CA2775230A1 - Organic forward osmosis system - Google Patents
Organic forward osmosis system Download PDFInfo
- Publication number
- CA2775230A1 CA2775230A1 CA 2775230 CA2775230A CA2775230A1 CA 2775230 A1 CA2775230 A1 CA 2775230A1 CA 2775230 CA2775230 CA 2775230 CA 2775230 A CA2775230 A CA 2775230A CA 2775230 A1 CA2775230 A1 CA 2775230A1
- Authority
- CA
- Canada
- Prior art keywords
- stream
- forward osmosis
- stage
- digester
- membrane
- 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
- 238000009292 forward osmosis Methods 0.000 title claims abstract description 155
- 239000012528 membrane Substances 0.000 claims abstract description 128
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 80
- 239000012267 brine Substances 0.000 claims abstract description 67
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 67
- 150000003839 salts Chemical class 0.000 claims abstract description 51
- 239000003337 fertilizer Substances 0.000 claims abstract description 45
- 238000010306 acid treatment Methods 0.000 claims abstract description 43
- 239000002253 acid Substances 0.000 claims abstract description 42
- 238000001223 reverse osmosis Methods 0.000 claims description 44
- 238000000034 method Methods 0.000 claims description 37
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 26
- 238000012216 screening Methods 0.000 claims description 24
- 239000002028 Biomass Substances 0.000 claims description 23
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 23
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 claims description 18
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 claims description 18
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 17
- 238000001914 filtration Methods 0.000 claims description 17
- 229910052698 phosphorus Inorganic materials 0.000 claims description 17
- 239000011574 phosphorus Substances 0.000 claims description 17
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical class [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims description 15
- WZISDKTXHMETKG-UHFFFAOYSA-H dimagnesium;dipotassium;trisulfate Chemical compound [Mg+2].[Mg+2].[K+].[K+].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O WZISDKTXHMETKG-UHFFFAOYSA-H 0.000 claims description 14
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Chemical compound [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 claims description 14
- FGIUAXJPYTZDNR-UHFFFAOYSA-N potassium nitrate Chemical compound [K+].[O-][N+]([O-])=O FGIUAXJPYTZDNR-UHFFFAOYSA-N 0.000 claims description 14
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims description 13
- 239000000835 fiber Substances 0.000 claims description 12
- 229910000147 aluminium phosphate Inorganic materials 0.000 claims description 9
- 238000001035 drying Methods 0.000 claims description 9
- 239000001103 potassium chloride Substances 0.000 claims description 9
- 235000011164 potassium chloride Nutrition 0.000 claims description 9
- 239000008213 purified water Substances 0.000 claims description 9
- 239000002699 waste material Substances 0.000 claims description 9
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 claims description 8
- 239000002131 composite material Substances 0.000 claims description 8
- 229910017604 nitric acid Inorganic materials 0.000 claims description 8
- 229910000027 potassium carbonate Inorganic materials 0.000 claims description 7
- 235000011181 potassium carbonates Nutrition 0.000 claims description 7
- 239000004323 potassium nitrate Substances 0.000 claims description 7
- 235000010333 potassium nitrate Nutrition 0.000 claims description 7
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 claims description 7
- 229910052939 potassium sulfate Inorganic materials 0.000 claims description 7
- 235000011151 potassium sulphates Nutrition 0.000 claims description 7
- 239000010409 thin film Substances 0.000 claims description 7
- 238000010981 drying operation Methods 0.000 claims description 4
- 239000000463 material Substances 0.000 description 21
- 238000004519 manufacturing process Methods 0.000 description 17
- 239000002357 osmotic agent Substances 0.000 description 14
- 238000011084 recovery Methods 0.000 description 14
- 239000000243 solution Substances 0.000 description 14
- 239000002351 wastewater Substances 0.000 description 12
- 238000001556 precipitation Methods 0.000 description 11
- 235000015097 nutrients Nutrition 0.000 description 10
- 239000007787 solid Substances 0.000 description 10
- 125000006850 spacer group Chemical group 0.000 description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 9
- 230000003204 osmotic effect Effects 0.000 description 8
- 238000000926 separation method Methods 0.000 description 8
- 230000020477 pH reduction Effects 0.000 description 7
- 238000012546 transfer Methods 0.000 description 7
- 235000013305 food Nutrition 0.000 description 6
- 238000000108 ultra-filtration Methods 0.000 description 6
- 239000012530 fluid Substances 0.000 description 5
- 238000003306 harvesting Methods 0.000 description 5
- 239000007788 liquid Substances 0.000 description 5
- 239000012466 permeate Substances 0.000 description 5
- 229920000728 polyester Polymers 0.000 description 5
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- 210000004779 membrane envelope Anatomy 0.000 description 4
- 239000003895 organic fertilizer Substances 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- 239000006228 supernatant Substances 0.000 description 4
- 229910002651 NO3 Inorganic materials 0.000 description 3
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 3
- -1 Polyethylene Polymers 0.000 description 3
- 238000007792 addition Methods 0.000 description 3
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 description 3
- 239000003651 drinking water Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- BHEPBYXIRTUNPN-UHFFFAOYSA-N hydridophosphorus(.) (triplet) Chemical compound [PH] BHEPBYXIRTUNPN-UHFFFAOYSA-N 0.000 description 3
- 238000007654 immersion Methods 0.000 description 3
- 230000002195 synergetic effect Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000004952 Polyamide Substances 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 238000007605 air drying Methods 0.000 description 2
- 230000004888 barrier function Effects 0.000 description 2
- 235000012206 bottled water Nutrition 0.000 description 2
- 238000005266 casting Methods 0.000 description 2
- 239000001913 cellulose Substances 0.000 description 2
- 229920002678 cellulose Polymers 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000029087 digestion Effects 0.000 description 2
- 239000010794 food waste Substances 0.000 description 2
- 239000013505 freshwater Substances 0.000 description 2
- 239000003292 glue Substances 0.000 description 2
- 238000001471 micro-filtration Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 235000013348 organic food Nutrition 0.000 description 2
- 229920002647 polyamide Polymers 0.000 description 2
- 239000004814 polyurethane Substances 0.000 description 2
- 229920002635 polyurethane Polymers 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 235000001508 sulfur Nutrition 0.000 description 2
- KXGFMDJXCMQABM-UHFFFAOYSA-N 2-methoxy-6-methylphenol Chemical compound [CH]OC1=CC=CC([CH])=C1O KXGFMDJXCMQABM-UHFFFAOYSA-N 0.000 description 1
- 241000894006 Bacteria Species 0.000 description 1
- 229920000049 Carbon (fiber) Polymers 0.000 description 1
- 229920001747 Cellulose diacetate Polymers 0.000 description 1
- 241000195493 Cryptophyta Species 0.000 description 1
- 239000004593 Epoxy Substances 0.000 description 1
- 239000004677 Nylon Substances 0.000 description 1
- 229930182556 Polyacetal Natural products 0.000 description 1
- 239000004698 Polyethylene Substances 0.000 description 1
- 239000004642 Polyimide Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 108091006629 SLC13A2 Proteins 0.000 description 1
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 239000002154 agricultural waste Substances 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 239000010828 animal waste Substances 0.000 description 1
- 229920006231 aramid fiber Polymers 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 238000000071 blow moulding Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
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- 229920002301 cellulose acetate Polymers 0.000 description 1
- 229920001727 cellulose butyrate Polymers 0.000 description 1
- 238000005097 cold rolling Methods 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005520 cutting process Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000005553 drilling Methods 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 229920001971 elastomer Polymers 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 239000011152 fibreglass Substances 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
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- 229920002313 fluoropolymer Polymers 0.000 description 1
- 239000004811 fluoropolymer Substances 0.000 description 1
- 238000005242 forging Methods 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
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- 230000002209 hydrophobic effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000001746 injection moulding Methods 0.000 description 1
- 229910017053 inorganic salt Inorganic materials 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 238000009285 membrane fouling Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 238000003801 milling Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 150000002823 nitrates Chemical class 0.000 description 1
- 229920001778 nylon Polymers 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 229920001568 phenolic resin Polymers 0.000 description 1
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- 239000010908 plant waste Substances 0.000 description 1
- 238000007747 plating Methods 0.000 description 1
- 229920002492 poly(sulfone) Polymers 0.000 description 1
- 239000004417 polycarbonate Substances 0.000 description 1
- 229920000515 polycarbonate Polymers 0.000 description 1
- 229920000573 polyethylene Polymers 0.000 description 1
- 229920001721 polyimide Polymers 0.000 description 1
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- 229920001296 polysiloxane Polymers 0.000 description 1
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- 239000013535 sea water Substances 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 239000001509 sodium citrate Substances 0.000 description 1
- 238000005476 soldering Methods 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229920001169 thermoplastic Polymers 0.000 description 1
- 229920001187 thermosetting polymer Polymers 0.000 description 1
- 239000004416 thermosoftening plastic Substances 0.000 description 1
- 238000001721 transfer moulding Methods 0.000 description 1
- HRXKRNGNAMMEHJ-UHFFFAOYSA-K trisodium citrate Chemical compound [Na+].[Na+].[Na+].[O-]C(=O)CC(O)(CC([O-])=O)C([O-])=O HRXKRNGNAMMEHJ-UHFFFAOYSA-K 0.000 description 1
- 229940038773 trisodium citrate Drugs 0.000 description 1
- 241001148471 unidentified anaerobic bacterium Species 0.000 description 1
