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    • 专利摘要:
    "process for producing a controlled salinity injection water stream". a process for producing a controlled salinity and controlled anion sulfate injection water stream that is suitable for injection into the oil containing formation of an oil reservoir, the process comprising the steps of: (a) feeding a source water having a total dissolved solids content in the range of 20,000 to 45,000 ppm and a sulfate anion concentration in the range of 1,000 to 4,000 ppm, preferably 1,500 ppm to 4,000 ppm for a desalination plant comprising a plurality of reverse osmosis membrane unit (or) and a plurality of nanofiltration membrane units (nf) wherein the source water is pressurized to an absolute pressure in the range 350 to 1250 psi (2.41 to 8.61 mpa), and dividing the water of source to provide a feed water for or membrane units (hereinafter "or feed water") and a feed water for nf membrane units (hereinafter "water" (b), if necessary, increase the feed water pressure from or to a value in the range 900 to 1250 psi (6.20 to 8.61 mpa) absolute before introducing the feeding to the ore membrane units and extracting an ore permeate and an ore retentate from the ore membrane units wherein the ore membrane units are operated in either a single phase, single pass or single phase mode. two-pass, single pass and wherein the permeate recovery is in the range of 35 to 75% by volume, preferably 35 to 60% by volume based on the volume of or feed water that is fed to the ore membrane units such that the orb permeate has a total dissolved solids content of less than 250 ppm, and an anionsulfate concentration of less than 3 ppm; (c) if necessary, reduce the nf feed water pressure to a value in the range 350 to 450 psi (2.41 to 3.10 mpa) absolute before introducing the nf feed water to the nf membrane and extract an nf permeate and an nf retentate from the nf membrane units in which the nf membrane units are operated in a single pass, single pass mode and wherein the nf membrane units nf are operated with an nf permeate recovery in the range of 35 to 60 vol% based on the volume of nf feed water that is fed to the nf membrane units such that the nf permeate has a dissolved content. in the range of 15,000 to 40,000 ppm, preferably 15,000 to 35,000 ppm, and an anion sulfate concentration of less than 40 ppm, preferably less than 30 ppm, and (d) mixing at least a portion of the ore permeate. at least a portion of the nf permeate in a ratio in the range of 2: 1 to 40: 1, preferably 4: 1 to 27: 1, in particular 10: 1 25: 1 to provide an injection water having a total dissolved solids content in the range of 500 to 5,000 ppm, and an anion concentration. sulfate of less than 7.5 ppm, preferably less than 5 ppm, more preferably less than 3 ppm.
    公开号:BR112012017561B1
    申请号:R112012017561
    申请日:2011-01-11
    公开日:2019-12-03
    发明作者:John Dale Williams
    申请人:Bp Exploration Operating Company Limited；
    IPC主号:
    专利说明:

    PROCESS FOR PRODUCTION OF A CONTROLLED SALINITY AGL CHAIN The present invention relates to a {supplying a low saline injection water. 5 oil reservoir having a salinity su to avoid damage formation and a low concentration of sulphate anion to prevent aci reservoir, and to a desali system to produce such an injection water. In particular, the invention provides a process and system for water of low controlled salinity, controlled sulfate concentration and controlled cation concentration.
    As described in patent application 5 WO 2008/029124, it is known that injecting salinity in a formation containing un oil in order to improve the recovery of reservoir oil.
    A problem associated with flooding 0 salinity is that desalination techniques produce water having a lower salinity: optimal salinity for improved recovery high levels of swellable clays, formation to be avoided when the injection water has a total dissolved te (TDS) in the 500 to 1 preference range, 1,000 to 5,000 ppm. However, it is not desirable to mix desalinated, low-content multivariate water with high salinity such as sea water with high sulfate anion content and / or high salinity water content. Thus, the high sulfate of such water streams mixed already in an acidification of the reservoir and / or unacceptable levels of insoluble mineral salts from deposits), when the injected water contains precipitated precursors, such as strontium and calcium which are commonly synergistic pres of formation. In addition, the desalination with a high-salinity sea water can result in the water stream having unacceptable levels of particular multiv 0 cations, calcium and magnesium cations. In order to obtain incremental oil recovery with low salinity injection, the proportion of excess water supply in the salinity could be increased by mixing with έ salinity. According to WO 2007/138327, it is already obtained by the steps of: substantially desalinating a first: water supply to provide a first low salinity treated water; treating a second supply of food providing a second supply of treated water <the reduced concentration of divalent ions in c the second supply of food is greater than the first supply of treated water; mixing the first treated water supply treated water supply to provide a mixed water having a desired salinity injection into a reservoir containing oil.
    In preferred winter modalities: 2007/138327, the first supply of a substantially desalted by a proce; The reverse while the water supply supply treatment step is carried out by nanofiltration. have the desired salinity suitable for oil-containing reservoir and have a sulfate anion level thereby mitigating the risk of mineral deposition or within the production formation.
