WO2012151447A2

WO2012151447A2 - Underground reactor system

Info

Publication number: WO2012151447A2
Application number: PCT/US2012/036400
Authority: WO
Inventors: Brandon Iglesias
Original assignee: The Administrators Of The Tulane Educational Fund
Priority date: 2011-05-03
Filing date: 2012-05-03
Publication date: 2012-11-08
Also published as: AU2012250684A1; EP2705131A2; AU2012250684B2; CN103608449A; US20140206912A1; RU2627594C2; BR112013028426A2; WO2012151447A3; CN106010615A; MX2013012789A; CA2834858A1; RU2013153484A; CN106010615B; CN103608449B; EP2705131A4

Abstract

An underground reactor for creating hydrocarbons and chemicals from organic material preferably includes a heat recovery device. Some embodiments of the present invention include at least one tube that injects biomass underground and at least one second tube that collects reacted biomass on the surface. Further tubes are also disclosed for the ability to control temperature and pressure and collect minerals and carbon dioxide. Methods for utilizing the reactor are additionally provided. Further embodiments include methods of using the reactor such as, for example, methods of creating fuel from algae and methods of using the minerals and carbon dioxide as food for an algae farm that will be used as biomass for the reactor.

Description

PATENT APPLICATION

Docket No. TU-278 (78442.29WO)

TITLE OF THE INVENTION UNDERGROUND REACTOR SYSTEM

INVENTOR

IGLESIAS, Brandon, a US citizen, of 2721 St. Charles Ave. 2B, New Orleans, Louisiana, 70130, US.

ASSIGNEE:

THE ADMINISTRATORS OF THE TULANE EDUCATIONAL FUND, a Louisiana, US, non-profit corporation, having an address of 6823 St. Charles Ave., Suite 300, Gibson Hall, New Orleans, LA 70118, US.

CROSS-REFERENCES TO RELATED APPLICATIONS

Priority of US Provisional Patent Application Serial No. 61/481,918, filed 3 May 2011, and US Provisional Patent Application Serial No. 61/602,841, filed 24 February 2012, both hereby incorporated herein by reference, is hereby claimed.

STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH

Not Applicable.

COMPACT DISK SUBMISSION NOT APPLICABLE.

BACKGROUND

As the world population continues to increase, more sustainable energy processes must be used to support more people. Many oil wells have been drilled around the globe to pump oil from the ground and then are abandoned once the well runs dry.

Meanwhile, biofuels has begun a completely separate track of development, where conversion of biomass to alcohol-based fuels are the primary focus.

Significant research and development into algae and diatoms began in 1978, due to the Organization of the Petroleum Exporting Countries (OPEC) oil embargo. Prior to 1978 Jack Myers and Bessel Kok published a book on Algal Culture "From Laboratory to Pilot Plant" and Massachusetts Institute of Technology (MIT) had mass culture projects on the rooftop circa 1950. Research ramped up when the Department of Energy's (DOE) Office of Fuels Development funded the original Aquatic Species Program (ASP) at the National Renewable Energy Laboratory (NREL) for 16 years to define and determine the industrial viability of algae to energy. The 1998 ASP close-out report identifies green algae and diatoms as the most primitive forms of plants, thus most efficient at cell division and growth because they do not waste energy on infrastructure, such as roots, stems and leaves as terrestrial plants do. 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. Additionally, it stated that there is little prospect for alternative industrial scale production of algae without using the open algae pond designs. Further, algae production cost analysis was recommended due to the difficulty of maintaining highly productive organisms. Algae biomass production rate is determined by the availability of nutrients, intensity of light, temperature and C(¾. The effect of light, nutrients and temperature are multiplicative. Calculations have been done indicating the temperatures and pressures required for a reaction to occur. As relative permittivity decreases, water acts more as a solvent, partially attributable to reduced polarity. Using the Arrhenius equation, water dissociation constant has been calculated for variable temperature and constant pressure, or variable pressure and constant temperature. 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.

Incorporated herein by reference are the following references:

US Patent No. 4,003,393 (which discloses a dissolvable pipeline pig). US 4,467,861 ; AU 2011200090 (Al); US2011/092726; WO2009149519A1 ; US 3,955,317; US 5,958,761 ; FR2564855; EP1923460; EP1382576; US2005/064577; DEI 02006045872; US2004/033557; US2007/295505; US 6,468,429; WO2011086358; GB2473865;

DEI 02006045872; US2004/0033557; US2007/0295505; US 4,937,052; US 4,272,383; US 7,866,385; US 7,977,282. Modeling Algae Growth in an Open-Channel Raceway by Scott C. James and Varun Boriah.

Advanced Organic Rankine Cycles in Binary Geothermal Power Plants by Uri Kaplan, World Energy Council, 2007.

Hydrothermal Liquifaction to Convert Biomass into Crude Oil by Yuanhui Zhang, ch. 10, Biofuels from Agricultural Wastes and Byproducts, 2010.

Biomass gasification in near- and super-critical water: Status and Prospects by Yukihiko

Matsumara, et al. , Biomass and Bioenergy, 2005. Organic Rankine Cycle Configurations by Uri Kaplan, Proceedings European Geothermal Congress, 2007.

