US20210292204A1 - Process - Google Patents
Process Download PDFInfo
- Publication number
- US20210292204A1 US20210292204A1 US17/204,231 US202117204231A US2021292204A1 US 20210292204 A1 US20210292204 A1 US 20210292204A1 US 202117204231 A US202117204231 A US 202117204231A US 2021292204 A1 US2021292204 A1 US 2021292204A1
- Authority
- US
- United States
- Prior art keywords
- wastewater stream
- process according
- treated
- wastewater
- stream
- 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.)
- Abandoned
Links
- 238000000034 method Methods 0.000 title claims abstract description 77
- 239000002351 wastewater Substances 0.000 claims abstract description 96
- 238000009300 dissolved air flotation Methods 0.000 claims abstract description 32
- 238000002309 gasification Methods 0.000 claims abstract description 29
- 239000007787 solid Substances 0.000 claims abstract description 25
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000007872 degassing Methods 0.000 claims abstract description 20
- 239000010813 municipal solid waste Substances 0.000 claims abstract description 14
- 238000001914 filtration Methods 0.000 claims abstract description 12
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 10
- 231100001240 inorganic pollutant Toxicity 0.000 claims abstract description 6
- 230000003472 neutralizing effect Effects 0.000 claims abstract description 4
- 239000004576 sand Substances 0.000 claims abstract description 3
- 239000007789 gas Substances 0.000 claims description 54
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 229910001868 water Inorganic materials 0.000 claims description 38
- 230000015572 biosynthetic process Effects 0.000 claims description 26
- 238000003786 synthesis reaction Methods 0.000 claims description 26
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 22
- 239000002699 waste material Substances 0.000 claims description 19
- 230000003647 oxidation Effects 0.000 claims description 18
- 238000007254 oxidation reaction Methods 0.000 claims description 18
- 239000003054 catalyst Substances 0.000 claims description 16
- 229910001385 heavy metal Inorganic materials 0.000 claims description 14
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 11
- 239000001257 hydrogen Substances 0.000 claims description 11
- 229910052739 hydrogen Inorganic materials 0.000 claims description 11
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 10
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 10
- 238000005273 aeration Methods 0.000 claims description 9
- 239000000701 coagulant Substances 0.000 claims description 8
- 238000006386 neutralization reaction Methods 0.000 claims description 8
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 claims description 6
- 229910017052 cobalt Inorganic materials 0.000 claims description 6
- 239000010941 cobalt Substances 0.000 claims description 6
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical group [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 150000002894 organic compounds Chemical class 0.000 claims description 5
- 229920000642 polymer Polymers 0.000 claims description 5
- LSNNMFCWUKXFEE-UHFFFAOYSA-N Sulfurous acid Chemical class OS(O)=O LSNNMFCWUKXFEE-UHFFFAOYSA-N 0.000 claims description 4
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 claims description 4
- 239000003513 alkali Substances 0.000 claims description 4
- 239000002440 industrial waste Substances 0.000 claims description 4
- 239000012528 membrane Substances 0.000 claims description 4
- 239000002028 Biomass Substances 0.000 claims description 3
- 239000004411 aluminium Substances 0.000 claims description 3
- 229910052782 aluminium Inorganic materials 0.000 claims description 3
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims description 3
- 239000000356 contaminant Substances 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 150000001495 arsenic compounds Chemical class 0.000 claims description 2
- 229940093920 gynecological arsenic compound Drugs 0.000 claims description 2
- 150000002826 nitrites Chemical class 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims 1
- 239000005864 Sulphur Substances 0.000 claims 1
- 238000004064 recycling Methods 0.000 abstract description 3
- 150000003839 salts Chemical class 0.000 abstract description 3
- 239000002957 persistent organic pollutant Substances 0.000 abstract description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 24
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 18
- 239000010802 sludge Substances 0.000 description 13
- -1 and the like) Substances 0.000 description 12
- 239000000047 product Substances 0.000 description 12
- 229910002092 carbon dioxide Inorganic materials 0.000 description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 10
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 8
- 239000002253 acid Substances 0.000 description 8
- 239000000446 fuel Substances 0.000 description 8
- 239000001569 carbon dioxide Substances 0.000 description 7
- 239000002245 particle Substances 0.000 description 7
- 241000196324 Embryophyta Species 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 239000000498 cooling water Substances 0.000 description 6
- 239000003344 environmental pollutant Substances 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 239000000463 material Substances 0.000 description 6
- 231100000719 pollutant Toxicity 0.000 description 6
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 description 6
- 239000000243 solution Substances 0.000 description 6
- 239000003575 carbonaceous material Substances 0.000 description 5
- 239000003921 oil Substances 0.000 description 5
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 4
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000000706 filtrate Substances 0.000 description 4
- 150000004820 halides Chemical class 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 238000001991 steam methane reforming Methods 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 3
- 229910052785 arsenic Inorganic materials 0.000 description 3
- 239000012267 brine Substances 0.000 description 3
- 239000003518 caustics Substances 0.000 description 3
- 238000005352 clarification Methods 0.000 description 3
- 238000005194 fractionation Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000012535 impurity Substances 0.000 description 3
- 238000005342 ion exchange Methods 0.000 description 3
- 239000004033 plastic Substances 0.000 description 3
- 229920003023 plastic Polymers 0.000 description 3
- 238000001556 precipitation Methods 0.000 description 3
- 230000008929 regeneration Effects 0.000 description 3
- 238000011069 regeneration method Methods 0.000 description 3
- 239000002893 slag Substances 0.000 description 3
- 239000004289 sodium hydrogen sulphite Substances 0.000 description 3
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 description 3
- 235000010265 sodium sulphite Nutrition 0.000 description 3
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 3
- 229910021653 sulphate ion Inorganic materials 0.000 description 3
- 239000004291 sulphur dioxide Substances 0.000 description 3
- 235000010269 sulphur dioxide Nutrition 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 2
- 229910021580 Cobalt(II) chloride Inorganic materials 0.000 description 2
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- 240000008042 Zea mays Species 0.000 description 2
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 2
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 2
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000015271 coagulation Effects 0.000 description 2
- 238000005345 coagulation Methods 0.000 description 2
- GVPFVAHMJGGAJG-UHFFFAOYSA-L cobalt dichloride Chemical compound [Cl-].[Cl-].[Co+2] GVPFVAHMJGGAJG-UHFFFAOYSA-L 0.000 description 2
- 230000003750 conditioning effect Effects 0.000 description 2
- 235000005822 corn Nutrition 0.000 description 2
- 150000001896 cresols Chemical class 0.000 description 2
- 229960002089 ferrous chloride Drugs 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 description 2
- NMCUIPGRVMDVDB-UHFFFAOYSA-L iron dichloride Chemical compound Cl[Fe]Cl NMCUIPGRVMDVDB-UHFFFAOYSA-L 0.000 description 2
- 229910052753 mercury Inorganic materials 0.000 description 2
- QSHDDOUJBYECFT-UHFFFAOYSA-N mercury Chemical compound [Hg] QSHDDOUJBYECFT-UHFFFAOYSA-N 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 150000002989 phenols Chemical class 0.000 description 2
- 239000003473 refuse derived fuel Substances 0.000 description 2
- 229910052938 sodium sulfate Inorganic materials 0.000 description 2
- 235000011152 sodium sulphate Nutrition 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 241000894007 species Species 0.000 description 2
- 238000000629 steam reforming Methods 0.000 description 2
- 239000004753 textile Substances 0.000 description 2
- 239000002023 wood Substances 0.000 description 2
- YNPBOAZAMMRLTE-UHFFFAOYSA-N 1-sulfido-1,3,5-triazin-1-ium Chemical class [S-][N+]1=CN=CN=C1 YNPBOAZAMMRLTE-UHFFFAOYSA-N 0.000 description 1
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 description 1
- 244000025254 Cannabis sativa Species 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 229920000742 Cotton Polymers 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- 244000068988 Glycine max Species 0.000 description 1
- 235000010469 Glycine max Nutrition 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 1
- 241001520808 Panicum virgatum Species 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002154 agricultural waste Substances 0.000 description 1
- 229940037003 alum Drugs 0.000 description 1
