WO2022174128A1 - H2o2 on-site production - Google Patents
H2o2 on-site production Download PDFInfo
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- WO2022174128A1 WO2022174128A1 PCT/US2022/016250 US2022016250W WO2022174128A1 WO 2022174128 A1 WO2022174128 A1 WO 2022174128A1 US 2022016250 W US2022016250 W US 2022016250W WO 2022174128 A1 WO2022174128 A1 WO 2022174128A1
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- 238000004519 manufacturing process Methods 0.000 title claims abstract description 30
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 123
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 claims abstract description 59
- 229910003455 mixed metal oxide Inorganic materials 0.000 claims abstract description 27
- 239000007784 solid electrolyte Substances 0.000 claims abstract description 23
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 21
- 238000009792 diffusion process Methods 0.000 claims abstract description 15
- 230000005611 electricity Effects 0.000 claims abstract description 13
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 239000008367 deionised water Substances 0.000 claims abstract description 8
- 229910021641 deionized water Inorganic materials 0.000 claims abstract description 8
- 238000000034 method Methods 0.000 claims description 22
- 239000012528 membrane Substances 0.000 claims description 21
- 239000007789 gas Substances 0.000 claims description 19
- 239000011324 bead Substances 0.000 claims description 18
- 238000005341 cation exchange Methods 0.000 claims description 17
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 15
- 239000001301 oxygen Substances 0.000 claims description 15
- 229910052760 oxygen Inorganic materials 0.000 claims description 15
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 claims description 11
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 claims description 10
- 239000000356 contaminant Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 10
- 239000003792 electrolyte Substances 0.000 claims description 10
- 239000003011 anion exchange membrane Substances 0.000 claims description 8
- 229920003303 ion-exchange polymer Polymers 0.000 claims description 8
- 230000008569 process Effects 0.000 claims description 8
- 238000011282 treatment Methods 0.000 claims description 8
- 229910052785 arsenic Inorganic materials 0.000 claims description 7
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 claims description 7
- 239000003456 ion exchange resin Substances 0.000 claims description 7
- 239000002253 acid Substances 0.000 claims description 6
- 239000006199 nebulizer Substances 0.000 claims description 6
- 238000004065 wastewater treatment Methods 0.000 claims description 6
- 238000011065 in-situ storage Methods 0.000 claims description 5
- 229910052742 iron Inorganic materials 0.000 claims description 5
- 238000006243 chemical reaction Methods 0.000 claims description 4
- 239000003014 ion exchange membrane Substances 0.000 claims description 4
- 239000003595 mist Substances 0.000 claims description 4
- 238000009303 advanced oxidation process reaction Methods 0.000 claims description 3
- 239000000645 desinfectant Substances 0.000 claims description 3
- 238000009297 electrocoagulation Methods 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 3
- 238000004659 sterilization and disinfection Methods 0.000 claims description 3
- 238000005345 coagulation Methods 0.000 claims description 2
- 230000015271 coagulation Effects 0.000 claims description 2
- 238000001914 filtration Methods 0.000 claims description 2
- 239000008235 industrial water Substances 0.000 claims description 2
- 238000001556 precipitation Methods 0.000 claims description 2
- 238000000746 purification Methods 0.000 claims description 2
- 238000004064 recycling Methods 0.000 claims description 2
- 238000004062 sedimentation Methods 0.000 claims description 2
- 238000002242 deionisation method Methods 0.000 claims 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 239000003729 cation exchange resin Substances 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 5
- 238000005342 ion exchange Methods 0.000 description 4
- 239000011347 resin Substances 0.000 description 4
- 229920005989 resin Polymers 0.000 description 4
- 235000011149 sulphuric acid Nutrition 0.000 description 4
- 239000001117 sulphuric acid Substances 0.000 description 4
- 238000013459 approach Methods 0.000 description 3
- 238000002474 experimental method Methods 0.000 description 3
- 229920000557 Nafion® Polymers 0.000 description 2
- PYKYMHQGRFAEBM-UHFFFAOYSA-N anthraquinone Natural products CCC(=O)c1c(O)c2C(=O)C3C(C=CC=C3O)C(=O)c2cc1CC(=O)OC PYKYMHQGRFAEBM-UHFFFAOYSA-N 0.000 description 2
- 150000004056 anthraquinones Chemical class 0.000 description 2
- 229920001429 chelating resin Polymers 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- -1 peroxide anion Chemical class 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- RTAQQCXQSZGOHL-UHFFFAOYSA-N Titanium Chemical compound [Ti] RTAQQCXQSZGOHL-UHFFFAOYSA-N 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 238000011021 bench scale process Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000010349 cathodic reaction Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 231100001261 hazardous Toxicity 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- MYWUZJCMWCOHBA-SECBINFHSA-N levmetamfetamine Chemical compound CN[C@H](C)CC1=CC=CC=C1 MYWUZJCMWCOHBA-SECBINFHSA-N 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000007800 oxidant agent Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 230000002572 peristaltic effect Effects 0.000 description 1
- 229920000515 polycarbonate Polymers 0.000 description 1
- 239000004417 polycarbonate Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000012508 resin bead Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- HDUMBHAAKGUHAR-UHFFFAOYSA-J titanium(4+);disulfate Chemical compound [Ti+4].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O HDUMBHAAKGUHAR-UHFFFAOYSA-J 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J3/00—Processes of utilising sub-atmospheric or super-atmospheric pressure to effect chemical or physical change of matter; Apparatus therefor
- B01J3/006—Processes utilising sub-atmospheric pressure; Apparatus therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J10/00—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor
- B01J10/02—Chemical processes in general for reacting liquid with gaseous media other than in the presence of solid particles, or apparatus specially adapted therefor of the thin-film type
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46109—Electrodes
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/467—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction
- C02F1/4672—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrochemical disinfection; by electrooxydation or by electroreduction by electrooxydation