Utilizing Organic Rankine Cycle Turbine Systems to Efficiently Drive Field Injection Pumps by Nadav Amir, GRC2007 Annual Meeting, 2007.

ASME Steam Tables. Thermodynamic and Transport Properties of Steam, The 1967 IFC formulation for industrial use. 6th Edition, ASME, 1993.

Benjamin, M. 2002. Water Chemistry, 1st edition. New York: McGraw Hill.

Aqueous Systems at Elevated Temperatures and Pressures: Physical Chemistry in Water, Steam and Hydrothermal Solutions, International Association for the Properties of Water and Steam, 2004.

Piezoelectricity: History and New Thrusts, Ultrasonics Symposium, 1996.

Adiabatic Processes http://hvperphysics.phy-astr.gsu.edu/hbase/thermo/adiab.html, Georgia State University

SUMMARY

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.

Some embodiments use algae as the biomass. Other embodiments have open algae ponds near the reactor that are used for feedstock. Some embodiments utilize effluent water to provide temperature control for algae raceway ponds by using indirect geothermal energy. Further embodiments allow for the reactor's recycle streams to provide Nitrogen,

Phosphorous, Potassium, carbon dioxide, and elevated temperature in open algae ponds. 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. Preferably, 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.

Preferably, the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.

Preferably, the equipment includes a pump.

Preferably, 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.

Preferably, the present invention further comprises a heat exchanger for extracting heat to be used in powering equipment used in the fuel creation process.

Preferably, 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.

Preferably, the equipment includes the pump. Preferably, the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.

Optionally, the organic material is biomass.

Preferably, the biomass is algae.

Optionally, the organic material is a polymer. Optionally, the organic material is solid waste.

Optionally, the organic material is reacted through liquefaction.

Optionally, the organic material is reacted through a thermochemical reaction.

Optionally, the organic material is reacted through hydrothermal processes. Preferably, the second tube is within the first tube.

Preferably, the first tube is closed at its bottom and the second tube is open at its bottom.

Preferably, the first tube is deeper underground than the second tube.

Preferably, the present invention further comprises a casing that encloses the first tube and the second tube. Optionally, the casing goes at least as deep as the first tube.

Optionally, the casing does not go as deep as the first tube.

Preferably, the present invention , further comprises a screen that goes down to the depth of the first tube.

Preferably, the casing is an insulator. Preferably, the insulator is cement.

Preferably the present invention further comprises at least a third tube that a heat transfer material may be pumped through.

Preferably, the heat transfer material is water.

Preferably, the present invention further comprises an oil, gas, water separator that separates the products effluent from the reactor.

Optionally, the separator is above ground.

Optionally, the separator is below ground. Optionally, a portion of the products are stored . Optionally, a portion of the products are used as food to grow biomass. Optionally, a portion of the products as used to generate electricity. Preferably, electricity is generated via a heat exchange. Optionally, at least the first tube is curved.

Optionally, at least the first tube is sloped. Optionally, at least the first tube forks.

The present invention includes a method of performing a high-pressure, high- temperature reaction comprising sending organic material underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert to the organic material to fuel, hydrocarbon, or chemicals; bringing the fuel, hydrocarbon, or chemicals up through a second conduit; andcirculating heat exchange fluid in a closed loop to keep the reaction zone at a desired temperature.

Preferably, the present invention further comprises using a heat exchanger for extracting heat to be used in powering equipment used in the conversion process.

Preferably, the present invention further comprises using an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the conversion process.

Preferably, the equipment includes the pump. The present invention includes a method of performing a high-pressure, high- temperature reaction comprising: sending organic material underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert to the organic material to fuel, hydrocarbon, or chemicals; bringing the fuel, hydrocarbon, or chemicals up through a second conduit; andusing a heat exchanger for extracting heat to be used in powering equipment used in the conversion process.

Preferably, the present invention further comprises circulating heat exchange fluid in a closed loop to keep the reaction zone at a desired temperature. Preferably, the present invention further comprises using an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the conversion process.

Preferably, the equipment includes the pump.

Preferably, pressure may be adjusted by increasing or decreasing tubular reactor depth.

Preferably, the present invention further comprises sending a heat transfer material underground. Optionally, the present invention further comprises controlling the temperature of the heat transfer material by adjusting circulation rate.

Optionally, the present invention further comprises controlling the temperature of the heat transfer material by increasing or decreasing the temperature of the organic material.

Preferably, the present invention further comprises frac'ing the rock prior to sending the heat transfer material underground. Optionally, the present invention further comprises sending the heat transfer material from underground into a heat exchanger.

Optionally, the present invention further comprises sending the heat transfer material from underground into an organic rankine cycle.

Preferably, the present invention further comprises separating the products into oil, gas and water-based solution.

Preferably, the present invention further comprises sending the water-based solution to a biomass growth.

Optionally, the present invention further comprises combusting off gas products and using the energy for drying heat exchange.

Optionally, the present invention further comprises combusting off gas products and using the energy to produce electricity.

Optionally, the present invention further comprises combusting off gas products and using the energy to produce mechanical energy.