- 239000001164 aluminium sulphate Substances 0.000 description 1
- 235000011128 aluminium sulphate Nutrition 0.000 description 1
- 239000010828 animal waste Substances 0.000 description 1
- 229920006318 anionic polymer Polymers 0.000 description 1
- 230000000845 anti-microbial effect Effects 0.000 description 1
- 239000004599 antimicrobial Substances 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 238000002453 autothermal reforming Methods 0.000 description 1
- 239000002551 biofuel Substances 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 125000002915 carbonyl group Chemical group [*:2]C([*:1])=O 0.000 description 1
- JJWKPURADFRFRB-UHFFFAOYSA-N carbonyl sulfide Chemical compound O=C=S JJWKPURADFRFRB-UHFFFAOYSA-N 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 229910052804 chromium Inorganic materials 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- BUACSMWVFUNQET-UHFFFAOYSA-H dialuminum;trisulfate;hydrate Chemical compound O.[Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O BUACSMWVFUNQET-UHFFFAOYSA-H 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 239000010419 fine particle Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 229910003439 heavy metal oxide Inorganic materials 0.000 description 1
- 125000001072 heteroaryl group Chemical group 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910000042 hydrogen bromide Inorganic materials 0.000 description 1
- CPELXLSAUQHCOX-UHFFFAOYSA-N hydrogen bromide Substances Br CPELXLSAUQHCOX-UHFFFAOYSA-N 0.000 description 1
- 229910000041 hydrogen chloride Inorganic materials 0.000 description 1
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 description 1
- 229910000040 hydrogen fluoride Inorganic materials 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 229910052745 lead Inorganic materials 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000002906 microbiologic effect Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 239000012071 phase Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000013502 plastic waste Substances 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 229920002401 polyacrylamide Polymers 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 239000002516 radical scavenger Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000010801 sewage sludge Substances 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 159000000000 sodium salts Chemical class 0.000 description 1
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000010907 stover Substances 0.000 description 1
- 239000011269 tar Substances 0.000 description 1
- 239000011275 tar sand Substances 0.000 description 1
- 229910052720 vanadium Inorganic materials 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- B09B3/0083—
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
-
- 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
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
- C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
- C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed by reaction of water vapour with carbon monoxide
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
- C02F1/004—Processes for the treatment of water whereby the filtration technique is of importance using large scale industrial sized filters
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/24—Treatment of water, waste water, or sewage by flotation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/28—Treatment of water, waste water, or sewage by sorption
- C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/48—Treatment of water, waste water, or sewage with magnetic or electric fields
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5272—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using specific organic precipitants
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- Y02W10/00—Technologies for wastewater treatment
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Definitions
- the present invention relates to a process for treating wastewater from a gasification process.
- Gasification processes are used to generate feedstock for Fischer-Tropsch (F-T) processes for the generation of hydrocarbon fuels.
- F-T Fischer-Tropsch
- the Fischer-Tropsch process is widely used to generate fuels from carbon monoxide and hydrogen and can be represented by the equation:
- This reaction is highly exothermic and is catalysed by a Fischer-Tropsch catalyst, typically a cobalt-based catalyst, under conditions of elevated temperature (typically at least 180° C., eg 200° C. or above) and pressure (eg at least 10 bar).
- the hydrogen and carbon monoxide feedstock is normally synthesis gas.
- the synthesis gas may be produced by gasifying a carbonaceous material at an elevated temperature, for example, about 700° C. or higher.
- the carbonaceous material may comprise any carbon-containing material that can be gasified to produce synthesis gas.
- the carbonaceous material may comprise biomass (e.g., plant or animal matter, biodegradable waste, and the like), a food resource (e.g., as corn, soybean, and the like), and/or a non-food resource such as coal (e.g., low grade coal, high grade coal, clean coal, and the like), oil (e.g., crude oil, heavy oil, tar sand oil, shale oil, and the like), solid waste (e.g., municipal solid waste, hazardous waste), refuse derived fuel (RDF), tyres, petroleum coke, trash, garbage, biogas, sewage sludge, animal waste, agricultural waste (e.g., corn stover, switch grass, grass clippings), construction demolition materials, plastic materials (e.g., plastic waste
- the fresh synthesis gas may be treated to adjust the molar ratio of H 2 to CO by steam reforming (eg, a steam methane reforming (SMR) reaction where methane is reacted with steam in the presence of a steam methane reforming (SMR) catalyst); partial oxidation; autothermal reforming; carbon dioxide reforming; or a combination of two or more thereof.
- steam reforming eg, a steam methane reforming (SMR) reaction where methane is reacted with steam in the presence of a steam methane reforming (SMR) catalyst
- partial oxidation eg, a steam methane reforming (SMR) reaction where methane is reacted with steam in the presence of a steam methane reforming (SMR) catalyst
- partial oxidation eg., autothermal reforming; carbon dioxide reforming; or a combination of two or more thereof.
- such treatment of the synthesis gas is considered to be broadly part of the F-T process and any wastewater streams resulting from
- the molar ratio of H 2 to CO in the fresh synthesis gas is desirably in the range from about 1.6:1 to about 2.2:1, or from about 1.8:1 to about 2.10:1, or from about 1.95:1 to about 2.05:1.
- the fresh synthesis gas may optionally be combined with a recycled tail gas (eg a recycled FT tail gas), which also contains H 2 and CO, to form a reactant mixture.
- a recycled tail gas eg a recycled FT tail gas
- the tail gas may optionally comprise H 2 and CO with a molar ratio of H 2 to CO in the range from about 0.5:1 to about 2:1, or from about 0.6:1 to about 1.8:1, or from about 0.7:1 to about 1.2:1.
- the combined FT synthesis gas feed (comprising of fresh synthesis gas combined with recycled tailgas) desirably comprises H 2 and CO in a molar ratio in the range from about 1.1 to about 2.1:1, or from about 1.7:1 to about 2.0:1, or from about 1.7:1 to about 1.9:1.
- the invention is concerned particularly but not exclusively with treating wastewater from a gasification process utilising Municipal Solid Waste (MSW) or Commercial and Industrial waste (C & I) as the gasification feedstock, which tends to generate wastewater with high levels of pollutants.
- MSW Municipal Solid Waste
- C & I Commercial and Industrial waste
- RTFO Renewable Transport Fuel Obligation
- F-T wastewater treatment is disclosed in WO2016193337A1 which discussed pre-treating the waste water by distillation or steam stripping, removing residual wax by gravity and feeding the resulting pretreated waste water to a granular sludge based anaerobic bioreactor.
- This document pays scant regard to the treatment of salt water streams except by ion exchange or reverse osmosis.
- the present invention provides a process for treating wastewater from a combined gasification and Fischer-Tropsch (F-T) process in which aqueous effluent from the gasification is treated with alkali to produce a first wastewater stream and the first wastewater stream is treated to remove inorganic pollutants present in the aqueous effluent, and a second wastewater stream, containing water produced in the F-T process and being distinct from the first wastewater stream, is treated separately from the first wastewater stream to remove organic compounds.
- F-T combined gasification and Fischer-Tropsch
- the treated first wastewater stream may be discharged to the environment.
- the treated second wastewater stream may be reused within plant utilised in the gasification and/or F-T process.
- the invention also provides a process for treating wastewater from a combined gasification and Fischer-Tropsch (F-T) process in which aqueous effluent from the gasification is treated with alkali to produce a first wastewater stream and the first wastewater stream is treated to remove inorganic pollutants present in the aqueous effluent, and a second wastewater stream, containing water produced in the F-T process and being distinct from the first wastewater stream, is treated separately from the first wastewater stream to remove organic compounds, wherein the treated first wastewater stream is discharged to the environment and the treated second wastewater stream is reused within plant utilised in the gasification and/or F-T process.
