Patent Grant
9399905
1. Field of the Invention
The present invention relates generally to methods and systems for production of hydrocarbons, hydrogen, and/or other products from various subsurface formations such as hydrocarbon containing formations.
2. Description of Related Art
Hydrocarbons obtained from subterranean formations are often used as energy resources, as feedstocks, and as consumer products. Concerns over depletion of available hydrocarbon resources and concerns over declining overall quality of produced hydrocarbons have led to development of processes for more efficient recovery, processing and/or use of available hydrocarbon resources. In situ processes may be used to remove hydrocarbon materials from subterranean formations. Chemical and/or physical properties of hydrocarbon material in a subterranean formation may need to be changed to allow hydrocarbon material to be more easily removed from the subterranean formation. The chemical and physical changes may include in situ reactions that produce removable fluids, composition changes, solubility changes, density changes, phase changes, and/or viscosity changes of the hydrocarbon material in the formation. A fluid may be, but is not limited to, a gas, a liquid, an emulsion, a slurry, and/or a stream of solid particles that has flow characteristics similar to liquid flow.
U.S. Pat. No. 7,575,052 to Sandberg et al., which is incorporated by reference as if fully set forth herein, describes an in situ heat treatment process that utilizes a circulation system to heat one or more treatment areas. The circulation system may use a heated liquid heat transfer fluid that passes through piping in the formation to transfer heat to the formation.
U.S. Patent Application Publication No. 2008-0135254 to Vinegar et al., which is incorporated by reference as if fully set forth herein, describes systems and methods for an in situ heat treatment process that utilizes a circulation system to heat one or more treatment areas. The circulation system uses a heated liquid heat transfer fluid that passes through piping in the formation to transfer heat to the formation. In some embodiments, the piping is positioned in at least two wellbores.
U.S. Patent Application Publication No. 2009-0095476 to Nguyen et al., which is incorporated by reference as if fully set forth herein, describes a heating system for a subsurface formation includes a conduit located in an opening in the subsurface formation. An insulated conductor is located in the conduit. A material is in the conduit between a portion of the insulated conductor and a portion of the conduit. The material may be a salt. The material is a fluid at operating temperature of the heating system. Heat transfers from the insulated conductor to the fluid, from the fluid to the conduit, and from the conduit to the subsurface formation.
There has been a significant amount of effort to develop methods and systems to economically produce hydrocarbons, hydrogen, and/or other products from hydrocarbon containing formations. At present, however, there are still many hydrocarbon containing formations from which hydrocarbons, hydrogen, and/or other products cannot be economically produced. There is also a need for improved methods and systems that reduce energy costs for treating the formation, reduce emissions from the treatment process, facilitate heating system installation, and/or reduce heat loss to the overburden as compared to hydrocarbon recovery processes that utilize surface based equipment.
Embodiments described herein generally relate to systems, methods, and heaters for treating a subsurface formation. Embodiments described herein also generally relate to heaters that have novel components therein. Such heaters can be obtained by using the systems and methods described herein.
In certain embodiments, the invention provides one or more systems, methods, and/or heaters. In some embodiments, the systems, methods, and/or heaters are used for treating a subsurface formation.
In certain embodiments, a method of treating a subsurface formation, includes: circulating at least one molten salt through piping located in the formation to heat at least a portion of the formation and heat at least some hydrocarbons in the formation to at least a mobilization temperature of the hydrocarbons; providing an oxidizing fluid to at least a portion of the piping; and oxidizing coke formed in the piping.
In certain embodiments, a method of treating a subsurface formation, includes circulating at least one molten salt through piping located in the formation to heat at least a portion of the formation and heat at least some hydrocarbons in the formation to at least a mobilization temperature of the hydrocarbons; and locating a liner in and/or around at least a portion of the piping to inhibit formation fluids from entering the piping and contacting the molten salt.
In certain embodiments, a method of treating a subsurface formation, includes: circulating at least one molten salt through at least one conduit of a conduit-in-conduit heater located in the formation to heat at least some hydrocarbons in the formation to at least a mobilization temperature of the hydrocarbons; producing at least some of the hydrocarbons from the formation; assessing an electrical resistance of at least one of the conduits of the conduit-in-conduit heater; and assessing a presence of a leak in at least one of the conduits based on the assessed resistance.
In certain embodiments, a method of treating a subsurface formation, includes: circulating at least one molten salt through at least one conduit of a conduit-in-conduit heater located in the formation to heat at least some hydrocarbons in the formation to at least a mobilization temperature of the hydrocarbons; producing at least some of the hydrocarbons from the formation; circulating an inert gas with the molten salt; and assessing a presence of a leak in at least one of the conduits by assessing a presence of the inert gas inside the walls of at least one of the conduits.
In certain embodiments, a method of treating a subsurface formation, includes: circulating at least one molten salt through piping in the formation to heat at least some hydrocarbons in the formation to at least a mobilization temperature of the hydrocarbons; producing at least some of the hydrocarbons from the formation; terminating circulation of the molten salt in the piping after a selected amount of hydrocarbons have been produced from the formation; and providing a compressed gas into the piping to remove molten salt remaining in the piping.
In certain embodiments, a method of heating a subsurface formation, includes: circulating a heated heat transfer fluid comprising a carbonate molten salt through piping positioned in at least two of a plurality of wellbores using a fluid circulation system, wherein the plurality of wellbores are positioned in a formation; and heating at least a portion of the formation.
In certain embodiments, a method for treating a hydrocarbon containing formation, includes: injecting a composition comprising solid salts in a section of the formation; providing heat from one or more heaters to the portion of the formation to heat the composition to about or above a melting point of the solid salts in the composition; and melting at least a portion of the solid salts to form a molten salt and create fractures in the section.
In further embodiments, features from specific embodiments may be combined with features from other embodiments. For example, features from one embodiment may be combined with features from any of the other embodiments.
In further embodiments, treating a subsurface formation is performed using any of the methods, systems, power supplies, or heaters described herein.
In further embodiments, additional features may be added to the specific embodiments described herein.
Advantages of the present invention may become apparent to those skilled in the art with the benefit of the following detailed description and upon reference to the accompanying drawings in which:
While the invention is susceptible to various modifications and alternative forms, specific embodiments thereof are shown by way of example in the drawings and may herein be described in detail. The drawings may not be to scale. It should be understood, however, that the drawings and detailed description thereto are not intended to limit the invention to the particular form disclosed, but on the contrary, the intention is to cover all modifications, equivalents and alternatives falling within the spirit and scope of the present invention as defined by the appended claims.
The following description generally relates to systems and methods for treating hydrocarbons in the formations. Such formations may be treated to yield hydrocarbon products, hydrogen, and other products.
“API gravity” refers to API gravity at 15.5° C. (60° F.). API gravity is as determined by ASTM Method D6822 or ASTM Method D1298.
“ASTM” refers to American Standard Testing and Materials.
In the context of reduced heat output heating systems, apparatus, and methods, the term “automatically” means such systems, apparatus, and methods function in a certain way without the use of external control (for example, external controllers such as a controller with a temperature sensor and a feedback loop, PID controller, or predictive controller).
“Asphalt/bitumen” refers to a semi-solid, viscous material soluble in carbon disulfide. Asphalt/bitumen may be obtained from refining operations or produced from subsurface formations.
