GB2620645A - Process - Google Patents
Process Download PDFInfo
- Publication number
- GB2620645A GB2620645A GB2210917.7A GB202210917A GB2620645A GB 2620645 A GB2620645 A GB 2620645A GB 202210917 A GB202210917 A GB 202210917A GB 2620645 A GB2620645 A GB 2620645A
- Authority
- GB
- United Kingdom
- Prior art keywords
- process according
- sulfur
- bio
- products
- feedstock
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 101
- 239000002028 Biomass Substances 0.000 claims abstract description 37
- 230000002906 microbiologic effect Effects 0.000 claims abstract description 21
- 150000002632 lipids Chemical class 0.000 claims abstract description 16
- 238000006243 chemical reaction Methods 0.000 claims abstract description 14
- 230000003647 oxidation Effects 0.000 claims abstract description 7
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 7
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 144
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 72
- 239000001569 carbon dioxide Substances 0.000 claims description 70
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 52
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 43
- 229910052799 carbon Inorganic materials 0.000 claims description 43
- 239000007788 liquid Substances 0.000 claims description 42
- 229910052717 sulfur Inorganic materials 0.000 claims description 39
- 239000011593 sulfur Substances 0.000 claims description 39
- 241000894006 Bacteria Species 0.000 claims description 26
- 230000000813 microbial effect Effects 0.000 claims description 18
- 238000010521 absorption reaction Methods 0.000 claims description 17
- 239000000126 substance Substances 0.000 claims description 17
- 239000003153 chemical reaction reagent Substances 0.000 claims description 14
- 239000012738 dissolution medium Substances 0.000 claims description 12
- 239000012530 fluid Substances 0.000 claims description 9
- 239000000446 fuel Substances 0.000 claims description 6
- 241000294064 Guyparkeria Species 0.000 claims description 5
- 241000605261 Thiomicrospira Species 0.000 claims description 5
- 229920000903 polyhydroxyalkanoate Polymers 0.000 claims description 5
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 4
- 241000916424 Alkalilimnicola Species 0.000 claims description 2
- 241001674396 Alkalispirillum Species 0.000 claims description 2
- 241000865990 Desulfurispirillum Species 0.000 claims description 2
- 241001523679 Desulfuromusa Species 0.000 claims description 2
- 241001248482 Ectothiorhodospiraceae Species 0.000 claims description 2
- 241000206596 Halomonas Species 0.000 claims description 2
- 241001141205 Thioalkalispira Species 0.000 claims description 2
- 241001528280 Thioalkalivibrio Species 0.000 claims description 2
- 241000605118 Thiobacillus Species 0.000 claims description 2
- 241000607598 Vibrio Species 0.000 claims description 2
- 238000005119 centrifugation Methods 0.000 claims description 2
- 239000012141 concentrate Substances 0.000 claims description 2
- 238000012544 monitoring process Methods 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 238000000638 solvent extraction Methods 0.000 claims description 2
- 208000037534 Progressive hemifacial atrophy Diseases 0.000 claims 1
- 241001430267 Rhodobacteraceae Species 0.000 claims 1
- 239000003513 alkali Substances 0.000 claims 1
- 238000012017 passive hemagglutination assay Methods 0.000 claims 1
- 239000007789 gas Substances 0.000 description 87
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 51
- 239000000047 product Substances 0.000 description 51
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 44
- 229910001868 water Inorganic materials 0.000 description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 20
- 238000004519 manufacturing process Methods 0.000 description 19
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 18
- 239000003546 flue gas Substances 0.000 description 17
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 15
- 239000000203 mixture Substances 0.000 description 13
- 239000000463 material Substances 0.000 description 10
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000006096 absorbing agent Substances 0.000 description 8
- 244000005700 microbiome Species 0.000 description 8
- 235000015097 nutrients Nutrition 0.000 description 7
- 238000006477 desulfuration reaction Methods 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 239000003570 air Substances 0.000 description 5
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 239000002551 biofuel Substances 0.000 description 5
- WERYXYBDKMZEQL-UHFFFAOYSA-N butane-1,4-diol Chemical compound OCCCCO WERYXYBDKMZEQL-UHFFFAOYSA-N 0.000 description 5
- 150000001720 carbohydrates Chemical class 0.000 description 5
- 235000014633 carbohydrates Nutrition 0.000 description 5
- 239000007795 chemical reaction product Substances 0.000 description 5
- 150000001875 compounds Chemical class 0.000 description 5
- 230000001965 increasing effect Effects 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 239000000243 solution Substances 0.000 description 5
- 239000002904 solvent Substances 0.000 description 5
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 4
- 239000007864 aqueous solution Substances 0.000 description 4
- 238000011143 downstream manufacturing Methods 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 230000014759 maintenance of location Effects 0.000 description 4
- 239000005014 poly(hydroxyalkanoate) Substances 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 125000003396 thiol group Chemical group [H]S* 0.000 description 4
- BVKZGUZCCUSVTD-UHFFFAOYSA-M Bicarbonate Chemical class OC([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-M 0.000 description 3
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 239000002253 acid Substances 0.000 description 3
- 239000012080 ambient air Substances 0.000 description 3
- 150000001412 amines Chemical class 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 230000001419 dependent effect Effects 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000003337 fertilizer Substances 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 2
- 229920000331 Polyhydroxybutyrate Polymers 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 150000001298 alcohols Chemical class 0.000 description 2
- 238000001311 chemical methods and process Methods 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 231100001261 hazardous Toxicity 0.000 description 2
- 239000003295 industrial effluent Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 229910052698 phosphorus Inorganic materials 0.000 description 2
- 239000005015 poly(hydroxybutyrate) Substances 0.000 description 2
- 102000004169 proteins and genes Human genes 0.000 description 2
- 108090000623 proteins and genes Proteins 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- 230000009919 sequestration Effects 0.000 description 2
- 241000894007 species Species 0.000 description 2
- 230000001954 sterilising effect Effects 0.000 description 2
- 238000004659 sterilization and disinfection Methods 0.000 description 2
- 150000003568 thioethers Chemical class 0.000 description 2
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical class [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- 102000003846 Carbonic anhydrases Human genes 0.000 description 1
- 108090000209 Carbonic anhydrases Proteins 0.000 description 1
- 102000004190 Enzymes Human genes 0.000 description 1
- 108090000790 Enzymes Proteins 0.000 description 1
- BDAGIHXWWSANSR-UHFFFAOYSA-M Formate Chemical compound [O-]C=O BDAGIHXWWSANSR-UHFFFAOYSA-M 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000012670 alkaline solution Substances 0.000 description 1
- 150000001413 amino acids Chemical class 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 150000003863 ammonium salts Chemical class 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- 230000003115 biocidal effect Effects 0.000 description 1
- 239000003139 biocide Substances 0.000 description 1
- 239000003225 biodiesel Substances 0.000 description 1
