• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 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 ether compound having a boiling point, at a pressure of 1 atmosphere, which is included between 0 ° C and 90 ° 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:FR3031111A1
    申请号:FR1463516
    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 underground formations containing fluid with fracturing fluids. BACKGROUND OF THE INVENTION [0002] Economically valuable underground fluids 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 underground formations containing fluid may also be oil or gas or condensed gas in its liquid state during its ascent to the surface, also called a condensate. 1.5 [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, underground formation near the production well or near the well. injection. 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 subterranean formations that can not produce hydrocarbons after a wellbore has been drilled and a well has been installed to enter the subterranean formation. One reason 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 hampers flow of fluids. [0006] And even for underground formations that already produce 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 treatment comprises injecting a liquid suspension, the fracturing fluid, down into the wellbore and back into the formation to an extent necessary to improve permeability. 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. [0008] 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", are dispersed in the fracturing carrier fluid and are then transported to the bottom of the fractures during the pumping operation. high pressure. The injection is continued jel; k1,1,14 4da., GireuRe fracture having sufficient dimensions 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 thin 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 and rounded nut shells. [0011] 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 of the subterranean formation containing hydrocarbons. hydrocarbons.
    [0002] In many examples this is a difficult problem that involves a considerable expense 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 efficient fracturing processes use water / o as a carrier fluid, more specifically either viscosified water or slick water (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 that 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 high enough that a substantial portion of this injected fluid is converted to 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. Avoiding sedimentation, or at least minimizing sedimentation, is important in order to maximize the transport efficiency that could be slowed down 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 3031111 (7.3 MPa) and the low critical temperature (31 ° C) make it necessary to compress the gas at a higher pressure. , 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 "Oil 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 and proppants. Viscosifying the carrier fluid, or gelling it, is useful to allow more effective transport of the proppants by increasing the friction between them and the carrier fluid. 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 limited in the horizontal portions of the surface equipment, in the wells and in the fractures. US Pat. No. 3,846,310 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 carrier fluid. hydrocarbon, 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 "011 and Gas Journal", July 5, 1971, page 60. [0020] Another disadvantage of US Patent 3846310 is the use of heptane under 1 atmosphere (101.325 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 difference), this would require expensive equipment to separate the two compounds in order to avoid heptane pollution by toluene. More recently, US 2011284230 claims a method of treating subterranean formations, 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 confining thefracturing 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, including 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, 3031111 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 neither water nor any chemical additive is used with heptafluoropropane and that, as for 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. The high volatility of R-227ea also represents 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 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 due to 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 by 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 a condensation of R-227ea which is in the gas phase after the first condensation. 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 that do not contain water and 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. Despite continuous research since 1966, there is still a need for alternative and / or improved fracturing carrier fluids that 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, that no water is added voluntarily, - 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 widest range 15 possible temperatures, for example between 20 ° C and 200 ° C, preferably between 70 ° C and 190 ° C, for a given size and nature of the proppant, - the fluid the fracturing carrier allows a sedimentation rate equal to or lower 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 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) versus carbon dioxide for 100 years integration and Ozone Depletion Potential (ODP) The GWP of R-227ea is 3220 and the ODP is 0. Propane GWP is of 20 and the ODP is 0 - the normal boiling point (or NBP) is the boiling point at a pressure of 1 atmosphere (101325 p), the transport performance of the proppant is evaluated with the sediment velocity of a single spherical solid particle (the proppant) in the flui carrier under the effect of gravity at a given temperature which corresponds to the temperature of the subsurface hydrocarbon formation; the lower the rate of sedimentation, 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 an underground formation, said fracturing carrier fluid comprising at least one linear or branched hydrofluorocarbon ether compound which has a boiling point which is between 0 ° C and 90 ° C. In the present invention, "hydrofluorocarbon ether compound" refers to a compound comprising carbon atoms, hydrogen, fluorine and optionally chlorine, and carrying at least one ether function, preferably a single ether function. 