“Carbon number” refers to the number of carbon atoms in a molecule. A hydrocarbon fluid may include various hydrocarbons with different carbon numbers. The hydrocarbon fluid may be described by a carbon number distribution. Carbon numbers and/or carbon number distributions may be determined by true boiling point distribution and/or gas-liquid chromatography.
“Condensable hydrocarbons” are hydrocarbons that condense at 25° C. and one atmosphere absolute pressure. Condensable hydrocarbons may include a mixture of hydrocarbons having carbon numbers greater than 4. “Non-condensable hydrocarbons” are hydrocarbons that do not condense at 25° C. and one atmosphere absolute pressure. Non-condensable hydrocarbons may include hydrocarbons having carbon numbers less than 5.
A “fluid” may be, but is not limited to, a gas, a liquid, an emulsion, a slurry, and/or a stream of solid particles that has flow characteristics similar to liquid flow.
A “formation” includes one or more hydrocarbon containing layers, one or more non-hydrocarbon layers, an overburden, and/or an underburden. “Hydrocarbon layers” refer to layers in the formation that contain hydrocarbons. The hydrocarbon layers may contain non-hydrocarbon material and hydrocarbon material. The “overburden” and/or the “underburden” include one or more different types of impermeable materials. For example, the overburden and/or underburden may include rock, shale, mudstone, or wet/tight carbonate. In some embodiments of in situ heat treatment processes, the overburden and/or the underburden may include a hydrocarbon containing layer or hydrocarbon containing layers that are relatively impermeable and are not subjected to temperatures during in situ heat treatment processing that result in significant characteristic changes of the hydrocarbon containing layers of the overburden and/or the underburden. For example, the underburden may contain shale or mudstone, but the underburden is not allowed to heat to pyrolysis temperatures during the in situ heat treatment process. In some cases, the overburden and/or the underburden may be somewhat permeable.
“Formation fluids” refer to fluids present in a formation and may include pyrolyzation fluid, synthesis gas, mobilized hydrocarbons, and water (steam). Formation fluids may include hydrocarbon fluids as well as non-hydrocarbon fluids. The term “mobilized fluid” refers to fluids in a hydrocarbon containing formation that are able to flow as a result of thermal treatment of the formation. “Produced fluids” refer to fluids removed from the formation.
A “heat source” is any system for providing heat to at least a portion of a formation substantially by conductive and/or radiative heat transfer. For example, a heat source may include electrically conducting materials and/or electric heaters such as an insulated conductor, an elongated member, and/or a conductor disposed in a conduit. A heat source may also include systems that generate heat by burning a fuel external to or in a formation. The systems may be surface burners, downhole gas burners, flameless distributed combustors, and natural distributed combustors. In some embodiments, heat provided to or generated in one or more heat sources may be supplied by other sources of energy. The other sources of energy may directly heat a formation, or the energy may be applied to a transfer medium that directly or indirectly heats the formation. It is to be understood that one or more heat sources that are applying heat to a formation may use different sources of energy. Thus, for example, for a given formation some heat sources may supply heat from electrically conducting materials, electric resistance heaters, some heat sources may provide heat from combustion, and some heat sources may provide heat from one or more other energy sources (for example, chemical reactions, solar energy, wind energy, biomass, or other sources of renewable energy). A chemical reaction may include an exothermic reaction (for example, an oxidation reaction). A heat source may also include an electrically conducting material and/or a heater that provides heat to a zone proximate and/or surrounding a heating location such as a heater well.
A “heater” is any system or heat source for generating heat in a well or a near wellbore region. Heaters may be, but are not limited to, electric heaters, burners, combustors that react with material in or produced from a formation, and/or combinations thereof.
“Heavy hydrocarbons” are viscous hydrocarbon fluids. Heavy hydrocarbons may include highly viscous hydrocarbon fluids such as heavy oil, tar, and/or asphalt. Heavy hydrocarbons may include carbon and hydrogen, as well as smaller concentrations of sulfur, oxygen, and nitrogen. Additional elements may also be present in heavy hydrocarbons in trace amounts. Heavy hydrocarbons may be classified by API gravity. Heavy hydrocarbons generally have an API gravity below about 20°. Heavy oil, for example, generally has an API gravity of about 10-20°, whereas tar generally has an API gravity below about 10°. The viscosity of heavy hydrocarbons is generally greater than about 100 centipoise at 15° C. Heavy hydrocarbons may include aromatics or other complex ring hydrocarbons.
Heavy hydrocarbons may be found in a relatively permeable formation. The relatively permeable formation may include heavy hydrocarbons entrained in, for example, sand or carbonate. “Relatively permeable” is defined, with respect to formations or portions thereof, as an average permeability of 10 millidarcy or more (for example, 10 or 100 millidarcy). “Relatively low permeability” is defined, with respect to formations or portions thereof, as an average permeability of less than about 10 millidarcy. One darcy is equal to about 0.99 square micrometers. An impermeable layer generally has a permeability of less than about 0.1 millidarcy.
Certain types of formations that include heavy hydrocarbons may also include, but are not limited to, natural mineral waxes, or natural asphaltites. “Natural mineral waxes” typically occur in substantially tubular veins that may be several meters wide, several kilometers long, and hundreds of meters deep. “Natural asphaltites” include solid hydrocarbons of an aromatic composition and typically occur in large veins. In situ recovery of hydrocarbons from formations such as natural mineral waxes and natural asphaltites may include melting to form liquid hydrocarbons and/or solution mining of hydrocarbons from the formations.
“Hydrocarbons” are generally defined as molecules formed primarily by carbon and hydrogen atoms. Hydrocarbons may also include other elements such as, but not limited to, halogens, metallic elements, nitrogen, oxygen, and/or sulfur. Hydrocarbons may be, but are not limited to, kerogen, bitumen, pyrobitumen, oils, natural mineral waxes, and asphaltites. Hydrocarbons may be located in or adjacent to mineral matrices in the earth. Matrices may include, but are not limited to, sedimentary rock, sands, silicilytes, carbonates, diatomites, and other porous media. “Hydrocarbon fluids” are fluids that include hydrocarbons. Hydrocarbon fluids may include, entrain, or be entrained in non-hydrocarbon fluids such as hydrogen, nitrogen, carbon monoxide, carbon dioxide, hydrogen sulfide, water, and ammonia.
An “in situ conversion process” refers to a process of heating a hydrocarbon containing formation from heat sources to raise the temperature of at least a portion of the formation above a pyrolysis temperature so that pyrolyzation fluid is produced in the formation.
An “in situ heat treatment process” refers to a process of heating a hydrocarbon containing formation with heat sources to raise the temperature of at least a portion of the formation above a temperature that results in mobilized fluid, visbreaking, and/or pyrolysis of hydrocarbon containing material so that mobilized fluids, visbroken fluids, and/or pyrolyzation fluids are produced in the formation.
“Insulated conductor” refers to any elongated material that is able to conduct electricity and that is covered, in whole or in part, by an electrically insulating material.
“Kerogen” is a solid, insoluble hydrocarbon that has been converted by natural degradation and that principally contains carbon, hydrogen, nitrogen, oxygen, and sulfur. Coal and oil shale are typical examples of materials that contain kerogen. “Bitumen” is a non-crystalline solid or viscous hydrocarbon material that is substantially soluble in carbon disulfide. “Oil” is a fluid containing a mixture of condensable hydrocarbons.
