the second polymeric kettle 154 and stripped
The qualified acetylene method PVC resin of output after drying.
Hydrogen chloride produces PVC devices 14 by the ethylene process and is made, due to hydrogen chloride by the Pintsch process of pyrolysis furnace 144 and
The refining and edulcoration of VCM refined units 145, after testing without free chlorine and moisture, greatly reduces and is generated in acetylene method production PVC
The possibility that chloroacetylene explodes, saves the installation cost of hydrochlorination, effectively reduces production cost.Therefore produced
Cheng Zhong, the production scale of the acetylene method production PVC devices 15 preferably produces chlorine made from PVC devices 14 according to the ethylene process
Depending on the scale for changing hydrogen, i.e., hydrogen chloride acetylene method production PVC devices described enough made from described ethylene process production PVC devices 14
15 use, it is not necessary to be additionally provided hydrogen chloride again, if the hydrogen chloride of the offer of ethylene process production PVC devices 14 is not enough,
The electrolytic chlorination potassium device 11, which provides a part of hydrogen chloride, to be used to supplement, the hydrogen chloride that the electrolytic chlorination potassium device 11 is provided
It is few, the scale relative reduction of the free chlorine that may wherein contain and water time share device is handled, installation cost can be saved.
The acetylene method production PVC devices 15 use alternating temperature transformation dehydration technique, by existing containing water management for VCM monomers
Below 50ppm, the polyvinyl chloride resin better quality for obtaining its polymerization.
Meanwhile, acetylene method production PVC devices 15 be configured with VCM monomers pressure-variable adsorption reclaim, mercury-containing waste water processing with
And the recovery of carbide slag slurries acetylene, resolving hydrochloric acid and the hydrochloric acid device such as parsing deeply.The present invention reclaims VCM rectifying using alternating temperature transformation
Acetylene and VCM in emission, further improve raw material availability, reduce production cost.Carbide slag slurries acetylene recovery device
The utilization rate of calcium carbide can be greatly improved, what is had an accident in reduction carbide slag slurries subsequent treatment because gathering acetylene gas can
Can property.The raw material converted after hydrogen chloride gas as VCM, solution are obtained using resolving hydrochloric acid, the deep analytic technique processing spent acid of hydrochloric acid
The problem of certainly abraum salt acid treatment is difficult.
Acetylene method is produced PVC, ethylene process production PVC and carries out Joint Production by the present invention, and the ethylene process produces PVC devices
Second polymeric kettle 154 of 14 the first polymeric kettle 146 and acetylene method production PVC devices 15 is using independent research
143m3Polymeric kettle, in the present embodiment, there is 10 polymeric kettles (wherein 6 production acetylene method PVC resins, 4 production second altogether
Alkene method polyvinyl chloride resin), the kettle interior diameter of the polymeric kettle is 4400mm, and chuck area is bigger.The production capacity of the polymeric kettle is
80000 tons/platform, the product quality height produced, the factor of merit can produce SG-3 types, SG-5 types, SG-7 types up to more than 95%
Etc. the polyvinyl chloride resin of a variety of trades mark, national sector standard requirement is satisfied by.
The polymeric kettle is made up of polymerization kettle, reflux condenser, the part of agitating device three.Kettle using half-pipe jacket,
Cold apron four in being set in kettle；Agitating device uses variable-frequency motor, double mechanical seal and the leaf sweepback blade of bottom stretching type three.
Polymeric kettle belongs to larger in the same industry, it is higher to automatically control, and reliability, security are extremely strong.Filled because polymeric kettle is stirred
It is speed change to put the course of work, and the present invention, using variable-frequency motor, can reduce power consumption according to its feature.
The Joint Production system that the present invention is provided is fed in the polymerization technique part of acetylene method, ethylene process using hot water, is gathered
Close reaction and be not required to hot water heating, thus be not in for the hot water of heating and mixed existing for removing the freezing aqueous phase of reaction heat
As so as to save steam and cold, reaching the purpose of energy-conservation.It polymerize simultaneously using good anti-sticking of enclosed charging, atomizing effect
Kettle technology and corresponding water washing device, kettle cleaning period can reach 500 kettles, reduce significant loss.