    It is known that the injection of a water that has levels of sulfate anions can stimulate the sulfate-reducing bacteria that produces hydrogen as a metabolite resulting in the action of a reservoir. Where it is desired to mitigate mineral deposit formation, the level of mixed water supply should be as low as ppm. However, where it is desired to mitigate acidification in a reservoir, the level of <5 in the supply of mixed water should be as possible, for example, less than 7.5 ppm, less than 5 ppm.
    It was revealed that it is necessary to control the operating conditions of the proc 0 2007/138327 in order to obtain a supply of i of the total dissolved solids content and to control the formation of damages and the low co "" "i Vl Π 1 1 I ■ £ “1 4- xJ í— * X *» I xJ IA —Ί X · * X- »νκ 4- ΊΧ XI TX reservoir.
    Thus, according to a first invention, a process of a controlled salinity injection water stream 5 is provided which is a controlled sulfate anion concentration which is injected into a formation containing oil of a re oil, the process comprising the steps of: feeding a source water having a total dissolved teo in the range of 20,000 to 45.C The concentration of sulfate anion in the range of 1 ppm, preferably 1,500 ppm to 4,000 ppm pa of desalination comprising a plurality of reverse osmosis membrane units of nanof 5 membrane units in which the source water is pressurized at a range of 350 to 1250 psi (2.41 to 8.61 MPa) dividing the source water to supply power to the membrane water units forward OR feed ") and 0 feed to the membrane units" NC feed water "); if necessary, increase the water pressure by volume, preferably 35 to 60% by volume volume of the OR feed water which is the OR membrane units such that the total dissolved solids content of minus 5 permeates a sulfate anion concentration of less than necessary, reduce the water pressure of the NC to a value in the range of 350 to 450 psi MPa) absolute before introducing the water from the NC to the NC membrane units and extracting 0 NF and an NF retentate from the NF units in which the NF membrane units are a single phase mode, single pass NF membrane units are operated with one of the NF permeate in the range of 35 to 60% in v 5 in the volume of the NC feed water that for the NC membrane units such that the op has a total dissolved solids content in the fs at 40,000 ppm, preferably 15,000 to 35.0 sulfate anion concentration of less than 0 preference , less than 30 ppm; and mixing at least a portion of the permeate minus a portion of the permeate of NF in a produced water, a water aquifer, residual.
    Preferably, the diss solids content (TDS) of the OR permeate is in the range of 50 to 5, preferably 100 to 225 ppm, more preferably 200 ppm, in particular, 150 to 175 ppm.
    Preferably, the OR permeate anic concentration is in the range of 0.5 to particular, 0.5 to 1.5 ppm.
    Preferably, the TDS of the NF permeate is less than 15,000 ppm, preferably no more ppm less than the TDS of the source water.
    Preferably, the NF permeate anic concentration is in the range of 10 to 5 preferably 10 to 25 ppm, in particular, d <
    The sulfate anion concentration of water depends on the desired dissolved solids content for this stream and, consequently, mixing ratio for the OR 0 NF permeate. Thus, the sulfate anion concentration of the steel will increase with increasing amounts of p in the mixed stream. Typically, the concentration and having a low sulfate concentration to mitigate the risk of acidification, depending on the choice of the source water, the water can also have a sufficiently low cation concentration for use as a low salinity injection, thus obtaining r oil increases from the reservoir.
    Accordingly, the present invention also has an improved process and plant to supply. The mixed salinity water stream contains controlled sulfate anion concentration and controlled multivalent cation for injection use for a flood of bai water. while mitigating the risk of damage formation 5 acidification in the reservoir.
    Thus, in a second form of the prosthesis, a process for the production of a controlled injection salinity, controlled anion sulfate color and controlled multivalent 0 concentration is provided which is suitable for formation containing oil from a reservoir. The process comprises the steps of: οΙ'ίγΥΊΑηΉον 'i ί m -ί no / -s - λπλ 4- / -> ri <-] zn i ί yy t of reverse osmosis membrane (OR) and one p nanofiltration membrane units (NC) in origin is pressurized to a value in the range of í (2.41 at 8.61 MPa) absolute, and dividing at 5 to provide an OR feed water to NC feed; if necessary, increase the water pressure of is OR to a value in the range of 900 to 1250 psi MPa) absolute before introducing the water of is 0 OR to the OR membrane units and extracts from OR and an OR retentate from of the OR membranes in which the member units operated or in a single-phase mode, pass in a two-phase, single-pass mode: recovery of the OR permeate is in the volume range, preferably 35 to 65 % by volume of OR feed water which is the OR membrane units such that a total dissolved solids content of less than 0 is a sulfate anion concentration of less and multivalent cation content of up to 10 ppm; if necessary, reduce the water pressure of ε Μ T V-S ΊΧ —l Ί Ί m TT —t Ί Xx IX - | Xl · Ρ -l Ί xl A O C / 1 C X, r-í -! is fed to NF permeate membrane units has a dissolved solids content, range 15,000 to 40,000 ppm, preferably 35,000 ppm, a concentration of sulfate anion 5 40 ppm, preferably less than 30 ppm and a multivalent t up to 200 ppm, preferably more preferably up to 100 ppm, and mixing at least a portion of the permeate minus a portion of the NF permeate in a range of 2: 1 to 40: 1, preferably 4: particular, 10: 1 to 25: 1 to provide injection having a dissolved solids content of 500 to 5,000 ppm, preferably 1,000, a sulfate anion concentration of less than .5 preferably, less than 5 ppm, more preferably than 3 ppm and a multivalent cation content of Again, the source water can be water; estuarine, a produced water, a residual aquifer. : 0 The preferred TDS for the source water, OR, the NF permeate and the injection water: indicated above for the first invention modality.