“Perforations” include openings, slits, apertures, or holes in a wall of a conduit, tubular, pipe or other flow pathway that allow flow into or out of the conduit, tubular, pipe or other flow pathway.
“Pyrolysis” is the breaking of chemical bonds due to the application of heat. For example, pyrolysis may include transforming a compound into one or more other substances by heat alone. Heat may be transferred to a section of the formation to cause pyrolysis.
“Pyrolyzation fluids” or “pyrolysis products” refers to fluid produced substantially during pyrolysis of hydrocarbons. Fluid produced by pyrolysis reactions may mix with other fluids in a formation. The mixture would be considered pyrolyzation fluid or pyrolyzation product. As used herein, “pyrolysis zone” refers to a volume of a formation (for example, a relatively permeable formation such as a tar sands formation) that is reacted or reacting to form a pyrolyzation fluid.
“Rich layers” in a hydrocarbon containing formation are relatively thin layers (typically about 0.2 m to about 0.5 m thick). Rich layers generally have a richness of about 0.150 L/kg or greater. Some rich layers have a richness of about 0.170 L/kg or greater, of about 0.190 L/kg or greater, or of about 0.210 L/kg or greater. Lean layers of the formation have a richness of about 0.100 L/kg or less and are generally thicker than rich layers. The richness and locations of layers are determined, for example, by coring and subsequent Fischer assay of the core, density or neutron logging, or other logging methods. Rich layers may have a lower initial thermal conductivity than other layers of the formation. Typically, rich layers have a thermal conductivity 1.5 times to 3 times lower than the thermal conductivity of lean layers. In addition, rich layers have a higher thermal expansion coefficient than lean layers of the formation.
“Superposition of heat” refers to providing heat from two or more heat sources to a selected section of a formation such that the temperature of the formation at least at one location between the heat sources is influenced by the heat sources.
“Synthesis gas” is a mixture including hydrogen and carbon monoxide. Additional components of synthesis gas may include water, carbon dioxide, nitrogen, methane, and other gases. Synthesis gas may be generated by a variety of processes and feedstocks. Synthesis gas may be used for synthesizing a wide range of compounds.
“Tar” is a viscous hydrocarbon that generally has a viscosity greater than about 10,000 centipoise at 15° C. The specific gravity of tar generally is greater than 1.000. Tar may have an API gravity less than 10°.
A “tar sands formation” is a formation in which hydrocarbons are predominantly present in the form of heavy hydrocarbons and/or tar entrained in a mineral grain framework or other host lithology (for example, sand or carbonate). Examples of tar sands formations include formations such as the Athabasca formation, the Grosmont formation, and the Peace River formation, all three in Alberta, Canada; and the Faja formation in the Orinoco belt in Venezuela.
“Temperature limited heater” generally refers to a heater that regulates heat output (for example, reduces heat output) above a specified temperature without the use of external controls such as temperature controllers, power regulators, rectifiers, or other devices. Temperature limited heaters may be AC (alternating current) or modulated (for example, “chopped”) DC (direct current) powered electrical resistance heaters.
“Thickness” of a layer refers to the thickness of a cross section of the layer, wherein the cross section is normal to a face of the layer.
A “u-shaped wellbore” refers to a wellbore that extends from a first opening in the formation, through at least a portion of the formation, and out through a second opening in the formation. In this context, the wellbore may be only roughly in the shape of a “v” or “u”, with the understanding that the “legs” of the “u” do not need to be parallel to each other, or perpendicular to the “bottom” of the “u” for the wellbore to be considered “u-shaped”.
“Upgrade” refers to increasing the quality of hydrocarbons. For example, upgrading heavy hydrocarbons may result in an increase in the API gravity of the heavy hydrocarbons.
“Visbreaking” refers to the untangling of molecules in fluid during heat treatment and/or to the breaking of large molecules into smaller molecules during heat treatment, which results in a reduction of the viscosity of the fluid.
“Viscosity” refers to kinematic viscosity at 40° C. unless otherwise specified. Viscosity is as determined by ASTM Method D445.
“Wax” refers to a low melting organic mixture, or a compound of high molecular weight that is a solid at lower temperatures and a liquid at higher temperatures, and when in solid form can form a barrier to water. Examples of waxes include animal waxes, vegetable waxes, mineral waxes, petroleum waxes, and synthetic waxes.
The term “wellbore” refers to a hole in a formation made by drilling or insertion of a conduit into the formation. A wellbore may have a substantially circular cross section, or another cross-sectional shape. As used herein, the terms “well” and “opening,” when referring to an opening in the formation may be used interchangeably with the term “wellbore.”
A formation may be treated in various ways to produce many different products. Different stages or processes may be used to treat the formation during an in situ heat treatment process. In some embodiments, one or more sections of the formation are solution mined to remove soluble minerals from the sections. Solution mining minerals may be performed before, during, and/or after the in situ heat treatment process. In some embodiments, the average temperature of one or more sections being solution mined may be maintained below about 120° C.
In some embodiments, one or more sections of the formation are heated to remove water from the sections and/or to remove methane and other volatile hydrocarbons from the sections. In some embodiments, the average temperature may be raised from ambient temperature to temperatures below about 220° C. during removal of water and volatile hydrocarbons.
In some embodiments, one or more sections of the formation are heated to temperatures that allow for movement and/or visbreaking of hydrocarbons in the formation. In some embodiments, the average temperature of one or more sections of the formation are raised to mobilization temperatures of hydrocarbons in the sections (for example, to temperatures ranging from 100° C. to 250° C., from 120° C. to 240° C., or from 150° C. to 230° C.).
In some embodiments, one or more sections are heated to temperatures that allow for pyrolysis reactions in the formation. In some embodiments, the average temperature of one or more sections of the formation may be raised to pyrolysis temperatures of hydrocarbons in the sections (for example, temperatures ranging from 230° C. to 900° C., from 240° C. to 400° C. or from 250° C. to 350° C.).
Heating the hydrocarbon containing formation with a plurality of heat sources may establish thermal gradients around the heat sources that raise the temperature of hydrocarbons in the formation to desired temperatures at desired heating rates. The rate of temperature increase through the mobilization temperature range and/or the pyrolysis temperature range for desired products may affect the quality and quantity of the formation fluids produced from the hydrocarbon containing formation. Slowly raising the temperature of the formation through the mobilization temperature range and/or pyrolysis temperature range may allow for the production of high quality, high API gravity hydrocarbons from the formation. Slowly raising the temperature of the formation through the mobilization temperature range and/or pyrolysis temperature range may allow for the removal of a large amount of the hydrocarbons present in the formation as hydrocarbon product.
In some in situ heat treatment embodiments, a portion of the formation is heated to a desired temperature instead of slowly raising the temperature through a temperature range. In some embodiments, the desired temperature is 300° C., 325° C., or 350° C. Other temperatures may be selected as the desired temperature.
Superposition of heat from heat sources allows the desired temperature to be relatively quickly and efficiently established in the formation. Energy input into the formation from the heat sources may be adjusted to maintain the temperature in the formation substantially at a desired temperature.
