CN106672902A - Method for producing chemical fertilizers and intermediate chemical products by aid of underground gasification product gas of coal - Google Patents
Method for producing chemical fertilizers and intermediate chemical products by aid of underground gasification product gas of coal Download PDFInfo
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- CN106672902A CN106672902A CN201710027486.1A CN201710027486A CN106672902A CN 106672902 A CN106672902 A CN 106672902A CN 201710027486 A CN201710027486 A CN 201710027486A CN 106672902 A CN106672902 A CN 106672902A
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- Prior art keywords
- gasification
- gas
- synthesis
- ammonia
- product
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- 238000002309 gasification Methods 0.000 title claims abstract description 172
- 239000003245 coal Substances 0.000 title claims abstract description 97
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 96
- 239000003337 fertilizer Substances 0.000 title claims abstract description 47
- 239000013461 intermediate chemical Substances 0.000 title claims abstract description 33
- 239000000126 substance Substances 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 claims abstract description 205
- 239000007789 gas Substances 0.000 claims abstract description 199
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 160
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 claims abstract description 137
- 239000000047 product Substances 0.000 claims abstract description 104
- 230000008569 process Effects 0.000 claims abstract description 88
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 71
- 239000004202 carbamide Substances 0.000 claims abstract description 71
- 229910001868 water Inorganic materials 0.000 claims abstract description 42
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 33
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 30
- 238000001816 cooling Methods 0.000 claims abstract description 30
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 27
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 27
- 239000001301 oxygen Substances 0.000 claims abstract description 27
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 27
- 239000011593 sulfur Substances 0.000 claims abstract description 27
- 239000011280 coal tar Substances 0.000 claims abstract description 10
- 238000000746 purification Methods 0.000 claims abstract description 6
- 238000003786 synthesis reaction Methods 0.000 claims description 151
- 230000015572 biosynthetic process Effects 0.000 claims description 150
- 235000013877 carbamide Nutrition 0.000 claims description 66
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims description 48
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims description 48
- 235000011130 ammonium sulphate Nutrition 0.000 claims description 47
- 239000013505 freshwater Substances 0.000 claims description 42
- PAWQVTBBRAZDMG-UHFFFAOYSA-N 2-(3-bromo-2-fluorophenyl)acetic acid Chemical compound OC(=O)CC1=CC=CC(Br)=C1F PAWQVTBBRAZDMG-UHFFFAOYSA-N 0.000 claims description 38
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 36
- 238000006243 chemical reaction Methods 0.000 claims description 33
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 29
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 28
- 150000001875 compounds Chemical class 0.000 claims description 28
- 239000001117 sulphuric acid Substances 0.000 claims description 24
- 235000011149 sulphuric acid Nutrition 0.000 claims description 24
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 22
- 238000006477 desulfuration reaction Methods 0.000 claims description 21
- 230000023556 desulfurization Effects 0.000 claims description 21
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 20
- 229910017604 nitric acid Inorganic materials 0.000 claims description 20
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical group O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims description 16
- 238000010521 absorption reaction Methods 0.000 claims description 15
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 15
- 238000005406 washing Methods 0.000 claims description 14
- 239000002253 acid Substances 0.000 claims description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims description 11
- 239000001257 hydrogen Substances 0.000 claims description 11
- 229910052757 nitrogen Inorganic materials 0.000 claims description 11
- 238000011084 recovery Methods 0.000 claims description 11
- 239000000243 solution Substances 0.000 claims description 10
- 239000003054 catalyst Substances 0.000 claims description 9
- 238000005262 decarbonization Methods 0.000 claims description 9
- 238000011143 downstream manufacturing Methods 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 9
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 8
- 238000005261 decarburization Methods 0.000 claims description 8
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 7
- 239000012467 final product Substances 0.000 claims description 7
- 239000008187 granular material Substances 0.000 claims description 7
- 239000002367 phosphate rock Substances 0.000 claims description 7
- 238000005201 scrubbing Methods 0.000 claims description 7
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 claims description 6
- ZCCIPPOKBCJFDN-UHFFFAOYSA-N calcium nitrate Chemical compound [Ca+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O ZCCIPPOKBCJFDN-UHFFFAOYSA-N 0.000 claims description 6
- 239000002245 particle Substances 0.000 claims description 6
- JCVAWLVWQDNEGS-UHFFFAOYSA-N 1-(2-hydroxypropylamino)propan-2-ol;thiolane 1,1-dioxide;hydrate Chemical compound O.O=S1(=O)CCCC1.CC(O)CNCC(C)O JCVAWLVWQDNEGS-UHFFFAOYSA-N 0.000 claims description 5
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 5
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 claims description 5
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims description 5
- 239000011777 magnesium Substances 0.000 claims description 5
- 239000012528 membrane Substances 0.000 claims description 5
- 239000011591 potassium Substances 0.000 claims description 5
- 229910052700 potassium Inorganic materials 0.000 claims description 5
- 238000011069 regeneration method Methods 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 5
- UNXRWKVEANCORM-UHFFFAOYSA-N triphosphoric acid Chemical compound OP(O)(=O)OP(O)(=O)OP(O)(O)=O UNXRWKVEANCORM-UHFFFAOYSA-N 0.000 claims description 5
- 239000011701 zinc Substances 0.000 claims description 5
- 229910052725 zinc Inorganic materials 0.000 claims description 5
- 239000004254 Ammonium phosphate Substances 0.000 claims description 4
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 4
- 229910000148 ammonium phosphate Inorganic materials 0.000 claims description 4
- 235000019289 ammonium phosphates Nutrition 0.000 claims description 4
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 claims description 4
- 229910052749 magnesium Inorganic materials 0.000 claims description 4
- 125000005342 perphosphate group Chemical group 0.000 claims description 4
- 239000002002 slurry Substances 0.000 claims description 4
- 238000001179 sorption measurement Methods 0.000 claims description 4
- 239000001226 triphosphate Substances 0.000 claims description 4
- 235000011178 triphosphate Nutrition 0.000 claims description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 3
- NGLMYMJASOJOJY-UHFFFAOYSA-O azanium;calcium;nitrate Chemical compound [NH4+].[Ca].[O-][N+]([O-])=O NGLMYMJASOJOJY-UHFFFAOYSA-O 0.000 claims description 3
- 229910000019 calcium carbonate Inorganic materials 0.000 claims description 3
- 239000011248 coating agent Substances 0.000 claims description 3
- 238000000576 coating method Methods 0.000 claims description 3
- 238000001035 drying Methods 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 3
- 238000005192 partition Methods 0.000 claims description 3
- 238000012216 screening Methods 0.000 claims description 3
- 230000004087 circulation Effects 0.000 claims description 2
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 abstract description 28
- 229910002092 carbon dioxide Inorganic materials 0.000 abstract description 25
- 238000005516 engineering process Methods 0.000 abstract description 16
- 239000006227 byproduct Substances 0.000 abstract description 15
- 230000008901 benefit Effects 0.000 abstract description 13
- 239000001569 carbon dioxide Substances 0.000 abstract description 10
- 230000002194 synthesizing effect Effects 0.000 abstract description 8
- 238000010248 power generation Methods 0.000 abstract description 3
- 206010027336 Menstruation delayed Diseases 0.000 abstract 1
- 230000003009 desulfurizing effect Effects 0.000 abstract 1
- 230000001131 transforming effect Effects 0.000 abstract 1
- 238000002347 injection Methods 0.000 description 12
- 239000007924 injection Substances 0.000 description 12
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 12
- 239000007800 oxidant agent Substances 0.000 description 9
- 230000001590 oxidative effect Effects 0.000 description 9
- 230000008859 change Effects 0.000 description 7