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. Preferably at 20 ° C, more preferably 25 ° C, above or below the normal boiling point of the recovered gaseous hydrocarbon which has the highest normal boiling point (respectively lower) among the mixture of gaseous hydrocarbons recovered. This makes it easier, for example, to recover 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 normal boiling point of the recovered hydrocarbon gas having the highest normal boiling point of the mixture of recovered hydrocarbons, eg butane, above 0 ° C. Among these suitable fracturing carrier fluids, the preferred ones are those which have a high normal boiling point, preferably greater than 0 ° C, more preferably greater than 10 ° C, more preferably greater than 20 ° C. The most preferred fracturing carrier fluids are those which have a normal boiling point above room temperature, so 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 which are liquid at room temperature is their ease of storage and use. These issues relating to ease of separation and the values of normal boiling points 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 100 ° C to 150 ° C to separate oil, gas and condensate as defined above. 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 again. in gas treatment units comprising separators, compressors, heat exchangers, and the like. The same principle applies to 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 (P, critical) less than 7 MPa, preferably less than 5 MPa, so that the tools compressors that are used for transport in gas lines can also be used for condensation of fracturing fluids. [0040] In the interest of low toxicity after recycling, it is also desirable that the NBP of the fracturing carrier fluid be very far from that of benzene, toluene, ethylbenzene and xylene, which are respectively of 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 between 0 ° C. and 90 ° C., preferably satisfies at least one, and preferably each of the following two requirements: a) An ODP strictly less than 0.02, preferably 0.01, and more preferably 0; 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 90 ° C and a critical pressure of 7 MPa or less, 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 lower than 200 ° C. According to another preferred embodiment of the present invention, said at least one linear or branched hydrofluorocarbon ether compound is of the formula (1): CnElmFpXgOt (1) in which n, m, p, q and t respectively represent the number of carbon atoms, hydrogen atoms, fluorine atoms, X atoms and O atoms (i.e. the number of ether function (s)) where n is 2 or 3 or 4, m 0, 9 p _k 3, q is 0 or 1, t is 1 or 2, and X is a halogen other than fluorine, and O is a oxygen atom, and wherein the compound of formula (1) has a normal boiling point (NBP) which is between 0 ° C and 90 ° C, preferably between 5 ° C and 85 ° C, more preferably between 10 ° C and 80 ° C. It will be understood that when q is 2, the atoms of X may be the same 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, respectively. hydrogen atoms, fluorine atoms and X atoms in the compound of formula (1). [0046] 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 2 or 3 or 4, m k 2 and the hydrogen atoms are borne by at least 2 different carbon atoms. According to another preferred embodiment, n represents 2 or 3. According to yet another embodiment, n represents 2 or 3, m k 2 and the hydrogen atoms are borne by at least 2 different carbon atoms. According to a further embodiment, t is 1. The carbon atoms in the compound of formula (1) may be arranged in a straight or branched chain. Preferably, the compound of formula (1) has 20 or 1 carbon-carbon double bond. 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 equal to 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 C, 1-1, FpXgOt in which n is 2 or 3, 2 m 5 , 4 5 p 5. 6, and q represents 0 or 1 and t represents 1. Also preferred are the compounds of the formula (1) in which m 2 and the hydrogen atoms are borne by at least 2 different carbon atoms . Non-limiting examples of compounds of formula (1) which are useful in the present invention include RE-134, RE-.236fa 1, RE-236ea1, RE-245cb1, RE-338mcf2 , RE-245fa1, RE-347mmy1, RE-254cb1, RE-245ca2, RE235da1, RE-365mcf2, CHF2-CHF-O-CHF2, CHF2-CH2-O-CF3, CH2- CHF-0-CF3, CH3-CF2-O-CF3, CF3-CHF-O-CH2F, CHF2-CF2-O-CH2F, the isomers of the above-listed compounds, as well as mixtures of two or more than two of the above compounds, in any proportions. 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 as well as a separation. easy fluid carrier fracturing recovered hydrocarbons. Furthermore, 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 the 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 the water, within a wide range of subterranean formation temperatures, preferably between 20 ° C and 200 ° C. 