- 238000007666 vacuum forming Methods 0.000 description 1
- 239000003643 water by type Substances 0.000 description 1
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Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/58—Multistep processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
- B01D61/0022—Apparatus therefor
-
- 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
- C02F1/445—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by forward osmosis
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
- C05F17/00—Preparation of fertilisers characterised by biological or biochemical treatment steps, e.g. composting or fermentation
- C05F17/50—Treatments combining two or more different biological or biochemical treatments, e.g. anaerobic and aerobic treatment or vermicomposting and aerobic treatment
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05F—ORGANIC FERTILISERS NOT COVERED BY SUBCLASSES C05B, C05C, e.g. FERTILISERS FROM WASTE OR REFUSE
- C05F7/00—Fertilisers from waste water, sewage sludge, sea slime, ooze or similar masses
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/08—Specific process operations in the concentrate stream
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2688—Biological processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2317/00—Membrane module arrangements within a plant or an apparatus
- B01D2317/04—Elements in parallel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/002—Forward osmosis or direct osmosis
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
- B01D61/025—Reverse osmosis; Hyperfiltration
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
- B01D61/14—Ultrafiltration; Microfiltration
- B01D61/147—Microfiltration
-
- 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
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by 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
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- 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
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/02—Biological treatment
- C02F11/04—Anaerobic treatment; Production of methane by such processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/24—Separation of coarse particles, e.g. by using sieves or screens
-
- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A40/00—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production
- Y02A40/10—Adaptation technologies in agriculture, forestry, livestock or agroalimentary production in agriculture
- Y02A40/20—Fertilizers of biological origin, e.g. guano or fertilizers made from animal corpses
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/40—Bio-organic fraction processing; Production of fertilisers from the organic fraction of waste or refuse
Abstract
An organic forward osmosis system includes an acid treatment stage comprising an acid treatment operation configured to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream. A forward osmosis stage is coupled to the acid treatment stage and includes a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by:
diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream.
diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream.
Description
Organic Forward Osmosis System [0001] Blank BACKGROUND
Technical Field [0002] This document relates to organic forward osmosis systems and processes that provide for the combined and simultaneous treatment of centrate wastewater from anaerobic digestion, reverse osmosis membrane water treatment waste brines, and the production of high-grade organic fertilizer.
Background [0003] The wastewater or centrate that is drawn from the bottom of anaerobic agricultural waste digester tanks is high in dissolved and colloidal solids.
These anaerobic digesters are primarily intended for the producing of methane gas and dry composted solids. The centrate that is drawn out of these digesters are generally much higher in nitrogen than phosphorus (not a valuable balanced fertilizer). At the same time this centrate is so high in ultra fine materials that will blind and/or foul most known filtration equipment. Even after pretreatment precipitation these fine solids would foul most membrane and filtration processes.
SUMMARY
Technical Field [0002] This document relates to organic forward osmosis systems and processes that provide for the combined and simultaneous treatment of centrate wastewater from anaerobic digestion, reverse osmosis membrane water treatment waste brines, and the production of high-grade organic fertilizer.
Background [0003] The wastewater or centrate that is drawn from the bottom of anaerobic agricultural waste digester tanks is high in dissolved and colloidal solids.
These anaerobic digesters are primarily intended for the producing of methane gas and dry composted solids. The centrate that is drawn out of these digesters are generally much higher in nitrogen than phosphorus (not a valuable balanced fertilizer). At the same time this centrate is so high in ultra fine materials that will blind and/or foul most known filtration equipment. Even after pretreatment precipitation these fine solids would foul most membrane and filtration processes.
SUMMARY
[0004] Aspects of this document relate to organic forward osmosis systems and processes. These aspects may include, and implementations may include, one or more or all of the components and steps set forth in the appended CLAIMS, which are hereby incorporated by reference.
[0005] In one aspect, an organic forward osmosis system for concentrating digester biomass intended for Organic Certified fertilizer is disclosed. The system may include an acid treatment stage comprising an acid treatment operation configured to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream. A forward osmosis stage is coupled to the acid treatment stage and configured to receive the acid treated, digester centrate stream from the acid treatment stage. The forward osmosis stage includes a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by: diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream.
[0006] Particular implementations may include one or more or all of the following.
[0007] The diluted salt brine stream may be maintained in the forward osmosis draw loop.
[0008] The system may also be for recovering water for re-use and may include a reverse osmosis stage coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage. The reverse osmosis stage may include a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
[0009] The acid treatment stage may be configured to augment digester biomass with phosphorus and the acid treatment operation comprises using Organic Certified phosphoric acid at an Organic Certifiable process pH of 3.5, thereby balancing a P:K:N
ratio of the fertilizer stream. Likewise the N level may be raised by using nitric acid for part of the acidification. Acidification could also be effected with pressurized CO2 addition.
ratio of the fertilizer stream. Likewise the N level may be raised by using nitric acid for part of the acidification. Acidification could also be effected with pressurized CO2 addition.
[0010] The salt brine stream may include an Organic Certified compatible potash salt. The potash salt may include one of potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, and potassium nitrate.
[0011] The at least one forward osmosis membrane may be a semipermeable thin film composite membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, a semipermeable cellulosic membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, or any combination thereof.
[0012] In another aspect, an organic forward osmosis system that simultaneously treats digester centrate, recovers digester biomass intended for Organic Certified fertilizer, and augments that biomass with phosphorus, nitrate or CO2 is disclosed. The system may include a digester stage including a digesting operation configured to produce a digester centrate stream from waste. An acid treatment stage coupled to the digester stage and configured to receive the digester centrate stream and augment digester biomass with phosphorus or nitrate or CO2. The acid treatment stage includes an acid treatment operation that uses Organic Certified phosphoric acid, nitric acid or CO2 at an Organic Certifiable process pH of 3.5 to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream with a balanced P:K:N
ratio. A
forward osmosis stage is coupled to the acid treatment stage and configured to receive the acid treated, digester centrate stream from the acid treatment stage. The forward osmosis stage includes a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by: diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream comprising an Organic Certified compatible potash salt in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream maintained in the forward osmosis draw loop.
ratio. A
forward osmosis stage is coupled to the acid treatment stage and configured to receive the acid treated, digester centrate stream from the acid treatment stage. The forward osmosis stage includes a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by: diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream comprising an Organic Certified compatible potash salt in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream maintained in the forward osmosis draw loop.
[0013] Particular implementations may include one or more or all of the following.
[0014] The system may also be for recovering water for re-use and may include a reverse osmosis stage coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage. The reverse osmosis stage may include a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
[0015] The salt brine stream may include an Organic Certified compatible potash salt.
The potash salt may include one of potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, and potassium nitrate.
The potash salt may include one of potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, and potassium nitrate.
[0016] The system may also include a screening stage coupled to the digester stage and configured to receive the digester centrate stream. The screening stage may include a screening operation configured to produce a screened, digester centrate stream and a screened reject stream. The acid treatment stage may be coupled to the screening stage and configured to receive the screened, digester centrate stream. A filtering stage may be coupled to the acid treatment stage and configured to receive the fertilizer stream and may include a filtering operation configured to produce a filtered, fertilizer stream. A
drying stage may be coupled to both the screening stage and the filtering stage configured to receive the screened reject stream and the filtered, fertilizer stream, the drying stage and may include a drying operation configured to produce fertilizer.
100171 The at least one forward osmosis membrane may be a semipermeable thin film composite membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, a semipermeable cellulosic membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, or any combination thereof.
