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    • 专利摘要:
    The present invention relates to a fracturing carrier fluid for fracturing an underground formation, said fracturing carrier fluid comprising at least one linear or branched hydrofluorocarbon compound which has a boiling point, at a pressure of 1 atmosphere, which is between 0 ° C and 65 ° C. The invention also relates to a fracturing fluid comprising said fracturing carrier fluid as well as proppants. The invention further relates to a method for fracturing an underground formation using said fracturing fluid.
    公开号:FR3031110A1
    申请号:FR1463515
    申请日:2014-12-31
    公开日:2016-07-01
    发明作者:Gilles Barreto
    申请人:Arkema France SA；
    IPC主号:
    专利说明:

    [0001] FIELD OF THE INVENTION The present invention relates to the treatment of subterranean formations containing fluid with fracturing fluids. Underground fluids of economic value are usually obtained from an underground formation via a well that enters the formation. Fluids from underground formations containing fluid may be water which is for example used as a geothermal source for heating, drinking water or as a source of salts. Fluids from subterranean fluid-containing formations may also be oil or gas or condensed gas in its liquid state as it rises toward the surface, also called a condensate. [0003] Unfortunately, underground formations containing fluid, and in particular underground formations containing oil and gas, are increasingly difficult to exploit from an economic point of view and require the use of processes and processes. specific equipment to improve the extraction of underground fluids through extraction wells. A typical improvement in well production can be achieved by treating the formation to increase the flow rate of underground fluids, such as oil and gas. In general, such an improvement in the production of the wells is obtained by using water which is injected into one or more other wells which enter the underground formation, referred to as wells. injection or injector (s), in order to maintain the pressure of the subterranean formation at a level sufficient to obtain economic flow from the subterranean formation to the surface through the production well (s). However, the improvement in productivity can not be stable over time due to clogging that may occur within the porosity of the subsurface formation near the production well or near the injection well. . In addition to oil and gas wells that are not able to continue to produce economically and that require a stimulation of production by treating the formation to increase the output rate of oil and / or gas, there are also underground formations that can not produce hydrocarbons after a borehole has been drilled and a well has been installed to enter the subterranean formation. One of the reasons is that they naturally have a very low permeability such as that associated with shale oil, shale gas, compact formation oil, compact formation gas and coal bed methane, permeability which impedes the flow of fluids. [0006] And even for underground formations that are already producing fluids under economic conditions, it may be desirable to further increase their production levels. A common and known method of stimulation treatment is fracturing. Conventionally, the execution of such a treatment comprises injecting a liquid suspension, the fracturing fluid, down into the wellbore and back into the formation to a degree necessary to improve the permeability to fluid, usually because the number and / or size of passages or fractures in the formation is increased. The fracturing fluid generally comprises the fracturing carrier fluid and solid particles. To create the fractures, the fracturing fluid is injected at high pressure, and in this case a high pressure pumping equipment is required. Usually, solid particles are also injected with the fracturing fluid in order to keep the fractures open. Such solid particles, also known as proppants or "proppants", are dispersed in the fracturing carrier fluid and are then transported to the bottom of the fractures during the high-pressure pumping operation. pressure. [0009] The injection is continued until a fracture of sufficient size is obtained to allow the correct and correct positioning of the proppants. Once the proppants are in place, the injected fluids may leak into the formation until the fracture has become sufficiently thinner to hold the proppants in place. The pressure at the wellhead is then lowered and the fluid is pumped back to the surface. The proppants are usually granular materials, typically sand. Other commonly used proppants include resin coated sand, intermediate strength retaining ceramics, and high strength proppants such as sintered bauxite and zirconium oxide. Many less common proppants include plastic pellets, steel shot, glass beads, high strength glass beads, aluminum pellets, rounded nut shells, and the like. For the treatment to be successful, the fracturing fluid, usually oil or water in the liquid phase, must be removed from the well typically to avoid clogging hydrocarbons of the underground formation containing hydrocarbons. .
