Apparatus and method for measuring two- or three- phase fluid flow utilizing one or more momentum flow meters and a volumetric flow meter

Abstract: An apparatus and method for measuring the flow rates of each component of two-phase flow consisting of a gas and a liquid or three-phase flow consisting of water, oil and gas, including a first volumetric flow meter stage, and second and third momentum flow meter stages coupled in a series flow path with the volumetric flow meter stage and in which a velocity ratio between the gas and the liquid in the series flow path is maintained to be one. A processor calculates 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 displays flow of liquid and gas or oil, water and gas components of the flow. To measure three-phase flow, a water-cut meter is provided to determine the amount of water flow, which is then used by the processor to determine the flow of the rest of the liquid. The second and third momentum flow meter stages can be implemented by two separate momentum flow meters or by a single momentum flow meter, such as a venturi flow meter having a venturi nozzle including 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 flow meter stage is sufficient.

Description: This invention relates to an apparatus and method for measuring two-phase flow (liquid/gas) or three-phase flow (liquid/liquid/gas) of fluids. 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. Patent 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 requires 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. Patents 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. US-A-3,488,996 discloses a method of determining the oil content of a flowing stream of oil and water by measuring, during a test period, the total volume of liquid, total mass of liquid and the specific gravity of both the oil and the water separately at operating temperature and thereafter effecting calculation of the percentage oil constituent from the measurements. JP-A-56125621 discloses a two-phase flow measuring device which can measure the two-phase flow under high temperature and high pressure highly accurately by combining a diaphragm type density meter and a drag disc type current meter. An object of the invention is to provide a new and improved apparatus and method for measuring multi-phase 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. Preferably flow measurement is to be achieved with an apparatus and method in which gas separating devices or densitometers or measurement of a void fraction is not necessary. It is also desirable 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. According to the invention there is provided an apparatus for measuring flow rates and pressure drops of gas and liquid components having the features recited in claim 1. The momentum flow meter means can comprise second and third momentum flow meter stages which 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. To measure three-phase (oil, water, gas) flow a water-cut meter may be 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. Where prediction of multi-phase fluid pressure drops in various flow apparata is required, 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. Further according to the invention there is provided a method of measuring flow rates and pressure droped of gas and liquid components comprising the operational steps as recited in claim 7. Embodiments of the present invention will now be described with reference to the accompanying drawings in which: Figure 1 is a block diagram of one embodiment for two-phase flow measurement; Figure 2 is a schematic diagram of one preferred embodiment for two-phase flow measurement, utilizing two venturi tubes and an ultra-sonic flow meter; Figure 3 is a schematic diagram of another preferred embodiment for measuring two-phase flow, using a combination of a single modified venturi meter with a positive displacement flow meter; Figure 4 is a schematic diagram of an embodiment of the present invention for three-phase flow with the flow meter shown in Figure 3 and a water-cut-monitor; Figure 5 is a schematic diagram illustrating how the flow meter shown in Figure 4 can be used to measure the relative pressure drop of a three-phase fluid; and Figure 6 is a flow chart of the overall process in accordance with one embodiment 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 Figure 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 this embodiment of the present invention forces the velocity ratio between the gas and the liquid (slip ratio) inside the apparatus to be 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 transducer 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 and pressure drop of the liquid and the gas components by solving equations presented hereinafter. Specifically, the computer 20 has a memory comprising differential pressure drop data stored as a function of a plurality of values of gas flow rate and liquid flow rate through a series flow path. The computer 20 also has a selection device coupled to the memory for selecting a corresponding differential pressure drop based on the measured gas or liquid flow rates stored in the memory. A calculating device, in computer 20 is coupled to receive a pressure drop signal from a pressure differential measuring device. The calculating device is capable of calculating a pressure drop ratio of the pressure drop signal and the selected differential pressure drop and outputting a