[go: up one dir, main page]

US20140206912A1 - Underground reactor system - Google Patents

Underground reactor system Download PDF

Info

Publication number
US20140206912A1
US20140206912A1 US14/115,278 US201214115278A US2014206912A1 US 20140206912 A1 US20140206912 A1 US 20140206912A1 US 201214115278 A US201214115278 A US 201214115278A US 2014206912 A1 US2014206912 A1 US 2014206912A1
Authority
US
United States
Prior art keywords
reactor
organic material
underground
temperature
pump
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
Application number
US14/115,278
Other languages
English (en)
Inventor
Brandon Iglesias
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Tulane University
Original Assignee
Tulane University
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Assigned to BIOLEX, INC. reassignment BIOLEX, INC. TERMINATION OF SECURITY INTEREST Assignors: INTERSOUTH PARTNERS IV, L.P., AS ATTORNEY-IN-FACT FOR THE SECURED PARTIES PURSUANT TO THE SECURITY AGREEMENTS
Application filed by Tulane University filed Critical Tulane University
Priority to US14/115,278 priority Critical patent/US20140206912A1/en
Publication of US20140206912A1 publication Critical patent/US20140206912A1/en
Abandoned legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24T—GEOTHERMAL COLLECTORS; GEOTHERMAL SYSTEMS
    • F24T10/00—Geothermal collectors
    • F24T10/10—Geothermal collectors with circulation of working fluids through underground channels, the working fluids not coming into direct contact with the ground
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/008—Controlling or regulating of liquefaction processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M21/00—Bioreactors or fermenters specially adapted for specific uses
    • C12M21/12—Bioreactors or fermenters specially adapted for specific uses for producing fuels or solvents
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/02—Form or structure of the vessel
    • C12M23/06—Tubular
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M23/00—Constructional details, e.g. recesses, hinges
    • C12M23/02—Form or structure of the vessel
    • C12M23/18—Open ponds; Greenhouse type or underground installations
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M29/00—Means for introduction, extraction or recirculation of materials, e.g. pumps
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/12—Means for regulation, monitoring, measurement or control, e.g. flow regulation of temperature
    • C12M41/18—Heat exchange systems, e.g. heat jackets or outer envelopes
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M43/00—Combinations of bioreactors or fermenters with other apparatus
    • C12M43/02—Bioreactors or fermenters combined with devices for liquid fuel extraction; Biorefineries
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M47/00—Means for after-treatment of the produced biomass or of the fermentation or metabolic products, e.g. storage of biomass
    • C12M47/06—Hydrolysis; Cell lysis; Extraction of intracellular or cell wall material
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K25/00—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for
    • F01K25/08—Plants or engines characterised by use of special working fluids, not otherwise provided for; Plants operating in closed cycles and not otherwise provided for using special vapours
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24T—GEOTHERMAL COLLECTORS; GEOTHERMAL SYSTEMS
    • F24T10/00—Geothermal collectors
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24T—GEOTHERMAL COLLECTORS; GEOTHERMAL SYSTEMS
    • F24T10/00—Geothermal collectors
    • F24T10/30—Geothermal collectors using underground reservoirs for accumulating working fluids or intermediate fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F24—HEATING; RANGES; VENTILATING
    • F24T—GEOTHERMAL COLLECTORS; GEOTHERMAL SYSTEMS
    • F24T50/00—Geothermal systems 
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/10—Feedstock materials
    • C10G2300/1011—Biomass
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12M—APPARATUS FOR ENZYMOLOGY OR MICROBIOLOGY; APPARATUS FOR CULTURING MICROORGANISMS FOR PRODUCING BIOMASS, FOR GROWING CELLS OR FOR OBTAINING FERMENTATION OR METABOLIC PRODUCTS, i.e. BIOREACTORS OR FERMENTERS
    • C12M41/00—Means for regulation, monitoring, measurement or control, e.g. flow regulation
    • C12M41/40—Means for regulation, monitoring, measurement or control, e.g. flow regulation of pressure
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E10/00—Energy generation through renewable energy sources
    • Y02E10/10—Geothermal energy
    • 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
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
    • 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
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/59—Biological synthesis; Biological purification
    • 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
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/30—Wastewater or sewage treatment systems using renewable energies
    • Y02W10/37—Wastewater or sewage treatment systems using renewable energies using solar energy
    • 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
    • Y02W30/20—Waste processing or separation