Optionally, the present invention further comprises combusting off gas products and using the energy to produce heat.

Preferably, the present invention further comprises sending a portion of the effluent products of the second tube to feed a biomass.

Preferably, the biomass is algae.

Preferably, a portion of the effluent products comprise carbon dioxide. Optionally, a portion of the products as used as feedstock for distillation process. Optionally, a portion of the products as used as feedstock for pyrolysis process. Preferably, the present invention further comprises spalling the rock The present invention includes post processing of bio-oil / crude oil leaving

ReactWell to be separated into light, distillate and heavy fractions prior to shipment. Oil stabilization to be accomplished by using an underground geothermal density and ionic separation unit that uses geothermal heat to drive density separation and ionic separation by bridging geothermal with piezo-electric rods that generate a voltage drop across the separation fluid due to the temperature gradient inside of the underground separation column. Thus, the column uses geothermal energy for heat and for ionic separation processes. Using density separation alone is not 'cost- effective' due to time constraints (current practice in my yellow grease tanks, goes slower during winter and faster during summer) - however, ionic separation is also used to speed-up separation processes, which is typically driven by an applied electrical voltage. Ionic separation columns use voltage differential to separate polar/ionic mixtures (learned about this in making biodiesel). Reversible piezoelectric materials generate temperature differences when driven by an applied voltage (this is a reversible process: may also be used to generate a voltage differential when element sides are exposed to a "Delta T" temperature difference):

Use of liquid alkali, alkaline, transitional, other metals, water, brine and various other compounds as heat transfer fluid

Demineralization Unit (DMIN) to remove minerals for resale via cooling or magnetic b-fields (ancillary revenue stream)

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

Use of pipe cleaning object, such as a pig, in 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.

Some helpful features of the invention include: Pig Friendly Design for easy scale removal on heat transfer fluid side in contact with formation fluids (geothermal reservoir)

a. Key difference between pig friendly design and prior design is the heat transfer fluid flowing within the inner diameter (I.D.) of the pipes. Pigs work best when they're servicing the I.D. of a pipe and not the O.D.

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.

Mixer/paddles/screws that mix casing working fluid to create convective heat transfer to tubular reactor;

Gear box that drives the downhole mixer - to be powered by ORC unit;

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);

Convective heat transfer using rotational speed of mixer(s);

Bio-oil stabilization: Downstream bio-oil processing will occur in a topping unit, to separate out light ends, distillate and heavier 6 oil material with later downstream oxygenate and nutrient recovery processing steps prior to leaving facility gates for refinery or petrochemical delivery. By incorporating a small topping unit and nutrient recovery into ReactWell's infrastructure, select cuts of hydrocarbon may be specifically tailored to fluidized catalytic crackers (FCC: "cat-crackers") and delayed coking units for a given refiner or petro-chemical complex to optimize finished product ASTM specs, while maximizing valuable nutrient recovery at the ReactWell facility. The key difference in ReactWell' s topping unit is that it de-couples fossil fuel use to separate fossil fuel into select fractions of light ends, distillate and heavy 6 oil bottoms. ReactWell accomplishes the oil fractionation using geothermal ionic separation technology, which uses geothermal derived loop heat pipe to drive density separation with latent heat capillary flow and piezoelectric material to create a voltage in response to the geothermal temperature gradient and stress from hydraulic head. Thus, liquid phase separation occurs

underground due to temperature, capillary action, stress and voltage gradients created and sustained by geothermal heat, wicking material selection, piezoelectric material selection and gravity.

In some instances the geothermal heat and associated gradient may not be sufficient to meet reactor conditions due to reduced permeability associated with scale and plugging over the lifetime of operating the underground reactor system. Additionally, it may be required to run the tubular reactor at higher temperatures. Thus, pre-heating the inlet to the tubular reactor and working heat transfer fluid through either combustion (recycling the effluent C0₂ to the algal pond), electric heater or concentrating solar power (CSP) may prove to be an effective solution in delaying re-fracking and stimulation of the reservoir. Advantages of embodiments of the present invention include:

Use of a cleaning/pigging device to remove scale/fouling;

Use of a working heat exchange fluid to isolate the geothermal reservoir fluid from fouling the tubular reactor;

Use of underground agitator(s) to force convective heat transfer;

Use of underground piezoelectric/thermal particles to transform stress into heat;

Use of underground catalyst; and

Use of underground vapor collapse to generate latent heat . BRIEF DESCRIPTION OF THE DRAWINGS

The following drawings form part of the present specification and are included to further demonstrate certain aspects of the present invention. The invention may be better understood by reference to one or more of these drawings in combination with the description of specific embodiments presented herein.

Figure 1. An exemplary geothermal depolymerization tubular reactor.

Figure 2. An exemplary underground reactor system.

Figure 3. Exemplary underground reactor fluid flow.

Figure 4. Exemplary hydro-geothermal reactor process flow diagram. Figure 5. Exemplary hydro-geothermal reactor process flow diagram.

Figure 6. An exemplary geothermal tubular reactor.

Figure 7. An exemplary geothermal tubular reactor.

Figure 8. An exemplary geothermal tubular reactor.