Mobilization and/or pyrolysis products may be produced from the formation through production wells. In some embodiments, the average temperature of one or more sections is raised to mobilization temperatures and hydrocarbons are produced from the production wells. The average temperature of one or more of the sections may be raised to pyrolysis temperatures after production due to mobilization decreases below a selected value. In some embodiments, the average temperature of one or more sections may be raised to pyrolysis temperatures without significant production before reaching pyrolysis temperatures. Formation fluids including pyrolysis products may be produced through the production wells.
In some embodiments, the average temperature of one or more sections may be raised to temperatures sufficient to allow synthesis gas production after mobilization and/or pyrolysis. In some embodiments, hydrocarbons may be raised to temperatures sufficient to allow synthesis gas production without significant production before reaching the temperatures sufficient to allow synthesis gas production. For example, synthesis gas may be produced in a temperature range from about 400° C. to about 1200° C., about 500° C. to about 1100° C., or about 550° C. to about 1000° C. A synthesis gas generating fluid (for example, steam and/or water) may be introduced into the sections to generate synthesis gas. Synthesis gas may be produced from production wells.
Solution mining, removal of volatile hydrocarbons and water, mobilizing hydrocarbons, pyrolyzing hydrocarbons, generating synthesis gas, and/or other processes may be performed during the in situ heat treatment process. In some embodiments, some processes may be performed after the in situ heat treatment process. Such processes may include, but are not limited to, recovering heat from treated sections, storing fluids (for example, water and/or hydrocarbons) in previously treated sections, and/or sequestering carbon dioxide in previously treated sections.
Heat sources 192 are placed in at least a portion of the formation. Heat sources 192 may include heaters such as insulated conductors, conductor-in-conduit heaters, surface burners, flameless distributed combustors, and/or natural distributed combustors. Heat sources 192 may also include other types of heaters. Heat sources 192 provide heat to at least a portion of the formation to heat hydrocarbons in the formation. Energy may be supplied to heat sources 192 through supply lines 194. Supply lines 194 may be structurally different depending on the type of heat source or heat sources used to heat the formation. Supply lines 194 for heat sources may transmit electricity for electric heaters, may transport fuel for combustors, or may transport heat exchange fluid that is circulated in the formation. In some embodiments, electricity for an in situ heat treatment process may be provided by a nuclear power plant or nuclear power plants. The use of nuclear power may allow for reduction or elimination of carbon dioxide emissions from the in situ heat treatment process.
When the formation is heated, the heat input into the formation may cause expansion of the formation and geomechanical motion. The heat sources may be turned on before, at the same time, or during a dewatering process. Computer simulations may model formation response to heating. The computer simulations may be used to develop a pattern and time sequence for activating heat sources in the formation so that geomechanical motion of the formation does not adversely affect the functionality of heat sources, production wells, and other equipment in the formation.
Heating the formation may cause an increase in permeability and/or porosity of the formation. Increases in permeability and/or porosity may result from a reduction of mass in the formation due to vaporization and removal of water, removal of hydrocarbons, and/or creation of fractures. Fluid may flow more easily in the heated portion of the formation because of the increased permeability and/or porosity of the formation. Fluid in the heated portion of the formation may move a considerable distance through the formation because of the increased permeability and/or porosity. The considerable distance may be over 1000 m depending on various factors, such as permeability of the formation, properties of the fluid, temperature of the formation, and pressure gradient allowing movement of the fluid. The ability of fluid to travel considerable distance in the formation allows production wells 196 to be spaced relatively far apart in the formation.
Production wells 196 are used to remove formation fluid from the formation. In some embodiments, production well 196 includes a heat source. The heat source in the production well may heat one or more portions of the formation at or near the production well. In some in situ heat treatment process embodiments, the amount of heat supplied to the formation from the production well per meter of the production well is less than the amount of heat applied to the formation from a heat source that heats the formation per meter of the heat source. Heat applied to the formation from the production well may increase formation permeability adjacent to the production well by vaporizing and removing liquid phase fluid adjacent to the production well and/or by increasing the permeability of the formation adjacent to the production well by formation of macro and/or micro fractures.
More than one heat source may be positioned in the production well. A heat source in a lower portion of the production well may be turned off when superposition of heat from adjacent heat sources heats the formation sufficiently to counteract benefits provided by heating the formation with the production well. In some embodiments, the heat source in an upper portion of the production well may remain on after the heat source in the lower portion of the production well is deactivated. The heat source in the upper portion of the well may inhibit condensation and reflux of formation fluid.
In some embodiments, the heat source in production well 196 allows for vapor phase removal of formation fluids from the formation. Providing heating at or through the production well may: (1) inhibit condensation and/or refluxing of production fluid when such production fluid is moving in the production well proximate the overburden, (2) increase heat input into the formation, (3) increase production rate from the production well as compared to a production well without a heat source, (4) inhibit condensation of high carbon number compounds (C6 hydrocarbons and above) in the production well, and/or (5) increase formation permeability at or proximate the production well.
Subsurface pressure in the formation may correspond to the fluid pressure generated in the formation. As temperatures in the heated portion of the formation increase, the pressure in the heated portion may increase as a result of thermal expansion of in situ fluids, increased fluid generation and vaporization of water. Controlling rate of fluid removal from the formation may allow for control of pressure in the formation. Pressure in the formation may be determined at a number of different locations, such as near or at production wells, near or at heat sources, or at monitor wells.
In some hydrocarbon containing formations, production of hydrocarbons from the formation is inhibited until at least some hydrocarbons in the formation have been mobilized and/or pyrolyzed. Formation fluid may be produced from the formation when the formation fluid is of a selected quality. In some embodiments, the selected quality includes an API gravity of at least about 20°, 30°, or 40°. Inhibiting production until at least some hydrocarbons are mobilized and/or pyrolyzed may increase conversion of heavy hydrocarbons to light hydrocarbons. Inhibiting initial production may minimize the production of heavy hydrocarbons from the formation. Production of substantial amounts of heavy hydrocarbons may require expensive equipment and/or reduce the life of production equipment.
In some hydrocarbon containing formations, hydrocarbons in the formation may be heated to mobilization and/or pyrolysis temperatures before substantial permeability has been generated in the heated portion of the formation. An initial lack of permeability may inhibit the transport of generated fluids to production wells 196. During initial heating, fluid pressure in the formation may increase proximate heat sources 192. The increased fluid pressure may be released, monitored, altered, and/or controlled through one or more heat sources 192. For example, selected heat sources 192 or separate pressure relief wells may include pressure relief valves that allow for removal of some fluid from the formation.
In some embodiments, pressure generated by expansion of mobilized fluids, pyrolysis fluids or other fluids generated in the formation may be allowed to increase although an open path to production wells 196 or any other pressure sink may not yet exist in the formation. The fluid pressure may be allowed to increase towards a lithostatic pressure. Fractures in the hydrocarbon containing formation may form when the fluid approaches the lithostatic pressure. For example, fractures may form from heat sources 192 to production wells 196 in the heated portion of the formation. The generation of fractures in the heated portion may relieve some of the pressure in the portion. Pressure in the formation may have to be maintained below a selected pressure to inhibit unwanted production, fracturing of the overburden or underburden, and/or coking of hydrocarbons in the formation.
After mobilization and/or pyrolysis temperatures are reached and production from the formation is allowed, pressure in the formation may be varied to alter and/or control a composition of formation fluid produced, to control a percentage of condensable fluid as compared to non-condensable fluid in the formation fluid, and/or to control an API gravity of formation fluid being produced. For example, decreasing pressure may result in production of a larger condensable fluid component. The condensable fluid component may contain a larger percentage of olefins.