Definitions

  • the ASP concluded that because of microalgae's primitive nature, oil yields were estimated at 30 times more per unit area of land for microalgae than terrestrial oil-seed crops. However, the focus of the ASP report was on making biodiesel from algae lipids, not synthetic crude oil.
  • the 1998 ASP close-out report emphasizes critical open algae pond issues, stemming from the inability to maintain consistently high algae biomass growth rates due to uncontrollable temperature changes in the weather and seasons.
  • Algae biomass production rate is determined by the availability of nutrients, intensity of light, temperature and CO 2 . The effect of light, nutrients and temperature are multiplicative.
  • Thermal spallation is a process that applies significant heat flux to hard rock.
  • the rapid stress causes surface grains to break away from rock in a process known in the art as spallation, which uses super-heated fluid to dissolve the rock.
  • Some embodiments of the invention include an underground hydro-geothermal reactor that converts a renewable oil feedstock to fuel via temperature and pressure.
  • Embodiments of the reactor may utilize produced coke and off gas to generate electricity and heat, produced carbon dioxide and heated mineral-rich water to enhance biomass growth.
  • the present invention includes an underground reactor for use in a fuel creation process for creating fuel from organic material, comprising a first tube that injects an organic material underground; a second tube that collects reacted organic material produced by the underground reactor; a heat exchanger for extracting heat to be used in powering equipment used in the fuel creation process.
  • the present invention further comprises an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the fuel creation process.
  • the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.
  • the equipment includes a pump.
  • the pump circulates heat exchange fluid to keep a reaction zone at a desired temperature.
  • the present invention includes an underground reactor for use in a fuel creation process for creating fuel from organic material, comprising a first tube that injects an organic material underground; a second tube that collects reacted organic material produced by the underground reactor; and a pump which circulates heat exchange fluid in a closed loop to keep a reaction zone at a desired temperature.
  • the present invention further comprises a heat exchanger for extracting heat to be used in powering equipment used in the fuel creation process.
  • the present invention further comprises an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the fuel creation process.
  • the equipment includes the pump.
  • the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.
  • the organic material is biomass.
  • the biomass is algae.
  • the organic material is a polymer.
  • the organic material is solid waste.
  • the organic material is reacted through liquefaction.
  • the organic material is reacted through a thermochemical reaction.
  • the organic material is reacted through hydrothermal processes.
  • the second tube is within the first tube.
  • the first tube is closed at its bottom and the second tube is open at its bottom.
  • the first tube is deeper underground than the second tube.
  • the present invention further comprises a casing that encloses the first tube and the second tube.
  • the casing goes at least as deep as the first tube.
  • the casing does not go as deep as the first tube.
  • the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.
  • Intent Separation of process fluid in tubular reactor from geothermal reservoir fluid by use of a working heat transfer fluid. Intent is to reduce maintenance by restricting geothermal fluid to pipe inner diameter for pigging to minimize downtime
  • pipe cleaning object such as a pig
  • oil industry lingo that dissolves (due to hydrothermal processes that depolymerize) into oil and gas when injected into the tubular reactor and never returns, but cleans pipe I.D. and O.D.
  • DMIN Demineralization Unit
  • Fins on heat transfer pipe transfer heat into working fluid contained within casing and act as baffles to break vortexes generated from mixer system ( 19 ), which forces convective heat transfer to the tubular reactor. Fins may also be on tubular reactor.
  • Geothermal reservoir fluid isolation from pipe O.D. scale can be pigged from I.D. with minimal downtime as this configuration does not require tubular removal (no tripping and downhole service downtime for weeks if not months);
  • FIG. 1 An exemplary geothermal depolymerization tubular reactor.
  • FIG. 2 An exemplary underground reactor system.
  • FIG. 3 Exemplary underground reactor fluid flow.
  • FIG. 4 Exemplary hydro-geothermal reactor process flow diagram.
  • FIG. 5 Exemplary hydro-geothermal reactor process flow diagram.
  • FIG. 6 An exemplary geothermal tubular reactor.
  • FIG. 7 An exemplary geothermal tubular reactor.
  • FIG. 8 An exemplary geothermal tubular reactor.
  • FIG. 9 An exemplary geothermal tubular reactor.
  • FIG. 10 An exemplary geothermal tubular reactor.
  • FIG. 11 An exemplary geothermal tubular reactor where there is no pump-around tube, the inlets and outlets are separated and there is no casing.
  • FIG. 12 Working heat transfer temperature curve inside of casing
  • FIG. 13 Working heat transfer temperature profile inside of casing subjected to forced convection
  • FIG. 14 Tubular reactor profile
  • FIG. 15 Tubular reactor profile subjected to forced convection
  • FIG. 16 Illustration of isolated hot geothermal reservoir fluid from hot working fluid from reactor process fluid
  • FIG. 17 Tubular reactor with geothermal reservoir fluid casing injection
  • FIG. 18 Tubular reactor with external geothermal reservoir fluid injection
  • FIG. 19 Tubular reactor with isolated geothermal reservoir fluid
  • FIG. 20 Tubular reactor with isolated geothermal reservoir fluid & forced convection
  • FIG. 21 Tubular reactor using piezothermal/electric particles and catalyst
  • FIG. 22 Tubular reactor using gas injection isolated from geothermal reservoir fluid
  • FIG. 23 CFD model of casing, tubular reactors and hot geothermal transfer pipes.
  • the algae laden water from an above ground raceway, open pond or settling tank system is injected downhole into the closed loop hydro-geothermal reactor.
  • the tubular reactor is primarily located inside of the casing, but may extend outside of the casing into an open end region.
  • the casing contains hot water that is either static or being circulated through a pump-around system either under natural hydraulic head or subject to geo-pressure from the rock formation, while being counter-balanced with above ground force.
  • An exemplary embodiment is shown in FIG. 1 .
  • the tubular reactor may be curve as the tube gets deeper to allow for the biomass to access greater hot geothermal rock for increased surface area.
  • the geothermal source may be either geo-pressured or not.
  • the depth of an underground reactor may range from 33 ft-40,502 ft (10 m-12,345 m).
  • a tubular reactor outer pipe may have a diameter of 1 inch to 100 ft (25 mm to 30 m)
  • a tubular reactor inner pipe may have a diameter of 1 inch to 100 ft (25 mm to 30 m)
  • a casing may have a diameter of 1 inch to 100 ft (25 mm to 30 m).
  • Certain embodiments may have a curved or sloped tube in order to have a longer period of time in the reactor.
  • a sloped tube may have a series of slopes gradually turning more horizontal as it moves deeper.
  • the tubing used in such installations will be sized appropriately to fit therein.
  • the tubing diameters will likely be about 12 up to 120 inches (30-305 cm).
  • temperatures needed for an effective reaction may be greater than 100° C. and up to 2,000° C.
  • pressures needed for an effective reaction may be 14.7 psig (203 kPa) up to 40,000 psig (275,892 kPa).
  • thermochemical or hydrothermal processes may occur within the reactor during certain ranges of T and P in water:
  • Some embodiments may use any type of organic matter to create products within the reactor under the relevant temperature and pressure conditions.
  • polymers may be used as an organic matter for reaction within a solvent (for example: water) in an underground reactor.
  • Some embodiments may use organic matter to produce chemicals, fuel or hydrocarbons depending on the organic matter used.
  • Effluent geothermal fluid flow may exit into an organic rankine cycle (orc).
  • the organic rankine is comprised of a vaporizer/preheater that uses the heat from the effluent geothermal tubular pump-around fluid to heat and vaporize the working organic fluid.
  • the working organic fluid for example: n-butane
  • the working organic fluid for example: n-butane
  • the working organic fluid for example: n-butane
  • the working organic fluid for example: n-butane
  • the condensed working organic fluid may then be recycled back to the vaporizer for re-heating.
  • the turbine may be connected to an injection pump and generator to produce electricity.
  • Embodiments with a tubular geothermal pump-around may provide tunable temperature control for the hydro-geothermal and depolymerization reactor by adjusting the pump around hot water flow rate and number of coiled tubing inserts.
  • An exemplary embodiment of this feature is illustrated in FIG. 3 .
  • Some embodiments may use any heat transfer fluid to flow through the reactor and tune the temperature.
  • reactor temperature may be adjusted by increasing or decreasing pump-around flow rate, increasing or decreasing tubular reactor flow rate, increasing or decreasing tubular reactor inlet temperature or increasing or decreasing pump-around re-injection temperature.
  • pump-around delivers enough heat via forced convection, then a shallower depth may be sufficient for the reactor in order to reach required temperatures. Without the tubular pump-around, greater drilling depths for a given geothermal resource would be required due to heat transfer limitations in the tubular pump-around, casing and downhole open-end region.
  • a pump-around pipe may have a diameter of 1 inch to 100 ft (25 mm to 30 m).
  • Some embodiments may use a heat exchanger to extract energy from the heated heat transfer fluid.
  • heat exchange devices that can be used include Rankine, Carnot, Stirling, Heat Regenerative Cyclone, thermoelectric (peltier-seebeck effect), Mesoscopic, Barton, Stoddard, Scuderi, Bell Coleman and Brayton.
  • off-gas products may be combusted to heat a heat transfer fluid for use in a heat exchanger.
  • the heat transfer fluid may be used for drying, producing electricity, heating aspects of the reactor, or producing mechanical energy.
  • Yet other embodiments may use an organic rankine cycle to directly drive a pump to feed the heat transfer fluid into the geothermal pump-around system, power a downhole pump in the tubular reactor and produce electricity.
