hp dsc can be used to determine the gas hydrate dissociation equilibrium points for any type of well fluid , as claimed by document u . s . pat . no . 6 , 571 , 604 . from this technique , it is also possible to determine the anti - agglomeration power of a water / oil system towards gas hydrates ( patent application fr - 04 / 08 , 058 ). other advantages of the present invention will be clear from reading the description of the non limitative examples hereafter . dsc is a technique that allows to measure the heat exchanges between a sample and a reference as a function of time or temperature . these data are collected on a curve referred to as thermogram . there are several types of dsc devices , commercially available . on the other hand , only few can work under controlled pressure . examples thereof are device dsc111 that can reach a pressure of 100 bars , and device hp micro dscvii that can reach 400 bars ( both marketed by the setaram company — france ). a detailed description of the technique and of its thermodynamic applications for hydrates can be found in various publications , notably : dalmazzone d , dalmazzone c , herzhaft b , spe journal 2002 , june , 196 - 202 ; dalmazzone d , clausse d , dalmazzone c , herzhaft b , american mineralogist 2004 , 89 , 1183 - 1191 ; le parlouër p , dalmazzone c , herzhaft b , rousseau l , mathonat c , journal of thermal analysis and calorimetry 2004 , 78 , 165 - 172 . according to the present invention that relates to kinetic studies , several types of measurement can be performed after suitable preparation of the sample to be studied . the gas that is going to form hydrates is selected ( methane for example ) and an operating pressure p 1 is set . as it has been described , it is fundamental for the sample to come in form of a stable emulsion in order to be able to carry out reliable and reproducible measurements . for oil - base well fluids ( in reverse emulsion : water - in - oil ), no specific preparation is required , except for homogenization of the sample already in form of an emulsion . muds referred to as oil - base muds are in fact at the root of emulsions of brine phase in an oil phase . in the case of multiphase oil and water effluents , a first stage consists in preparing a stable emulsion from a sampling . for water - base muds , we have an aqueous phase which , if it is studied as it is , will give , upon cooling by dsc , different responses , notably as regards the induction time . a large number of samples would have to be studied to obtain a statistical response . in this invention , we emulsify the water - base mud in a non water - miscible liquid that does not crystallize in the temperature range we are dealing with ( between − 50 ° c . and 20 ° c .). this emulsification can be performed in an oil used for manufacturing oil - base drilling fluids : mineral oil , synthetic oil based on polyalphaolefins or vegetable oil esters such as , for example , hdf 2000 or edc 99 from total solvants , or radiagreen bdmf ( vegetable oil esters ) from oleon . it is also possible to use any solvent type from petrochemistry : aromatic solvents , aliphatic solvents , isoparaffins , kerosine cuts , gasolines , gas oils , with a preference for non - aromatic solvents and oils for safety reasons . to stabilize the emulsion , any surfactant type of hlb ( hydrophile - lipophile balance ) ranging between 1 and 10 , preferably between 4 and 8 , which favours the formation of water - in - oil type emulsions can be used . non - ionic , anionic or cationic surfactants or surfactant mixtures can be used , preferably non - ionic surfactants or non - ionic , anionic mixtures . the emulsifying system described in document fr - 2 , 859 , 215 is preferably used . preparing in a vessel the oil continuous phase into which the surfactant system is incorporated , stirring until dissolution or homogeneous dispersion of the surfactant mixture in the oil phase , incorporating then the aqueous phase to be studied , dropwise , under gentle stirring , for example with a bar magnet or a low - speed homogenizer . after complete incorporation of the aqueous phase , carrying out emulsification of the system proper . this emulsification can be performed using any technique known to the person skilled in the art : shaking , shearing with a rotor / stator system of ultra - turrax or polytron type , ultrasounds , shearing in a couette type system , colloid mill , high - pressure homogenizer , etc . a rotor / stator homogenizer is preferably used . it is possible to emulsify the aqueous solution using very viscous oils such as silicone oil or paraffin oils . in this case , it is not systematically necessary to add surfactants in order to stabilize the emulsion . the viscosity of the continuous phase can provide sufficient stability . after emulsification , the sample is ready to be analyzed by dsc . after homogenization of the emulsion under gentle stirring to provide good dispersion of the droplets in the emulsion , 10 and 100 mg emulsion are taken and fed into the measuring cell of the dsc microcalorimeter . the kinetic analysis is then carried out as described