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, in particular compared to the use of water as a fracturing carrier fluid. Among these advantages, we can mention: a low or no solubilization of the mineral salts present in the underground formations, and consequently a process for recycling the fracturing carrier fluid that is cheaper and simpler, a lesser impact on the integrity of the subterranean formation (e.g., 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 (eg 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 In the case of corrosion equipment, 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 the 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, polyesters, and the like. steel grit, glass beads, high strength glass beads, aluminum pellets, rounded nut shells, and the like. Retaining agents that can be used are of all types known in the art, mesh US 12 mesh US 100, preferably the mesh. US 20 to US 100 mesh. Larger proppants are generally sieved with US 20 and US 40 mesh screens, i.e. 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 pm. These proppants are particularly suitable for use in groundwater. The concentration of proppant is generally 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, as defined above, that is to say comprising at least one compound of the formula (1) ) as defined above, with optional compression and / or cooling (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 tank 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 using a pump, up to a higher pressure. at the 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 equilibrium temperature. gas-liquid. 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. 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 groundwater, gelled water, hydrocarbons, gelled hydrocarbons, foam fluids, and the like. The method of the invention also comprises the recycling of any fracturing fluid or pretreatment fluid or rinsing fluid, which contains no proppant, or at least a small amount of agent ( s) of support.
    [0003] 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 stages: recovering, by pumping and / or by decompression (eg return to 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 so to produce the recovered fluid; - Separating from the recovered fluid the fracturing carrier fluid to obtain a gas or a liquid, alone or mixed with hydrocarbons, using any technique known in the art, including for example one or more separator (s) one or more dehydrators, variations in temperature, pressure and time, and the like. As described above, the fracturing carrier fluid to be used in the present invention allows a reduced sedimentation rate of the proppant particles that is dispersed therein. The theoretical sedimentation rate (vi) of a single regular spherical 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 2004, pages 933 to 937), which corresponds to the maximum speed or the terminal speed or the speed limit: vi = 1 8V 0)) 1 / 0.75 x 0.4Rgd3 Rgd2 in which R = Ap (2) P fluid and, replacing R of equation (2) in equation (1), we obtain the following equation which allows to calculate the sedimentation rate "v1", expressed in ms-1: gd2-AP (11 fluid + 0.75 x 0.4d3 gp Ap fluid) in which "vfluid" is the kinematic viscosity of the carrier fluid, expressed as the "fluid" , "rin rapport" "fluidfluide" is the dynamic viscosity of the carrier fluid Pa.s, "g" is the constant access queue leration of gravity (9.81 ms-2), "d" is the particle diameter expressed in meters, n "rfluiden is the density of the carrier fluid expressed in kg.m-3, and" Ap "is the difference in density between the particle and the carrier fluid in the liquid phase, expressed in kg.m-3. By way of example for the calculation of the sedimentation rate, quartz sand particles may be chosen since quartz sand is often used as a propping agent. Quartz sand particle density is defined as the density value of the quae which is 2650 kg.m-3. By way of example, a regular particle having a diameter of 425 μm and a density of 2650 kg.rn-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 range of 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 / o 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 that 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 response of the transducer which is measured through 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). 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) again weighing said vessel 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.rn-3) is reproduced below with a definition of the variables: Density of the liquid mliq (m - mvap) (m - (Vvap X dvap)) - (m - ((Vtot - Vliq) X dvap))) = Vliq Vliq Vliq Vliq 30 in which Vtot (total volume of the vat) is equal to Vio + Vvap, where Viiq 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 m ... ho + mvap, where mlio is the mass of liquid, and mvap is the mass of gas, and Dvap is the density of the gas at temperature T. 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 that is called the capillary. Above 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 spots 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 the temperature for fracturing carrier fluids of the prior art, and then finally to calculate the sedimentation rate. a proppant in said prior art fracturing fluids. Table 1 below shows several compounds of the formula (1) which may be useful in the practice of the present invention: RE-134, RE-236fa1, RE-236ea1, RE-245cb1, RE-338mcf2, RE-245fa1, RE-347mmy1, RE-254cb1, RE-245ca2 and RE-235da1 all have NBP greater than 0 ° C. 3031111 - 18 - - Table 1 -, Compound NBP (° C) Tc (° C) R-227ea -16 102 RE-125 42 81 RE-143a 24 105 RE-134 5.5 147! RE-236fa1 6 -129 RE-236ea1 23 -. RE-245cb1 6 134 RE-338mcf2 28 148 REeadefal 29 171 RE-347mmy1 29 161 RE-254cb1 35 - RE-245ca2 43 189
    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 ether compound having a boiling point at a pressure of 1 atmosphere (101,325 Pa), which is included between 0 ° C and 90 ° C.