  • the condensing section of the organic rankine cycle may be used to assist in drying algae biomass or other organic materials when combined with a forced draft system powered by electricity or direct drive.
  • the organic working fluid in the condensing section may serve to warm algae ponds.
  • the tubular reactor's effluent products may contain sterilized mineral rich water, carbon and a hydrocarbon/gas mixture.
  • the processes of depolymerization, hydrolysis, decarboxylation, and thermal degradation result in the formation of a hydrocarbon oil/gas/carbon/carbon-dioxide mixture.
  • the solid carbon and hydrocarbon is formed by a combination of depolymerization, hydrolysis, decarboxylation, and thermal degradation underground.
  • Some embodiments may include standard oil/water/gas separation equipment to separate the hydrocarbon and gas.
  • the oil-free hot tubular reactor's mineral rich effluent water may be returned back to the open algae farm raceway system or other biomass system.
  • total hot water return volume may be set at 1 ⁇ 3 of raceway water volume, so that 1 ⁇ 3 of the raceway water may be turned over and processed each day.
  • the separated gas mixture and carbon dioxide may be combusted to generate electricity, heat and carbon dioxide.
  • the carbon dioxide may be injected downhole into the tubular reactor's effluent to assist in pumping as well as into the effluent stream prior or after being recycled back into algae pond or break tank.
  • the reactor's maximum size is a function of the hydro-geothermal depolymerization reactor's effluent flow rate, temperature, mineral content, amino acid content and carbonation, which is dependent upon the geothermal resource, tubular reactor depth, pump-around rate and direction.
  • Environmental variables that impact the reactor may include ambient temperature, wind velocity, cloud cover, evaporation rate, precipitation, relative humidity, and atmospheric pressure.
  • Key process variables include reactor effluent flow rate and temperature in addition to the algae pond dimensions such as depth, width, length, and circulation.
  • Carbon dioxide may be produced during the decarboxylation step in the presence of water, heat, pressure, algae, biomass, waste, and polymers underground in the tubular. In some embodiments, the carbon dioxide may be recycled within the process.
  • the algae in water, biomass, waste water, waste and polymer are subject to pressures and temperatures above ambient (300+° F. (149+° C.) and 300+ psig (2,170+ kPA)) underground the material undergoes hydrolysis, decarboxylation and degradation to form the oil and gas along with solid carbon, carbon dioxide and hot mineral rich water.
  • the oil/gas/water mixture is then separated with the water recycled to the algae pond and the oil and gas sent to downstream processing units for electricity, heat, chemical, transport fuel, and coke production. Exemplary flow charts indicating this process is illustrated in FIGS. 4 and 5 . Coke production may occur via pyrolysis.
  • Benefits for existing industrial facilities & algae cultivation include renewable oil production, industrial waste water consumption and multiplicative growth enhancement for large scale algae farm with CO 2 and mineral rich hot water.
  • E Electricity to power pumps and auxiliary equipment H1 Products of coke combustion include heat and possibly low pressure steam if CCGT used T1 Combustion product of turbine generates heat and possibly low pressure steam if CCGT used T2 Combustion product of turbine generates CO 2 and H 2 O H2 Combustion product of coke generates CO 2 and H 2 O
  • FIG. 12 plots the bulk temperature profile of the closed-loop working heat transfer fluid inside of the casing. Heat transfer occurs through conduction, natural convection and radiant heat transfer.
  • the working heat transfer fluid in the casing (see FIG. 19-3 ) is plotted in FIG. 13 .
  • FIG. 13 plots the bulk temperature profile of the closed-loop working heat transfer fluid inside of the casing. Heat transfer occurs through conduction, natural convection and radiant heat transfer.
  • the working heat transfer fluid in the casing (see FIG. 20-3 ) is plotted in FIG. 13 .
  • FIG. 14 plots the tubular reactor temperature profile of the closed-loop process fluid inside of the reactor's annular flow space and center pipe return without forced convection.
  • the tubular reactor (see FIG. 19-19 ) is immersed in the working heat transfer fluid (see FIG. 19-3 ).
  • Process reactants enter the reactor (see FIG. 19-15 ), also shown in the bottom left hand section of the plot.
  • the process fluid flows underground through the annular space (see FIG. 19-4 ) then returns through the center pipe (see FIG. 19-5 ).
  • the reactor temperature profile may be adjusted by adjusting the temperature and flow rate of injection stream ( FIG. 19-14 ), demineralization flow rate ( FIG. 19-13 ), organic rankine cycle flow rate ( FIG.
  • FIG. 15 plots the tubular reactor temperature profile of the closed-loop process fluid inside of the reactor's annular flow space and center pipe return with forced convection.
  • the tubular reactor (see FIG. 19-19 ) is immersed in the working heat transfer fluid (see FIG. 19-3 ).
  • Process reactants enter the reactor (see FIG. 19-15 ), also shown in the bottom left hand section of the plot.
  • the process fluid flows underground through the annular space (see FIG. 19-4 ) then returns through the center pipe (see FIG. 19-5 ).
  • the reactor temperature profile may be adjusted by adjusting the temperature and flow rate of injection stream ( FIG. 19-14 ), demineralization flow rate ( FIG. 19-13 ), organic rankine cycle flow rate ( FIG.
  • FIG. 16 lists the heat transfer mechanism and fluids used to confine geothermal reservoir fluid scaling, corrosion and depots to the inner diameter of the hot geothermal transfer pipe (see FIG. 19-7 ).
  • the purpose of isolating the hot geothermal reservoir fluids (injected or pre-existing) from the tubular reactor is to reduce maintenance downtime by providing pigging of the pipe inner diameter.
  • Pigging is a process by which a plastic/rubber object with abrasive edges/cutters is driven by pressure through a pipe to typically clean the pipe's inner diameter from scale and other oxides/deposits that restrict heat transfer and fluid flow. If pigging was not able to be performed the entire tubular reactor would have to be removed to remove scale.
  • FIG. 17 lists a casing contained injection and reactor configuration.
  • the continuously stirred rods devices ( FIG. 17-4 ) maintains high velocity flow rate along the outer diameter of the tubular reactor to minimize scaling and fouling by continuously sweeping the surface and aids in convective heat transfer.
  • Geothermal reservoir fluid is injected in ( FIG. 17-3 ) and flows downhole and into the reservoir ( FIG. 17-9 ) and through the fracked rock ( FIG. 17-10 ) and flows back out through the return pipe ( FIG. 17-8 ) into the organic rankine unit ( FIG. 17-2 ), which direct drives pumps and auxiliary equipment.
  • the geothermal reservoir fluid directly contacts the outer diameter of the tubular reactor and may be drawn off through ( FIGS. 17-5 and 17 - 2 ) streams for mineralization recovery through a demineralization unit (DMIN).
  • the bottom hole temperature may exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).
  • FIG. 18 lists a casing contained reactor configuration with external injection line.
  • the continuously stirred rods devices ( FIG. 18-5 ) maintains high velocity flow rate along the outer diameter of the tubular reactor to minimize scaling and fouling by continuously sweeping the surface and aids in convective heat transfer.
  • Geothermal reservoir fluid is injected in ( FIG. 18-14 ) and flows downhole and into the reservoir ( FIG. 18-10 ) and through the fracked rock ( FIG. 18-9 ) and flows back out through the return pipe ( FIG. 18-11 ) into the organic rankine unit ( FIG. 18-16 ), which direct drives pumps and auxiliary equipment.
  • the geothermal reservoir fluid directly contacts the outer diameter of the tubular reactor and may be drawn off through ( FIGS. 18-15 and 18 - 16 ) streams for mineralization recovery through a demineralization unit (DMIN).
  • the bottom hole temperature may exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).
  • FIG. 19 lists a casing contained reactor configuration with external injection line ( FIG. 19-14 ), casing contained/internal geothermal reservoir fluid isolation and heat transfer line ( FIG. 19-13 ), casing contained/internal tubular reactor ( FIG. 19-19 ), and external geothermal reservoir fluid return line ( FIG. 19-16 ).
  • Geothermal reservoir fluid is injected in ( FIG. 19-14 ) and flows downhole and into the reservoir ( FIG. 19-10 ) and through the fracked rock ( FIG. 19-9 ) and flows back out through the return pipe ( FIG. 19-11 ) into the organic rankine unit ( FIG. 19-16 ), which direct drives pumps and auxiliary equipment.
  • the geothermal reservoir fluid does not directly contact the outer diameter of the tubular reactor, but is isolated to the inner diameter of several hot heat transfer pipes that return to the surface to be drawn off through ( FIGS. 19-13 and 19 - 16 streams for mineralization recovery through a demineralization unit (DMIN).
  • DMIN demineralization unit
  • the key difference between FIG. 19 and prior FIGS. 17 and 18 is the use of a hot heat transfer pipe ( FIG. 19-7 ) to isolate the hot geothermal reservoir fluids from the reactor to prevent scaling/fouling on the reactor's wall.
  • the primary enabling benefit of ( FIG. 19-7 ) is to provide easy maintenance/pigging through the inner diameter to remove scale and increase heat transfer.
  • the working heat transfer fluid ( FIG. 19-3 ) transfer heat into the tubular reactor by wetting both tubular reactor and hot heat transfer geothermal pipe.
  • the bottom hole temperature may exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).
  • FIG. 20 lists a casing contained reactor configuration with external injection line ( FIG. 20-14 ), casing contained/internal geothermal reservoir fluid isolation and heat transfer line ( FIG. 20-13 ), casing contained/internal tubular reactor ( FIG. 20-19 ), and external geothermal reservoir fluid return line ( FIG. 20-16 ).
  • Geothermal reservoir fluid is injected in ( FIG. 20-14 ) and flows downhole and into the reservoir ( FIG. 20-10 ) and through the fracked rock ( FIG. 20-9 ) and flows back out through the return pipe ( FIG. 20-11 ) into the organic rankine unit ( FIG. 20-16 ), which direct drives pumps and auxiliary equipment.
  • the geothermal reservoir fluid does not directly contact the outer diameter of the tubular reactor, but is isolated to the inner diameter of several hot heat transfer pipes that return to the surface to be drawn off through ( FIGS. 20-13 and 20 - 16 streams for mineralization recovery through a demineralization unit (DMIN).