    Preferably, the multivalent concentration in the permeate of OR is in the range ppm, preferably 1 to 5 ppm, in particular, 5 Preferably, the multivalent concentration in the permeate of NF is in the range <ppm, preferably 50 to 150 ppm . The concentration of multivalent cations: injection will depend on the desired TDS to 0 and, consequently, the proportion of pc mixture of OR and permeate of NF. Thus, the multivalent concentration of the injection water will increase increasing amounts of the mixed NF permeate. Typically, the multivalent concentration 5 for a water stream with a total dissolved solids content of 1000 ppm from 2 to 10 ppm, and the values for the multivalent dc cation range should be sized at the highest TDS injection. 0 As discussed above, where oil recovery is desired to increase with low salinity water, the ratio between the desired salinity and the desired low multivalent concentration to obtain the increment increases when injected into a hydrocarbon form of a reservoir as long as 5 dissolved solids total damage formation and an i concentration low enough to mitigate the risk of in the reservoir (as well as mitigate the risk of insoluble mineral salts in formation and production).
    Typically, the formation in which the controlled salinity water (controlled TDS), lowers the controlled sulfate anion and low controlled multivalent concentration is injected is a sandstone containing oil that contains a high te · swellable, for example, smectite clays. swellable clays means an argj content of 10% by weight or greater, for example, a swellable te in the range of 10 to 30% by weight. 0 Typically, in this first and second π the present invention, the permeate of OR and the perme are mixed in a volume ratio (origin volume; (D) the temperature at which the OR units are operated; (E) volume recovery in percent. 5 OR and NF membrane units are operated; (F) the desired salinity of the injection water; (G) the desired concentration of anion sulfate injection, and (H) the multivalent cation concentration of the injection.
    Factors (F), (G) and (H) are, in turn, characteristics of the reservoir in which treated water is desired such as the amount of clays, levels of sulfate-reducing bacteria and 5 of multivalent cation of synergistic water depending on proportion of the mixture of permeate of NF permeate, the current of the inj water and sufficient salinity to control the form is a sulfate concentration sufficiently »0 to control the acidification in the sufficient multivalent cation concentration reservoir in which the ratio between the concentration ΊΊΐ ^ ΊΤΤηΙ / ΎΤΊ ^ Λ y] - Ί - »yJ yk -I vi —I y-χ y / X -yk -Λ ν '-Λ 1 / VI salinity (TDS content) of the water to be preferred is the conductivity of the Conductivity water is a measure of the TDS content of the injection. Alternatively, or additionally, the measure may be related to the multivalent concentration in the injection water or in the permeac divalent anion concentration selected sulfate anions, in the injection water or in the pe Alternatively, or additionally, the variable 0 is related to the concentration of kat in injection water or NF permeate, or that of selected multivalent cations, such as calcium and / or magnesium cations in NF permeate water. 5 The flow of the source water injection water stream can also be controlled by a measured variable.
    By "single-phase, single-pass mode that the feed water is passed through the plurality of individual membrane units arranged in parallel. Thus, one pass water for each of the me units: ΧΌΥΎΌΥί-Ι-ΛΊ χΊ ΙΧΥΥΊ Π / 4 / Λ Χχ Ί Ί TVt '"Λ xJ Χ Ί a defined period of time, for example, ο λ of feed processed in one day and combined c permeate volume produced in one day.