- 239000007844 bleaching agent Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000004098 cellular respiration Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000001627 detrimental effect Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 230000029087 digestion Effects 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 1
- 238000010353 genetic engineering Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000003116 impacting effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- -1 industrial Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- 239000002609 medium Substances 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 150000007523 nucleic acids Chemical group 0.000 description 1
- 239000002417 nutraceutical Substances 0.000 description 1
- 235000021436 nutraceutical agent Nutrition 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000011368 organic material Substances 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 239000013618 particulate matter Substances 0.000 description 1
- 230000037361 pathway Effects 0.000 description 1
- 235000020030 perry Nutrition 0.000 description 1
- 239000000825 pharmaceutical preparation Substances 0.000 description 1
- 229940127557 pharmaceutical product Drugs 0.000 description 1
- 230000000243 photosynthetic effect Effects 0.000 description 1
- 229920000218 poly(hydroxyvalerate) Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 239000002243 precursor Substances 0.000 description 1
- 235000019624 protein content Nutrition 0.000 description 1
- 235000005974 protein supplement Nutrition 0.000 description 1
- 229940116540 protein supplement Drugs 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
- 235000000346 sugar Nutrition 0.000 description 1
- 150000008163 sugars Chemical class 0.000 description 1
- 150000003505 terpenes Chemical class 0.000 description 1
- 150000003573 thiols Chemical class 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/64—Fats; Fatty oils; Ester-type waxes; Higher fatty acids, i.e. having at least seven carbon atoms in an unbroken chain bound to a carboxyl group; Oxidised oils or fats
- C12P7/6436—Fatty acid esters
- C12P7/6445—Glycerides
- C12P7/6463—Glycerides obtained from glyceride producing microorganisms, e.g. single cell oil
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P1/00—Preparation of compounds or compositions, not provided for in groups C12P3/00 - C12P39/00, by using microorganisms or enzymes
- C12P1/04—Preparation of compounds or compositions, not provided for in groups C12P3/00 - C12P39/00, by using microorganisms or enzymes by using bacteria
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
- B01D53/526—Mixtures of hydrogen sulfide and carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/84—Biological processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
- C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- C12P7/00—Preparation of oxygen-containing organic compounds
- C12P7/62—Carboxylic acid esters
- C12P7/625—Polyesters of hydroxy carboxylic acids
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12Y—ENZYMES
- C12Y108/00—Oxidoreductases acting on sulfur groups as donors (1.8)
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/95—Specific microorganisms
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/302—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/05—Biogas
-
- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12R—INDEXING SCHEME ASSOCIATED WITH SUBCLASSES C12C - C12Q, RELATING TO MICROORGANISMS
- C12R2001/00—Microorganisms ; Processes using microorganisms
- C12R2001/01—Bacteria or Actinomycetales ; using bacteria or Actinomycetales
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Health & Medical Sciences (AREA)
- Zoology (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Biomedical Technology (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Analytical Chemistry (AREA)
- Biochemistry (AREA)
- General Engineering & Computer Science (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Microbiology (AREA)
- Biotechnology (AREA)
- Sustainable Development (AREA)
- Cell Biology (AREA)
- Mycology (AREA)
- Molecular Biology (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Carbon And Carbon Compounds (AREA)
- Treating Waste Gases (AREA)
- Apparatus Associated With Microorganisms And Enzymes (AREA)
Abstract
A microbiological process and apparatus suitable for the conversion of CO2 into a bioproduct such as biomass, lipid, PHA, BDO, in a bioreactor 12. Energy required for the conversion is at least partially provided by concomitant oxidation of a sulfurous feedstock such as H2S
Description
PROCESS
TECHNICAL FIELD
The present invention relates to chemotrophic carbon capture and desulfurization and concerns a combined process of bio-desulfurization and carbon capture utilising chemotrophs to produce one or more bio-products.
Bio-desulfurization is a known process for removing sulfur/sulfides from gas streams (e.g. natural gas, associated gas, syngas, amine acid gas, flue gas, landfill gas, biogas, effluent from anaerobic digesters), and also from liquid streams such as diesel and crude oil. The primary or sole focus of conventional bio-desulfurization processes is the removal of sulfur (e.g. H25). Such processes are not typically concerned with carbon capture -either at all or with conditions desirable for its optimization. In fact, conventional bio-desulfurization processes such as the Thiopaq 08LG Process generally seek to minimize the amount of biomass build-up (carbon capture) for ease of operation of the bio-desulfurization process.
BACKGROUND TO THE INVENTION
US 11,091,781 and US 10,597,681 disclose systems and methods for fixing carbon using bacteria. The systems include a reaction chamber with a solution contained therein. The solution may include hydrogen, carbon dioxide, bioavailable nitrogen, and a chemolithoautotrophic bacteria. The system may also include a pair of electrodes that split water contained within the solution to form the hydrogen. Additionally, the system may be operated so that a concentration of the bioavailable nitrogen in the solution is below a threshold nitrogen concentration to cause the chemolithoautotrophic bacteria to produce a product.
US 2022/0154228 discloses compositions and methods for a hybrid biological and chemical process that captures and converts carbon dioxide and/or other forms of inorganic carbon and/or Cl carbon sources and/or mixtures containing Cl chemicals into organic chemicals including biofuels or other valuable biomass, chemical, industrial, or pharmaceutical products.
US 9,957,534 discloses microorganisms containing exogenous or heterologous nucleic acid sequences, wherein the microorganisms are capable of growing on gaseous carbon dioxide, gaseous hydrogen, syngas, or combinations thereof. In some embodiments the microorganisms are chemotrophic bacteria that produce or secrete at least 10% of lipid by weight. Also disclosed are methods of fixing gaseous carbon into organic carbon molecules useful for industrial processes, and methods of manufacturing chemicals or producing precursors to chemicals useful in fuels.
US 1Q507,426 and US 9,764,279 disclose methods and systems to achieve clean fuel processing systems in which carbon dioxide emissions from sources may be processed in at least one processing reactor containing a plurality of chemoautotrophic bacteria which can convert the carbon dioxide emissions into biomass which may then be used for various products such as biofuels, fertilizer, or feedstocks. Sulfate-reducing bacteria may be used to supply sulfur containing compounds to the chemoautotrophic bacteria.
US 10,376,837 discloses methods and systems to achieve clean fuel processing systems in which carbon dioxide emissions from sources may be processed in at least one processing reactor containing a plurality of chemoautotrophic bacteria which can convert the carbon dioxide emissions into biomass which may then be used for various products such as biofuels, fertilizer, or feedstocks. Bacteria that reduce oxidized nitrogenous species may be used to supply reduced nitrogenous compounds to the chemoautotrophic bacteria.