  • DMIN demineralization unit
  • the key difference between FIG. 20 and prior FIGS. 17 and 18 is the use of a hot heat transfer pipe ( FIG. 20-7 ) to isolate the hot geothermal reservoir fluids from the reactor to prevent scaling/fouling on the reactor's wall.
  • the primary enabling benefit of ( FIG. 20-7 ) is to provide easy maintenance/pigging through the inner diameter to remove scale and increase heat transfer.
  • the working heat transfer fluid FIG.
  • FIG. 20-3 transfer heat into the tubular reactor by wetting both tubular reactor and hot heat transfer geothermal pipe.
  • the secondary key difference between FIG. 20 and FIG. 19 is the use of a continuously stirred rod set to force convection down hole to increase heat transfer rate.
  • the bottom hole temperature may exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).
  • FIG. 21 lists a casing contained reactor configuration with external injection line ( FIG. 21-14 ), casing contained/internal geothermal reservoir fluid isolation and heat transfer line ( FIG. 21-13 ), casing contained/internal tubular reactor ( FIG. 21-19 ), and external geothermal reservoir fluid return line ( FIG. 21-16 ).
  • Geothermal reservoir fluid is injected in ( FIG. 21-14 ) and flows downhole and into the reservoir ( FIG. 21-10 ) and through the fracked rock ( FIG. 21-9 ) and flows back out through the return pipe ( FIG. 21-11 ) into the organic rankine unit ( FIG. 21-16 ), which direct drives pumps and auxiliary equipment.
  • the geothermal reservoir fluid does not directly contact the outer diameter of the tubular reactor, but is isolated to the inner diameter of several hot heat transfer pipes that return to the surface to be drawn off through ( FIGS. 21-13 and 21 - 16 streams for mineralization recovery through a demineralization unit (DMIN).
  • DMIN demineralization unit
  • the key difference between FIG. 21 and prior FIG. 20 are the use of piezo particles to transform stress, generated by gravity acting on the downhole column of circulating heat transfer fluid, into electrical current and heat. Additionally, catalyst may be circulated within the tubular reactor along with piezo particles.
  • the bottom hole temperature may exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).
  • FIG. 22 lists a casing contained reactor configuration with external injection line ( FIG. 22-14 ), casing contained/internal geothermal reservoir fluid isolation and heat transfer line ( FIG. 22-13 ), casing contained/internal tubular reactor ( FIG. 22-19 ), and external geothermal reservoir fluid return line ( FIG. 22-16 ).
  • Geothermal reservoir fluid is injected in ( FIG. 22-14 ) and flows downhole and into the reservoir ( FIG. 22-10 ) and through the fracked rock ( FIG. 22-9 ) and flows back out through the return pipe ( FIG. 22-11 ) into the organic rankine unit ( FIG. 22-16 ), which direct drives pumps and auxiliary equipment.
  • the geothermal reservoir fluid does not directly contact the outer diameter of the tubular reactor, but is isolated to the inner diameter of several hot heat transfer pipes that return to the surface to be drawn off through ( FIGS. 22-13 and 22 - 16 streams for mineralization recovery through a demineralization unit (DMIN).
  • DMIN demineralization unit
  • the key difference between FIG. 22 and prior FIG. 21 is the use of gas that is adiabatically compressed to release latent heat within the tubular reactor and working heat transfer fluid isolated from the geothermal reservoir.
  • the bottom hole temperature may exceed 200° C. and pressures in excess of 500 psig (3,549 kPa).
  • FIG. 23 highlights the use of one or more tubular reactors and hot geothermal pipes within the cemented casing. It is important to note that the fully cemented casing acts as a great insulator by reducing heat loss.
  • the hot heat transfer pipe(s) shown in FIG. 22-7 may be pigged with a dissolving pig that never returns. Plastic/rubber will depolymerize within the hot tubular and dissolve the pig over time. Thus, the pig never returns once it is injected into ReactWell's hot geothermal pipe, because it dissolves due to the high temperature and pressure.
  • One embodiment to test the system may comprise a bench top scale version of reactor comprised of a larger diameter pipe containing one pump-around, oil/gas/water separator, one tubular reactor and auxiliary temperature and pressure instrumentation.
  • the reactor will be vertically installed and bottom (bottom-hole) rests inside of a heater. The heater is used to simulate geothermal temperature source. Effluent pump-around will be cooled through condenser and recycled back to injection pump for recycle in pump-around circuit.
  • the tubular reactor source tank will contain a select type of organic material in water with an option for catalyst addition.
  • the tubular reactor will inject the biomass laden water into the reactor's annular space, react downhole and flow out into a sample chamber with in-line analyzer.
  • the pump-around discharge will be controlled with a back-pressure control valve.
  • the tubular reactor discharge will be controlled with a back-pressure control valve.
  • One embodiment to test the system will initially inventory the tubular reactor and pump-around with a fixed quantity of deionized water (DI), start circulation on the pump-around. Then turn on the heater and start condenser cooling fluid flow and adjust accordingly. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor injection of aqueous organic material will begin. Once the aqueous organic material injection has completed, a known quantity of DI will flush the tubular reactor. After the flush, then the tubular reactor's effluent DI will begin to be recycled into the inlet. Then the heater will be turned-off. Once the heat transfer fluid temperature in the pump-around system reaches ambient temperature, then the tubular reactor injection pump will be turned-off. Then the pump-around injection pump and condenser cooling fluid will be turned-off. The bench top equipment should be depressurized to ambient conditions prior to opening any chambers, vessels, reactors, piping or tubing.
  • DI deionized water
  • One embodiment to test the system will initially inventory the tubular reactor and pump-around with a fixed quantity of deionized water (DI), start circulation on the pump-around. Then turn on the heater and start condenser cooling fluid flow and adjust accordingly. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor injection of aqueous organic material will begin. The tubular reactor's effluent products will be routed to an oil/gas/water separator. The water will be recycled and mixed with new organic feedstock and water. The oil and gas will be analyzed. Upon determining the steady-state test completion a known quantity of DI will flush the tubular reactor. After flush then start recycling the tubular reactor's effluent DI into the inlet.
  • DI deionized water
  • the heater will be turned-off. Once heat transfer fluid temperature in the pump-around system reaches ambient temperature then the tubular reactor injection pump will be turned-off. Then the pump-around injection pump and condenser cooling fluid will be turned-off.
  • the bench top equipment should be depressurized to ambient conditions prior to opening any chambers, vessels, reactors, piping or tubing.
  • One embodiment to test the system comprises a heater capable of discharge temperatures in excess of 400° C., condensing unit, a reactor as described in this application, oil/gas/water separator, injection pump for pump-around circuit and downhole pump for tubular reactor effluent discharge along with associated auxiliary temperature, pressure and flow instrumentation and gauges.
  • the reactor is comprised of a larger diameter pipe containing one pump-around and one tubular reactor. The reactor will be vertically installed and bottom (bottom-hole) rests inside of a heater.
  • the heater is used to simulate geothermal temperature source. Effluent pump-around will be cooled through condenser and recycled back to injection pump for recycle in pump-around circuit.
  • the tubular reactor source tank will contain a select type of organic material in water with an option for catalyst addition.
  • the tubular reactor will inject the biomass laden water into the reactor's annular space, react downhole and flow out into an oil/water/gas separator.
  • the separated water will be recycled to a water storage tank.
  • the oil will be routed to an oil storage tank.
  • the gas will be stored, combusted or vented to atmosphere.
  • the pump-around discharge will be controlled with a back-pressure control valve.
  • the tubular reactor discharge will be controlled with a back-pressure control valve.
  • One embodiment to test the system will initially inventory the tubular reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around. Then turn on the heater and start condenser cooling fluid flow and adjust accordingly. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor injection of aqueous organic material will begin. The tubular reactor's effluent products will be routed to an oil/gas/water separator. The water will be recycled and mixed with new organic feedstock and water. The separated oil will be routed to a storage vessel and gas will be stored, analyzed and vented. Depending upon environmental regulations the gas may require combustion or incineration prior to analysis.
  • the tubular reactor Upon completing the steady-state test the tubular reactor will be flushed with treated water. Then turn-off heater. Once heat transfer fluid temperature in the pump-around system reaches ambient temperature then turn-off the tubular reactor injection pump. Then turn-off the pump-around injection pump and condenser cooling fluid.
  • the unit should be depressurized to ambient conditions prior to opening any chambers, vessels, reactors, piping or coiled tubing.
  • One embodiment of the invention comprises completing siting study, drilling appropriate exploration holes underground, drilling a tubular reactor underground, installing casing, cementing, fracking bottom-hole rock, hydrothermal spalling of downhole rock to increase surface area, permeability and porosity, tubular pump-around(s), packers to stabilize downhole tubulars, tubular reactor(s) and associated downhole instrumentation, pumps and gauges.
  • an organic rankine cycle (ORC) unit will be installed above ground and piped-up to the ReactWell pump-around tubular(s) and lined-up to pump-around injection pump(s) and associated power equipment.
  • the tubular reactor(s) inlet(s) will be fitted to organic feedstock in adjacent algae farm and other opportunity organic waste streams.
  • the tubular reactor(s) effluents will be piped-up to oil/gas/water separation equipment and vessels.