    [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 ether compound is of the formula (1): ## STR2 ## wherein n, m, p, q and t respectively represent the number of carbon atoms, hydrogen atoms, fluorine atoms, X atoms and O atoms (i.e. the number of ether function (s)), where n is 2 or 3 or 4, m 0, 9> pk 3, q is 0 or 1, t is 1 or 2, and X is a halogen atom other than fluorine, and O represents an oxygen atom, and wherein the compound of formula (1) has a normal boiling point (NBP) which is between 0 ° C and 90 ° C, preferably between 5 ° C and 85 ° C, more preferably between 10 ° C and 80 ° C.
    [0004]
    The fracturing carrier fluid according to claim 3, wherein said at least one linear or branched hydrofluorocarbon ether compound is of the formula (1) where n is 2 or 3, 5 m, 4, 4 and 6 , q represents 0 or 1 and t represents 1.
    [0005]
    The fracturing carrier fluid according to any one of the preceding claims, wherein said at least one hydrofluorocarbon ether compound is selected from RE-134, RE-236fa1, RE-236ea1, RE-245cb1, RE-338mcf2, RE-245fa1, RE-347mmy1, RE-254cb1, RE-245ca2, RE-235da1, RE-365mcf2, CHF2-CF-IF-0-CHF2, CF1F2-CF- 12-0-CF3, CH2-C1-1F-O-CF3, CH3-CF2-O-CF3, CF3-CHF-O-CH2F, CHF2-CF2-O-CH2F, isomers of the compounds listed herein above, as well as mixtures of two or more of the above compounds, in any proportions. 3031111 - 20 -
    [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. 10
    [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. 15
    [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. 20
    [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 therein.
    [0011]
    The method of claim 10, further comprising recycling the fracturing carrier fluid. 3031111 -21-
    [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 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.