- 230000005611 electricity Effects 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 6
- 239000000203 mixture Substances 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 238000006386 neutralization reaction Methods 0.000 description 5
- 238000007254 oxidation reaction Methods 0.000 description 5
- PNEYBMLMFCGWSK-UHFFFAOYSA-N Alumina Chemical compound [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 4
- 229910019142 PO4 Inorganic materials 0.000 description 4
- 238000005553 drilling Methods 0.000 description 4
- 239000007788 liquid Substances 0.000 description 4
- 239000010802 sludge Substances 0.000 description 4
- 238000011144 upstream manufacturing Methods 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- VFNGKCDDZUSWLR-UHFFFAOYSA-N disulfuric acid Chemical compound OS(=O)(=O)OS(O)(=O)=O VFNGKCDDZUSWLR-UHFFFAOYSA-N 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- 102000004160 Phosphoric Monoester Hydrolases Human genes 0.000 description 2
- 108090000608 Phosphoric Monoester Hydrolases Proteins 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000003111 delayed effect Effects 0.000 description 2
- 238000001704 evaporation Methods 0.000 description 2
- 230000008020 evaporation Effects 0.000 description 2
- 238000005755 formation reaction Methods 0.000 description 2
- 238000005469 granulation Methods 0.000 description 2
- 230000003179 granulation Effects 0.000 description 2
- 230000036571 hydration Effects 0.000 description 2
- 238000006703 hydration reaction Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000005457 optimization Methods 0.000 description 2
- 238000000197 pyrolysis Methods 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 238000007711 solidification Methods 0.000 description 2
- 230000008023 solidification Effects 0.000 description 2
- 238000010025 steaming Methods 0.000 description 2
- 238000002560 therapeutic procedure Methods 0.000 description 2
- 210000002700 urine Anatomy 0.000 description 2
- 238000009623 Bosch process Methods 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- OPKOKAMJFNKNAS-UHFFFAOYSA-N N-methylethanolamine Chemical compound CNCCO OPKOKAMJFNKNAS-UHFFFAOYSA-N 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 229910001260 Pt alloy Inorganic materials 0.000 description 1
- 229910000629 Rh alloy Inorganic materials 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 241001148470 aerobic bacillus Species 0.000 description 1
- 238000004176 ammonification Methods 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 238000011953 bioanalysis Methods 0.000 description 1
- 230000017531 blood circulation Effects 0.000 description 1
- 239000012267 brine Substances 0.000 description 1
- 239000011575 calcium Substances 0.000 description 1
- DIOLOCSXUMYFJN-UHFFFAOYSA-N calcium;azane Chemical group N.[Ca+2] DIOLOCSXUMYFJN-UHFFFAOYSA-N 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 229910052593 corundum Inorganic materials 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000001351 cycling effect Effects 0.000 description 1
- 230000000994 depressogenic effect Effects 0.000 description 1
- 150000004683 dihydrates Chemical class 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
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 206010016256 fatigue Diseases 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- SZVJSHCCFOBDDC-UHFFFAOYSA-N iron(II,III) oxide Inorganic materials O=[Fe]O[Fe]O[Fe]=O SZVJSHCCFOBDDC-UHFFFAOYSA-N 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000004579 marble Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 238000010297 mechanical methods and process Methods 0.000 description 1
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 229910000069 nitrogen hydride Inorganic materials 0.000 description 1
- 229910052756 noble gas Inorganic materials 0.000 description 1
- 150000002835 noble gases Chemical class 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 239000010909 process residue Substances 0.000 description 1
- 208000018299 prostration Diseases 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000010189 synthetic method Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- QORWJWZARLRLPR-UHFFFAOYSA-H tricalcium bis(phosphate) Chemical compound [Ca+2].[Ca+2].[Ca+2].[O-]P([O-])([O-])=O.[O-]P([O-])([O-])=O QORWJWZARLRLPR-UHFFFAOYSA-H 0.000 description 1
- 229910000391 tricalcium phosphate Inorganic materials 0.000 description 1
- 229940048102 triphosphoric acid Drugs 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 229910001845 yogo sapphire Inorganic materials 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
- C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C1/00—Ammonia; Compounds thereof
- C01C1/02—Preparation, purification or separation of ammonia
- C01C1/04—Preparation of ammonia by synthesis in the gas phase
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05C—NITROGENOUS FERTILISERS
- C05C9/00—Fertilisers containing urea or urea compounds
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C273/00—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups
- C07C273/02—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds
- C07C273/04—Preparation of urea or its derivatives, i.e. compounds containing any of the groups, the nitrogen atoms not being part of nitro or nitroso groups of urea, its salts, complexes or addition compounds from carbon dioxide and ammonia
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0415—Purification by absorption in liquids
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0435—Catalytic purification
- C01B2203/044—Selective oxidation of carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
- C01B2203/0435—Catalytic purification
- C01B2203/0445—Selective methanation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Analytical Chemistry (AREA)
- Treating Waste Gases (AREA)
- Fertilizers (AREA)
Abstract
The invention provides a method for producing chemical fertilizers and intermediate chemical products by the aid of underground gasification product gas of coal. One of schemes includes that gasification modes for crude synthetic gas which is generated on the basis of a plurality of ISC underground gasification furnaces by means of gasification and has an appropriate economic scale include air gasification modes or oxygen-rich gasification modes. The method includes steps of (1), pretreating the crude synthetic gas; (2), desulfurizing dry synthetic gas; (3), transforming and cooling the dry synthetic gas; (4), decarburizing the dry synthetic gas; (5), carrying out methanation and purification; (6), synthesizing ammonia; (7), synthesizing urea. The method has the advantages that technological processes for comprehensively utilizing the synthetic gas on downstream are provided for the underground gasification product gas of the coal besides power generation, byproducts (such as sulfur, carbon dioxide, technological water and coal tar) in underground gasification technologies for the coal are sufficiently utilized by the aid of technological processes for producing the chemical fertilizers and the intermediate chemical products from the integral synthetic gas, accordingly, the processing treatment and discharge costs in late periods can be reduced, and sales revenue of project products further can be increased.
Description
Technical field
The invention provides a kind of using underground coal gasification(UCG) product gas production chemical fertilizer, intermediate chemical product and tail gas
The technological process method of generating, belongs to the downstream comprehensive utilization process technical field of underground coal gasification(UCG).
Background technology
Underground coal gasification(UCG)（ISC）Be one by oxidant, the burning and gasification reaction by subterranean coal is straight coal
Switch through the process for turning to product gas.Product gas are commonly known as synthesis gas, can be used as fuel production, Chemical Manufacture, generating etc.
The raw material of downstream process.The technical process set shaft building completion, underground coal mining and coal gasification process technology, with safety
Well, the advantages of investing little, high efficiency, pollution less.
Coal gasification process is the process that coal is changed into synthesis gas by a series of chemical reaction.It is wherein main
Reaction includes：
C+H20 → H2+CO（Steam gasification reacts）
CO+H20 ↔ H2+CO2（Water gas shift reaction）
CO+3H2↔ CH4+H20 （Methanation reaction）
C+2H2 → CH4（Hydrogen gasification reaction）
C+½O2→ CO （Partial oxidation reaction）
C+O2 → CO2（Complete oxidation）
C+CO2→ 2CO（Carbon dioxide gasification reacts）
One drilling well for being used for oxidant injection is referred to as " injection well ", and another drilling well for being used to produce product gas is referred to as " producing
Product well ".Directed drilling and vertical drilling all can be used as injection well or product wells.Underground coal gasification(UCG)（ISC）May be in injection well
Also need to use the peupendicular hole of one or more and product well between（For example：Functional well and service well）.
