Patent Application
20230045845
The present invention relates to production of hydrocarbons from a subterranean reservoir using steam injection to enhance production, such as in a SAGD well system, and more particularly to use of a particle, which may be a nanoparticle, to adsorb hydrogen sulfide in the subterranean reservoir to reduce hydrogen sulfide (H2S) production to the surface.
Steam Injection Including Steam Assisted Gravity Drainage to Enhance Hydrocarbon Production.
In general, steam injection is a technique for enhancing production of hydrocarbons from a subterranean reservoir to the surface by injecting steam into a reservoir to reduce the viscosity of hydrocarbons in the reservoir, so that the hydrocarbons flow more readily to a producing well.
Steam assisted gravity drainage (SAGD) is an example of steam injection that involves injecting steam from the surface into an upper horizontal well (an injection well) disposed in the reservoir above a lower horizontal well (a production well). The injected steam exits the injection well and rises in the reservoir to form a steam-saturated zone, which is conceptualized as a “steam chamber”, where hydrocarbons are heated by the steam and thereby reduced in viscosity. The reduced-viscosity hydrocarbons drain downward by gravity into the production well, and are produced to the surface.
Hydrogen Sulfide Removal from Produced Oil and Natural Gas Streams.
Crude oil and natural gas produced from reservoirs may have high concentrations of hydrogen sulfide (H2S). H2S is a dangerous, toxic, and corrosive gas.
Methods are available for treating and removing H2S from crude oil and natural gas streams after they have been produced to the surface. For example, the gas phase gas can be reacted with amines (i.e., alkylamines) in an absorber tower, but this is capital intensive. The gas phase and the liquid phase can be reacted with triazine-based scavengers, but this is not effective for high concentrations of H2S, or high levels of the liquid phase. The gas phase can be incinerated, but this has high greenhouse gas impacts.
Further, the Alberta Energy and Utilities Board, Interim Directive ID 2001-3, titled “Sulphur Recovery Guidelines for the Province of Alberta” (Aug. 29, 2001) requires higher sulphur recovery requirements as the rate of sulphur being processed increases. For example, these Guidelines require 70% and a 99.8% sulphur recovery rates at sulphur inlet rates of 1-5 tonnes and 2000 tonnes per day, respectively.
Prior Art.
U.S. patent application publication no. 2002/0157536 A1 (Espin et al.; Oct. 31, 2002), titled “Method for Removing H2S an CO2 from Crude and Gas Streams” discloses positioning a metal-containing nanoparticle in a stream containing H2S, with the metal-containing nanoparticle being selected from metal oxides, metal hydroxides and combinations thereof, whereby the nanoparticles adsorb the contaminants from the stream. In one embodiment, Espin et al. discloses that the stream is a downhole stream established from a hydrocarbon producing subterranean formation, and the nanoparticles are positioned in fractures induced into formation in the form of proppants and/or additives to proppants. The hydrocarbon stream produced through the fractures is exposed to the nanoparticles and H2S is adsorbed downhole.
PCT International patent application publication no. WO 2008/070990 (Larter et al.; Jun. 19, 2008), titled “Preconditioning an Oilfield Reservoir” discloses a method of enhancing recovery of a petroleum product in an oilfield reservoir that includes heavy or bitumen. The method involves injecting water including a preconditioning agent into a mobile water film included in the oilfield reservoir, and preconditioning the reservoir with the preconditioning agent prior to production of the petroleum product form the oilfield reservoir. Larter et al. discloses embodiments where the preconditioning agent includes hydrogen sulfide to modify the viscosity of oil in the reservoir. Larter et al. discloses other embodiments where the precondition agent contains a water soluble sulphate to make hydrogen sulfide in the reservoir to enliven oil being produced and hence improve recovery. Larter et al. discloses still other embodiments where the preconditioning is performed to modify magnetic properties of the reservoir, and the preconditioning agent may include magnetite nanoparticles, such as nanomagnetite or magnetite, complexed with multidentate carboxylic.