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- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
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- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
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- C25B11/03—Electrodes; Manufacture thereof not otherwise provided for characterised by shape or form perforated or foraminous
- C25B11/031—Porous electrodes
- C25B11/032—Gas diffusion electrodes
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- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
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- C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
- C25B11/052—Electrodes comprising one or more electrocatalytic coatings on a substrate
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- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
- C25B11/04—Electrodes; Manufacture thereof not otherwise provided for characterised by the material
- C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
- C25B11/055—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the substrate or carrier material
- C25B11/057—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the substrate or carrier material consisting of a single element or compound
- C25B11/061—Metal or alloy
- C25B11/063—Valve metal, e.g. titanium
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- C25B11/00—Electrodes; Manufacture thereof not otherwise provided for
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- C25B11/051—Electrodes formed of electrocatalysts on a substrate or carrier
- C25B11/073—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material
- C25B11/091—Electrodes formed of electrocatalysts on a substrate or carrier characterised by the electrocatalyst material consisting of at least one catalytic element and at least one catalytic compound; consisting of two or more catalytic elements or catalytic compounds
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- C25B15/00—Operating or servicing cells
- C25B15/08—Supplying or removing reactants or electrolytes; Regeneration of electrolytes
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- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
- C25B9/17—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof
- C25B9/19—Cells comprising dimensionally-stable non-movable electrodes; Assemblies of constructional parts thereof with diaphragms
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
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- C02F2001/46152—Electrodes characterised by the shape or form
- C02F2001/46157—Perforated or foraminous electrodes
- C02F2001/46161—Porous electrodes
- C02F2001/46166—Gas diffusion electrodes
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/103—Arsenic compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/46115—Electrolytic cell with membranes or diaphragms
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/4616—Power supply
- C02F2201/4617—DC only
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2201/00—Apparatus for treatment of water, waste water or sewage
- C02F2201/46—Apparatus for electrochemical processes
- C02F2201/461—Electrolysis apparatus
- C02F2201/46105—Details relating to the electrolytic devices
- C02F2201/46195—Cells containing solid electrolyte
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2305/00—Use of specific compounds during water treatment
- C02F2305/02—Specific form of oxidant
- C02F2305/026—Fenton's reagent
Definitions
- Hydrogen peroxide (3 ⁇ 4(3 ⁇ 4) is commonly used chemical for domestic and industrial applications such as disinfection, water, and wastewater treatment.
- 3 ⁇ 4(3 ⁇ 4 is produced industrially by an anthraquinone process (Campos -Martin et al., 2006).
- This traditional process is energy intensive and economically feasible at industrial scale owing to low yields of 3 ⁇ 4(3 ⁇ 4 where additional steps are required to make it more concentrated.
- Xia et al. (Science, 11 Oct 2019, 366 (6462); 226-231) proposed a novel method using a solid electrolyte, atmospheric oxygen, pure deionized water, and hydrogen gas to generate highly concentrated H2O2 in water, reportedly achieving 20% (on a w/w basis). This method is promising for achieving concentrated H2O2 in decentralized locations addressing the limitations of the anthraquinone process.
- the invention provides methods, composition, and systems for on-site decentralized production of 3 ⁇ 4(3 ⁇ 4 with atmospheric 02, water, and electricity.
- the invention provides a system for H2O2 on-site production without 3 ⁇ 4 gas or deionized water, comprising an air humidifier, a condenser, and a reactor, wherein (a) the air humidifier is configured to produce and feed a stream of air saturated with water vapor into the reactor through the condenser, (b) the condenser is configured to cool the air from the humidifier, and convert some of the water vapor to liquid form as it enters the reactor, and (c) the reactor comprises a porous solid electrolyte (ion exchange resins), proton exchange membrane, mixed metal oxide anode and a gas diffusion cathode.
- the solid electrolyte comprises two packed beds of ion exchange resin beads.
- MMO mixed-metal-oxide
- cation- exchange membrane such as a proton exchange membrane, trade name Nafion
- the cooling function is separated from the H 2 O 2 production function, wherein liquid water is first obtained through chilling a humid stream, and then separately, some of that water and atmospheric oxygen are electrically converted into H 2 O 2 , see, e.g. Fig.
- a stream of air saturated with water vapor is passed through an electrical chiller and the resulting water condensate is continuously fed into the delivery chamber of a nebulizer, wherein the exit nozzle of the nebulizer is aimed at the exterior surface of the air-cathode, wherein a fine mist of condensate water collects on the active surface of the air cathode, and reacts with atmospheric O 2 in the presence of electricity to produce H 2 O 2 in-situ, which then drips down the surface of the air cathode to be collected;
- the system is configured wherein the entire reaction of oxygen reduction to H 2 O 2 formation takes place at the interface of air diffusion cathode, condensed water, and ion exchange beads. As the condensed water flows through the porous solid electrolyte, H 2 O 2 is collected from the interface (air diffusion cathode, water, and solid electrolyte) and flushed out along with residual condensed water to form H 2 O 2 solution.
- the system is configured wherein the entire reaction takes place on the water- film on the solid electrolyte beads, as air saturated with water-vapor flows through the porous electrolyte, H 2 O 2 is generated in the water film on the electrolyte beads is flushed out as vapor with rest of the airflow, and at the exit of the reactor, a condenser captures vapor of water and H 2 O 2 and coverts into H 2 O 2 solution.