100181 In still another aspect, an organic forward osmosis system that simultaneously treats digester centrate, recovers digester biomass intended for Organic Certified fertilizer, augments that biomass with phosphorus or nitrogen or CO2, and recovers water for re-use is disclosed. The system may include a digester stage including a digesting operation configured to produce a digester centrate stream from waste. An acid treatment stage coupled to the digester stage and configured to receive the digester centrate stream and augment digester biomass with phosphorus or nitrogen or CO2. The acid treatment stage includes an acid treatment operation that uses Organic Certified phosphoric acid, nitric acid, or CO2 at an Organic Certifiable process pH of 3.5 to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream with a balanced P:K:N ratio. A forward osmosis stage is coupled to the acid treatment stage and configured to receive the acid treated, digester centrate stream from the acid treatment stage. The forward osmosis stage includes a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by: diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane;
and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream comprising an Organic Certified compatible potash salt in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream maintained in the forward osmosis draw loop. A reverse osmosis stage may be coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage. The reverse osmosis stage may include a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
[0019] Particular implementations may include one or more or all of the following.
[0020] The system may also be for recovering water for re-use and may include a reverse osmosis stage coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage. The reverse osmosis stage may include a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
[0021] The salt brine stream may include an Organic Certified compatible potash salt.
The potash salt may include one of potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, and potassium nitrate.
[0022] The system may also include a screening stage coupled to the digester stage and configured to receive the digester centrate stream. The screening stage may include a screening operation configured to produce a screened, digester centrate stream and a screened reject stream. The acid treatment stage may be coupled to the screening stage and configured to receive the screened, digester centrate stream. A filtering stage may be coupled to the acid treatment stage and configured to receive the fertilizer stream and may include a filtering operation configured to produce a filtered, fertilizer stream. A
drying stage may be coupled to both the screening stage and the filtering stage configured to receive the screened reject stream and the filtered, fertilizer stream, the drying stage and may include a drying operation configured to produce fertilizer.
[0023] The at least one forward osmosis membrane may be a semipermeable thin film composite membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, a semipermeable cellulosic membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, or any combination thereof.
[0024] The foregoing and other aspects, features, and advantages will be apparent to those of ordinary skill in the art from the DESCRIPTION and DRAWINGS, and from the CLAIMS.
BRIEF DESCRIPTION OF DRAWINGS
[0025] Implementations will hereinafter be described in conjunction with the appended DRAWINGS (which are not necessarily to scale), where like designations denote like elements.
[0026] FIG. 1 is a schematic block diagram of an implementation of an organic forward osmosis system.
DESCRIPTION
[0027] This document features organic forward osmosis systems. These systems embody the use of an acidic pretreatment of anaerobic digester centrate by the addition of phosphoric acid, nitric acid or CO2 with a follow-on use of forward osmosis (FO) with reverse osmosis (RO) for the simultaneous production of organic fertilizer and advanced water treatment. The systems and processes harvest pretreatment process sludge as fertilizer with the phosphorous and nitrogen integrated into it. This integration of processes into a single system (the combination of a phosphorus and nitrogen adding centrate pretreatment with FO/RO water production) achieves the nutrient (nitrogen to phosphorous) balancing of fertilizer production from agricultural biomass digesters while simultaneously harvesting potentially potable water grade water from the process.
[0028] The use of phosphoric acid used in organic fertilizer production to separate out the bulk of the useful organic and nitrogen material prior to the membrane based recovery of 50% to 80% of the digester centrate water for high grade water recycle for processes normally requiring new fresh water at or near drinking water quality is a unique synergy that has not been previously achieved. By integrating the water recovery with the required additions for balancing the fertilizer the water recovery chemical treatment cost and resource use is essentially 100% offset by the production requirements of fertilizer production.
[0029] There are many features of organic forward osmosis system implementations disclosed herein, of which one, a plurality, or all features or steps may be used in any particular implementation. In the following description, reference is made to the accompanying DRAWINGS which form a part hereof, and which show by way of illustration possible implementations. It is to be understood that other implementations may be utilized, and structural, as well as procedural, changes may be made without departing from the scope of this document. As a matter of convenience, various components will be described using exemplary materials, sizes, shapes, dimensions, and the like. However, this document is not limited to the stated examples and other configurations are possible and within the teachings of the present disclosure.
Overview [0030] FO provides a solution to the thermodynamics for a low value high mass application like fertilizer production. FO provides a non-membrane fouling anaerobic digester (e.g. anaerobic bacteria) biomass harvest and fertilizer production in combination with both phosphorus and nitrogen nutrient balancing and water treatment and high quality water recovery.
[0031] FO is a membrane technology that uses membranes with similar selectivity to those used in RO. But instead of applying high pressure to squeeze water from a solution, FO uses a solution with high osmotic potential to draw water through the membrane from a solution of low osmotic potential. The FO process (also termed direct osmotic concentration) has been described in an earlier patent (Herron et al.
US
5,821,430), which is hereby incorporated by reference.
[0032] FO was developed as a membrane based food processing water removal process, and thus can simultaneously remove water from liquid slurries similar to concentrated anaerobic digester centrate and produce RU level treated water as a byproduct. It should be noted that the recovery of nutrients at the FO
membrane has been used to retain subtle flavors and color compounds of food products and will be important to the organic fertilizer production and exquisitely thorough recovery of complex organic nutrients for use in the fertilizer. FO/RO will also deny these same nutrients to any receiving waters where these same nutrients would promote growth of aquatic plants and algae in the environment where that growth is not desirable.
[0033] Far less energy is required to separate and dewater digesters using an FO
membrane than other separation processes. If a constant source of brine is available that brine will provide better than 90% water removal (the recovery of up to 90% of the centrate water after acidic precipitation) and the retention of up to 98% of the nutrient value of the centrate water that is removed from the centrate by precipitation (the supernate) with no further energy input to the process than that required to bring both the digester bearing wastewater to one side of the membrane and the osmotic agent or brine to the other side of the membrane.
[0034] FO/RO will allow for high-grade water reuse production from high ammonia nitrogen (but low phosphorus) agricultural digester centrate/wastewater. This synergistic process is uniquely valuable to organic food production and processing operations, and represents a significant potential advance in sustainable food process technology.
Systems and Processes [0035] System implementations combine a phosphorus and nitrate adding centrate pretreatment with FO/RO water production that achieves the nutrient (nitrogen to phosphorous) balancing of fertilizer production from agricultural biomass digesters while simultaneously harvesting potentially potable water grade water.
[0036] There are a variety of organic forward osmosis system implementations that simultaneously treat digester centrate, recover digester biomass, augment that biomass with phosphorus, and recover water for reuse. Notwithstanding, turning to FIG.
1 and for the exemplary purposes of this disclosure, organic forward osmosis system 1 and its related process is shown. In system 1, FO is used in conjunction with RU to concentrate the waste stream and achieve high quality water recovery.
[0037] First, in a digester stage, bacteria or other digesters digest the food waste or other appropriate waste. For example, primary settling and one or more stages of anaerobic digestion may occur first in a standard anaerobic digester system 10 having a settling tank 12, a tank with water baffles 14 for example followed by a tank with a variable surface lid 16 for example to account for the heat and gases (e.g.
methane, carbon dioxide, etc.) from the digesters. The released methane gas can be collected and burned in a modified diesel generator for example to produce electricity.
[0038] Next, in a screening stage, the clarified residual liquid (the digester centrate) is then decanted off and pumped through a rough screening operation (here represented by an auger screen 20 for example). 200 to 400 micron screening is done at this primary screen stage and is a common practice for recovery of larger particles of plant and animal waste commonly entrained in the liquid centrate drained for food processing related digesters. Shaker screen 20 is then used to remove solids particles down to about 100 microns. In a drying stage, the resulting larger particles that were screened (the reject) are diverted to an air drying bin 30, while the screened digester centrate is diverted to the primary separation tank 40.
100391 At this point the suspended solids remaining in the screened digester centrate stream are colloidal or very slow settling but also quite problematic for all common forms of filtration or diffusion based membrane separation. This material is amenable to FO
membrane separation but is present at a concentration that would greatly overload this process too quickly to maintain operations. The process for recovery of usable water from this screened digester centrate stream is enabled in the separation tank 40 by the use of acidification and precipitation by pH adjustment from the ammonia driven high pH
values of the digester liquids (over pH 8) to well below the CO2 equivalency point (generally at or above 3.5). This acidification stage causes a precipitation driven separation of solids referred to as sweep-floc.
[0040] By using organically certifiable phosphoric acid and nitric acid (and possibly other balancing organically certified acid products (e.g., citric acid, sulfuric acid, and the like)) and having end point precipitation tank pHs near 3.5, the acidification process remains organically certifiable as well as an effective way to add necessary phosphors, nitrates and other components (e.g. sulfurs) to the wet solids at the bottom of the precipitation tank 40. In this way the common task of acidification pretreatment of the centrate wastewater is combined with the task of harvesting and nutrient balancing the solids that are to be re-tasked as marketable fertilizer. This will result in the correct balance of phosphors and other components (e.g. sulfurs) in the system and achieve the final fertilizer needs and N:P:K(:S) ratios.