S. I. Martinez, and C. Bastidas, in “Application of Transition Metal Nanoparticles in the Streams Production of Heavy Crude Oil Treatment: H2S Mitigation”, (2017) Society of Petroleum Engineers, 2017, disclose experiments to simulate application of iron oxide, copper oxide, and nickel oxide nanoparticles during temperature and pressure conditions of steam injection for oil production. Martinez et al. uses a high vacuum gas oil (HVGO) (an aromatic solvents mixture) as a carrier fluid for the nanoparticles. Martinez et al., however, does not indicate how such carrier fluid might be used in relation to a steam injection process. Use of such a carrier fluid would add cost and complexity to hydrocarbon production.
There remains a need in the art for methods of producing hydrocarbons from a subterranean reservoir using a steam injection operation, including from a SAGD well system, and reducing the amount of H2S that is produced to the surface. Doing so may help to reduce corrosion of surface equipment, improve safety of personnel at the surface, and comply with regulations regarding sulfur recovery.
In one aspect, the present invention comprises a method for producing hydrocarbons from a subterranean reservoir. The method comprises the steps of: (a) injecting a mixture of steam and H2S-sorbent particles into the subterranean reservoir; (b) allowing the steam to reduce viscosity of the hydrocarbons in the subterranean reservoir, and allowing the H2S-sorbent particles to attach to the subterranean reservoir; (c) allowing the H2S-sorbent particles to adsorb hydrogen sulfide (H2S) in the subterranean reservoir; and (d) producing the hydrocarbons to the surface (i.e., to ground level), without producing the H2S-sorbent particles with adsorbed H2S that remain attached to the subterranean reservoir.
In one embodiment, the method is implemented using a single well. That is, in step (a), the mixture of steam and H2S-sorbent particles are injected into the subterranean reservoir via a well. In step (d), the hydrocarbons are produced to the surface via the well that was used in step (a) to inject the mixture of steam and H2S-sorbent particles into the subterranean reservoir.
In other embodiments, the method is implemented using a pair of wells, such as used in a steam flooding operation (also known as a steam drive operation), or in a SAGD operation. That is, in step (a), the mixture of steam and H2S-sorbent particles is injected into the subterranean reservoir via a first well. In step (d), the hydrocarbons are produced to the surface via a second well that is different from the first well. In a particular embodiment, the pair of wells is implemented by a SAGD well system, wherein the first well in an injection well comprising a horizontal or deviated injection well leg, and the second well is a production well comprising a horizontal or deviated production well leg below the injection tubing leg. In such embodiment, the method comprises, after step (c) and before step (d), the further step of allowing hydrocarbons in the subterranean reservoir to drain by gravity into the production well leg, while the H2S-sorbent particles with adsorbed H2S remain attached to the subterranean reservoir.
In embodiments of the method implemented using a first well and second well, as described above, the method may comprise, either before or after step (a), the further steps of: (e) injecting a mixture of a carrier fluid and additional H2S-sorbent particles into the subterranean formation via the second well; (f) allowing the additional H2S-sorbent particles to adsorb hydrogen sulfide (H2S) in the subterranean reservoir; and (g) producing the hydrocarbons to the surface, without producing the additional H2S-sorbent particles with adsorbed H2S that remain attached to the subterranean reservoir. The carrier fluid may be either a liquid, such as water, or a gas, such as nitrogen.
In embodiments of the method, step (a) of injecting the mixture of steam and H2S-sorbent particles creates a first region of H2S-sorbent particles and a second region of H2S-sorbent particles in the subterranean reservoir, wherein a concentration of H2S-sorbent particles in the first region is higher than a concentration of H2S-sorbent particles, if any, in the second region. The method may further comprise establishing a pressure gradient in the subterranean reservoir that directs H2S to flow through the first region in preference to the second region.