- F-T combined gasification and Fischer-Tropsch
- Salty inorganic wastewaters are separately treated from organic laden, non-salty wastewaters. In preferred embodiments, this allows the non-salty (fresh) water to be reused within the facility for cooling water makeup or other resource.
- the first wastewater stream may for example comprise treated aqueous effluent from any one or more of a gasification zone, a partial oxidation zone, a clean-up zone and/or a hydrogen to carbon monoxide ratio shifting zone (e.g. a water gas shift zone).
- a gasification zone e.g. a gasification zone
- a partial oxidation zone e.g. a partial oxidation zone
- a clean-up zone e.g. a water gas shift zone
- aqueous effluent from one or more of stages a. to c. is treated by degassing and subsequent neutralisation and aqueous effluent from stages d and e. (and optionally also stage f.) is separately treated.
- the first wastewater stream can normally be economically treated to remove pollutants to satisfy regulatory requirements, even if the feedstock is derived from MSW or C & I waste.
- the treated first wastewater stream is discharged to the environment.
- the treatment comprises:
- the invention provides a process for treating wastewater from a combined gasification and Fischer-Tropsch (F-T) process in which aqueous effluent from the gasification is treated with alkali to produce a first wastewater stream and the first wastewater stream is treated to remove inorganic pollutants present in the aqueous effluent, wherein the treatment comprises:
- the preliminary degassing step reduces the requirement for neutralisation and enhances the economics of the process. Acid gases such as CO 2 and SO 2 which would otherwise exert a caustic demand are released. This also helps maintain a lower salinity in the final treated effluent.
- wastewater treatment of the present invention in both its aspects, has been found to be remarkably effective in reducing heavy metal and other pollutants, even when using a relatively dirty feedstock such as MSW or C & I waste.
- the process comprises the further step:
- the first wastewater stream is neutralised in a reaction zone which is agitated by an oxidising gas (eg air).
- an oxidising gas eg air
- reaction zone is agitated by bubble aeration in the presence of a catalyst, preferably a cobalt catalyst or a ferrous catalyst, for the oxidation of one or more of: sulphites, nitrites and arsenic compounds.
- a catalyst preferably a cobalt catalyst or a ferrous catalyst
- the first wastewater stream is treated with activated carbon (preferably powdered activated carbon) to absorb organic compounds and/or heavy metals.
- activated carbon preferably powdered activated carbon
- the treated first wastewater stream is subjected to a dissolved air flotation process to separate spent activated carbon and other suspended solids (if present).
- the suspended solids will typically include heavy metal oxides.
- the first wastewater stream is filtered with a sand filter, multimedia filter or membrane filter, to remove any remaining spent activated carbon and suspended solids (if present).
- This feature enables virtually complete clarification of the wastewater in an economical fashion.
- the first wastewater stream is treated with a coagulating agent, preferably an aluminium or iron-based coagulant and/or a flocculation-promoting polymer, to assist in the removal of suspended solids.
- a coagulating agent preferably an aluminium or iron-based coagulant and/or a flocculation-promoting polymer, to assist in the removal of suspended solids.
- This feature is particularly advantageous in combination with dissolved air flotation because it agglomerates the small particles in the effluent and assists their removal by the dissolved air flotation.
- the coagulant also assists in the capture of heavy metals.
- the first wastewater stream is subject to an air or steam stripping process, preferably under alkaline conditions, to remove ammonia.
- the stripped ammonia is captured and reused within the facility.
- the first wastewater stream is treated with a sulphide compound.
- the sulphide may be an inorganic sulphide such as sodium sulphide for example, or an organic sulphide compound, preferably a heteroaromatic sulphide, most preferably an S-triazine sulphide salt, to precipitate heavy metals.
- the invention also provides a plant configured to operate the process disclosed herein.
- the plant may be a combined gasification and Fischer-Tropsch (F-T) plant.
- FIG. 1 is a schematic diagram of a Feedstock Conditioning Facility used to process MSW or C & I waste to a feedstock for a combined gasification and F-T process;
- FIG. 2 is a schematic diagram of a combined gasification and F-T process utilising the feedstock generated by the FCF of FIG. 1 ;
- FIG. 3 is a schematic diagram of the unit T 1 (apparatus 72 a - 72 e ) used for treatment of the 1st WWT (Wastewater) stream in FIG. 1 , and
- FIG. 4 is a schematic diagram showing the degassing tank and reaction tank arrangement of unit T 1 in more detail.
- the FCF shown receives bagged C&I and MSW Waste from a bunker (not shown) from which the bags of waste are transferred to a bag splitter 1 .
- the waste from bag splitter 1 is fed to a vibration conveyor c 1 which passes beneath a belt magnet 2 and an eddy current rotor 3 which remove ferrous and non-ferrous metals respectively.
- the processed waste then passes to a density separator 4 which removes high density materials such as glass and rubble which are not combustible.
- the processed waste is then transferred by a conveyor c 2 to fine shredder 5 which reduces the particle size to 25 mm or less.
- the size-reduced waste is then transferred by a conveyor c 3 to a belt dryer 4 where excess moisture is removed.
- the dried waste (typical moisture content 10 wt %) is then transferred by a conveyor c 4 to a bunker 7 .
- Bunker 7 also receives Solid Recovered Fuel (SRF) which is a waste product of somewhat higher calorific value than MSW and C&I waste and is typically derived from paper, card, wood, textiles and plastics.
- SRF Solid Recovered Fuel
- the combined material from bunker 7 is then transferred by a crane to conveyor assembly c 7 , which feeds the processed feedstock a baler 8 .
- baled feedstock from baler 8 is fed to a feeder 12 , which pressurises the feedstock to reactor pressure and feeds it to a gasifier 21 of a reactor assembly R.
- Reactor assembly R further comprises a partial oxidation (POx) reactor 22 and a radiant cooler 23 .
- POx partial oxidation
- the gasifier 21 comprises a steam reforming reactor incorporating a deep fluidised bed, the bed operating temperature being typically 600-800° C.
- the fluidised bed is fluidised with superheated steam and causes the carbonaceous material of the feedstock to pyrolyse and react with the steam to form hydrogen, carbon monoxide and carbon dioxide.
- the syngas product of gasifier 21 is fed to partial oxidation reactor 22 , which also receives F-T tailgas from an F-T reactor 51 and also oxygen.
- Reactor 22 is operated at a temperature above the ash melting point at a sufficient residence time to convert tars and oils and methane in the syngas to carbon oxides, hydrogen and water.
- the syngas output of partial oxidation reactor 22 is fed to a cooler 23 which comprises radiant and convective cooler units. Reactor 22 also generates molten ash which is solidified in cooler 23 .
- the HRSG heat recovery steam generator
- the HRSG has a blowdown stream of water which contains slag particles from the gasifier and PDX.
- the concentration of suspended solids is relatively high in this stream and it is therefore sent directly to the sludge dewatering centrifuge 72 e (centrifuge rather than cyclone) for removal of the bulk of the solids before the liquid phase is co-treated with the rest of the salty water.
- the cooled syngas from cooler 23 is fed to a Venturi scrubber 31 a of a gas cleanup unit C, which further comprises an acid gas removal unit 31 b , a compressor 41 and an acid gas removal unit 42 .
- Venturi scrubber 31 a Particulate matter is removed in Venturi scrubber 31 a , and the resulting scrubbed syngas is passed to a halide removal unit 31 b .
- Halide removal unit 31 b comprises a packed column over which sodium hydroxide solution is passed to absorb hydrogen chloride, bromide and fluoride.