below . first method : the sample in form of an emulsion is first cooled at a constant rate v 1 (− 1 to − 2 k / min ) until an exothermic peak corresponding to the crystallization of the hydrates is observed in the thermogram . the temperature corresponding to the vertex of the peak is denoted by t 1 . the sample is heated at a constant rate until an endothermic peak corresponding to the dissociation of the hydrate is observed . t 1 is always lower than equilibrium temperature t 1 diss corresponding to the hydrate dissociation temperature at pressure p 1 . the behaviour of another sample can then be compared by carrying out exactly the same experiment , at the same pressure p 1 and at the same cooling rate v 1 . a crystallization temperature t 2 is then obtained . the undercooling degree δt corresponding to the difference between the equilibrium temperature and the crystallization temperature is then calculated . the greater the undercooling degree observed , the higher the kinetic inhibiting effect . for this method , one has to ensure that only hydrate is formed during continuous cooling , therefore that a single endothermic dissociation peak corresponding to the hydrate considered is obtained , and that no ice melting peak is observed . in fact , if ice forms before or at the same time as the hydrate , this method is not sufficient . second method : the sample in form of an emulsion is cooled at a constant rate v 1 to an isotherm temperature t ′ 1 ranging between the temperature t 1 obtained by continuous cooling as explained in the first method and the equilibrium temperature t 1 diss corresponding to the hydrate dissociation temperature at pressure p 1 . if it has not been possible to determine t 1 according to the first method , one will experimentally select the isotherm temperatures below t 1 diss that allow to obtain , upon heating , a single endothermic peak corresponding to the hydrate dissociation , as explained above . various isotherms are carried out at t ′ 1 , with different durations , at p 1 ( corresponding to the undercooling degree δt 1 = t 1 diss − t ′ 1 ). for each isotherm , at the end of the durations selected , the sample is heated at a constant rate ( 1 to 2 k / min ) until the endothermic dissociation peak of the hydrate is obtained . integration of this dissociation peak allows to draw the curve of the energy released as a function of the isotherm duration . this energy is directly proportional to the amount of hydrates formed . extrapolation of the curve on the abscissa axis allows to determine a pseudo induction time t ′ 1 . the slope of the curve allows to deduce a crystallization rate . it is then possible to compare the behaviour of another sample by carrying out exactly the same experiment , at the same pressure p 1 and at the same isotherm temperature corresponding to the same undercooling degree δt 1 . the line of the curve of energy released as a function of the isotherm duration allows to obtain an induction time t ′ 2 and a crystallization rate . the greater t ′ 2 in relation to t ′ 1 , the gentler the slope of the curve , and the greater the kinetic inhibition . third method : the sample in form of an emulsion is cooled at a constant rate v 1 to an isotherm temperature t ′ 1 ranging between the temperature t 1 obtained upon continuous cooling as explained in the first method and the equilibrium temperature t 1 diss corresponding to the hydrate dissociation temperature at pressure p 1 . once t ′ 1 reached ( corresponding to an undercooling degree δt 1 ), this temperature is kept constant for several hours and the heat exchanges are recorded as a function of time . the formation of hydrates is translated into the appearance of an exothermic peak . the time t ′ 1 referred to as “ induction ” time , corresponding to the start of the exothermic peak , and the time t 1 corresponding to the vertex of the exothermic peak , are recorded . it is also possible to integrate the exothermic crystallization peak as a function of time in order to obtain the energy released per sample mass unit as a function of time . this energy is directly proportional to the amount of hydrates formed . the slope of the curve drawn allows to obtain a crystallization rate . it is then possible to compare the behaviour of another sample by carrying out exactly the same experiment , at the same pressure p 1 and at the isotherm temperature corresponding to the same undercooling degree δt 1 . an induction time t ′ 2 and a crystallization time t 2 are thus obtained . the greater these times t ′ 2 and t 2 in relation to t ′ 1 and t 1 , the higher the kinetic inhibition . if we draw the released energy curve as a function of time , the gentler the slope , the higher the kinetic inhibition . in cases where the exothermic hydrate formation peak is not exploitable , the procedure selected is the second indirect method that uses the energy released in dissociation . kinetic study of an oil - base mud under a pressure of 33 . 