In embodiments of the method, steps (a) to (d) are performed in a first cycle, and then steps (a) to (d) are repeated in a second cycle. In such embodiments, step (a) of the first cycle may inject a first amount or concentration of H2S-sorbent particles in the mixture into the subterranean formation, and step (a) of the second cycle may inject a second amount or concentration of H2S-sorbent particles in the mixture into the subterranean formation, wherein the second amount or concentration is different from the first amount or concentration.
In embodiments of the method, the H2S-sorbent particles comprise a material selected from the group comprising a metal-organic framework (MOF), zinc oxide (ZnO), iron oxide (Fe2O3), magnetite (Fe3O4), copper oxide (CuO), nickel oxide (NiO), calcium oxide (CaO), manganese oxide (MnO2), and molybdenum oxide (MoO2).
The present invention may allow for a reduction of the amount of H2S, if any, that is produced to the surface. Injection of the H2S-sorbent particles may be performed during the steam phase of the steam injection operation, such as SAGD operations, cyclic steam stimulation, and steam flooding. This may be advantageous in that the conventional workflow of the steam injection operation is not materially altered by the need to inject a carrier fluid into the subterranean reservoir.
In the drawings, like elements may be assigned like reference numerals. The drawings are not necessarily to scale, with the emphasis instead placed upon the principles of the present invention. Additionally, each of the embodiments depicted are but one of a number of possible arrangements utilizing the fundamental concepts of the present invention.
Definitions.
The present invention relates to production of hydrocarbons from a subterranean reservoir using a steam injection operation, and H2S-sorbent particles to adsorb hydrogen sulfide (H2S) in the subterranean reservoir to reduce the amount of H2S, if any, produced to the surface.
Any term or expression not expressly defined herein shall have its commonly accepted definition understood by a person skilled in the art. As used herein, the following terms have the following meanings.
“Subterranean reservoir” refers to a subsurface body of rock having porosity and permeability that is sufficient to permit storage and transmission of a liquid or gaseous fluid.
“Steam chamber”, in the context of a SAGD well system, refers to a region a subterranean reservoir that is in fluid and pressure communication with an injection well, and that is subject to depletion of hydrocarbons, by gravity drainage, into a production well that is disposed parallel and below the injection well.
“Steam injection operation” refers to any method of producing hydrocarbons from a subterranean reservoir that involves injection of steam into the subterranean reservoir to decrease the viscosity of the hydrocarbons, so that the hydrocarbons flow more easily in the subterranean reservoir. Without limitation, steam injection operations include methods known in the art as steam assisted gravity drainage (SAGD), steam flooding or steam drive, and cyclic steam stimulation (CSS).
“Hydrocarbons” refer to hydrocarbon substances naturally occurring in a subterranean reservoir. Hydrocarbons may be in liquid, gaseous, or solid phases. Without limitation, hydrocarbons may include “heavy oil”, referring to hydrocarbons having a mass density of greater than about 900 kg/m3 under natural reservoir conditions. Without limitation, hydrocarbons may also include “bitumen” having a mass density of greater than about 1,000 kg/m3 under natural reservoir conditions, and existing in semi-solid or solid phase under natural reservoir conditions. It will be understood that “hydrocarbon production”, “producing hydrocarbons” and like terms, as used herein, do not preclude co-production of non-hydrocarbon substances that may be mixed with hydrocarbons such as trace metals, and gases such as hydrogen sulfide that may be dissolved under natural reservoir conditions, but exist in a gaseous phase at surface conditions.
“H2S-sorbent particle” refers to a particle that has an affinity for H2S. In embodiments, this affinity may be based on principles of adsorption—i.e., the H2S-sorbent particle physically adheres and/or chemically bonds to H2S. In embodiments, the H2S-sorbent particle has a maximum dimension (e.g., a diameter) less than about 1000 nm, more particularly less than 500 nm, more particularly less than 250 nm. In embodiments, the H2S-sorbent particle is a “nanoparticle”, which as used herein, refers to a particle that has a maximum dimension less than 100 nm. In embodiments, a nanoparticle may have a maximum dimension less than 50 nm, and more particularly less than 25 nm.