- the system is configured with the use of a cation exchange membrane positioned between anode and cathode to allow the transport of protons to the cathode, and block the transport of peroxide anion ( HCF ) from the electrolyte to the anode, improving the production rate of 3 ⁇ 4(3 ⁇ 4 from the device;
- a cation exchange membrane positioned between anode and cathode to allow the transport of protons to the cathode, and block the transport of peroxide anion ( HCF ) from the electrolyte to the anode, improving the production rate of 3 ⁇ 4(3 ⁇ 4 from the device;
- the system is configured with the use of an anion exchange membrane positioned between anode and cathode to allow the transport of peroxide anion (HCF ) from the cathode into the bulk solid electrolyte which will be flushed out along with condensed water.
- HCF peroxide anion
- the system is configured with the use of a cation exchange membrane positioned in front of the anode, and an anion-exchange-membrane in front of the cathode, the anion exchange membrane prevents the transport of protons to the cathode, and the cation exchange membrane blocks the transport of HO2 from the electrolyte to the anode, improving the production rate of H2O2 from the device;
- the system is configured along with an iron based electrochemical system (Fe-EC) used for arsenic and other contaminants removal.
- Fe-EC iron based electrochemical system
- the cathodic reaction leads to the generation of 3 ⁇ 4 gas on the cathode, which is normally released to the atmosphere.
- Fe- EC processes aeration is required to maintain dissolved oxygen levels in the water releasing humid air into the headspace of the reactor.
- the humid air from the head space of Fe-EC reactors saturated with water vapor and 3 ⁇ 4 gas is supplied through a condenser to the solid electrolyte based electrochemical system for H2O2 generation described above.
- the 3 ⁇ 4 gas is oxidized at the MMO anode first instead of water oxidation to oxygen, generating H2O2 at lower cell potential compared to the reactor configurations described in Fig. 1.
- the in-situ generated FFCFin this system may be used in Fe-EC system as an external oxidant to remove arsenic and other contaminants at large treatment volumes at low operating costs, thus avoiding the supply chain of H2O2;
- the system comprises inlet water
- the air humidifier is configured to receive the inlet water to produce the stream of air saturated with water vapor
- the inlet (input) water is of a poor quality water source, including unprocessed, untreated (e.g. without water purification treatments such as filtration, sedimentation, precipitation, disinfection and coagulation, etc) water sources, including raw pond, well or river water, rainwater or runoff, reclaimed municipal, agricultural or industrial water sources, etc. and/or
- the system is configured to provide an observed Faradaic efficiency of H2O2 of 10-30%.
- the invention provides a method of on-site production of H2O2 with only electricity and poor-quality water, and without 3 ⁇ 4 gas or deionized water, the method comprising deploying a disclosed system;
- the invention provides a method of H2O2 on-site production with electricity and poor quality water, and without 3 ⁇ 4 gas or deionized water, the method comprising: (a) producing air saturated with water vapor with an air humidifier; (b) feeding a stream of the air saturated with water vapor though a condenser into an 3 ⁇ 4(3 ⁇ 4 production reactor comprising a porous solid electrolyte (a packed bed of ion exchange resin beads) sandwiched between a mixed-metal-oxide (MMO) anode and a gas diffusion cathode, wherein the condenser cools the air and converts some of the water vapor to liquid form as it enters the porous solid electrolyte; (c) applying a DC current between the electrodes, wherein water is oxidized to O2 on the MMO anode, and atmospheric oxygen entering through the air-diffusion-cathode is reduced to H2O2 in the presence of water and this H2O2 is flushed out of
- FIG. 2 Schematic of working prototype of the reactor device. Operating current density and voltage in this experimental setup was 15 mA/cm2 and 4.23 V. The observed Faradaic efficiency of H2O2 was 10 % in preliminary experiments, and optimized in subsequent experiments to 10-30%.
- FIG. 3 Schematic of the reactor device wherein the cooling function is separated from the H2O2 production function, wherein liquid water is first obtained through chilling a humid stream, and then separately, some of that water and atmospheric oxygen are electrically converted into H2O2
- H2O2 production reactor comprises a porous solid electrolyte (a packed bed of ion exchange resin beads) sandwiched between a mixed-metal-oxide (MMO) anode and a gas diffusion cathode.
- MMO mixed-metal-oxide
- a commercially available air-humidifier feeds a stream of air, saturated with water- vapor, that enters our reactor through a condenser.
- the condenser cools the air and converts some of the water vapor to liquid form as it enters the porous solid electrolyte.
- some of the condensed water is oxidized to O2 on the MMO anode, and the atmospheric oxygen entering through the air-diffusion-cathode is reduced to H2O2 in presence of water at the solid electrolyte and air cathode interface.
- This H2O2 is flushed out of the reactor with the unreacted water as a H2O2 solution.
- H2O2 solution At outlet, drops of H2O2 solution will be collected, which can be used (i) in water treatment applications such as iron electrocoagulation process used for removing arsenic and other contaminants at high throughput volumes (ii) in UV assisted advanced oxidation processes in wastewater treatment for removing emerging contaminants of concern (iii) to make dilute disinfectant for domestic uses or in hospitals.
- a bench scale electrochemical reactor was built with rectangular polycarbonate sheets (14 cm x 14 cm) to form two closed chambers (Anodic and Cathodic) separated by an ion-exchange membrane (e.g., Nafion, CMI-7000 from Membranes International Inc. or any other cation-exchange membrane).
- the anode chamber has an empty volume -100 ml, and is filled with cation exchange resin beads (e.g., “Amberlite IRC- 120H” obtained from thermo scientific) as a solid electrolyte.
- One side of the anode chamber is formed with an MMO mesh (mixed metal oxide IrC RuCU coating on Titanium mesh, 8 cm X 8 cm from Magneto Special Anodes, Netherlands), and the other opposite side of the anode chamber is an (8 cm X 8 cm) cation exchange membrane.