    By "two-phase, single-pass mode 5 that the feed water is fed to two membrane units that are arranged the retentate from the first units, to be used as feed water for the second membrane in the series. Typically, can the plurality of first member units arranged in parallel and a plurality of second membrane arranged in parallel Generally less second membrane units than the first membrane since the sec 5 units will process a smaller volume of water over the period of defined time than the units, membrane Typically, the strand currents of the first membrane units are to provide a first permeate stream and 0 of the retentate from the mixed first units to form a first stream The first stream of the retentate is then use —ϊ Ί -i YVl V “X 4“ νΛ —X v »-Ί —i -VS Ί 1 -Ί V · —x Π -! zl —1 z“ x. z-] z “i 1 - fc-S -Ί jJ —X zJ ζ- . □ typically mixed to provide a combined retentate which is discharged pair of desalination. However, there are others that form the various currents when operating a plurality of membrane 5 in a "two-phase, pa mode that are within the general knowledge of the art. The percentage recovery of the units when operated in a" two phases, the only one "is: [(volume of the first stream d from the units of the first membrane second stream of permeate from the second membrane) / the volume of food water units of the first membrane)) x 100]. This 5 determined over a period of time, for example, one day.
    NF membrane units are pi operated in a "single-phase, pass-through" OR membrane units are preferably 0 or a "single-phase, single-pass" two-phase, single-pass "mode" single phase, single pass ". A I TX X X <X * T "XX t ΤΎ x x> X X * Ί t VX xJ X. xJ X XI xJ X VA.
    Typically, the pressure differential of OR membrane units (water pressure and OR - combined OR retentate pressure) is 25 to 100 psi (0.17 to 0.68 MPa), preferably 5 (0.24 to 0 , 51 MPa), for example, about 50 ps. Therefore, the currents of the retentate OR membrane units are relatively high. Preferably, some OR retentate streams that are to be 0 from the combined C membrane units and the OF retentate stream passed through a recovery unit eg a hid recovery turbine: turbocharger that is coupled to a pump 5 for OR feed water. Thus, hydraulic recovery recovers the unit energy of the OR retentate and uses recovered water to increase the OR water pressure thereby reducing the pot requirements of the desalination plant. Typically, the current of the OR retentate combined with hydraulic recovery is less than 100 psi y y -> 4 y * 1 A —i ^ 7 Ct w y-y yr / A A 6 volume of NC feed water.
    Typically, the pressure differential NF membrane units (NF water pressure - NF retentate pressure) is at 5 100 psi (0.17 to 0.68 MPa). Therefore, the current of the combined NF retentate is typically low to ensure energy and current recovery. However, if desired energy is recovered from the retentate current 0 a hydraulic recovery unit.
    Preferably, the desalination plant has at least two membrane trains, more preferably, from 2 to 8, for example in particular, from 4 to 6 membrane trains, in c 5 comprises a plurality of memory units and a plurality of units of NF membrane. the ratio of OR membrane units to NF membrane in each train is in the d range preferably, 4: 1a 27: 1, in particular, 10: 0 therefore, an advantage of the present invention plant is that a NF separac which reduces space and weight considerations. maintenance, or the event of an emergency.
    Each train can be supplied with dedicated pumping, and, optionally, dedicated hydraulic recovery. Alternati '5 there is a common pumping system, optional common hydraulic recovery system, for trains.
    Preferably, the membrane units are arranged in a plurality of rows 0 in order to reduce the mark of the dess plant it is preferable that these rows are arranged in another. Preferably, each train has between 3 and 15 rows, preferably, and rows. Generally, there are between 4 and 5 membrane reads, preferably between 6 to 12 units in each row. Typically, n units are arranged together, for example, all or i membrane units of one or more of the NF membrane units. Where c 0 OR units are operated in a "two-phase, single" mode, it is preferred that the prim units in the series are arranged together in the NF membrane units and the OR membranes of each train comprise a compartment pressure confinement less than one membrane, preferably 4 to 85 compartments can be formed of glass or steel resin. Typically, each compares: to withstand a pressure in excess of 1100 p absolute, preferably in excess of 1300 p absolute, in particular, in excess of 1400 p absolute. Typically, the compartments are cylindrical and are arranged parallel to a row (or cradle), with the longitudinal axes of the overlying compartments in substantially horizontal. 5 In a first preferred aspect of the prosthesis, the source water can be pressurized <desired feed for the train units, for example, using a b pressure. The source water is then divided into the OR feed water for the OR units and the NC feed water for the NC membranes. Where the membrane units c Γ ”''" Λ V “X ν '—x zJ í — i Wi Ί 1 TY1 vyx jZx. Z * J z *. J> —xy — J Ί Ϊ -f- i — I y — xx% —x - »r NF feed, a combined retentary current driver and a permeate dii for an OR feed direct permeate current and NF feed dii are in fluid feed communication to the Where it contains only units of OR membrane o 'NF membrane, a feed line ate leading from the appropriate 0 director (OR feed head and dl NC feed, respectively) to individual membrane each row. Simi flow line of the common retentate and a common permeate line lead from the unit; 5 individuals from each row to the permeate and retentate direc respectively, where it contains both the OR membrane