US 10,543,458 discloses a process to treat a gas comprising hydrogen sulfide and mercaptans, comprising the steps: (a) contacting the hydrogen sulfide and mercaptans comprising gas with an aqueous solution comprising sulfide-oxidising bacteria thereby obtaining a loaded aqueous solution and a gas having a lower content of hydrogen sulfide and mercaptans, (b) contacting the loaded aqueous solution with mercaptan reducing microorganisms immobilized on a carrier under anaerobic conditions, (c) separating the aqueous solution obtained in step (b) from the mercaptan reducing microorganisms to obtain a first liquid effluent, and (d) contacting the first liquid effluent with an oxidant to regenerate the sulfide-oxidising bacteria to obtain a second liquid effluent comprising regenerated sulfide-oxidising bacteria. The sulfide-oxidising bacteria as present in step (a) are comprised of regenerated sulfide-oxidising bacteria obtained in step (d).
US 10,801,045 discloses pathways, mechanisms, systems and methods to confer chemoautotrophic production of carbon-based products, such as sugars, alcohols, chemicals, amino acids, polymers, fatty acids and their derivatives, hydrocarbons, isoprenoids, and intermediates thereof, in organisms such that these organisms efficiently convert inorganic carbon to organic carbon-based products of interest using inorganic energy, such as formate, and the use of organisms for the commercial production of various carbon-based products.
The prior art is primarily concerned with either removal of sulfur (e.g. H2S) or CO2 capture and/or utilisation. The prior art fails to provide a process where carbon capture is linked with sulfur removal.
In a process for producing one or more bio-products comprising of capturing carbon dioxide (CO2), the removal of further impurities such as hydrogen sulfide (H2S) results in the production of an improved product. None of the prior art documents contain any satisfactory teaching as to how to remove H2S in combination with such a process where carbon is captured using a microorganism.
SUMMARY OF THE INVENTION
The object of the present invention is to provide an improved process for capturing carbon dioxide to produce one or more bio-products, in which sulfur (e.g. H2S) is also removed and utlilized, unlike in conventional processes in the art In this specification one or more bio-products means one or more products derived from organic material available on a renewable or recyclable basis, and may include materials, chemicals and energy. Specific examples of bio-products include, but are not limited to, biomass, biochemicals, lipids, carbohydrates, and alcohols, and include polyhydroxyalkanoates, polyhydroxybutyrates, polyhydroxyvalerates and the like.
A further object of the present invention is to provide a system for carrying out the improved process that is efficient when compared to conventional methods, that is capable of enhancing bio-product production, and that allows control of bio-product composition.
According to the present invention there is provided a microbiological process for the conversion of CO2 into one or more bio-products, in which the energy required for the microbiological conversion is at least partially provided by the concomitant microbiological oxidation of a sulfurous feedstock.
The microbiological process is preferably effected by one or more chemotrophic organisms.
Preferably one or more of the chemotrophic organisms are sulfur oxidising bacteria.
Preferably the sulfurous feedstock is at least partially oxidized to elemental sulfur by the sulfur oxidising bacteria.
Chemotrophic organisms may be provided as a single genus, species and or strain. Consortia of different organisms may also be used. The organisms may be aerobic, anaerobic, facultatively or otherwise.
The invention finds utilization in any industrial process in which both sulfide (or sulfanyl -typically primarily H25 but also mercaptans/thiols etc. may be envisaged) and CO2 are present. The process of the invention can be applied in downstream facilities such as refineries and chemical plants, midstream facilities such as acid gas treatment plant and acid gas injection wells, and upstream industry such as sour oil and gas wells, biogas and landfill gas facilities. The operators of such facilities when utilising the process of the invention may benefit from regulatory/governmental incentives with respect to carbon sequestration, and also stand to achieve effective desulfurisation without resort to capital-intensive and operationally complex Claus units and processes.
Therefore the present invention provides a microbiological process in accordance with the foregoing comprising the steps of: i. contacting raw carbon dioxide and sulfur-containing feedstocks, either separately or in combination, with an absorption or dissolution medium to form a reagent stream comprising dissolved or absorbed inorganic carbon and sulfur; and contacting at least a portion of the reagent stream with a microbial broth in a bioreactor to oxidize sulfur and produce one or more bio-products from the carbon dioxide.
The dissolved or absorbed inorganic carbon is typically provided in the form of a bicarbonate or carbonate (preferably at least mostly bicarbonate).
The dissolved or absorbed inorganic sulfur is typically provided in the form of a sulfide, sulfhydryl or sulfanyl (most commonly sulfhydryl -e.g. NaSH).
The process of the invention may make use of the pH control taught in our co-pending but currently unpublished application USSN 63364275 filed May 6, 2022-the entire disclosure of which is hereby incorporated by reference.
The process of the invention may further comprise: separating the one or more bio-products into one or more bio-products and a liquid stream; and iv. recycling at least a portion of the liquid stream to step i. of the process for use as, or part of, the absorption or dissolution medium A key advantage of the present invention is combined CO2 capture and sulfur removal in a single process which can both abate greenhouse gas emissions, as well as safely remediate hazardous sulfurous streams.
As is well known, carbon dioxide (CO2) is a common greenhouse gas emission, produced by burning fuels. Conventional methods of carbon capture include photosynthetic approaches, and sequestration in oil deposits. Hydrogen sulfide (H2S) is a highly hazardous gas, which is toxic to humans and inhibits cellular respiration. Conventionally H2S is removed from fuel gases by amine gas treating technology, where it is converted to an ammonium salt, and subsequently to elemental sulfur.
Linking carbon capture with H2S removal has a distinct advantage in that oxidation of H2S to elemental sulfur provides the electrons and energy needed for carbon fixation, reducing the overall energy required for the process compared to conventional processes in the art, and in the process of the invention generating one or more useful bio-products.
The pH of the absorption or dissolution medium is preferably controlled to facilitate its capacity to absorb or dissolve carbon dioxide and to contribute to reaction conditions in the bioreactor conducive to production of the one or more bio-products, as is taught in our aforementioned co-pending but currently unpublished application USSN 63364275 filed May 6, 2022.
The required pH control may be effected by biological means (e.g. selection of suitable microbes and/or microbial digestion conditions), chemical means (e.g. by adjusting the pH of the absorption or dissolution medium or of the recycle stream which contributes to it), or by both.
The pH of the absorption or dissolution medium may for example be adjusted by the addition of make up water. Often it will be desirable to increase the pH of the recycle stream within a desired range, which can be achieved by the addition of alkaline make up water.
The recycle stream may have a pH of between about 10.5 and about 11.5. In one embodiment, the recycle stream has a pH of about 11.
