KR102338769B1 - System for manufacturing smart water - Google Patents

Abstract

Smart water system according to an embodiment of the present invention, a separation unit for removing the solid material contained in the production water generated in the crude oil extraction process; a crystallization unit for removing the ionic material contained in the produced water that has passed through the separation unit; a storage unit for storing the produced water discharged from the crystallization unit; and a recovery unit for recovering the ion component from the crystallization sludge discharged from the crystallization unit, wherein the recovered ion component is injected into the storage unit or a transfer line connected to the storage unit to produce smart water do it with

Description

Smart water production system {System for manufacturing smart water}

The present invention relates to a smart water production system, and more particularly, to a smart water production system for efficiently producing smart water used in a crude oil extraction process.

The content described in this section merely provides background information for the present embodiment and does not constitute the prior art.

In the case of mining underground oil, production using natural pressure without pressure reinforcement is called the first recovery step, and the second recovery step in which water or oil is added underground to reinforce the pressure. The step of adding material or energy other than the existing material is called the tertiary recovery step.

DOE and others in the US define the technology applied to this third recovery stage as EOR (Enhanced Oil Recovery) 'EOR', but in general, EOR (Enhanced Oil Recovery) is a method of mining crude oil because the pressure is lower than that of the first. When it decreases, it refers to a method to increase production by injecting water or gas.

The EOR technique is mainly considered a method of lowering the viscosity of crude oil by heat treatment, carbon dioxide injection, polymer injection, etc. It is known that the total production can be produced by about 33% more than natural production if EOR technology is applied.

On the other hand, when oil stored in the ground is mined, underground water is also ejected along with the oil. .

Production water basically ^{contains ions such as Na +} , Ca ²⁺ , and Mg ²⁺ , but if their concentration is too high or low, the ionic bond between the production water and residual oil is not sufficient, so the normal process is often impossible . In other words, there is a problem that the production water must be at an appropriate concentration in order to actively use it for the improvement of oil recovery.

US 7069990 B1 : Enhanced Oil Recovery Methods

Journal of the Korean Society of Resources and Engineers J. Korean Soc. Miner. Energy Resources. Eng. Vol. 55, No. 6 (2018) pp. 660-669, https://doi.org/10.32390/ksmer.2018.55.6.660 : Research trends and prospects for chemical methods for improving oil recovery

One aspect of the present invention is a smart water production system that produces smart water of an appropriate concentration by adding ^{Ca 2+} , Mg ²⁺ ions in order to recover the produced water ejected during oil extraction and use it in the petroleum recovery enhancement (EOR) process. is intended to provide

In addition, another aspect of the present invention aims to provide a smart water oil recovery improvement system using a smart water production system.

In another aspect of the present invention, in order to recover the produced water ejected during petroleum extraction and use it in the petroleum recovery enhancement (EOR) process, Ca ²⁺ , Mg ²⁺ ions are added to produce smart water of an appropriate concentration. The purpose is to provide a method.

A smart water system according to an embodiment of the present invention for solving the above problems is a separation unit for removing solid substances contained in the production water generated in the crude oil extraction process, and the ionicity contained in the production water passing through the separation unit A crystallization unit for removing substances, a storage unit for storing the produced water discharged from the crystallization unit, and a recovery unit for recovering an ion component from the crystallization sludge discharged from the crystallization unit, wherein the recovered ion component is stored in the storage unit or the production unit Smart water is manufactured by injecting water into the transfer line connected to the storage unit.

In addition, the recovery unit includes a dissociation unit for dissociating the ionic component by mixing the crystallization sludge and acidic water, and an extraction unit for extracting the ionic component dissociated from the dissociation unit.

In addition, the ionic component of the recovery unit may include Ca ²⁺ , Mg ²⁺ _{, and the acidic water may be prepared by collecting CO 2} generated in the crude oil extraction process and mixing it with water.

In addition, the separator may use at least one selected from the group consisting of a filter, a disk filter, a sand filter, an ultrafiltration device, an activated carbon filter, a biological water treatment device, an aeration device, and a membrane device.

In addition, the crystallization part is filled with a seed inside, and the crystallizer reacts with the water to be treated including contaminants or ions in a turbulent flow phase to crystallize on the surface of the seed, and the reactant that is not crystallized on the seed is produced as fine particles It is provided at the upper part of the reaction tank and the reaction tank, and is provided at the upper part of the separation tank and the separation tank where laminar and turbulent flows coexist so as to return some of the fine particles rising by buoyancy to the reaction tank, and some of the fine particles rising by buoyancy It may include a sedimentation tank for precipitating the fine particles by generating a laminar flow so as not to leak out.