    [0002] In many examples this is a difficult problem which involves a considerable expenditure of time and money. Current well treatments generally require the use of large volumes of fracturing fluid. For example, during a fracturing treatment, wells, in particular horizontal wells, commonly require up to 20000 tons of aqueous fracturing fluid. Before production from the reservoir can be restarted, a substantial, if not all, portion of the aqueous fracturing fluid must be removed. This represents a significant expense of time and pumping costs. [0013] Nowadays, the most effective fracturing processes use water ru) as a carrier fluid, more specifically either viscosified water or slick water in the English language. Due to the higher cost of oil compared to that of water as a fracturing fluid, oil fracturing is limited to subterranean formations that are sensitive to water. Indeed, some formations contain specific clays which will swell when they come into contact with water, deteriorating the permeability even in the presence of fractures. However, the oil usually contains organic pollutants such as benzene which is carcinogenic, toluene which causes serious damage to health in case of prolonged exposure by inhalation, ethylbenzene and xylene, which will come into contact with and will dilute in the water in the underground formation with a risk of pollution once on the surface. Benzene, toluene, ethylbenzene and xylene, also known as BTEX, are listed by the EPA in the Clean Air Act of 1990 as part of the 188 harmful agents of air pollution. [0014] In addition, certain regions in which stimulation is used suffer from significant water supply limitations, for example Texas in the US Other locations include agricultural areas or residential areas in their vicinity. which necessitates a high quality treatment of reflux water pumped back to the surface after fracking operations and before these waters are discharged. In 1966, Dow Chemicals proposed (see for example US Pat. No. 3,368,627) a fracturing process which uses a combination of C2-C6 hydrocarbons and carbon dioxide as the fracturing fluid. The mixture is designed to achieve a sufficiently high critical temperature or a critical pressure sufficiently low to remain liquid at the temperature and pressure prevailing during injection at the bottom of the well, but also at a sufficiently low critical temperature or at a low temperature. a critical pressure sufficiently high that a substantial portion of this injected fluid is converted into a gas upon a release of pressure applied to the liquid during injection. Indeed, the temperature and the critical pressure are important parameters for a fracturing fluid that is able to be in the gas state. Below the critical temperature, a fluid can exist in a solid and / or liquid and / or gaseous form depending on the pressure and the temperature. Above the critical temperature, a fluid may exist in gaseous form and / or supercritical fluid as a function of pressure and temperature. If the temperature in the reservoir is greater than the critical temperature of the fracturing fluid, the liquid fracturing fluid will undergo a phase transition upon heating to a supercritical fluid during injection. The supercritical fluid has a higher density and viscosity than a gas at the same temperature and lower than a liquid at the same pressure. Thus the friction of the proppants with the carrier fluid is less when the carrier fluid is in the supercritical state than when it is in the liquid state. In this way, the sedimentation of the proppants under the effect of gravity, which have a higher density than that of the carrier fluid, is greater in the horizontal parts of the surface equipment, in the wells and in the fractures when the Fracturing carrier fluid is in the supercritical state. The sedimentation of the proppants is characterized by the sedimentation rate of the proppant particles. Preventing sedimentation, or at least minimizing sedimentation, is important in order to maximize the transport efficiency that could be slowed by the friction of the proppant particles with the surface of the pipeline equipment and the fracture walls. Therefore, minimizing or avoiding sedimentation in equipment and fractures increases the likelihood that proppants will reach fractures and limit the build-up of proppant in the horizontal portions of equipment and fractures. Consequently, the transport efficiency of the proppants is lower when the sedimentation rate is higher, and this is for example the case when the fracturing carrier fluid is in the supercritical state rather than when it is at the liquid state. This patent US 3368627 proposes a solution to avoid the use of water and to reduce the amount of energy required to pump the fracturing fluid back to the surface. This process, however, employs two fluids, in the gas phase at ambient pressure and temperature, which must be compressed to make them liquid, which increases the number of equipment. In addition, carbon dioxide is difficult to compress because of its critical point: the high critical pressure (7.3 MPa) and the critical low temperature (31 ° C) make it necessary to compress the gas to a higher pressure. 7.3 MPa and / or cool to temperatures below 31 ° C to make it liquid. [0018] Attempts have been made to simplify the process and to use only a carrier fluid other than water to suspend the proppants. The "OH and Gas Journal", July 5, 1971, page 60, discloses a gelled liquid gas useful for fracturing gas wells The gelled liquid gas contains carbon dioxide, liquid petroleum gases, a gelling material as well as BACKGROUND OF THE INVENTION Viscosifying the carrier fluid, or gelling it, is useful to allow more effective transportation of the proppants by increasing the friction between them and the carrier fluid. The gravity-supporting agents, which have a higher density than the carrier fluid, are limited in the horizontal portions of the surface equipment, in the wells and in the fractures. [0007] US Patent 3846310 discloses the use of a mixture of a first alcoholate of a Group IA metal and a second alcoholate of a Group IIIA element as a gelling agent for a hydrocarbon carrier fluid such as, for example, a liquefied petroleum gas, heptane. In the presence of water, it is said that the gelling agent passes into an aqueous phase, thereby reducing the viscosity of the hydrocarbon. It is said that when treating a gas or condensate production formation, it is preferable that the liquid hydrocarbon is volatile under the reservoir conditions. During the injection operations, the liquid hydrocarbon