DK177793B1 - System and Method of Separating Oil and Particles from Produced Water or Fracturing water - Google Patents
System and Method of Separating Oil and Particles from Produced Water or Fracturing water Download PDFInfo
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- DK177793B1 DK177793B1 DK201370603A DKPA201370603A DK177793B1 DK 177793 B1 DK177793 B1 DK 177793B1 DK 201370603 A DK201370603 A DK 201370603A DK PA201370603 A DKPA201370603 A DK PA201370603A DK 177793 B1 DK177793 B1 DK 177793B1
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Abstract
This invention relates to a system and a method of separating oil and water from produced or fracturing water comprising at least the steps of feeding through produced or fracturing water to a mechanical separation system comprising a solid-fluid separator with a membrane system configured to process the produced or fracturing water in an intended separation direction; and which membrane system is configured with a back flush system. The method comprises a step of separating oil to an oil conduit and water to a water conduit. The method comprises a step of back flushing the membrane system with a back flushing fluid using water from the water conduit. For continuous operation the step of back flushing is performed periodically.
Description
DK 177793 B1
Title
System and Method of Separating Oil and Particles from Produced Water or Fracturing Water 5 Field of the Invention
This invention relates to systems and method of separating oil and particles from produced water or fracturing water. In particular this invention relates to maintaining an operational membrane system during operation of a separation system.
10 Produced water is water that surfaces together with oil or gas in an oil or gas well, hence the term produced.
Fracking is the process where water with chemicals and sand is pumped into a hydrocarbon containing formation in order to create fractures from where oil and gas can be produced.
15
The method is gaining increasing popularity, but is mainly used in tight reservoirs or shale formation.
For water that surfaces after a fracking operation, the specific term is frac flow-back water 20 or fracturing water.
The amount of water pumped into the underground is site specific, of which 5%-30% comes back as flowback water. Flowback water constitutes huge volumes, and therefore has a big natural impact if not treated or disposed of in a well. Typical flow back water composition is 25 shown in the below table.
Content: Value:
Water 90%
Proppant (silica sand) 9.5 %
Chemicals 0.5 %
1000 mg/L-7000 mg/L
Page 1 of 23 DK 177793 B1
Total Suspended Solids (TSS)
Total Dissolved Solids (TDS) 30,000 mg/L - 180,000 mg/L
Total Organic Carbon (TOC) 30 mg/L-40 mg/L
Oil & Grease 20 mg/L -100 mg/L
Volume pr. frac 2200 m3 - 8000 m3
Background of the invention
This invention intends to improve the overall performances of a separation system, to improve, maintain or reduce decrease in efficiency over time of a membrane system in the 5 separation system.
Relevant prior art is disclosed in GB1456304, which discloses a process and a shystem for treating an oil-water emulsion. First solids are removed in a surge tank. The liquid fraction is then introduced to an ultrafiltration membrane unit and the retentate is led to an oil 10 separator, which separates oil from a residual fraction which is recycled to the ultrafiltration unit.
Known problems in operation of separation systems include fouling and possible irreversible fouling of the membrane. An object of this invention is to avoid or reduce fouling thereby 15 maintaining or avoiding or postponing decline in the efficiency loss of the membrane.
Several problematic issues exist in operational separation of oil and water from produced or fracturing water, some issues or challenges include silica precipitation in the porous matrix of the membrane. This may be in steam Enhanced Oil Recovery {EOR)_applications.
20
Other issues include irreversible fouling by naphthenic and other petroleum acids.
Yet other issues include pore blocking of membranes by asphaltenes.
25 Summary
An objective of this invention is achieved by a system of separating oil and water from produced or fracturing water with an intended separation direction, the system comprising a Page 2 of 23 DK 177793 B1 solid-fluid separator such as a hydro cyclone followed by a membrane system configured to output clean water and to feed remaining fluid to a an oil extractor system configured to output oil.
5 By fracturing water may be understood as any fracturing fluids.
In particular a system wherein the membrane system is further configured with a flushing system and preferably a backward flush system is advantageous.
A further advantageous system may be achieved when the backward flush system is further 10 configured to flush or back-flush with a flushing agent.