[0041] Turning back to the process flow, in a filter stage wet solids at the bottom of the precipitation tank 40 are pumped through a sludge filter, belt press, screen, or any other filtration system 50. 15 to 60 micron screening is done at this stage.
The resulting larger particles that were filtered (the reject) are diverted to the air drying bin 30 to be re-tasked as marketable fertilizer, while the screened liquid is drawn into an ultra-filtration (UF) or Microfiltration (MF) membrane contactor 60. The UF reject water is returned to the anaerobic digester system 10 for enhanced concentration while the UF
produced water is drawn into the FO loop 70 of the FO stage (described next).
[0042] The FO stage is a process that involves selective mass transfer across a membrane that allows a desired component to cross the membrane from a solution of higher concentration of the component to a solution of lower concentration. A
semi-permeable membrane allows water to pass but blocks the movement of dissolved species.
[0043] The membrane may have a design similar to that disclosed in U.S.
Patent No.
4,033,878 to Foreman et al., entitled "Spiral Wound Membrane Module for Direct Osmosis Separations," issued July 5, 1977, the disclosure of which is hereby incorporated entirely herein by reference. A spiral wound membrane design configuration is inexpensive and can provide one of the greatest membrane surface areas in a vessel per cost (it can have a high membrane density (about 30 m2 per 20 cm diameter by 100 cm long element)).
[0044] In general, a spiral wound configuration, a permeate spacer, a feed spacer and two membranes can be wrapped around a perforated tube and glued in place. The membranes are wound between the feed spacer and the permeate spacer. Feed fluid is forced to flow longitudinally through the module through the feed spacer, and fluid passing through the membranes flows inward in a spiral through the permeate spacer to the center tube. To prevent feed fluid from entering the permeate spacer, the two membranes are glued to each other along their edges with the permeate spacer captured between them. The feed spacer remains unglued. Module assemblies are wound up to a desired diameter and the outsides are sealed.
[0045] In use, the membrane forces a draw solution (i.e., brine) to flow through the entire, single membrane envelope. The brine is pumped into one end of a center tube with perforations. A barrier element fixed halfway down the tube forces the brine flow through the perforations into the membrane envelope. A glue barrier is applied to the center of the membrane envelope so that fluid must flow to the far end of the membrane where a gap allows it to cross over to the other side of the membrane envelope then back into the second half of the center tube and out of the element. While a single envelope can be employed, there may be multiple envelopes wound/wrapped around the center tube with feed fluid spacers between the envelopes. Furthermore, a plurality of membranes may be used and may operate in a parallel flow configuration.
[0046] Here in FIG. 1, because the driving force causing the transfer of mass through the FO membrane is osmotic pressure, no additional energy input is required to cause the transfer to occur beyond what is required to place the solutions in contact with the membrane (through transfer pump 72, etc.). Water moves from the waste to the brine due to a concentration gradient and not due to applied pressure or heat or any other power input.
[0047] As a result, as salt brine is contacted to one side of the FO
membrane and dilute wastewater is contacted to the opposite side, water will diffuse through the membrane from the wastewater to the brine. The semi-permeable membrane will keep unwanted impurities and sediment in the wastewater, thus, producing clean diluted brine.
Depending upon the material used for the membrane, the structure of the membrane, and the arrangement of the membrane within the system, the amount and rate of transfer may be enhanced and/or controlled.
[0048] Specifically, at the point of acidification, the majority of the solids have been removed, but the supernatant in the primary separation tank 40 still contains a great deal of potentially high fouling materials that are fine enough to pass most filters but large enough to cause fouling of most membrane processes. FO provides membrane rejection and recovery of these partials and ionic contaminates while allowing over 90%
of the water to be recovered and then produced by the downstream RO system 86, which re-concentrates the osmotic agent (OA) to drive the FO. The OA may be composed of an Organic certification compatible potash salt (e.g. potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, potassium nitrate, and the like). The FO/RO combination provides an extremely low fouling membrane water treatment process for wastewaters like the pretreated supernatant. This combination of FO/RO with the phosphoric-nitric pretreatment and the synergistic nutrient balancing effect combine to produce the novel process.
[0049] Thus, during the FO stage the supernatant and UF produced water (high grade water consisting of 50% to 80% recovered digester centrate water) is then flowed through the FO membrane element 74 by transfer pump 72 and recycled. The OA or brine (high osmotic potential draw solution) from RO reject is pumped through the other side of the FO element 74 (i.e. on the other side of the FO membrane within the element 74). Water drawn across the membrane due to osmotic pull will dilute the OA or brine, which is then returned to the OA tank 82. The OA or brine is re-concentrated and maintained in a FO
draw solution loop 80. FO operates at low pressures thereby reducing fouling of the membrane. The only pressures applied are to provide circulation and are typically 1 to 2 Bar.
[0050] For the recovery of water, FO is followed by the collection of the diluted OA
or brine into the OA tank 82. Re-concentration of the brine after it absorbs water from the supernatant and UF produced water stream is accomplished by RO. Diluted OA
or brine from the OA tank is pumped by transfer pump 84 under pressure to the RO
system 86 elements where it is re-concentrated to appropriate draw strength, and the clean product water is simultaneously produced. This completes the recovery of wastewater to high-grade reuse water (e.g., 95% of the value of the wastewater). Thus, the RO system 86 produces a purified water stream that can be reused.
[0051] Thus, the wastewater can be from a food waste methane digester and FO can convert it into a useful fertilizer. Potassium Chloride brine can be used as the osmotic agent so that the fertilizer can be certified as Organic. The diluted brine can be re-concentrated by RO, delivering a purified water stream that can be reused in the food processing plant for example.
drying stage may be coupled to both the screening stage and the filtering stage configured to receive the screened reject stream and the filtered, fertilizer stream, the drying stage and may include a drying operation configured to produce fertilizer.
100171 The at least one forward osmosis membrane may be a semipermeable thin film composite membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, a semipermeable cellulosic membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, or any combination thereof.
100181 In still another aspect, an organic forward osmosis system that simultaneously treats digester centrate, recovers digester biomass intended for Organic Certified fertilizer, augments that biomass with phosphorus or nitrogen or CO2, and recovers water for re-use is disclosed. The system may include a digester stage including a digesting operation configured to produce a digester centrate stream from waste. An acid treatment stage coupled to the digester stage and configured to receive the digester centrate stream and augment digester biomass with phosphorus or nitrogen or CO2. The acid treatment stage includes an acid treatment operation that uses Organic Certified phosphoric acid, nitric acid, or CO2 at an Organic Certifiable process pH of 3.5 to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream with a balanced P:K:N ratio. A forward osmosis stage is coupled to the acid treatment stage and configured to receive the acid treated, digester centrate stream from the acid treatment stage. The forward osmosis stage includes a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by: diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane;
and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream comprising an Organic Certified compatible potash salt in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream maintained in the forward osmosis draw loop. A reverse osmosis stage may be coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage. The reverse osmosis stage may include a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
[0019] Particular implementations may include one or more or all of the following.
[0020] The system may also be for recovering water for re-use and may include a reverse osmosis stage coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage. The reverse osmosis stage may include a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
[0021] The salt brine stream may include an Organic Certified compatible potash salt.
The potash salt may include one of potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, and potassium nitrate.
[0022] The system may also include a screening stage coupled to the digester stage and configured to receive the digester centrate stream. The screening stage may include a screening operation configured to produce a screened, digester centrate stream and a screened reject stream. The acid treatment stage may be coupled to the screening stage and configured to receive the screened, digester centrate stream. A filtering stage may be coupled to the acid treatment stage and configured to receive the fertilizer stream and may include a filtering operation configured to produce a filtered, fertilizer stream. A
drying stage may be coupled to both the screening stage and the filtering stage configured to receive the screened reject stream and the filtered, fertilizer stream, the drying stage and may include a drying operation configured to produce fertilizer.
[0023] The at least one forward osmosis membrane may be a semipermeable thin film composite membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, a semipermeable cellulosic membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, or any combination thereof.
[0024] The foregoing and other aspects, features, and advantages will be apparent to those of ordinary skill in the art from the DESCRIPTION and DRAWINGS, and from the CLAIMS.