In some in situ heat treatment process embodiments, pressure in the formation may be maintained high enough to promote production of formation fluid with an API gravity of greater than 20°. Maintaining increased pressure in the formation may inhibit formation subsidence during in situ heat treatment. Maintaining increased pressure may reduce or eliminate the need to compress formation fluids at the surface to transport the fluids in collection conduits to treatment facilities.
Maintaining increased pressure in a heated portion of the formation may surprisingly allow for production of large quantities of hydrocarbons of increased quality and of relatively low molecular weight. Pressure may be maintained so that formation fluid produced has a minimal amount of compounds above a selected carbon number. The selected carbon number may be at most 25, at most 20, at most 12, or at most 8. Some high carbon number compounds may be entrained in vapor in the formation and may be removed from the formation with the vapor. Maintaining increased pressure in the formation may inhibit entrainment of high carbon number compounds and/or multi-ring hydrocarbon compounds in the vapor. High carbon number compounds and/or multi-ring hydrocarbon compounds may remain in a liquid phase in the formation for significant time periods. The significant time periods may provide sufficient time for the compounds to pyrolyze to form lower carbon number compounds.
Generation of relatively low molecular weight hydrocarbons is believed to be due, in part, to autogenous generation and reaction of hydrogen in a portion of the hydrocarbon containing formation. For example, maintaining an increased pressure may force hydrogen generated during pyrolysis into the liquid phase within the formation. Heating the portion to a temperature in a pyrolysis temperature range may pyrolyze hydrocarbons in the formation to generate liquid phase pyrolyzation fluids. The generated liquid phase pyrolyzation fluids components may include double bonds and/or radicals. Hydrogen (H2) in the liquid phase may reduce double bonds of the generated pyrolyzation fluids, thereby reducing a potential for polymerization or formation of long chain compounds from the generated pyrolyzation fluids. In addition, H2 may also neutralize radicals in the generated pyrolyzation fluids. H2 in the liquid phase may inhibit the generated pyrolyzation fluids from reacting with each other and/or with other compounds in the formation.
Formation fluid produced from production wells 196 may be transported through collection piping 198 to treatment facilities 200. Formation fluids may also be produced from heat sources 192. For example, fluid may be produced from heat sources 192 to control pressure in the formation adjacent to the heat sources. Fluid produced from heat sources 192 may be transported through tubing or piping to collection piping 198 or the produced fluid may be transported through tubing or piping directly to treatment facilities 200. Treatment facilities 200 may include separation units, reaction units, upgrading units, fuel cells, turbines, storage vessels, and/or other systems and units for processing produced formation fluids. The treatment facilities may form transportation fuel from at least a portion of the hydrocarbons produced from the formation. In some embodiments, the transportation fuel may be jet fuel, such as JP-8.
In some in situ heat treatment process embodiments, a circulation system is used to heat the formation. Using the circulation system for in situ heat treatment of a hydrocarbon containing formation may reduce energy costs for treating the formation, reduce emissions from the treatment process, and/or facilitate heating system installation. In certain embodiments, the circulation system is a closed loop circulation system. The system may be used to heat hydrocarbons that are relatively deep in the ground and that are in formations that are relatively large in extent. In some embodiments, the hydrocarbons may be 100 m, 200 m, 300 m or more below the surface. The circulation system may also be used to heat hydrocarbons that are shallower in the ground. The hydrocarbons may be in formations that extend lengthwise up to 1000 m, 3000 m, 5000 m, or more. The heaters of the circulation system may be positioned relative to adjacent heaters such that superposition of heat between heaters of the circulation system allows the temperature of the formation to be raised at least above the boiling point of aqueous formation fluid in the formation.
In some embodiments, heaters are formed in the formation by drilling a first wellbore and then drilling a second wellbore that connects with the first wellbore. Piping may be positioned in the u-shaped wellbore to form u-shaped heaters. Heaters are connected to a heat transfer fluid circulation system by piping. In some embodiments, the heaters are positioned in triangular patterns. In some embodiments, other regular or irregular patterns are used. Production wells and/or injection wells may also be located in the formation. The production wells and/or the injection wells may have long, substantially horizontal sections similar to the heating portions of heaters, or the production wells and/or injection wells may be otherwise oriented (for example, the wells may be vertically oriented wells, or wells that include one or more slanted portions).
As depicted in
After exiting formation 212, the heat transfer fluid passes through first heat exchanger 206 and second heat exchanger 208 to fluid movers 210. First heat exchanger 206 transfers heat between heat transfer fluid exiting formation 212 and heat transfer fluid exiting fluid movers 210 to raise the temperature of the heat transfer fluid that enters heat supply 204 and reduce the temperature of the fluid exiting formation 212. Second heat exchanger 208 further reduces the temperature of the heat transfer fluid. In some embodiments, second heat exchanger 208 includes or is a storage tank for the heat transfer fluid. Heat transfer fluid passes from second heat exchanger 208 to fluid movers 210. Fluid movers 210 may be located before heat supply 204 so that the fluid movers do not have to operate at a high temperature.
In an embodiment, the heat transfer fluid is carbon dioxide. Heat supply 204 is a furnace that heats the heat transfer fluid to a temperature in a range from about 700° C. to about 920° C., from about 770° C. to about 870° C., or from about 800° C. to about 850° C. In an embodiment, heat supply 204 heats the heat transfer fluid to a temperature of about 820° C. The heat transfer fluid flows from heat supply 204 to heaters 201. Heat transfers from heaters 201 to formation 212 adjacent to the heaters. The temperature of the heat transfer fluid exiting formation 212 may be in a range from about 350° C. to about 580° C., from about 400° C. to about 530° C., or from about 450° C. to about 500° C. In an embodiment, the temperature of the heat transfer fluid exiting formation 212 is about 480° C. The metallurgy of the piping used to form heat transfer fluid circulation system 202 may be varied to significantly reduce costs of the piping. High temperature steel may be used from heat supply 204 to a point where the temperature is sufficiently low so that less expensive steel can be used from that point to first heat exchanger 206. Several different steel grades may be used to form the piping of heat transfer fluid circulation system 202.
In some embodiments, vertical, slanted, or L-shaped wellbores are used instead of u-shaped wellbores (for example, wellbores that have an entrance at a first location and an exit at another location).
In some embodiments, portions of wellbore 222 adjacent to overburden 218 are larger than portions of the wellbore adjacent to hydrocarbon containing layer 220. Having a larger opening adjacent to the overburden may allow for accommodation of insulation used to insulate inlet conduit 214 and/or outlet conduit 216. Some heat loss to the overburden from the return flow may not affect the efficiency significantly, especially when the heat transfer fluid is molten salt or another fluid that needs to be heated to remain a liquid. The heated overburden adjacent to heater 201 may maintain the heat transfer fluid as a liquid for a significant time should circulation of heat transfer fluid stop. Having some allowance for heat transfer to overburden 218 may eliminate the need for expensive insulation systems between outlet conduit 216 and the overburden. In some embodiments, insulative cement is used between overburden 218 and outlet conduit 216.