According to an embodiment the flushing and preferably the backward flush system may further be configured to flush with pulses and preferably back-flush with back-pulses.
15 In an embodiment the membrane system is a ceramic membrane system.
Such system may be configured in a variety of implementations and the person skilled in the art will be able to choose several starting points.
20 One such starting point of a system may be a system configured with a unit for feeding the produced or fracturing water to a solid-fluid separator such as a hydro cyclone followed by a membrane system configured to output clean water and feed a remaining fluid to a decanter configured to output solids and to feed a remaining fluid to a high speed separator configured to output oil and with a feedback conduit for feeding a remaining water 25 containing fluid back to the membrane system.
Another such starting point of a system may be a system configured with a unit for feeding the produced or fracturing water to a solid-fluid separator such as a hydro cyclone followed by a decanter with an output to solids and a feed of a liquid fraction to a membrane system 30 configured to output clean water and feed remaining fluid to a high speed separator configured to output oil and with a feedback conduit for feeding a remaining water containing fluid back to the membrane system.
Page 3 of 23 DK 177793 B1
Yet another such starting point of a system may be a system configured with a unit for feeding the produced or fracturing water to a solid-fluid separator such as a hydro cyclone followed by a membrane system configured to output clean water and feed remaining fluid 5 to centrifuge, preferably a nozzle centrifuge, configured to output oil and with a feedback conduit for feeding a remaining water containing fluid back to the membrane system.
All of those disclosed systems may have the membrane system further configured to be flushed by a back flushing system using a flushing agent, which back flushing system 10 comprises a back flush pump configured to provide pressure, preferably in connection with a pressure vessel a back flush valve configured to regulate the provided pressure in the membrane system for a given period of time, and a permeate valve configured to equalise pressure in the membrane system.
15 According to an embodiment, the flushing system and/or the backward flushing system may be configured to produce a flushing sequence with pulses of variable pressures, variable pulse width and/or variable pulse period.
The effects of these system elements are understood as they are or in the context of using 20 the systems. Furthermore an object of this invention is achieved by a method of separating oil and water from produced or fracturing water comprising at least the steps of feeding through produced or fracturing water to a mechanical separation system comprising a solid-fluid separator with a membrane system configured to process the produced water in an intended separation direction; and which membrane system is configured with a back flush 25 system. The method comprises a step of separating oil to an oil conduit and water to a water conduit. The method comprises a step of back flushing the membrane system with a back flushing fluid using water from the water conduit. For continuous operation the step of back flushing is performed periodically.
30 The back flushing results in cleaning the membrane to maintain performance over time and thereby providing a more efficient method than without back flushing.
Page 4 of 23 DK 177793 B1
The cleaning may be of particles, chemicals, grease, grown organic organism or any other impurity or combinations thereof.
One particular issue observed is membrane fouling during filtration. It is a common 5 phenomenon that heavily influence membrane performance due to the impact on the permeate flux and trans-membrane pressure.
Back flushing has been observed to maintain a high performance of the membranes and back flushing has in some cases been found to be essential for the process of separating oil 10 and water to function since fouling otherwise would make the separation process impossible, work with difficulties, or with lower than feasible efficiencies.
In order to maintain the high performance of the membranes back flushing as a process where the flow occurs from the permeate side through the membrane and lifts dirt and 15 deposits off membrane surface lasting seconds or minutes.
The liquid or fluid forced through the membrane can be permeate, clean water or water with addition of miscellaneous chemicals.
20 Typically the produced water contains particles ranging from lOOnm to 500 micron. Those particles can negatively impact the functioning of membranes and back flushing will help clean the membranes from those particles.
A separation system will typically be designed for flows between 5m3/h to 200 m3/h. The 25 pressure of the fluid through the system will not exceed 6 bar (90 psi). Thus this invention relates to separation systems of this capacity although a person skilled in the art will not be limited to such capacities.
In one or more embodiments each step of back flushing is performed using at least one back 30 pulse; preferably a series of 5 to 20 back pulses.
Page 5 of 23 DK 177793 B1
Back pulsing or pulses of back flushing is defined as a back flush for a very short time (seconds or milliseconds), typically at frequent intervals.