is under pressure and retains its liquid state. When the applied pressure is released, the liquid will be converted into a highly mobile vapor due to its volatility in the reservoir conditions, thereby promoting rapid well cleaning. In areas where there is no water in the subterranean formation, the gelling agent, which does not evaporate, will remain in the subterranean formation, leading to the formation of deposits that clog fractures and reduce flow of hydrocarbons initially present in the underground formation. This limitation is also seen in the publication of the "Oi / and Gas Journal", July 5, 1971, page 60. [0020] Another disadvantage of US Patent 3846310 is the use of heptane. kPa), this alkane has a boiling point of 98 ° C, while that of toluene is 111 ° C. Since the boiling points are close to each other (less than 20 ° C of difference), this would require expensive equipment to separate the two compounds in order to avoid the pollution of heptane by toluene. [0021] More recently, US 2011284230 claims a method of treating formations. underground, the method comprising introducing a fracturing hydrocarbon fluid comprising a liquefied petroleum gas into the subterranean formation, subjecting the fracturing hydrocarbon fluid to pressures greater than the formation pressure, and containment Fracturing hydrocarbon fluid in the subterranean formation for a period of at least 4 hours. It is also said that the fracturing hydrocarbon fluid produced by the above processes may comprise at least one gelling agent, and that the gelling agent may be any suitable gelling agent for gelling LPG, comprising ethane, propane, butane, pentane or mixtures of ethane, propane, butane and pentane. However, when using a gelling agent, the problem is the formation of deposits once the pressure is released. If the pressure is not sufficiently relaxed to effect evaporation of the hydrocarbons from the fracturing fluid, there is a risk when said fracturing fluid is pumped back to the surface. This will be difficult because of the high viscosity of the gelled fracturing fluid. In such cases, English breakers may be used to reduce the viscosity. Conversely, this increases the complexity with the control of the dosage and the delayed action time of the cleavage agent on the gelling agent. When no gelling agent is used, the viscosity of LPG, including ethane, propane, butane, pentane or mixtures of ethane, propane, butane and pentane, is very low, and the transport performance of the proppants is low. [0024] ECorp Stimulation Technologies (see http://www.ecorpintl.com/) promotes the use of propane as a fracturing fluid without a gelling agent. Worn in liquid form, propane is injected with sand or ceramic. It is said that almost all the injected propane (from 95% to 100%) returns as a gas, due to the natural phenomenon of pressure difference between the subterranean formation and the surface. It is said that the recovered propane is re-used for stimulation operations, or re-injected into pipelines with the rest of the extracted gas. Unfortunately, this technology has a poor performance in the transport of proppants. [0025] ECorp Stimulation Technologies also promotes the use of a fluorinated propane derivative which is 1,1,1,2,3,3,3-heptafluoropropane. This molecule is also known as a refrigerant under the code name R-227ea, according to the American Society of Heating Standard 34, Refrigerating and Air Conditioning Engineers (ASHRAE, 3031110 7 2010a and 2010b). R-227ea is presented as a stimulating fluid, in order to completely eliminate the risk associated with the flammability of conventional propane. It is said that no water or any chemical additive is used with heptafluoropropane and that, as with conventional propane, heptafluoropropane would be recovered in a gaseous form for immediate or future re-use. It is said that the R-227ea can be easily separated from the components of the natural gas extracted from the well, in particular propane and butane. [0026] While this technology offers recycling opportunities and also provides better performance of proppant transport than liquid propane, its proppant transport performance is lower than that of water, except for ° C and 60 ° C where it is equivalent because of the accuracy of the calculation, as will be illustrated. R-227ea in particular has a lower transport performance of proppants than water, as will be illustrated, at a temperature above 60 ° C, which is found in all shale formations. The high volatility of R-227ea is also a disadvantage when the fracturing fluid is prepared and injected at a relatively high ambient temperature, for example about 40 ° C and higher, as can occur in warm regions such as than Texas. Mixers are used to mix the proppants with the liquid carrier fluid. Proppants maintained in mixers at the well site for use as proppants in the fracturing operation can reach temperatures such as 65 ° C because of exposure of the mixers to the sun. When the proppants and the liquid carrier fluid are mixed, a portion of the liquid carrier fluid may change phase, resulting in less fluid volume. To avoid this, it is necessary to maintain the liquid fracturing carrier fluid at such a temperature by increasing the pressure inside the mixer or cooling it, which makes it more expensive. In addition, the separation with butane makes it necessary to proceed in two steps: first a condensation of butane which is less volatile (the boiling point at a pressure of 1 atmosphere (101325 Pa), which is the Normal boiling point, or NBP, is 0 ° C for n-butane while the NBP of R-227ea is -16 ° C), and then condensation of R-227ea which is in phase gas after the first condensation. US Patent Application Publication No. 2014/0251623 discloses the use of fluids which may comprise non-gelled liquid alkanes, halogenated hydrocarbons, emulsified hydrocarbons, propylene carbonate, and a fluidized solid proppant material for carrying out the processes. fracturing operations. The purpose is to provide fluids which have reduced flammability compared to known alkanes used. The proposed fluids include certain specific halogenated hydrocarbons. However, these halogenated hydrocarbons are in the gaseous state at ambient temperature and pressure, so that they are not easy to handle and store under these conditions, with high risks of leakage. Therefore, there is still a need for fracturing fluids that do not contain water while being at least as effective or even more effective than water-based fracturing fluids. There is also a need for fracturing fluids which do not contain water and which are easy to handle and