Advantageously, a pH of between about 10.5 and about 11.5 prevents live bacteria from entering the gas contactor.
In some embodiments, make up water or solvent may be added to the recycle stream prior to the recycle stream returning to the gas contactor and/or bioreactor.
Preferably, the pH of the liquid stream from the gas contactor to bioreactor is maintained between 8 and 10, preferably between 9 and 10, most preferably between 9 and 9.5. In one embodiment, the pH of the recycle stream is between 9 and 9.5.
If the pH of the liquid stream is not within the desired range (for example, between 9 and 10, most preferably between 9 and 9.5), an alkaline compound, for example, sodium hydroxide, may be added into makeup water to maintain the pH in the desired range. Therefore, in some embodiments the makeup water comprises an alkaline compound. In some further embodiments, the makeup water comprises sodium hydroxide.
The alkaline compound, for example sodium hydroxide, may be added to the makeup water to increase the pH of the makeup water to between about 12 and 13. Preferably, the resulting pH of the makeup water is about 12.5.
Increasing the pH of the makeup water can helps sterilize the recycle stream. Sterilization of the recycle stream can further be achieved by any methods known in the art, including, but not limited to, raising the pH of the recycle stream to prevent growth, adding biocide, adding bleaching agent(s), UV sterilization, gamma irradiation or increasing temperature Additionally, increasing the pH may improve carbon dioxide absorption and prevent unwanted microbial growth in the gas contactor. It may also help avoid sulfuric acid formation in the bioreactor.
The process of the invention is particularly effective in reducing the energy required for carbon capture and utilisation, and removing harmful contaminants from the bio-products (for example biomass used to produce fuels). In conventional chemical processes a large part of energy required for carbon capture is consumed in regenerating the solvent used for the CO2 and H25 absorption. In the present invention, biological systems are used to consume the dissolved CO2 present in the form of bicarbonate in solution, and the H25 present in the form of elemental sulfur, thereby producing the recyclable solvent and saving the energy conventionally needed for regeneration of solvent.
The source of the fluid feedstock stream may for example be flue gas, ambient air, and/or any other process gas stream(s) containing carbon dioxide and sulfurous material (such as hydrogen sulfide) -the raw feedstock(s). The use of such sources advantageously aids in reducing otherwise detrimental carbon dioxide and sulfurous emissions. The raw feedstock may be provided as a single stream comprising a mixture of CO2 and sulfurous material (e.g. H2S), or as two separate streams individually comprising CO2 and sulfurous material (e.g. H2S).
The contacting of the raw feedstock(s) with an absorption or dissolution medium to form a reagent stream comprising dissolved inorganic carbon and sulfur may be effected in a suitable vessel such as a gas contactor (or, as will be explained below) more than one gas contactor). The absorption/dissolution medium typically has a relatively low carbon dioxide and sulfurous content, which is substantially increased by contact with the raw feedstock. Thus, the process may further comprise increasing the carbonaceous and sulfurous content of the recycle stream by dissolving or absorbing CO2 and sulfurous feedstock into the reagent stream, for example with the aid of one or more gas contactors.
As mentioned, the process may utilize two (or more) separate gas contactors, especially when there are separate streams of CO2 and sulfurous feedstock to the process. A system comprising two (or more) gas contactors provides a greater degree of operational flexibility -for example by making it easier to control the C/S ratio in the reagent stream. The C/S ratio may be important in controlling the specification of the end bio-product(s). When the sulfurous stream is H2S in that case w/w CO2/H2S ratio in the (combined) feedstock may be from about 0.1:1 to about 100:1, for example from about 1:1 to about 50:1, preferably from about 2:1 to about 25:1, more preferably from about 3:1 to about 15:1, for example about 6 or 7:1, in particular about 6.5:1.
The C/S ratio may also be expressed in molar terms (and it will be noted that H2S is not necessarily the sulfurous feedstock). The molar ratio C/S is preferably around 10:1 to about 0.1:1, for instance from about 5:1 to about 0.5:1. A molar ratio of approximate parity (i.e. about 1:1) may sometimes be desirable.
The ratio of C/S can have important consequences in the process of the invention -for example when the bioreactor is charged with a consortia of microbiological organisms, the selection of C/S ratio will cause some of those organisms to respond preferentially, thereby impacting the nature of the end product. For example, when the end product is biomass -and it is desired to produce biomass with high lipid content -the C/S ratio may be selected accordingly to favour those microorganisms which yield the desired biomass compositional characteristic.
There are various types of commercially available gas contactors known in the art. The gas contactor suitable for use in the present invention may be dependent on the composition of the inlet fluid stream. Known commercially available contactors my include, but are not limited to, absorption columns with unstructured packing, absorption columns with structured packing or absorption columns with trays.
The packing of the gas contactors or trays utilized are specifically designs to improve gas and/or liquid mass transfer. Such designs are known and can be found, for example from Perry's Chemical Engineers' Handbook. New York: McGraw-Hill, 1984.
The raw feedstock may be pre-supplied to such a gas contactor before entering the bioreactor. The gas contactor and the bioreactor may therefore be provided as separate zones. Alternatively, the gas contactor and bioreactor may be provided as a single hybrid zone. In this case, it will be understood that in the process of the present invention the gas contactor and the bioreactor may be a single vessel, for example a tubular plug flow reactor. In this case, the recycle stream would be fed directly into the bioreactor in addition to the fluid stream comprising carbon dioxide and hydrogen sulfide.
The raw feedstock may be treated within the gas contactor to produce a carbon-rich feedstock liquid (the reagent stream comprising dissolved or absorbed inorganic carbon) and an off-gas substantially free of carbon dioxide. For example the gas contactor may be configured to absorb carbon dioxide from the raw feedstock (for example, ambient air) flue gas or any other process gas stream containing CO2) to produce a concentrated carbon liquid stream (as reagent stream) and an off-gas substantially free of carbon dioxide.
The off-gas substantially free from carbon dioxide may be utilized in any commonly known process. For example, the off-gas free from carbon dioxide may be used in processes such as hot air regeneration of adsorbents or used as a compressed air feed.
The raw feedstock may optionally be fed through a pressure booster prior to entering the gas contactor and/or the bioreactor. Optionally the raw feedstock may be pre-treated prior to entering the process, for example by clean-up or concentration.
The raw carbonaceous feedstock may comprise up to about 100% v/v carbon dioxide, but may comprise various other materials, such as are typically found in industrial effluents, flue gases, off-gases and/or ambient air.
The raw sulfurous feedstock may comprise up to about 100% v/v H2S, but may comprise various other materials, such as are typically found in industrial effluents, flue gases and/or off-gases.