Metal-organic framework”, and its abbreviation “MOF”, refers to a porous material formed by compounds comprising metal ions or metal-ion clusters coordinated to organic ligands.
Referring back to
A variety of H2S-sorbent particles may be used in the present invention to adsorb H2S in the subterranean reservoir. Non-limiting examples are described below under the heading “H2S-sorbent particles.” It will be evident that the H2S-sorbent particles should have high affinity for H2S-sorbent particles at pressure and temperatures conditions in the subterranean reservoir, and relatively little to no affinity for hydrocarbons in the subterranean reservoir under those conditions.
Preferably, the selected H2S-sorbent particles are capable of adsorbing H2S over the full range of temperatures expected to be encountered in the steam chamber of a SAGD well system, which typically ranges from about 15° C. to about 300° C. In particular embodiments, the H2S-sorbent particles may have high affinity for H2S at temperatures of about 110° C. or greater, more particularly of about 200° C. or greater, and even more particularly, of about 230° C. or greater, to about 300° C. In this regard, calcium oxide (CaO) and iron oxide (Fe2O3) are reported to have been effective for H2S removal at high temperatures.
The H2S-sorbent particles should be sized so that they can permeate through the pores of the subterranean reservoir, without substantially impairing transmission of a liquid or gaseous fluid through the subterranean reservoir. A suitable size of H2S-sorbent particles may be selected having regard to the characteristics of a particular subterranean reservoir. As a non-limiting example, for subterranean reservoirs containing oil sands in Alberta, Canada, a suitable maximum dimension (e.g., diameter) of H2S-sorbent particles may be less than about 1,000 nm, more particularly less than about 500 nm, and even more particularly less than about 250 nm. In some embodiments, the H2S-sorbent particles may be nanoparticles—i.e., particles having a maximum dimension (e.g., diameter) less than about 100 nm, more particularly less than about 50 nm, and even more particularly less than about 25 nm.
Use of H2S-sorbent particles having higher surface area per mass may increase their efficacy in adsorption of the H2S gas. In embodiments, the H2S-sorbent particles have a surface area per mass in the range from about 1 to about 3,000 m2/g. In some embodiments, the surface area per mass may be greater than 50 m2/g, greater than about 100 m2/g, greater than about 250 m2/g, greater than about 500 m2/g, greater than about 750 m2/g, and greater than about 1,000 m2/g.
The H2S-sorbent particles may be selected to have a desired adsorption capacity, having regard to factors such as the amount or concentration of the H2S gas to be sequestered, or a desired rate of sequestration. For example, they may have an adsorption capacity (mg H2S/g sorbent material) in the range from about 0.1-15,000 mg/g. In some embodiments, the adsorption capacity may be greater than about 10 mg/g, more particularly greater than about 50 mg/g, more particularly greater than about 100 mg/g, more particularly greater than about 500 mg/g, and more particularly greater than about 1,000 mg/g.
Having regard to the H2S affinity of the selected H2S-sorbent particles, the concentration of H2S-sorbent particles in the mixture may be selected to be effective in absorbing H2S present in concentrations in the hydrocarbons in the subterranean reservoir, which typically range from about 100 ppm to about 30,000 ppm.