- MMO mesh mixed metal oxide IrC RuCU coating on Titanium mesh, 8 cm X 8 cm from Magneto Special Anodes, Netherlands
- 8 cm X 8 cm) cation exchange membrane This MMO anode is in close physical and electrical contact with cation exchange resin beads located inside the anode chamber.
- the cation exchange membrane too is in close physical and electrical contact with the cation exchange resin beads.
- a dilute chilled solution of sulphuric acid (10 miliMolar) is continuously recirculated through the cation exchange resin bed, at a flow rate of 10 mL/min with a peristaltic pump.
- the dilute solution of sulphuric acid is maintained at a chilled temperature (about 5 C) by passing the tubing through an ice bath.
- the cathode chamber has an empty volume -100 ml, and is also filled with cation exchange resin beads (e.g., Amberlite IRC-120H) which acts as a solid electrolyte.
- the other active surface of the cathode chamber is an air diffusion cathode (8 cm X 8 cm, recipe was described in Barazesh et al 2015).
- the cathode chamber has a multiplicity of air-inlets at the top side, and a multiplicity of outlets at the bottom side. The outlets at the bottom side are connected to a collection chamber that is evacuated continuously with a small air pump (1/16th HP).
- the inlets at the top side are supplied with air saturated with water vapor at about room temperature, obtained from an evaporative humidifier (e.g., a commercially available model Vicks Warm Mist Humidifier, V745A/V745-JUV).
- an evaporative humidifier e.g., a commercially available model Vicks Warm Mist Humidifier, V745A/V745-JUV.
- the air saturated with water vapor from the evaporative humidifier is sucked into the cathode chamber owing to the depressurized collection chamber connected to the cathode chamber.
- the air experiences a drop in temperature owing to the passage of chilled sulphuric acid on the other side of the cathodic ion exchange membrane. This causes a release of pure water (3 ⁇ 40) in the interstitial spaces in the resin bed.
- a plurality of heat extraction devices e.g., solid-state Peltier cooling modules (12V 6A Thermoelectric Peltier, Eujgoov, purchased from Amazon.com, or cooling coils from a small vapor compression chiller, e.g., Frigidaire chiller model EFMIS137) are installed in thermal contact with (but electrical isolation from) the MMO Anode. Operation of the cooling mechanism leads to continuous heat extraction from the anode chamber, and therefore also from the cathode chamber. The interstitial spaces in the resin beads in the anode chamber are filled with diluted inactive acid (e.g. 10 mM dilute sulfuric acid) to improve conductivity of the ion bed.
- diluted inactive acid e.g. 10 mM dilute sulfuric acid
- Air saturated with water vapor is passed through the cathode chamber as described above. Pure water condenses at the surfaces of the ion exchange beads in the cathode chamber as described above, passage of electricity converts some of that water into H2O2 as described above. Condensed water, generated 3 ⁇ 4(3 ⁇ 4, and supplied air all exit together into the low-pressure collection chamber, from which the air is extracted continuously with a small pump as described above.
- the reactor is designed and filled with cation exchange resin beads as described above, with differences: (1) the resin bed in the anode chamber is filled with a dilute (10 mM) solution of sulphuric acid, but it is not circulated, and there is no cooling of the anode chamber; (2) the catalyst side (of carbon black) of the air cathode is made to face away from the resin bed; and/or (3) there is a collection mechanism for the H2O2 formed on the exterior surface of the air-cathode, as it drips down into a gutter.
- the cooling function is separated from the 3 ⁇ 4(3 ⁇ 4 production function, compared to the first two embodiments described above.
- a stream of air saturated with water vapor is passed through a small electrical chiller (such as Frigidaire chiller model EFMIS137) and the resulting water condensate is continuously fed into the delivery chamber of a small electric nebulizer (e.g., “just Nebulizers” model J- 1100312).
- the exit nozzle of the nebulizer is aimed at the exterior surface of the air-cathode. Fine mist of condensate water collects on the active surface of the air cathode, and reacts with atmospheric 02 in the presence of electricity to produce H2O2 in- situ, which then drips down the surface of the air cathode to be collected and used.
Abstract
On-site decentralized production of H2O2 is achieved with atmospheric O2, poor quality water and electricity, and without external supply of H2 gas or deionized water, with a system comprising an air humidifier, a condenser, and a electrochemical reactor, wherein the air humidifier is configured to produce and feed a stream of air saturated with water-vapor into the reactor through the condenser, the condenser is configured to cool the air from the humidifier, and convert some of the water vapor to liquid form as it enters the reactor, and the reactor comprises a porous solid electrolyte sandwiched between a mixed-metal-oxide anode and a gas diffusion cathode.
Description
H2O2 on-site production
This invention was made with government support under Contract Number DE- IA0000018 awarded by the U.S. Department of Energy. The government has certain rights in the invention.
[01] Introduction
[02] Hydrogen peroxide (¾(¾) is commonly used chemical for domestic and industrial applications such as disinfection, water, and wastewater treatment. Currently, ¾(¾ is produced industrially by an anthraquinone process (Campos -Martin et al., 2006). This traditional process is energy intensive and economically feasible at industrial scale owing to low yields of ¾(¾ where additional steps are required to make it more concentrated. Recently, Xia et al. (Science, 11 Oct 2019, 366 (6462); 226-231) proposed a novel method using a solid electrolyte, atmospheric oxygen, pure deionized water, and hydrogen gas to generate highly concentrated H2O2 in water, reportedly achieving 20% (on a w/w basis). This method is promising for achieving concentrated H2O2 in decentralized locations addressing the limitations of the anthraquinone process.