BRIEF DESCRIPTION OF DRAWINGS
[0025] Implementations will hereinafter be described in conjunction with the appended DRAWINGS (which are not necessarily to scale), where like designations denote like elements.
[0026] FIG. 1 is a schematic block diagram of an implementation of an organic forward osmosis system.
DESCRIPTION
[0027] This document features organic forward osmosis systems. These systems embody the use of an acidic pretreatment of anaerobic digester centrate by the addition of phosphoric acid, nitric acid or CO2 with a follow-on use of forward osmosis (FO) with reverse osmosis (RO) for the simultaneous production of organic fertilizer and advanced water treatment. The systems and processes harvest pretreatment process sludge as fertilizer with the phosphorous and nitrogen integrated into it. This integration of processes into a single system (the combination of a phosphorus and nitrogen adding centrate pretreatment with FO/RO water production) achieves the nutrient (nitrogen to phosphorous) balancing of fertilizer production from agricultural biomass digesters while simultaneously harvesting potentially potable water grade water from the process.
[0028] The use of phosphoric acid used in organic fertilizer production to separate out the bulk of the useful organic and nitrogen material prior to the membrane based recovery of 50% to 80% of the digester centrate water for high grade water recycle for processes normally requiring new fresh water at or near drinking water quality is a unique synergy that has not been previously achieved. By integrating the water recovery with the required additions for balancing the fertilizer the water recovery chemical treatment cost and resource use is essentially 100% offset by the production requirements of fertilizer production.
[0029] There are many features of organic forward osmosis system implementations disclosed herein, of which one, a plurality, or all features or steps may be used in any particular implementation. In the following description, reference is made to the accompanying DRAWINGS which form a part hereof, and which show by way of illustration possible implementations. It is to be understood that other implementations may be utilized, and structural, as well as procedural, changes may be made without departing from the scope of this document. As a matter of convenience, various components will be described using exemplary materials, sizes, shapes, dimensions, and the like. However, this document is not limited to the stated examples and other configurations are possible and within the teachings of the present disclosure.
Overview [0030] FO provides a solution to the thermodynamics for a low value high mass application like fertilizer production. FO provides a non-membrane fouling anaerobic digester (e.g. anaerobic bacteria) biomass harvest and fertilizer production in combination with both phosphorus and nitrogen nutrient balancing and water treatment and high quality water recovery.
[0031] FO is a membrane technology that uses membranes with similar selectivity to those used in RO. But instead of applying high pressure to squeeze water from a solution, FO uses a solution with high osmotic potential to draw water through the membrane from a solution of low osmotic potential. The FO process (also termed direct osmotic concentration) has been described in an earlier patent (Herron et al.
US
5,821,430), which is hereby incorporated by reference.
[0032] FO was developed as a membrane based food processing water removal process, and thus can simultaneously remove water from liquid slurries similar to concentrated anaerobic digester centrate and produce RU level treated water as a byproduct. It should be noted that the recovery of nutrients at the FO
membrane has been used to retain subtle flavors and color compounds of food products and will be important to the organic fertilizer production and exquisitely thorough recovery of complex organic nutrients for use in the fertilizer. FO/RO will also deny these same nutrients to any receiving waters where these same nutrients would promote growth of aquatic plants and algae in the environment where that growth is not desirable.
[0033] Far less energy is required to separate and dewater digesters using an FO
membrane than other separation processes. If a constant source of brine is available that brine will provide better than 90% water removal (the recovery of up to 90% of the centrate water after acidic precipitation) and the retention of up to 98% of the nutrient value of the centrate water that is removed from the centrate by precipitation (the supernate) with no further energy input to the process than that required to bring both the digester bearing wastewater to one side of the membrane and the osmotic agent or brine to the other side of the membrane.
[0034] FO/RO will allow for high-grade water reuse production from high ammonia nitrogen (but low phosphorus) agricultural digester centrate/wastewater. This synergistic process is uniquely valuable to organic food production and processing operations, and represents a significant potential advance in sustainable food process technology.
Systems and Processes [0035] System implementations combine a phosphorus and nitrate adding centrate pretreatment with FO/RO water production that achieves the nutrient (nitrogen to phosphorous) balancing of fertilizer production from agricultural biomass digesters while simultaneously harvesting potentially potable water grade water.
[0036] There are a variety of organic forward osmosis system implementations that simultaneously treat digester centrate, recover digester biomass, augment that biomass with phosphorus, and recover water for reuse. Notwithstanding, turning to FIG.
1 and for the exemplary purposes of this disclosure, organic forward osmosis system 1 and its related process is shown. In system 1, FO is used in conjunction with RU to concentrate the waste stream and achieve high quality water recovery.
[0037] First, in a digester stage, bacteria or other digesters digest the food waste or other appropriate waste. For example, primary settling and one or more stages of anaerobic digestion may occur first in a standard anaerobic digester system 10 having a settling tank 12, a tank with water baffles 14 for example followed by a tank with a variable surface lid 16 for example to account for the heat and gases (e.g.
methane, carbon dioxide, etc.) from the digesters. The released methane gas can be collected and burned in a modified diesel generator for example to produce electricity.
[0038] Next, in a screening stage, the clarified residual liquid (the digester centrate) is then decanted off and pumped through a rough screening operation (here represented by an auger screen 20 for example). 200 to 400 micron screening is done at this primary screen stage and is a common practice for recovery of larger particles of plant and animal waste commonly entrained in the liquid centrate drained for food processing related digesters. Shaker screen 20 is then used to remove solids particles down to about 100 microns. In a drying stage, the resulting larger particles that were screened (the reject) are diverted to an air drying bin 30, while the screened digester centrate is diverted to the primary separation tank 40.
100391 At this point the suspended solids remaining in the screened digester centrate stream are colloidal or very slow settling but also quite problematic for all common forms of filtration or diffusion based membrane separation. This material is amenable to FO
membrane separation but is present at a concentration that would greatly overload this process too quickly to maintain operations. The process for recovery of usable water from this screened digester centrate stream is enabled in the separation tank 40 by the use of acidification and precipitation by pH adjustment from the ammonia driven high pH
values of the digester liquids (over pH 8) to well below the CO2 equivalency point (generally at or above 3.5). This acidification stage causes a precipitation driven separation of solids referred to as sweep-floc.
[0040] By using organically certifiable phosphoric acid and nitric acid (and possibly other balancing organically certified acid products (e.g., citric acid, sulfuric acid, and the like)) and having end point precipitation tank pHs near 3.5, the acidification process remains organically certifiable as well as an effective way to add necessary phosphors, nitrates and other components (e.g. sulfurs) to the wet solids at the bottom of the precipitation tank 40. In this way the common task of acidification pretreatment of the centrate wastewater is combined with the task of harvesting and nutrient balancing the solids that are to be re-tasked as marketable fertilizer. This will result in the correct balance of phosphors and other components (e.g. sulfurs) in the system and achieve the final fertilizer needs and N:P:K(:S) ratios.
[0041] Turning back to the process flow, in a filter stage wet solids at the bottom of the precipitation tank 40 are pumped through a sludge filter, belt press, screen, or any other filtration system 50. 15 to 60 micron screening is done at this stage.
The resulting larger particles that were filtered (the reject) are diverted to the air drying bin 30 to be re-tasked as marketable fertilizer, while the screened liquid is drawn into an ultra-filtration (UF) or Microfiltration (MF) membrane contactor 60. The UF reject water is returned to the anaerobic digester system 10 for enhanced concentration while the UF
produced water is drawn into the FO loop 70 of the FO stage (described next).
[0042] The FO stage is a process that involves selective mass transfer across a membrane that allows a desired component to cross the membrane from a solution of higher concentration of the component to a solution of lower concentration. A
semi-permeable membrane allows water to pass but blocks the movement of dissolved species.
[0043] The membrane may have a design similar to that disclosed in U.S.
Patent No.
4,033,878 to Foreman et al., entitled "Spiral Wound Membrane Module for Direct Osmosis Separations," issued July 5, 1977, the disclosure of which is hereby incorporated entirely herein by reference. A spiral wound membrane design configuration is inexpensive and can provide one of the greatest membrane surface areas in a vessel per cost (it can have a high membrane density (about 30 m2 per 20 cm diameter by 100 cm long element)).
[0044] In general, a spiral wound configuration, a permeate spacer, a feed spacer and two membranes can be wrapped around a perforated tube and glued in place. The membranes are wound between the feed spacer and the permeate spacer. Feed fluid is forced to flow longitudinally through the module through the feed spacer, and fluid passing through the membranes flows inward in a spiral through the permeate spacer to the center tube. To prevent feed fluid from entering the permeate spacer, the two membranes are glued to each other along their edges with the permeate spacer captured between them. The feed spacer remains unglued. Module assemblies are wound up to a desired diameter and the outsides are sealed.