Pulses are simply a very short back flush and created by a fast acting valve and a pump, a 5 pressurized vessel or a piston
In one or more embodiments, the use of a "block" or a square pulse on the permeate side is advantageous. Such square pulse can be obtained by building up the pressure and then release it with a quick-release mechanism or by activating the piston.
10
Such square pulses may be more efficient, as it will loosen the fouling material over the entire surface, as opposed to smoother pulses, which will only loosen the easiest removable fouling material.
15 A person skilled in the art will appreciate that more frequent back pulses may be preferable over long lasting back pulses, as it is the initial impact from the pulse which is the most efficient part of the pulse.
In one or more embodiments each back pulse may be performed between 1 ms and 10 s; 20 preferably between 100 ms and 1 s.
The pressure amplitude shall be between 0.5 bar and the system maximum allowable pressure. The amplitude is achieved by either increasing permeate pressure or by decreasing the retentate pressure or by doing both simultaneously.
25
The widths described above may be found experimentally using a few iterations. A person skilled in the art will appreciate that the widths will vary and may depend on the feed.
In general, it is advantageous to keep the pulses as short as possible in order to avoid 30 excessive loss of production time and/or clean water.
Page 6 of 23 DK 177793 B1
One strategy may be to start with a short pulse width. If it works, then a pulse width half the width may be tried, and so repeated until a diminishing effect is reached.
If the starting width does not work, then a pulse width double the starting width may be 5 tried, and so repeated until an effect is reached.
When either of the above widths is determined, interpolating the interval between the two widths may be used to find an optimum width.
10 In one or more embodiments each back flush is performed within a period of time; preferably between every 1 min to 10 min; most preferably between every 3 to 5 min. This may be per membrane loop or per housing comprising a membrane
In a similar fashion to finding a pulse width, a flushing interval or period may be found.
15 A person skilled in the art will find it natural to experiment to find an optimal overall efficiency and include parameters such as water used, efficiency of membrane, energy used and time required to obtain or maintain a level.
20 In one or more embodiments, the pulse width and pulse period is changed or controlled dynamically. In a further embodiment the width and period parameters are used as control parameters to control for a predetermined efficiency as a set point.
In one or more embodiments the method further comprises a step of adding a flushing 25 agent to the back flushing fluid and thus flushing with a fluid containing a flushing agent.
Thereby further enhancing the effect of the back flushing. Hence the back flush will work both mechanically by loosening the foulants, and chemically by dissolving them.
30 Generally, however, it is not desirable to add an agent since an agent may cause precipitation of salts or other substances in the system.
Page 7 of 23 DK 177793 B1
An agent will also induce an additional operating cost, so operators are generally reluctant to frequently introduce chemicals into the system.
However, it has been found that a particular flushing agent is suitable in systems or methods 5 of separating produced or fracturing water as disclosed. One such flushing agent comprises no more than a total of 100 % of: between 5 to 70 % w/w Sodium Carbonate; between 1 to 20 % w/w Disodium Metasilicate; between 1 to 20 % w/w Sodium Percabonate; 10 between 1 to 20 % w/w Sodium Silicate; between 0.1 to 15 w/w % of a Fatty Alcohol Alkoxylate; preferably between about 25 to 60 % w/w Sodium Carbonate; between 4 to 15 % w/w Disodium Metasilicate; 15 between 4 to 15 % w/w Sodium Percabonate; between 4 to 15 % w/w Sodium silicate; between 1 to 10 % w/w of a Fatty Alcohol Alkoxylate.
An alternative flushing agent comprises no more than a total of 100 % of: 20 between 0.1 to 10 % w/w Sodium Silicate preferably premixed with between 0.1 to 10 % w/w Nonionic surfactant and mixed with: between 1 to 20 % w/w Sodium percarbonate; between 5 to 40 % w/w Sodium silicate; between 5 to 40 % w/w Sodium carbonate; and 25 preferably between 1 to 5 % w/w Sodium Silicate preferably premixed with between 1 to 5 % w/w Nonionic surfactant and mixed with: between 5 to 15 % w/w Sodium percarbonate; between 15 to 30 % w/w Sodium silicate; 30 between 15 to 30 % w/w Sodium carbonate.