When having injection well, product well and horizontal channel to couple together the two in coal seam, this construction is referred to as a coal
Charcoal underground gasification（ISC）Unit or well pair.ISC units include combustion zone, gasification zone and pyrolysis zone.Wherein, combustion zone is in coal seam
Near middle oxidant decanting point；Gasification zone is centered around around combustion zone or in combustion zone downstream with radial form, and coal exists
Gasification zone is gasified, part is oxidized, so as to generate product gas；Pyrolysis zone typically exists in gasification zone downstream, the pyrolytic reaction of coal
Here occur.The product gas of high temperature are finally transported to ground from gasification zone toward downstream flow from product well well head.In coal combustion
Or while gasification, it is big that the ISC burned out area in coal seam can grow change.
The product gas generated by underground coal gasification(UCG)（Crude synthesis gas）Usually contain synthesis gas（CO、CO2、H2、CH4And its
The mixture of his gas）And other compositions（Solid particle, water, coal tar, hydrocarbon vapours, other microcomponents include H2S、
NH4, COS etc.）.Its complicated component degree depends on many aspects：The oxidant that underground coal gasification(UCG) is used（Air or other
Oxidant, such as oxygen, oxygen-enriched air or vapour mixture）, inherent water in coal seam or surrounding formations penetrate in coal seam water,
The operating parameter of ature of coal and coal underground gasifying technology, including temperature, pressure etc..
According to existing patent documentation, the comprehensive utilization of current underground coal gasification(UCG) product gas is still faced with many difficult problems,
It is specific as follows：
A) in addition to synthesis gas is directly used in generating, heavy industrialization project implementation and operation are lacked.
B) all kinds of side-products of underground coal gasification(UCG) production, such as hydrogen sulfide/sulfur, fresh water (FW), carbon dioxide, coal tar
These side-products are reduced or remove Deng industrialization method of comprehensive utilization or technique without clear and definite and maturation.
C) the downstream syngas production chemical fertilizer for coal underground gasifying technology and the technological process side of chemical products are lacked
Case.
D) air gasification in coal underground gasifying technology, three kinds of different process of oxygen-rich gasification and pure oxygen gasification are produced
The difference of synthesis gas product quality is larger, directly affects the processing condition and method of chemical fertilizer downstream and chemical products, it is impossible to without exception
In.
The content of the invention
It is an object of the invention to solve the deficiencies in the prior art, there is provided using underground coal gasification(UCG) product gas productionization
The method of fertilizer and its intermediate chemical product.Specifically, methods described is included using the air gas in coal underground gasifying technology
The technique of change, the synthesis gas production chemical fertilizer of three kinds of different process of oxygen-rich gasification and pure oxygen gasification and its intermediate chemical product
Flow process, realizes optimization and improves the purpose of underground coal gasification(UCG) product gas comprehensive utilization process.
The technical solution adopted for the present invention to solve the technical problems is：
The method for producing chemical fertilizer and intermediate chemical product using underground coal gasification(UCG) product gas, based on multiple ISC underground gasifications
The crude synthesis gas for possessing appropriate economic scale that stove is produced by gasification, gasification mode is air gasification or oxygen-rich gasification, described
Method comprises the steps：
（1）Crude synthesis gas pretreatment：Crude synthesis gas Jing cooling, washing and separative element obtain 60 DEG C of temperature ＜ dry synthesis gas with
And coal tar and fresh water (FW)；
（2）Dry synthetic gas desulfurization：By Claus method, chemiadsorption or shell Sulfinol acid gas absorption method to dry synthesis gas
Carry out desulfurization process；Afterwards loss of essence sulphuring treatment is carried out using ZnO particle or renewable ZnO and zinc titanate granule, the sulfur of removing is returned
Receive；
（3）Dry synthesis gas conversion and cooling：Dry synthesis gas after desulfurization is heated to 260 DEG C in preheating device, is delivered to isothermal
WGS unit, CO is converted into using steam by contained CO2And H2；
（4）Dry synthesis gas decarbonization：Step（3）After dry synthesis air cooling after process, decarburization unit is delivered to, by CO2Removing is simultaneously
Reclaim, for urea synthesis, decarbonization process used include chemiadsorption, physisorphtion, absorption bed process, absorption regeneration method,
Low temperature processing or membrane separation process；
（5）Methanation and purification, through step（4）The synthesis gas of process only contains CH4, N2、H2With CO that may be present and CO2,
In methanation unit, by nickel-base catalyst further will likely be remaining CO and CO2Removing, methane passes through purification unit
Remove, in final synthesis gas N is comprised only2And H2；
（6）Synthesis ammonia；Step（5）Synthesis gas after process is delivered to synthesis ammonia unit after synthesic gas compressor supercharging,
Under high pressure, H2And N2Reaction generates ammonia, and generates ammonia after scrubbing tower is separated from unreacted gas and cooled down；
（7）Urea synthesis：From step（6）Ammonia and step are extracted in ammonia（4）The CO of recovery2Urea synthesis are delivered to together
Unit, produces final product carbamide.
Another implementation, using underground coal gasification(UCG) product gas the side of chemical fertilizer and intermediate chemical product is produced
Method, it is characterised in that：Based on the crude synthesis gas for possessing appropriate economic scale that multiple ISC underground gasification furnaces are produced by gasification,
Gasification mode is pure oxygen gasification, and the gasification mode injects oxygen by air-separating plant to underground gasification furnace carries out purity oxygen
Change, the air-separating plant produces nitrogen simultaneously, be fed directly to synthesize ammonia unit, methods described bag by booster compressor
Include following steps：
（1）Crude synthesis gas pretreatment：Crude synthesis gas Jing cooling, washing and separative element obtain 60 DEG C of temperature ＜ dry synthesis gas with
And coal tar and fresh water (FW)；
（2）Dry synthetic gas desulfurization：By Claus method, chemiadsorption or shell Sulfinol acid gas absorption method to dry synthesis gas
Carry out desulfurization process；Afterwards loss of essence sulphuring treatment is carried out using ZnO particle or renewable ZnO and zinc titanate granule, the sulfur of removing is returned
Receive；
（3）Dry synthesis gas conversion and cooling：Dry synthesis gas after desulfurization is heated to 260 DEG C in preheating device, is delivered to isothermal
WGS unit, CO is converted into using steam by contained CO2And H2；
（4）Dry synthesis gas decarbonization：Step（3）After dry synthesis air cooling after process, decarburization unit is delivered to, by CO2Removing is simultaneously
Reclaim, for urea synthesis, decarbonization process used includes chemisorbed, physical absorption, adsorbent bed, absorption regeneration method, low temperature point
From method or film analysis method；
（5）Dry synthesis gas pressure-variable adsorption：Dry synthesis gas passes through psa unit by H2Selectively, it is efficiently separating, from
And obtain purity>96% hydrogen；
（6）Synthesis ammonia；Step（5）The hydrogen of acquisition is delivered to synthesis ammonia unit, under high pressure, H Jing after compressor supercharging2And N2
Reaction generates ammonia, and generates ammonia after scrubbing tower is separated from unreacted gas and cooled down；
（7）Urea synthesis：From step（6）Ammonia and step are extracted in ammonia（4）The CO of recovery2Urea synthesis are delivered to together
Unit, produces final product carbamide；
Step（6）Middle N2:H2Mol ratio is controlled to 0.33 by adjusting the nitrogen that air-separating plant is generated.
Preferably, methods described also includes：
Step（2a）The sulfur of recovery obtains sulphuric acid through reaction；
Step（7a）Synthesis ammonium sulfate, by step（6）The ammonia and step of production（2a）The sulphuric acid for obtaining sends into ammonium sulfate synthesis
Unit, synthetic product ammonium sulfate.
Preferably, methods described also includes：
Step（2a）The sulfur of recovery obtains sulphuric acid through reaction；
Step（6a）Nitric acid synthesis, step（6）The ammonia of generation, Jing absorbs and generates nitric acid after being oxidized；
Step（7a）Synthesis ammonium sulfate, by step（6）The ammonia and step of production（2a）The sulphuric acid for obtaining sends into ammonium sulfate synthesis
Unit, synthetic product ammonium sulfate；
Step（7b）Nitric acid synthesis ammonium, by step（6）The ammonia and step of production（6a）The nitric acid for obtaining sends into ammonium nitrate synthesis
Unit, synthetic product ammonium nitrate.