- the resulting 1st wastewater (WWT) stream, containing halide salts, is passed to a degassing tank 72 a of a first water treatment assembly T 1 .
- the syngas output of halide removal unit 31 b is compressed in a compressor 41 and then cooled, condensing liquid (wastewater) which is then removed from the syngas and fed to a degassing tank and then on to Dissolved Air Flotation (DAF) unit 73 a , discussed below.
- DAF Dissolved Air Flotation
- the compressed syngas from compressor 41 is fed to acid gas removal unit 42 , which operates at low temperature and high pressure and uses methanol as a solvent for removal of hydrogen sulphide, carbonyl sulphide, carbon dioxide and trace impurities such as hydrogen cyanide, ammonia, formic acid and metal carbonyls which might otherwise be detrimental to the downstream process units, in particular by poisoning the F-T catalyst.
- Unit 42 preferably utilises the RECTISOLTM process.
- the dissolved impurities are removed from the methanol solvent by stepwise flashing and are passed to an incinerator 45 .
- the acid gas removal unit 42 also includes a mercury guard bed for absorption of mercury.
- Liquid from the RECTISOLTM process in acid gas removal unit 42 and from the shift process in unit 43 is fed via a degassing tank (not shown) to DAF unit 73 a .
- Acid gas from unit 42 is fed to incinerator 45 .
- Absorbed carbon dioxide is regenerated and fed to a CO 2 compressor 47 , which discharges purified carbon dioxide to the atmosphere and also generates contaminated water which is fed via a degassing tank (not shown) to DAF 73 a.
- the syngas output of acid gas removal unit 42 is fed to a shift reactor 43 where the hydrogen content of the syngas is increased.
- Shift reactor 42 communicates with a pressure swing adsorption reactor 44 in which impurities in the hydrogen such as carbon monoxide, carbon dioxide, methane, nitrogen and argon are removed.
- Liquid generated in shift reactor 43 is fed to a degassing tank 72 a and then on to DAF 73 a.
- F-T unit 51 comprises three parallel F-T reactors in a train, each made up of an outer shell (pressure vessel) containing 4 microchannel cores. Each core is made up of multiple vertical and cross-flow microchannels.
- Water generated in the F-T reaction is fed to a steam stripper 71 of a second water treatment assembly T 2 .
- F-T products from the F-T unit 51 are fed to a liquid upgrading unit 61 , which produces high quality naphtha and Synthetic Paraffinic Kerosene (SPK).
- the liquid upgrading unit is configured as a recycle hydrocracker to achieve full conversion of F-T materials while maximizing SPK production. This is achieved by hydrocracking, hydroisomerisation, and hydrotreating, using appropriate catalysts.
- liquid upgrading unit 61 The output of liquid upgrading unit 61 is fed to a fractionator 62 , which generates SPK as the main fuel product. Contaminated water from fractionation 62 is fed to steam stripper 71 .
- the first WWT stream from the Venturi scrubber 31 a is degassed in the degassing tank 72 a .
- This degassing tank operates under vacuum and, as shown in FIG. 4 , is fitted with a multi-tiered cascade system CS to allow gases to escape naturally.
- the degassing tank is fitted with an externally mounted mixer pump MP to prevent suspended solids settling inside the tank.
- the tank is also benched, with the outlet pipework at the lowest point, to prevent solids accumulating in the tank.
- Off-gas is sent to the incinerator 45 , along with other process gases.
- sulphurous gases are incinerated to sulphur dioxide, and this gas is then scrubbed from the incinerator flue with a sodium hydroxide solution before the vent gas is released to atmosphere.
- reaction tank 72 b for oxidation to sodium sulphate in the presence of a cobalt or ferrous catalyst.
- Reaction tank 72 b is aerated by means of a coarse bubble aeration system A ( FIG. 4 ) using two blowers. Aeration allows for the oxidation and precipitation of species such as sulphites/bisulphites, nitrite and arsenic. Neutralisation of the feed is accomplished by dosing of sodium hydroxide. The aeration also mixes the tank effectively.
- the spent caustic solution contains sodium sulphite and sodium bisulphite, and this wastewater is combined with the degassed water from degassing tank 72 a and fed into a reaction tank 72 b where the wastewater streams are both neutralized with sodium hydroxide and oxidized by aeration. Sulphite is converted to sulphate with the aid or a cobalt or ferrous catalyst. Powdered Activated Carbon (PAC) is also dosed (see FIGS. 3 and 4 ) for removal of residual mercaptans following degassing, as well as certain heavy metals, phenols, cresols or other organics that could be present in the water. Cobalt (II) chloride or ferrous chloride catalyst is dosed to catalyse the oxidation of sulphite to sulphate. This tank as well as the subsequent DAF unit 72 c is odour controlled.
- PAC Powdered Activated Carbon
- a heavy metal scavenger (TMT-15 or similar) is dosed, along with coagulant and polymer to improve the capture of heavy metals and suspended solids in the DAF unit.
- An aluminium based coagulant is then added to DAF unit 72 c via an alum dosing pump to facilitate coagulation.
- Washwater from a downstream filtration process, unit 72 d is also fed to the DAF unit 72 c for clarification. It is assumed that the solids in the degassed water are finely divided soot particles, washed from the gasifier overhead product. In order to remove these very fine particles, they must be coagulated into larger flocs for easier removal by clarification and filtration.
- a polymer preferably a polyacrylamide anionic polymer, is added to the DAF unit 72 c by a polymer dosing package (not shown) to facilitate flocculation.
- TMT-15 (1, 3, 5-triazine-2, 4, 6-triathione sodium salt) or similar, is dosed for precipitation of heavy metals, subject to limits in the discharge permits.
- the floc particles are floated to the surface of the DAF unit 72 c .
- the solids form a sludge which is continuously scraped to a sludge hopper (not shown) for transfer to the sludge dewatering centrifuge 72 e which generates sludge cake for disposal.
- Clarified water from the DAF unit 72 c is then pumped to a filtration unit 72 d .
- This provides continuous filtration.
- the type of filtration will be site specific depending on the discharge water quality requirements.
- an ammonia stripping system may be required between the DAF unit 72 c and the filtration unit 72 d .
- Ammonia can be stripped by dosing sodium hydroxide to raise the pH, then counter-current stripping in a packed tower with either air or steam as the stripping medium.
- TDS total dissolved solids
- TDS total dissolved solids
- Sludge from the DAF unit 72 c is dewatered in sludge dewatering centrifuge 72 e , along with PDX slag/water from unit 230 . Centrate from centrifuge 72 e is reprocessed in DAF unit 72 c . Clarified water from DAF unit 72 c is then further polished in a filtration unit 72 d . Ammonia stripping with air or steam may optionally be included here if required by the pollution load and discharge permit conditions. The filters (and stripped) water is then sent to an effluent balancing tank (not shown) where it is blended with other saline streams including cooling water blowdown and softener regeneration brine, before being discharged to a suitable watercourse.
- Salty wastewater from the scrubber unit 31 a (1st WWT) is routed to a degassing tank 72 a operating under vacuum.
- the tank is fitted with a multi-tiered cascade system CS to allow gases to escape naturally.
- the reaction tank 72 a is fitted with an externally mounted mixer pump MP to prevent suspended solids settling inside the tank.
- the tank is also benched, with the outlet pipework at the lowest point, to prevent solids accumulating in the tank.
- a vent from the tank is routed to the incinerator 45 .
- the degassed water is passed forward to reaction tank 72 b for neutralisation, oxidation and adsorption.
- reaction tank 72 b for neutralisation, oxidation and adsorption.
- sulphurous gases are incinerated to sulphur dioxide, and this gas is then scrubbed from the incinerator flue with a sodium hydroxide solution.
- the resulting sodium sulphite/bisulphite solution is also sent to reaction tank 72 b for oxidation to sodium sulphate in the presence of a cobalt or ferrous catalyst.