5 mpa kinetic tests were carried out on an oil - base drilling mud . the composition of the fluid studied is given in the table hereafter . the base oil hdf 2000 is supplied by total solvants . the pliolite df01 added as filtrate reducer is a product synthesized by the eliokem company . the carbogel clay used is an organophilic clay supplied by bhi . the radiagreen - emul emulsifying system is supplied by oleon nv . the cacl2 is dissolved in the water phase ( 15 % by weight ). this brine is then emulsified in the oil phase containing the other components , using a silverson l4rt agitator at 6000 rpm according to the api &# 39 ; s recommendations . if pliolite df01 is used as filtrate reducer , the latter is first incorporated to the base oil ( 15 - minute stirring ) and left to mature at 80 ° c . under 170 psi ( 11 . 7 b ) for 24 hours . preparation is then continued by adding the other products as recommended by the api . the mud is thereafter subjected to maturing at 80 ° c . for 16 hours prior to any handling . the stability of the emulsion , essential to carry out a reliable kinetic study as explained above , was checked by means of a calorimetric analysis with a dsc at atmospheric pressure . in fact , it is very difficult to measure the size of the water droplets in such a complex emulsion as an oil - base mud , mainly because of the large amount of solids contained in this type of fluid . dsc allows to analyze a mud sample without diluting it , thus without disturbing it . this sample undergoes cooling until crystallization of the water droplets is observed . the lower the crystallization temperature observed , the smaller the drops , and the more stable the emulsion . the applications of this technique to emulsion stability measurement are described in the following document : dalmazzone , c ., clausse , d ., ( 2001 ). microcalorimetry . in encyclopedic handbook of emulsion technology , ( j . sjöblom , ed . ), marcel dekker , new york , chap . 14 , pp . 327 - 347 . in this example , a dsc 2920 ta instruments is used . a 7 . 1 - mg oil - base mud sample was subjected to a cooling - heating cycle at a sweep rate of 2 . 5 ° c ./ min at atmospheric pressure . cooling ( crystallization of the water drops ) was studied between 20 ° c . and − 100 ° c ., and heating ( melting of the ice drops ) between − 100 ° c . and 20 ° c . fig1 ( heat flow flx in mw / mg as a function of the temperature t in ° c .) shows the crystallization peak of the water drops of the emulsion observed at very low temperature (− 68 ° c .). the melting peak of the salt water droplets ends at about − 15 ° c ., which gives a high undercooling degree ( δt = melting temperature − crystallization temperature = 53 ° c .). this high undercooling degree , associated with a very narrow and gaussian crystallization peak , is characteristic of a very fine and stable emulsion . the reproducibility of the cycle shows the stabilized character of the emulsion , which allows the method according to the invention to be implemented . for the kinetic study of the formation of methane hydrates in oil - base mud , an hp micro dscvii device marketed by setaram was used to allow to work under controlled methane pressure up to 40 mpa . a first sweep at v 1 = 1 ° c ./ min under 33 . 5 mpa methane allowed to determine the dissociation temperature t 1 diss ( about 14 ° c .) and the crystallization temperature t 1 ( about − 25 ° c .) ( first method ). we then studied the formation of hydrates for various isotherms t ′ 1 ranging between t 1 and t 1 diss , because the formation peak is entirely detectable at this pressure ( third method ). fig2 shows the thermograms obtained during reproducibility tests e 1 , e 2 , e 3 carried out at an isotherm temperature t ′ 1 of − 9 ° c . ( δt 1 = 23 ° c ., p 1 = 33 . 5 mpa , v 1 = 1 ° c ./ min ). the good reproducibility of induction times t ′ 1 of the order of 25 min ( start of the exothermic peak ) and of times t 1 corresponding to the vertex of the exothermic peaks ranging between 80 and 100 min can be observed . fig3 shows the thermograms obtained upon the formation of methane hydrates with isotherms at t ′ 1 =− 4 , − 9 , − 11 , − 14 , − 19 and − 24 ° c . ( i . e . δt 1 = 18 , 23 , 25 , 28 , 33 and 38 ° c . respectively ) at p 1 = 33 . 5 mpa . the increase of induction times t ′ 1 and of times t 1 corresponding to the vertex of the exothermic peaks with the decrease of the undercooling degree δt 1 can be noted . these kinetics were reproduced for p 1 = 13 . 5 mpa and 23 . 5 mpa and the same behaviours were observed . it is also possible to integrate the exothermic crystallization peak as a function of time in order to obtain the energy e ( j / g ) released per sample mass unit as a function of time ( fig4 ). this energy e is directly proportional to the amount of hydrates formed . the slope of the curve obtained is related to a crystallization rate . finally , it can be noted that , for the lower pressures (& lt ; 12 mpa ), it can be very difficult to observe the exothermic hydrate formation peak during the isotherms . in this case , the second method described above is used . the hydrate formation kinetics was studied according to this method with a dsc111 setaram calorimeter . the test pressure was p 1 = 11 mpa . the sample was cooled at a constant