Figure 9. An exemplary geothermal tubular reactor. Figure 10. An exemplary geothermal tubular reactor.

Figure 11. An exemplary geothermal tubular reactor where there is no pump-around tube, the inlets and outlets are separated and there is no casing.

Figure 12. Working heat transfer temperature curve inside of casing

Figure 13. Working heat transfer temperature profile inside of casing subjected to forced convection

Figure 14. Tubular reactor profile Figure 15. Tubular reactor profile subjected to forced convection

Figure 16. Illustration of isolated hot geothermal reservoir fluid from hot working fluid from reactor process fluid

Figure 17. Tubular reactor with geothermal reservoir fluid casing injection Figure 18. Tubular reactor with external geothermal reservoir fluid injection

Figure 19. Tubular reactor with isolated geothermal reservoir fluid

Figure 20. Tubular reactor with isolated geothermal reservoir fluid & forced convection

Figure 21. Tubular reactor using piezothermal/electric particles and catalyst

Figure 22. Tubular reactor using gas injection isolated from geothermal reservoir fluid Figure 23. CFD model of casing, tubular reactors and hot geothermal transfer pipes.

Calculations. The sheets attached after the figures in US Provisional Patent Application Serial No. 61/602,841 provide calculations illustrating the feasibility of embodiments of the present invention.

DETAILED DESCRIPTION DEDICATED GEOTHERMAL TUBULAR REACTOR (HYDROLYSIS,

DEPOLYMERIZATION, DECARBOXYLATION, AND THERMAL DEGRADATION)

Downhole temperatures and pressures exist to create and sustain hydro-geothermal reactions and thermal depolymerization given available geothermal energy within the earth. Bedrock temperature as a function of depth will be used as the reference temperature driving force. The tubular depolymerization reactor section will be modeled with the casing full of water that is not subject to forced circulation.

Hydro- Geothermal Reactor

Table 1 : Depolymerization variables of interest

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. When the downhole algae in water pressure and temperature exceeds atmospheric and ambient temperature the algae and other organic matter undergoes hydrolysis and partial thermal degradation to form carbon, C(¾, off-gas, hydrocarbon and hot mineral rich water containing amino acids. 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 Figure 1.

In one embodiment, 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.

In some embodiments, the depth of an underground reactor may range from 33 ft - 40,502 ft (10 m -_12,345 m). In some embodiments, 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), and 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. As dry oil and gas exploration, production and geothermal holes can be used in the present invention, the tubing used in such installations will be sized appropriately to fit therein. For example, in a hole of about 5,000+ feet (1,524+ m) in length, the tubing diameters will likely be about 12 up to 120 inches (30 - 305 cm).

In some embodiments, there may be more than one tubular reactor.

In some embodiments, temperatures needed for an effective reaction may be greater than 100 °C and up to 2,000 °C, and pressures needed for an effective reaction may be 14.7psig (203 kPa) up to 40,000 psig (275,892 kPa).

Based on the temperature and pressure ranges within the reactor, liquefaction thermochemical or hydrothermal processes may occur within the reactor during certain ranges of T and P in water:

100°C up to 374°C (subcritical water) and 14.7 psig (203 kPa) up to 30,000 psig (206,944 kPa)

374°C up to 500+°C (supercritical water) and 14.7 psig (203 kPa) up to 30,000 psig (206,944 kPa)

Some embodiments may use any type of organic matter to create products within the reactor under the relevant temperature and pressure conditions. In certain embodiments, 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.

In some embodiments, there may be a dedicated geothermal tubular with multiple tubulars with coiled tubing option for increased forced convection heat-transfer at one or multiple geothermal heat mines. Effluent geothermal fluid flow may exit into an organic rankine cycle (ore). 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) fluid vapors drive a turbine and the turbine exhaust vapors may be force-draft cooled with hot air for use in drying processes and later water cooled to provide additional warmth to algae ponds. 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 Figure 3. Some embodiments may use any heat transfer fluid to flow through the reactor and tune the temperature.

In some embodiments, 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.

VARIABLE DESCRIPTION

Tinlet Bottom hole inlet temperature

Toutlet Discharge outlet temperature

Ti₅rock Rock temperature profile Ti₅down Downward flowing fluid temperature in casing

T ¹ i,up Upward flowing fluid temperature in tubular

¹ casing Water flow rate in casing

Finlet Water flow rate in tubular ttube Total water residence time in tubular teasing Total water residence time in casing

Table 2: Geothermal pump-around key variables

If 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.

In some embodiments, 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. Examples of 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. In yet other embodiments, 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. Further, 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. Further, the organic working fluid in the condensing section may serve to warm algae ponds.

HOT EFFLUENT WATER CONTAINING MINERALS, AMINO ACIDS AND CARBON 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.

Post-separation, 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. In some embodiments, total hot water return volume may be set at V₃ of raceway water volume, so that V₃ of the raceway water may be turned over and processed each day.

