EP0845291A1 - Homogenisierapparat/Mischverfahren mit hoher Scherkraft zur Direkt-Hydratisierung von Frakturierungsflüssigkeiten und zur Direkt-Mischung von Zementschlamm - Google Patents

Homogenisierapparat/Mischverfahren mit hoher Scherkraft zur Direkt-Hydratisierung von Frakturierungsflüssigkeiten und zur Direkt-Mischung von Zementschlamm Download PDF

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Publication number
EP0845291A1
EP0845291A1 EP97309589A EP97309589A EP0845291A1 EP 0845291 A1 EP0845291 A1 EP 0845291A1 EP 97309589 A EP97309589 A EP 97309589A EP 97309589 A EP97309589 A EP 97309589A EP 0845291 A1 EP0845291 A1 EP 0845291A1
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EP
European Patent Office
Prior art keywords
fluid
hydratable
mixing
hydrated
rate
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP97309589A
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English (en)
French (fr)
Inventor
D V Satyanarayana Gupta
Ronald G. Pierce
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Canadian Fracmaster Ltd
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Canadian Fracmaster Ltd
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Filing date
Publication date
Priority claimed from CA002191690A external-priority patent/CA2191690A1/en
Application filed by Canadian Fracmaster Ltd filed Critical Canadian Fracmaster Ltd
Publication of EP0845291A1 publication Critical patent/EP0845291A1/de
Withdrawn legal-status Critical Current

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B28—WORKING CEMENT, CLAY, OR STONE
    • B28C—PREPARING CLAY; PRODUCING MIXTURES CONTAINING CLAY OR CEMENTITIOUS MATERIAL, e.g. PLASTER
    • B28C5/00—Apparatus or methods for producing mixtures of cement with other substances, e.g. slurries, mortars, porous or fibrous compositions
    • B28C5/08—Apparatus or methods for producing mixtures of cement with other substances, e.g. slurries, mortars, porous or fibrous compositions using driven mechanical means affecting the mixing
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/40—Mixing liquids with liquids; Emulsifying
    • B01F23/405—Methods of mixing liquids with liquids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/50—Mixing liquids with solids
    • B01F23/51—Methods thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F33/00—Other mixers; Mixing plants; Combinations of mixers
    • B01F33/80—Mixing plants; Combinations of mixers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F2101/00—Mixing characterised by the nature of the mixed materials or by the application field
    • B01F2101/49—Mixing drilled material or ingredients for well-drilling, earth-drilling or deep-drilling compositions with liquids to obtain slurries