corresponding pressure drop ratio signal. The pressure drop ratio signal is received by a multiplying device of computer 20. The multiplying device is capable of multiplying the pressure drop ratio signal with a predetermined signal indicative of a pressure drop of a known mixture through a different flow segment of the flow path to determine a pressure drop of the fluid in the different flow segment of the flow path. Figure 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 10 1 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 Figures 1 and 2 can be reduced to one, by drilling one more pressure tap along the venturi nozzle, as shown in Figure 3. Such a modified venturi flowmeter is designated by numeral 31 in Fig. 3. Here the volumetric flow meter 10 2 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, with 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 Figure 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. Figure 4 shows-a water-cut meter 32 (such as described in U.S. Patents 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. 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 the flow measurements are performed utilizing momentum equations. In the following analysis, the following English and Greek letters and subscripts are used and have the noted meanings: English letters A - cross sectional area c - percent of water d - longitude differential g - gravity constant m - total mass flux M - momentum flux p - pressure P - circumference Q - volumetric flow rate R - gas constant s - velocity ratio between the gas and the liquid ("slip") T - absolute temperature v - specific volume x - quality Greek letters α - void fraction β - slope of the instrumentation ρ - density τ - wall shear Subscripts G - gas O - oil PD - positive displacement TOTAL - sum of all the fluid components TP - two-phase W - water In performing a two-phase flow measurement, Q L and Q G 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 the three unknowns are the following: 1) The volumetric flow meter equation for stage 1: Q PD = Q L + Q G Q PD is derived from the volumetric flow meter output. 2) The momentum equation for stage 2 (for example the venturi meter shown in Figure 3 from tap 1 to tap 2) : p 1 - p 2 = f 1 (Q L , Q G , ρ L ) where p 1 -p 2 is the differential pressure derived from transducer 28 in Figure 3. 3) The momentum equation for stage 3 (for example the venturi meter shown in Figure 3 from tap 1 to tap 3): p 1 - p 3 = f 2 (Q L , Q G , ρ L ) where p 1 - p 3 is the differential pressure derived from transducer 30 in Figure 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: and from the first tap of the venturi to the third tap: In equations 4 and 5 ρ TP , m, x and α are functions of Q G , Q L and ρ L : ρ TP = (1 - α)ρ L + αρ G m = Q L ρ L - Q G ρ G A α = Q G Q G + sQ L x = Q G ρ G Q L ρ L + Q G ρ G Substituting equations 6, 7, 8 and 9 into equations 4 and 5, and then solving with equation 1, provides solutions for Q L , Q G and ρ L 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 embodiments of the present invention utilize 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: C = Q W Q W + Q O + Q G The liquid flow rate is the sum of the water and the oil flow rates: Q L = Q O + Q W Therefore, the equation for determining the water flow rate can be written as: Q W = (Q L + Q G )c and then Q O can be derived from equation 12 once Q W is known. Figure 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 Δp water/air for different values of Q air and Q water . When a multi-phase fluid consisting of different components than water and air flows through the meter, stages 1, 2 and 3 measure Q G and Q L , while stage 5 measures the differential pressure across the meter (Δp fluid ). The Δp water/air that corresponds to the equivalent air and water values for the measured Q G and Q L 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: Δp fluid Δp water/air = const| same flow conditions 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 or segments 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 pressure 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 this embodiment of the present invention provides an accurate prediction of the pressure drop across the vertical pipe for the working fluid. Figure 6 shows a flow chart that summarizes the process in accordance with this embodiment of the present invention. In Figure 6, in step 100, the output of the volumetric flow meter 10, Q PD , is measured. In step 110, differential pressure, p 1 -p 2 , is measured. In step 120, the differential pressure p 1 -p 3 is measured. In step 130, the water-cut, c, is measured. The outputs of the steps 100, 110 and 120 are fed to the computer 20 which then at step 140 calculates Q L , Q G and ρ L , solving equations 1, 4 and 5 and utilizing equations 6-9. In step 150, Q water and Q oil are calculated utilizing equations 10-12, and in step 160, the results of the various calculations performed as thus far described, Q G , Q water and Q oil are displayed. Figure 6 also illustrates steps by which the ratio Δp fluid /Δp water/air is determined. In step 170, Δp fluid is measured by means of the sensor 36 shown in Figure 5. In step 180, a look-up table is utilized to determine Δp water/air , based on the values of Q L and Q G determined in step 140. In step 190 the ratio of Δp fluid , determined in step 170 and Δp water/air , determined in step 180, is determined and likewise displayed in step 150.