For vertical, slanted, or L-shaped heaters, the wellbores may be drilled longer than needed to accommodate non-energized heaters (for example, installed but inactive heaters). Thermal expansion of the heaters after energization may cause portions of the heaters to move into the extra length of the wellbores designed to accommodate the thermal expansion of the heaters. For L-shaped heaters, remaining drilling fluid and/or formation fluid in the wellbore may facilitate movement of the heater deeper into the wellbore as the heater expands during preheating and/or heating with heat transfer fluid.
For vertical or slanted wellbores, the wellbores may be drilled deeper than needed to accommodate the non-energized heaters. When the heater is preheated and/or heated with the heat transfer fluid, the heater may expand into the extra depth of the wellbore. In some embodiments, an expansion sleeve may be attached at the end of the heater to ensure available space for thermal expansion in case of unstable boreholes.
Outlet conduit 216 may include insulating sleeve 224′. Insulating sleeve 224′ may end near the boundary between overburden 218 and hydrocarbon layer 220. In some embodiments, insulating sleeve 224′ is installed using a coiled tubing rig. An upper first portion of insulating sleeve 224′ may be secured to outlet conduit 216 above or near wellhead 226 by weld 228. Heater 201 may be supported in wellhead 226 by a coupling between the outer support member of insulating sleeve 224′ and the wellhead. The outer support member of insulating sleeve 224′ may have sufficient strength to support heater 201.
In some embodiments, insulating sleeve 224′ includes a second portion (insulating sleeve portion 224″) that is separate and lower than the first portion of insulating sleeve 224′. Insulating sleeve portion 224″ may be secured to outlet conduit 216 by welds 228 or other types of seals that can withstand high temperatures below packer 230. Welds 228 between insulating sleeve portion 224″ and outlet conduit 216 may inhibit formation fluid from passing between the insulating sleeve and the outlet conduit. During heating, differential thermal expansion between the cooler outer surface and the hotter inner surface of insulating sleeve 224′ may cause separation between the first portion of the insulating sleeve and the second portion of the insulating sleeve (insulating sleeve portion 224″). This separation may occur adjacent to the overburden portion of heater 201 above packer 230. Insulating cement between casing 238 and the formation may further inhibit heat loss to the formation and improve the overall energy efficiency of the system.
Packer 230 may be a polished bore receptacle. Packer 230 may be fixed to casing 238 of wellbore 222. In some embodiments, packer 230 is 1000 m or more below the surface. Packer 230 may be located at a depth above 1000 m, if desired. Packer 230 may inhibit formation fluid from flowing from the heated portion of the formation up the wellbore to wellhead 226. Packer 230 may allow movement of insulating sleeve portion 224″ downwards to accommodate thermal expansion of heater 201. In some embodiments, wellhead 226 includes fixed seal 232. Fixed seal 232 may be a second seal that inhibits formation fluid from reaching the surface through wellbore 222 of heater 201.
In some embodiments, the heater includes a flow switcher. The flow switcher may allow the heat transfer fluid from the circulation system to flow down through the overburden in the inlet conduit of the heater. The return flow from the heater may flow upwards through the annular region between the inlet conduit and the outlet conduit. The flow switcher may change the downward flow from the inlet conduit to the annular region between the outlet conduit and the inlet conduit. The flow switcher may also change the upward flow from the inlet conduit to the annular region. The use of the flow switcher may allow the heater to operate at a higher temperature adjacent to the treatment area without increasing the initial temperature of the heat transfer fluid provided to the heaters.
For vertical, slanted, or L-shaped heaters where the flow of heat transfer fluid is directed down the inlet conduit and returns through the annular region between the inlet conduit and the outlet conduit, a temperature gradient may form in the heater with the hottest portion being located at a distal end of the heater. For L-shaped heaters, horizontal portions of a set of first heaters may be alternated with the horizontal portions of a second set of heaters. The hottest portions used to heat the formation of the first set of heaters may be adjacent to the coldest portions used to heat the formation of the second set of heaters, while the hottest portions used to heat the formation of the second set of heaters are adjacent to the coldest portions used to heat the formation of the first set of heaters. For vertical or slanted heaters, flow switchers in selected heaters may allow the heaters to be arranged with the hottest portions used to heat the formation of first heaters adjacent to coldest portions used to heat the formation of second heaters. Having hottest portions used to heat the formation of the first set of heaters adjacent to coldest portions used to heat the formation of the second set of heaters may allow for more uniform heating of the formation.
In some embodiments, solar salt (for example, a salt containing 60 wt % NaNO3 and 40 wt % KNO3) is used as the heat transfer fluid in the circulated fluid system. Solar salt may have a melting point of about 230° C. and an upper working temperature limit of about 565° C. In some embodiments, LiNO3 (for example, between about 10% by weight and about 30% by weight LiNO3) may be added to the solar salt to produce tertiary salt mixtures with wider operating temperature ranges and lower melting temperatures with only a slight decrease in the maximum working temperature as compared to solar salt. The lower melting temperature of the tertiary salt mixtures may decrease the preheating requirements and allow the use of pressurized water and/or pressurized brine as a heat transfer fluid for preheating the piping of the circulation system. The corrosion rates of the metal of the heaters due to the tertiary salt compositions at 550° C. is comparable to the corrosion rate of the metal of the heaters due to solar salt at 565° C. TABLE 1 shows melting points and upper limits for solar salt and tertiary salt mixtures. Aqueous solutions of tertiary salt mixtures may transition into a molten salt upon removal of water without solidification, thus allowing the molten salt to be provided and/or stored as aqueous solutions.
Using molten salts as a heat transfer fluid for in situ heat treatment process has many advantages. Many molten salts will react with certain hydrocarbons, thus, if circulating molten salts are used to heat a portion of a treatment area, a leak in the system which allows molten salts to contact subsurface hydrocarbons may cause problems. Reaction of molten salts with hydrocarbons may disrupt heat transfer systems, decrease permeability in the treatment area, decrease hydrocarbon production, and/or impede the flow of hydrocarbons through at least a portion of the treatment area being heated by circulating molten salt heaters.
When a leak forms in one or more portions of a conduit of a circulating molten salt system, coke may form and/or infiltrate in the conduit adjacent to the leak. Coke deposits in one or more conduits in a heater may lead to several problems (for example, hot spots and/or heater failure). In some embodiments, an oxidizing fluid may be provided to one or more portions of the conduit. Oxidizing fluid may include, for example, air. Oxidizing fluid may oxidize any coke which has formed in the conduit.
In some embodiments, oxidizing fluid may be mixed with the molten salt before the molten salt is circulated through the heater in the formation. Mixing air with the molten salt may inhibit any significant coke formation in the conduits. As shown, heater 201 may be coupled to heat transfer fluid circulation system 202 and may include inlet conduit 214, and outlet conduit 216. Heat transfer fluid circulation system 202 may provide heat transfer fluid mixed with oxidizing fluid to inlet conduit 214 of L-shaped heater 201. In some embodiments, oxidizing fluid may be provided to one or more conduits of a heater intermittently and/or as needed.
In some embodiments, liner 240 (see
As shown in
In some embodiments, electrical conductivity may be used to assess the inception, existence, and/or location of leaks in the heater using heat transfer fluids such as molten salts. A resistance across one or more conduits of, for example, a conduit-in-conduit heater may be monitored for any changes. Changes in the monitored resistance may indicate the inception and/or worsening of a leak in the conduit. The conduits forming the conduit-in-conduit heater may include a void in the walls forming the conduits. The void in the walls forming the conduit may include a thermal insulation material positioned in the void. If a breach forms in the conduit walls, heat transfer fluid may enter through the breach leaking through to the other side. Some heat transfer fluids, for example molten salts, leaking through the breach in the conduit may conduct electricity creating a short across the conduit wall. The electrical short created by the leaking molten salt may then modify the measured resistance across the conduit wall in which the breach has occurred.