Preferably, methods described also includes：
Step 7（c）, synthesize phosphoric acid, with phosphate rock as raw material, its triphosphate for containing and step（2a）Concentrated sulphuric acid it is anti-
Phosphoric acid and calcium sulfate should be generated.
Preferably, methods described also includes：
Step 7（d）, synthesize NPK compound fertilizers, with phosphate rock as raw material, its triphosphate for containing and step（6a）Nitre
Acid reaction generates phosphoric acid and calcium nitrate solution, and phosphoric acid, sulphuric acid and ammonium nitrate are mixed with previous solu, is neutralized using ammonia, in
With after the completion of, ammonium sulfate, the compound containing potassium and magnesium, ammonium phosphate, perphosphate are added, finally slurry is delivered to into pelletize work
Skill, Jing pelletizes, drying, screening, crushing, cooling and coating obtain NPK compound fertilizers.
Preferably, by step（7b）The ammonium nitrate of synthesis mixes with Calcium Carbonate, obtains calcium ammonium nitrate.
Preferably, by step（7b）The ammonium nitrate of synthesis and proper proportion step（7）The carbamide mixing of acquisition, acquisition urea-
Ammonium nitrate.
Preferably, step（1）Fresh water (FW) be delivered to technique unit for treating water and processed, the technique water circulation of process is again
It is used in ISC underground gasification furnaces, crude synthesis gas cooling, washing and separative element and other downstream processes.
The invention has the beneficial effects as follows：The Technology flow process that the present invention is provided solves technical problem in detail below and chooses
War, including：The synthesis gas downstream comprehensive utilization process stream in addition to generating is provided for underground coal gasification(UCG) product gas
Journey, while including the additional aspects produced as chemical fertilizer and its intermediate chemicals using emission power generation；Whole synthesis gas productionization
The technological process of fertilizer and its intermediate chemicals, makes full use of the side-product in coal underground gasifying technology（Such as sulfur, titanium dioxide
Carbon, fresh water (FW), coal tar etc.）.The cost that post-production is processed and discharged is not only reduced, Project Product sale is also add and is received
Enter.
Description of the drawings
In order to more clearly describe the Technology flow process of the present invention, the accompanying drawing to be used needed for specific embodiment is retouched
State as follows.It should be evident that drawings in the following description are only some embodiments of the present invention, for the common skill in this area
For art personnel, on the premise of not paying creative work, can be with according to these other accompanying drawings of accompanying drawings acquisition.
Fig. 1 is the square technique stream of underground coal gasification(UCG) air gasification product gas production carbamide and intermediate chemicals ammonia
Cheng Tu；
Fig. 2 is the square technological process of underground coal gasification(UCG) oxygen-rich gasification product gas production carbamide and intermediate chemicals ammonia
Figure；
Fig. 3 is the square technological process of underground coal gasification(UCG) pure oxygen gasification product gas production carbamide and intermediate chemicals ammonia
Figure；
Fig. 4 is the square process chart of underground coal gasification(UCG) air gasification product gas production carbamide and ammonium sulfate；
Fig. 5 is the square process chart of underground coal gasification(UCG) oxygen-rich gasification product gas production carbamide and ammonium sulfate；
Fig. 6 is the square process chart of underground coal gasification(UCG) pure oxygen gasification product gas production carbamide and ammonium sulfate；
Fig. 7 is the square of underground coal gasification(UCG) air gasification product gas production carbamide, ammonium sulfate, ammonium nitrate and NPK compound fertilizers
Process chart；
Fig. 8 is the square of underground coal gasification(UCG) oxygen-rich gasification product gas production carbamide, ammonium sulfate, ammonium nitrate and NPK compound fertilizers
Process chart；
Fig. 9 is the square of underground coal gasification(UCG) pure oxygen gasification product gas production carbamide, ammonium sulfate, ammonium nitrate and NPK compound fertilizers
Process chart；
In the drawings, identical reference refers to same parts.Specifically, the reference implication being related in each accompanying drawing is such as
Under：
1st, air compressor；2nd, air；3rd, ISC underground gasification furnaces；4th, crude synthesis gas；5th, crude synthesis gas cooling, washing and separation
Unit；6th, dry synthesis gas；7th, coal tar；8th, fresh water (FW)；9th, technique unit for treating water；10th, the fresh water (FW) for processing；11st, Waste
Material；12nd, dry synthetic gas desulfurization unit；13rd, the sulfur for reclaiming；14th, dry synthesis gas conversion and cooling unit；15th, synthesis QI prostration is done
Carbon unit；16th, the carbon dioxide of removing（For downstream urea production）；17th, methanation and purifier units（For removing dry synthesis
Methane in gas）；18th, methane-rich gas（For selling or generating electricity）；19th, remaining ingredient hydrogen and nitrogen（For synthesizing ammonia）；
20th, ammonia unit is synthesized；21st, ammonia；22nd, urea synthesis unit；23rd, carbamide；24th, it is equipped with the air-separating plant of nitrogen recycling
（ASU）；25th, oxygen；26th, nitrogen（Synthesize ammonia for downstream）；27th, gasification unit for treating water；28th, the technique of after-treatment
Water；29th, psa unit（PSA）（For the hydrogen in separating synthetic gas）；30th, the methane-rich gas after pressure-variable adsorption（With
In sale or generating）；31st, the detached hydrogen of pressure-variable adsorption（For synthesizing ammonia）；32nd, gas washing in SA production unit；33rd, sulphuric acid（For
Ammonium sulfate production）；34th, ammonium sulfate production unit；35th, ammonium sulfate；36th, nitric acid production unit；37th, nitric acid（For ammonium nitrate and
NPK compound fertilizers are produced）；38th, ammonium nitrate production unit；39th, ammonium nitrate（For sale or the production of NPK compound fertilizers）；40th, phosphorus
Sour production unit；41st, phosphate rock（For phosphoric acid production）；42nd, phosphoric acid（For the production of NPK compound fertilizers）；43rd, potassium（K）, magnesium
（Mg）, ammonium phosphate, perphosphate（For the production of NPK compound fertilizers）；44th, NPK acidolysis mixedization production unit；45th, NPK compound fertilizer
Material（Nitrate, phosphate and potassium）.
Specific embodiment
Below in conjunction with the accompanying drawings, technical scheme is made further explanation.
Fig. 1 is the square technique stream of underground coal gasification(UCG) air gasification product gas production carbamide and intermediate chemicals ammonia
Cheng Tu.Underground coal gasification(UCG) air gasification technique needs an air compressor 1 to produce high-pressure oxidation agent, air 2（Containing about
21mole% oxygen）.Air 2 injects ISC underground gasification furnaces 3 to realize the air gasification of subterranean coal by injection well.In air
Nitrogen（About 78mole%）Underground coal gasification(UCG) reaction is not involved in as noble gases, directly by after ISC underground gasification furnaces 3
It is present in synthesis gas product.After downstream syngas handling process, with remaining hydrogen 19 in synthesis gas, common entrance is closed
Ammonification unit 20 produces ammonia 21.Crude synthesis gas 4 are delivered to ground by product well, and into crude synthesis gas cooling, washing and
Separative element 5.Crude synthesis gas 4 are by direct cooling technique（Liquid or gas cooling, Venturi, cooling tower etc.）Or indirectly
Cooling technique（Blade fan, heat exchanger etc.）It is quickly cooled to<80oC.Directly cooling technique contains crude synthesis gas washing
Step, and indirectly cooling technique then needs at least one scrubbing tower by the trace contaminant in crude synthesis gas（Such as chloride, hydrargyrum
Deng）Remove from crude synthesis gas.Synthesis gas after washing removes the freedom remained in synthesis gas subsequently into gas-liquid separator
Liquid, generates temperature<60oThe dry synthesis gas 6 of C.