In some embodiments, 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. In some embodiments, 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. VARIABLE DESCRIPTION

^outlet Reactor outlet temperature

Foutlet Reactor outlet flow rate

Tamb Ambient temperature

Vw, y Wind velocity and direction

Fdis charge Pond discharge rate

Erate Evaporation rate

P Precipitation

RH Relative humidity

Patm Atmospheric pressure

Pdepth Algae pond depth

Plength Algae pond length

Pwidth Algae pond width

Τ ₅γ₅ζ pond Algae pond temperature

distribution

F x,y,z Algae pond circulation

Table 3: Algae Raceway & Process Variables

PRODUCTION OF CARBON DIOXIDE UNDERGROUND FROM ALGAE IN WATER, BIOMASS, WASTE AND POLYMERS

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. PRODUCTION OF HYDROCARBON LIQUID/GAS MIXTURE UNDERGROUND FROM ALGAE IN WATER, BIOMASS, WASTE AND POLYMER CREATED FROM GEOTHERMAL DRIVEN HYDROLYSIS AND THERMAL DEGRADATION

When 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. In some embodiments, 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 Figures 4 and 5. Coke production may occur via pyrolysis.

STREAM DESCRIPTION

Fl Algae in water raceway is injected into Hydro- Geothermal

Reactor

PI Produced oil from reactor

P2 Produced light end gas and CO₂

P3 Produced mineral and amino acid hot effluent water to be

recycled back into algae pond for N-P-K and Temperature algae growth multiplicative enhancement

Table 4: Hydro-Geothermal Reactor Streams

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 CO₂ and mineral rich hot water. STREAM DESCRIPTION

F0 Algae in aqueous phase is fed into hydro-geothermal reactor

Fl Industrial waste water is fed into hydro-geothermal reactor

F2 Combined waste water and algae feed stream to reactor

PI Oil produced from reactor is then fed to coker for gasification

P2 Reactor light ends and CO₂ fed to turbine

P3 Hot water effluent enriched with minerals and amino acids recycled to algae pond to enhance growth rate

CI Coker light ends and CO₂ fed to turbine for electricity, heat and

CO₂ generation

C2 Produced coke can be used to generate electricity, heat and CO₂

TF Produced transportation fuel may be processed into renewable gasoline, jet, kerosene and diesel.

E Electricity to power pumps and auxiliary equipment

HI Products of coke combustion include heat and possibly low pressure steam if CCGT used

Tl Combustion product of turbine generates heat and possibly low pressure steam if CCGT used T2 Combustion product of turbine generates C0₂ and ¾0

H2 Combustion product of coke generates CO₂ and ¾0

Table 5: ReactWell PFD

Figure 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 Figure 19-3) is plotted in Figure 13.

Figure 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 Figure 20-3) is plotted in Figure 13. Figure 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 Figure 19-19) is immersed in the working heat transfer fluid (see Figure 19-3). Process reactants enter the reactor (see Figure 19-15), also shown in the bottom left hand section of the plot. The process fluid flows underground through the annular space (see Figure 19-4) then returns through the center pipe (see Figure 19-5). The reactor temperature profile may be adjusted by adjusting the temperature and flow rate of injection stream (Figure 19-14), demineralization flow rate (Figure 19-13), organic rankine cycle flow rate (Figure 19- 16), concentration and distribution of piezo particles in the working heat transfer fluid (see Figure 22-21) or tubular reactor (see Figure 22-22), concentration and distribution of catalyst into the tubular reactor (see Figure 22-23), gas flow rate into the tubular reactor inlet line (see Figure 22-15), inlet temperature of process fluid (Figure 19-15) and flow rate of process fluid (Figure 19-15). Figure 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 Figure 19-19) is immersed in the working heat transfer fluid (see Figure 19-3). Process reactants enter the reactor (see Figure 19-15), also shown in the bottom left hand section of the plot. The process fluid flows underground through the annular space (see

Figure 19-4) then returns through the center pipe (see Figure 19-5). The reactor temperature profile may be adjusted by adjusting the temperature and flow rate of injection stream (Figure 19-14), demineralization flow rate (Figure 19-13), organic rankine cycle flow rate (Figure 19- 16), concentration and distribution of piezo particles in the working heat transfer fluid (see Figure 22-21) or tubular reactor (see Figure 22-22), concentration and distribution of catalyst into the tubular reactor (see Figure 22-23), gas flow rate into the tubular reactor inlet line (see Figure 22-15), inlet temperature of process fluid (Figure 19-15), flow rate of process fluid (Figure 19-15) and mixer rod rotational velocity (Figure 22-18.b) and mixer rod impeller, screw or paddle geometry (Figure 22- 18b) Figure 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 Figure 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. Thus, by isolating the geothermal working fluid within a pipe and using a working heat transfer fluid (water, brine, mercury, etc.) to transfer heat from the isolated geothermal fluid into the tubular reactor, feasible operation of an underground reactor is accomplished by significantly reducing maintenance downtime and costs.

Figure 17 lists a casing contained injection and reactor configuration. The continuously stirred rods devices (Figure 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 (Figure 17-3) and flows downhole and into the reservoir (Figure 17-9) and through the fracked rock (Figure 17-10) and flows back out through the return pipe (Figure 17-8) into the organic rankine unit (Figure 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 (Figure 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).