The Joint Production system that the present invention is provided is used when conveying hydrogen chloride into acetylene method production PVC devices 15
Hydrogen chloride compressor.General single-stage compressor can not meet process requirements, and compound compressor is the presence of high energy consumption, fault rate
High, complex structure and other problems, and the Joint Production system that the present invention is provided only needs single-stage compressor just can meet process requirements, also
Adapt to the rarefaction of air of Qinghai high altitude localities, the low state of inlet pressure, it has, and reliability is high, simple in construction, maintenance side
Just, the low feature of energy consumption.Because HCl has high corrosion characteristic, the corrosion resistance and sealing of compressor are proposed high
It is required that, rubber technology is served as a contrast by unique casing, inlet guide vane, is adapted to run under high-temp chlorination hydrogen environment, it is selected
Material be expensive Hastelloy material, with more corrosion resistance, environment is played a very good protection.Also compressor
Automaticity it is high, can continuously safe operation, adjusting means simply, preferably operates, can remote control completely, be not required to scene
It is on duty, the safety and health of personnel under hazardous environment is so also beneficial to, meets law clinic education rule.
The ethylene process that the present invention is provided production PVC devices 14 at the first polymeric kettle 146 provided with stripping retracting device,
Centrifuge mother liquor processing unit and exhaust gas processing device.The acetylene method production PVC devices 15 are also set at the second polymeric kettle 154
There are stripping retracting device, centrifuge mother liquor processing unit and exhaust gas processing device.
The stripping retracting device that the present invention is provided in terms of liquid phase, to the greatest extent may be used by the way of slurry stripping and wastewater stripping
The recovery raw material VCM of energy, not only reduces consumption of raw materials, and reduce pollutions of the VCM to environment；Polymeric size stripping is selected
In the novel tower-type slurry stripping process that state-of-the-art Arkema develops in the world at present, slurry VCM contents 10ppm with
Under, it is ensured that the drying process of polyvinyl chloride reaches environmental protection standard.The centrifuge mother liquor processing unit is reclaimed to the stripping
Liquid after device processing is handled, and after produced a part of centrifuge mother liquor filtration treatment, for technique flushing water, can be subtracted
The consumption of few desalted water；After another part centrifuge mother liquor in-depth processing, for circulating cooling make-up water, the recycling of water is improved
Rate；The exhaust gas processing device, in terms of gas phase, to reclaim the VCM in tail gas, so that the consumption for reducing vinyl chloride is determined
Volume, decreases pollutions of the VCM to environment, therefore the present invention is handled waste gas and waste water, you can effectively reclaim raw material,
Also so that whole combined producing process is more environmentally friendly, more economical.
Step 4: production polypropylene：
Propylene made from step one prepares acrylic resin through the polypropylene production apparatus 16.
The polypropylene production apparatus 16 uses the UNIPOLTM PP techniques of Dow Chemical.The technique is a kind of gas
Phase fluid bed produces polymarization method for prodcing polyacrylates, using effective catalyst system.The polypropylene production apparatus 16 includes what is be linked in sequence
Vertical gas-phase fluidized-bed reactor 161, recycle gas compressor 162, recycle gas cooler 163, extruder grain unit 164 and
Tail gas treating unit 165, the tail gas treating unit 165 includes tail gas recycle compressor, the tail gas recovery tower being linked in sequence, tail
Gas reclaims compressor and is connected with recycle gas cooler 163, and tail gas recovery tower is connected with fluidized-bed reactor 161, constitutes at tail gas
Reason circulation.