Definitions

  • the present invention relates to the mixing of chemical agents and base fluids to form well treatment fluids and more particularly to a method and apparatus for continuously mixing such fluids including, but not limited to, fracturing and acidizing gels, polyemulsions, foams and cement slurries, on a real time on-the-fly basis.
  • High viscosity aqueous fluids such as fracturing gels, acidizing gels, cement slurries and high density completion fluids, are commonly used in the oil industry for the treatment of subterranean wells.
  • the gels for example are normally made using dry polymer additives or agents which are mixed with water or other aqueous fluids at the job site.
  • Mixing procedures used in the past have resulted in a number of problems. For example, early "batch" mixing procedures involved mixing bags of powdered polymer in tanks at the job site. This resulted in uneven and inaccurate mixing, lumping of the powder into insoluble balls or globules which obstructed the flow of the gel, chemical dust hazards, and required the transport and use of huge tanks adding greatly to costs.
  • a known method of solving the lumping, gel ball problem is to delay hydration long enough for the individual polymer particles to disperse and become surrounded by water so that no dry particles are trapped inside a gelled coating to form a gel ball. This delay is achieved by coating the polymer with material such as borate salts, glyoxal, non-lumping HEC, sulfosuccinate, metallic soaps, surfactants, or other materials of opposite surface charge to the polymer.
  • a stabilized polymer slurry also referred to as a liquid gel concentrate.
  • the liquid gel concentrate is premixed prior to transport and then later added to the water at the well site.
  • a liquid gel concentrate comprising water, the polymer or polymers, and an inhibitor having a property of reversibly reacting with the hydratable polymer in a manner wherein the rate of hydration of the polymer is retarded.
  • a change in the pH condition of the concentrate such as by dilution and/or the addition of a buffering agent (pH changing chemical) to the concentrate
  • the inhibition reaction is reversed, and the polymer or polymers hydrate to yield the desired viscosified fluid.
  • This reversal of the inhibition of the hydration of the gelling agent in the concentrate may be carried out directly in the concentrate or later when the concentrate is combined with additional water.
  • the aqueous-based liquid gel concentrate of Briscoe has worked well at eliminating gel balls and is still in routine use in the industry. However, aqueous concentrates can suspend only a limited quantity of polymer due to the physical swelling and viscosification that occurs in a water-based medium. Typically, about 0.8 pounds of polymer can be suspended per gallon of the concentrate.
  • hydrocarbon carrier fluid for the slurry, rather than water, higher quantities of solids can be suspended. For example, up to about five pounds of polymer can be suspended in a gallon of diesel fuel carrier.
  • a liquid gel concentrate is disclosed in Harms and Norman U.S. Patent No. 4,722,646.
  • the hydrocarbon-based liquid gel concentrate is later mixed with water at the well site in a manner similar to that for aqueous-based liquid gel concentrates to yield a hydrated viscosified fluid, but hydrocarbon-based concentrates have the advantage of holding more polymer.
  • Proppants can be added to the hydrated gel prior to injection of the fluid down the well bore. Elevated viscosities in the treatment fluid are required to maximize its proppant carrying capacity and to minimize leak off into the treated formation during the high pressure fracturing phase of the operation.
  • Batching is expensive because of wasted time and unused fluid resulting from treatment delays, termination of the treatment before pumping all fluids, and fluid residues remaining at the bottom of the storage tanks that cannot be pumped out.
  • the disposal of unused gelled fluid has also become an expensive process due to stricter laws on the disposal of chemical wastes.
  • McIntire in '856 proposes hydration of a hydratable gel by achieving near absolute theoretical plug flow through a plurality of tanks in series fluid communication.
  • the plug flow is accompanied by high shear of the hydratable gel along its flow path through the series of tanks using a radial flow impeller positioned within at least one of the tanks.
  • some or even all of the tanks are provided with mixing impellers.
  • High shear rotary mixing means are disposed in a blender tub divided into first and second zones with first and second mixers disposed in the first and second zones.
  • the plurality of rotary mixers provides a total circulation flow rate at least an order of magnitude greater than the mixture flow rate through the tub so that an average fluid particle of the mixture passes through the mixers a total of at least 10 times while passing through the blender tub.
  • Wilson initially applies a relatively low level of mixing energy to the hydratable gel/water mixture and then allows this mixture to flow through a first compartment of a residence tank for approximately 45 seconds, after which the mixture enters via plug flow into a second recycle compartment.
  • the product in the recycle compartment is withdrawn in portions.
  • the withdrawn portion is subjected to high shear and is then returned to the recycle compartment. This reoccurs until fully hydrated product is introduced into an exit compartment.
  • in-line high shear rotor/stator mixers (sometimes also referred to as homogenizers or emulsifiers) can be used to hydrate gel slurries on the fly without the need for hydration units having or requiring large residence volumes.
  • a base fluid normally water
  • a base fluid is pumped directly into a high shear in-line mixer with gel concentrate added to the water supply line by means such as an injection Tee or venturi.