[0045] In use, the membrane forces a draw solution (i.e., brine) to flow through the entire, single membrane envelope. The brine is pumped into one end of a center tube with perforations. A barrier element fixed halfway down the tube forces the brine flow through the perforations into the membrane envelope. A glue barrier is applied to the center of the membrane envelope so that fluid must flow to the far end of the membrane where a gap allows it to cross over to the other side of the membrane envelope then back into the second half of the center tube and out of the element. While a single envelope can be employed, there may be multiple envelopes wound/wrapped around the center tube with feed fluid spacers between the envelopes. Furthermore, a plurality of membranes may be used and may operate in a parallel flow configuration.
[0046] Here in FIG. 1, because the driving force causing the transfer of mass through the FO membrane is osmotic pressure, no additional energy input is required to cause the transfer to occur beyond what is required to place the solutions in contact with the membrane (through transfer pump 72, etc.). Water moves from the waste to the brine due to a concentration gradient and not due to applied pressure or heat or any other power input.
[0047] As a result, as salt brine is contacted to one side of the FO
membrane and dilute wastewater is contacted to the opposite side, water will diffuse through the membrane from the wastewater to the brine. The semi-permeable membrane will keep unwanted impurities and sediment in the wastewater, thus, producing clean diluted brine.
Depending upon the material used for the membrane, the structure of the membrane, and the arrangement of the membrane within the system, the amount and rate of transfer may be enhanced and/or controlled.
[0048] Specifically, at the point of acidification, the majority of the solids have been removed, but the supernatant in the primary separation tank 40 still contains a great deal of potentially high fouling materials that are fine enough to pass most filters but large enough to cause fouling of most membrane processes. FO provides membrane rejection and recovery of these partials and ionic contaminates while allowing over 90%
of the water to be recovered and then produced by the downstream RO system 86, which re-concentrates the osmotic agent (OA) to drive the FO. The OA may be composed of an Organic certification compatible potash salt (e.g. potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, potassium nitrate, and the like). The FO/RO combination provides an extremely low fouling membrane water treatment process for wastewaters like the pretreated supernatant. This combination of FO/RO with the phosphoric-nitric pretreatment and the synergistic nutrient balancing effect combine to produce the novel process.
[0049] Thus, during the FO stage the supernatant and UF produced water (high grade water consisting of 50% to 80% recovered digester centrate water) is then flowed through the FO membrane element 74 by transfer pump 72 and recycled. The OA or brine (high osmotic potential draw solution) from RO reject is pumped through the other side of the FO element 74 (i.e. on the other side of the FO membrane within the element 74). Water drawn across the membrane due to osmotic pull will dilute the OA or brine, which is then returned to the OA tank 82. The OA or brine is re-concentrated and maintained in a FO
draw solution loop 80. FO operates at low pressures thereby reducing fouling of the membrane. The only pressures applied are to provide circulation and are typically 1 to 2 Bar.
[0050] For the recovery of water, FO is followed by the collection of the diluted OA
or brine into the OA tank 82. Re-concentration of the brine after it absorbs water from the supernatant and UF produced water stream is accomplished by RO. Diluted OA
or brine from the OA tank is pumped by transfer pump 84 under pressure to the RO
system 86 elements where it is re-concentrated to appropriate draw strength, and the clean product water is simultaneously produced. This completes the recovery of wastewater to high-grade reuse water (e.g., 95% of the value of the wastewater). Thus, the RO system 86 produces a purified water stream that can be reused.
[0051] Thus, the wastewater can be from a food waste methane digester and FO can convert it into a useful fertilizer. Potassium Chloride brine can be used as the osmotic agent so that the fertilizer can be certified as Organic. The diluted brine can be re-concentrated by RO, delivering a purified water stream that can be reused in the food processing plant for example.
Specifications, Materials, Manufacture, Assembly [0052] It will be understood that implementations are not limited to the specific components disclosed herein, as virtually any components consistent with the intended operation of an organic forward osmosis system may be utilized. Accordingly, for example, although particular components and so forth, are disclosed, such components may comprise any shape, size, style, type, model, version, class, grade, measurement, concentration, material, weight, quantity, and/or the like consistent with the intended operation of a organic forward osmosis system implementation. Implementations are not limited to uses of any specific components, provided that the components selected are consistent with the intended operation of an organic forward osmosis system implementation.
[0053] Accordingly, the components defining any organic forward osmosis system implementation may be formed of any of many different types of materials or combinations thereof that can readily be formed into shaped objects provided that the components selected are consistent with the intended operation of a organic forward osmosis system implementation. For example, the components may be formed of:
rubbers (synthetic and/or natural) and/or other like materials; glasses (such as fiberglass), carbon-fiber, aramid-fiber, any combination thereof, and/or other like materials; polymers such as thermoplastics (such as ABS, Acrylic, Fluoropolymers, Polyacetal, Polyamide;
Polycarbonate, Polyethylene, Polysulfone, and/or the like), thermosets (such as Epoxy, Phenolic Resin, Polyimide, Polyurethane, Silicone, and/or the like), any combination thereof, and/or other like materials; composites and/or other like materials;
metals and/or other like materials; alloys and/or other like materials; any other suitable material; and/or any combination thereof.
[0054] For the exemplary purposes of this disclosure, as a restatement of or in addition to what has already been described and disclosed above, the FO or PRO
membranes used in various implementations may be constructed of a wide variety of materials and have a wide variety of operating characteristics. For example, the membranes may be semi-permeable, meaning that they pass substantially exclusively the components that are desired from the solution of higher concentration to the solution of lower concentration, for example, passing water from a more dilute solution to a more concentrated solution. Any of a wide variety of membrane types may be utilized using the principles disclosed in this document.
[0055] Also, as a restatement of or in addition to what has already been described and disclosed above, the FO or PRO membranes used in various implementations may be made from a thin film composite RU membrane or a membrane cast by an immersion precipitation process (which could be cast on a porous support fabric such as woven or nonwoven nylon, polyester or polypropylene). The membranes used may be hydrophilic, membranes with salt rejections in the 80% to 95% range when tested as a reverse osmosis membrane (60 psi, 500 PPM NaC1, 10% recovery, 25° C.). The nominal molecular weight cut-off of the membrane may be 100 daltons. The membranes may be made from a hydrophilic membrane material, for example, cellulose acetate, cellulose proprianate, cellulose butyrate, cellulose diacetate, blends of cellulosic materials, polyurethane, polyamides. The membranes may be asymmetric (that is, for example, the membrane may have a thin rejection layer on the order of five (5) or less microns thick and a dense and porous sublayers up to 300 microns thick overall) and may be formed by an immersion precipitation process. The membranes are either unbacked, or have a very open backing that does not impede water reaching the rejection layer, or are hydrophilic and easily wick water to the membrane. Thus, for mechanical strength they may be cast upon a hydrophobic porous sheet backing, wherein the porous sheet is either woven or non-woven but having at least about 30% open area. The woven backing sheet may be a polyester screen having a total thickness of about 65 microns (polyester screen) and total asymmetric membrane is 105 microns in thickness. The asymmetric membrane may be cast by an immersion precipitation process by casting a cellulose material onto a polyester screen. The polyester screen may be 65 microns thick, 55% open area.
100561 For the exemplary purposes of this disclosure, the brines may generally be inorganic salt. For example, a brine may be Sodium chloride=6.21 wt %;
Potassium chloride=7.92 wt %, Trisodium citrate=10.41 wt %, and the like.
[0057] Various organic forward osmosis system implementations may be manufactured using conventional procedures as added to and improved upon through the procedures described here. Some components defining organic forward osmosis system implementations may be manufactured simultaneously and integrally joined with one another, while other components may be purchased pre-manufactured or manufactured separately and then assembled with the integral components.
[0058] Manufacture of these components separately or simultaneously may involve extrusion, pultrusion, vacuum forming, injection molding, blow molding, resin transfer molding, casting, forging, cold rolling, milling, drilling, reaming, turning, grinding, stamping, cutting, bending, welding, soldering, hardening, riveting, punching, plating, and/or the like. If any of the components are manufactured separately, they may then be coupled with one another in any manner, such as with adhesive, a weld, a fastener, wiring, any combination thereof, and/or the like for example, depending on, among other considerations, the particular material forming the components.
[0059] For the exemplary purposes of this disclosure, in one implementation a process for making a spiral wound membrane filter element or module may include: (a) assembling an envelope sandwich; (b) assembling a center tube onto the envelope sandwich; and (c) wrapping the envelope sandwich having the center tube and glue to form the spiral wound membrane module.