store at ambient temperature and pressure. There is also a need for fracturing fluids which do not contain water, which do not contain carcinogenic products and which are easy to recycle as fracturing fluids without being polluted with benzene, toluene, ethylbenzene and the like. xylene. In spite of continuous research since 1966, there is still a need for alternative and / or improved fracturing carrier fluids which overcome the disadvantages of the fracturing carrier fluids of the state of the art. The inventors have now discovered that the above objectives are achieved in whole or at least in part with the fracturing carrier fluids of the present invention which is described in detail below. The object of the present invention is therefore to provide a fracturing carrier fluid which has one or more, and preferably all, of the following characteristics: the fracturing carrier fluid is non-aqueous, that is to say that no water is added voluntarily, 25 - the fracturing carrier fluid is low toxicity compared to the oil and more generally has a low environmental impact, - the fracturing carrier fluid is easily converted into a liquid or a gas, and vice versa, during variations of the temperature and / or variations of the pressure, the fracturing carrier fluid allows a sedimentation rate equal to or less than that of the known fracturing carrier fluids, over the largest temperature range possible, for example between 20 ° C and 200 ° C, preferably between 70 ° C and 190 ° C, for a given size and nature of the proppant, - flui Fracturing carrier allows a rate of sedimentation equal to or less than that of water, over the widest possible range of temperatures, for example between 20 ° C and 200 ° C, preferably between 30 ° C and 190 ° C more preferably between 30 ° C and 140 ° C, for a given size and nature of the proppant; - the fracturing carrier fluid is easy to separate / recover from a rising fluid (eg containing natural gas, condensate or oil, ...), and - the fracturing carrier fluid is easy to re-transform in the liquid state. In the following description of the present invention, the following definitions and methods will be used: the environmental impact of the solvents is measured by the greenhouse effect potential (GWP) with respect to the carbon dioxide for a 100-year integration and Ozone Depletion Potential (ODP). The GWP of R-227ea is 3220 and the ODP is 0. The GWP of propane is 20 and the ODP is 0; The normal boiling point (or NBP) is the boiling point at a pressure of 1 atmosphere (101325 Pa); the transport performance of the proppant is evaluated with the sedimentation rate of a single spherical solid particle (the proppant) in the carrier fluid under the effect of gravity at a given temperature which corresponds to the temperature of the subsurface hydrocarbon formation; the lower the sedimentation rate, the longer the time required for the sedimentation of the proppant. In a first aspect, the present invention relates to a fracturing carrier fluid for fracturing a subterranean formation, said fracturing carrier fluid comprising at least one linear or branched hydrofluorocarbon compound which has a boiling point which is included between 0 ° C and 65 ° C. In the present invention, "hydrofluorocarbon compound" refers to a compound comprising carbon atoms, hydrogen, fluorine and optionally chlorine. The selection of the appropriate fracturing carrier fluid depends on the normal boiling points of the recovered hydrocarbons: according to a preferred embodiment, the normal boiling point of the appropriate fracturing carrier fluid has a difference of at least 10 ° C, preferably at 20 ° C, more preferably 25 ° C, above or below the normal boiling point of the recovered hydrocarbon gas which has the highest (and lowest) normal boiling point, the gaseous hydrocarbon mixture recovered. This makes it easier to recover, for example by distillation, the fracturing carrier fluid. According to a further preferred embodiment, the normal boiling point of the fracturing carrier fluid is at least 10 ° C, preferably 20 ° C, more preferably 25 ° C, above the point normal boiling of the recovered hydrocarbon gas which has the highest normal boiling point of the recovered hydrocarbon mixture, eg butane, above 0 ° C. Among these suitable fracturing carrier fluids, the preferred ones are those having a high normal boiling point, preferably greater than 0 ° C., more preferably greater than 10 ° C., more preferably greater than 20 ° C. ° C. The most preferred fracturing carrier fluids are those which have a normal boiling point above room temperature, such that the fracturing carrier fluids are liquid at room temperature and thus easily separated from other gaseous hydrocarbons recovered at room temperature. ambient temperature and pressure. Another advantage of these fracturing carrier fluids that are liquid at room temperature is their ease of storage and use. These issues of ease of separation and normal boiling point values are important, particularly with regard to the separation and distillation / condensation plant. Especially used are separators and dehydrators which usually operate at a temperature of between 100 ° C and 150 ° C to separate oil, gas and condensate as defined above.
    [0003] Therefore, in yet another preferred embodiment, the most suitable fracturing carrier fluids have an NBP of less than 100 ° C in order to be easily separated from recovered (liquid or gaseous) hydrocarbons and then recondensed in the gas treatment units comprising separators, compressors, heat exchangers, and the like. The same principle applies for separations, distillations or condensations at a pressure above atmospheric pressure. In another preferred embodiment, the fracturing carrier fluids according to the present invention have a critical pressure (critical P) of less than 7 MPa, preferably less than 5 MPa, so that the compression tools which are 25 used for transport in the gas lines can also be used for the condensation of fracturing carrier fluids. For the sake of low toxicity after recycling, it is also desirable that the NBP fracturing carrier fluid is very far from that of benzene, toluene, ethylbenzene and xylene, which are respectively 80 ° C, 111 ° C, 136 ° C and about 140 ° C. Therefore NBP below 60 ° C is preferable when the recovered hydrocarbons comprise one or more component (s) selected from benzene, toluene, ethylbenzene and xylene. Therefore, a suitable fracturing carrier fluid, in addition to having a NBP of 0 ° C to 65 ° C, preferably satisfies at least one, and preferably each of the following two requirements: a) ODP strictly less than 0.02, preferably 0.01, and more preferably 0; 3031110 b) a critical pressure equal to or less than 7 MPa, preferably equal to or less than 5 MPa. According to a preferred aspect, the fracturing carrier fluid suitable for use in the present invention has a NBP of between 0 ° C. and 65 ° C. and a critical pressure equal to or less than 7 MPa, preferably equal to or less than at 5 MPa. According to another preferred aspect, the fracturing carrier fluid according to the invention has a critical temperature equal to or greater than 110 ° C and equal to or less than 200 ° C. According to another preferred embodiment of the present invention, said at least one linear or branched hydrofluorocarbon compound is of the formula (1): ## STR1 ## in which n, m, p and q respectively represent the number of carbon atoms, hydrogen atoms, fluorine atoms and X atoms, with nk 3, m 0, p 1, q represents 0 or 1 or 2, and X represents an atom of halogen other than fluorine, and wherein the compound of formula (1) has a normal boiling point (NBP) which is between 0 ° C and 65 ° C, preferably between 5 ° C and 60 ° C, more preferably between 10 ° C and 55 ° C. It will be understood that when q is equal to 2, the atoms of X may be identical or different. Preferably q is 0 or 1. It will also be understood that the sum (m + p + q) is equal to or less than 2n + 2, where n, m, p and q represent the number of carbon atoms, d hydrogen atoms, fluorine atoms and X atoms in the compound of formula (1). Preferably, X represents chlorine, bromine or iodine, more preferably chlorine or bromine, more preferably even X represents chlorine. According to a preferred embodiment, n represents 3 or 4 or 5, preferably n represents 3 or 4. According to another preferred embodiment, m is such that 0 m 5 11. According to yet another embodiment of the invention, In this embodiment, the carbon atoms in the compound of the formula (1) can be arranged in a straight or branched chain. Preferably, the compound of formula (1) has one or one carbon-carbon double bond. Preferably, the compound of formula (1) has a carbon-carbon double bond when q is 2. [0050] According to a particularly preferred embodiment of the present invention, the compound of formula (1) above has a critical temperature equal to or greater than 110 ° C and equal to or less than 200 ° C, preferably equal to or greater than 130 ° C and equal to or less than 200 ° C. According to a particularly preferred embodiment of the present invention, the compound of formula (1) above has the formula CnI-1, FpXq, where n is 3 or 4, 0 m 5 7, 5, 5, 9, and q represents 0 or 1. Also preferred are compounds of the formula (1) wherein each of the carbon atoms bears at least one fluorine atom. Nonlimiting examples of compounds of formula (1) which are useful in the present invention include 1,1,1,3-tetrafluoropropane, 1,1,2,2,3-pentafluoropropane, 1, 1,1,3,3-pentafluoropropane, 1,1,1,2,3,3-hexafluoropropane, 1,3-difluoropropane, 1-chloro-3,3,3-trifluoropropene, 1,1, 3,3-tetrafluoropropane, 1,2,2,3-tetrafluoropropane, 1,1,1,2,2,4,4,4-octafluorobutane, 1,1,1,2,2,3, 3,4-octafluorobutane, 1,1,1,2,2,3,3,4,4-nonafluorobutane and mixtures of two or more thereof in any proportion. The thermodynamic properties of the compounds of formula (1), as defined above with their critical temperature and their NBP, allow easy handling of the fracturing carrier fluid and easy separation of the fluid. Fracturing carrier of recovered hydrocarbons. In addition, it has surprisingly been found that fracturing carrier fluids comprising at least one fluorinated compound of formula (1) above, having the thermodynamic characteristics mentioned above, contribute to facilitating handling and use, allow a sedimentation rate of the proppant in the fracturing carrier fluid that is equal to or less than that of known fracturing carrier fluids, and as close as possible or preferably less than the sedimentation rate in water within a wide range of subterranean formation temperatures, preferably between 20 ° C and 200 ° C. [0054] According to another preferred embodiment, the fracturing carrier fluid according to the invention has a critical pressure of less than 70 bar (7 MPa), preferably less than 50 bar (5 MPa), while Carbon (CO2) has a critical pressure of 73 bar (7.3 MPa). This therefore constitutes another advantage of the fluid of the present invention which is liquid at a lower pressure value, in other words less pressure is sufficient to obtain the liquid fracturing fluid. In addition, the use of compounds of the formula (1) has many advantages, particularly compared to the use of water as a carrier fluid fracturing. Among these advantages, we can mention: a low, or even an absence of solubilization of the mineral salts present in the underground formations, and consequently a process for recycling the fracturing carrier fluid which is cheaper and more simple, an impact less on the integrity of the subterranean formation (eg minimized or even no swelling of the subterranean formation), and the like. According to a preferred embodiment, the fracturing carrier fluid according to the invention contains no toxic or harmful aromatic compounds, such as benzene, toluene, ethylbenzene and xylene, unlike known fracturing oils. which can still be used. The fracturing carrier fluid may also comprise one or more additive (s) well known to those skilled in the art. Examples of such additives include, as a non-limiting list, biocides, corrosion inhibitors, surfactants (e.g., fluorinated surfactants), deposit inhibitors, anti-foaming agents, rheology modifiers ( for example, viscosity enhancers, drag reducers, etc.) and the like, as well as mixtures of two or more of the additives listed above, in any proportions. For example, drag reducers are used to reduce friction and to increase the flow rate at constant pumping, biocides are used to protect the drag reducer against biodegradation, corrosion inhibitors are used to protect the equipment against corrosion, surfactants are used to increase the impregnation of the fracturing fluid on the surfaces of the equipment and / or to promote its foaming, and deposit inhibitors are used to prevent deposits from of formation water. In another aspect, the present invention relates to a fracturing fluid comprising at least one fracturing carrier fluid as defined above and proppants. The proppants which can be used in the fracturing fluid according to the invention are any type of proppants known to those skilled in the art, and are usually in the form of granular materials. Typical proppants include sand, resin-coated