From the coal tar 7 and fresh water (FW) 8 isolated from scrubbing tower and gas-liquid separator is carried out further into downstream process
Reason.Wherein, fresh water (FW) 8 is delivered to technique unit for treating water 9.By Mechanical Method（Gravitational settling, oil skimmer, filtration, reverse osmosiss）、
Chemical method（Such as coagulating agent, antisludging agent, corrosion inhibiter, pH nertralizers）And bioanalysises（Aerobic bacteria, anaerobic bacteria, activated sludge
Method, cyclic activated sludge process, the fixed film activity sludge of integration, membrane bioreactor etc.）Processed.The fresh water (FW) of process
10 can be with cycling and reutilization in the cooling of ISC underground gasification furnaces 3, crude synthesis gas, washing and separative element 5 and other downstream processes
（For example synthesize ammonia unit 20）.The process residue 11 of generation, including solid waste, sludge and strong brine, need by rubbish
Landfill, burning or third party's facility carry out specialty extraction and are processed.
Dry synthesis gas 6 enters desulfurization unit 12, by Claus method, chemiadsorption（MERICHEM LO-CAT techniques）、
Shell Sulfinol acid gas absorption method etc. carries out desulfurization process to dry synthesis gas.Afterwards, using ZnO particle or renewable ZnO and
Zinc titanate granule carries out loss of essence sulphuring treatment（ZnO(s)+H2S(g) → ZnS(s)+H2O(l)）, it is to avoid the residual sulfur in synthesis gas
Downstream is caused to synthesize the catalyst of ammonia 20（Fe-series catalyst）Poisoning.The sulfur for being removed by desulfurization unit 12 and being reclaimed is simple substance sulphur
13, direct marketing or can further be processed using upstream device.
The main component of the dry synthesis gas after desulfurization is CO2、CH4、H2, CO and N2.By other upstreams or downstream units
Dry synthesis gas is preheated to 260 DEG C by waste heat recovery using tail gas 18 as fuel gas in preheating device.It is then sent to
Warm WGS unit 14, CO is converted into using steam by CO2And H2。
After dry synthesis air cooling, decarburization unit 15 is delivered to, the carbon dioxide 16 is removed and reclaimed, for synthesizing urine
Element 22.The decarbonization process for being adopted includes chemiadsorption（Methylethanolamine, Benfield etc.）, physisorphtion（Low-temp methanol
Wash, SELEXOL techniques）, absorption bed process（Aluminium oxide, zeolite, activated carbon）, absorption regeneration method（Transformation, alternating temperature, washing）, low temperature
Partition method or membrane separation process.According to practical operation situation, selection is wherein most easily integrated, the method with Optimum Economic benefit.Institute
The layout for stating technological process can be to be required to be adjusted according to actual items, for example, be placed in WGS unit 14 de-
The upstream of sulfur unit 12, and desulfurization unit 12 and decarburization unit 15 are integrated into into an acid gas removal unit, shared some processes set
It is standby.
CH is comprised only through the synthesis gas of above-mentioned process4, N2And H2.In methanation unit 17, by nickel-base catalyst
By the remaining CO that synthetic ammonia catalyst can be caused to be poisoned and CO2Removing（CO(g) + 3H2(g) ↔ CH4(g) + H2O (l), CO2
(g) + 4H2(g) ↔ CH4(g) + 2H2O(l)）.The water that reaction is generated will be recovered and be delivered to technique unit for treating water 9,
Methane 18 will be removed by purification unit, and in final synthesis gas 19 N is comprised only2And H2.Methane-rich gas 18, can directly make
Enter for fuel gas sale or by the firepower/steam boiler capable of burning mixture of reciprocable generator, gas turbine or outfit steam turbine power generation
Row generates electricity.
Detached synthesis gas 19, is delivered to synthesis ammonia unit 20 after synthesic gas compressor is pressurized.In the unit, H2With
N2Under high pressure reaction generates ammonia 21, and generates ammonia after scrubbing tower is separated from unreacted gas and cooled down, described
Ammonia can be extracted at downstream process from ammonia.Ammonia synthesis process is based on Ha Bai-Bosch process（Haber-Bosch）, example
Such as woods moral ammonia synthesis process（LAC）, Switzerland's Casale techniques（HEC）Or other are commercially combined to ammonia technology.3H2(g) + N2(g)
↔ 2NH3(g)（Ammonia synthesis reaction, Fe3O4As catalyst, Al2O3, K2O and CaO are used as promoter）
Water needed for ammonia synthesis process is supplied the fresh water (FW) 10 of process by technique unit for treating water 9.The ammonia synthesis process leads to
Often include reclaiming unreacted gas and looping back charging aperture being reacted again, so as to realize high conversion.The ammonia produced
Gas 21 and the carbon dioxide 16 for reclaiming, are delivered to urea synthesis unit 22, produce final product carbamide 23.The urea synthesis
Reaction is as follows：
2NH3(g) + CO2(g) ↔ NH2COONH4 ↔ CO(NH2)2(s) + H2O(l)（Urea synthesis react）
In above-mentioned technical proposal, the technological process for producing carbamide using underground coal gasification(UCG) air gasification product gas has following
Advantage：
The technique only needs to the oxidant needed for providing by air compressor, therefore required capital input is minimum；
Take full advantage of the raw material of the side-product carbon dioxide as urea synthesis of underground coal gasification(UCG)；Consume the coal ground therapeutic method to keep the adverse QI flowing downwards
Fresh water (FW) produced by chemical industry skill, and shared the cost of investment of technique water processing establishment；
Methane-rich gas produced by the technique can be used to generate electricity or as fuel gas sale.
Meanwhile, in above-mentioned technical proposal, using underground coal gasification(UCG) air gasification product gas the technological process of carbamide is produced
There is following shortcoming：
N due to being air gasification, in product gas2Content is higher, far beyond H2Content.Normal conditions, close after desulfurization process
The N in gas2With H2Molar ratio be 1.4-1.8.
For the N in the unstripped gas for synthesizing ammonia2：H2Ratio is uncontrollable, thus may cause the conversion ratio of ammonia synthesis reaction
It is relatively low with production efficiency, especially large-scale production project.
After Water gas shift/WGS, decarburization and methanation are processed, N in synthesis gas2：H2Molar ratio be 1.7-2.4, and
Preferably stoichiometric proportion is 0.33.
In addition, the technique does not use side-product sulfur（What sulfur recovery was obtained）.The technological deficiency will be in following technologies
Solve one by one in the technical scheme of optimization.
Fig. 2 is the square technique of underground coal gasification(UCG) oxygen-rich gasification product gas production carbamide and intermediate chemicals ammonia
Flow chart.The technique is by air compressor 1 and air-separating plant（ASU）24 adjust O in oxidant2And N2Ratio, to
ISC underground gasification furnaces 3 inject oxygen-enriched air（O2Content 50%-80%）Carry out oxygen-rich gasification.The technique can adjust synthesis ammonia list
N needed for the unstripped gas of unit 202:H2Molar ratio so as to reach preferable stoichiometric proportion 0.33.At other synthesis gas
The technique that science and engineering skill produces carbamide with underground coal gasification(UCG) air gasification product gas（Fig. 1）It is essentially identical.Difference is oxygen-enriched work
Skill uses air-separating plant and gasification unit for treating water.Air-separating plant can produce side-product N2 26, for item
Mesh communal facility.The gasification water needs to reinject ISC underground gasification furnaces 3 after special handling, including filter, it is soft
Change or reverse osmosiss, addition anti-corrosion inhibitor are to ensure the integrity of injection well and other underground equipments in its service life.
Gasification is used in unit for treating water 27, including water injection equipment provides under operating pressure required discharge to meet.