In
In
In
In
As known to persons skilled in the art, SAGD (and other steam injection operations as described below) may be performed over many years with multiple cycles of a steam injection phase followed by a hydrocarbon production phase. Accordingly, steps 100 to 108 may be performed repeatedly in cycles, with each performance of step 100 corresponding to a steam injection phase of a cycle, and each performance of step 108 corresponding to a hydrocarbon production phase of the cycle. In particular, the amount or concentration of H2S-sorbent particles in the mixture that is injected into the subterranean reservoir at each cycle may be selectively varied, possibly to account for factors such as the amount or concentration of H2S-sorbent particles that have been previously injected in past cycles, or will be injected in subsequent cycles. This can be used to achieve a variety of advantageous effects. As one example, the concentration or amount of H2S-sorbent particles that is injected in any given cycle can be limited, with a view to incrementally increasing the concentration or amount of H2S-sorbent particles attached to the subterranean reservoir over multiple cycles. As another example, the concentration or amount of H2S-sorbent particles that is injected in any given cycle can be selected to control the distribution of H2S-sorbent particles in the subterranean reservoir. For instance, the volumetric portion of the subterranean reservoir that is “seeded” with the H2S-sorbent particles can be incrementally increased over multiple cycles. As still another example, the concentration or amount of H2S-sorbent particles in the mixture that is injected in any given cycle can be varied over cycles to account for varying levels of H2S concentration in produced fluids during the operation of the well, or to selectively vary the H2S concentration of fluids produced to the surface during the operation of the well.
Referring back to
Controlled Placement of H2S-Sorbent Particles.
The contact time between non-condensable gases and the H2S-sorbent particles in the subterranean reservoir may be quite brief due to flow of the gas phase. As such, creating regions of the subterranean reservoir that have higher concentrations of H2S-sorbent particles, and preferentially promoting flow of non-condensable gases (including H2S) through such regions may promote contact of H2S with the H2S-sorbent particles, and therefore make the most economical and effective use of the H2S-sorbent particles.
As a non-limiting example, referring back to the
By control of the steam flow control devices (and the use of possible sealing elements associated with the injection tubing 202, such as sealing elements used for zonal isolation), it is possible to establish pressure gradients of the steam mixed with H2S-sorbent particles 220 that are injected into the subterranean reservoir in step 100. These pressure gradients will affect the distribution of H2S-sorbent particles 220, as the injected steam and H2S-sorbent particles 220 will tend to migrate from regions of higher pressure to regions of lower pressure. In
Pressure gradients also tend to cause non-condensable gases in the steam chamber 212 to flow from regions of relatively high pressure to regions of relatively low pressure. Accordingly, the steam flow control devices or other means may also be selectively controlled to establish a pressure gradient that affects the flow of non-condensable gases in the steam chamber 212 to regions of the steam chamber 212 having relatively higher concentrations of H2S-sorbent particles 220. For example, after the H2S-sorbent particles 220 are allowed to attach the sand particles of the subterranean reservoir, injection of steam (without further injection H2S-sorbent particles 220) into the steam chamber 212 may be continued. Opening of the first steam flow control device 224 and closing of the second steam flow control device 226 may create a region of relatively higher pressure in the vicinity of the first steam flow control device 224, as compared with the region in the vicinity of the second steam flow control device 226. Accordingly, non-condensable gases (possibly including hydrogen sulfide) will tend to flow from left to right in the drawing plane of
Adaption to Other Well Systems and Steam Injection Operations.
In the embodiment of
As known in the art, cyclic steam stimulation typically involves a “steam phase” of injecting steam into the reservoir via the well, a “soak phase” of allowing the steam to soak into the reservoir in the vicinity of the well and thereby reduce viscosity of hydrocarbons, and a “production phase” of producing hydrocarbons to the surface from the same well. The method of the present invention may be implemented by: injecting a mixture of steam and H2S-sorbent particles into the subterranean reservoir via the well during the “steam phase”; allowing H2S-sorbent particles to attach to the subterranean reservoir, and adsorb hydrogen sulfide (H2S) in the subterranean reservoir during the “soak phase”; and producing the hydrocarbons to the surface via the same well during the “production phase”, without producing the H2S-sorbent particles with adsorbed H2S that remain attached to the subterranean reservoir, Thus, it will be understood that the method may be implemented using a single well system, which may be a vertical well.