    类似技术:
    公开号 | 公开日 | 专利标题
    Tumba et al.2011|Phase equilibria of methane and carbon dioxide clathrate hydrates in the presence of aqueous solutions of tributylmethylphosphonium methylsulfate ionic liquid
    CA2721573C|2017-01-03|Solvent assisted oil recovery
    CA2996882C|2020-08-18|Use of gaseous phase natural gas as a carrier fluid during a well intervention operation
    FR3031111A1|2016-07-01|
    FR3031110A1|2016-07-01|
    Mohsenzadeh et al.2015|Effects of concentration, salinity and injection scenario of ionic liquids analogue in heavy oil recovery enhancement
    RU2652049C1|2018-04-24|Method of gasocyclic injection of liquid carbon dioxide under supercritical conditions in the oil producing well
    US11155750B2|2021-10-26|Use of natural gas as a soluble servicing gas during a well intervention operation
    Gupta et al.2019|Phase equilibrium of methane hydrate in aqueous solutions of polyacrylamide, xanthan gum, and guar gum
    FR3059039A1|2018-05-25|NANOEMULSIONS FOR USE IN SUBTERRANEAN FRACTURING TREATMENTS
    Mahmoud2014|Effect of elemental-sulfur deposition on the rock petrophysical properties in sour-gas reservoirs
    FR2890395A1|2007-03-09|METHOD AND THERMODYNAMIC INHIBITORS OF GAS HYDRATES IN WATER-BASED FLUIDS
    Atsenuwa et al.2014|Effect of Viscosity of Heavy Oil Class-A on Oil Recovery in SP Flooding Using Lauryl Sulphate and Gum Arabic
    Kelland et al.2021|Powerful Synergy of Acetylenic Diol Surfactants with Kinetic Hydrate Inhibitor Polymers—Choosing the Correct Synergist Aqueous Solubility
    RU2586356C1|2016-06-10|Composition and method for increasing oil recovery of oil reservoirs
    FR3073859A1|2019-05-24|SURFACE ACTIVE AGENT FOR WELL STIMULATION
    US10907088B2|2021-02-02|Use of natural gas as a vaporizing gas in a well intervention operation
    Burrows et al.2021|CO2-soluble surfactants for enhanced oil recovery from shale
    WO2016110655A1|2016-07-14|Injectivity additive
    RU2684786C2|2019-04-15|Borehole fluids and method for use thereof
    WO2016110654A1|2016-07-14|Injectivity additive
    US20130098467A1|2013-04-25|Method for improving the flow conditions in pipes that have been used for transporting heavy or extra-heavy crudes or crudes with high asphaltene content
    FR2961551A1|2011-12-23|Preparing hydrocarbons comprises extracting fluid in subterranean formation, separating fluid in liquid and gaseous phases, injecting compound inhibiting formation of hydrates, transporting liquid and gaseous phases in pipe and recovering
    同族专利:
    公开号 | 公开日
    US20160186047A1|2016-06-30|
    AU2015373485B2|2018-11-29|
    US10308867B2|2019-06-04|
    WO2016107797A1|2016-07-07|
    FR3031111B1|2018-07-20|
    CA2971510A1|2016-07-07|
    RU2667536C1|2018-09-21|
    CA2971510C|2019-04-16|
    AR103331A1|2017-05-03|
    AU2015373485A1|2017-07-13|
    EP3240944A1|2017-11-08|
    BR112017014175A2|2018-03-06|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    WO1997020599A1|1995-12-04|1997-06-12|Mainstream Engineering Corporation|Fire extinguishing methods and blends utilizing fluorinated hydrocarbon ethers|
    CA2356081A1|1998-12-11|2000-06-22|Minnesota Mining And Manufacturing Company|Foamed nitrogen in liquid co2 for fracturing|
    WO2000036272A1|1998-12-11|2000-06-22|Minnesota Mining & Manufacturing Company|Foamed nitrogen in liquid co2 for fracturing|
    US368627A|1887-08-23|Half to adolph mack |
    US3368627A|1966-03-21|1968-02-13|Dow Chemical Co|Method of well treatment employing volatile fluid composition|
    US3846310A|1972-03-03|1974-11-05|Exxon Production Research Co|Hydraulic fracturing method using gelled hydrocarbons|
    US5211873A|1991-10-04|1993-05-18|Minnesota Mining And Manufacturing Company|Fine-celled plastic foam containing fluorochemical blowing agent|