The technological process of the utilization underground coal gasification(UCG) oxygen-rich gasification product gas production carbamide of Fig. 2 has following advantage：
For synthesizing the synthesis gas N of ammonia unit2:H2Molar ratio can control preferable stoichiometric proportion 0.33；
Take full advantage of the raw material of the side-product carbon dioxide as urea synthesis of underground coal gasification(UCG)；
The fresh water (FW) produced by coal underground gasifying technology is consumed, and has shared the cost of investment of technique water processing establishment；
Methane-rich gas produced by the technique can be used to generate electricity or as fuel gas sale；The technique needs air-separating plant
（ASU）, gasification unit for treating water and continuous oil pipe device, therefore required capital input is of a relatively high.
By the raw material components of control injection synthesis ammonia unit, can effectively reduce the size of synthesis ammonia unit, therefore phase
To counteracting the great number capital input produced by upstream equipment.
Meanwhile, the technique possesses higher conversion and production efficiency, effectively increases income from sales；Air-separating plant
（ASU）Can be shared by ISC underground gasification furnace groups with the expense of gasification unit for treating water.
But the technological process of the utilization underground coal gasification(UCG) oxygen-rich gasification product gas production carbamide of Fig. 2 still has following lacking
Point：The technique adjusts the unstripped gas of Ammonia Production by the oxygen content of the oxidant of control injection ISC underground gasification furnaces
Composition.Due to the burned out area volume and residence time of ISC underground gasification furnaces itself, the unstripped gas of Ammonia Production is caused into sub-control
System is of virtually longer delayed/response time, in addition, the technique does not use side-product sulfur.
Fig. 3 is the square technique stream of underground coal gasification(UCG) pure oxygen gasification product gas production carbamide and intermediate chemicals ammonia
Cheng Tu.The technique passes through completely air-separating plant（ASU）The injection oxygen 25 of 24 to ISC underground gasification furnace 3 carries out pure oxygen gasification.
The described air-separating plant can also produce nitrogen 26 simultaneously, and be fed directly to synthesize ammonia unit by a booster compressor
20.Now, the N in syngas for synthetic ammonia2:H2Molar ratio can in time carry out dynamic regulation and control by control system.By
It is very high in the oxygen purity 25 of injection（>92%）, therefore after desulfurization 12, conversion and cooling down 14 and the process of decarburization 15, do and close
Into the N in gas2Content is few.Other synthesis gas handling process produce carbamide with underground coal gasification(UCG) air gasification product gas
Technique（Fig. 1）It is essentially identical.In the underground coal gasification(UCG) pure oxygen gasification product gas production urea technique flow process, dry synthesis gas is again
By a psa unit（PSA）29 by H2Selectively, it is efficiently separating, so as to obtain purity>96% hydrogen
31.The hydrogen 31 is delivered in the feed compressor of synthesis ammonia unit 20, wherein N2:H2Molar ratio can be separated by air
Effectively preferable stoichiometric proportion 0.33 is arrived in control to the nitrogen 26 that device 24 is generated.Psa unit（PSA）29 discharges
Can be used for generating electricity rich in Methane offgas or sell as fuel gas.The underground coal gasification(UCG) pure oxygen gasification product gas production urine
In plain technological process, air compressor is only driven, is debugged and misoperation（Downstream units are interrupted）When use, and air compress
Machine is that have ISC underground gasification furnaces group to share, therefore air compressor is not contained in the normal operational process of the technique.
The technological process of the utilization underground coal gasification(UCG) pure oxygen gasification product gas production carbamide of Fig. 3 has following advantage：
For synthesizing the synthesis gas N of ammonia unit2:H2Molar ratio can with molar ratio by control system dynamic control to preferably
Stoichiometric proportion 0.33, and delayed/response time is extremely short；
High conversion ratio and production efficiency can reduce the long-term running cost of project；Nitrogen content is few in synthesis gas, single
Active component in gasification furnace product gas is high.
For identical scale carbamide and ammonia produce, the technique can efficiently reduce ISC underground gasification furnaces quantity and
The size of downstream units needed for reducing；
Take full advantage of the raw material of the side-product carbon dioxide as urea synthesis of underground coal gasification(UCG)；Consume the coal ground therapeutic method to keep the adverse QI flowing downwards
Fresh water (FW) produced by chemical industry skill, and shared the cost of investment of technique water processing establishment；
Methane-rich gas produced by the technique can be used to generate electricity or as fuel gas sale；The expense of gasification unit for treating water
Can be shared by ISC underground gasification furnace groups.
The technological process of the utilization underground coal gasification(UCG) pure oxygen gasification product gas production carbamide of Fig. 3 has following shortcoming：
For technique compared to underground coal gasification(UCG) air and oxygen-rich gasification product gas production carbamide, the large-scale air point of the technique
Higher from the capital input needed for device, the technique does not use side-product sulfur.
Fig. 4 is using underground coal gasification(UCG) air gasification product gas production carbamide, ammonium sulfate and intermediate chemicals sulfur
The square process chart of acid.The technique produces the technique base of carbamide in the product gas of underground coal gasification(UCG) air gasification shown in Fig. 1
Increase gas washing in SA production unit 32 on plinth.The sulfur 13 reclaimed by desulfurization unit 12 produces sulphuric acid 33.Its key step includes：Sulfur
Sulphur burning/oxidation reaction prepares SO2And SO2Catalysis oxidation prepares SO3（S(s) + O2(g) → SO2(g)；2SO2(g) +
O2(g) ↔ 2SO3(g)（V2O5As catalyst））.Sulphur trioxide conversion is many for the method for sulphuric acid, it is the most frequently used to connect
Tactile method and wet sulfuric acid process.Contact method, sulfur trioxide firstly generates oleum（H2S2O7）, then it is diluted to concentrated sulphuric acid（SO3(g) +
H2SO4(l) → H2S2O7(l)；H2S2O7(l) + H2O(l) → H2SO4(l) ）.Wet sulfuric acid process, sulfur trioxide first with steaming
Soda pop symphysis is into gas sulphuric acid, then is condensed into fluid sulphuric acid（SO3(g) + H2O(g) → H2SO4(g)；H2SO4(g) →
H2SO4(l)）.Water needed for sulfuric acid production process is provided by technique unit for treating water 9.Sulphuric acid 33 is delivered to ammonium sulfate production unit
34 produce ammonium sulfate product 35 with the reaction of ammonia 21 of the production of synthesis ammonia unit 20（2NH3(g) + H2SO4(l) → (NH4)2SO4(aq,s)）.
Fig. 5 is using underground coal gasification(UCG) oxygen-rich gasification product gas production carbamide, ammonium sulfate and intermediate chemicals sulfur
The square process chart of acid.Fig. 6 is underground coal gasification(UCG) pure oxygen gasification product gas production carbamide, ammonium sulfate and intermediate
The square process chart of product sulphuric acid.The sulphuric acid and ammonium sulfate production technique of Fig. 5 and Fig. 6 is essentially identical with technique described in Fig. 4.
Difference is the equipment size matching of downstream process.The amount of intermediate chemicals ammonia need to simultaneously meet the life of carbamide and ammonium sulfate
Produce and require.
Compared with the utilization underground coal gasification(UCG) product gas of Fig. 1-3 produce the technique of carbamide, increase the work of production ammonium sulfate
Skill has following advantage：
Side-product sulfur and the fresh water (FW) production ammonium sulfate product for processing are taken full advantage of, the income from sales of project is increased；
The fresh water (FW) produced by coal underground gasifying technology is consumed, and has shared the cost of investment of technique water processing establishment；
According to changing according to market price, final products are flexibly changed between carbamide and ammonium sulfate production.