  • One embodiment of the invention will initially inventory the tubular reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, and kick-start and pressurize the pump-around system. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and lined up to generate electricity. Adequate condenser cooling fluid flow may be maintained and adjusted accordingly. The cooling fluids may be sourced from algae pond(s) to provide geothermal heating. Once the pump-around temperatures and pressure stabilizes as determined by temperature and pressure instrumentation/indicators, then the tubular reactor(s) injection of aqueous organic material will begin.
  • ORC organic rankine cycle
  • the tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator.
  • the hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth.
  • the separated oil will be routed to a storage vessel.
  • the gas primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond.
  • the tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature.
  • the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off and depressurized. Once temperatures stabilize then the tubular reactor pump-around will be shut-off and depressurized.
  • ORC organic rankine cycle
  • the unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.
  • One embodiment of the invention will initially inject geothermal fluid downhole into an injection line, inside of the casing, into fracked hot dry rock (HDR).
  • HDR fracked hot dry rock
  • the hot geothermal fluid will then flow through fracked rock back into the casing's annular space between the injection line, reactor and casing I.D. then to the surface for mineral scavenging and subsequent re-injection through the original injection line.
  • ORC organic rankine unit
  • the reactor's tubular pump-around system will be inventoried with a fixed quantity of treated water, circulation started using a separate startup pump.
  • the tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator, downstream bio-oil stabilization unit using ionic separation driven by an applied voltage differential by either ORC electricity or piezoelectric/thermal underground (rods) will further separate light from heavy and also provide opportunity to run downstream catalysis.
  • the hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth.
  • the separated oil will be routed to a storage vessel.
  • the gas primarily comprised of carbon dioxide and methane, will be combusted with produced CO 2 used to carbonate the effluent water being recycled to the algae pond.
  • One embodiment of the invention will initially inject geothermal fluid downhole into an injection line, inside of the casing, into fracked hot dry rock (HDR).
  • HDR fracked hot dry rock
  • the hot geothermal fluid will then flow through fracked rock back into the casing's annular space between the injection line, reactor and casing I.D. then to the surface for mineral scavenging and subsequent re-injection through the original injection line.
  • ORC organic rankine unit
  • the reactor's tubular pump-around system will be inventoried with a fixed quantity of treated water, circulation started using a separate startup pump.
  • the tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator, downstream bio-oil stabilization unit using ionic separation driven by an applied voltage differential by either ORC electricity or piezoelectric/thermal underground (rods) will further separate light from heavy and also provide opportunity to run downstream catalysis.
  • the hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth.
  • the separated oil will be routed to a storage vessel.
  • the gas primarily comprised of carbon dioxide and methane, will be combusted with produced CO 2 used to carbonate the effluent water being recycled to the algae pond.
  • One embodiment of the invention will initially inventory the casing with a heat transfer fluid not exposed to the hot dry rock or process. Then inject water downhole into an injection line, outside of the casing, into fracked hot dry rock (HDR). The water will then flow through fracked rock into the casing, through the inner diameter of heat pipes and to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a third drill hole that will power an organic rankine unit (ORC). Then reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, and kick-start and pressurize the pump-around system.
  • ORC organic rankine unit
  • temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and lined up to generate electricity.
  • Adequate condenser cooling fluid flow may be maintained and adjusted accordingly.
  • the cooling fluids may be sourced from algae pond(s) to provide geothermal heating.
  • the tubular reactor(s) injection of aqueous organic material will begin.
  • the tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator.
  • the hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth.
  • the separated oil will be routed to a storage vessel.
  • the gas primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond.
  • the organic rankine cycle ORC
  • the tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature.
  • the organic rankine cycle ORC
  • the tubular reactor pump-around will be shut-off and depressurized.
  • the unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.
  • One embodiment of the invention will initially inventory the casing with a heat transfer fluid not exposed to the hot dry rock or process. Then inject water downhole into an injection line, outside of the casing, into fracked hot dry rock (HDR). The water will then flow through fracked rock into the casing and to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a third drill hole that will power an organic rankine unit (ORC). Then reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, start stir rod agitation and kick-start and pressurize the pump-around system.
  • ORC organic rankine unit
  • temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and lined up to generate electricity.
  • Adequate condenser cooling fluid flow may be maintained and adjusted accordingly.
  • the cooling fluids may be sourced from algae pond(s) to provide geothermal heating.
  • the tubular reactor(s) injection of aqueous organic material will begin.
  • the tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator.
  • the hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth.
  • the separated oil will be routed to a storage vessel.
  • the gas primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond.
  • the organic rankine cycle ORC
  • the tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature.
  • the organic rankine cycle ORC
  • the tubular reactor pump-around will be shut-off, stir rod turned off and depressurized.
  • the unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.
  • One embodiment of the invention will initially inventory the casing with a heat transfer fluid not exposed to the hot dry rock or process and containing piezothermal/piezoelectric particles to generate current and heat when stressed by hydraulic force. Then inject water downhole through fracked rock into the casing and to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a third drill hole that will power an organic rankine unit (ORC). Then reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, start stir rod agitation and kick-start and pressurize the pump-around system.
  • ORC organic rankine unit
  • temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and lined up to generate electricity.
  • Adequate condenser cooling fluid flow may be maintained and adjusted accordingly.
  • the cooling fluids may be sourced from algae pond(s) to provide geothermal heating.
  • the tubular reactor(s) injection of aqueous organic material will begin.
  • the tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator.
  • the hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth.
  • the separated oil will be routed to a storage vessel.
  • the gas primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond.
  • the organic rankine cycle ORC
  • the tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature.
  • the organic rankine cycle ORC
  • the tubular reactor pump-around will be shut-off, stir rod turned off and depressurized.
  • the unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.
  • One embodiment of the invention will initially inventory the casing with a heat transfer fluid not exposed to the hot dry rock or process and containing piezothermal/piezoelectric particles to generate current and heat when stressed by hydraulic force. Then inject water downhole through fracked rock into the casing and to the surface for mineral scavenging and subsequent re-injection through the original injection line. Further, there will be a third drill hole that will power an organic rankine unit (ORC). Then reactor and pump-around with a fixed quantity of treated water, start circulation on the pump-around using a separate startup pump, start stir rod agitation and kick-start and pressurize the pump-around system.
  • ORC organic rankine unit
  • temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and lined up to generate electricity.
  • Adequate condenser cooling fluid flow may be maintained and adjusted accordingly.
  • the cooling fluids may be sourced from algae pond(s) to provide geothermal heating.
  • the tubular reactor(s) injection of aqueous organic material will begin.
  • the tubular reactor(s)'s effluent products will be routed to an oil/gas/water separator.
  • the hot effluent mineral rich water will be recycled and mixed with existing algae water in ponds or vessels to multiplicatively enhance algae growth.
  • the separated oil will be routed to a storage vessel.
  • the gas primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond.
  • the organic rankine cycle ORC
  • the tubular reactor effluent will be lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature.
  • the organic rankine cycle ORC
  • the tubular reactor pump-around will be shut-off, stir rod turned off and depressurized.
  • the unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Organic Chemistry (AREA)
  • Wood Science & Technology (AREA)
  • Zoology (AREA)
  • Bioinformatics & Cheminformatics (AREA)
  • General Engineering & Computer Science (AREA)
  • Sustainable Development (AREA)
  • Genetics & Genomics (AREA)
  • Biotechnology (AREA)
  • Biochemistry (AREA)
  • Biomedical Technology (AREA)
  • Microbiology (AREA)
  • General Health & Medical Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • Sustainable Energy (AREA)
  • Molecular Biology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Thermal Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Physics & Mathematics (AREA)
  • Cell Biology (AREA)
  • Clinical Laboratory Science (AREA)
  • Analytical Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Processing Of Solid Wastes (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
US14/115,278 2011-05-03 2012-05-03 Underground reactor system Abandoned US20140206912A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US14/115,278 US20140206912A1 (en) 2011-05-03 2012-05-03 Underground reactor system