Claims: An apparatus for measuring flow rates and pressure drops of a gas component and a liquid component having a known density in a fluid flowing in a flow path, comprising: a. volumetric flow meter means (10) capable of measuring a total flow rate (Q PD ) for said fluid and outputting a total flow rate signal indicative of the measured total flow rate; b. momentum flow meter means (12,14) coupled in series with said volumetric flow meter means in said flow path, said momentum flow meter means capable of measuring the momentum flux of said fluid and outputting a corresponding momentum signal; c. processor means (20) coupled to said volumetric flow meter means (10) and said momentum flow meter means, said processor capable of determining the flow rate of said gas component (Q G ) and the flow rate of said liquid component (Q L ) in said fluid by solving predetermined equations for total flow and momentum or energy utilizing said total flow rate signal and said momentum signal; d. a pressure differential measuring device (26,28) installed in said flow path such that said pressure differential measuring device is capable of measuring the pressure drop (ΔP FLUID ) across said flow path of said volumetric flow meter means and said momentum flow meter means, said measuring device further capable of producing a pressure drop signal, indicative of the measured pressure differential; e. a memory comprising differential pressure drop data (ΔP WATER/AIR ) stored as a function of plural values of gas flow rate and liquid flow rate through said flow path; f. a selection device coupled to said memory, and capable of selecting from said memory a corresponding differential pressure drop (ΔP WATER/AIR ) based on the measured gas and liquid flow rates; g. a calculating device coupled to receive the pressure drop signal (ΔP WATER/AIR ) from said pressure differential measuring device and capable of calculating a pressure drop ratio of said pressure drop signal (ΔP FLUID ) and the selected differential pressure drop and outputting a corresponding pressure drop ratio signal; and h. a multiplying device coupled to receive a pressure drop ratio signal from said calculating device, said multiplying device capable of multiplying said pressure drop ratio signal with a predetermined signal indicative of a pressure drop of a known mixture through a different segment of said flow path to determine a pressure drop of said fluid in said different segment of said flow path. An apparatus according to claim 1 further comprising at least one of a static mixer (22, 24) or a dynamic mixer (22,24) capable of forcing a known velocity ratio between said gas component and said liquid component in said flow path. An apparatus according to claim 1 or claim 2, wherein said volumetric flow meter means comprises a positive displacement flow meter (10 2 ). An apparatus according to claim 1 or claim 2, wherein said momentum flow meter means comprises a venturi flow meter (31). An apparatus according to any one of claims 1 to 4 further comprising: a. water-cut meter means (32) coupled to said processor (20) and capable of measuring an amount of water in said liquid component and outputting a corresponding water-cut signal; b. said processor being capable of determining flow rates of a gas constituent (Q G ), a water constituent (Q W ), and a further constituent (Q OIL ) of said liquid component based on said water-cut signal and the determined liquid and gas flow rates; and c. indicator means (160) coupled to said processor and capable of displaying the determined flow rates of said water constituent and said further constituent. An apparatus according to any one of claims 1 to 5 including indicator means for displaying the determined flow rates of said liquid constituent and said gas constituent. A method of measuring flow rates and pressure drops of a gas component and a liquid component having a known density in a fluid flowing in a flow path, the method comprising the steps of: a. measuring a total flow rate (Q PD ) in said flow path and outputting a corresponding total flow rate signal; b. measuring the momentum flux of said fluid at a point in said flow path and outputting a corresponding momentum signal; c. determining the flow rate of said gas component (Q G ) and the flow rate of said liquid component (Q L ) by solving predetermined equations for total flow and momentum or energy utilising said total flow rate signal and said momentum signal; d. measuring the pressure drop (ΔP FLUID ) across the said flow path and producing a pressure drop signal indicative of the measured pressure differential; e. from a table of differential pressure drops (ΔP WATER/AIR ) stored as a function of plural values of gas flow rates and liquid flow rates through said flow path, selecting a corresponding differential pressure drop based on the measured gas and liquid flow rates; f. calculating a pressure drop ratio of said pressure drop signal and the selected differential pressure drop and outputting a corresponding pressure drop ratio signal; and g. multiplying said pressure drop ratio signal with a predetermined signal indicative of a pressure drop of a known mixture through a different segment of said flow path to determine a pressure drop of said fluid in said different segment of said flow path. A method according to claim 7 further comprising the step of forcing a known velocity ratio between said gas component and said liquid component in said flow path. A method according to claim 7 or claim 8 further comprising the steps of: a. measuring an amount for water in said liquid component and outputting a corresponding water-cut signal (c); b. determining flow rates of said gas constituent (Q G ), said water constituent (Q W ), and a further constituent (Q O ) of said liquid component based on said water-cut signal and the determined liquid and gas flow rates; and c. displaying the determined flow rates of said water constituent and said further constituent. A method according to claim 7, 8 or 9 further comprising the step of displaying the determined flow rates of said liquid constituent and said gas constituent.

Inventors: AGAR JORAM, FARCHI DAVID, AGAR, JORAM, FARCHI, DAVID
Applicants: AGAR CORP INC, AGAR CORPORATION INC.
Application year: 1993
Main classification: G01F1
IPC codes: G01F1