The amount of carbon dioxide may be balanced mainly by nitrogen, water and oxygen. Additional trace amounts of SOR, NOR, H2S, particulate matter, CO and other compounds typically present in industrial gas, petrochemical, or other heavy industrial operations may be present.
The microbial broth comprises a solvent selected from at least one of amine, alkaline solution (for example, sodium hydroxide or potassium hydroxide), using wastewater for bioremediation of organic stream, ammonia and/or enzyme (for example, carbonic anhydrase) The inventors have found that such an environment in the bioreactor provides a controlled environment that achieves optimal microbial growth.
The sulfur oxidizing bacteria (SOB) can be found in prior art descriptions. These include, but are not limited to, Thioalkalimicrobium, Thioalkalivibrio, Thiobacillus, Alkatilimnicola, Guyparkeria, Halomonas, Alkalispirillum, Vibrio, Thiomicrospira, Guyporkeria, Thioalkalispira (formerly Thioalkolimicrobium), Ectothiorhodospiraceae, Rhodobacteroceae, Roseinotrobacter, Alkalilimnicola, Guyparkeria, Desulfuromusa, Desulfurispirillum.
The bio-product composition or conversion efficiency may be optionally improved through genetic engineering and enhanced reactor design.
The biological means used in the present invention may be dependent on the final bio-product.
The bioreactor conditions may be controlled through in-line monitoring to determine the C/5 ratio and carbon speciation. This information can be used to optimize the operating pH and gas flow rates to maximize CO2 capture and system performance.
The nutrient supply to the process of the invention is controlled to maximise bio-product formation. Preferably the nutrient supply to the bioreactor is above 2mg(N)/I and/or 2mg(P)/I, preferably above 2.5, more preferably above 3 mg(N or P)/l, and is manipulated to maximise the amount of bio-product (e.g. biomass) produced. This nutrient concentration is typically higher than is conventional in current bio-desulfurisation technology -in fact, in such conventional technology the nutrient supply is deliberately maintained below these ranges.
The process of the invention yields one or more bio-products, such as biomass, PHA/B, 1,4-butanediol, amongst others, with desirably high lipid, carbohydrate and/or protein contents. In one aspect, the process may be adapted to preferentially to produce lipids in preference to protein and carbohydrates. This may be achieved by operating the bioreactor in a time-limited nutrient starved environment (i.e. with low N or P bioavailability) in order temporarily to stress the microorganisms and encourage lipid production.
It may also be desirable to limit the amount of oxygen supplied to the bioreactor in order to avoid the formation of sulfur dioxide. Running the bioreactor "oxygen-lean" in this way helps maximise elemental sulfur production by the sulfur oxidising bacteria.
Advantageously, the process according to the present invention can be used to produce biomass with different characteristics.
When the one or more bio-products comprises biomass, it may in some circumstances be desirable to maximise lipid content-in which case the biomass may comprise at least about 40%w/w lipid content, for example at least about 50%w/w lipid content, e.g. 60%w/w or 70%w/w lipid content.
Alternatively, where for example PHA/PHB or BDO is targeted as the end product the lipid content may be lower -for example 40%w/w or less, for instance 30%w/w or less.
The one or more bio-products produced from the process according to the present invention may be used, by way of non-limiting example, as an energy source, a final product, an intermediate product in a different process, or a carbon storage medium. Preferable end uses may be dependent on the product composition. In the instance that the one or more bio-products is biomass with a high lipid content will be desirable for biofuel production, such as biodiesel. Conversely, high carbohydrate content is more favourable for production of ethanol, and high protein biomass is suited for the production of protein supplements for agricultural feed or nutraceuticals.
In one embodiment, there may be a method of separating the reduced elemental sulfur from biomass.
Depending on the location and end product, this may include centrifugation, solvent extraction, hydro cyclone, or any other separation method known in the art.
In another embodiment, once the sulfur is extracted and the target molecules removed from the one or more bio-products, there will be a portion of waste biomass or biomass debris. This debris can be used as a feed into anaerobic digester for biogas generation. The debris can also be utilized to feed a secondary bioreactor. The secondary bioreactor can optionally be a reactor with sulfate reducing bacteria (SRBs) which may produce H2S to be fed back into the first reactor to improve carbon capture. This will be useful where sites are lacking sufficient H25 for complete carbon capture. This second reactor may also be specifically designed to produce a number of other biologic chemicals, such as PHA/B, 1,4-butanediol, or other.
According to a second aspect of the present invention, there is provided an apparatus for the conversion of CO2 into one or more bio-products, in which the energy required for the microbiological conversion is at least partially provided by the concomitant microbiological oxidation of a sulfurous feedstock, the apparatus comprising: means for contacting raw carbon dioxide and sulfur-containing feedstocks, either separately or in combination, with an absorption or dissolution medium to form a reagent stream comprising dissolved or absorbed inorganic carbon and sulfur; and ii. means for contacting at least a portion of the reagent stream with a microbial broth in a bioreactor to oxidize sulfur and produce one or more bio-products from the carbon dioxide.
An apparatus according to the present invention may further comprise a gas contactor to concentrate the fluid stream with high carbon content, and/or a second bioreactor for producing H25 to be recycled and improve carbon capture.
The process according to the present invention may optionally further comprise at least one downstream process.
The downstream process may comprise a process that produces a gas comprising carbon dioxide, for example a biofuels production process.
The downstream process may comprise a process that converts elemental sulfur into a useful end product such as a fertiliser or commodity chemical.
By-products or products from the downstream process may advantageously be recycled and used in the process according to the present invention, thereby improving the environmental impact of the overall process and reducing the need for the introduction of external means.
FIGURES AND EXAMPLES
The invention will now be more particularly described with reference to the following examples and Figures, in which; Figure 1 depicts a schematic diagram of a process of sequestering carbon and removing H2S according to the invention, wherein a co-mingled feed is used.
Figure 2 depicts a schematic diagram of a process of sequestering carbon and removing H2S according to the invention, wherein separate feeds are used.
Figure 3 depicts a schematic diagram of a process according to the invention in which elemental sulfur produced by the process is recycled via a sulfur reducing bioreactor to generate H2S for use in the process as the sulfurous feedstock.
Figure 1 In the process of the invention schematically represented by Figure 1 the feedstock gas comprising CO2 and H2S is supplied in line 201 at atmospheric pressure to a pressure booster 10 which increases the pressure of the feedstock gas to an extent so the flue gas overcomes hydraulic head in gas contactor 11. Pressurized gas passes through line 202 to gas contactor 11, which is also supplied by line 203 with a liquid recycle stream from the process, in combination with make-up water from line 204. In gas contactor 11, CO2 and H2S in the feedstock stream is dissolved in the liquid recycle stream and is supplied on in line 205 to bioreactor 12. A substantially carbon dioxide free and hydrogen sulfide free off-gas is vented in line 206.