- Reaction tank 72 b is aerated by means of a coarse bubble aeration system A using two blowers. Aeration allows for the oxidation and precipitation of species such as sulphites/bisulphites, nitrite and arsenic. Neutralisation of the feed is accomplished by dosing of sodium hydroxide. The aeration also mixes the tank effectively.
- Powdered Activated Carbon is also dosed for removal of residual mercaptans following degassing, as well as certain heavy metals, phenols, cresols or other organics that could be present in the water.
- Cobalt (II) chloride or ferrous chloride catalyst is dosed to catalyse the oxidation of sulphite to sulphate. This tank as well as the subsequent DAF unit 72 c is odour controlled.
- first water treatment assembly T 1 The range of selected contaminants that can be dealt with by first water treatment assembly T 1 are given in Table 1 below.
- Process water from F-T unit 51 and fractionation unit 62 are sent to the steam stripper 71 , as noted above.
- the above combined process water feed stream (2nd WWT STREAM) is first preheated and then flows down through a packed/trayed tower stripping section where it is contacted by rising steam.
- the flow of steam is set in ratio to the feed flow.
- the steam volatizes most of the organic content of the feed, yielding a bottoms stream of water with small amounts of hydrocarbons.
- the bottoms stream is arranged to preheat the feed stream.
- the bottoms stream is further cooled in an effluent cooler (not shown).
- the cooled stripped water is sent for further treatment to a DAF unit 73 b via a DAF feed tank 73 a .
- DAF feed tank 73 a receives wastewater streams from compressor 41 , gas removal unit 42 , shift reactor 43 and CO2 compressor 47 . These additional streams are degassed prior to entering the tank, to release entrained gases including carbon dioxide.
- the above DAF assembly removes any remaining free oil from the combined stream, as well as any residual solids.
- the feed is first pH corrected with sodium hydroxide, and subsequently fed into the DAF coagulation zone.
- a coagulant for example aluminium sulphate, is dosed to coagulate the solids and oil droplets into larger particles in order to separate them from the water phase.
- Air for the DAF process is supplied by a dedicated compressor (not shown).
- the air is dissolved under pressure into a recycled water flow in a contactor (not shown) and the aerated water is depressurized as it is mixed with influent feed to produce micro-bubbles of air.
- the bubbles attach to the coagulated particles and float them to the top of the DAF unit 73 b , where they are removed as sludge by a skimmer (not shown), into a built-in sludge hopper (not shown). The sludge is removed off site by tanker.
- Clarified water from the DAF unit 73 b is pumped to a Membrane Bio Reactor (MBR) 73 c which is fed with nutrients and converts organic pollutants to microbiological sludge, which may be transferred to a sewage works or other off-site or on site sludge treatment facilities.
- MLR Membrane Bio Reactor
- the purified water from MBR 73 c is dosed with anti-corrosion, anti-microbial and anti-deposition chemicals at dosing unit 84 a and then fed to a cooling tower 84 b where it is cooled prior to the treated cooling water being fed to units requiring cooling.
- Users of cooling water include:
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Abstract
Description
- The present invention relates to a process for treating wastewater from a gasification process. Gasification processes are used to generate feedstock for Fischer-Tropsch (F-T) processes for the generation of hydrocarbon fuels.
- The Fischer-Tropsch process is widely used to generate fuels from carbon monoxide and hydrogen and can be represented by the equation:
-
(2n+1)H2 +nCO→CnH2n+2 +nH2O - This reaction is highly exothermic and is catalysed by a Fischer-Tropsch catalyst, typically a cobalt-based catalyst, under conditions of elevated temperature (typically at least 180° C., eg 200° C. or above) and pressure (eg at least 10 bar). A product mixture is obtained, and n typically encompasses a range from 10 to 120. It is desirable to minimise methane selectivity, i.e. the proportion of methane (n=1) in the product mixture, and to maximise the selectivity towards C5 and higher (n≥5) paraffins, typically to a level of 90% or higher. It is also desirable to maximise the conversion of carbon monoxide.
- The hydrogen and carbon monoxide feedstock is normally synthesis gas.
- The synthesis gas may be produced by gasifying a carbonaceous material at an elevated temperature, for example, about 700° C. or higher. The carbonaceous material may comprise any carbon-containing material that can be gasified to produce synthesis gas. The carbonaceous material may comprise biomass (e.g., plant or animal matter, biodegradable waste, and the like), a food resource (e.g., as corn, soybean, and the like), and/or a non-food resource such as coal (e.g., low grade coal, high grade coal, clean coal, and the like), oil (e.g., crude oil, heavy oil, tar sand oil, shale oil, and the like), solid waste (e.g., municipal solid waste, hazardous waste), refuse derived fuel (RDF), tyres, petroleum coke, trash, garbage, biogas, sewage sludge, animal waste, agricultural waste (e.g., corn stover, switch grass, grass clippings), construction demolition materials, plastic materials (e.g., plastic waste), cotton gin waste, landfill gas, a mixture of two or more thereof, and the like. The carbonaceous material may also be Solid Recovered Fuel (SRF) which is a waste product of relatively high calorific value typically derived from paper, card, wood, textiles and plastics.
- The fresh synthesis gas may be treated to adjust the molar ratio of H2 to CO by steam reforming (eg, a steam methane reforming (SMR) reaction where methane is reacted with steam in the presence of a steam methane reforming (SMR) catalyst); partial oxidation; autothermal reforming; carbon dioxide reforming; or a combination of two or more thereof. In the present application, such treatment of the synthesis gas is considered to be broadly part of the F-T process and any wastewater streams resulting from such treatment are considered to be wastewater streams from the F-T process rather than from the gasification process as such.
- The molar ratio of H2 to CO in the fresh synthesis gas is desirably in the range from about 1.6:1 to about 2.2:1, or from about 1.8:1 to about 2.10:1, or from about 1.95:1 to about 2.05:1.
- The fresh synthesis gas may optionally be combined with a recycled tail gas (eg a recycled FT tail gas), which also contains H2 and CO, to form a reactant mixture. The tail gas may optionally comprise H2 and CO with a molar ratio of H2 to CO in the range from about 0.5:1 to about 2:1, or from about 0.6:1 to about 1.8:1, or from about 0.7:1 to about 1.2:1.
- The combined FT synthesis gas feed (comprising of fresh synthesis gas combined with recycled tailgas) desirably comprises H2 and CO in a molar ratio in the range from about 1.1 to about 2.1:1, or from about 1.7:1 to about 2.0:1, or from about 1.7:1 to about 1.9:1.
- The invention is concerned particularly but not exclusively with treating wastewater from a gasification process utilising Municipal Solid Waste (MSW) or Commercial and Industrial waste (C & I) as the gasification feedstock, which tends to generate wastewater with high levels of pollutants. The disposal of such wastewater and the removal of such pollutants is of pressing concern.
- There is a demand for disposal of MSW and C & I waste which does not involve landfill.
- There is furthermore a demand for fuel derived from renewable resources. For example, the Renewable Transport Fuel Obligation (RTFO) obligates UK suppliers of road transport fuels (such as refiners and importers) in excess of 450,000 litres annually to use a certain percentage of sustainable biofuels.
- It is known to recycle wastewater from an F-T process.
- Furthermore, it is known, eg from WO 2017/011025A and WO 2017/039741A to treat separate wastewater streams from gasification and F-T processes in a combined gasification and F-T installation utilising MSW as the feedstock. However, these patent applications disclose no details of the wastewater treatment or of the pollutants removed from the wastewater.
- F-T wastewater treatment is disclosed in WO2016193337A1 which discussed pre-treating the waste water by distillation or steam stripping, removing residual wax by gravity and feeding the resulting pretreated waste water to a granular sludge based anaerobic bioreactor. This document pays scant regard to the treatment of salt water streams except by ion exchange or reverse osmosis.