In some embodiments, the electrical resistance of at least one of the conduits of the conduit-in-conduit heaters may be assessed. A presence of a leak in at least one of the conduits may be assessed based on the assessed resistance. The electrical resistance may be assessed intermittently or on a continuous basis. The electrical resistance may be assessed for either one or both conduits of the conduit-in-conduit heater.
In some embodiments, a location of a breach in the conduit may be assessed. The location may be assessed due to the fact that the relationship between the electrical resistance and the depth at which the breach has occurred is very linear as is demonstrated in
In some embodiments, a gas in combination with, for example, a gas detection system may be used to detect a breach, and subsequent leaks, in one or more conduits of a conduit-in-conduit heater. One or more gases may be dissolved in the heat transfer fluid, for example a molten salt. The gas may be dissolved in the molten salt before the molten salt is transferred to the conduit-in-conduit heater (for example, in a storage tank used to store the molten salt). The gas may be dissolved in the molten salt as the molten salt is injected in the heater. The dissolved gas may circulate through the heater along with the molten salt.
In some embodiments, one or more of the gases may include an inert gas (for example, nitrogen, argon, helium, or mixtures thereof). In some embodiments, the gas detection system may include a pressure transducer or a gas analyzer. A breach in a conduit of the heater may result in a leak of at least some of the circulating molten salts in the annulus space of the conduit. Once the molten salt leaks in the annular space of the conduit, at least some of the gas dissolved in the molten salt may be released from the molten salt in the annular space of the conduit. The annular space may be under reduced pressure (for example, in order to provide more insulation value) and reduced temperature. The reduced pressure of the annular space may further facilitate the release of the dissolved gas from any molten salts which have leaked in the annular space. Table 2 shows the solubility of several inert gases including helium, argon, and nitrogen in molten nitrates. Solubility of the gas in the salt may generally scale substantially linearly with partial pressure according to Henry's Law.
The gas released from the heater may be detected by the gas detection system. The gas detection system may be coupled to one or more openings in fluid communication with the annular space of the conduit. Heaters currently in use may have preexisting openings which may be adapted to accommodate the gas detection system. Heaters currently in use may be retrofitted for the currently described leak detection system.
In some embodiments, the gas detection system may be coupled to a plurality of heaters. Once a heater has formed a breach in one of the conduits, the heater in question may be identified by sequentially isolating each heater coupled to the gas detection system. In some embodiments, a leak detection system based upon detection of gases in annular spaces may not be able to assist in assessing the location of the breach (as the electrical resistance leak detection system may allow). In some embodiments, a leak detection system based upon detection of gases in annular spaces may not be able to assist in assessing the formation of breaches in one or more conduits along any horizontal portions.
The use of circulating molten salts to heat underground hydrocarbon containing formations has many advantages relative to other known methods of heating a formation. It would be advantageous to be able to shut down a heating system using circulating molten salts in a more controlled manner. As opposed to other types of heating systems one cannot simply turn off a heat transfer fluid based heating system. Heat transfer fluid must be removed from the conduits of the conduit-in-conduit heaters during a shut-down procedure. When the heat transfer fluid is molten salt, removal of the salts presents different challenges. If the circulating pumps are turned off the molten salt will begin to cool and solidify clogging the conduits. Due to the fact that salts are typically soluble in one or more solvents, one strategy for removing the salt from the heater conduits is to flush the conduits with an aqueous solution. However, flushing the conduits with an aqueous solution may take anywhere from days to months depending on the temperature of the formation. In some embodiments, secondary fluids (for example, fluids produced during in situ heat treatment and/or conversion processes) may be used to flush out salts from the conduits. Due to the typically higher boiling point of secondary fluids, removing remaining salts from the conduits may be accomplished faster than using an aqueous solution (for example, from hours to days instead of days to months). In some embodiments, a “pig” may be used to push the salts out of the conduits. A pig may include any material or device which will fit within the confines of the conduit in conduit heaters such that the pig will move through the conduit while allowing a minimal amount of salt to pass around the pig as it is conveyed through the conduit. Typically a pig is conveyed through a conduit using hydraulic pressure. Using a pig to remove heat transfer fluids may reduce the shut-down time for the circulating molten salt heater to a time period measured in hours. Using a pig to shut-down the heater may include the use of additional specialized surface equipment (for example, modified wellheads, specially designed pigging system for high temperature applications). In certain embodiments, only U-shaped heaters may use a pig during a shut-down procedure. All three shut-down methods have different advantages.
Fluids may be used to shut-down circulating molten salt heaters. In some embodiments, compressed gases may be used to shut-down circulating molten salt heaters. Compressed gases may combine many of the different advantages of the other three shut-down methods.
Using compressed gases to shut-down circulating molten salt heaters may have several advantages over using aqueous solutions or secondary fluids. Using compressed gases may be faster, require fewer surfaces resources, more mobile, and allow for emergency shutdown relative to using aqueous solutions or secondary fluids. Using compressed gases to shut-down circulating molten salt heaters has several advantages over using a pig and compressed gases to convey the pig. Using compressed gases may require fewer surfaces resources and have fewer limitations on what types of heaters may be shut down relative to using a pig and compressed gases to convey the pig.
Some of the disadvantages of using compressed gases include reduced efficiency of salt displacement relative to using aqueous solutions or secondary fluids. In some embodiments, a displacement efficiency of the conveyance of molten salts moving through a conduit heater may be changed by varying the transient pressure profile. Using compressed gases to convey molten salts may result in different types of flow profiles. Varying transient pressure profiles may result in various pressure profiles including, for example, Taylor flow, dispersed bubble flow, churn flow, or annular flow. Taylor flow may be generally described as a two phase flow pattern such that the gas and molten salt move through the conduit as separate portions (except for a thin film of molten salts along the walls of the conduit between the walls and the portions of gases). Dispersed bubble flow may be generally described as a multiphase flow profile in which the compressed gas moves as small dispersed bubbles through the molten salt. Churn flow may be generally described as a multiphase flow profile (typically observed in near-vertical pipes) in which large, irregular slugs of gas move up the approximate center of the conduit, usually carrying droplets of molten salt with them. Most of the remaining molten salt flows up along the conduit walls. As opposed to Taylor flow, neither phase is continuous and the gas portions are relatively unstable, and take on large, elongated shapes. Churn flow may occur at relatively high gas velocity and as the gas velocity increases, it changes into annular flow. Annular flow may be generally described as a multiphase flow profile in which the compressed gas flows in the approximate center of the conduit, and the molten salt is substantially contained in a thin film on the conduit wall. Annular flow typically occurs at high velocities of the compressed gas, and may be observed in both vertical and horizontal wells.
Taylor flow may result in maximum displacement efficiency. In some embodiments, modifying the transient pressure profile of compressed gases may allow a maximum displacement efficiency (for example, a Taylor flow profile) to be achieved during shut-down of circulating molten salt heaters.