units and a dedicated common power line is to line OR membrane units that drive the OR feeder and an additional common dedicated feed to the; NF membrane leading from the above di, the inlet or feed pressure of NF units is in the range of 350 to 450 p absolute, in particular 380 to 420 psi (2, ê absolute, for example, about 400 psi absolute 5. Where the source water pressure desired inlet pressure for the NC units, the pressure relief valve can be fc on each common NC supply line this can be reduced for the inlet pressure <0 Alternatively, a control valve provided on or in each feed line NF membrane units where the valve regulates the flow of the source water to the NF membranes and also relieves the pressure from ê 5 to the desired inlet pressure for the NF membranes. It is also envisaged that a control can be provided upstream of the NF feed direction, thus controlling the source separation between the feed driver and the NF feed driver and, consequently, the separation of the source water between the units.of OR and NF membrane units. If ne Τ7ηΊτΓ1ΐΊ- X, I “i TT" I Xx x] Xx V> Xx Xi Xi Λ Λ A Zx 4- X> L nnlx XTA X <Xx therefore, it is necessary to increase the rush OR feed using an c preference, the compression pump is coupled with hydraulic recovery that retrieves the ene 5 of the combined retentate current that leaves the OR membrane. This recovery system h: be a hydraulic turbine, thus a shaft of driving a shaft of the pump However, the person skilled in the art will compose additional energy to be supplied for compression if the OR feed water is at the desired inlet pressure for the OR units. 5 Typically , the source water is press value in the range of 350 to 1,100 psi (2.41 absolute before being divided to provide OR feed and NE feed water to pressurize the source water to an inlet value above 0 for the units of water-dividing membrane the original one to supply OR and NF power. Thus, it is preferred that the NF water feed driver (which has typically been relieved at pressure in the range of 350 to 450 psi (MPa) absolute), a retentive driver 5 combined retentate stream and an permeate dii for a chain of permeate combir row contains only membrane units; common power line is provided leads from the OR feed driver to 0 individual c <OR membrane
    Similarly, a flow line from the retentate to the flow line of the common permeate leads to individual OR membrane units of the retentate and royal permeate 5 Where a row contains membrane units the common feed line is supplied to the NF membrane leading from the NC feed. Similarly, the NC units in the row are provided with common retentate and permeate lines 0 and the retentate and king permeate directives where a row contains both r units In a similar manner with the first aspectc of the present invention, a flow controller provided so as to control the separation of the magnet between the OR feeder and the NC feeder 5. Typically, a pressure valve is supplied upstream of the NC supply direction such that the pressure can be the desired inlet pressure for the NC units. However, it is also envisaged that a .0 pressure relief may be provided on the common NC supply or supply. Alternatively, above, a control valve can be upstream of the NI feed driver as well as separating the source water from the NC feed water. The provision of the membrane membrane units of the desalination plant makes it possible to continue to operate and produce saline water with sulfate anion concentration and multivalent concentration in the event that it becomes necessary: or more of the trains for maintenance or cleaning. membrane (s) contained in a common NF permeate line, these lines make a combined NF permeate line and back pressure can be provided on that line and combined NF. The back pressure valve at 5 NF permeate pressure is sufficient in OR permeate pressure to allow NF to be injected into the permeate driver, the resulting mixed permeate is the injection stream which then enters an injection flow line. Suitably, the backflow valve when the NF permeate pressure exceeds a defined one and allows sufficient foot flow through the valve to maintain the foot pressure above the pre-defined pressure. Typically, the set pressure of the back pressure valve is of pel (0.03 MPa) greater than the pressure of the perrn Generally, the pressure of the permeate of OR is 10 to 75 psi (0.06 to 0.51 MPa) absolute , from 20 to 55 psi (0.13 to 0.37 MPa) absolute. 0 Preferably, the source water can have at least one of: filtration to remove the cleaning material with chlorine, dosing with biocide, / 4 oo Ti m Λίπ 4- x πζλυπ i ίτπ ί Ί -ΐ / 4 / λ v- V Ή upstream of the desalination plant, pre-aerator can be provided downstream and desalination in order to control injection corrosion, injection pumps and the 5 advantage advantage of providing a downstream aerator is water that is de-aerated is substantially if the deaerator was available upstream and desalination. However, having a desalination plant deaerat reduces the risk of the interior of the desalination plant and, therefore, the use of cheaper steels. I was therefore able to provide an upstream desaler with desalination.
    In another embodiment of the present 5 a desalination plant is provided with a plurality of trains each comprising ur of OR membrane units and a plurality of NF membrane in which the ratio of OR membrane to membrane units of 0 membrane train it is in the range of 2: 1 preference, 4: 1 to 27: 1, in particular 10: 1 that each membrane train is supplied with: permeate lines combine to provide injection water; (C) a line of retentate (or directs »membrane units of OR and a line 5 (or direction) to the membrane units (D) a flow controller and valve therein on the NC supply line.