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US201161481918P 2011-05-03 2011-05-03
US201261602841P 2012-02-24 2012-02-24
PCT/US2012/036400 WO2012151447A2 (en) 2011-05-03 2012-05-03 Underground reactor system
US14/115,278 US20140206912A1 (en) 2011-05-03 2012-05-03 Underground reactor system

Publications (1)

Publication Number Publication Date
US20140206912A1 true US20140206912A1 (en) 2014-07-24

Family

ID=47108238

Family Applications (1)

Application Number Title Priority Date Filing Date
US14/115,278 Abandoned US20140206912A1 (en) 2011-05-03 2012-05-03 Underground reactor system

Country Status (10)

Country Link
US (1) US20140206912A1 (es)
EP (1) EP2705131A4 (es)
CN (2) CN103608449B (es)
AU (1) AU2012250684B2 (es)
BR (1) BR112013028426A2 (es)
CA (1) CA2834858A1 (es)
MX (1) MX2013012789A (es)
PH (1) PH12013502247A1 (es)
RU (1) RU2627594C2 (es)
WO (1) WO2012151447A2 (es)

Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104923550A (zh) * 2015-06-29 2015-09-23 北京水木清辉环保科技有限责任公司 一种餐厨垃圾处理装置
JP5839531B1 (ja) * 2015-05-12 2016-01-06 株式会社エスト 地熱交換器および地熱発電装置
JP2016151198A (ja) * 2015-02-16 2016-08-22 俊一 田原 沸騰水型地熱交換器および沸騰水型地熱発電装置
JP6067173B1 (ja) * 2016-09-30 2017-01-25 俊一 田原 地熱交換器および地熱発電装置
CN106874542A (zh) * 2017-01-04 2017-06-20 滨州东瑞机械有限公司 一种液力透平叶轮多工况多目标优化设计方法
US9714643B2 (en) 2014-06-05 2017-07-25 Est. Inc. Boiling-water geothermal heat exchanger and boiling-water geothermal power generation equipment
US9982205B2 (en) 2015-08-03 2018-05-29 Craig Pichach Subterranean gasification system and method
WO2019157341A1 (en) * 2018-02-08 2019-08-15 Greenfire Energy Inc. Closed loop energy production from producing geothermal wells
CN112366013A (zh) * 2020-11-10 2021-02-12 中国核动力研究设计院 一种适用于热管反应堆的带核试验方法
US11480074B1 (en) 2021-04-02 2022-10-25 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11486330B2 (en) 2021-04-02 2022-11-01 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11486370B2 (en) 2021-04-02 2022-11-01 Ice Thermal Harvesting, Llc Modular mobile heat generation unit for generation of geothermal power in organic Rankine cycle operations
US11493029B2 (en) 2021-04-02 2022-11-08 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11578706B2 (en) 2021-04-02 2023-02-14 Ice Thermal Harvesting, Llc Systems for generating geothermal power in an organic Rankine cycle operation during hydrocarbon production based on wellhead fluid temperature
US11592009B2 (en) 2021-04-02 2023-02-28 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11644015B2 (en) 2021-04-02 2023-05-09 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11644014B2 (en) 2021-04-02 2023-05-09 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power in an organic Rankine cycle operation
US20230212493A1 (en) * 2022-01-06 2023-07-06 Premium Oceanic Inc. Systems and methods for conversion of a biomass into biofuel using a geothermal heat source
US11959466B2 (en) 2021-04-02 2024-04-16 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power in an organic Rankine cycle operation
US12180861B1 (en) 2022-12-30 2024-12-31 Ice Thermal Harvesting, Llc Systems and methods to utilize heat carriers in conversion of thermal energy
US12312981B2 (en) 2021-04-02 2025-05-27 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US12404484B2 (en) 2022-01-06 2025-09-02 Blue Evolution Inc. Systems and methods for conversion of a biomass into biofuel using a geothermal heat source
WO2025259701A1 (en) * 2024-06-11 2025-12-18 Lacey Kevin S Systems and methods for treating organic waste with geothermal energy
US12534990B2 (en) 2022-12-29 2026-01-27 Ice Thermal Harvesting, Llc Power generation assemblies for hydraulic fracturing systems and methods