Use [0060] This synergistic organic FO system and process is uniquely valuable to organic food production and processing operations, and represents a significant potential advance in sustainable food process technology. The organic FO system and process simultaneously treats digester centrate, recovers digester biomass, augments that biomass with phosphorus, and recovers water for reuse.
[0061] Implementations of an organic FO system are also useful in a variety of other FO/water treatment applications, such as osmotic-driven water purification and filtration, desalination of sea water, purification of contaminated aqueous waste streams, and the like. Implementations may also be used for PRO systems. The difference is that PRO
generates osmotic pressure to drive a turbine or other energy-generating device. All that would be needed is to switch to feeding fresh water (as opposed to osmotic agent) and the salt water feed can be fed to the outside instead of source water (for water treatment applications).
[0062] In places where the description above refers to particular implementations, it should be readily apparent that a number of modifications may be made without departing from the spirit thereof and that these implementations may be alternatively applied. The accompanying CLAIMS are intended to cover such modifications as would fall within the true spirit and scope of the disclosure set forth in this document. The presently disclosed implementations are, therefore, to be considered in all respects as illustrative and not restrictive, the scope of the disclosure being indicated by the appended CLAIMS rather than the foregoing DESCRIPTION. All changes that come within the meaning of and range of equivalency of the CLAIMS are intended to be embraced therein.
[0053] Accordingly, the components defining any organic forward osmosis system implementation may be formed of any of many different types of materials or combinations thereof that can readily be formed into shaped objects provided that the components selected are consistent with the intended operation of a organic forward osmosis system implementation. For example, the components may be formed of:
rubbers (synthetic and/or natural) and/or other like materials; glasses (such as fiberglass), carbon-fiber, aramid-fiber, any combination thereof, and/or other like materials; polymers such as thermoplastics (such as ABS, Acrylic, Fluoropolymers, Polyacetal, Polyamide;
Polycarbonate, Polyethylene, Polysulfone, and/or the like), thermosets (such as Epoxy, Phenolic Resin, Polyimide, Polyurethane, Silicone, and/or the like), any combination thereof, and/or other like materials; composites and/or other like materials;
metals and/or other like materials; alloys and/or other like materials; any other suitable material; and/or any combination thereof.
[0054] For the exemplary purposes of this disclosure, as a restatement of or in addition to what has already been described and disclosed above, the FO or PRO
membranes used in various implementations may be constructed of a wide variety of materials and have a wide variety of operating characteristics. For example, the membranes may be semi-permeable, meaning that they pass substantially exclusively the components that are desired from the solution of higher concentration to the solution of lower concentration, for example, passing water from a more dilute solution to a more concentrated solution. Any of a wide variety of membrane types may be utilized using the principles disclosed in this document.
[0055] Also, as a restatement of or in addition to what has already been described and disclosed above, the FO or PRO membranes used in various implementations may be made from a thin film composite RU membrane or a membrane cast by an immersion precipitation process (which could be cast on a porous support fabric such as woven or nonwoven nylon, polyester or polypropylene). The membranes used may be hydrophilic, membranes with salt rejections in the 80% to 95% range when tested as a reverse osmosis membrane (60 psi, 500 PPM NaC1, 10% recovery, 25° C.). The nominal molecular weight cut-off of the membrane may be 100 daltons. The membranes may be made from a hydrophilic membrane material, for example, cellulose acetate, cellulose proprianate, cellulose butyrate, cellulose diacetate, blends of cellulosic materials, polyurethane, polyamides. The membranes may be asymmetric (that is, for example, the membrane may have a thin rejection layer on the order of five (5) or less microns thick and a dense and porous sublayers up to 300 microns thick overall) and may be formed by an immersion precipitation process. The membranes are either unbacked, or have a very open backing that does not impede water reaching the rejection layer, or are hydrophilic and easily wick water to the membrane. Thus, for mechanical strength they may be cast upon a hydrophobic porous sheet backing, wherein the porous sheet is either woven or non-woven but having at least about 30% open area. The woven backing sheet may be a polyester screen having a total thickness of about 65 microns (polyester screen) and total asymmetric membrane is 105 microns in thickness. The asymmetric membrane may be cast by an immersion precipitation process by casting a cellulose material onto a polyester screen. The polyester screen may be 65 microns thick, 55% open area.
100561 For the exemplary purposes of this disclosure, the brines may generally be inorganic salt. For example, a brine may be Sodium chloride=6.21 wt %;
Potassium chloride=7.92 wt %, Trisodium citrate=10.41 wt %, and the like.
[0057] Various organic forward osmosis system implementations may be manufactured using conventional procedures as added to and improved upon through the procedures described here. Some components defining organic forward osmosis system implementations may be manufactured simultaneously and integrally joined with one another, while other components may be purchased pre-manufactured or manufactured separately and then assembled with the integral components.
[0058] Manufacture of these components separately or simultaneously may involve extrusion, pultrusion, vacuum forming, injection molding, blow molding, resin transfer molding, casting, forging, cold rolling, milling, drilling, reaming, turning, grinding, stamping, cutting, bending, welding, soldering, hardening, riveting, punching, plating, and/or the like. If any of the components are manufactured separately, they may then be coupled with one another in any manner, such as with adhesive, a weld, a fastener, wiring, any combination thereof, and/or the like for example, depending on, among other considerations, the particular material forming the components.
[0059] For the exemplary purposes of this disclosure, in one implementation a process for making a spiral wound membrane filter element or module may include: (a) assembling an envelope sandwich; (b) assembling a center tube onto the envelope sandwich; and (c) wrapping the envelope sandwich having the center tube and glue to form the spiral wound membrane module.
Use [0060] This synergistic organic FO system and process is uniquely valuable to organic food production and processing operations, and represents a significant potential advance in sustainable food process technology. The organic FO system and process simultaneously treats digester centrate, recovers digester biomass, augments that biomass with phosphorus, and recovers water for reuse.
[0061] Implementations of an organic FO system are also useful in a variety of other FO/water treatment applications, such as osmotic-driven water purification and filtration, desalination of sea water, purification of contaminated aqueous waste streams, and the like. Implementations may also be used for PRO systems. The difference is that PRO
generates osmotic pressure to drive a turbine or other energy-generating device. All that would be needed is to switch to feeding fresh water (as opposed to osmotic agent) and the salt water feed can be fed to the outside instead of source water (for water treatment applications).
[0062] In places where the description above refers to particular implementations, it should be readily apparent that a number of modifications may be made without departing from the spirit thereof and that these implementations may be alternatively applied. The accompanying CLAIMS are intended to cover such modifications as would fall within the true spirit and scope of the disclosure set forth in this document. The presently disclosed implementations are, therefore, to be considered in all respects as illustrative and not restrictive, the scope of the disclosure being indicated by the appended CLAIMS rather than the foregoing DESCRIPTION. All changes that come within the meaning of and range of equivalency of the CLAIMS are intended to be embraced therein.
Claims (19)
1. An organic forward osmosis system for concentrating digester biomass intended for Organic Certified fertilizer comprising:
an acid treatment stage comprising an acid treatment operation configured to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream; and a forward osmosis stage coupled to the acid treatment stage configured to receive the acid treated, digester centrate stream from the acid treatment stage, the forward osmosis stage comprising a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by:
diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream.
an acid treatment stage comprising an acid treatment operation configured to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream; and a forward osmosis stage coupled to the acid treatment stage configured to receive the acid treated, digester centrate stream from the acid treatment stage, the forward osmosis stage comprising a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by:
diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream.
2. The system of claim I wherein the diluted salt brine stream is maintained in the forward osmosis draw loop.
3. The system of claim 2 further for recovering water for re-use, the system further comprising a reverse osmosis stage coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage, the reverse osmosis stage comprising a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
4. The system of claim I wherein the acid treatment stage is configured to augment digester biomass with phosphorus and the acid treatment operation comprises using one of Organic Certified phosphoric acid, nitric acid, and CO2 at an Organic Certifiable process pH of 3.5, thereby balancing a P:K:N ratio of the fertilizer stream.
5. The system of claim 1 wherein the salt brine stream comprises an Organic Certified compatible potash salt.
6. The system of claim 5 wherein the Organic Certified compatible potash salt comprises one of potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, and potassium nitrate.
7. The system of claim 1 wherein the at least one forward osmosis membrane is one of a semipermeable thin film composite membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, a semipermeable cellulosic membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, and any combination thereof.
8. The system of claim 1 wherein the at least one forward osmosis membrane comprises a plurality of forward osmosis membranes that operate in a parallel flow configuration.