  • Back pressure is maintained in the pipeline mixer either by means of an elongated hose from the mixer to the blender where proppants are added to the hydrated gel or by means of a restriction or gate valve downstream of the mixer or a combination of the two.
  • a method of rapidly hydrating a liquid polymer concentrate to form a fluid for treating a subterranean formation comprising the steps of combining an effective amount of said concentrate with a hydrating fluid to ultimately yield a treatment fluid having a viscosity within a predetermined range; supplying said concentrate and hydrating fluid into high shear rate mixing means for mixing thereof at a predetermined shear rate to rapidly hydrate said concentrate; and directing the flow of hydrated fluid away from said mixing means for eventual use treating said formation.
  • a method of hydrating a hydratable gel to form a hydrated fluid comprising the steps of dispersing a predetermined quantity of said hydratable gel into a stream of hydrating fluid to form a mixture; supplying said mixture to high shear rate mixing means for shear mixing said mixture at a shear rate of at least 25,000 s -1 to hydrate said hydratable gel; and directing the hydrated fluid away from the mixing means at a controlled rate to maintain back pressure in said mixing means.
  • apparatus for hydrating a hydratable fluid to form a hydrated fluid comprising high shear rate mixing means for shear mixing therein of said hydratable fluid and a hydrating fluid to form said hydrated fluid, said mixing means having an inlet and an outlet; supply means for introducing a mixture of said hydratable fluid dispersed in a stream of said hydrating fluid to said inlet; means for regulating the flow of said mixture through said mixing means; and conduit means from said outlet for directing said hydrated fluid away from said mixing means.
  • apparatus for hydrating a polymer gel slurry to form a hydrated and viscosified fracturing fluid for the treatment of a subterranean formation comprising high shear rate mixing means for the mixing therein of said gel slurry and a fluid for hydrating said gel slurry to form said hydrated fluid, said mixing means having an inlet and an outlet; pump means for supplying a mixture of said gel slurry and said hydrating fluid to said inlet; and means in fluid communication with said outlet for directing said hydrated fluid away from said mixing means at a controlled rate for subsequent use treating said formation.
  • FIG. 1 there is shown schematically the present system for the mixing of a stabilized polymer slurry or concentrate with a base fluid which normally will be water.
  • a base fluid which normally will be water.
  • the following description is limited by way of example to the formation of fracturing fluids for the treatment of underground stratigraphic formations from the mixture of a polymer concentrate and a base fluid, it will be understood that this same system can be used to mix together other fluids, including fluids having particulate suspensions therein. Examples include the mixing of polyemulsions, foams, cement slurries, drilling fluid and so forth.
  • the use of the present system for the hydration of gelled fracturing fluids is particularly significant however in view of its ability to completely or nearly completely hydrate the fluids in a sufficiently short period of time to obviate the need for prior art residence volumes.
  • a base fluid normally water
  • a centrifugal pump 30 through a supply line 25 into a high shear rotor/stator type pipeline mixer/homogenizer 50 at a pressure in the range of, but not restricted to, 250 to 300 psi.
  • a polymer slurry is injected at a metered predetermined rate into supply line 25 via an injection Tee 40 for dispersal of the concentrate in the water stream.
  • a venturi can be used for dispersal of the slurry into the water stream if preferred.
  • Tee 40 can be located as shown in the drawing between pump 30 and mixer 50 but may also be located advantageously between reservoir 20 and pump 30 for better premixing of the water/slurry mixture.
  • An exhaust line 60 from the mixer directs the viscosified hydrated fracturing fluid usually to a blender 100 for the introduction of proppants into the fluid prior to injection down the wellbore 125 for treatment of the subterranean formations using conventional high pressure frac pumps 110.
  • Blenders and frac pumps are well known in the art and are not therefore described in detail herein.
  • the residence time of the hydrated gel/water mixture in pipeline mixer 50 can range from almost instantaneous flow through (i.e. near 0) to even a minute or more but will normally be in the range of 1 to 10 seconds and as a practical matter, the residence time is likely to be in the range of 1 to 2 seconds depending upon fluid throughput.
  • mixer residence time refers to the amount of time a particular particle or sample of the gel/water mixture requires to travel from the mixer inlet, through the rotor/stator to the mixer outlet. Residence times can be controlled by regulating the mixer's outflow.
  • this is accomplished by subjecting the mixer's shear cavity to a back pressure in the range of 40 to 200 psi but preferably in the range of approximately 120 to 150 psi.
  • Optimum back pressures which could be inside or outside this range, may have to be determined on a job-by-job basis depending upon equipment used, ambient temperatures, fluid characteristics, desired throughputs, and possibly other factors as well. Pinching the flow of fluid from the mixer to create back pressure prevents or at least inhibits cavitation and maintains the system, at least upstream of the pinch point, full of fluid. It's felt this helps ensure that the water and gel are mixed immediately and that each particle of fluid is exposed to the high shear rates developed by the mixer.