Page 8 of 23 DK 177793 B1
Yet another alternative flushing agent flushing agent comprises no more than a total of 100 % of: between 0.1 to 20 % w/w Citric acid; between 0.1 to 10 % w/w Glycolic acid; 5 between 1 to 20 % w/w Lactic acid; between 0,1 to 10 % w/w Surfactant; preferably between 5 to 15 % w/w Citric acid; between 1 to 5 % w/w Glycolic acid; 10 between 5 to 15 % w/w Lactic acid; between 1 to 5 % w/w Surfactant;
Circulating a flushing agent in the system for no less than 20 s up to, but not limited to 120 min may be required to achieve the effect depending on the fracturing or produced water, 15 the mixtures of the flushing agents and the dilutions.
In one or more embodiments, the solution with the flushing agent may be circulated in the system 1-120 min at elevated temperatures. A subsequent water flush will remove the solution from the system.
20
In alternative embodiments adding an acid to the flushing procedure may make the flushing further advantageous. A citric acid may be used.
An objective of this invention may be achieved by an exemplary method of separating oil 25 and water from produced or fracturing water using a water-oil separation system configured with unit for feeding the produced water to a solid-fluid separator such as a hydro cyclone followed by a membrane system configured to output clean water and feed a remaining fluid to a decanter configured to output solids and to feed a remaining fluid to a high speed separator configured to output oil and with a feedback conduit for feeding a remaining 30 water containing fluid back to the membrane system, which membrane system further is configured to be flushed by a back flushing system using a flushing agent.
Page 9 of 23 DK 177793 B1
In such configuration using a flushing agent comprising no more than a total of 100 % of: between 0.1 to 10 % w/w Sodium Silicate preferably premixed with; between 0.1 to 10 % w/w Nonionic surfactant and mixed with between 1 to 20 % w/w Sodium percarbonate; 5 between 5 to 40 % w/w Sodium silicate; between 5 to 40 % w/w Sodium carbonate; and a carrier such as water as required; preferably between 1 to 5 % w/w Sodium Silicate preferably premixed with; 10 between 1 to 5 % w/w Nonionic surfactant and mixed with between 5 to 15 % w/w Sodium percarbonate; between 15 to 30 % w/w Sodium silicate; between 15 to 30 % w/w Sodium carbonate; and a carrier such as water as required.
15
An objective of this invention may be achieved by an exemplary method of separating oil and water from produced or fracturing water using a water-oil separation system configured with a unit for feeding the oil rich fluid to a solid-fluid separator such as a hydro cyclone followed by a decanter with an output to solids and a feed of a liquid fraction to a 20 membrane system configured to output clean water and feed remaining fluid to a high speed separator configured to output oil and with a feedback conduit for feeding a remaining water containing fluid back to the membrane system and which membrane system further is configured to be flushed by a back flushing system using a flushing agent.
25 In such configuration using a flushing agent comprising no more than a total of 100 % of: between 0.1 to 10 % w/w Sodium Silicate preferably premixed with; between 0.1 to 10 % w/w Nonionic surfactant and mixed with between 1 to 20 % w/w Sodium percarbonate; between 5 to 40 % w/w Sodium silicate; 30 between 5 to 40 % w/w Sodium carbonate; and a carrier such as water as required; preferably
Page 10 of 23 DK 177793 B1 between 1 to 5 % w/w Sodium Silicate preferably premixed with between 1 to 5 % w/w Nonionic surfactant and mixed with; between 5 to 15 % w/w Sodium percarbonate; between 15 to 30 % w/w Sodium silicate; 5 between 15 to 30 % w/w Sodium carbonate; and a carrier such as water as required.
An objective of this invention may be achieved by an exemplary method separating oil and water from produced or fracturing water using a water-oil separation system configured 10 with means for feeding the oil rich fluid to a solid-fluid separator such as a hydro cyclone followed by a membrane system configured to output clean water and feed remaining fluid to a nozzle centrifuge configured to output oil and with a feedback conduit for feeding a remaining water containing fluid back to the membrane system; and which membrane system further is configured to be flushed by a back flushing system using a flushing agent.