sand, intermediate-strength retaining ceramics, high-strength proppants such as sintered bauxite and zirconium oxide, plastic granules, plastic granules and the like. steel shot, glass beads, high strength glass beads, aluminum pellets, rounded nut shells, and the like. Supporting agents which can be used are of all types known in the art, from mesh US 12 to mesh US 100, preferably mesh US 20 mesh US 100. The largest proppants are generally 35 sieved with mesh screens US 20 and US 40, that is to say they pass through a sieve which has a mesh size of 850 pm and they do not pass through a sieve which has a mesh size of 425 μm. These proppants are particularly suitable for use in groundwater. The concentration of proppant is essentially between 20 grams and 600 grams per liter of fracturing carrier fluid, more preferably between 25 grams and 250 grams per liter of fracturing carrier fluid. In yet another aspect, the present invention relates to a method of fracturing a subterranean formation using the fracturing fluid as defined above. The fracturing method according to the present invention comprises at least the following steps: a) providing a fracturing carrier fluid comprising at least one compound of the formula (1) as defined above, with compression and / or cooling optional (s) to, such that the fracturing carrier fluid is in the form of a liquid; b) preparing a fracturing fluid by mixing the liquid fracturing carrier fluid of step a) with proppants in a vessel so as to obtain a liquid fracturing fluid; and c) injecting said liquid fracturing fluid of step b) (i.e., a liquid dispersion) into a subterranean formation at a pressure sufficient to open one or more fractures in it. The compression in step a) can be carried out using any method known to those skilled in the art, and for example by means of a pump, to a pressure greater than gas-liquid equilibrium pressure. The cooling in step a) can be carried out using any method known to those skilled in the art, and for example using a heat exchanger, at a temperature below the temperature of 30.degree. gas-liquid balance. Before step a) of the process according to the invention, the subterranean formation may be pre-treated by injecting the fracturing carrier fluid according to the invention as a liquid without a proppant, and / or by injecting liquid water and / or liquid hydrocarbons and / or a foam composed of water or hydrocarbons mixed with a gas.
    [0004] According to another alternative, the formation may be rinsed after step c) by injecting the fracturing carrier fluid according to the invention without a proppant or liquid water or liquid hydrocarbon, or finally a foam composed of water or hydrocarbons mixed with a gas. The process of the invention may be preceded and / or combined and / or followed by one or more known fracturing processes, which use ground water, gelled water or gelled water. , hydrocarbons, gelled hydrocarbons, foam fluids, and the like. The method of the invention also includes the recycling of any fracturing fluid or pretreatment fluid or rinsing fluid, which does not contain any proppants, or at least a small amount of agent. (s) of support. This recycling of the fracturing carrier fluid according to the invention, after its use as a fracturing fluid or as a pretreatment fluid or as a rinsing fluid for a fracturing operation, comprises at least the following steps: - recovering, by pumping and or by decompression (for example return to a normal pressure), at least a portion of the fluid and a portion of the hydrocarbons initially present in the formation, the fluid being the fracturing carrier fluid, from the hydrocarbon reservoir in order to produce the recovered fluid; separating from the recovered fluid the fracturing carrier fluid in order to obtain a gas or a liquid, alone or mixed with hydrocarbons, by means of any technique known in the art, comprising for example one or more separator (s) , one or more dehydrators, variations in temperature, pressure and time, and the like. [0067] As described above, the fracturing carrier fluid for use in the present invention allows a reduced sedimentation rate of the proppant particles that is dispersed therein. The theoretical sedimentation rate (v1) of a single spherical regular particle at a given equilibrium temperature and a given equilibrium pressure in a fluid is calculated using the following empirical equations (1) by Fergusson and Church , published in the "Journal of Sedimentary Research", (volume 74, No. 6, November 25 2004, pages 933 to 937), which corresponds to the maximum speed or the terminal velocity or the limiting speed: Rgd 2 V = (1) 18v + V0.75 x 0.4Rgd3 where R = OP (2) P fluid and, replacing R of equation (2) in equation (1), the following equation is obtained: allows to calculate the sedimentation rate "v1", expressed in ms "1: gd2Ap vi = (18iffinde + J0.75 x 0.4dgpfluidAp) in which" vfluiden is the kinematic viscosity of the carrier fluid, expressed as the ratio unfluid / Pfluide "," rlfluid "is the dynamic viscosity of the carrier fluid in Pa.s," g "is the constant of gravity acceleration (9.81 ms-2), "d" is the particle diameter expressed in meters, "rfluid" is the density of the carrier fluid expressed in kg.m-3, and "Op" is the Difference in density between the particle and the carrier fluid in the liquid phase, expressed in kg.rn-3. In the calculations that follow, the particle density is defined as the density value of quartz which is 2650 kg.m3 because quartz sand is often used as a proppant. By way of example, a regular particle having a diameter of 425 μm and a density of 2650 kg.m-3 has a sedimentation rate in the fracturing carrier fluid according to the invention which is lower than that in water. in a temperature range equal to or greater than 65 ° C - 75 ° C. The same regular particle in the 1,1,1,2,3,3,3-heptafluoropropane (R227ea) fluorinated hydrocarbon has a higher sedimentation rate than that in water within a temperature range. from 10 ° C to 190 ° C. The critical pressure and the critical temperature of a fluid are measured in the following way: the measurement principle is based on the variation of the heat capacity during the phase during which the state changes during heating to 0.2. ° C per minute. A closed test cell is filled with about 1 g of the fluid sample and can then thermally equilibrate before heating is started. The transition is detected by the heat flux exchanged by the test cell which contains the fluid sample using a calorimeter which makes it possible to know the critical temperature defined by the starting point. The critical