  • Back pressure can be developed by inserting a choke or gate valve 61 and back pressure meter 62 into exhaust line 60.
  • the diameter and/or length of the exhaust line can be varied. For example, in tests conducted by the applicant, good results were obtained using a 4 inch diameter line 60 feet in length measured from the mixer to blender 100. Better results however seem to be available from longer lines on the order of 100 to 125 feet or at least a combination of line length and diameter that provides on the order of 20 seconds or more of residence time in the line for fluids sheared at the rate of 56,000 s -1 in mixer 50.
  • line residence time refers to the amount of time a particle or sample of the gel/water mixture requires to travel from the mixer outlet to blender 100.
  • back pressure directly affects gel viscosity and the speed of hydration (i.e. with back pressure, does the gel hydrate more quickly than without back pressure) or whether its effect is indirect resulting from the control or regulation of mixer residence times and avoidance of cavitation and fluid by-pass of the mixer's rotor.
  • Mixer 50 is a commercially available product. In tests conducted by the applicant, good results have been obtained using either a Greerco Corp. 4" Tandem-Shear Pipeline Mixer or a Silverson Machines, Inc. 3" 600 LSH High Shear Mixer. Larger units are available from both companies. Two or more such mixers can be used connected together for example in series although to date this has not been found to result in significantly improved hydration times or viscosities.
  • a batch of polymer slurry was prepared using 590 liters of diesel fuel mixed with 5 kilograms of SA-1X mixed together and sheared for 10 to 15 minutes. One liter of methanol was then added and mixed in for 10 to 15 minutes. This was followed by the addition of 10 liters of S-11 mixed in for an additional 10 to 15 minutes. Guar gum (WG-15) was added in the amount of 550 kilograms mixed in for 25 minutes. The direction of rotation of the mixing auger was reversed for each bag of the powdered polymer.
  • the resulting gel slurry achieves a viscosity of 14 to 16 cP at a shear rate of 511 s -1 when loaded to water in the ratio of 6 litres of slurry (equivalent to 3 kg of WG-15) per cubic meter of water. Based therefore on these tests, 100% hydration was considered to have been achieved at a viscosity of 14 cP @ 511 s -1 .
  • concentrate was introduced into supply line 25 at the rate of 11 ⁇ 2 l/min. to 100 l/min. to be mixed with water introduced at the rate of 1 ⁇ 4 to 10 m 3 /min. for a system throughput of 1 ⁇ 4 m 3 /min. to ⁇ 11 m 3 /min.
  • full hydration to achieve initial viscosities at or about 14 cp at 511 s -1 were obtained in mixer residence times of near instantaneous to a few seconds.
  • the applicant has found the opposite to be true. More specifically, the applicant has found that the use of a low volume pipeline (inline) high shear mixer that applies an intense burst of shear over a short period of time measured in seconds provides the needed on-the-fly volumes of completely or near-completely hydrated gel for commercial fracturing operations in such a short period of time that residence tanks, blending tubs and the like are no longer required.
  • a low volume pipeline (inline) high shear mixer that applies an intense burst of shear over a short period of time measured in seconds provides the needed on-the-fly volumes of completely or near-completely hydrated gel for commercial fracturing operations in such a short period of time that residence tanks, blending tubs and the like are no longer required.
  • Shear rates can be varied in 3 ways or a combination thereof: change the rotor diameter; change the rotor speed; and adjust the gap between the rotor and stator. During operations, the shear rate will normally be adjusted by changing the rotor speed. For smaller (3"/4") mixer sizes, speeds of 3600 to 4800 rpm are typical. If using a 6" Greerco, for example, speeds of around 2500 rpm seem adequate. In tests performed by the applicant, a gap between the rotor and stator of 0.001" has produced good results.
  • the final concentration and rate required at the blender can be achieved by adding the slurry concentrate to the water and treating this mixture through high shear mixer 50. If higher throughputs are required, there are several options. One is to use a larger mixer capable of treating the mixture at the desired shear and flowthrough rates. A second option is to add a higher concentration of slurry (polymer) than the finally desired concentration through the mixer and adding makeup water through a supply line 59 that taps into line 60 downstream of mixer 50 and prior to the sample port. This makeup water can be metered to dilute the polymer concentrations back to the desired final level. This second option may be the more practical as it does not require that a second higher volume mixer be on site.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Dispersion Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Structural Engineering (AREA)
  • Mixers Of The Rotary Stirring Type (AREA)
  • Soil Conditioners And Soil-Stabilizing Materials (AREA)
  • Preparation Of Clay, And Manufacture Of Mixtures Containing Clay Or Cement (AREA)
EP97309589A 1996-11-29 1997-11-27 Homogenisierapparat/Mischverfahren mit hoher Scherkraft zur Direkt-Hydratisierung von Frakturierungsflüssigkeiten und zur Direkt-Mischung von Zementschlamm Withdrawn EP0845291A1 (de)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CA2191690 1996-11-29
CA002191690A CA2191690A1 (en) 1996-11-29 1996-11-29 Homogenizer/high shear mixing technology for on-the-fly hydration of fracturing fluids and on-the-fly mixing of cement slurries
CA2220972 1997-11-20
CA002220972A CA2220972C (en) 1996-11-29 1997-11-20 Homogenizer/high shear mixing technology for on-the-fly hydration of fracturing fluids and on-the-fly mixing of cement slurries

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EP0845291A1 true EP0845291A1 (de) 1998-06-03

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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1693102A2 (de) 2005-02-16 2006-08-23 Sandra Knape Verfahren und Vorrichtung zum Homogenisieren eines pumpfähigen Stoffes
EP1712271A2 (de) * 2005-04-13 2006-10-18 Ekato Unimix Gmbh Vorrichtung zum Homogenisieren und/oder Dispergieren Fliessfähiger Stoffe
WO2009109758A3 (en) * 2008-03-07 2009-11-19 Halliburton Energy Services, Inc. On-the-fly acid blender with sampling equipment
US8393390B2 (en) 2010-07-23 2013-03-12 Baker Hughes Incorporated Polymer hydration method
WO2013173033A1 (en) * 2012-05-16 2013-11-21 Halliburton Energy Services, Inc. Automatic flow control in mixing fracturing gel
WO2015076784A1 (en) * 2013-11-19 2015-05-28 Surefire Usa, Llc Methods for manufacturing hydraulic fracturing fluid
US9353585B2 (en) 2008-03-07 2016-05-31 Halliburton Energy Services, Inc. On-the-fly acid blender with sampling equipment
US9447313B2 (en) 2013-06-06 2016-09-20 Baker Hughes Incorporated Hydration system for hydrating an additive and method
US9452394B2 (en) 2013-06-06 2016-09-27 Baker Hughes Incorporated Viscous fluid dilution system and method thereof

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN100344854C (zh) * 2005-09-09 2007-10-24 万奥普（北京）石油工程技术开发研究院有限公司 化学驱多元配注工艺及其所用多元静态混流装置
US8746338B2 (en) 2011-03-10 2014-06-10 Baker Hughes Incorporated Well treatment methods and systems
US9719340B2 (en) 2013-08-30 2017-08-01 Praxair Technology, Inc. Method of controlling a proppant concentration in a fracturing fluid utilized in stimulation of an underground formation
US10436001B2 (en) 2014-06-02 2019-10-08 Praxair Technology, Inc. Process for continuously supplying a fracturing fluid

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US3741533A (en) * 1971-10-14 1973-06-26 Dow Chemical Co Mixing apparatus
GB1500901A (en) * 1973-10-25 1978-02-15 Cementation Res Ltd Forming a colloidal suspension
EP0186552A2 (de) * 1984-12-07 1986-07-02 ELF FRANCE, Société Anonyme dite: Verfahren und Vorrichtung für die Produktion einer Suspension von festen Teilchen, stabil in der Zeit
EP0239148A1 (de) * 1986-03-27 1987-09-30 Pumptech N.V. Mischer für pulverige und flüssige Materialien (insbesondere Zement und Wasser) oder Flüssig-Flüssig-Materialien
US4828034A (en) * 1987-08-14 1989-05-09 Dowell Schlumberger Incorporated Method of hydrating oil based fracturing concentrate and continuous fracturing process using same
US5046856A (en) * 1989-09-12 1991-09-10 Dowell Schlumberger Incorporated Apparatus and method for mixing fluids
US5052486A (en) * 1989-09-08 1991-10-01 Smith Energy Services Method and apparatus for rapid and continuous hydration of polymer-based fracturing fluids

Patent Citations (7)

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Publication number Priority date Publication date Assignee Title
US3741533A (en) * 1971-10-14 1973-06-26 Dow Chemical Co Mixing apparatus
GB1500901A (en) * 1973-10-25 1978-02-15 Cementation Res Ltd Forming a colloidal suspension
EP0186552A2 (de) * 1984-12-07 1986-07-02 ELF FRANCE, Société Anonyme dite: Verfahren und Vorrichtung für die Produktion einer Suspension von festen Teilchen, stabil in der Zeit
EP0239148A1 (de) * 1986-03-27 1987-09-30 Pumptech N.V. Mischer für pulverige und flüssige Materialien (insbesondere Zement und Wasser) oder Flüssig-Flüssig-Materialien
US4828034A (en) * 1987-08-14 1989-05-09 Dowell Schlumberger Incorporated Method of hydrating oil based fracturing concentrate and continuous fracturing process using same
US5052486A (en) * 1989-09-08 1991-10-01 Smith Energy Services Method and apparatus for rapid and continuous hydration of polymer-based fracturing fluids
US5046856A (en) * 1989-09-12 1991-09-10 Dowell Schlumberger Incorporated Apparatus and method for mixing fluids

Cited By (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1693102A2 (de) 2005-02-16 2006-08-23 Sandra Knape Verfahren und Vorrichtung zum Homogenisieren eines pumpfähigen Stoffes
EP1693102A3 (de) * 2005-02-16 2006-11-02 Sandra Knape Verfahren und Vorrichtung zum Homogenisieren eines pumpfähigen Stoffes
EP1712271A2 (de) * 2005-04-13 2006-10-18 Ekato Unimix Gmbh Vorrichtung zum Homogenisieren und/oder Dispergieren Fliessfähiger Stoffe
EP1712271A3 (de) * 2005-04-13 2007-10-24 Ekato Unimix Gmbh Vorrichtung zum Homogenisieren und/oder Dispergieren Fliessfähiger Stoffe
AU2009220989B2 (en) * 2008-03-07 2013-07-11 Halliburton Energy Services, Inc. On-the-fly acid blender with sampling equipment
WO2009109758A3 (en) * 2008-03-07 2009-11-19 Halliburton Energy Services, Inc. On-the-fly acid blender with sampling equipment
US9353585B2 (en) 2008-03-07 2016-05-31 Halliburton Energy Services, Inc. On-the-fly acid blender with sampling equipment
US8393390B2 (en) 2010-07-23 2013-03-12 Baker Hughes Incorporated Polymer hydration method
WO2013173033A1 (en) * 2012-05-16 2013-11-21 Halliburton Energy Services, Inc. Automatic flow control in mixing fracturing gel
US9592479B2 (en) 2012-05-16 2017-03-14 Halliburton Energy Services, Inc. Automatic flow control in mixing fracturing gel
US9771512B2 (en) 2012-05-16 2017-09-26 Halliburton Energy Services, Inc. Automatic flow control in mixing fracturing gel
US9447313B2 (en) 2013-06-06 2016-09-20 Baker Hughes Incorporated Hydration system for hydrating an additive and method
US9452394B2 (en) 2013-06-06 2016-09-27 Baker Hughes Incorporated Viscous fluid dilution system and method thereof
US10124307B2 (en) 2013-06-06 2018-11-13 Baker Hughes, A Ge Company, Llc Viscous fluid dilution system and method thereof
WO2015076784A1 (en) * 2013-11-19 2015-05-28 Surefire Usa, Llc Methods for manufacturing hydraulic fracturing fluid

Also Published As

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NO975485L (no) 1998-06-02
CA2220972A1 (en) 1998-03-10
ID19015A (id) 1998-06-04
CA2220972C (en) 1999-03-09
NO975485D0 (no) 1997-11-28

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