15
In such configuration using a flushing agent comprising no more than a total of 100 % of: between 0.1 to 10 % w/w Sodium Silicate preferably premixed with between 0.1 to 10 % w/w Nonionic surfactant and mixed with; between 1 to 20 % w/w Sodium percarbonate; 20 between 5 to 40 % w/w Sodium silicate; between 5 to 40 % w/w Sodium carbonate; and a carrier such as water as required; preferably between 1 to 5 % w/w Sodium Silicate preferably premixed with 25 between 1 to 5 % w/w Nonionic surfactant and mixed with between 5 to 15 % w/w Sodium percarbonate; between 15 to 30 % w/w Sodium silicate; between 15 to 30 % w/w Sodium carbonate; and a carrier such as water as required.
This method and system would be suitable for produced water, where the system needs to be compact; the oil has an API degree over 10 and does not contain large amounts of solid, 30
Page 11 of 23 DK 177793 B1 e.g. less than 1000 mg/L. This could for example be separation of produced water from a conventional well situated far from ordinary oil/gas infrastructure, which therefore has the need for onsite treatment of the water.
5 An objective of this invention may be achieved by a method of separating oil and water from produced or fracturing water wherein performing at least one back flush of the module using a 0,1 to 10 % w/w solution of a flushing agent comprising no more than a total of 100 % of: between 0.1 to 20 % w/w Citric acid; 10 between 0.1 to 10 % w/w Glycolic acid; between 1 to 20 % w/w Lactic acid; between 0,1 to 10 % w/w Surfactant; and a carrier such as water as required; preferably 15 between 5 to 15 % w/w Citric acid; between 1 to 5 % w/w Glycolic acid; between 5 to 15 % w/w Lactic acid; between 1 to 5 % w/w Surfactant; and a carrier such as water as required; 20
Thereby is provided an alternative separation, albeit less effective separation than those previously disclosed.
It is noted that the solid-liquid separator might be preceded by an oxidation step, where ions 25 in the feed liquid will be oxidized in order to form particles which subsequently will be removed by the solid-liquid separator. The ions will preferably be Fe2+ or Fe3+ oxidized into Fe(OH)2 or other.
An object of the invention is further achieved by a method of restarting a system configured 30 for separating oil and water from produced or fracturing water as disclosed and having a clogged membrane; the method comprising performing at least one back flush of the module using a method as disclosed.
Page 12 of 23 DK 177793 B1
It is understood that the restarting can be done either with a flushing system permanently attached or by attaching a flushing system as disclosed and then performing a back flush as described.
5 A person skilled in the art will appreciate that conduits between the units need to be applied as needed. Moreover a person skilled in the art will appreciate that additional conduits may be needed to balance the intended flows in the system. Likewise a person skilled in the art will appreciate when there is a need to add buffers to the system.
10 The present invention will now be described more fully hereinafter with reference to the accompanying drawings, in which exemplary embodiments of the invention are shown. The invention may, however, be embodied in different forms and should not be construed as limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the 15 invention to those skilled in the art. Like reference numerals refer to like elements throughout. Like elements will, thus, not be described in detail with respect to the description of each figure.
Brief Description of Drawings 20 Embodiments of the invention will be described in the figures, whereon:
Fig. 1 illustrates a first embodiment of an oil-water separation system;
Fig. 2 illustrates a second embodiment of an oil-water separation system;
Fig. 3 illustrates a third embodiment of an oil-water separation system;
Fig. 4 illustrates pressures of back pulses and shapes of back pulses 25 Fig. 5 illustrates an implementation of a procedure for performing a back flush; and
Fig. 6 illustrates the effect on the flux through a membrane system using different kinds of back flushing.
Detailed Description 1 Water-Oil Separation system 2 Water
Page 13 of 23 DK 177793 B1 1 Toil 4 Produced or fracturing water 5 Oil field 6 Solids 8 O i I ext ra cto r syste m 10 Solid-fluid separator 12 Decanter 14 High Speed separator 16 Membrane system 18 Membranes 19 Nozzle centrifuge 20 Separation direction 22 Backward direction 30 Flushing System 32 Flush Agent 34 Backward Flush System 40 Back Pulses 42 Pulse width 44 Pulse period 50 Back flushing 52 Permeate valve 54 Back flush pump 56 Bypass valve 58 Back flush valve
Fig. 1 to fig. 3 depict individual configurations or embodiments of water-oil separation systems 1 configured to separate water 2 and oil 3 from an oil water fluid such as produced (or frac) water 4 most likely from an oil field 5. The produced water 4 may contain solids 6 of 5 varying sizes.