- In one aspect the present invention provides a process for treating wastewater from a combined gasification and Fischer-Tropsch (F-T) process in which aqueous effluent from the gasification is treated with alkali to produce a first wastewater stream and the first wastewater stream is treated to remove inorganic pollutants present in the aqueous effluent, and a second wastewater stream, containing water produced in the F-T process and being distinct from the first wastewater stream, is treated separately from the first wastewater stream to remove organic compounds.
- The treated first wastewater stream may be discharged to the environment. The treated second wastewater stream may be reused within plant utilised in the gasification and/or F-T process.
- Thus, the invention also provides a process for treating wastewater from a combined gasification and Fischer-Tropsch (F-T) process in which aqueous effluent from the gasification is treated with alkali to produce a first wastewater stream and the first wastewater stream is treated to remove inorganic pollutants present in the aqueous effluent, and a second wastewater stream, containing water produced in the F-T process and being distinct from the first wastewater stream, is treated separately from the first wastewater stream to remove organic compounds, wherein the treated first wastewater stream is discharged to the environment and the treated second wastewater stream is reused within plant utilised in the gasification and/or F-T process.
- This has the advantage that the treatment of the wastewater streams is optimised.
- Salty inorganic wastewaters are separately treated from organic laden, non-salty wastewaters. In preferred embodiments, this allows the non-salty (fresh) water to be reused within the facility for cooling water makeup or other resource.
- The first wastewater stream may for example comprise treated aqueous effluent from any one or more of a gasification zone, a partial oxidation zone, a clean-up zone and/or a hydrogen to carbon monoxide ratio shifting zone (e.g. a water gas shift zone).
- In a preferred embodiment there is provided a process for the manufacture of one or more useful products (such as long chain hydrocarbons for example) comprising:
-
- a. gasifying a carbonaceous feedstock, preferably comprising waste materials and/or biomass, in a gasification zone to generate a raw synthesis gas;
- b. optionally partially oxidising the raw synthesis gas in a partial oxidation zone to generate partially oxidised raw synthesis gas;
- c. supplying at least a portion of the, optionally partially oxidised, raw synthesis gas to a clean-up zone to remove contaminants and provide a clean synthesis gas;
- d. optionally shifting the hydrogen to carbon monoxide ratio of the clean synthesis gas in a hydrogen to carbon monoxide ratio shifting zone to generate shifted clean synthesis gas;
- e. supplying the, optionally shifted, clean synthesis gas to an F-T reaction train to generate at least one first useful product;
- f. optionally upgrading the first useful product in a second further reaction train to generate a second useful product,
- wherein aqueous effluent from one or more of stages a. to c. is treated by degassing and subsequent neutralisation and aqueous effluent from stages d and e. (and optionally also stage f.) is separately treated.
- It has been found that the first wastewater stream can normally be economically treated to remove pollutants to satisfy regulatory requirements, even if the feedstock is derived from MSW or C & I waste.
- Preferably the treated first wastewater stream is discharged to the environment.
- Preferably the treatment comprises:
-
- a) degassing, and subsequently
- b) neutralising
- c) preferably clarifying, and
- d) preferably filtering
- the first wastewater stream.
- In a related aspect the invention provides a process for treating wastewater from a combined gasification and Fischer-Tropsch (F-T) process in which aqueous effluent from the gasification is treated with alkali to produce a first wastewater stream and the first wastewater stream is treated to remove inorganic pollutants present in the aqueous effluent, wherein the treatment comprises:
-
- a) degassing, and subsequently
- b) neutralising,
- c) preferably clarifying, and
- d) preferably filtering
- the first wastewater stream.
- The preliminary degassing step reduces the requirement for neutralisation and enhances the economics of the process. Acid gases such as CO2 and SO2 which would otherwise exert a caustic demand are released. This also helps maintain a lower salinity in the final treated effluent.
- Additionally, the wastewater treatment of the present invention, in both its aspects, has been found to be remarkably effective in reducing heavy metal and other pollutants, even when using a relatively dirty feedstock such as MSW or C & I waste.
- Preferably the process comprises the further step:
- c) oxidising dissolved or suspended components of the neutralised first wastewater stream.
- This facilitates removal of heavy metals, as well as reducing the chemical oxidation demand (COD) of the wastewater.
- Preferably the first wastewater stream is neutralised in a reaction zone which is agitated by an oxidising gas (eg air).
- This ensures complete mixing and hence neutralisation and also enables neutralisation and oxidation in one and the same reaction vessel.
- In a preferred embodiment the reaction zone is agitated by bubble aeration in the presence of a catalyst, preferably a cobalt catalyst or a ferrous catalyst, for the oxidation of one or more of: sulphites, nitrites and arsenic compounds.
- Preferably the first wastewater stream is treated with activated carbon (preferably powdered activated carbon) to absorb organic compounds and/or heavy metals.
- This enables a significant reduction of pollutants in an economical fashion.
- Preferably the treated first wastewater stream is subjected to a dissolved air flotation process to separate spent activated carbon and other suspended solids (if present).
- This process complements the treatment with activated carbon. The suspended solids will typically include heavy metal oxides.
- Preferably the first wastewater stream is filtered with a sand filter, multimedia filter or membrane filter, to remove any remaining spent activated carbon and suspended solids (if present).
- This feature enables virtually complete clarification of the wastewater in an economical fashion.
- Preferably the first wastewater stream is treated with a coagulating agent, preferably an aluminium or iron-based coagulant and/or a flocculation-promoting polymer, to assist in the removal of suspended solids.
- This feature is particularly advantageous in combination with dissolved air flotation because it agglomerates the small particles in the effluent and assists their removal by the dissolved air flotation. The coagulant also assists in the capture of heavy metals.
- Preferably the first wastewater stream is subject to an air or steam stripping process, preferably under alkaline conditions, to remove ammonia. The stripped ammonia is captured and reused within the facility.
- Preferably the first wastewater stream is treated with a sulphide compound. The sulphide may be an inorganic sulphide such as sodium sulphide for example, or an organic sulphide compound, preferably a heteroaromatic sulphide, most preferably an S-triazine sulphide salt, to precipitate heavy metals.
- These last two features are particularly advantageous in combination when the first wastewater stream is made alkaline, because this reduces still further the solubility of precipitated heavy metal complexes.
- The invention also provides a plant configured to operate the process disclosed herein. The plant may be a combined gasification and Fischer-Tropsch (F-T) plant.
- Other preferred features are defined in the dependent claims.
- All the preferred features can be combined in any combination.
- Preferably the preferred process steps and combinations thereof are performed in the order stated above.
- A preferred embodiment of the invention is described below by way of example only with reference to
FIGS. 1 to 4 of the accompanying drawings, wherein: -
FIG. 1 is a schematic diagram of a Feedstock Conditioning Facility used to process MSW or C & I waste to a feedstock for a combined gasification and F-T process; -
FIG. 2 is a schematic diagram of a combined gasification and F-T process utilising the feedstock generated by the FCF ofFIG. 1 ; -
FIG. 3 is a schematic diagram of the unit T1 (apparatus 72 a-72 e) used for treatment of the 1st WWT (Wastewater) stream inFIG. 1 , and -
FIG. 4 is a schematic diagram showing the degassing tank and reaction tank arrangement of unit T1 in more detail. - Referring to
FIG. 1 , the FCF shown receives bagged C&I and MSW Waste from a bunker (not shown) from which the bags of waste are transferred to abag splitter 1. - The waste from
bag splitter 1 is fed to a vibration conveyor c1 which passes beneath a belt magnet 2 and aneddy current rotor 3 which remove ferrous and non-ferrous metals respectively. - Oversized items are also removed at this stage.