Fluidized-bed reactor is open-core type container, and its top carries expanding reach, and bottom belt is distributed device, first reactor behaviour
Make pressure for 3.4MPaG, 67 DEG C of temperature, second reactor operating pressure is 2.1MPaG, temperature 70 C；Recycle gas compressor is
Single-stage, centrifugal compressor.The gas fluidized-bed process is simple, economical, with high reliability, operating flexibility, security；Should
Technique can produce crushing-resistant copolymerization using a reactor with regard to that can produce homopolymerization and random copolymerization product, second reactor of series winding
Product, and production ethene or the high crushing-resistant copolymerization product of rubber bodies content need not reduce yield or worry fouling；This technique is removed
Beyond pelletizing water overflow water, without liquid waste discharge, the hydro carbons for being discharged into air is also seldom, therefore the influence to environment is very
Small, compared with other techniques, the technique more easily reachs environmental protection, the various of health and safety and strictly regulates requirement.
Specifically, polymerization-grade propylene made from step one is after propylene refining, with hydrogen (H2) enter and contain catalyst
The production PP powder resins of fluidized-bed reactor 161 of system, powder resin passes through recycle gas compressor 162, recycle gas cooler
163 carry out carrying out the generation pellet PP resins of Squeezinggranulator group 164 after blanking degassing, and tail gas enters tail through tail gas recycle compressor
Gas recovery tower, Propylene recovery raw material reenters reactor and reacted from tail gas, effectively reduces wastage of material, also reduces tail
Pollution of the gas to environment.
Further, hydrogen may come from hydrogen made from the electrolytic chlorination potassium device 11, by the electrolytic chlorination
Potassium device 11 is connected by pipeline with the polypropylene production apparatus 16, can be organically combined device, further be improved material
Utilization rate；The catalyst system includes major catalyst titanium tetrachloride-magnesium chloride, co-catalyst T2- electron donors.
The raw material proportioning of each device and the output of product are as shown in table 2 in the present embodiment.
The output of the raw material proportioning of table 2 and product
Embodiment 2
Polyvinyl chloride resin is prepared according to the step in embodiment 1, but chlorine is only provided by the electrolytic chlorination potassium device 11.
Embodiment 3
Polyvinyl chloride resin is prepared according to the step in embodiment 1, but the production scale of acetylene method production PVC devices 15 is pressed
Depending on the scale of hydrogen chloride made from ethylene process production PVC devices 14, i.e., the original of described acetylene method production PVC devices 15
Material hydrogen chloride is only provided by ethylene process production Polyvinyl Chloride System 14.
Embodiment 4
Polyvinyl chloride resin is prepared according to the step in embodiment 1, but chlorine is only provided by the electrolytic chlorination potassium device 11, chlorine
Change hydrogen only to be provided by ethylene process production Polyvinyl Chloride System 14.
The production target of polyvinyl chloride resin prepared by above example is as shown in table 3.
The production target of the polyvinyl chloride resin produced by the present invention of table 3
From table 3 it can be seen that using polyvinyl chloride resin made from the Joint Production system of the invention provided, each side index is equal
Meet even better than national sector standard, and be high-class product, illustrate that the Joint Production system of the invention provided and method are suitable
For actual production, and it can ensure that the quality of product is remarkable, with very strong competitiveness.
By taking ethylene process production PVC parts in embodiment 1 as an example, scheme and the energy consumption of domestic existing scheme that the present invention is provided
Comparing result is as shown in table 4.
The energy consumption comparison result of the domestic existing scheme of table 4 and the present invention program
From table 4, it can be seen that by taking ethylene process production PVC parts as an example, the combine production method provided using the present invention, energy
Consumption is far below the process units of country's existing scheme, the scheme of the invention provided the only annual section altogether in ethylene process production PVC parts
25424 tons of coal is about marked, energy-saving effect is obvious.
Shown by above example, the Joint Production system and method for the Corvic that the present invention is provided is prepared
Product quality more preferably, this method compared to conventional method effectively utilize each device accessory substance, mitigate production in explode can
Can, production cost is reduced, and production process is more energy efficient more environmentally friendly, realizes the theory of recycling economy.
It should be noted that the present invention will be described rather than limits the invention for above-described embodiment, and this
Art personnel can design alternative embodiment without departing from the scope of the appended claims.In claim
In, any reference symbol between bracket should not be configured to limitations on claims.Word "comprising" is not excluded for depositing
In element or step not listed in the claims.