But meanwhile, compared with the technique of carbamide is produced using underground coal gasification(UCG) product gas, increase the work of production ammonium sulfate
Skill has following shortcoming：The capital input of project and operation cost are higher, it is likely that increased by additional product ammonium sulfate
Income from sales is offset；The coal seam higher for sulfur content, needs more ammonias to remove to synthesize ammonium sulfate product-need balance
Ammonia supply between urea production and ammonium sulfate production.
Fig. 7 is using underground coal gasification(UCG) air gasification product gas production carbamide, ammonium sulfate, ammonium nitrate, NPK compound fertilizers
And the square process chart of intermediate chemicals nitric acid, phosphoric acid.Specifically can be determined to select according to the market demand and price
Which kind of product.Technique leading portion production carbamide, ammonium sulfate technique it is same as shown in Figure 4.The production of nitric acid 37 is using such as
Ostwald synthetic methods（The double pressure methods of as little as middle pressure, in be depressed into high pressure list pressure method etc.）.Ammonia 21 is in Pt/Rh alloys
It is oxidized on mesh catalyst, produces NO as intermediate（4NH3(g) + 5O2(g) → 4NO(g) + 6H2O(g)）.Then enter
One step and air（Oxidant）React to form NO2（2NO(g) + O2(g) ↔ 2NO2(g)）, last NO2Inhaled by reverse current
Midwifery is into nitric acid 37（3NO2(g) + H2O(l) ↔ 2HNO3(aq) + NO(g)）.Ammonia oxidizing process releases big calorimetric, can
Other down stream process units and communal facility are used for using waste-heat recovery device production steam.Intermediate product nitric acid 37 is delivered to
Downstream ammonium nitrate production unit 38 and NPK compound fertilizers production unit 44, for being processed further final products.
Nitric acid 37 reacts in ammonium nitrate production unit 38 with ammonia 21（Neutralization reaction）To produce ammonium nitrate 39（HNO3
(l) + NH3(g) → NH4NO3(aq)）.：
Ammonium nitrate（AN）Synthesis technique generally includes three steps：Neutralization, evaporation and solidification（Pelletize or granulation）.Neutralization device bag
Include and freely seethe with excitement container, blood circulation or tubular reactor.Come according to the optimum condition of project construction scale and heat comprehensive utilization
Select optimised process.Vaporising device is used to remove the water in ammonium nitrate solution.It is generally used in the waste heat steaming that neutralization device is produced
Vapour or at the scene other steam are evaporated process.After evaporation process, the ammonium nitrate solution of concentration（ANSOL）39 can be delivered to
NPK compound fertilizers production unit 44 is processed further processing.Solidification/prilling generally by concentration ammonium nitrate solution to
Under be ejected in granulation tower, while be inversely passed through air being dried to dripping drops.Stay when drop reaches tower bottom solid
Body ammoniumnitrate prill 39 is used as final product.Granulating process may also be employed more complicated equipment and additive, contribute to ammonium nitrate
The formation of granule and the stability of raising granule.For example, by ammonium nitrate and solid packing material Calcium Carbonate（From limestone or white
Marble）Mixing, final product is calcium ammonium nitrate（CAN）.It is final to produce if ammonium nitrate solution is mixed with the carbamide of required ratio
Thing is urea-ammonium nitrate（UAN）.
The synthesis technique of phosphoric acid is more, can be by two hydration methods, half hydration method, dual-stage dihydrate process, single phase half
Hydrate or dual-stage hemihydrate process etc. are realizing.Its ultimate principle is using the triphosphoric acid being present in phosphate rock 41
Salt generates phosphatase 24 2 and calcium sulfate with the reaction of concentrated sulphuric acid 33（Gypsum Fibrosum）（Ca5(PO4)2(s) + 3H2SO4(l) → 2H3PO4(l)
+ 3CaSO4(s)）.
The synthesis of NPK compound fertilizers is using the mixed chemical industry skill of acidolysis.The method is consumed using underground coal gasification(UCG) work simultaneously
The sulphuric acid 33 of the production of by-product sulfur 13 of skill.First, it is phosphate rock 41 is miscible with nitric acid 37 in reactor, obtain phosphoric acid and
The solution of calcium nitrate（Ca3(PO4)2(s) + 6HNO3(l) + 12H2O(l) → 2H3PO4(l) + 3Ca(NO3)2(aq) +
12H2O(l)）.Secondly, by phosphatase 24 2, sulphuric acid 33 and ammonium nitrate solution 39（Or nitric acid 37）Mix with above-mentioned solution, and utilize ammonia
In gas 21 and Acid Slurry.After the completion of neutralization, add other components for example ammonium sulfate 35, the compound containing potassium and magnesium, ammonium phosphate and
Perphosphate 43.Finally slurry is delivered to into prilling, including pelletize, drying, screening, crushing, cooling and coating.
Fig. 8 is using underground coal gasification(UCG) oxygen-rich gasification product gas production carbamide, ammonium sulfate, ammonium nitrate, NPK compound fertilizers
And the square process chart of intermediate chemicals nitric acid, phosphoric acid.Fig. 9 is the production of underground coal gasification(UCG) pure oxygen gasification product gas
The square process chart of carbamide, ammonium sulfate, ammonium nitrate, NPK compound fertilizers and intermediate chemicals nitric acid, phosphoric acid.Fig. 8 and
The ammonium nitrate of Fig. 9 and the production technology of NPK compound fertilizers are essentially identical with technique described in Fig. 7.Difference is setting for downstream process
The matching of standby size, the amount of intermediate chemicals ammonia need to simultaneously meet carbamide, ammonium sulfate, ammonium nitrate and NPK compound fertilizers
Production requirement.
With using underground coal gasification(UCG) product gas production carbamide compare with the technique of ammonium sulfate, increase production ammonium nitrate and
The technique of NPK compound fertilizers has following advantage：
Take full advantage of production ammonium nitrate and the NPK such as underground coal gasification(UCG) side-product such as sulfur, the fresh water (FW), the carbon dioxide that process
Compound fertilizer, effectively increases the income from sales of project；
The fresh water (FW) produced by coal underground gasifying technology is consumed, and has shared the cost of investment of technique water processing establishment；Have
Beneficial to the comprehensive utilization for integrating downstream units waste heat；
According to being changed according to market price, flexibly change most between the production of carbamide, ammonium sulfate, ammonium nitrate and NPK compound fertilizers
Finished product；
Production calcium ammonium nitrate may be selected（CAN）With urea-ammonium nitrate（UAN）.
With using underground coal gasification(UCG) product gas production carbamide compare with the technique of ammonium sulfate, increase production ammonium nitrate and
The technique of NPK compound fertilizers has following shortcoming：
The capital input of project and operation cost are higher, it is likely that being offset by the income from sales that additional product increases.For
The higher coal seam of sulfur content, need more ammonias go to synthesize downstream product-need balance urea production, ammonium sulfate production,
Ammonia supply between ammonium nitrate production and the production of NPK compound fertilizers.
Correlation properties, structure, feature that " embodiment " mentioned above is included in described in embodiment
It is all related to the wherein at least one embodiment of the present invention.Therefore, the above is repeatedly referred to " in an embodiment "
Not all refer in particular to same embodiment in place.Additionally, the correlation properties for describing in embodiments, structure, feature can be with
Any suitable mode one or more combination.
Embodiments described above is the invention is not limited in, for a person skilled in the art, the present invention may be used also
To have various change and adjustment, without departing from the spirit and principles in the present invention, the change and adjustment all should be in models of the present invention
In enclosing.