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN107367081B (zh) * 2017-07-17 2023-09-01 浙江陆特能源科技股份有限公司 中深层多功能地源井及其使用方法
CN108930529B (zh) * 2018-09-12 2021-06-04 中国地质大学（北京） 基于废弃油气井的油-热-电联产方法
CN109851030B (zh) * 2019-02-03 2020-10-09 中国原子能科学研究院 超临界水氧化反应器及处理放射性有机废物的方法
US12006495B2 (en) * 2019-08-13 2024-06-11 ExxonMobil Technology and Engineering Company Solar steam explosion of algae

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4272383A (en) * 1978-03-17 1981-06-09 Mcgrew Jay Lininger Method and apparatus for effecting subsurface, controlled, accelerated chemical reactions
US20030062163A1 (en) * 2001-09-17 2003-04-03 Southwest Research Institute Pretreatment processes for heavy oil and carbonaceous materials
US6989135B2 (en) * 1999-07-01 2006-01-24 Syntroleum Corporation Hydrocarbon conversion system with enhanced combustor and method

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3606999A (en) * 1967-08-04 1971-09-21 Harold L Lawless Method of and apparatus for carrying out a chemical or physical process
CA1115496A (en) * 1978-03-17 1982-01-05 Jay L. Mcgrew Method and apparatus for effecting subsurface, controlled, accelerated chemical reactions
US4845034A (en) * 1985-01-22 1989-07-04 Houston Industries Incorporated Biochemically reacting substrates in subterranean cavities
JPS6443344A (en) * 1987-08-12 1989-02-15 Univ Tohoku Vessel for underground chemical reaction
ES2019734A6 (es) * 1989-11-13 1991-07-01 Ayala Martinez Guillermo Sistema de extraccion de energia geometrica.
US5484231A (en) * 1993-11-29 1996-01-16 Mobil Oil Corporation Disposal of slurries of municipal waste in deep geothermal reservoirs
US5958761A (en) * 1994-01-12 1999-09-28 Yeda Research And Developement Co. Ltd. Bioreactor and system for improved productivity of photosynthetic algae
CN101505961A (zh) * 2006-03-25 2009-08-12 奥尔特维亚能量公司 用于提高能量效率的生物质燃料合成方法
US7905683B2 (en) * 2007-04-27 2011-03-15 Enertech Environmental, Inc. Disposal of slurry in underground geologic formations
CA2732134A1 (en) * 2008-07-28 2010-02-04 Forbes Oil And Gas Pty Ltd Apparatus for liquefaction of carbonaceous material
CN101892964B (zh) * 2010-07-30 2012-09-05 龚智勇 万米单深井重力真空辅助热管循环干热岩发电方法及装置

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4272383A (en) * 1978-03-17 1981-06-09 Mcgrew Jay Lininger Method and apparatus for effecting subsurface, controlled, accelerated chemical reactions
US6989135B2 (en) * 1999-07-01 2006-01-24 Syntroleum Corporation Hydrocarbon conversion system with enhanced combustor and method
US20030062163A1 (en) * 2001-09-17 2003-04-03 Southwest Research Institute Pretreatment processes for heavy oil and carbonaceous materials

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
Demirbas, Biomass resource facilities and biomass conversion processing for fuels and chemicals, 2001, Energy conversion and management, vol. 42, pp. 1357-1378. *
Fournadzhieva et al., Use of geothermal fluids for cultivation of the microalga Spirulina in Nigrita – Serres. In: Proceedings of 7th National Conference on Renewable Energy Sources (Patras 6-8/11/2002), Institute of Solar Technology, vol B, pp 97-104, 2002. *