[03] However, this prior method may be infeasible or impractical in remote low-income communities or developing countries where access to hydrogen gas and high quality DI water is challenging or nonexistent. Overcoming the limitations of prior systems, and building on our own experimental systems, we describe a novel approach to synthesize H2O2 for onsite use without the supply of hydrogen gas and DI water, that is practical even in remote locations with supply chain limitations.
[04] Summary of the Invention
[05] The invention provides methods, composition, and systems for on-site decentralized production of ¾(¾ with atmospheric 02, water, and electricity.
[06] In an aspect the invention provides a system for H2O2 on-site production without ¾ gas or deionized water, comprising an air humidifier, a condenser, and a reactor, wherein (a) the air humidifier is configured to produce and feed a stream of air saturated with water vapor into the reactor through the condenser, (b) the condenser is configured to cool the air from the humidifier, and convert some of the water vapor to liquid form as it enters the reactor, and (c) the reactor comprises a porous solid electrolyte (ion exchange resins), proton exchange membrane, mixed metal oxide anode and a gas diffusion cathode. The solid electrolyte comprises two packed beds of ion exchange resin beads. One bed is sandwiched between a mixed-metal-oxide (MMO) anode and cation- exchange membrane (such as a proton exchange membrane, trade name Nafion), and
the second packed bed is between the cation-exchange membrane and a gas (air) diffusion cathode.
[07] The arrangement is schematically described in Figure 1. A cold dilute solution of acid in water is continuously pumped through the bed between the MMO anode and the cation- exchange membrane. Water vapor that is passed through the second bed between the cation- exchange membrane and the air-diffusion cathode, condenses into liquid water upon giving up its heat through the cation-exchange membrane to the chilled acid bed. An external DC voltage (of about 4.3 volts) is applied across the electrode. In our experiments this developed a current of 0.99 Amps, for electrodes of area about 100 sq. cm. each. Upon applying this external voltage, water is oxidized to O2 on the MMO anode, and atmospheric oxygen entering through the gas- diffusion-cathode is reduced to H2O2 in the presence of water inside the pores surrounding the ion exchange beds or in the presence of water film on the ion exchange beads. Freshly formed H2O2 inside the pores of the solid electrolyte is flushed out of the reactor with the unreacted water to form H2O2 solution and collected at the outlet as shown in Fig. 1.
[08] In embodiments:
[09] the cooling function is separated from the H2O2 production function, wherein liquid water is first obtained through chilling a humid stream, and then separately, some of that water and atmospheric oxygen are electrically converted into H2O2, see, e.g. Fig. 3, optionally, wherein a stream of air saturated with water vapor is passed through an electrical chiller and the resulting water condensate is continuously fed into the delivery chamber of a nebulizer, wherein the exit nozzle of the nebulizer is aimed at the exterior surface of the air-cathode, wherein a fine mist of condensate water collects on the active surface of the air cathode, and reacts with atmospheric O2 in the presence of electricity to produce H2O2 in-situ, which then drips down the surface of the air cathode to be collected;
[10] the system is configured wherein the entire reaction of oxygen reduction to H2O2 formation takes place at the interface of air diffusion cathode, condensed water, and ion exchange beads. As the condensed water flows through the porous solid electrolyte, H2O2 is collected from the interface (air diffusion cathode, water, and solid electrolyte) and flushed out along with residual condensed water to form H2O2 solution.
[11] the system is configured wherein the entire reaction takes place on the water- film on the solid electrolyte beads, as air saturated with water-vapor flows through the porous electrolyte, H2O2 is generated in the water film on the electrolyte beads is flushed out as vapor with rest of the airflow, and at the exit of the reactor, a condenser captures vapor of water and H2O2 and coverts into H2O2 solution.
[12] the system is configured with the use of a cation exchange membrane positioned
between anode and cathode to allow the transport of protons to the cathode, and block the transport of peroxide anion ( HCF ) from the electrolyte to the anode, improving the production rate of ¾(¾ from the device;
[13] the system is configured with the use of an anion exchange membrane positioned between anode and cathode to allow the transport of peroxide anion (HCF ) from the cathode into the bulk solid electrolyte which will be flushed out along with condensed water.
[14] the system is configured with the use of a cation exchange membrane positioned in front of the anode, and an anion-exchange-membrane in front of the cathode, the anion exchange membrane prevents the transport of protons to the cathode, and the cation exchange membrane blocks the transport of HO2 from the electrolyte to the anode, improving the production rate of H2O2 from the device;
[lf|] the system is configured along with an iron based electrochemical system (Fe-EC) used for arsenic and other contaminants removal. Wherein Fe-EC system, the cathodic reaction leads to the generation of ¾ gas on the cathode, which is normally released to the atmosphere. In Fe- EC processes aeration is required to maintain dissolved oxygen levels in the water releasing humid air into the headspace of the reactor. The humid air from the head space of Fe-EC reactors saturated with water vapor and ¾ gas is supplied through a condenser to the solid electrolyte based electrochemical system for H2O2 generation described above. The ¾ gas is oxidized at the MMO anode first instead of water oxidation to oxygen, generating H2O2 at lower cell potential compared to the reactor configurations described in Fig. 1. The in-situ generated FFCFin this system may be used in Fe-EC system as an external oxidant to remove arsenic and other contaminants at large treatment volumes at low operating costs, thus avoiding the supply chain of H2O2;
[16] the system comprises inlet water, the air humidifier is configured to receive the inlet water to produce the stream of air saturated with water vapor, the inlet (input) water is of a poor quality water source, including unprocessed, untreated (e.g. without water purification treatments such as filtration, sedimentation, precipitation, disinfection and coagulation, etc) water sources, including raw pond, well or river water, rainwater or runoff, reclaimed municipal, agricultural or industrial water sources, etc. and/or
[17] the system is configured to provide an observed Faradaic efficiency of H2O2 of 10-30%.