Claims (9)
1. the method for producing chemical fertilizer and intermediate chemical product using underground coal gasification(UCG) product gas, it is characterised in that：Based on many
The crude synthesis gas for possessing appropriate economic scale that individual ISC underground gasification furnaces are produced by gasification, gasification mode be air gasification or
Oxygen-rich gasification, methods described comprises the steps：
（1）Crude synthesis gas pretreatment：Crude synthesis gas Jing cooling, washing and separative element obtain 60 DEG C of temperature ＜ dry synthesis gas with
And coal tar and fresh water (FW)；
（2）Dry synthetic gas desulfurization：By Claus method, chemiadsorption or shell Sulfinol acid gas absorption method to dry synthesis gas
Carry out desulfurization process；Afterwards loss of essence sulphuring treatment is carried out using ZnO particle or renewable ZnO and zinc titanate granule, the sulfur of removing is returned
Receive；
（3）Dry synthesis gas conversion and cooling：Dry synthesis gas after desulfurization is heated to 260 DEG C in preheating device, is delivered to isothermal
WGS unit, CO is converted into using steam by contained CO2And H2；
（4）Dry synthesis gas decarbonization：Step（3）After dry synthesis air cooling after process, decarburization unit is delivered to, by CO2Remove and return
Receive, for urea synthesis, decarbonization process used includes chemiadsorption, physisorphtion, absorption bed process, absorption regeneration method, low
Warm partition method or membrane separation process；
（5）Methanation and purification, through step（4）The synthesis gas of process only contains CH4, N2、H2With CO that may be present and CO2,
In methanation unit, by nickel-base catalyst further will likely be remaining CO and CO2Removing, methane passes through purification unit
Remove, in final synthesis gas N is comprised only2And H2；
（6）Synthesis ammonia；Step（5）Synthesis gas after process is delivered to synthesis ammonia unit after synthesic gas compressor supercharging,
Under high pressure, H2And N2Reaction generates ammonia, and generates ammonia after scrubbing tower is separated from unreacted gas and cooled down；
（7）Urea synthesis：From step（6）Ammonia and step are extracted in ammonia（4）The CO of recovery2Urea synthesis are delivered to together
Unit, produces final product carbamide.
2. the method for producing chemical fertilizer and intermediate chemical product using underground coal gasification(UCG) product gas, it is characterised in that：Based on many
The crude synthesis gas for possessing appropriate economic scale that individual ISC underground gasification furnaces are produced by gasification, gasification mode is pure oxygen gasification, should
Gasification mode injects oxygen by air-separating plant to underground gasification furnace carries out pure oxygen gasification, and the air-separating plant is simultaneously
Production nitrogen, is fed directly to synthesize ammonia unit by booster compressor, and methods described comprises the steps：
（1）Crude synthesis gas pretreatment：Crude synthesis gas Jing cooling, washing and separative element obtain 60 DEG C of temperature ＜ dry synthesis gas with
And coal tar and fresh water (FW)；
（2）Dry synthetic gas desulfurization：By Claus method, chemiadsorption or shell Sulfinol acid gas absorption method to dry synthesis gas
Carry out desulfurization process；Afterwards loss of essence sulphuring treatment is carried out using ZnO particle or renewable ZnO and zinc titanate granule, the sulfur of removing is returned
Receive；
（3）Dry synthesis gas conversion and cooling：Dry synthesis gas after desulfurization is heated to 260 DEG C in preheating device, is delivered to isothermal
WGS unit, CO is converted into using steam by contained CO2And H2；
（4）Dry synthesis gas decarbonization：Step（3）After dry synthesis air cooling after process, decarburization unit is delivered to, by CO2Remove and return
Receive, for urea synthesis, decarbonization process used includes chemiadsorption, physisorphtion, absorption bed process, absorption regeneration method, low
Warm partition method or membrane separation process；
（5）Dry synthesis gas pressure-variable adsorption：Dry synthesis gas passes through psa unit by H2Selectively, it is efficiently separating, so as to
Obtain purity>96% hydrogen；
（6）Synthesis ammonia；Step（5）The hydrogen of acquisition is delivered to synthesis ammonia unit, under high pressure, H Jing after compressor supercharging2And N2
Reaction generates ammonia, and generates ammonia after scrubbing tower is separated from unreacted gas and cooled down；
（7）Urea synthesis：From step（6）Ammonia and step are extracted in ammonia（4）The CO of recovery2Urea synthesis are delivered to together
Unit, produces final product carbamide；
Step（6）Middle N2:H2Mol ratio is controlled to 0.33 by adjusting the nitrogen that air-separating plant is generated.
3. utilization underground coal gasification(UCG) product gas according to claim 1 and 2 production chemical fertilizer and intermediate chemical product
Method, it is characterised in that：Methods described also includes：
Step（2a）The sulfur of recovery obtains sulphuric acid through reaction；
Step（7a）Synthesis ammonium sulfate, by step（6）The ammonia and step of production（2a）The sulphuric acid for obtaining sends into ammonium sulfate synthesis
Unit, synthetic product ammonium sulfate.
4. utilization underground coal gasification(UCG) product gas according to claim 1 and 2 production chemical fertilizer and intermediate chemical product
Method, it is characterised in that：Methods described also includes：
Step（2a）The sulfur of recovery obtains sulphuric acid through reaction；
Step（6a）Nitric acid synthesis, step（6）The ammonia of generation, Jing absorbs and generates nitric acid after being oxidized；
Step（7a）Synthesis ammonium sulfate, by step（6）The ammonia and step of production（2a）The sulphuric acid for obtaining sends into ammonium sulfate synthesis
Unit, synthetic product ammonium sulfate；
Step（7b）Nitric acid synthesis ammonium, by step（6）The ammonia and step of production（6a）The nitric acid for obtaining sends into ammonium nitrate synthesis
Unit, synthetic product ammonium nitrate.
5. utilization underground coal gasification(UCG) product gas according to claim 4 produce the side of chemical fertilizer and intermediate chemical product
Method, it is characterised in that：Methods described also includes：
Step 7（c）, synthesize phosphoric acid, with phosphate rock as raw material, its triphosphate for containing and step（2a）Concentrated sulphuric acid it is anti-
Phosphoric acid and calcium sulfate should be generated.
6. utilization underground coal gasification(UCG) product gas according to claim 5 produce the side of chemical fertilizer and intermediate chemical product
Method, it is characterised in that：Methods described also includes：
Step 7（d）, synthesize NPK compound fertilizers, with phosphate rock as raw material, its triphosphate for containing and step（6a）Nitre
Acid reaction generates phosphoric acid and calcium nitrate solution, and phosphoric acid, sulphuric acid and ammonium nitrate are mixed with previous solu, is neutralized using ammonia, in
With after the completion of, ammonium sulfate, the compound containing potassium and magnesium, ammonium phosphate, perphosphate are added, finally slurry is delivered to into pelletize work
Skill, Jing pelletizes, drying, screening, crushing, cooling and coating obtain NPK compound fertilizers.
7. utilization underground coal gasification(UCG) product gas according to claim 1 produce the side of chemical fertilizer and intermediate chemical product
Method, it is characterised in that：By step（7b）The ammonium nitrate of synthesis mixes with Calcium Carbonate, obtains calcium ammonium nitrate.
8. utilization underground coal gasification(UCG) product gas according to claim 1 produce the side of chemical fertilizer and intermediate chemical product
Method, it is characterised in that：By step（7b）The ammonium nitrate of synthesis and proper proportion step（7）The carbamide mixing of acquisition, obtains urea-nitre
Sour ammonium.
9. utilization underground coal gasification(UCG) product gas according to claim 1 produce the side of chemical fertilizer and intermediate chemical product
Method, it is characterised in that：Step（1）Fresh water (FW) be delivered to technique unit for treating water and processed, the technique water circulation of process is again
It is used in ISC underground gasification furnaces, crude synthesis gas cooling, washing and separative element and other downstream processes.
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| CN113767087A (en) * | 2019-04-29 | 2021-12-07 | 蒂森克虏伯工业解决方案股份公司 | Process for the catalytic production of urea |
| CN114000977A (en) * | 2021-10-29 | 2022-02-01 | 西安热工研究院有限公司 | A wind energy storage system and method based on coal-to-ammonia |
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