Figure 18 lists a casing contained reactor configuration with external injection line. The continuously stirred rods devices (Figure 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 (Figure 18-14) and flows downhole and into the reservoir (Figure 18-10) and through the fracked rock (Figure 18-9) and flows back out through the return pipe (Figure 18- 11) into the organic rankine unit (Figure 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 (Figure 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). Figure 19 lists a casing contained reactor configuration with external injection line (Figure 19-14), casing contained/internal geothermal reservoir fluid isolation and heat transfer line (Figure 19-13), casing contained/internal tubular reactor (Figure 19-19), and external geothermal reservoir fluid return line (Figure 19-16). Geothermal reservoir fluid is injected in (Figure 19-14) and flows downhole and into the reservoir (Figure 19-10) and through the fracked rock (

Figure 19-9) and flows back out through the return pipe (Figure 19-11) into the organic rankine unit (Figure 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 (Figure 19-13 and 19-16 streams for mineralization recovery through a demineralization unit (DMIN). The key difference between Figure 19 and prior Figure 17 and 18 is the use of a hot heat transfer pipe (Figure 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 (Figure 19-7) is to provide easy maintenance / pigging through the inner diameter to remove scale and increase heat transfer. The working heat transfer fluid (Figure

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). Figure 20 lists a casing contained reactor configuration with external injection line (Figure

20- 14), casing contained/internal geothermal reservoir fluid isolation and heat transfer line (Figure 20-13), casing contained/internal tubular reactor (Figure 20-19), and external geothermal reservoir fluid return line (Figure 20-16). Geothermal reservoir fluid is injected in (Figure 20-14) and flows downhole and into the reservoir (Figure 20-10) and through the fracked rock (

Figure 20-9) and flows back out through the return pipe (Figure 20-11) into the organic rankine unit (Figure 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 (Figure 20-13 and 20-16 streams for mineralization recovery through a demineralization unit (DMIN). The key difference between Figure 20 and prior Figure 17 and 18 is the use of a hot heat transfer pipe (Figure 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 (Figure 20-7) is to provide easy maintenance / pigging through the inner diameter to remove scale and increase heat transfer. The working heat transfer fluid (Figure 20-3) transfer heat into the tubular reactor by wetting both tubular reactor and hot heat transfer geothermal pipe. The secondary key difference between Figure 20 and Figure 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). Figure 21 lists a casing contained reactor configuration with external injection line (Figure

21- 14), casing contained/internal geothermal reservoir fluid isolation and heat transfer line (Figure 21-13), casing contained/internal tubular reactor (Figure 21-19), and external geothermal reservoir fluid return line (Figure 21-16). Geothermal reservoir fluid is injected in (Figure 21-14) and flows downhole and into the reservoir (Figure 21-10) and through the fracked rock (Figure 21-9) and flows back out through the return pipe (Figure 21-11) into the organic rankine unit (Figure 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 (Figure 21-13 and 21-16 streams for mineralization recovery through a demineralization unit (DMIN). The key difference between Figure 21 and prior Figure 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).

Figure 22 lists a casing contained reactor configuration with external injection line (Figure

22- 14), casing contained/internal geothermal reservoir fluid isolation and heat transfer line (Figure 22-13), casing contained/internal tubular reactor (Figure 22-19), and external geothermal reservoir fluid return line (Figure 22-16). Geothermal reservoir fluid is injected in (Figure 22-14) and flows downhole and into the reservoir (Figure 22-10) and through the fracked rock (Figure 22-9) and flows back out through the return pipe (Figure 22-11) into the organic rankine unit (Figure 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 (Figure 22-13 and 22-16 streams for mineralization recovery through a demineralization unit (DMIN). The key difference between Figure 22 and prior Figure 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). Figure 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 Figure 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.

EXAMPLES

Examples and methods of use are described herein as a basis for teaching one skilled in the art to employ the invention in any appropriate manner. These examples disclosed herein are not to be interpreted as limiting.

Example 1

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. Example 2 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.

Example 3

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. Then 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.

Example 4 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 backpressure control valve.

Example 5

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. 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.

Example 6 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. Then 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. Then 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. Example 7

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. 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. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When a pump-around requires servicing the tubular reactor's will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and serviced. 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. In the event of total rework of the reactor, 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. The unit should be depressurized to ambient conditions and verified prior to opening any chambers, vessels, reactors, piping or coiled tubing.

It is noted that terms like "preferably," "commonly," and "typically" are not utilized herein to limit the scope of the claimed invention or to imply that certain features are critical, essential, or even important to the structure or function of the claimed invention. Rather, these terms are merely intended to highlight alternative or additional features that may or may not be utilized in a particular embodiment of the present invention.

Detailed descriptions of one or more embodiments are provided herein. It is to be understood, however, that the present invention may be embodied in various forms.

Therefore, specific details disclosed herein (even if designated as preferred or advantageous) are not to be interpreted as limiting, but rather are to be used as a basis for the claims and as a representative basis for teaching one skilled in the art to employ the present invention in any appropriate manner.

A number of embodiments have been described. Nevertheless it will be understood that various modifications may be made without departing from the spirit and scope of the invention. Accordingly, other embodiments are included as part of the invention and may be encompassed by the attached claims. Furthermore, the foregoing description of various embodiments does not necessarily imply exclusion. For example, "some" embodiments, "exemplary" embodiments, or "other" embodiments may include all or part of "some," "other," and "further" embodiments within the scope of this invention.