As known in the art, steam flooding or steam drive typically involves injecting steam into a reservoir via a first well to reduce the viscosity of hydrocarbons and displace the hydrocarbons toward a different second well. In contrast to SAGD, the first well and the second well may both be entirely vertical wells that are horizontally spaced apart from each other. The method of the present invention may be implemented by: injecting a mixture of steam and H2S-sorbent particles into the subterranean reservoir via the first well; allowing H2S-sorbent particles to attach to the subterranean reservoir that is disposed horizontally between the first and second wells, and adsorb hydrogen sulfide (H2S) in that subterranean reservoir; and producing the hydrocarbons to the surface via the second well, without producing the H2S-sorbent particles with adsorbed H2S that remain attached to the subterranean reservoir. Thus, it will be understood that the method may be implemented using a dual well system having a pair of entirely vertical wells.
H2S-Sorbent Particles.
The following description provides non-limiting examples of particles that are believed would be useful in the present invention to adsorb H2S in the subterranean reservoir, and a line of reasoning for their use. In general, References no. 1 to 14, below, provide information regarding efficacy of nanoparticles for adsorption of H2S. It is believed that such nanoparticles would be effective in adsorption of at least some amount of H2S in temperature and pressure conditions typically encountered in a subterranean reservoir.
Zinc Oxide (ZnO) Particles.
Zinc oxide and H2S react to produce zinc sulfide (ZnS) and water, according to the following reaction.
ZnO(s)+H2S(g)→ZnS(s)+H2O(l)
Zinc oxide particles are typically a solid, white, and odorless powder. Zinc oxide may be more stable and cost effective when compared with other adsorbents. A possible disadvantage is the limited feasibility of regeneration—i.e., desorption of adsorbed H2S to render the particle able to adsorb H2S again.
Reference no. 1 [Awume] reports performance characteristics of zinc oxide nanoparticles in the removal of H2S from gas streams. At ambient temperatures zinc oxide nanoparticles are up to 99% effective in capturing H2S gas. As feed H2S concentrations increases, the adsorption capacity also increases and the nanoparticles reach a saturation state more quickly, as summarized below in Table 1. Smaller zinc oxide nanoparticles (18 nm) have an overall higher adsorption capacity compared to larger particles (80 nm-200 nm). Larger zinc oxide nanoparticles, however, reached their saturation state faster, regardless of H2S feed concentration.
The saturation rate of adsorbent is unaffected by temperature, but the adsorption capacity of zinc oxide nanoparticles increases with an increase in temperature, as summarized below in Table 2.
Adsorption capacities increase with an increase in the zinc oxide nanoparticle quantity. The saturation rate of the adsorbent was higher with a decrease in nanoparticle quantity, regardless of the H2S feed concentration.
Synthesized zinc oxide nanoparticles (14-25 nm) can completely remove H2S from water-based drilling mud in ˜15 minutes, whereas bulk zinc oxide can remove ˜2.5% of H2S in as long as 90 minutes under the same operating conditions.
Reference no. 6 [Whittaker] describes NanoActive™ Sulphur Scavenger (NASS) (Timilon Technology Acquisitions LLC; Naples, Fla., USA), which is a zinc oxide (ZnO) nanoparticle sulphur recovery technology developed for the neutralization of H2S in crude oil and gas streams. Whittaker reports that NASS's two-step decomposition mechanism (adsorption by physisorption, followed by nonreversible chemical decomposition) substantially enhances its detoxification abilities because decomposition is less dependent on temperature. Whittaker reports that use of NASS™ improves scavenger efficacy between 4 and 6 times, depending on feed composition. Whittaker reports that the range at which NASS stand-alone systems are economical is up to 10,000 ppm H2S in liquid streams, and 1,000 ppm H2S at 320 m3/hr to 10,000 ppm H2S at 30 m3/hr in gas streams. At these levels, NASS reduces H2S to 0 ppm. For higher concentrations, NASS is used incombination with existing removal technologies.
Iron Oxide (Fe2O3) Particles.