- The processed waste then passes to a
density separator 4 which removes high density materials such as glass and rubble which are not combustible. - The processed waste is then transferred by a conveyor c2 to
fine shredder 5 which reduces the particle size to 25 mm or less. - The size-reduced waste is then transferred by a conveyor c3 to a
belt dryer 4 where excess moisture is removed. The dried waste (typical moisture content 10 wt %) is then transferred by a conveyor c4 to abunker 7. -
Bunker 7 also receives Solid Recovered Fuel (SRF) which is a waste product of somewhat higher calorific value than MSW and C&I waste and is typically derived from paper, card, wood, textiles and plastics. - The combined material from
bunker 7 is then transferred by a crane to conveyor assembly c7, which feeds the processed feedstock abaler 8. - Gasification
- Referring now to
FIG. 2 , baled feedstock frombaler 8 is fed to afeeder 12, which pressurises the feedstock to reactor pressure and feeds it to agasifier 21 of a reactor assembly R. - Reactor assembly R further comprises a partial oxidation (POx)
reactor 22 and aradiant cooler 23. - The
gasifier 21 comprises a steam reforming reactor incorporating a deep fluidised bed, the bed operating temperature being typically 600-800° C. The fluidised bed is fluidised with superheated steam and causes the carbonaceous material of the feedstock to pyrolyse and react with the steam to form hydrogen, carbon monoxide and carbon dioxide. - The syngas product of
gasifier 21 is fed topartial oxidation reactor 22, which also receives F-T tailgas from anF-T reactor 51 and also oxygen.Reactor 22 is operated at a temperature above the ash melting point at a sufficient residence time to convert tars and oils and methane in the syngas to carbon oxides, hydrogen and water. - The syngas output of
partial oxidation reactor 22 is fed to a cooler 23 which comprises radiant and convective cooler units.Reactor 22 also generates molten ash which is solidified in cooler 23. - The HRSG (heat recovery steam generator) has a blowdown stream of water which contains slag particles from the gasifier and PDX. The concentration of suspended solids is relatively high in this stream and it is therefore sent directly to the
sludge dewatering centrifuge 72 e (centrifuge rather than cyclone) for removal of the bulk of the solids before the liquid phase is co-treated with the rest of the salty water. - The cooled syngas from cooler 23 is fed to a
Venturi scrubber 31 a of a gas cleanup unit C, which further comprises an acidgas removal unit 31 b, acompressor 41 and an acidgas removal unit 42. - Particulate matter is removed in
Venturi scrubber 31 a, and the resulting scrubbed syngas is passed to ahalide removal unit 31 b.Halide removal unit 31 b comprises a packed column over which sodium hydroxide solution is passed to absorb hydrogen chloride, bromide and fluoride. The resulting 1st wastewater (WWT) stream, containing halide salts, is passed to adegassing tank 72 a of a first water treatment assembly T1. - The syngas output of
halide removal unit 31 b is compressed in acompressor 41 and then cooled, condensing liquid (wastewater) which is then removed from the syngas and fed to a degassing tank and then on to Dissolved Air Flotation (DAF)unit 73 a, discussed below. - The compressed syngas from
compressor 41 is fed to acidgas removal unit 42, which operates at low temperature and high pressure and uses methanol as a solvent for removal of hydrogen sulphide, carbonyl sulphide, carbon dioxide and trace impurities such as hydrogen cyanide, ammonia, formic acid and metal carbonyls which might otherwise be detrimental to the downstream process units, in particular by poisoning the F-T catalyst.Unit 42 preferably utilises the RECTISOL™ process. The dissolved impurities are removed from the methanol solvent by stepwise flashing and are passed to anincinerator 45. The acidgas removal unit 42 also includes a mercury guard bed for absorption of mercury. - Liquid from the RECTISOL™ process in acid
gas removal unit 42 and from the shift process inunit 43 is fed via a degassing tank (not shown) toDAF unit 73 a. Acid gas fromunit 42 is fed toincinerator 45. - Absorbed carbon dioxide is regenerated and fed to a CO2 compressor 47, which discharges purified carbon dioxide to the atmosphere and also generates contaminated water which is fed via a degassing tank (not shown) to
DAF 73 a. - The syngas output of acid
gas removal unit 42 is fed to ashift reactor 43 where the hydrogen content of the syngas is increased.Shift reactor 42 communicates with a pressureswing adsorption reactor 44 in which impurities in the hydrogen such as carbon monoxide, carbon dioxide, methane, nitrogen and argon are removed. Liquid generated inshift reactor 43 is fed to adegassing tank 72 a and then on toDAF 73 a. - F-T Synthesis
- The syngas from
reactor 43 is fed via aguard bed 48 to a Fischer-Tropsch unit 51.F-T unit 51 comprises three parallel F-T reactors in a train, each made up of an outer shell (pressure vessel) containing 4 microchannel cores. Each core is made up of multiple vertical and cross-flow microchannels. - Water generated in the F-T reaction is fed to a
steam stripper 71 of a second water treatment assembly T2. - F-T products from the
F-T unit 51 are fed to aliquid upgrading unit 61, which produces high quality naphtha and Synthetic Paraffinic Kerosene (SPK). The liquid upgrading unit is configured as a recycle hydrocracker to achieve full conversion of F-T materials while maximizing SPK production. This is achieved by hydrocracking, hydroisomerisation, and hydrotreating, using appropriate catalysts. - The output of
liquid upgrading unit 61 is fed to afractionator 62, which generates SPK as the main fuel product. Contaminated water fromfractionation 62 is fed to steamstripper 71. - Treatment of 1st WWT
- Referring to
FIGS. 2, 3 and 4 , the first WWT stream from theVenturi scrubber 31 a is degassed in thedegassing tank 72 a. This degassing tank operates under vacuum and, as shown inFIG. 4 , is fitted with a multi-tiered cascade system CS to allow gases to escape naturally. The degassing tank is fitted with an externally mounted mixer pump MP to prevent suspended solids settling inside the tank. The tank is also benched, with the outlet pipework at the lowest point, to prevent solids accumulating in the tank. - Off-gas is sent to the
incinerator 45, along with other process gases. In theincinerator 45, sulphurous gases are incinerated to sulphur dioxide, and this gas is then scrubbed from the incinerator flue with a sodium hydroxide solution before the vent gas is released to atmosphere. - The resulting sodium sulphite/bisulphite solution is also sent to
reaction tank 72 b for oxidation to sodium sulphate in the presence of a cobalt or ferrous catalyst.Reaction tank 72 b is aerated by means of a coarse bubble aeration system A (FIG. 4 ) using two blowers. Aeration allows for the oxidation and precipitation of species such as sulphites/bisulphites, nitrite and arsenic. Neutralisation of the feed is accomplished by dosing of sodium hydroxide. The aeration also mixes the tank effectively. - The spent caustic solution contains sodium sulphite and sodium bisulphite, and this wastewater is combined with the degassed water from degassing
tank 72 a and fed into areaction tank 72 b where the wastewater streams are both neutralized with sodium hydroxide and oxidized by aeration. Sulphite is converted to sulphate with the aid or a cobalt or ferrous catalyst. Powdered Activated Carbon (PAC) is also dosed (seeFIGS. 3 and 4 ) for removal of residual mercaptans following degassing, as well as certain heavy metals, phenols, cresols or other organics that could be present in the water. Cobalt (II) chloride or ferrous chloride catalyst is dosed to catalyse the oxidation of sulphite to sulphate. This tank as well as thesubsequent DAF unit 72 c is odour controlled. - Flows then pass to a DAF (dissolved air flotation)
unit 72 c. A heavy metal scavenger (TMT-15 or similar) is dosed, along with coagulant and polymer to improve the capture of heavy metals and suspended solids in the DAF unit. An aluminium based coagulant is then added toDAF unit 72 c via an alum dosing pump to facilitate coagulation. - Washwater from a downstream filtration process,
unit 72 d, is also fed to theDAF unit 72 c for clarification. It is assumed that the solids in the degassed water are finely divided soot particles, washed from the gasifier overhead product. In order to remove these very fine particles, they must be coagulated into larger flocs for easier removal by clarification and filtration. - A polymer, preferably a polyacrylamide anionic polymer, is added to the
DAF unit 72 c by a polymer dosing package (not shown) to facilitate flocculation. - TMT-15 (1, 3, 5-triazine-2, 4, 6-triathione sodium salt) or similar, is dosed for precipitation of heavy metals, subject to limits in the discharge permits. The floc particles are floated to the surface of the
DAF unit 72 c. The solids form a sludge which is continuously scraped to a sludge hopper (not shown) for transfer to thesludge dewatering centrifuge 72 e which generates sludge cake for disposal. - Clarified water from the
DAF unit 72 c is then pumped to afiltration unit 72 d. This provides continuous filtration. The type of filtration will be site specific depending on the discharge water quality requirements. - Depending on ammonia loading in the wastewater and the relevant discharge permits, an ammonia stripping system may be required between the
DAF unit 72 c and thefiltration unit 72 d. Ammonia can be stripped by dosing sodium hydroxide to raise the pH, then counter-current stripping in a packed tower with either air or steam as the stripping medium. - The high total dissolved solids (TDS) levels of the filtrate precludes its recycling as cooling water make up. Filtrate is therefore discharged via an effluent balancing tank (not shown). Here it is blended with other salty waste streams such as ion exchange softener regeneration brine and cooling tower blowdown.