temperature is graphically defined as the temperature that corresponds to the intersection of the slopes before and after the transition in the heat flow curve (starting point). The pressure in the cell is measured continuously during heating of the test cell. The value of the pressure reached at the temperature which corresponds to the critical temperature is read directly, and the critical pressure is calculated by taking into account the experimental correction of the pressure transducer due to the effect of the temperature on the transducer response. which is measured via calibration. To determine the critical temperature and the critical pressure, a C80 calorimeter sold by Setaram is used. The accuracy for the critical temperature is 0.5 ° C and for the critical pressure is 0.4 bar (40 kPa). In order to measure the density of the liquid in the liquid phase, the procedure used is as follows: 1) wash and dry the tank; 2) evacuate; 3) weigh the tank; 4) charging said tank with the test fluid; 5) weighing said vessel again to obtain the weight of the added test fluid; 6) allow the temperature to equilibrate to the test temperature; 7) record the volume of liquid; 8) calculate the density. The method for calculating the density of the liquid (in kg.m-3) is reproduced below with a definition of the variables: Density of the liquid = ihq = - mvap) - (Vvap X dvap)) (m - ((Vtot - Vliq) X dvap))) Vliq Vliq Vliq Vliq in which - Vtot (total volume of the vat) is equal to Vhq + Vvap, where Vhq is the volume of liquid measured in the vat, and Vvap is the volume of gas in the tank, - m (total mass of fluid added to the tank) is equal to li mg Mvap, is the mass - 10 of liquid, and mvap is the mass of gas, and - dvap is the density of the gas at temperature T. [0074] The density of the gas is calculated using the ideal gas law. The accuracy for the temperature is 0.2 ° C. The accuracy for the density of the liquid is 0.1%. To obtain the value of the dynamic viscosity, the measured kinematic viscosity is multiplied by the density of the liquid. Kinematic viscosity is measured using Cannon-Fenske Ostwald brand viscometers. The viscometers are calibrated at each temperature with fluids whose viscosity is known. An Ostwald-type viscosity tube consists of a U-shaped glass tube which is held vertically in a temperature-controlled bath. In one limb of the U is a narrow narrow bore section which is called the capillary. On top of it is a bulb, and another bulb is provided at the foot of the other branch. In use, a liquid is sucked into the upper bulb by suction and can then flow down through the capillary into the lower bulb. Two marks (one above and one below the lower bulb) indicate a known volume. The time required for the liquid level to pass between these marks is proportional to the kinematic viscosity. Although the tubes have a conversion factor, each tube used in the measurement program described has been calibrated by a fluid whose properties are known at each temperature. The time required for the test liquid to flow through a known diameter capillary having a certain factor between two marked points is measured. By multiplying the time required by the factor of the viscometer, the kinematic viscosity is obtained. The viscometers were immersed in a controlled constant temperature bath at ± 0.2 ° C. The viscosity data obtained using this procedure is accurate to within ± 2%. The calculation and measurement methods described above make it possible to evaluate the viscosity and the density as a function of temperature for fracturing carrier fluids of the prior art, and then to finally calculate the speed. sedimentation of a proppant in said fracturing carrier fluids of the prior art. Figure 1 shows the sedimentation rate in different fluids of the prior art as a function of temperature. Taking into account the accuracy of the calculation, a particle having a diameter of 425 μm and a density of 2650 kg.m-3 has a sedimentation rate in the R-227ea equivalent to that in the water in the temperature range. 35 ° C - 60 ° C, outside this range the sedimentation rate is higher than that in water. R1234yf and R1234ze (E), which each have 3 carbon atoms, 2 hydrogen atoms, 4 fluorine atoms and 1 carbon-carbon double bond, give a sedimentation rate which is always greater than that in water, and are not part of the invention. Figure 1 also shows the sedimentation rate in a fracturing carrier fluid according to the invention, R-1233zd, which is equal to that in water over a wider range of temperatures. R-1233zd, which has 3 carbon atoms, 2 hydrogen atoms, 3 fluorine atoms, 1 chlorine atom and 1 carbon-carbon double bond gives a sedimentation rate which is lower than that observed in water in the range of 50 ° C to 100 ° C. R-1233zd is part of the invention. Sedimentation rate values, as a function of temperature, for various fracturing carrier fluids according to the invention as well as for water, are presented in FIG. 2. In R-245ca, which has 3 carbon atoms, 3 hydrogen atoms and 5 fluorine atoms, a particle having a diameter of 425 μm and a density of 2650 kg.m-3, has a sedimentation rate lower than that in water in the range of 10 ° C to 140 ° C. R-245ca is part of the invention. In R-245fa, which also has 3 carbon atoms, 3 hydrogen atoms and 5 fluorine atoms, a particle having a diameter of 425 μm and a density of 2650 kg.m-3, presents a Sedimentation rate lower than that in water in the range 25 ° C to 105 ° C. R-245fa is part of the invention. In R-236ea, which also has 3 carbon atoms, 2 hydrogen atoms and 6 fluorine atoms, a particle having a diameter of 425 μm and a density of 2650 kg.m-3 has a velocity of sedimentation lower than that in water in the range 20 ° C to 105 ° C. R-236ea is part of the invention. Table 1 below shows several compounds of formula (1) which may be useful in the practice of the present invention: R-1233zd, R-245ca, R-245fa and R236ea all have a NBP greater than 0 ° C and a critical temperature greater than 110 ° C. Table 1 - Compound NBP (° C) Tc (° C) R-227ea -16.3 102 R-1234yf -29.4 95 R-1234ze (E) -19 109 R-245fa 15 154 R-236ea 6 139 R-1233zd 20 165 R-245ca 25 174
    权利要求:
    Claims (12)
    [0001]
    REVENDICATIONS1. A fracturing carrier fluid for fracturing an underground formation, said fracturing carrier fluid comprising at least one linear or branched hydrofluorocarbon compound having a boiling point at a pressure of 1 atmosphere (101,325 Pa), which is between 0 ° C and 65 ° C. 10
    [0002]
    The fracturing carrier fluid of claim 1 which has a critical temperature of 110 ° C or higher and 200 ° C or less.