Iron oxide reacts with H2S to produce iron sulfide (FeS) and water, according to the following reaction.
Fe2O3+3H2S→Fe2S3+3H2O
Iron oxide nanoparticles have been shown to be very effective for H2S removal from gas streams at temperatures in excess in 300° C. Reference no. 12 [Blatt et al.] indicates that impregnating a custom-activated carbon with these nanoparticles resulted in a slight enhanced removal efficiency.
SULFATREAT™ (Schlumberger Limited, Houston, Tex., USA) is a granular iron oxide based H2S adsorbent and SELECT FAMILY™ (Schlumberger Limited, Houston, Tex., USA) is a mixed metal oxide-based H2S adsorbent, both of which are used to remove H2S from gas streams in fixed bed processes. It is possible that these sorbents may be physically reduced to nanoparticle size.
Magnetite (Fe3O4) Particles.
Magnetite reacts with H2S at low pH to form hydrogen as a byproduct, according to the following equation.
Fe3O4+6H2S→3FeS2+4H2O+2H2
Reference no. 4 [Martinez et al.] reports that magnetite nanoparticles have reached more than 93% in H2S mitigation.
Copper Oxide (CuO) Particles.
Copper oxide reacts with H2S is according to the following equation.
CuO+H2S→CuS+H2O
Reference no. 4 [Martinez et al.] reports that copper oxide is thermodynamically favorable for sulphur removal, and that the reaction between copper oxides and sulfides is very fast and effective. Also, this oxide can be reduced to the metallic copper easily.
Reference no. 7 [Georgiadis et al.] reports that the presence of copper increased the mobility of sulfur anions in Cu-containing ZnS particles. Georgiadis et al. also reports that CuO has an extremely high equilibrium sulfidation constant that allows an extremely low equilibrium constant even at high temperatures.
Adsorbents with high Cu concentrations have been shown to be more efficient in capturing H2S compared to adsorbents with high Zn concentrations.
Nickel Oxide (NiO) Particles.
Nickel oxide reacts with H2S is according to the following equation.
NiO+H2S→NiS+H2O
Reference no. 4 [Martinez et al.] reports results in H2S mitigation (83%) in studies of the application of nickel nanoparticles to treat heavy crude oil, Martinez et al. reports that three faces of nickel were generated (NiO, Ni° and Ni2S3), and for this reason, it was difficult to determine which material is working as the scavenger.
Gold (Au) Particles.
Reference no. 8 [Mubeen et al.] reports that H2S is known to adsorb strongly onto gold because of the high chemical affinity between gold and sulphur. At temperatures between 165° K. and 520° K., H2S decomposes to form SH which is chemisorbed onto the gold surface while H2 is released. However, gold nanoparticles are a very expensive option and there is not much literature relating to gold and H2S adsorption.
Calcium Oxide (CaO) Particles.
Calcium oxide reacts with H2S is according to the following equation.
CaO+H2S→CaS+H2O
Reference no. 10 [Wang] reports that calcium oxide a good choice for H2S adsorption at elevated temperatures (250-500° C.).
Manganese Oxide (MnO2) Particles.
Manganese oxide reacts non-catalytically with H2S is according to the following equation.
MnO2+2H2S→MnS+S+2H2O
Reference no. 9 [Konkol et al.] reports that desulphurization performance of different metallic oxides on activated carbon decreases in the following order: Mn>Cu>Fe>Ce>Co>V.
Molybdenum Oxide (MoO2) Particles.
Reference no. 13 [Hassankiadeh et al.] reports that molybdenum oxide nanoparticles have an adsorption capacity of 0.081 and 0.074 g H2S/g molybdenum oxide in low temperature and low concentration of H2S using non-spherical and spherical molybdenum oxide sorbent, respectively.
Metal-Organic Frameworks.