Stream B in line 205 enters bioreactor 12 charged with a microbial broth and maintained under conditions of temperature/pressure/pH effective to ensure consumption by the microbial broth of the stream B to generate a biomass product and a liquid vehicle. Bioreactor 12 is supplied with air (oxygen) through line 207. The one or more bio-products and a liquid vehicle are supplied on in line 209 to biomass separator 13, and vent gas leaves the bioreactor through line 208. The biomass separator 13 separates the one or more bio-products, which is removed through line 210, and a recycle stream A which is recycled to gas contactor 11 in line 203 after combination with make-up water in line 204.
The fluid feedstock stream supplied in line 201 is (in this example) flue gas from a chemical plant -but other sources such as power plant or other industrial process could be used.
The feedstock gas is supplied in line 201 at atmospheric pressure to a pressure booster 10 which increases the pressure of the feedstock gas to an extent so the flue gas overcomes hydraulic head in gas contactor 11. Gas contactor 11 is supplied in line 203 with a liquid recycle stream from the process, in combination with make-up water from line 204.
In gas contactor 11 carbon dioxide and H2S in the feedstock stream are dissolved in the alkaline liquid recycle stream and supplied on in line 205 to bioreactor 12. A substantially carbon dioxide-free and hydrogen sulfide-free off-gas is vented in line 206.
Stream B in line 205 enters bioreactor 12 charged with a microbial broth and maintained under conditions of temperature/pressure/pH effective to ensure consumption by the microbial broth of the stream B to generate one or more bio-products and a liquid vehicle. Both are supplied on in line 207 to biomass separator 13, from which is recovered in line one or more bio-products and, in line 208, a recycle stream A which is recycled to gas contactor 11 in line 203 after combination with make-up water in line 204.
Figure 2 and Example
In the process of the invention schematically represented by Figure 2 the feedstock gas comprising CO2 is supplied in line 301 at atmospheric pressure to a pressure booster 10 which increases the pressure of the feedstock gas to an extent so the flue gas overcomes hydraulic head in gas contactor 11. Pressurized gas passes through line 302 to gas contactor 11, which is also supplied by line 303 with a liquid recycle stream from the process, in combination with make-up water from line 304. The gas contactor is also supplied with a separate stream containing H2S from line 305. In gas contactor 11, CO2 and H2S are dissolved in the liquid recycle stream and is supplied on in line 307 to bioreactor 12. A substantially carbon dioxide free and hydrogen sulfide free off-gas is vented in line 306.
The fluid feedstock stream supplied in line 301 is (in this example) flue gas from a chemical plant -but other sources such as power plant or other industrial process could be used.
The fluid feedstock stream supplied in line 305 is (in this example) an H25 stream -but other sources such as chemical or power plant or other industrial process could be used.
Stream B in line 307 enters bioreactor 12 charged with a microbial broth and maintained under conditions of temperature/pressure/pH effective to ensure consumption by the microbial broth of the stream B to generate a biomass product and a liquid vehicle. Bioreactor 12 is supplied with air (oxygen) through line 308. The one or more bio-products and a liquid vehicle are supplied on in line 310 to biomass separator 13, and vent gas leaves the bioreactor through line 309. The biomass separator 13 separates the one or more bio-products, which is removed through line 311, and a recycle stream A which is recycled to gas contactor 11 in line 303 after combination with make-up water in line 304.
EXAMPLE
In the process of the invention schematically represented in Figure 2 a carbon containing feedstock stream (flue gas) and an H2S feedstock stream (H2S gas) are supplied to a Gas Contactor 11.
The composition of the Flue gas is as follows: Material %v/v N2 75 CO2 10 H20 9 02 5 SO2 300 (ppm) CO 700 (ppm) NOX 150 (ppm) 503 20 (ppm) The flue gas may be supplied at atmospheric pressure or elevated pressure. If supplied at atmospheric pressure, a pressure booster may be used to increase pressure of the flue gas to overcome hydraulic head in gas contactor 11. Gas contactor 11 is also supplied by H2S containing stream. Gas contactor 11 is also supplied a liquid recycle stream from the process. In gas contactor 11 carbon dioxide and hydrogen sulfide are dissolved into the liquid stream and supplied to bioreactor 12. A substantially carbon dioxide free and hydrogen sulfide free off gas is vented as off gas.
The composition of the H2S containing stream is as follows: Material %v/v H2S 100% The composition of the liquid stream fed into bioreactor 12 is as follows: Material Concentration (Ibmol/hr) CO2 0.47 OH- 2.89 HCO3- 1419.50 C032- 1043.09 HS- 476.3 The composition of the off gas vented from gas contactor 11 is as follows: Material %v/v N2 85 H20 9 02 5 Trace components 1% Bioreactor 12 is fed with the liquid stream from gas contactor 11 and with compressed air as an oxygen source.
Bioreactor 12 is charged with a microbial broth and maintained under conditions of temperature/pressure/pH effective to ensure consumption by the microbial broth of the liquid stream fed from gas contactor 11 to generate a sulfur-containing biomass product and a liquid vehicle. The sulfur-containing biomass and the liquid vehicle are supplied to Biomass Separator 13. A concentrated sulfur-containing biomass and a substantially biomass-free liquid are produced. The biomass-free liquid is returned to the gas contactor 11 via line 303. In some embodiments, the concentrated sulfur-containing biomass can be processed further to separate elemental sulfur from the biomass. In other embodiments, the concentrated sulfur-containing biomass is used directly as a feedstock for further bioreactors.
In certain embodiments, the bioreactor 12 operating parameters are optimized to promote biomass growth. In other embodiments, the bioreactor operating parameters are optimized to promote lipid buildup. In still more embodiments, the bioreactor operating parameters are optimized to promote carbohydrate accumulation The above described flue gas and H2S containing gas stream can be processed according to the invention substantially to remove the hydrogen sulfide and capture the carbon dioxide.
Figure 3 In the process of the invention schematically represented by Figure 3 elemental sulfur product from the process of the invention is recycled via an H2S bioreactor to provide a sulfurous stream for the process of the invention.
Flue gas is supplied to CO2 absorber 20 through line 401. In CO2 absorber 20 the carbon dioxide is absorbed by a recycled liquid stream, passing through line 402 to a H2S absorber 21. H25 absorber 21 is also supplied by a stream 403 from H2S bioreactor 22. In H2S absorber 21, the hydrogen sulfide is absorbed into the recycled liquid stream.
The fluid feedstock stream supplied in line 401 is (in this example) flue gas from a chemical plant -but other sources such as power plant or other industrial process could be used.