rate v 1 = 1 ° c ./ min down to an isotherm temperature t ′ 1 ranging between temperature t 1 obtained upon continuous cooling as in the first method and the equilibrium temperature t 1 diss corresponding to the hydrate dissociation temperature at pressure p 1 . after various isotherm durations at p 1 and at undercooling degree δt 1 ( t 1 diss − t ′ 1 ), the sample was heated at a constant rate ( 1 ° c ./ min ) until an endothermic hydrate dissociation peak was obtained . integration of this dissociation peak allows to draw the curve of energy release as a function of the isotherm duration . this energy is directly proportional to the amount of hydrates formed . the results are given in fig5 . extrapolation of the curve on the abscissa axis allows to determine a pseudo induction time t 1 . the slope of the curve is related to a crystallization rate . kinetic study of a solid - free water - base mud under a pressure of 23 . 5 mpa the same type of kinetic study was carried out on a solid - free water - base mud referred to as bss . this mud , having the following composition , was prepared according to the api &# 39 ; s recommendations with a hamilton beach agitator ( 10 , 000 rpm ). this mud was studied as it was to achieve a kinetic study . none of the aforementioned methods ( 1 , 2 or 3 ) allowed to obtain reproducible results . according to the present invention , a stable emulsion of water / oil type was prepared from this mud so as to be able to statistically study the formation of methane hydrates . the composition and the preparation mode are summed up in the table hereafter . the continuous phase of the emulsion was first prepared from an hdf2000 base oil ( total solvants ) to which the emulsifying mixture used for the oil - base mud described in example 1 was added ( radiagreen emul : emulsifier and co - emulsifier by oleon nv ). the mixture was stirred with an ultra - turrax homogenizer at 6000 rpm for 1 min , then the water - base mud bss was added dropwise . when the entire aqueous phase was incorporated , the speed was increased to 9500 rpm and stirring continued for 5 minutes . the stability of the water - in - oil type emulsion was tested by calorimetry with a dsc 2920 ta instruments at atmospheric pressure . a 5 . 7 - mg sample was subjected to 3 cooling - heating cycles ( cy i , cy ii , cy iii ) with a sweep rate of 5 ° c ./ min between 20 ° c . and − 90 ° c . fig6 shows that the emulsion is perfectly stable since a narrow and relatively gaussian peak is obtained for the crystallization of the water drops in the mud at a very low temperature ( about − 68 ° c . ), which does not vary even after several thermal cycles . for the kinetic study of methane hydrate formation in the water - base mud emulsion , we used an hp micro dscvii from setaram at a methane pressure p 1 of 23 . 5 mpa . a first sweep at v 1 = 1 ° c ./ min at this methane pressure allowed to determine the dissociation temperature t 1 diss ( about 8 ° c .). on the other hand , in the case of this mud , it was not possible to determine t 1 because ice formed at the same time as hydrates upon continuous cooling . we studied the formation of hydrates at different isotherms t ′ 1 below t 1 diss because the formation peak is totally detectable at this pressure ( method 3 ), and we selected the isotherm temperatures for which a single endothermic peak corresponding to the dissociation of the methane hydrate upon heating was observed . the reproducibility of the measurements was checked on 3 different emulsions ( see fig7 for δt 1 = 18 ° c ., p 1 = 23 . 5 mpa , v 1 = 1 ° c ./ min ). fig8 shows the thermograms obtained upon methane hydrate formation with isotherms at t ′ 1 =− 5 , − 10 and − 15 ° c . ( i . e . δt 1 = 13 , 18 and 23 ° c . respectively ) at p 1 = 23 . 5 mpa . the increase of induction times t ′ 1 and of times t 1 corresponding to the vertex of the exothermic peaks with the decrease of the undercooling degree δt 1 can be noted . in this example , we studied the effect of a product used as a kinetic hydrate formation inhibitor for applications in petroleum production . it is the hytreat product supplied by tr oil services ( tros , aberdeen ). it was tested in a proportion of 0 . 5 % by weight incorporated in the water - base mud studied in example 2 . after incorporation of the kinetic inhibitor , the water - base mud was emulsified according to the same procedure as above in a continuous oil phase , as shown in the table hereafter . kinetic test for δt1 = 18 ° c ., p1 = 23 . 5 mpa and v1 = 1 ° c ./ min fig9 shows the hydrate formation peaks obtained with an isotherm at − 10 ° c . ( p 1 = 23 . 5 mpa and v 1 = 1 ° c ./ min ). it can be observed that the kinetic inhibitor tested under these conditions ( curve 0 . 5 % inhib ) allows to increase induction time t ′ 1 from 70 minutes ( curve ss inhib ) to about 250 minutes , and the time t 1 corresponding to the vertex of the peak from 150 to 350 minutes . the present invention is not limited to drilling or completion fluids , its scope extends to any fluid likely to form gas hydrates and for which knowledge of the formation kinetics is important .