    [0003]
    3. Fracturing carrier fluid according to claim 1, wherein said at least one linear or branched hydrofluorocarbon compound is of the formula (1): CnI-1,, Fp; (1) wherein n, m, p and q represent respectively the number of carbon atoms, hydrogen atoms, fluorine atoms and X atoms, with nk 3, m 0, p 1 , q represents 0 or 1 or 2, and X represents a halogen atom other than fluorine, and wherein the compound of formula (1) has a normal boiling point (NBP) which is between 0 ° C. and 65 ° C, preferably between 5 ° C and 60 ° C, more preferably between 10 ° C and 55 ° C.
    [0004]
    The fracturing carrier fluid according to claim 3, wherein said at least one linear or branched hydrofluorocarbon compound is of the formula (1) where n is 3 or 4, 25 M 5 7, 3
    [0005]
    5. p 5 9, and q represents 0 or 1. 5. Fracturing carrier fluid according to any one of the preceding claims, wherein said at least one hydrofluorocarbon compound is selected from the group consisting of 1,1,1,3- tetrafluoropropane, 1,1,2,2,3-pentafluoropropane, 1,1,1,3,3-pentafluoropropane, 1,1,1,2,3,3-hexafluoropropane, 1,3-difluoropropane , 1-chloro-3,3,3-trifluoropropene, 1,1,3,3-tetrafluoropropane, 1,2,2,3-tetrafluoropropane, 1,1,1,2,2,4,4 , 4-octafluorobutane, 1,1,1,2,2,3,3,4-octafluorobutane, 1,1,1,2,2,3,3,4,4-nonafluorobutane and mixtures of two or more than two of these, in any proportions. 35 3031110 - 21 -
    [0006]
    6. Fracturing carrier fluid according to any one of the preceding claims, further comprising one or more additive (s) chosen (s) from biocides, corrosion inhibitors, surfactants, deposit inhibitors, anti-corrosive agents, foamers, rheology modifiers, and the like, as well as mixtures of two or more of the additives listed above in any proportions.
    [0007]
    7. Fracturing fluid comprising at least one fracturing carrier fluid according to any one of the preceding claims and proppants.
    [0008]
    The fracturing fluid of claim 7, wherein the proppants are selected from sand, resin-coated sand, intermediate-strength retaining ceramics, high-strength proppants, plastic granules, steel shot, glass beads, high strength glass beads, aluminum pellets, rounded nut shells, and the like.
    [0009]
    The fracturing fluid of claim 7 or 8, wherein the concentration of proppant is between 20 grams and 600 grams per liter of fracturing carrier fluid, more preferably between 25 grams and 250 grams per liter of carrier fluid. fracturing.
    [0010]
    A method of fracturing a subterranean formation using the fracturing fluid according to any one of claims 7 to 9, comprising at least the following steps: a) providing a fracturing carrier fluid according to any one of claims 1 to 6 , with optional compression and / or cooling (s), such that the fracturing carrier fluid is in the form of a liquid; b) preparing a fracturing fluid by mixing the liquid fracturing carrier fluid of step a) with proppants in a tank so as to obtain a liquid fracturing fluid; and c) injecting said liquid fracturing fluid of step b) into a subterranean formation at a pressure sufficient to open one or more fractures in it.
    [0011]
    The method of claim 10, further comprising recycling the fracturing carrier fluid. 3031110 - 22 -
    [0012]
    The method of claim 10 further comprising recycling the fracturing carrier fluid, wherein said recycling comprises at least the following steps: recovering, by pumping and / or decompressing, at least a portion of the fluid and a portion of the hydrocarbons initially present in the formation, the fluid being the fracturing carrier fluid, from the hydrocarbon reservoir to produce the recovered fluid; and separating the fracturing carrier fluid from the recovered fluid in order to obtain a gas or a liquid, alone or mixed with hydrocarbons.
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    同族专利:
    公开号 | 公开日
    CA2971530A1|2016-07-07|
    US10253247B2|2019-04-09|
    US20160186046A1|2016-06-30|
    RU2673291C1|2018-11-23|
    AR103329A1|2017-05-03|
    WO2016107796A1|2016-07-07|
    CA2971530C|2019-04-16|
    AU2015373484A1|2017-07-13|
    FR3031110B1|2018-07-13|
    EP3240855A1|2017-11-08|
    AU2015373484B2|2018-05-10|
    BR112017013932A2|2018-01-09|
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    法律状态:
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    2016-07-01| PLSC| Publication of the preliminary search report|Effective date: 20160701 |
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    优先权:
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