In some embodiments, the molten salt includes a carbonate salt or a mixture of carbonate salts. Examples of different carbonate salts may include lithium, sodium, and/or potassium carbonate salts. The molten salt may include about 40% to about 60% by weight lithium carbonate, from about 20% to about 40% by weight sodium carbonate salt and about 20% to about 30% by weight potassium carbonate. In some embodiments, the molten salt is a eutectic mixture of carbonate salts. The eutectic carbonate salt mixture may be a mixture of carbonate salts having a melting point above 390° C., or from about 390° C. to about 700° C., or about 600° C. The composition of the carbonate molten salt may be varied to produce a carbonate molten salt having a desired melting point using for example, known phase diagrams for eutectic carbonate salts. For example, a carbonate molten salt containing 44% by weight lithium carbonate, 31% by weight sodium carbonate, and 25% by weight potassium carbonate has a melting point of about 395° C. Due to higher melting points, heat transfer from hot carbonate molten salts to the formation may be enhanced. Higher temperature may reduce the time necessary to heat the formation to a desired temperature.
In some in situ heat treatment process embodiments, a circulation system containing carbonate molten salts is used to heat the formation. Using the carbonate molten salt circulation system for in situ heat treatment of a hydrocarbon containing formation may reduce energy costs for treating the formation, reduce the need for leakage surveillance, and/or facilitate heating system installation.
In some embodiments, a carbonate molten salt is used to heat the formation. In some embodiments, a carbonate molten salt is provided to piping in a formation after the formation has been heated using a heat transfer fluid described herein. The use of a carbonate molten salt may allow the formation to be heated if piping in the formation develops leakage. In some embodiments, disposable piping may be used in the formation. In some embodiments, carbonate molten salts are used in circulation systems that have been abandoned. For example, a carbonate molten salt may be circulated in piping in a formation that has developed leaks.
Over time contact of carbonate molten salt 284 may degrade or decompose parts of portion 286 of heater 201 to form openings in the portion (as shown in
In some embodiments, permeability or injectivity in a hydrocarbon containing formation is created by selectively fracturing portions of the formation. A solid salt composition may be injected into a section of the formation (for example, a lithium/sodium/potassium nitrate salts and/or lithium/sodium/potassium carbonate salts). In some embodiments, the solid salt composition is moved through the formation using a gas, for example, carbon dioxide, or hydrocarbon gas. In some embodiments, the solid salt composition may be provided to the formation as an aqueous slurry. Heat may be provided from one or more heaters to heat the portion to about a melting point of the salt. The heaters may be temperature limited heaters. As the solid salt composition becomes molten or liquid, the pressure in the formation may increase from expansion of the melting solid salt composition. The expansion pressure may be at a pressure effective to fracture the formation, but below the fracture pressure of the overburden. Fracturing of the section may increase permeability of the formation. In some embodiments, at least a portion of the heated solid salt compositions contacts at least some hydrocarbons causes an increase in pressure in the section and create fractures in the formation.
The molten salt may move through the formation towards cooler portions of the formation and solidify. In some embodiments, heaters may be positioned in some of the fractures in the section and heat is provided to a second section of the formation. In some embodiments, heat from the heaters in the fractures may melt or liquefy the solid salt composition and more fractures may be formed in the formation. In some embodiments, the heaters melt the molten salt and heat from the molten salt is transferred to the formation. In some embodiments, fluid is injected into at least some of fractures formed in the section. Use of molten salts to increase permeability in formations may allow heating of relatively shallow formations with low overburden fracture pressures.
It is to be understood the invention is not limited to particular systems described which may, of course, vary. It is also to be understood that the terminology used herein is for the purpose of describing particular embodiments only, and is not intended to be limiting. As used in this specification, the singular forms “a”, “an” and “the” include plural referents unless the content clearly indicates otherwise. Thus, for example, reference to “a core” includes a combination of two or more cores and reference to “a material” includes mixtures of materials.
In this patent, certain U.S. patents and U.S. patent applications have been incorporated by reference. The text of such U.S. patents and U.S. patent applications is, however, only incorporated by reference to the extent that no conflict exists between such text and the other statements and drawings set forth herein. In the event of such conflict, then any such conflicting text in such incorporated by reference U.S. patents and U.S. patent applications is specifically not incorporated by reference in this patent.
Further modifications and alternative embodiments of various aspects of the invention will be apparent to those skilled in the art in view of this description. Accordingly, this description is to be construed as illustrative only and is for the purpose of teaching those skilled in the art the general manner of carrying out the invention. It is to be understood that the forms of the invention shown and described herein are to be taken as the presently preferred embodiments. Elements and materials may be substituted for those illustrated and described herein, parts and processes may be reversed, and certain features of the invention may be utilized independently, all as would be apparent to one skilled in the art after having the benefit of this description of the invention. Changes may be made in the elements described herein without departing from the spirit and scope of the invention as described in the following claims.
This patent application is a continuation of U.S. patent application Ser. No. 14/160,031 entitled “LEAK DETECTION IN CIRCULATED FLUID SYSTEMS FOR HEATING SUBSURFACE FORMATIONS” to Nguyen filed on Apr. 8, 2011, which is a divisional of U.S. patent application Ser. No. 13/083,246 (now U.S. Pat. No. 8,631,866 issued on Jan. 21, 2014) entitled “LEAK DETECTION IN CIRCULATED FLUID SYSTEMS FOR HEATING SUBSURFACE FORMATIONS” to Nguyen filed on Apr. 8, 2011, which claims priority to U.S. Provisional Patent No. 61/322,643 entitled “CIRCULATED FLUID SYSTEMS FOR HEATING SUBSURFACE FORMATIONS” to Nguyen et al. filed on Apr. 9, 2010; U.S. Provisional Patent No. 61/322,513 entitled “TREATMENT METHODOLOGIES FOR SUBSURFACE HYDROCARBON CONTAINING FORMATIONS” to Bass et al. filed on Apr. 9, 2010; and International Patent Application No. PCT/US11/31553 entitled “LEAK DETECTION IN CIRCULATED FLUID SYSTEMS FOR HEATING SUBSURFACE FORMATIONS” to Nguyen filed on Apr. 7, 2011, all of which are incorporated by reference in their entirety. This patent application incorporates by reference in its entirety each of U.S. Pat. No. 6,688,387 to Wellington et al.; U.S. Pat. No. 6,991,036 to Sumnu-Dindoruk et al.; U.S. Pat. No. 6,698,515 to Karanikas et al.; U.S. Pat. No. 6,880,633 to Wellington et al.; U.S. Pat. No. 6,782,947 to de Rouffignac et al.; U.S. Pat. No. 6,991,045 to Vinegar et al.; U.S. Pat. No. 7,073,578 to Vinegar et al.; U.S. Pat. No. 7,121,342 to Vinegar et al.; U.S. Pat. No. 7,320,364 to Fairbanks; U.S. Pat. No. 7,527,094 to McKinzie et al.; U.S. Pat. No. 7,584,789 to Mo et al.; U.S. Pat. No. 7,533,719 to Hinson et al.; U.S. Pat. No. 7,562,707 to Miller; U.S. Pat. No. 7,841,408 to Vinegar et al.; and U.S. Pat. No. 7,866,388 to Bravo; U.S. Patent Application Publication Nos. 2010-0071903 to Prince-Wright et al. and 2010-0096137 to Nguyen et al.
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