The feedstock gas may be supplied at atmospheric pressure or elevated pressure. If supplied at atmospheric pressure, a pressure booster may be used to increase pressure of the sour gas to overcome hydraulic head in gas absorber 20.
The carbon and sulfur containing reagent stream passes from through line 404 to aerobic bioreactor 23 charged with a microbial broth and maintained under conditions of temperature/pressure/pH effective to ensure consumption by the microbial broth of the stream to generate one or more bioproducts and a liquid vehicle. Bioreactor 23 is supplied with nutrients, sodium hydroxide and water through line 406, which also contains recycled liquid vehicle. The one or more bio-products and a liquid vehicle are supplied on in line 407 to settler 24, from which is recovered one or more bio-products. In line 408, a recycle stream of CO2 is recycled to CO2 absorber 20.
The mixture of one or more bio-products and a liquid vehicle pass from settler 24 through line 409, firstly to centrifuge 25, which is operated under conditions to separate elemental sulfur through line 411. The substantially sulfur-free product mixture passes from centrifuge 25, through line 410, to centrifuge 26, which operates under conditions to separate the bio-products from the liquid vehicle. The desired bioproduct is collected through line 412 and the recycled liquid vehicle is removed through line 406 and recycled to the aerobic bioreactor, being combined with nutrients, sodium hydroxide and water supplied through line 413. A bleed outlet 414 is also present to allow the removal of excess liquid vehicle.
The sulfur removed through line 411 is provided to H25 bioreactor 22, which is also supplied with biomass debris from line 415. H2S bioreactor is charged with sulfate reducing bacteria producing a stream of H25 that is fed back into the H25 absorber 21 through line 403 to improve carbon capture.
For the avoidance of doubt, all features relating to process for sequestering carbon dioxide also relate, where appropriate to the apparatus for sequestering carbon dioxide and vice versa.
Claims (23)
- CLAIMS1. A microbiological process for the conversion of CO2 into bio-product, in which the energy required for the microbiological conversion is at least partially provided by the concomitant microbiological oxidation of a sulfurous feedstock.
- 2. The microbiological process according to claim 1 effected by one or more chemotrophic organisms.
- 3. The microbiological process according to claim 2 wherein one or more of the chemotrophic organisms are sulfur oxidising bacteria.
- 4. The process according to any one of Claims 1 to 3 wherein the microbiological conversion and/or the concomitant microbiological oxidation is effected by one or more organisms selected from Thioalkalimicrobium, Thioalkalivibrio, Thiobacillus, Alkali! imnicola, Guyparkeria, Halomonas, Alkalispirillum, Vibrio, Thiomicrospira, Guyparkeria, Thioalkalispira (formerly Thioalkalimicrobium), Ectothiorhodospiraceae, Rhodobacteraceae, Roseinatrobacter, Alkalilimnicola, Guyparkeria, Desulfuromusa, Desulfurispirillum.
- 5. The microbiological process according to any one of claims 1 to 4 wherein the sulfurous feedstock is at least partially oxidized to elemental sulfur by sulfur oxidising bacteria.
- 6. The process according to any one of Claims 1 to 5 wherein the reduced elemental sulfur is removed from the one or more bio-products by a method selected from centrifugation, solvent extraction, or by means of a hydrocyclone.
- 7. The microbiological process according to any one of claims 1 to 6 comprising the steps of: i. contacting a raw carbon dioxide and sulfur-containing feedstock with an absorption or dissolution medium to form a reagent stream comprising dissolved or absorbed inorganic carbon and sulfur; and ii. contacting at least a portion of the reagent stream with a microbial broth in a bioreactor to oxidize sulfur and produce one or more bio-products from the carbon dioxide.
- 8. The microbiological process according to claim 7 further comprising: iii. separating the one or more bio-products into one or more bio-products and a liquid stream; and iv. recycling at least a portion of the liquid stream to step i. of the process for use as, or part of, the absorption or dissolution medium.
- 9. The process according to Claim 7 or claim 8 wherein carbon dioxide and the sulfur are introduced into the process as or as part of a single feedstock stream.
- 10. The process according to Claim 7 or claim 8 wherein carbon dioxide and the sulfur are introduced into the process as separate feedstock streams.
- 11. The process according to any one of Claims 7 to 10 wherein in-line monitoring is used to determine the carbon dioxide/sulfur ratio and/or carbon speciation.
- 12. The process according to any one of Claims 7 to 11 wherein the pH of the absorption or dissolution medium is controlled.
- 13. The process according to any one of Claims 1 to 12 wherein the process is operated in a nutrient-starved environment and the one or more bio-products is lipid-rich.
- 14. The process according to any one of Claims 1 to 13 wherein debris from the one or more bioproducts is used as a feedstock for an anaerobic digester to generate biogas.
- 15. The process according to any one of Claims 1 to 8 wherein the debris from the one or more bio-products is used as a feedstock for a secondary bioreactor, wherein the reactor uses sulfate reducing bacteria to produce H2S.
- 16. The process according to Claim 15, wherein the H25 produced by the secondary bioreactor is used as or as part of the sulfurous feedstock.
- 17. The process according to Claim 15 or 16, wherein the secondary bioreactor produces biologic chemicals.
- 18. The process according to any of the preceding claims, wherein the one or more bio-products comprises biomass, lipids for fuels, PHAs or BDO.
- 19. An apparatus for the conversion of CO2 into one or more bio-products, in which the energy required for the microbiological conversion is at least partially provided by the concomitant microbiological oxidation of a sulfurous feedstock, the apparatus comprising: i. means for contacting raw carbon dioxide and sulfur-containing feedstocks, either separately or in combination, with an absorption or dissolution medium to form a reagent stream comprising dissolved or absorbed inorganic carbon and sulfur; and means for contacting at least a portion of the reagent stream with a microbial broth in a bioreactor to oxidize sulfur and produce one or more bio-products from the carbon dioxide.
- 20. An apparatus according to Claim 19 further comprising a gas contactor to concentrate the fluid stream.
- 21. The system according to Claim 20, wherein the system further comprises a secondary bioreactor charged with sulfate reducing bacteria.
- 22. An apparatus according to any of claims 19 to 21 configured to operate the process of any one of claims 1 to 18.
- 23. One or more bio-products produced by a process according to any one of Claims 1 to 18.