[18] In an aspect the invention provides a method of on-site production of H2O2 with only electricity and poor-quality water, and without ¾ gas or deionized water, the method comprising deploying a disclosed system;
[19] In an aspect the invention provides a method of H2O2 on-site production with electricity and poor quality water, and without ¾ gas or deionized water, the method comprising: (a)
producing air saturated with water vapor with an air humidifier; (b) feeding a stream of the air saturated with water vapor though a condenser into an ¾(¾ production reactor comprising a porous solid electrolyte (a packed bed of ion exchange resin beads) sandwiched between a mixed-metal-oxide (MMO) anode and a gas diffusion cathode, wherein the condenser cools the air and converts some of the water vapor to liquid form as it enters the porous solid electrolyte; (c) applying a DC current between the electrodes, wherein water is oxidized to O2 on the MMO anode, and atmospheric oxygen entering through the air-diffusion-cathode is reduced to H2O2 in the presence of water and this H2O2 is flushed out of the reactor with the unreacted water as a H2O2 solution; and (d) collecting at the outlet of the reactor, drops of H2O2 solution, which can be used (i) in water treatment applications such as iron electrocoagulation process used for removing arsenic and other contaminants at high throughput volumes (ii) in an UV assisted advanced oxidation processes in wastewater treatment for removing emerging contaminants of concern (iii) to make dilute disinfectant for domestic uses or in hospitals.
[20] The invention encompasses all combinations of the particular embodiments recited herein, as if each combination had been laboriously recited.
[21] Brief Description of the Drawings
[22] Fig. 1. Schematic of the configuration 1 reactor design
[23] Fig. 2. Schematic of working prototype of the reactor device. Operating current density and voltage in this experimental setup was 15 mA/cm2 and 4.23 V. The observed Faradaic efficiency of H2O2 was 10 % in preliminary experiments, and optimized in subsequent experiments to 10-30%.
[24] Fig. 3. Schematic of the reactor device wherein the cooling function is separated from the H2O2 production function, wherein liquid water is first obtained through chilling a humid stream, and then separately, some of that water and atmospheric oxygen are electrically converted into H2O2
[25] Description of Particular Embodiments of the Invention
[26] Unless contraindicated or noted otherwise, in these descriptions and throughout this specification, the terms “a” and “an” mean one or more, the term “or” means and/or. The examples and embodiments described herein are for illustrative purposes only and that various modifications or changes in light thereof will be suggested to persons skilled in the art and are to be included within the spirit and purview of this application and scope of the appended claims. All publications, patents, and patent applications cited herein, including citations therein, are hereby incorporated by reference in their entirety for all purposes.
[27] This invention provides for on-site decentralized production of lUCUwith atmospheric O2, poor quality water (e.g., pond water), and electricity. It overcomes the supply chain limitations of more stringent inputs demanded by current state of the art devices for ¾(¾ production.
[28] In our novel approach, we use water vapor in a stream of saturated air to obtain a ¾(¾ solution. A fraction of the water molecules are converted to ¾(¾ and the rest of condensed water is used to capture and flush the ¾(¾ into an outlet stream. Our H2O2 production reactor comprises a porous solid electrolyte (a packed bed of ion exchange resin beads) sandwiched between a mixed-metal-oxide (MMO) anode and a gas diffusion cathode. A commercially available air-humidifier feeds a stream of air, saturated with water- vapor, that enters our reactor through a condenser. The condenser cools the air and converts some of the water vapor to liquid form as it enters the porous solid electrolyte. Upon applying a DC current between the electrodes, some of the condensed water is oxidized to O2 on the MMO anode, and the atmospheric oxygen entering through the air-diffusion-cathode is reduced to H2O2 in presence of water at the solid electrolyte and air cathode interface. This H2O2 is flushed out of the reactor with the unreacted water as a H2O2 solution. At outlet, drops of H2O2 solution will be collected, which can be used (i) in water treatment applications such as iron electrocoagulation process used for removing arsenic and other contaminants at high throughput volumes (ii) in UV assisted advanced oxidation processes in wastewater treatment for removing emerging contaminants of concern (iii) to make dilute disinfectant for domestic uses or in hospitals.
[29] One embodiment of this invention is as follows. A bench scale electrochemical reactor was built with rectangular polycarbonate sheets (14 cm x 14 cm) to form two closed chambers (Anodic and Cathodic) separated by an ion-exchange membrane (e.g., Nafion, CMI-7000 from Membranes International Inc. or any other cation-exchange membrane). The anode chamber has an empty volume -100 ml, and is filled with cation exchange resin beads (e.g., “Amberlite IRC- 120H” obtained from thermo scientific) as a solid electrolyte. One side of the anode chamber is formed with an MMO mesh (mixed metal oxide IrC RuCU coating on Titanium mesh, 8 cm X 8 cm from Magneto Special Anodes, Netherlands), and the other opposite side of the anode chamber is an (8 cm X 8 cm) cation exchange membrane. This MMO anode is in close physical and electrical contact with cation exchange resin beads located inside the anode chamber. The cation exchange membrane too is in close physical and electrical contact with the cation exchange resin beads. A dilute chilled solution of sulphuric acid (10 miliMolar) is continuously recirculated through the cation exchange resin bed, at a flow rate of 10 mL/min with a peristaltic pump. The dilute solution of sulphuric acid is maintained at a chilled temperature (about 5 C) by passing the tubing through an ice bath. The cathode chamber has an empty volume -100 ml, and
is also filled with cation exchange resin beads (e.g., Amberlite IRC-120H) which acts as a solid electrolyte. The other active surface of the cathode chamber is an air diffusion cathode (8 cm X 8 cm, recipe was described in Barazesh et al 2015). The cathode chamber has a multiplicity of air-inlets at the top side, and a multiplicity of outlets at the bottom side. The outlets at the bottom side are connected to a collection chamber that is evacuated continuously with a small air pump (1/16th HP). The inlets at the top side are supplied with air saturated with water vapor at about room temperature, obtained from an evaporative humidifier (e.g., a commercially available model Vicks Warm Mist Humidifier, V745A/V745-JUV). The air saturated with water vapor from the evaporative humidifier is sucked into the cathode chamber owing to the depressurized collection chamber connected to the cathode chamber. During its passage through the interstitial spaces in the cathode exchange resins, the air experiences a drop in temperature owing to the passage of chilled sulphuric acid on the other side of the cathodic ion exchange membrane. This causes a release of pure water (¾0) in the interstitial spaces in the resin bed. Chemical reactions described above are driven by passage of externally supplied electricity to the device. In this embodiment, a DC voltage of 8 Volts was applied across the MMO anode and the air-cathode, and a current of 2.5 Amps was observed. The condensate captured in the collection chamber under these conditions was about 100 mL per hour, and it was observed to have an ¾(¾ concentration of 1600 mg/L. (measurement made using a HACH DR 6000 spectrophotometer with the titanium(IV) sulfate method at 405 nm). We observed that this production rate and this H2O2 concentration could be maintained for several hours without degradation of the production.