    US5925611A|1995-01-20|1999-07-20|Minnesota Mining And Manufacturing Company|Cleaning process and composition|
    US7595281B2|2005-05-18|2009-09-29|Halliburton Energy Services, Inc.|Methods to increase recovery of treatment fluid following stimulation of a subterranean formation comprising in situ fluorocarbon coated particles|
    US20060264334A1|2005-05-18|2006-11-23|Bj Services Company|Non-damaging fracturing fluids and methods for their use|
    EP1837325A1|2006-03-24|2007-09-26|SOLVAY |Process for the manufacture of 1,1,1,3,3-pentafluoropropane|
    US20090095014A1|2007-10-12|2009-04-16|Andrew Sun|Working fluid of a blend of 1,1,1,2-tetrafluoroethane, 1,1,1,2,3,3,3-heptafluoropropane, and 1,1,1,3,3,3-hexafluoropropane and method and apparatus for using|
    US20100051272A1|2008-09-02|2010-03-04|Gas-Frac Energy Services Inc.|Liquified petroleum gas fracturing methods|
    WO2010080353A2|2008-12-18|2010-07-15|3M Innovative Properties Company|Method of contacting hydrocarbon-bearing formations with fluorinated phosphate and phosphonate compositions|
    JP5945883B2|2011-11-25|2016-07-05|矢崎総業株式会社|Wire harness with clip and wire harness provided with the wire harness with clip|
    WO2014138468A1|2013-03-07|2014-09-12|Prostim Labs, Llc|Fracturing systems and methods for a wellbore|
    FR3003569B1|2013-03-20|2015-12-25|Arkema France|COMPOSITION COMPRISING HF AND 1,3,3,3-TETRAFLUOROPROPENE|US20170218260A1|2016-01-28|2017-08-03|Neilin Chakrabarty|DME Fracing|
    RU2749223C1|2020-03-27|2021-06-07|Общество с ограниченной ответственностью «ГеоСплит»|Method of qualitative and quantitative estimation of downhole gas inflows in multistage hydraulic fracturing in a multiphase flow system|
    RU2759874C1|2021-03-04|2021-11-18|Шлюмберже Текнолоджи Б.В.|Method and system for measuring the interfacial tension between two fluids|
    法律状态:
    2015-11-10| PLFP| Fee payment|Year of fee payment: 2 |
    2016-07-01| PLSC| Publication of the preliminary search report|Effective date: 20160701 |
    2016-11-11| PLFP| Fee payment|Year of fee payment: 3 |
    2017-11-13| PLFP| Fee payment|Year of fee payment: 4 |
    2019-11-14| PLFP| Fee payment|Year of fee payment: 6 |
    2020-11-12| PLFP| Fee payment|Year of fee payment: 7 |
    2021-11-15| PLFP| Fee payment|Year of fee payment: 8 |
    优先权:
    申请号 | 申请日 | 专利标题
    FR1463516|2014-12-31|
    FR1463516A|FR3031111B1|2014-12-31|2014-12-31|FLUID COMPOSITION FOR STIMULATION IN THE FIELD OF OIL AND GAS PRODUCTION|FR1463516A| FR3031111B1|2014-12-31|2014-12-31|FLUID COMPOSITION FOR STIMULATION IN THE FIELD OF OIL AND GAS PRODUCTION|
    AU2015373485A| AU2015373485B2|2014-12-31|2015-12-22|Fluoroether fluid composition and method for stimulation in the field of oil and gas production|
    RU2017126989A| RU2667536C1|2014-12-31|2015-12-22|Composition of fluid for intensification of oil and gas production|
    BR112017014175A| BR112017014175A2|2014-12-31|2015-12-22|fluoroether fluid composition and method for stimulation in the field of oil and gas production|
    CA2971510A| CA2971510C|2014-12-31|2015-12-22|Fluid composition for stimulation in the field of oil and gas production|
    EP15813463.5A| EP3240944A1|2014-12-31|2015-12-22|Fluoroether fluid composition and method for stimulation in the field of oil and gas production|
    PCT/EP2015/081021| WO2016107797A1|2014-12-31|2015-12-22|Fluoroether fluid composition and method for stimulation in the field of oil and gas production|
    ARP150104349A| AR103331A1|2014-12-31|2015-12-30|FLOSS COMPOSITION FOR STIMULATION IN THE FIELD OF OIL AND GAS PRODUCTION|
    US14/983,879| US10308867B2|2014-12-31|2015-12-30|Fluid composition and method for stimulation in the field of oil and gas production|
    [返回顶部]