Claims (10)
1. the Joint Production system of a kind of Corvic, it is characterised in that it includes chlorine generating means (10), ethene life
Device (13), ethylene process production Polyvinyl Chloride System (14) and acetylene method production Polyvinyl Chloride System (15) are produced, wherein,
The chlorine generating means (10), ethylene producing device (13) produce Polyvinyl Chloride System (14) with the ethylene process respectively
Connection, ethene made from chlorine made from the chlorine generating means (10) and the ethylene producing device (13) is supplied to
The ethylene process production Polyvinyl Chloride System (14), for producing Corvic；
The ethylene process production Polyvinyl Chloride System (14) is connected with acetylene method production Polyvinyl Chloride System (15), by calcium carbide and water
Obtained acetylene and the byproduct hydrogen chloride of ethylene process production Polyvinyl Chloride System (14) are supplied to the acetylene method to give birth to
Polyvinyl Chloride System (15) is produced, for producing Corvic.
2. the Joint Production system of Corvic according to claim 1, it is characterised in that the chlorine generating means
(10) electrolytic chlorination potassium device (11) and electrolytic chlorination magnesium apparatus (12), the electrolytic chlorination potassium device (11) and electrolytic chlorine are included
Change magnesium apparatus (12) to be connected with ethylene process production Polyvinyl Chloride System (14) respectively, be the ethylene process production polyvinyl chloride
Device (14) provides chlorine, and the electrolytic chlorination potassium device (11) also connects with acetylene method production Polyvinyl Chloride System (15)
Connect, hydrogen chloride made from the electrolytic chlorination potassium device (11) is supplied to the acetylene method production Polyvinyl Chloride System (15), uses
In production Corvic.
3. the Joint Production system of Corvic according to claim 2, it is characterised in that the ethylene process production is poly-
In TOWER OUTLET IN VINYL CHLORIDE UNIT (14), chlorine is provided by the electrolytic chlorination potassium device (11), and the electrolytic chlorination potassium device (11) provides
Chlorine it is not enough when the electrolytic chlorination magnesium apparatus (12) a part of chlorine be provided supplemented.
4. the Joint Production system of Corvic according to claim 2, it is characterised in that the acetylene method production is poly-
In TOWER OUTLET IN VINYL CHLORIDE UNIT (15), the accessory substance that hydrogen chloride produces Polyvinyl Chloride System (14) by the ethylene process is provided, the ethene
The electrolytic chlorination potassium device (11) provides a part of chlorination when the hydrogen chloride that method production Polyvinyl Chloride System (14) is provided is not enough
Hydrogen is supplemented.
5. the Joint Production system of Corvic according to claim 1, it is characterised in that the Joint Production system
Also include polypropylene production apparatus (16), the polypropylene production apparatus (16) is connected with the ethylene producing device (13), institute
Accessory substance propylene made from stating ethylene producing device (13) is supplied to the polypropylene production apparatus (16), for producing polypropylene
Resin.
6. the Joint Production system of Corvic according to claim 1, it is characterised in that the ethylene process production is poly-
TOWER OUTLET IN VINYL CHLORIDE UNIT (14) use high/low temperature chlorination combined producing process, chlorine made from the chlorine generating means (10) and
Ethene feeding low temperature direct chlorination reactor (141), high temperature direct chlorination reactor made from the ethylene producing device (13)
(142) be made dichloroethanes, then through high boiling tower (143) is refined, low pressure cracking and polymerisation, Corvic is made.