Example 8 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). 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. Further, there will be a second hole and casing that will power an organic rankine unit (ORC) with effluent hot geothermal reservoir fluid, so that the fluid remains hot prior to entry into the ORC cycle. The reactor' s tubular pump-around system will be inventoried with a fixed quantity of treated water, circulation started using a separate startup pump. After the tubular pump-around system has been circulating then start injecting geothermal fluid downhole to. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and line up to generate electricity. Generated electricity may come from turbine and piezoelectric/thermal devices. ORC condenser cooling fluid flow will be adjusted accordingly. The cooling fluids may be sourced from fin fans or 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. 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 CO₂ used to carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When the injection pipe or effluent hot geothermal reservoir fluid pipe requires servicing the tubular reactor's will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and isolated. The tubular reactor effluent will be slowly lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature. In the event of total rework of the reactor, the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off, isolated and depressurized. Once temperatures stabilize then 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, pulling pipe, making trips, removing vessels, reactors, piping or coiled tubing.

Example 9 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). 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. Further, there will be a second hole and casing that will power an organic rankine unit (ORC) with effluent hot geothermal reservoir fluid, so that the fluid remains hot prior to entry into the ORC cycle. The reactor' s tubular pump-around system will be inventoried with a fixed quantity of treated water, circulation started using a separate startup pump. After the tubular pump-around system has been circulating then start injecting geothermal fluid downhole to. Once temperatures reach organic rankine cycle (ORC) targets then switch to the direct drive injection pump to power the pump-around circuit and line up to generate electricity. Generated electricity may come from turbine and piezoelectric/thermal devices. ORC condenser cooling fluid flow will be adjusted accordingly. The cooling fluids may be sourced from fin fans or 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. 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 C(¾ used to carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When the injection pipe or effluent hot geothermal reservoir fluid pipe requires servicing the tubular reactor's will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and isolated. The tubular reactor effluent will be slowly lined-up to coolers to maintain low temperatures inside of the reactor to prevent thermal stresses due to rapid change in temperature. In the event of total rework of the reactor, the tubular reactor(s) will be inventoried with treated water, the organic rankine cycle (ORC) will be shut-off, isolated and depressurized. Once temperatures stabilize then 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, pulling pipe, making trips, removing vessels, reactors, piping or coiled tubing.

Example 10

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. 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.

Example 11

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. 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. 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. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When a pump-around requires servicing the tubular reactor' s will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and serviced. 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. In the event of total rework of the reactor, 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, 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.

Example 12

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. 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. 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. Post processing of bio-oil / crude oil leaving ReactWell to be separated into light, distillate and heavy fractions prior to shipment. Oil stabilization to be accomplished by using an underground geothermal density and ionic separation unit that uses geothermal heat to drive density separation and ionic separation by bridging geothermal with piezo-electric rods that generate a voltage drop across the separation fluid due to the temperature gradient inside of the underground separation column. Thus, the column uses geothermal energy for heat and for ionic separation processes. Using density separation alone is not 'cost-effective' due to time constraints (current practice in my yellow grease tanks, goes slower during winter and faster during summer) - however, ionic separation is also used to speed-up separation processes, which is typically driven by an applied electrical voltage. The gas, primarily comprised of carbon dioxide, will carbonate the effluent water being recycled to the algae pond. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When a pump-around requires servicing the tubular reactor' s will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and serviced. 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. In the event of total rework of the reactor, 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, 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.

Example 13

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. 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. When one of the tubular reactor(s) requires servicing it will first be flushed with treated water then serviced. When a pump-around requires servicing the tubular reactor's will be flushed with treated water and kept online. The organic rankine cycle (ORC) will be shut-off and serviced. 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. In the event of total rework of the reactor, 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, 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.

What is claimed is:

Claims

1. An underground reactor for use in a fuel creation process for creating fuel from

organic material, comprising: a first conduit that injects an organic material underground ; a second conduit 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.

2. The reactor of claim 1 , further comprising an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the fuel creation process.

3. The reactor of claim 1, wherein the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.

4. The reactor of claim 1 , wherein the equipment includes a pump.

5. The reactor of claim 3, wherein the pump circulates heat exchange fluid to keep a reaction zone at a desired temperature.

6. An underground reactor for use in a fuel creation process for creating fuel from

organic material, comprising: a first conduit that injects an organic material underground ; a second conduit 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.

7. The reactor of claim 6, further comprising a heat exchanger for extracting heat to be used in powering equipment used in the fuel creation process.

8. The reactor of claim 7, further comprising an organic rankine cycle for converting the heat from the heat exchanger to energy to power equipment used in the fuel creation process.