- The high total dissolved solids (TDS) levels of the filtrate precludes its recycling as cooling water make up. Filtrate is therefore discharged via an effluent balancing tank (not shown). Here it is blended with other salty waste streams such as ion exchange softener regeneration brine and cooling tower blowdown. In this manner the treated water from the
filtration unit 72 d is safely discharged to the environment. - Sludge from the
DAF unit 72 c is dewatered insludge dewatering centrifuge 72 e, along with PDX slag/water from unit 230. Centrate fromcentrifuge 72 e is reprocessed inDAF unit 72 c. Clarified water fromDAF unit 72 c is then further polished in afiltration unit 72 d. Ammonia stripping with air or steam may optionally be included here if required by the pollution load and discharge permit conditions. The filters (and stripped) water is then sent to an effluent balancing tank (not shown) where it is blended with other saline streams including cooling water blowdown and softener regeneration brine, before being discharged to a suitable watercourse. - Salty wastewater from the
scrubber unit 31 a (1st WWT) is routed to adegassing tank 72 a operating under vacuum. Referring again toFIG. 4 , the tank is fitted with a multi-tiered cascade system CS to allow gases to escape naturally. - The
reaction tank 72 a is fitted with an externally mounted mixer pump MP to prevent suspended solids settling inside the tank. The tank is also benched, with the outlet pipework at the lowest point, to prevent solids accumulating in the tank. - A vent from the tank is routed to the
incinerator 45. The degassed water is passed forward toreaction tank 72 b for neutralisation, oxidation and adsorption. In theincinerator 45, sulphurous gases are incinerated to sulphur dioxide, and this gas is then scrubbed from the incinerator flue with a sodium hydroxide solution. The resulting sodium sulphite/bisulphite solution is also sent toreaction tank 72 b for oxidation to sodium sulphate in the presence of a cobalt or ferrous catalyst. -
Reaction tank 72 b is aerated by means of a coarse bubble aeration system A using two blowers. Aeration allows for the oxidation and precipitation of species such as sulphites/bisulphites, nitrite and arsenic. Neutralisation of the feed is accomplished by dosing of sodium hydroxide. The aeration also mixes the tank effectively. - Powdered Activated Carbon (PAC) is also dosed for removal of residual mercaptans following degassing, as well as certain heavy metals, phenols, cresols or other organics that could be present in the water. Cobalt (II) chloride or ferrous chloride catalyst is dosed to catalyse the oxidation of sulphite to sulphate. This tank as well as the
subsequent DAF unit 72 c is odour controlled. - The range of selected contaminants that can be dealt with by first water treatment assembly T1 are given in Table 1 below.
-
TABLE 1 Stream 310-102, Gas 450-106, Clean-up Spent POX wastewater Caustic Slag/Water Total suspended 2,000-20,000 0-100 100,000-500,000 solids, mg/l Total Organic 1-100 1-10 N/A Carbon, mg/l Chemical oxygen 10-1,000 5,000-20,000 N/A demand, mg/l Halides, mg/l 2,000-20,000 0-200 2,000-20,000 Phosphorus, mg/l 0-20 0-20 0-20 Hydrogen sulphide, 100-1,000 5,000-30,000 100-1,000 sulphur dioxide, sulphite ion and bisulphite ion, mg/l as S Ammonia as N, mg/l 20-200 0-10 1,000-50,000 Heavy metals*, mg/l 1-100 0-2 10-100 *Includes As, Hg, Ni, Cd, Cu, Pb, Cr, Co, Ga, Mo, V and Zn - Treatment of 2nd WWT
- Process water from
F-T unit 51 andfractionation unit 62 are sent to thesteam stripper 71, as noted above. - The above combined process water feed stream (2nd WWT STREAM) is first preheated and then flows down through a packed/trayed tower stripping section where it is contacted by rising steam. The flow of steam is set in ratio to the feed flow. The steam volatizes most of the organic content of the feed, yielding a bottoms stream of water with small amounts of hydrocarbons. The bottoms stream is arranged to preheat the feed stream. The bottoms stream is further cooled in an effluent cooler (not shown).
- The cooled stripped water is sent for further treatment to a
DAF unit 73 b via aDAF feed tank 73 a.DAF feed tank 73 a receives wastewater streams fromcompressor 41,gas removal unit 42, shiftreactor 43 andCO2 compressor 47. These additional streams are degassed prior to entering the tank, to release entrained gases including carbon dioxide. - The above DAF assembly removes any remaining free oil from the combined stream, as well as any residual solids.
- The feed is first pH corrected with sodium hydroxide, and subsequently fed into the DAF coagulation zone. A coagulant, for example aluminium sulphate, is dosed to coagulate the solids and oil droplets into larger particles in order to separate them from the water phase.
- Air for the DAF process is supplied by a dedicated compressor (not shown). The air is dissolved under pressure into a recycled water flow in a contactor (not shown) and the aerated water is depressurized as it is mixed with influent feed to produce micro-bubbles of air. The bubbles attach to the coagulated particles and float them to the top of the
DAF unit 73 b, where they are removed as sludge by a skimmer (not shown), into a built-in sludge hopper (not shown). The sludge is removed off site by tanker. - Clarified water from the
DAF unit 73 b is pumped to a Membrane Bio Reactor (MBR) 73 c which is fed with nutrients and converts organic pollutants to microbiological sludge, which may be transferred to a sewage works or other off-site or on site sludge treatment facilities. - The purified water from
MBR 73 c is dosed with anti-corrosion, anti-microbial and anti-deposition chemicals atdosing unit 84 a and then fed to acooling tower 84 b where it is cooled prior to the treated cooling water being fed to units requiring cooling. - Users of cooling water include:
-
- ash handling (not shown)
-
gasifier 21 - gas cleanup unit C
- shift
reactor 43 -
incinerator 45 -
F-T unit 51 -
fractionation 62 - wastewater treatment units T1 and T2.
Claims (22)
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WO2012151605A1 (en) * | 2011-05-11 | 2012-11-15 | Linc Energy Ltd | Conditioning of syngas from underground coal gasification |
WO2016044348A1 (en) * | 2014-09-15 | 2016-03-24 | Velocys Technologies, Ltd. | Methods of making purified water from the fischer-tropsch process |
WO2016193337A1 (en) * | 2015-06-04 | 2016-12-08 | Shell Internationale Research Maatschappij B.V. | Method of treating water coming from a fischer-tropsch reactor |
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