[30] In another embodiment, a plurality of heat extraction devices (e.g., solid-state Peltier cooling modules (12V 6A Thermoelectric Peltier, Eujgoov, purchased from Amazon.com, or cooling coils from a small vapor compression chiller, e.g., Frigidaire chiller model EFMIS137) are installed in thermal contact with (but electrical isolation from) the MMO Anode. Operation of the cooling mechanism leads to continuous heat extraction from the anode chamber, and therefore also from the cathode chamber. The interstitial spaces in the resin beads in the anode chamber are filled with diluted inactive acid (e.g. 10 mM dilute sulfuric acid) to improve conductivity of the ion bed. Air saturated with water vapor is passed through the cathode chamber as described above. Pure water condenses at the surfaces of the ion exchange beads in the cathode chamber as described above, passage of electricity converts some of that water into H2O2 as described above. Condensed water, generated ¾(¾, and supplied air all exit together into the low-pressure collection chamber, from which the air is extracted continuously with a small pump as described above.
[31] In another embodiment of the invention, the reactor is designed and filled with cation exchange resin beads as described above, with differences: (1) the resin bed in the anode
chamber is filled with a dilute (10 mM) solution of sulphuric acid, but it is not circulated, and there is no cooling of the anode chamber; (2) the catalyst side (of carbon black) of the air cathode is made to face away from the resin bed; and/or (3) there is a collection mechanism for the H2O2 formed on the exterior surface of the air-cathode, as it drips down into a gutter. In this embodiment, the cooling function is separated from the ¾(¾ production function, compared to the first two embodiments described above. A stream of air saturated with water vapor is passed through a small electrical chiller (such as Frigidaire chiller model EFMIS137) and the resulting water condensate is continuously fed into the delivery chamber of a small electric nebulizer (e.g., “just Nebulizers” model J- 1100312). The exit nozzle of the nebulizer is aimed at the exterior surface of the air-cathode. Fine mist of condensate water collects on the active surface of the air cathode, and reacts with atmospheric 02 in the presence of electricity to produce H2O2 in- situ, which then drips down the surface of the air cathode to be collected and used.
[32] With this invention, there is no need for H2 gas or deionized pure water to produce H2O2 solution. All needed supplies are widely available: namely atmospheric oxygen, any acceptable water for the humidifier, and some electricity, thus overcoming the supply chain limitations of the H2O2 production of prior methods.
[33] Advantages of our novel approach include:
[34] (i) on site generation of H2O2 using locally available resources with minimal supply chain;
[35] (ii) does not involve hazardous hydrogen gas;
[36] (iii) continuous recirculation of the chilled dilute acid through the anode chamber reduces the ohmic heating of the constituents inside the reactors (e.g., electrolyte, ion exchange resins and membrane) especially at high current densities ranging from 5 mA/cm2 to 1000 mA/cm2;
[37] (iv) locally available water can be used to make water vapor which will be fed into our reactor;
[38] (v) regions where high humidity exists, air can be pumped directly into our reactor to make H2O2. These conditions can exist near coastal areas, and locally within centralized plants for water and wastewater treatment;
[39] (vi) our process does not require expensive and highly flammable hydrogen gas as an input supply and therefore is safer and less costly than prior H2O2 production methods such as Xia (2019, supra);
[40] (vii) practical applications including community and municipal scale drinking water treatments, community and municipal scale recycling and reuse of wastewater treated effluent, industrial wastewater treatment, treating hospital wastewater.
Claims
1. A system for ¾(¾ on-site production without external supply of ¾ gas or deionized water, comprising: an air humidifier, a condenser, and a reactor, wherein the air humidifier is configured to produce and feed a stream of air saturated with water vapor into the reactor through the condenser, the condenser is configured to cool the air from the humidifier, and convert some of the water vapor to liquid form as it enters the reactor, the reactor comprises a porous solid electrolyte configured as a packed bed of ion exchange resin beads sandwiched between a mixed-metal-oxide (MMO) anode and a gas (air) diffusion cathode, and upon applying a DC current between the electrodes, water is oxidized to 02 on the MMO anode, and atmospheric oxygen entering through the gas diffusion cathode is reduced in presence of condensed water to form H2O2, and this H2O2 is flushed out of the reactor with unreacted water, and H2O2 solution is collected at the outlet.
2. The system of claim 1, wherein the cooling function is separated from the H2O2 production function, wherein liquid water is first obtained through chilling a humid stream, and then separately, some of that water and atmospheric oxygen are electrically converted into H2O2.