9. The reactor of claim 7, wherein the equipment includes the pump.

10. The reactor of claim 7, wherein the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.

11. The underground reactor of claim 1, wherein the organic material is biomass.

12. The underground reactor of claim 2, wherein the biomass is algae.

13. The underground reactor of claim 1, wherein the organic material is a polymer.

14. The underground reactor of claim 1, wherein the organic material is solid waste.

15. The underground reactor of claim 1, wherein the organic material is reacted through liquefaction.

16. The underground reactor of claim 1, wherein the organic material is reacted through a thermochemical reaction.

17. The underground reactor of claim 1, wherein the organic material is reacted through hydrothermal processes.

18. The underground reactor of claim 1, wherein the second conduit is within the first conduit.

19. The underground reactor of claim 18, wherein the first conduit is closed at its bottom and the second conduit is open at its bottom.

20. The underground reactor of claim 18, wherein the first conduit is deeper underground than the second conduit.

21. The underground reactor of claim 18, further comprising a casing that encloses the first conduit and the second conduit.

22. The underground reactor of claim 21, wherein the casing goes at least as deep as the first conduit.

23. The underground reactor of claim 21, wherein the casing does not go as deep as the first conduit.

24. The underground reactor of claim 23, further comprising a screen that goes down to the depth of the first conduit.

25. The underground reactor of claim 22, wherein the casing is an insulator.

26. The underground reactor of claim 25, wherein the insulator is cement.

27. The underground reactor of claim 21, further comprising at least a third conduit that a heat transfer material may be pumped through.

28. The underground reactor of claim 27, wherein the heat transfer material is water.

29. The underground reactor of claim 28, further comprising an oil, gas, water separator that separates the products effluent from the reactor.

30. The underground reactor of claim 29, wherein the separator is above ground.

31. The underground reactor of claim 29, wherein the separator is below ground.

32. The underground reactor of claim 27, wherein a portion of the products are stored .

33. The underground reactor of claim 27, wherein a portion of the products are used as food to grow biomass.

34. The underground reactor of claim 27, wherein a portion of the products as used to generate electricity.

35. The underground reactor of claim 27, wherein electricity is generated via a heat exchange.

36. The underground reactor of claim 1, wherein at least the first conduit is curved.

37. The underground reactor of claim 1, wherein at least the first conduit is sloped.

38. The underground reactor of claim 37, wherein at least the first conduit forks.

39. A method of performing a high-pressure, high-temperature reaction comprising:

(a) sending organic material underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert to the organic material to fuel, hydrocarbon, or chemicals;

(b) bringing the fuel, hydrocarbon, or chemicals up through a second conduit; and circulating heat exchange fluid in a closed loop to keep the reaction zone at a desired temperature.

40. The method of claim 39, further comprising using a heat exchanger for extracting heat to be used in powering equipment used in the conversion process.

41. The method of claim 40, wherein the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.

42. The method of claim 39, further comprising using an organic rankine cycle for

converting the heat from the heat exchanger to energy to power equipment used in the conversion process.

43. The method of claim 41, wherein the equipment includes the pump.

44. A method of performing a high-pressure, high-temperature reaction comprising:

(a) sending organic material underground through a first conduit, wherein sufficient pressure and temperature is applied to the organic material in a reaction zone to convert to the organic material to fuel, hydrocarbon, or chemicals; (b) bringing the fuel, hydrocarbon, or chemicals up through a second conduit; and

(c) using a heat exchanger for extracting heat to be used in powering equipment used in the conversion process.

45. The method of claim 44, further comprising circulating heat exchange fluid in a closed loop to keep the reaction zone at a desired temperature.

46. The method of claim 44, further comprising using an organic rankine cycle for

47. The method of claim 44, wherein the equipment includes the pump.

48. The method of claim 44, wherein the equipment used in the fuel creation process is directly driven by a device which extracts energy from the heat exchanger.

49. The method of claim 48, wherein pressure may be adjusted by increasing or

decreasing tubular reactor depth.

50. The method of claim 44, further comprising sending a heat transfer material

underground.

51. The method of claim 50, further comprising controlling the temperature of the heat transfer material by adjusting circulation rate.

52. The method of claim 50, further comprising controlling the temperature of the heat transfer material by increasing or decreasing the temperature of the organic material.

53. The method of claim 50, further comprising frac'ing the rock prior to sending the heat transfer material underground.

54. The method of claim 50, further comprising sending the heat transfer material from underground into a heat exchanger.

55. The method of claim 50, further comprising sending the heat transfer material from underground into an organic rankine cycle.

56. The method of claim 48, further comprising separating the products into oil, gas and water-based solution.

57. The method of claim 56, further comprising sending the water-based solution to a biomass growth.

58. The method of claim 48, further comprising combusting off gas products and using the energy for drying heat exchange.

59. The method of claim 48, further comprising combusting off gas products and using the energy to produce electricity.

60. The method of claim 48, further comprising combusting off gas products and using the energy to produce mechanical energy.

61. The method of claim 48, further comprising combusting off gas products and using the energy to produce heat.

62. The method of claim 48, further comprising sending a portion of the effluent products of the second conduit to feed a biomass.

63. The method of claim 62, wherein the biomass is algae.

64. The method of claim 62, wherein a portion of the effluent products comprise carbon dioxide.

65. The method of claim 48, wherein a portion of the products as used as feedstock for distillation process.

66. The method of claim 48, wherein a portion of the products as used as feedstock for pyrolysis process.

67. The method of claim 50, further comprising spalling the rock.