Page 14 of 23 DK 177793 B1
The water-oil systems 1 depicted have several elements or subsystems in common. Those elements include a solid-fluid separator 10 which may be a hydro cyclone or any equivalent and configured to separate solids 6 from the produced water 4, a decanter 12 configured to further separate solid fractions 6' in the process, a high speed separator 14 configured to 5 extract oil 3 and preferably purified oil 3.
The water-oil systems 1 further have a membrane system that may be a membrane system 16 configured with membranes 18 to extract water 2 and preferably clean water.
10 Each system has an intended direction of separation 20 and each unit or subsystem is configured to be coupled each with an intended direction of separation 20. Each system or sub system has an opposite flow direction to the direction of separation, i.e. a backward direction 22.
15 In an embodiment it may be desirable to use a nozzle centrifuge 19 rather than high speed separator 14. This illustrated in fig. 3.
The illustrated embodiments in fig. 1, 2, and 3 all have an additional embodiment with a flushing system 30 configured to flush the water-oil system 1 and as specifically illustrated 20 configured to flush the membrane system 16 and thus the membranes 18 with a flush agent 32. In particular the embodiments illustrate the flushing systems 30 configured as a back flushing systems 34.
Fig. la illustrates a water-oil separation system 1 configured with unit for feeding the 25 produced water 4 to a solid-fluid separator 10 such as a hydro cyclone followed by a membrane system 16 configured to output clean water 2 and feed a remaining fluid to a decanter 12 configured to output solids 6 and to feed a remaining fluid to a high speed separator 14 that is configured to output oil 5 and with a feedback conduit for feeding a remaining water containing fluid back to the membrane system 16.
Fig lb illustrates an embodiment as in fig. la where the membrane system 16 further is configured to be flushed by a back flushing system 34 using a flushing agent 32.
30
Page 15 of 23 DK 177793 B1
Fig. 2a illustrates a water-oil separation system 1 configured with a unit for feeding produced water 4 to a solid-fluid separator 10 such as a hydro cyclone followed by a decanter 12 with an output of solids 6 and a feed of a liquid fraction to a membrane system 5 16 configured to output clean water 2 and feed remaining fluid to a high speed separator 14 configured to output oil 3 and with a feedback conduit for feeding a remaining water containing fluid back to the membrane system 16.
Fig. 2b illustrates an embodiment as in fig. 2a where the membrane system 16 further is 10 configured to be flushed by a back flushing system 34 using a flushing agent 32.
Fig. 3a illustrates a water-oil separation system 1 configured with means for feeding the produced water 4 to a solid-fluid separator 10 such as a hydro cyclone followed by a membrane system 16 configured to output clean water 2 and feed remaining fluid to a 15 nozzle centrifuge 19 configured to output oil 3 and with a feedback conduit for feeding a remaining water containing fluid back to the membrane system 16 and
Fig. 3b illustrates an embodiment as in fig. 3a where the membrane system 16 further is configured to be flushed by a back flushing system 34 using a flushing agent 32.
20
Fig. 4 illustrates back pulses 40 that the back flushing system 34 is configured to generate.
Each back pulse 40 has a pulse width 42 and a pulse period 44.
Fig. 4a illustrates back pulses 40 that are formed as squares and fig. 4b back pulses 40 that 25 are smoother.
Fig. 5 illustrates a procedure for back flushing 50. The procedure may be used for the different embodiments described and generally relates to an implementation of a back flush system 34.
Generally it is understood that a person skilled in the art will know which type of conduits or pipes to use and which valves and pumps to use. The below description is therefore a guide 30
Page 16 of 23 DK 177793 B1 to an implementation that will realise the described steps in the procedure of back flushing 50 with references to the previous disclosed systems.
There is a first step during which a permeate valve 52 closes. There is a second step where a 5 back flush pump 54 starts to pressurise the pressure vessel. There is a third step where a bypass valve 56 opens to maintain the pressure low in the loop. There is a fourth step where a back flush valve 58 opens for the duration of the pulse width 42 of a back pulse 40 and closes again. There is a fifth step where the permeate valve 52 opens again. The time between the closing and reopening of the permeate valve 52 in step one and step five 10 essentially defines the pulse period 44.