3. The system of claim 1, wherein the cooling function is separated from the ¾(¾ production function, wherein liquid water is first obtained through chilling a humid stream, and then separately, some of that water and atmospheric oxygen are electrically converted into ¾(¾, wherein a stream of air saturated with water vapor is passed through an electrical chiller and the resulting water condensate is continuously fed into the delivery chamber of a nebulizer, wherein the exit nozzle of the nebulizer is aimed at the exterior surface of the air-cathode, wherein a fine mist of condensate water collects on the active surface of the air cathode, and reacts with atmospheric O2 in the presence of electricity to produce ¾(¾ in-situ, which then drips down the surface of the air cathode to be collected.
4. The system of claim 1, configured wherein the entire reaction takes place on the water-film on the solid electrolyte beads or in the pore water surrounding the solid electrolyte beads, as air saturated with water- vapor flows through the porous electrolyte, ¾(¾ is generated in the water film on the electrolyte beads and is flushed out with the unreacted water as a ¾(¾ solution
which is collected at the outlet.
5. The system of claim 1, configured with the use of a cation- exchange membrane positioned in front of the anode, and an anion-exchange-membrane in front of the cathode, the anion exchange membrane prevents the transport of protons to the cathode, and the cation exchange membrane blocks the transport of HC from the electrolyte to the anode, improving the production rate of H2O2 from the device.
6. The system of claim 1, configured wherein the reactor comprises an air diffusion cathode fabricated with ion exchange polymers, similar to the cathodes employed in membrane capacitive deionization technology, wherein this modified air diffusion cathodes avoids the use of ion exchange membranes in the reactor.
7. The system of claim 1, configured wherein the reactor comprises a solid-state cooler (e.g., thermoelectric modules), externally connected to the anode side of the reactor to avoid recycling of chilled acid for additional cooling of the reactor. In this configuration, the inside of the MMO anode is wetted with dilute acid and a thin layer (thickness ~ mm) of solid electrolyte is used in between the cation exchange membrane and the MMO anode which results in smaller voltage drop in the reactor.
8. The system of claim 1, configured with the use of only cation-exchange membrane positioned in front of the anode, to block the transport of HO2 from the electrolyte to the anode, improving the production rate of ¾(¾ from the device.
9. The system of claim 1, configured with the use of only anion-exchange-membrane positioned in front of the air diffusion cathode to prevent the transport of protons to the cathode, improving the production rate of ¾(¾ from the device.
10. The system of claim 1, configured with the use of a cation-exchange membrane positioned in front of the anode, and an anion-exchange-membrane in front of the cathode, the anion exchange membrane prevents the transport of protons to the cathode, and the cation exchange membrane blocks the transport of HO2 from the electrolyte to the anode, improving the production rate of H2O2 from the device.
11. The system of claim 1, configured wherein the operating voltages ranges from 0.5 V to 1000
V and operating current densities ranges from 0.1 mA/cm2 to 1000 mA/cm2.
12. The system of claim 1, coupled with an iron based electrochemical system (Fe-EC) used for arsenic and other contaminants removal, wherein air saturated with water and EE gas from the head space of the Fe-EC reactors is collected and supplied to the electrochemical reactor described above through a condenser. The e condensed water vapor is used to generate concentrated H2O2 at the outlet, wherein the EE gas is oxidized at the MMO anode first, before splitting of water into oxygen, wherein the in-situ generated H2O2 in this system may be used in Fe-EC system to remove arsenic and other contaminants at large treatment volumes at low operating costs, avoiding the supply chain of H2O2.
13. The system of claim 1, configured to provide an observed Faradaic efficiency of H2O2 of 10- 30%.
14. The system of claim 1 wherein the system comprises inlet water, the air humidifier is configured to receive the inlet water to produce the stream of air saturated with water vapor, the inlet (input) water is of a poor quality water source, including unprocessed, untreated (e.g. without water purification treatments such as filtration, sedimentation, precipitation, disinfection and coagulation, etc.) water sources, including raw pond, well or river water, rainwater or runoff, reclaimed municipal, agricultural or industrial water sources, etc.
15. A method of ¾(¾ on-site production with electricity and poor quality water, and without external supply of ¾ gas or deionized water, the method comprising deploying or operating the system of any of claim 1-14 to produce ¾(¾.
16. A method of ¾(¾ on-site production with electricity and poor quality water, and without external supply of ¾ gas or deionized water, the method comprising: producing air saturated with water vapor with an air humidifier; feeding a stream of the air saturated with water vapor though a condenser into an ¾(¾ production reactor comprising a porous solid electrolyte (a packed bed of ion exchange resin beads) sandwiched between a mixed-metal-oxide (MMO) anode and a gas diffusion cathode, wherein the condenser cools the air and converts some of the water vapor to liquid form as it enters the porous solid electrolyte; applying a DC current between the electrodes, wherein some of the condensed water is oxidized to O2 on the MMO anode, and atmospheric oxygen entering through the air- diffusion-
cathode is reduced to ¾(¾ in the presence of water and this ¾(¾ is flushed out of the reactor with the unreacted water as a ¾(¾ solution; and collecting at the outlet of the reactor, drops of concentrated ¾(¾, which are suitable for use (i) in water treatment applications such as iron electrocoagulation process used for removing arsenic and other contaminants at high throughput volumes (ii) in UV assisted advanced oxidation processes in wastewater treatment for removing emerging contaminants of concern (iii) to make dilute disinfectant for domestic uses or in hospitals.
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US6254762B1 (en) * | 1998-09-28 | 2001-07-03 | Permelec Electrode Ltd. | Process and electrolytic cell for producing hydrogen peroxide |
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