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
EP22192405.3A EP4306204A1 (en) | 2022-07-13 | 2022-08-26 | Microbiological process for the conversion of carbon dioxide into a bioproduct |
JP2022146199A JP2024012021A (en) | 2022-07-13 | 2022-09-14 | process |
KR1020220130362A KR20240009312A (en) | 2022-07-13 | 2022-10-12 | Process |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US202263368291P | 2022-07-13 | 2022-07-13 |
Publications (2)
Publication Number | Publication Date |
---|---|
GB202210917D0 GB202210917D0 (en) | 2022-09-07 |
GB2620645A true GB2620645A (en) | 2024-01-17 |
Family
ID=84540536
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
GB2210917.7A Pending GB2620645A (en) | 2022-07-13 | 2022-07-26 | Process |
Country Status (2)
Country | Link |
---|---|
GB (1) | GB2620645A (en) |
WO (1) | WO2024015886A2 (en) |
Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4760027A (en) * | 1986-04-09 | 1988-07-26 | Combustion Engineering, Inc. | Microbiological desulfurization of gases |
WO2011056183A1 (en) * | 2009-11-06 | 2011-05-12 | Sequesco | Biological and chemical process utilizing chemoautotrophic microorganisms for the chemosynthetic fixation of carbon dioxide and/or other inorganic carbon sources into organic compounds, and the generation of additional useful products |
WO2018056787A1 (en) * | 2016-09-26 | 2018-03-29 | 에스케이이노베이션 주식회사 | Carbon dioxide conversion process using carbon dioxide mineralization process and metabolic reaction of sulfur-oxidizing microorganisms linked thereto |
US10507426B2 (en) * | 2009-07-27 | 2019-12-17 | The University Of Wyoming Research Corporation | Systems and methods for biological conversion of carbon dioxide pollutants into useful products |
US10801045B2 (en) * | 2011-10-31 | 2020-10-13 | Ginkgo Bioworks, Inc. | Methods for making chemoautotrophic cells by engineering an energy conversion pathway and a carbon fixation pathway |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9957534B2 (en) | 2008-11-06 | 2018-05-01 | Kiverdi, Inc. | Engineered CO2-fixing chemotrophic microorganisms producing carbon-based products and methods of using the same |
US11274321B2 (en) | 2008-11-06 | 2022-03-15 | Kiverdi, Inc. | Use of oxyhydrogen microorganisms for non-photosynthetic carbon capture and conversion of inorganic and/or C1 carbon sources into useful organic compounds |
EP2970859A4 (en) | 2013-03-14 | 2017-07-19 | The University Of Wyoming Research Corporation | Conversion of carbon dioxide utilizing chemoautotrophic microorganisms systems and methods |
EP3034157A1 (en) | 2015-02-19 | 2016-06-22 | Paqell B.V. | Process for treating a hydrogen sulphide and mercaptans comprising gas |
US10597681B2 (en) | 2015-09-14 | 2020-03-24 | President And Fellows Of Harvard College | Carbon fixation systems and methods |
US20170218740A1 (en) | 2016-01-28 | 2017-08-03 | Craig Pichach | Subterranean conversion of carbon dioxide to biomass by chemolithotropy |
BE1027695B1 (en) | 2019-10-01 | 2021-12-03 | Avecom Nv | METHOD FOR THE PRODUCTION OF BIOMASS OR THEIR DERIVATIVES |
-
2022
- 2022-07-26 GB GB2210917.7A patent/GB2620645A/en active Pending
-
2023
- 2023-07-13 WO PCT/US2023/070094 patent/WO2024015886A2/en unknown
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4760027A (en) * | 1986-04-09 | 1988-07-26 | Combustion Engineering, Inc. | Microbiological desulfurization of gases |
US10507426B2 (en) * | 2009-07-27 | 2019-12-17 | The University Of Wyoming Research Corporation | Systems and methods for biological conversion of carbon dioxide pollutants into useful products |
WO2011056183A1 (en) * | 2009-11-06 | 2011-05-12 | Sequesco | Biological and chemical process utilizing chemoautotrophic microorganisms for the chemosynthetic fixation of carbon dioxide and/or other inorganic carbon sources into organic compounds, and the generation of additional useful products |
US10801045B2 (en) * | 2011-10-31 | 2020-10-13 | Ginkgo Bioworks, Inc. | Methods for making chemoautotrophic cells by engineering an energy conversion pathway and a carbon fixation pathway |
WO2018056787A1 (en) * | 2016-09-26 | 2018-03-29 | 에스케이이노베이션 주식회사 | Carbon dioxide conversion process using carbon dioxide mineralization process and metabolic reaction of sulfur-oxidizing microorganisms linked thereto |
Also Published As
Publication number | Publication date |
---|---|
WO2024015886A2 (en) | 2024-01-18 |
WO2024015886A3 (en) | 2024-02-22 |
GB202210917D0 (en) | 2022-09-07 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
Angelidaki et al. | Biogas upgrading and utilization: Current status and perspectives | |
CN104860474B (en) | Method for carbon sequestration and biological treatment of sulfur-containing waste alkali liquor | |
JP2023514132A (en) | Use of Fermentation Tail Gas in Integrated Gasification and Gas Fermentation Systems | |
RU2162729C2 (en) | Method of removing hydrogen sulfide and/or carbonyl sulfide from gas | |
López et al. | Biogas technologies and cleaning techniques | |
Chen et al. | Enhanced sustainable integration of CO2 utilization and wastewater treatment using microalgae in circular economy concept | |
CN107537293B (en) | Closed cycle microbial desulfurization and elemental sulfur recovery method | |
AU2013383361B2 (en) | Sulfur management for processes and control systems for the efficient anaerobic conversion of hydrogen and carbon oxides to alcohols | |
CN102989272A (en) | Method and device for synchronously removing sulfur dioxide and nitric oxide by flue gas biological method | |
Ghayur et al. | Biological and chemical treatment technologies for waste amines from CO2 capture plants | |
CZ426598A3 (en) | Sulfur reducing bacterium and its utilization in processes of biological desulfurization | |
CN203389526U (en) | Biological desulphurization device | |
Nazari et al. | The study of biological technologies for the removal of sulfur compounds | |
EP3284827A1 (en) | Production of algae using co2-containing gas | |
Torres et al. | Biogas treatment for H2S, CO2, and other contaminants removal | |
CN110643403A (en) | Chemical absorption combined biological removal hydrogen sulfide and sulfur resource technology in methane | |
Andreides et al. | Biological H2S removal from gases | |
EP4306204A1 (en) | Microbiological process for the conversion of carbon dioxide into a bioproduct | |
AU2013274711B2 (en) | Integrated processes for bioconverting syngas to oxygenated organic compound with sulfur supply | |
Venkiteshwaran et al. | Anaerobic digester biogas upgrading using microalgae | |
GB2620645A (en) | Process | |
US20240102055A1 (en) | Method for producing a fermentation product | |
CN112892202B (en) | Sulfur-containing gas desulfurization device system and method | |
CN1702374A (en) | Apparatus and process for separating carbon dioxide by coal replacement combustion based on calcium sulfate | |
CN112473344A (en) | Biological desulfurization system without aeration and treatment method |