    As discussed above, it is envisaged that a flow and a pressure relief valve »0 combined in the form of a control valve Preferably, the units of m and arranged in rows placed one on top, the NF membrane units together in one or more rows. Typically, 5 diaphragms comprise between 3 and 15 corr rows comprising between 4 and 16 member units Preferably, a compression pump is an OR feed line and a hydraulic d unit in the OR retentate line where the hydraulic recovery is coupled to the pump d Typically, the hydraulic turbine recovery unit of the type descr 7 Ί t / h vmh ot ί τ τ Όι m ζ> · η Ί- '-χ ίί ϋί ί / 4 -λ / 4 vo / μί ν -χ / -χ ν- —χ ζ ~ χ t — χ -ΐ bbls (4,625.08 and 6,937, 62 L) of water due to desired salinity and low desired concentration.
    Preferably, a check valve 5 provided on the line of MC NF permeate the precise measurement of NF permeate in the foot thus resulting in the production of a water of the desired characteristics, for example, desired control, sulfa anion concentration The desired multivalent cation concentration. The present invention will now be described and the following examples and figures, in which: Figure 1 is a schematic diagram and desalination plant of the present invention, Figure 2 is a schematic diagram of process modification and design; present invention, and Figure 3 is a schematic diagram of membrane units for use in the present invention.
    In Figure 1, a water supply from a desalination plant that comprises a y] zx ί τ vx -i yJ —s yl y y y3 y. y »witx iz —x y y] y, / wx y. y -P -iy —x y] y. zx y * zvi ■> filtration system to remove the material to a desired level, typically at a level with a sediment density index (SE of less than 5 and preferably less than 3.5 SDI can be obtained using a known varieties, including microfiltration, ultra media filtration systems and filtrate pc filtration can be dosed with a cleaner downstream of the filtration system to remove free residual chlorine that could otherwise be used in the membrane units. they are downstream of the pump 4. The water of origin passed through a deaerator to remove thereby controlling corrosion in the dewatering plant; .5 downstream of the desalination plant, for example injection, injection pumps, and desired wells, Source water can also be biocide upstream of pump 4, in order to biological activity that otherwise might! The system Inhibitor of deposits can also be: source water upstream of pump 4, in order to deposit on the membrane surfaces the supply of NF 6 is controlled by flow 7. The pressure of the supply water is reduced to a value in the range of 350 to 45 '3.10 MPa) absolute through a valve 5 pressure 8 before to be fed to the NF 3 membranes. The OR 9 retentate removed from the OR 2 membrane and the NF retentate 10 NF 3 membrane units are discarded; OR 11 permeate removed from merr 0 units and NF 12 permeate removed from NF 3 units are combined to provide a water of controlled salinity and controlled concentration. Figure 2 is a modification of the desalination process of Figure 1, in which the source water pressure pump to an absolute value of Mpa) before dividing the OR 5 source water and a feed water of OR 5 to the plurality 0 of the OR 2 membrane is then compressed into the desired operating pressure of the OR 2 units (1100 psig) using an absolute (2.41 to 3.10 MPa) pump through a vacuum · pressure gauge 8, as described in relation to Figure 3 illustrates a train cross section of membrane 20 for use in the desalination process 5 of the present invention. The train c comprises seven rows 21 with each row eight membrane units 22 arranged substantially horizontal one on top of the other it is anticipated that the membrane train may buy .0 or less than seven rows and that each comprises more than or less than eight membrane. Each of the compartment membrane units that is substantially cylindrical having a length in the range of 35 to 345 in .5 8.76 meters), and an internal diameter in the inch range (6.35 cm to 1.91 meters). 0 share at least one spiral wound membrane (r preferably two to four membranes, preferably three or four wound membranes: 0 each of the spiral membranes wound in the form of a cylinder and have a length of 30 to 60 inches (0.762 at 1.52 meters) and X «» 4— X. IA VX X, vx X —X 4 Ύ ϊ · X. x] Xx Ό CT ■ —X Ί O Vx X. Ί Λ X * ·. xJ -. X. / Π The diaphragm train 20 has a dii feed 23a for the source water feeder 23b for NC water C. The feeder di 5 typically disposes substantially at the ve midpoint of the train such that the half of the OR membrane in each row is disposed on the sides of the row. For example, where each membrane has eight OR membrane units, the OR membrane can be supplied in both OR 23a feed director. train are osmosis units remaining ro are nanof membrane units with the proportion of OR units for unit 5 dependent on the desired mixture ratio of OR and NF permeate which, in turn, is recovery in% by volume of the permeate to the OR and NF membrane units. Figure 3 NF membrane units 24 arranged at the bottom 0 to the left of the feed driver; However, it is also provided that the NF feed dir 23b can be arranged on the pc a second common feed line 26 from the NF feed director 23b and NF membrane units 24 arranged for NF feed director 23b. Thus, the 5 through the second feed line and NC water supply. A control valve and pressure relief valve (do not go supplied on the second supply line <reduce the water supply pressure <0 working pressure of the units) The pressure relief valve is controlled by pressure controller (not shown ) such that NF feed water downstream of span 2 range 350 to 450 psi (2.41 to 3.10 MPa) 5 NF membrane units 24 are single pass d units with retentate from the membrane NF being rejected by a common retentate line (not shown) that leads to an NF retentate line (not shown) The permead * 0 each NF membrane unit is fed with common NF permeate p (not shown) which directs permeate of NF (not shown).