Cited By (58)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US9714643B2 (en) 2014-06-05 2017-07-25 Est. Inc. Boiling-water geothermal heat exchanger and boiling-water geothermal power generation equipment
JP2016151198A (ja) * 2015-02-16 2016-08-22 俊一 田原 沸騰水型地熱交換器および沸騰水型地熱発電装置
WO2016132624A1 (ja) * 2015-02-16 2016-08-25 株式会社エスト 沸騰水型地熱交換器および沸騰水型地熱発電装置
US10060652B2 (en) 2015-02-16 2018-08-28 Kyoei Denki Kogyo Corporation Boiling-water geothermal heat exchanger and boiling-water geothermal power generation equipment
JP5839531B1 (ja) * 2015-05-12 2016-01-06 株式会社エスト 地熱交換器および地熱発電装置
CN104923550A (zh) * 2015-06-29 2015-09-23 北京水木清辉环保科技有限责任公司 一种餐厨垃圾处理装置
US9982205B2 (en) 2015-08-03 2018-05-29 Craig Pichach Subterranean gasification system and method
JP6067173B1 (ja) * 2016-09-30 2017-01-25 俊一 田原 地熱交換器および地熱発電装置
CN106874542A (zh) * 2017-01-04 2017-06-20 滨州东瑞机械有限公司 一种液力透平叶轮多工况多目标优化设计方法
WO2019157341A1 (en) * 2018-02-08 2019-08-15 Greenfire Energy Inc. Closed loop energy production from producing geothermal wells
JP2021513620A (ja) * 2018-02-08 2021-05-27 グリーンファイア・エナジー・インコーポレイテッドＧｒｅｅｎｆｉｒｅ Ｅｎｅｒｇｙ Ｉｎｃ 生産性地熱井からの閉ループエネルギー生成
US11255576B2 (en) 2018-02-08 2022-02-22 Greenfire Energy Inc. Closed loop energy production from producing geothermal wells
JP7135094B2 (ja) 2018-02-08 2022-09-12 グリーンファイア・エナジー・インコーポレイテッド 生産性地熱井からの閉ループエネルギー生成
CN112366013A (zh) * 2020-11-10 2021-02-12 中国核动力研究设计院 一种适用于热管反应堆的带核试验方法
US11680541B2 (en) 2021-04-02 2023-06-20 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11905934B2 (en) 2021-04-02 2024-02-20 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11486370B2 (en) 2021-04-02 2022-11-01 Ice Thermal Harvesting, Llc Modular mobile heat generation unit for generation of geothermal power in organic Rankine cycle operations
US11493029B2 (en) 2021-04-02 2022-11-08 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11542888B2 (en) 2021-04-02 2023-01-03 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11549402B2 (en) 2021-04-02 2023-01-10 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11572849B1 (en) 2021-04-02 2023-02-07 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11578706B2 (en) 2021-04-02 2023-02-14 Ice Thermal Harvesting, Llc Systems for generating geothermal power in an organic Rankine cycle operation during hydrocarbon production based on wellhead fluid temperature
US11592009B2 (en) 2021-04-02 2023-02-28 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11598320B2 (en) 2021-04-02 2023-03-07 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11624355B2 (en) 2021-04-02 2023-04-11 Ice Thermal Harvesting, Llc Modular mobile heat generation unit for generation of geothermal power in organic Rankine cycle operations
US11644015B2 (en) 2021-04-02 2023-05-09 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11644014B2 (en) 2021-04-02 2023-05-09 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power in an organic Rankine cycle operation
US11668209B2 (en) 2021-04-02 2023-06-06 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11480074B1 (en) 2021-04-02 2022-10-25 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US12454896B2 (en) 2021-04-02 2025-10-28 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11732697B2 (en) 2021-04-02 2023-08-22 Ice Thermal Harvesting, Llc Systems for generating geothermal power in an organic Rankine cycle operation during hydrocarbon production based on wellhead fluid temperature
US11761433B2 (en) 2021-04-02 2023-09-19 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power in an organic Rankine cycle operation
US11761353B2 (en) 2021-04-02 2023-09-19 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11773805B2 (en) 2021-04-02 2023-10-03 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11879409B2 (en) 2021-04-02 2024-01-23 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11486330B2 (en) 2021-04-02 2022-11-01 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US11933279B2 (en) 2021-04-02 2024-03-19 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11933280B2 (en) 2021-04-02 2024-03-19 Ice Thermal Harvesting, Llc Modular mobile heat generation unit for generation of geothermal power in organic Rankine cycle operations
US11946459B2 (en) 2021-04-02 2024-04-02 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US11959466B2 (en) 2021-04-02 2024-04-16 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power in an organic Rankine cycle operation
US12385474B2 (en) 2021-04-02 2025-08-12 Ice Thermal Harvesting, Llc Systems for generating geothermal power in an organic Rankine cycle operation during hydrocarbon production based on working fluid temperature
US11971019B2 (en) 2021-04-02 2024-04-30 Ice Thermal Harvesting, Llc Systems for generating geothermal power in an organic Rankine cycle operation during hydrocarbon production based on wellhead fluid temperature
US12049875B2 (en) 2021-04-02 2024-07-30 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power in an organic Rankine cycle operation
US12060867B2 (en) 2021-04-02 2024-08-13 Ice Thermal Harvesting, Llc Systems for generating geothermal power in an organic Rankine cycle operation during hydrocarbon production based on working fluid temperature
US12104553B2 (en) 2021-04-02 2024-10-01 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US12110878B2 (en) 2021-04-02 2024-10-08 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US12135016B2 (en) 2021-04-02 2024-11-05 Ice Thermal Harvesting, Llc Systems for generating geothermal power in an organic Rankine cycle operation during hydrocarbon production based on wellhead fluid temperature
US12140124B2 (en) 2021-04-02 2024-11-12 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power at a drilling rig
US12146475B2 (en) 2021-04-02 2024-11-19 Ice Thermal Harvesting, Llc Systems and methods for generation of electrical power in an organic rankine cycle operation
US12163485B2 (en) 2021-04-02 2024-12-10 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US12312981B2 (en) 2021-04-02 2025-05-27 Ice Thermal Harvesting, Llc Systems and methods utilizing gas temperature as a power source
US12305624B2 (en) 2021-04-02 2025-05-20 Ice Thermal Harvesting, Llc Modular mobile heat generation unit for generation of geothermal power in organic rankine cycle operations
US11959055B2 (en) * 2022-01-06 2024-04-16 Premium Oceanic Inc. Systems and methods for conversion of a biomass into biofuel using a geothermal heat source
US12404484B2 (en) 2022-01-06 2025-09-02 Blue Evolution Inc. Systems and methods for conversion of a biomass into biofuel using a geothermal heat source
US20230212493A1 (en) * 2022-01-06 2023-07-06 Premium Oceanic Inc. Systems and methods for conversion of a biomass into biofuel using a geothermal heat source
US12534990B2 (en) 2022-12-29 2026-01-27 Ice Thermal Harvesting, Llc Power generation assemblies for hydraulic fracturing systems and methods
US12180861B1 (en) 2022-12-30 2024-12-31 Ice Thermal Harvesting, Llc Systems and methods to utilize heat carriers in conversion of thermal energy
WO2025259701A1 (en) * 2024-06-11 2025-12-18 Lacey Kevin S Systems and methods for treating organic waste with geothermal energy

Also Published As

Publication number Publication date
BR112013028426A2 (pt) 2019-09-24
AU2012250684A1 (en) 2013-11-21
WO2012151447A2 (en) 2012-11-08
CA2834858A1 (en) 2012-11-08
EP2705131A2 (en) 2014-03-12
CN103608449B (zh) 2016-06-22
RU2013153484A (ru) 2015-06-10
AU2012250684B2 (en) 2017-02-23
CN103608449A (zh) 2014-02-26
CN106010615A (zh) 2016-10-12
MX2013012789A (es) 2014-09-22
EP2705131A4 (en) 2015-01-14
RU2627594C2 (ru) 2017-08-09
WO2012151447A3 (en) 2012-12-27
CN106010615B (zh) 2020-07-24
PH12013502247A1 (en) 2014-01-13

Similar Documents

Publication Publication Date Title
AU2012250684B2 (en) Underground reactor system
CN107847898B (zh) 生物质的生长和处理的系统和方法
US20140046105A1 (en) Underground reactor system
US10808190B2 (en) Apparatus and method for conversion of solid waste into synthetic oil, gas, and fertilizer
Gallup Production engineering in geothermal technology: a review
US8381523B2 (en) Geothermal electricity production methods and geothermal energy collection systems
CN101265868B (zh) 利用油气水分离器分离出的流体综合发电的方法和装置
US8017366B1 (en) Self-contained biofuel production and water processing apparatus
Sigfússon et al. 2014 JRC geothermal energy status report
CA2650617A1 (en) Method and apparatus for capture and sequester of carbon dioxide and extraction of energy from large land masses during and after extraction of hydrocarbon fuels or contaminants using energy and critical fluids
US20240126957A1 (en) Well reactor systems and methods for biomass conversion and computer-readable media
BR112015007638B1 (pt) sistemas de fermentação alimentados por gás
Rajabzadeh et al. Biomass leachate treatment and nutrient recovery using reverse osmosis: experimental study and hybrid artificial neural network modeling
Pambudi et al. Performance evaluation and optimization of fluidized bed boiler in ethanol plant using irreversibility analysis
EP4602134A1 (en) Systems and methods for converting biomass to biocrude using hydrothermal liquefaction
CN201381828Y (zh) 常压油井热洗清蜡置换装置
Alkhasov et al. Evaluating the effect from constructing binary geothermal power units based on spent petroleum and gas boreholes in the south regions of Russia
El Bast Numerical and experimental studies for the conception of a robust hydrothermal liquefaction reactor
Darzi Computational Modeling of Closed-Loop Geothermal System
Alireza Computational Modeling of Closed-loop Geothermal System
US20250043672A1 (en) Comprehensive Enerty Systems
WO2025053988A2 (en) Systems and methods for converting biomass to hydrochar using hydrothermal carbonization
Bolkeny et al. Natural gas hydrate fundamentals methods of analysis of hydrate cage structures and applications as an energy source
Bordage et al. A study of biofuel production using molten salt catalysts
Rahnavard¹ et al. A Feasibility Study on Implementing the Energy Piles in Electric Power Industries

Legal Events

Date Code Title Description
STCB Information on status: application discontinuation

Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION