|Publication number||USRE36597 E|
|Application number||US 08/969,619|
|Publication date||Mar 7, 2000|
|Filing date||Sep 25, 1997|
|Priority date||Mar 17, 1992|
|Also published as||CA2103254A1, CA2103254C, DE69318775D1, DE69332546D1, EP0584329A1, EP0584329B1, EP0738880A2, EP0738880A3, EP0738880B1, US5461930, US5551305, WO1993019347A1|
|Publication number||08969619, 969619, US RE36597 E, US RE36597E, US-E-RE36597, USRE36597 E, USRE36597E|
|Inventors||Joram Agar, David Farchi|
|Original Assignee||Agar Corporation Inc.|
|Export Citation||BiBTeX, EndNote, RefMan|
|Patent Citations (13), Non-Patent Citations (6), Referenced by (14), Classifications (7), Legal Events (2)|
|External Links: USPTO, USPTO Assignment, Espacenet|
1. Field of the Invention
This invention relates to-an apparatus and method for measuring two-phase flow (liquid/gas) or three-phase flow (liquid/liquid/gas) of fluids.
2. Discussion of Background
The measurement of oil, water and gas flow finds application in various fields. In oil production, it is required for reservoir control and fiscal reasons. High accuracy of measurement is necessary as well as small instrumentation space requirements. Additional applications exist in petrochemical, nuclear and other industries.
In the past, three principal methods have been utilized for flow measurements.
As disclosed in U.S. Pat. No. 4,760,742, the gas in a liquid is physically separated from the liquid, and each fluid is measured separately. A water-cut monitor is used to measure the amount of the water and the oil in the liquid phase. Two conventional single-phase flow meters are used to measure the gas and the liquid flow rates. This method can yield high accuracy, but require gas-separating devices which are either very large or are very sensitive to flow rates and the liquid's viscosity, surface tension, etc.
A second approach is described in U.S. Pat. Nos. 4,168,624 and 4,050,896, wherein the total flow is measured at two different flow conditions (for example: different temperatures and different pressures along the pipeline). The changing of the gas volume during the change of this condition makes it possible to calculate the flow rates of the gas and the liquid. To achieve high accuracy in this method, a large difference in flow conditions between the two flow meters is required. This requires a large pressure drop, which is costly in terms of pumping energy.
A third technique as described by Baker, "Measuring Multi-Phase Flow", Chemical Engineer, No 453, pp 39-45, October 1988, and Reimann et al, "Measurement of Two-Phase Mass Flow Rate: A Comparison of Different Techniques", Int J. of Multi-Phase Flows, Vol. 8, No. 1, pp. 33-46, 1982, measures the total momentum flux, total density, total volumetric flow rate, and the water cut. All are required to calculate the amount of gas, oil and water. One such device uses the combination of a turbine flow meter, a venturi flow meter, a gamma ray densitometer or void fraction meter and a water-cut monitor. The advantage of this method is that it enables the use of venturies which have low pressure drops. The weak link in this technique is the densitometer, which is sensitive to the flow characteristics and the fluid's contaminants (heavy metals, etc.).
In many multi-phase flow applications it is desirable to predict the pressure drops which will occur in various piping apparata with different combinations of multi-phase fluids. This information is critical to piping design, pump sizing, etc. While information has been compiled on the pressure drops of a two-phase fluid comprising of water and air, it has not been possible to predict the pressure drops for other, more unique multi-phase fluids.
Accordingly, one object of the invention is to provide a new and improved apparatus and method for measuring multiphase flow by means of simple, low cost, compact equipment which has high flow rate measuring accuracy.
Another object is to provide a novel apparatus and method for measuring multi-phase flow and which entails small pressure drops and therefore requires little pumping energy.
Yet a further object is to provide a novel apparatus and method as above noted, which does not need gas separating devices or densitometers or measurement of a void fraction to perform the flow measurement.
Still a further object of this invention is to provide a novel apparatus and method capable of developing a table predicting the pressure drops which will occur in piping apparata for different multi-phase fluids.
These and other objects are achieved according to the present invention by providing a novel apparatus for measuring the flow rates of each component of two-phase flow consisting of a gas and a liquid, including a first volumetric flow meter stage, second and third momentum flow meter stages coupled in a series flow path with the volumetric flow meter stage, wherein a velocity ratio between the gas and the liquid in the series flow path is maintained at a known value, e.g., one, and a processor for calculating flow rates of the components of flow by solving volumetric flow and momentum or energy equations defining flow through the first through third stages utilizing a volumetric flow output from the first stage and momentum flux outputs from said second and third stages, and an indicator for displaying flow rates of the liquid and gas components of the two-phase flow.
The second and third momentum flow meter stages can be implemented by two separate momentum flow meters or by a single momentum flow meter having a venturi nozzle including at least three pressure taps for obtaining at least two differential pressure measurements. In the event that the density of the liquid component is known, a single momentum flux measurement from a single momentum flow meter stage is sufficient to measure two-phase flow.
To measure three-phase (oil, water, gas) flow a water-cut meter is provided to determine the amount of water flow, which is then used by the processor to determine the amount of oil flow. The flow rates of oil, water and gas are then displayed.
To enable prediction of multi-phase fluid pressure drops in various flow apparata, a differential pressure measurement is taken across the first through third (and optionally fourth) stages, and means are provided to calculate and display ratios of the pressure drops of multi-phase fluids relative to the known pressure drops of fluids comprising water and air.
A more complete appreciation of the invention and many of the attendant advantages thereof will be readily obtained as the same becomes better understood by reference to the following detailed description when considered in connection with the accompanying drawings, wherein:
FIG. 1 is a block diagram of an apparatus for two-phase flow measurement according to the present invention;
FIG. 2 is a schematic diagram of an apparatus for two-phase flow measurement according to the present invention, utilizing two venturi tubes and an ultra-sonic flow meter;
FIG. 3 is a schematic of a preferred embodiment for measuring two-phase flow, using a combination of a single modified venturi meter with a positive displacement flow meter;
FIG. 4 is a schematic diagram of an embodiment of the present invention for three-phase flow with the flow meter shown in FIG. 3 and a water-cut monitor;
FIG. 5 is a schematic diagram illustrating how the flow meter shown in FIG. 4 can be used to measure the relative pressure drop of a three-phase fluid; and
FIG. 6 is a flow chart of the overall process of the present invention for measuring three-phase flow and determining pressure drop ratios, according to the apparata described in relation to FIGS. 2-5.
Referring now to the drawings, wherein like reference numerals designate identical or corresponding parts throughout the several views, and more particularly to FIG. 1 thereof, there is shown schematically an embodiment of the apparatus of the invention, including a volumetric flowmeter 10 serving as a first stage in which a mixture of gas and liquid flows through the volumetric flow meter 10. This flow meter 10 measures the total flow rate for the mixture. The mixture then flows through second and third stages, consisting of two momentum flow meters 12 and 14 with different dimensions (for example, two venturi flow meters with different throat diameters). Momentum flow meters are flow meters that measure the momentum flux of the fluid (M=mv). In order to avoid using a void fraction meter, the present invention forces the velocity ratio between the gas and the liquid (slip ratio) inside the apparatus to be a known value, a slip ratio of one being conveniently enforced. This is achieved through using either static or dynamic mixers or a positive displacement meter. In each stage the absolute pressure and temperature are measured by means of temperature transducers 16 and pressure transducers 18. One momentum flow meter can also be used by itself, in the instance that the liquid component's density is known. The data from Stages 1, 2 and 3 is transferred to a computer 20 that calculates the flow rates of the liquid and the gas components by solving equations presented hereinafter.
FIG. 2 shows an example of a more concrete embodiment of the invention for two-phase flow measurement. Stage 1 is an ultra-sonic flow meter 101 installed between two static mixers 22 and 24. The ultrasonic flow meter measures volumetric flow. Other volumetric flow meters can also be used, such as turbine, vortex shedding, magnetic, heat transfer, variable area, paddle and Coriolis volumetric flow meter. In this modification the static mixers 22, 24 are used to force a unitary velocity ratio between the phases. Instead of measuring the absolute pressure independently in each stage, the absolute pressure is measured with a pressure transducer 18 in stage 1, and is calculated using differential pressure transducers 26 and 28 in stages 2 and 3.
The two momentum flow meters shown in FIGS. 1 and 2 can be reduced to one, by drilling one more pressure tap along the venturi nozzle, as shown in FIG. 3. Such a modified venturi flowmeter is designated by numeral 31 in FIG. 3. Here the volumetric flow meter 102 is a positive displacement (P.D.) type. The advantage of using a P.D. flow meter is that it provides an exact measurement of the sum of the liquid and gas flow rates, will no slip between the gas and liquid phases inside the meter or immediately after the meter. Thus, the P.D. flow meter forces the slip ratio to a known amount, i.e., unity, and permits dispensing with the static mixers of the FIG. 2 embodiment.
The embodiments shown in FIG. 1-3 are above-described using one or two venturi-type momentum flow meters. However, it should be understood that other momentum flow meters can be used to practice the present invention. For example, a target or drag-disk-type flow meter having different paddle dimensions can also be utilized to obtain sufficient parametric data to solve the energy and momentum equations of the fluids. For more detail about particular instrumentation described herein, see Hewitt, G. F., "Measurement of Two Phase Flow Parameters", Whitstable, Litho Ltd , Whitstable, Kent, Great Britain, 1978, and Holman, J. P., "Experimental Methods for Engineers", McGraw-Hill Book Company, 1978.
The differential pressure transducers 26 and 28 measure the pressure difference along the venturi nozzle. A three-phase flowmeter in which a mixture of oil, water and gas can be measured is constructed with the addition of a fourth stage water-cut meter. FIG. 4 shows a water-cut meter 32 (such as described in U.S. Pat. Nos. 4,503,383 and 4,771,680) that measures the water concentration c of the mixture. Absolute pressure and temperature are measured in this stage by transducers 16 and 34, respectively. Reference numeral 31 designates the modified venturi flowmeter having the pressure taps 1-3 and associated transducers shown in FIG. 3 in correspondence with stages 2 and 3 shown in FIG. 1. Because of the change in the specific volume of the gas (v=p/RT), measurement of the absolute pressure and temperature at all stages is necessary.
Next described is the analytical basis by which the present invention performs flow measurements utilizing momentum equations. In the following analysis, the following English and Greek letters and subscripts are used and have the noted meanings:
c--percent of water
m--total mass flux
Q--volumetric flow rate
s--velocity ratio between the gas and the liquid ("slip")
B--slope of the instrumentation
TOTAL--sum of all the fluid components
In performing a two-phase flow measurement, QL and QG are unknowns, but not the only unknowns.
The density of the liquid is also unknown (other unknown properties of the liquid and the gas have only a minor effect on the present method, and are therefore ignored here). The three equations that need to be solved for three unknowns are the following:
1) The volumetric flow meter equation for stage 1:
Q.sub.PD =Q.sub.L +Q.sub.G (1)
QPD is derived from the volumetric flow meter output.
2) The momentum equation for stage 2 (for example the venturi meter shown in FIG. 3 from tap 1 to tap 2):
ρ.sub.1 -ρ=f.sub.1 (Q.sub.L, Q.sub.G, ρ.sub.L) (2)
where ρ1 -ρ2 is the differential pressure derived from transducer 28 in FIG. 3.
3) The momentum equation for stage 3 (for example the venturi meter shown in FIG. 3 from tap 1 to tap 3):
ρ.sub.1 -ρ.sub.3 =f.sub.2 (Q.sub.L, Q.sub.G, ρ.sub.L) (3)
where ρ1 -ρ3 is the differential pressure derived from transducer 30 in FIG. 3.
Certain assumptions must be made for the equations to be solvable:
1) The expansion of the gas along the venturi nozzle is isothermal.
2) Evaporation and dissolution of vapor and gas are negligible.
3) The ideal gas equation holds, and the liquid is incompressible.
4) The velocity ratio between the gas and the liquid=1, or can be found experimentally as a function of the liquid and the gas flow rates.
Equations 2 and 3, shown here in general form, are in fact integral equations derived from the full expression of the momentum equation (see Hetsroni, G., "Handbook of Multi-Phase Systems", Chaps 1.2, 2.1, 2.3, Hemisphere Publishing Corporation, U.S.A., 1982).
The momentum equation can be simplified to a model for one-dimensional, steady-state flow based on the Separated Two-Phase Flow model (see Hetsroni, G., supra) and can integrate from the first tap of the venturi to the second tap: ##EQU1## and from the first tap of the venturi to the third tap: ##EQU2##
In equations 4 and 5 ρTP, m, x and α are functions of QG, QL and ρL : ##EQU3##
Substituting equations 6, 7, 8 and 9 into equations 4 and 5, and then solving with equation 1, provides solutions for QL, QG and ρL since we have three equations and three unknowns.
Equations 4 and 5 are solved using known numerical analysis techniques. The selection of a particular numerical analysis technique is based on a trade-off between accuracy and speed of execution, and is a function also of the availability of fast and economic computation devices. The relative merits of some techniques are discussed in Scheid, "Theory and Problems of Numerical Analysis", Schaum's Outline Series, McGraw-Hill Book Co., 1968. The technique most appropriate for equations 4 and 5, today, is the Runge-Kutta method described in Chapter 19 of Scheid, supra. It is anticipated, however, that the development of cheaper and faster computation devices, or more efficient or more accurate methods of solving integral equations, will suggest other techniques to be utilized in the future. Similarly, a method well suited for solving the set of equations 1, 4 and 5 is the Newton method described in Chapter 25 of Scheid.
More or less detailed, and different types of models can be written as well, depending on the required accuracy of the meter. Applying the momentum equations provides a much more accurate solution than the energy equations, since the momentum equations only have to take into account the friction on the wall (easy to estimate), as compared with the energy equations which have to take into account the energy losses (very difficult to estimate). Generally, it is considered that the present invention utilizes conservation equations, which can be either momentum or energy equations (see Hetsroni, supra).
The equation for deriving three-phase flow (oil/water/gas) by the addition of a water-cut meter in stage 4 is: ##EQU4## The liquid flow rate is the sum of the water and the oil flow rates:
Q.sub.L, =Q.sub.O +Q.sub.W (11)
Therefore, the equation for determining the water flow rate can be written as:
Q.sub.W =(Q.sub.L +Q.sub.G)C (12)
and then QO can be derived from equation 12 once QW is known.
FIG. 5 shows how the multi-phase flow meter can also be used to predict pressure drops for different multi-phase fluids in different piping devices. The addition of differential pressure transducer (36) provides measurement of the pressure drop across the meter. In the calibration process a look-up table is generated, which contains the measured pressure drop across the meter when different proportions and rates of water and air are flowed through it. In effect the look-up table is a matrix of values of ΔPwater/air for different values of Qair and Qwater.
When a multi-phase fluid consisting of different components than water and air flows through the meter, stages 1, 2 and 3 measures QG and QL, while stage 5 measures the differential pressure across the meter (ΔPfluid). The ΔPwater/air that corresponds to the equivalent air and water values for the measured QG and QL of the working fluid is then looked up in the above-noted look-up table, and the pressure drop ratio is calculated.
The equation for the pressure drop ratio of the working multi-phase fluid relative to an equivalent water/air mixture is: ##EQU5##
Once this ratio has been calculated, it can be applied to obtain an accurate prediction of the pressure drop of multi-phase fluids in other devices in the line, where the pressure drop of an equivalent water/air mixture is known.
For example, to obtain the pressure drop in a vertical pipe in a field pipe line where crude oil, water and natural gas are flowing, a priori knowledge of the present drop for an air/water mixture in the same vertical pipe at the same flow rate is needed. This can be found in field handbooks (see Perry et al, "Chemical Engineer's Handbook", McGraw-Hill , Book Co., 1973, pp. 5.40-5.47). Multiplication of this number with the pressure drop ratio calculated according to the present invention provides an accurate prediction of the pressure drop across the vertical pipe for the working fluid.
FIG. 6 shows a flow chart that summarizes the process of the present invention.
In FIG. 6, in step 100, the output of the volumetric flow meter 10, QPD, is measured. In step 110, differential pressure, ρ1 -ρ2, is measured. In step 120, the differential pressure ρ1 -ρ3 is measured. In step 130, the water-cut, c, is measured. The outputs of the steps 100, 110, 120 and 130 are fed to the computer 20 which then calculates QL, QG and ρL, solving equations 1, 4 and 5 and utilizing equations 6-9. In step 150, Qwater and Qoil are calculated utilizing equations 10-12, and in step 160, the results of the various calculations performed as thus far described, QG, Qwater and Qoil are displayed.
FIG. 6 also illustrates steps by which the ratio ΔPfluid /ΔPwater/air is determined. In step 170, ΔPfluid is measured by means for the sensor 36 shown in FIG. 5. In step 180, a look-up table is utilized to determine ΔPwater/air, based on the values of QL and QG determined in step 140. In step 190 the ratio of ΔPluid, determined in step 170 and ΔPwater/air, determined in step 180, is determined and likewise displayed in step 160.
Obviously, numerous modifications and variations of the present invention are possible in light of the above teachings. It is therefore to be understood that within the scope of the appended claims, the invention may be practiced otherwise than as specifically described herein.
|Cited Patent||Filing date||Publication date||Applicant||Title|
|US3488996 *||Sep 7, 1967||Jan 13, 1970||Exxon Research Engineering Co||Determination of oil in a flowing stream|
|US4050896 *||Sep 13, 1976||Sep 27, 1977||Maschinenfabrik Hennecke Gmbh||Method and apparatus for the production of reaction mixtures from liquid reaction components|
|US4168624 *||Mar 20, 1978||Sep 25, 1979||Schlumberger Technology Corporation||Method and apparatus for determining the volume flowrate of each phase in a diphase mixture|
|US4236406 *||Dec 11, 1978||Dec 2, 1980||Conoco, Inc.||Method and apparatus for sonic velocity type water cut measurement|
|US4503383 *||Jan 7, 1982||Mar 5, 1985||Agar Corporation, N.V.||Device for detecting an interface between two fluids|
|US4604902 *||Oct 24, 1984||Aug 12, 1986||Geoscience Ltd||Means and techniques useful in mass flowmeters for multiphase flows|
|US4640902 *||May 31, 1985||Feb 3, 1987||Rockwell International Corporation||Low thermal conductivity Si3 N4 /ZrO2 composite ceramics|
|US4760742 *||Apr 10, 1987||Aug 2, 1988||Texaco Inc.||Multi-phase petroleum stream monitoring system and method|
|US5551305 *||Jun 7, 1995||Sep 3, 1996||Agar Corporation Inc.||Apparatus and method for measuring two- or three- phase fluid flow utilizing one or more momentum flow meters and a volumetric flow meter|
|DE438505C *||Dec 21, 1926||Siemens Ag||Woltmannmesser|
|FR1487394A *||Title not available|
|JPS56125621A *||Title not available|
|WO1991015738A1 *||Feb 14, 1991||Oct 17, 1991||Joram Agar||Improvements to two and three-phase flow measurement|
|1||AGA Gas Measurement Manual, Chapter IV, "Orifice Meters," pp. 41-85, 1 st ed. (1963).|
|2||*||AGA Gas Measurement Manual, Chapter IV, Orifice Meters, pp. 41 85, 1 st ed. (1963).|
|3||*||International Journal of Multiphase Flow, vol. 8, No. 1, 1982, pp. 33 46, J. Reinann, et al., Measurements Of Two Phase Mass Flow Rate: A Comparision Of Different Techniques .|
|4||International Journal of Multiphase Flow, vol. 8, No. 1, 1982, pp. 33-46, J. Reinann, et al., "Measurements Of Two-Phase Mass Flow Rate: A Comparision Of Different Techniques".|
|5||*||The Chemical Engineer, Oct. 1988, pp. 39 45, R. Baker, Measuring Multiphase Flow .|
|6||The Chemical Engineer, Oct. 1988, pp. 39-45, R. Baker, "Measuring Multiphase Flow".|
|Citing Patent||Filing date||Publication date||Applicant||Title|
|US6990414||Mar 2, 2004||Jan 24, 2006||Brad Belke||Electronic gas flow measurement and recording device|
|US7293471 *||Feb 24, 2005||Nov 13, 2007||Roxar Flow Measurement As||Flow meter for measuring fluid mixtures|
|US7434479 *||Jan 31, 2006||Oct 14, 2008||Sulzer Pumpen Ag||Method and an arrangement for the flow monitoring of multiphase mixtures|
|US7469188||Dec 9, 2004||Dec 23, 2008||Multi Phase Meters As||Method and flow meter for determining the flow rate of a multiphase fluid|
|US7624652||Dec 18, 2006||Dec 1, 2009||Multi Phase Meters As||Method and apparatus for tomographic multiphase flow measurements|
|US7637167 *||Apr 25, 2008||Dec 29, 2009||Schlumberger Technology Corporation||Apparatus and method for characterizing two phase fluid flow|
|US7640813 *||Apr 12, 2007||Jan 5, 2010||Krohne Messtechnik Gmbh & Co. Kg||Process for operating a Coriolis mass flow rate measurement device|
|US20040173091 *||Mar 2, 2004||Sep 9, 2004||Brad Belke||Electronic gas flow measurement and recording device|
|US20050188771 *||Feb 24, 2005||Sep 1, 2005||Roxar Flow Measurement As||Flow meter|
|US20060248963 *||Jan 31, 2006||Nov 9, 2006||Sulzer Pumpen Ag||Method and an arrangement for the flow monitoring of multiphase mixtures|
|US20070124091 *||Dec 9, 2004||May 31, 2007||Multi Phase Meters As||Method and flow meter for determining the flow rate of a multiphase fluid|
|US20080011101 *||Apr 12, 2007||Jan 17, 2008||Krohne Messtechnik Gmbh & Co. Kg||Process for operating a coriolis mass flow rate measurement device|
|US20090126502 *||Dec 18, 2006||May 21, 2009||Arnstein Wee||Method and Apparatus for Tomographic Multiphase Flow Measurements|
|US20090266175 *||Apr 25, 2008||Oct 29, 2009||Schlumberger Technology Corp.||Apparatus and method for characterizing two phase fluid flow|
|International Classification||G01F1/36, G01F1/74|
|Cooperative Classification||G01F1/36, G01F1/74|
|European Classification||G01F1/36, G01F1/74|
|Apr 9, 2003||FPAY||Fee payment|
Year of fee payment: 8
|Apr 6, 2007||FPAY||Fee payment|
Year of fee payment: 12