Fig. 6 illustrates a temperature standardised flux through a membrane system installed with ceramic membrane during a clearing procedure of the membrane system.
15 The temperature standardised flux shows the effect of a back flushing 50.
In order to clean the system a cleaning procedure was initiated, with a water flush, a flush with a membrane detergent and a flush with the alkaline detergent with the composition mentioned earlier.
20
The initial water flush was performed for about ΛΑ hrs resulting in a small increase in flux from 0.5 to 0.7 LMH/kPa.
A flux level of about 0.7-0.8 LMH/kPa is seen until about lhrs. Between 1 to 2 hrs a back 25 flushing 50 using an acid flushing agent, a citric acid, is observed to improve the flux rate to about 2 LMH/kPa with a noticeable flux increase from 0.7 to 1.5 LMH/KPA followed by a period where the effects of the acid back flushing diminishes. The citric acid solution was an approximate 1 % solution at a pH of 2-3.
30 The oil-water separating virtually clogs at about 2 hrs taking the flow to about zero and an alkaline wash, a mixture of some percents of a sodium hydroxide, an anionc surfactant, a citric acid, a sodium carbonate dissolved in alcohols, which is not within the composition of
Page 17 of 23 DK 177793 B1 the disclosed flushing agent is performed for 1.5 hrs until about 3.5 hrs after the acid wash.
At about 3 hrs, the permeate valve was opened to allow filtration with alkaline wash. There was no noticeable flux increase observed. The alkaline wash solution was approximately 1-2 % at a pH of 7.
5
At about 3.5 hrs and for about 1 hrs a cleaning procedure using a cleaning agent branded as Solution 100 provided by the applicant, which has a composition within the preferred range was used as a flushing agent, was performed and an increase in flux from 1.5 to 2.2 LMH/kPA was observed. The Solution 100 was approximately 1-2 % at a pH of 8-9.
10
The oil-water separation system membrane system recovers its flux at about 3.5 hrs at a flux level of about 2 LMH/kPa.
A final flush with water was performed for about Vi hrs after 4.5 hrs of operation. The flux 15 still continued to increase during this time to about 2.3 LMH/kPa.
The system may have still have contained a branded Solution 100 by the applicant and more water was added to the system during the flush and the system was neutral at the end.
20 The system was seen to have obtained 99 % of the water flux measured with a clean system.
Hence flushing using back-flushing improves the flux of the membrane system and thus the oil-water separation system.
Page 18 of 23
Claims (12)
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DK201370603A DK177793B1 (en) | 2013-02-15 | 2013-10-22 | System and Method of Separating Oil and Particles from Produced Water or Fracturing water |
Applications Claiming Priority (4)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DK201370086A DK177844B1 (en) | 2012-12-18 | 2013-02-15 | System and method for separating oil and particles from produced water or fracturing water |
| DK201370086 | 2013-02-15 | ||
| DK201370603A DK177793B1 (en) | 2013-02-15 | 2013-10-22 | System and Method of Separating Oil and Particles from Produced Water or Fracturing water |
| DK201370603 | 2013-10-22 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| DK177793B1 true DK177793B1 (en) | 2014-07-07 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| DK201370603A DK177793B1 (en) | 2013-02-15 | 2013-10-22 | System and Method of Separating Oil and Particles from Produced Water or Fracturing water |
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| Country | Link |
|---|---|
| DK (1) | DK177793B1 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO20190082A1 (en) * | 2019-01-22 | 2020-07-23 | Rena Quality Group As | A WATER-OIL SLUDGE SEPARATION SYSTEM |
-
2013
- 2013-10-22 DK DK201370603A patent/DK177793B1/en active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO20190082A1 (en) * | 2019-01-22 | 2020-07-23 | Rena Quality Group As | A WATER-OIL SLUDGE SEPARATION SYSTEM |
| NO345234B1 (en) * | 2019-01-22 | 2020-11-16 | Rena Quality Group As | A WATER-OIL SLUDGE SEPARATION SYSTEM |
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