9. An organic forward osmosis system that simultaneously treats digester centrate, recovers digester biomass intended for Organic Certified fertilizer, and augments that biomass with phosphorus and nitrogen, the system comprising:
a digester stage comprising a digesting operation configured to produce a digester centrate stream from waste;
an acid treatment stage coupled to the digester stage and configured to receive the digester centrate stream and augment digester biomass with phosphorus and nitrogen, the acid treatment stage comprising an acid treatment operation that uses one of Organic Certified phosphoric acid, nitric acid, and CO2 at an Organic Certifiable process pH of 3.5 to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream with a balanced P:K:N ratio; and a forward osmosis stage coupled to the acid treatment stage configured to receive the acid treated, digester centrate stream from the acid treatment stage, the forward osmosis stage comprising a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by:
diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream comprising an Organic Certified compatible potash salt in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream maintained in the forward osmosis draw loop.
a digester stage comprising a digesting operation configured to produce a digester centrate stream from waste;
an acid treatment stage coupled to the digester stage and configured to receive the digester centrate stream and augment digester biomass with phosphorus and nitrogen, the acid treatment stage comprising an acid treatment operation that uses one of Organic Certified phosphoric acid, nitric acid, and CO2 at an Organic Certifiable process pH of 3.5 to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream with a balanced P:K:N ratio; and a forward osmosis stage coupled to the acid treatment stage configured to receive the acid treated, digester centrate stream from the acid treatment stage, the forward osmosis stage comprising a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by:
diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream comprising an Organic Certified compatible potash salt in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream maintained in the forward osmosis draw loop.
10. The system of claim 9 further for recovering water for re-use, the system further comprising a reverse osmosis stage coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage, the reverse osmosis stage comprising a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
11. The system of claim 9 wherein the Organic Certified compatible potash salt comprises one of potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, and potassium nitrate.
12. The system of claim 9 further comprising:
a screening stage coupled to the digester stage and configured to receive the digester centrate stream, the screening stage comprising a screening operation configured to produce a screened, digester centrate stream and a screened reject stream;
wherein the acid treatment stage is coupled to the screening stage and configured to receive the screened, digester centrate stream;
a filtering stage coupled to the acid treatment stage and configured to receive the fertilizer stream and comprising a filtering operation configured to produce a filtered, fertilizer stream; and a drying stage coupled to both the screening stage and the filtering stage configured to receive the screened reject stream and the filtered, fertilizer stream, the drying stage comprising a drying operation configured to produce fertilizer.
a screening stage coupled to the digester stage and configured to receive the digester centrate stream, the screening stage comprising a screening operation configured to produce a screened, digester centrate stream and a screened reject stream;
wherein the acid treatment stage is coupled to the screening stage and configured to receive the screened, digester centrate stream;
a filtering stage coupled to the acid treatment stage and configured to receive the fertilizer stream and comprising a filtering operation configured to produce a filtered, fertilizer stream; and a drying stage coupled to both the screening stage and the filtering stage configured to receive the screened reject stream and the filtered, fertilizer stream, the drying stage comprising a drying operation configured to produce fertilizer.
13. The system of claim 1 wherein the at least one forward osmosis membrane is one of a semipermeable thin film composite membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, a semipermeable cellulosic membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, and any combination thereof
14. The system of claim 1 wherein the at least one forward osmosis membrane comprises a plurality of forward osmosis membranes that operate in a parallel flow configuration.
15. An organic forward osmosis system that simultaneously treats digester centrate, recovers digester biomass intended for Organic Certified fertilizer, augments that biomass with phosphorus and nitrogen, and recovers water for re-use, the system comprising:
a digester stage comprising a digesting operation configured to produce a digester centrate stream from waste;
an acid treatment stage coupled to the digester stage and configured to receive the digester centrate stream and augment digester biomass with phosphorus and nitrogen, the acid treatment stage comprising an acid treatment operation that uses one of Organic Certified phosphoric acid, nitric acid, and CO2 at an Organic Certifiable process pH of 3.5 to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream with a balanced P:K:N ratio; and a forward osmosis stage coupled to the acid treatment stage configured to receive the acid treated, digester centrate stream from the acid treatment stage, the forward osmosis stage comprising a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by:
diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream comprising an Organic Certified compatible potash salt in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream maintained in the forward osmosis draw loop; and a reverse osmosis stage coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage, the reverse osmosis stage comprising a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
a digester stage comprising a digesting operation configured to produce a digester centrate stream from waste;
an acid treatment stage coupled to the digester stage and configured to receive the digester centrate stream and augment digester biomass with phosphorus and nitrogen, the acid treatment stage comprising an acid treatment operation that uses one of Organic Certified phosphoric acid, nitric acid, and CO2 at an Organic Certifiable process pH of 3.5 to produce an acid treated, digester centrate stream in a forward osmosis reject loop and a fertilizer stream with a balanced P:K:N ratio; and a forward osmosis stage coupled to the acid treatment stage configured to receive the acid treated, digester centrate stream from the acid treatment stage, the forward osmosis stage comprising a forward osmosis operation configured to remove water from the acid treated, digester centrate stream by:
diverting the acid treated, digester centrate stream to one side of at least one forward osmosis membrane; and contacting an opposite side of the at least one forward osmosis membrane with a salt brine stream comprising an Organic Certified compatible potash salt in a forward osmosis draw loop and osmotically pulling water across the at least one forward osmosis membrane from the acid treated, digester centrate stream to the salt brine stream using only a concentration gradient; and thereby producing a concentrated, acid treated, digester centrate stream and a diluted salt brine stream maintained in the forward osmosis draw loop; and a reverse osmosis stage coupled to the forward osmosis stage configured to receive the diluted salt brine stream from the forward osmosis stage, the reverse osmosis stage comprising a reverse osmosis operation configured to pump under pressure the diluted salt brine stream to at least one reverse osmosis membrane and produce a re-concentrated salt brine stream maintained in the forward osmosis draw loop and a recycled purified water stream for re-use.
16. The system of claim 15 wherein the Organic Certified compatible potash salt comprises one of potassium chloride, potassium carbonate, potassium sulfate, potassium magnesium sulfate, langbeinite, and potassium nitrate.
17. The system of claim 15 further comprising:
a screening stage coupled to the digester stage and configured to receive the digester centrate stream, the screening stage comprising a screening operation configured to produce a screened, digester centrate stream and a screened reject stream;
wherein the acid treatment stage is coupled to the screening stage and configured to receive the screened, digester centrate stream;
a filtering stage coupled to the acid treatment stage and configured to receive the fertilizer stream and comprising a filtering operation configured to produce a filtered, fertilizer stream; and a drying stage coupled to both the screening stage and the filtering stage configured to receive the screened reject stream and the filtered, fertilizer stream, the drying stage comprising a drying operation configured to produce fertilizer.
a screening stage coupled to the digester stage and configured to receive the digester centrate stream, the screening stage comprising a screening operation configured to produce a screened, digester centrate stream and a screened reject stream;
wherein the acid treatment stage is coupled to the screening stage and configured to receive the screened, digester centrate stream;
a filtering stage coupled to the acid treatment stage and configured to receive the fertilizer stream and comprising a filtering operation configured to produce a filtered, fertilizer stream; and a drying stage coupled to both the screening stage and the filtering stage configured to receive the screened reject stream and the filtered, fertilizer stream, the drying stage comprising a drying operation configured to produce fertilizer.
18. The system of claim 15 wherein the at least one forward osmosis membrane is one of a semipermeable thin film composite membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, a semipermeable cellulosic membrane in one of a fiber, plate and frame, and spiral wound membrane configuration, and any combination thereof.
19. The system of claim 15 wherein the at least one forward osmosis membrane comprises a plurality of forward osmosis membranes that operate in a parallel flow configuration.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA 2775230 CA2775230A1 (en) | 2012-04-19 | 2012-04-19 | Organic forward osmosis system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA 2775230 CA2775230A1 (en) | 2012-04-19 | 2012-04-19 | Organic forward osmosis system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2775230A1 true CA2775230A1 (en) | 2013-10-19 |
Family
ID=49378633
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2775230 Abandoned CA2775230A1 (en) | 2012-04-19 | 2012-04-19 | Organic forward osmosis system |
Country Status (1)
| Country | Link |
|---|---|
| CA (1) | CA2775230A1 (en) |
-
2012
- 2012-04-19 CA CA 2775230 patent/CA2775230A1/en not_active Abandoned
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| FZDE | Discontinued |
Effective date: 20150422 |