Non-limiting examples of MOFs that maybe used to adsorb H2S are reviewed by Georgiadis et al. [Reference no. 7], and Georgiadis et al. [Reference no. 22], including MOFs based on vanadium, aluminum, chromium, titanium, zeolites, zinc, zinc oxide, zirconium oxide, graphite oxide, and MOF's known as M-MOF-74, and Ni-MOF-74.
Interpretation.
The corresponding structures, materials, acts, and equivalents of all means or steps plus function elements in the claims appended to this specification are intended to include any structure, material, or act for performing the function in combination with other claimed elements as specifically claimed.
References in the specification to “one embodiment”, “an embodiment”, etc., indicate that the embodiment described may include a particular aspect, feature, structure, or characteristic, but not every embodiment necessarily includes that aspect, feature, structure, or characteristic. Moreover, such phrases may, but do not necessarily, refer to the same embodiment referred to in other portions of the specification. Further, when a particular aspect, feature, structure, or characteristic is described in connection with an embodiment, it is within the knowledge of one skilled in the art to affect or connect such module, aspect, feature, structure, or characteristic with other embodiments, whether or not explicitly described. In other words, any module, element or feature may be combined with any other element or feature in different embodiments, unless there is an obvious or inherent incompatibility, or it is specifically excluded.
It is further noted that the claims may be drafted to exclude any optional element. As such, this statement is intended to serve as antecedent basis for the use of exclusive terminology, such as “solely,” “only,” and the like, in connection with the recitation of claim elements or use of a “negative” limitation. The terms “preferably,” “preferred,” “prefer,” “optionally,” “may,” and similar terms are used to indicate that an item, condition or step being referred to is an optional (not required) feature of the invention.
The singular forms “a,” “an,” and “the” include the plural reference unless the context clearly dictates otherwise. The term “and/or” means any one of the items, any combination of the items, or all of the items with which this term is associated. The phrase “one or more” is readily understood by one of skill in the art, particularly when read in context of its usage.
The term “about” can refer to a variation of ±5%, ±10%, ±20%, or ±25% of the value specified. For example, “about 50” percent can in some embodiments carry a variation from 45 to 55 percent. For integer ranges, the term “about” can include one or two integers greater than and/or less than a recited integer at each end of the range. Unless indicated otherwise herein, the term “about” is intended to include values and ranges proximate to the recited range that are equivalent in terms of the functionality of the composition, or the embodiment.
As will be understood by one skilled in the art, for any and all purposes, particularly in terms of providing a written description, all ranges recited herein also encompass any and all possible sub-ranges and combinations of sub-ranges thereof, as well as the individual values making up the range, particularly integer values. A recited range includes each specific value, integer, decimal, or identity within the range. Any listed range can be easily recognized as sufficiently describing and enabling the same range being broken down into at least equal halves, thirds, quarters, fifths, or tenths. As a non-limiting example, each range discussed herein can be readily broken down into a lower third, middle third and upper third, etc.
As will also be understood by one skilled in the art, all language such as “up to”, “at least”, “greater than”, “less than”, “more than”, “or more”, and the like, include the number recited and such terms refer to ranges that can be subsequently broken down into sub-ranges as discussed above. In the same manner, all ratios recited herein also include all sub-ratios falling within the broader ratio.
All publications, patents and patent applications mentioned in this specification are indicative of the level of skill of those skilled in the art to which this invention pertains and are herein incorporated by reference, where permitted, to the same extent as if each individual publication, patent, or patent applications was specifically and individually indicated to be incorporated by reference.
This Application claims priority of U.S. Provisional Application No. 63/229,926 entitled “STEAM-ENHANCED HYDROCARBON RECOVERY USING HYDROGEN SULFIDE-SORBENT PARTICLES TO REDUCE HYDROGEN SULFIDE PRODUCTION FROM A SUBTERRANEAN RESERVOIR” filed on Aug. 5, 2021, the disclosure of which is expressly incorporated by reference herein in its entirety.
| Number | Date | Country | |
|---|---|---|---|
| 63229926 | Aug 2021 | US |