    Like the NF membrane units, a; OR membranes shown in Figure 3 are one-phase, single-pass. However, as the train pod OR membrane units <5 two-phase, single-pass units exist. In the art, I would understand how to modify the tra: so that the OR membrane units are a two-pass, single-pass mode. The OR membrane units of each row is to be fed through a common reject line (not shown) to the re-director (not shown). The NF retentate and optionally combined retent and / or are discharged from the environment, for example, to the sea, or are in an injection well or in a formation containing I or an aquifer. The permeate of the m units of each row is fed through common OR permeate (not shown) to a permeate dJ (not shown) where it is combined with 0 NC. The NF permeate line is provided with back pressure to ensure that the NF pressure is sufficiently above the multivalent heat (sum of ct magnesium concentrations) of 1830 ppm, feeding water at a rate of 320,000 barrels of water per day (ml desalination plant comprising a p 5 units of OR membrane and a plurality of NF membrane. The water supply is divided to provide an alirm water for the OR membrane units (310 mbwd) feed NC for units of 0 mbwd). The OR membrane units were the absolute pressure of 1000 psi (6.89 MPa) and 50% by volume, to provide 155 stream of OR permeate having a sulfate anion concentration TDS of 1.5 ppm and ume 5 of multivalent cation of 2.5 ppm. The water from and NC to the NC membrane units was pressure through a 400 psi (2.75 MPa) pressure relief valve to the absolute operation of the NC membrane units) 0 of the NC membrane were operated at a volume recovery, to provide 5 mbwd of one; permeate of NF having a dissolved solids content. Example 2 A stream of bai injection water can be prepared from water with a TDS content of 35,800 ppm, a sulfate concentration of 2,750 ppm and a multivalent concentration (sum of the concentrations of ct magnesium), of 1830 ppm, feeding water at a rate of 320 thousand barrels of water per day (ml desalination plant comprising a p .0 units of OR membrane and a plurality of <NF membrane. origen to provide a water supply for OR membrane units (261.4 mbwd) and NF supply for the membrar units 5 mbwd). The OR membrane units were at a pressure of 1000 psi (6.89 MPa) absolute and 50% by volume, to provide 130.7 mbwd of permeate OR having a TDS of 177 ppm, a cc anion sulfate of 1 , 5 ppm and a multivalent concentration of 2.5 ppm. The feed water to the NF membrane units was reduced through a pressure relief valve n r * d Αχ / 1ΓΊΓΊ vsz-ιη / O TE ΚΛ Ό -. . t-s. η λ Ί n 4— x / combined to provide 160 mbwd of an injection color having a TDS of 5000 ppm, a cc anion sulfate of 5.8 ppm and a multivalent concentration of 26.2 ppm (using a permeate ratio 5 of OR to permeate NF of 4.5: 1).
    权利要求:
    Claims (10)
    [1]
    1. Process for producing a water stream for injection of controlled salinity and controlled sulfate anion content that is suitable for injection into a formation containing oil from an oil reservoir, the process characterized by the fact that it comprises the steps of: ( a) feed a source water having a total dissolved solids content in the range of 20,000 to 45,000 ppm and a concentration of sulfate anion in the range of 1,000 to 4,000 ppm, for a desalination plant comprising a plurality of osmosis membrane units reverse (OR) and a plurality of nanofiltration membrane (NC) units in which the source water is pressurized to a pressure in the range of 2.41 to 8.61 MPa (350 to 1250 psi) absolute by a pumping system common for said plurality of OR membrane units and said plurality of NF membrane units, and dividing the source water to provide a feed water for the OR membrane units (hereinafter "OR feed water") and a feed water for the NC membrane units (hereinafter "NC feed water"); (b) increase the pressure of the OR feed water to a value in the range of 6.20 to 8.61 MPa (900 to 1250 psi) absolute if the OR feed water divided from the source water has a pressure less than 6 , 20 Mpa (900psi) absolute before introducing OR feed water to the OR membrane units and extracting an OR permeate and an OR retentate from the OR membrane units where the OR membrane units are operated in any a single-phase, single-pass mode or in a two-phase, single-pass mode where the recovery of OR permeate is in the range of 35 to 75% by volume based on the volume of the OR feed water that it is fed to the OR membrane units such that the OR permeate has a total dissolved solids content of less than 250 ppm, and a sulfate anion concentration of less than 3 ppm; (c) reduce the pressure of the NF feed water to a value in the range of 2.41 to 3.10 MPa (350 to 450 psi) absolute if the NF feed water divided from the source water has a pressure greater than 3.10 Mpa (450 psi) absolute by means of a pressure relief valve or a control valve before introducing the NF feed water to the NF membrane units and extracting an NF permeate and an NF retentate from the NF membrane units in which the NF membrane units are operated in a single-phase, single-pass mode and in which the NF membrane units are operated with an NF permeate recovery in the range of 35 to 60% in volume based on the volume of the NF feed water that is fed to the NF membrane units such that the NF permeate has a total dissolved solids content in the range of 15,000 to 40,000 ppm and a sulfate anion concentration of less than 40 ppm; and (d) mixing at least a portion of the OR permeate and at least a portion of the NF permeate in a ratio ranging from 2: 1 to 40: 1 at a mixing point, to provide an injection water having a content total dissolved solids in the range of 500 to 5,000 ppm and a sulfate anion concentration of less than 7.5 ppm; and where the NF permeate pressure is maintained at least 0.03 MPa (5 psi) above the OR permeate pressure via a back pressure valve which is supplied upstream of the mixing point for the permeate of NF and OR permeate and wherein the NF permeate is injected into the OR permeate at the mixing point to form the injection water.