7. a kind of combine production method of Corvic, it is characterised in that comprise the following steps that：
1) ethene and propylene is made using methanol decomposition catalytic cracking process in ethylene producing device (13)；
2) ethene made from the ethylene producing device (13) and chlorine produce Polyvinyl Chloride System (14) through ethylene process and prepared
Corvic is obtained, chlorine is provided by electrolytic chlorination potassium device (11), the chlorine that the electrolytic chlorination potassium device (11) provides
Electrolytic chlorination magnesium apparatus (12) provides a part of chlorine and supplemented during unsaturated vapor；
3) acetylene made from calcium carbide and water and hydrogen chloride produce Polyvinyl Chloride System (15) through acetylene method and prepare polychlorostyrene second
Olefine resin, the accessory substance that hydrogen chloride produces Polyvinyl Chloride System (14) by ethylene process is provided, and the ethylene process produces polyvinyl chloride
The electrolytic chlorination potassium device (11) provides a part of hydrogen chloride and supplemented when the hydrogen chloride that device (14) is provided is not enough；
4) propylene made from the ethylene producing device (13) prepares acrylic resin through polypropylene production apparatus (16).
8. the combine production method of Corvic according to claim 7, it is characterised in that the ethylene producing device
(13) methanol decomposition catalytic cracking process is used, methanol reacts with catalyst in fluidized-bed reactor, reaction inactivation
Catalyst burns laggard fluidized bed reactor cycles reaction in regenerator, and ethene and propylene is made through drying separating treatment.
9. the combine production method of Corvic according to claim 7, it is characterised in that the acetylene method production is poly-
In TOWER OUTLET IN VINYL CHLORIDE UNIT (15), vinyl chloride is made with the obtained acetylene of water reaction and hydrogen chloride in calcium carbide in the reactor, then through becoming
Temperature becomes press-dehydrating, high low boiling tower rectifying and polymerisation, and Corvic is made.
10. the combine production method of Corvic according to claim 7, it is characterised in that the polypropylene production
Device (16) uses continuous fluidized bed polymerization technique, and the accessory substance propylene from the ethylene producing device (13) enters with hydrogen
Enter vertical gas-phase fluidized-bed reactor (161) the production polypropylene powder resin containing catalyst system, obtained polypropylene powder
Expect that resin enters Squeezinggranulator group (164) generation after recycle gas compressor (162) and recycle gas cooler (163) degassing
Polypropylene granules resin.
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| CN107629158A (en) * | 2017-10-11 | 2018-01-26 | 青海盐湖工业股份有限公司 | A kind of Production of PVC system and chlorine distribution method with chlorine distributor |
| CN107629158B (en) * | 2017-10-11 | 2019-09-13 | 青海盐湖工业股份有限公司 | A kind of Production of PVC system and chlorine distribution method with chlorine distributor |
| CN108047358A (en) * | 2017-12-07 | 2018-05-18 | 青海盐湖工业股份有限公司 | A kind of polyvinyl chloride Joint Production system and its interlocking control method |
| CN108047358B (en) * | 2017-12-07 | 2020-09-15 | 青海盐湖工业股份有限公司 | Polyvinyl chloride joint production system and interlocking control method thereof |
| CN109180417A (en) * | 2018-09-29 | 2019-01-11 | 青海盐湖工业股份有限公司 | A kind of method and system using low-purity chlorine production dichloroethanes EDC |
| CN109456431A (en) * | 2018-10-11 | 2019-03-12 | 青海省矿业集团股份有限公司 | A kind of polyolefin cleaning loop production method and system |
| CN109456431B (en) * | 2018-10-11 | 2021-07-20 | 青海省矿业集团股份有限公司 | Clean closed-loop production method and system for polyolefin |
| CN112807522A (en) * | 2021-03-10 | 2021-05-18 | 山东孟友玻璃科技有限公司 | Flexible needle tube, preparation method thereof and flexible instillation needle |
| CN112807522B (en) * | 2021-03-10 | 2023-05-23 | 山东孟友新材料科技有限责任公司 | Flexible needle tube, preparation method thereof and flexible instillation needle |
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Application publication date: 20170915 Assignee: Qinghai Salt Lake Magnesium Industry Co.,Ltd. Assignor: QINGHAI SALT LAKE INDUSTRY Co.,Ltd. Contract record no.: X2023990000996 Denomination of invention: A joint production system and method for polyvinyl chloride resin Granted publication date: 20200324 License type: Exclusive License Record date: 20240102 |