    [2]
    2. Process, according to claim 1, characterized by the fact that the source water has a multivalent cation concentration in the range of 700 to 3,000 ppm, the OR permeate has a multivalent cation content of up to 10 ppm, the NF permeate has a multivalent cation content of up to 200 ppm, and the injection water has a multivalent cation content of up to 50 ppm.
    [3]
    3. Process according to claim 1, characterized by the fact that the energy is recovered from the OR retentate using a hydraulic recovery unit and in which the OR water pressure is increased in step (b) , using a compression pump that is coupled to the hydraulic recovery unit.
    [4]
    4. Process according to claim 1, characterized by the fact that the pressure of the NF feed water is reduced in pressure in step (c) to a pressure in the range of 2.41 to 3.10 MPa (350 to 450 psi) absolute, through a pressure relief valve.
    [5]
    5. Process according to claim 1, characterized by the fact that the source water is selected from sea water, estuarine water, a produced water, a water aquifer, and a waste water.
    [6]
    6. Process according to claim 1, characterized by the fact that the total dissolved solids content of the OR permeate is in the range of 50 to 225 ppm and the sulfate anion content of the OR permeate is at least 0, 5.
    [7]
    7. Process according to claim 1, characterized by the fact that the total dissolved solids content of the NF permeate is not more than 15,000 ppm less than the total dissolved solids content of the source water and in which the permeate of NF has a sulfate anion concentration of at least 10 ppm.
    [8]
    8. Process according to claim 2, characterized by the fact that the concentration of multivalent cation in the OR permeate is in the range of 1 to 10 ppm and the concentration of multivalent cation in the NF permeate is in the range of 50 to 200 ppm.
    [9]
    9. Process according to any one of claim 1, characterized by the fact that one or more of the source water flow rate, the proportion of the OR permeate and NF permeate mixture, and the injection water flow rate are determined according to a measured variable that is selected from one or more of the injection water conductivity, the total concentration of divalent anions in the injection water or in the NF permeate, and the concentration of sulfate anions in the injection water or in the NF permeate .
    [10]
    10. Process according to claim 4, characterized by the fact that the pressure of the NC feed water is reduced in pressure in step (c) to a pressure in the range of 2.62 to 2.89 MPa (380 to 420 psi) absolute, through a pressure relief valve.
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    公开号 | 公开日
    EP2523908B1|2018-10-24|
    EA025116B1|2016-11-30|
    WO2011086346A1|2011-07-21|
    EA201201005A1|2013-02-28|
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    CA2786348C|2018-04-03|
    US9492790B2|2016-11-15|
    AU2011206433A1|2012-07-19|
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    US20150083656A1|2015-03-26|
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    法律状态:
    2018-04-10| B06F| Objections, documents and/or translations needed after an examination request according [chapter 6.6 patent gazette]|
    2019-01-29| B06T| Formal requirements before examination [chapter 6.20 patent gazette]|
    2019-10-08| B09A| Decision: intention to grant [chapter 9.1 patent gazette]|
    2019-12-03| B16A| Patent or certificate of addition of invention granted [chapter 16.1 patent gazette]|Free format text: PRAZO DE VALIDADE: 20 (VINTE) ANOS CONTADOS A PARTIR DE 11/01/2011, OBSERVADAS AS CONDICOES LEGAIS. (CO) 20 (VINTE) ANOS CONTADOS A PARTIR DE 11/01/2011, OBSERVADAS AS CONDICOES LEGAIS |
    优先权:
    申请号 | 申请日 | 专利标题
    EP10250063|2010-01-14|
    PCT/GB2011/000032|WO2011086346A1|2010-01-14|2011-01-11|Process of supplying water of controlled salinity|
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