In addition, the crystallization unit may include an internal conveying pipe for recirculating a portion of the fluid from the separation tank to the lower portion of the reaction tank.

In addition, the production water in which the fluid flow in the separation tank is greater than 2,100 to 4,000 or less, the value calculated by the following Equation 2 is changed to 2,100 or less, and the fluid flow is the value calculated by the following Equation 4, and the connection part supplied to the settling tank may further include

[Equation 2]

Re ₂₁ = D ₂ V ₂ ρ/μ

(Here, D ₂ is the diameter (m) _{of the separation tank, V 2} is the flow rate (m/sec) of the separation tank, ρ is

Density (kg/m ³ ), μ is viscosity (kg/ms))

[Equation 4]

Re ₄₂ = D ₄ V ₄ ρ/μ

(Here, D ₄ is the diameter (m) _{of the connection part, V 4} is the flow rate (m/sec) of the connection part, ρ is the density (kg/m ³ ), μ is the viscosity (kg/ms) to be.)

In addition, it may include an electrolysis unit for stabilizing and coagulating particulate matter in the product water discharged from the crystallization unit to additionally remove it, and a second separation unit for additionally removing fine particles from the product water discharged from the electrolysis unit. may include

In addition, it may further include an RO treatment unit for additionally removing ionic substances from the produced water discharged from the second separation unit.

Another aspect of the present invention is an oil recovery enhancement system using the smart water production system.

Another aspect of the present invention relates to a method for producing smart water,

Separation step of removing the solid material contained in the production water;

a crystallization step of removing the ionic material contained in the produced water that has undergone the separation step; and

and a recovery step of recovering ion components from the crystallization sludge generated in the crystallization step, and a smart water generation step of preparing smart water by injecting the recovered ionic components into the production water after the crystallization step.

In the smart water production system according to one aspect of the present invention, when the produced water ejected from the ground is used in the EOR process, the produced water used is reformed into smart water of an appropriate concentration and re-injected, thereby increasing the efficiency of the EOR process. have.

^{At this time, the Ca 2+} , Mg ²⁺ ion components used for concentration control are recovered from the crystallization sludge generated in the crystallization device and mixed with the production water, so there is no need to purchase a separate drug, install a storage place, or manage the drug. That is, the crystallization sludge generated in the crystallization device is produced by using NaOH, a pH adjuster, of ^{Ca 2+} , Mg ²⁺ ions present in the production water, and the crystallization sludge itself can be used as a ^{Ca 2+} , Mg ^{2+ ion source.} have. Therefore, by reusing the crystallized sludge and injecting it into smart water, economic efficiency and convenience can be improved.

In addition, ^{when dissociating Ca 2+} and Mg ²⁺ ions in the crystallization sludge, carbon dioxide generated in the oil field is injected and used, so that environmental problems that occur when carbon dioxide is directly released into the atmosphere can be prevented.

1 is a conceptual diagram for explaining the basic concept of the present invention.
2 is a block diagram of a smart water production system according to an embodiment of the present invention.
3 is a schematic diagram of a crystallization unit used in a smart water production system according to an embodiment of the present invention.
4 is a schematic diagram of a dissolved air flotation device used in a smart water production system according to an embodiment of the present invention.
5 is a conceptual diagram of a recovery unit used in a smart water production system according to an embodiment of the present invention.

As used herein, "smart water" refers to water adjusted to a specific component and a specific concentration in the production water for use in the EOR process. Also, "system" means a group of devices that are formed by combining several unit devices used in a process.

Hereinafter, one aspect of the present invention will be described with reference to the drawings. 1 is a schematic diagram for explaining the concept of the present invention.

The EOR process used in the present invention is a smart water EOR process in which the injected water is converted into smart water and injected in order to increase the production of crude oil.

The smart water EOR process uses smart water adjusted to appropriate concentrations of calcium and magnesium as the injection water for the EOR process, and the residual oil is additionally mined by injecting smart water. At this time, the residual oil is mixed with production water and discharged, and it is separated into production water and petroleum.

Next, this produced water is again converted into smart water with appropriate components and concentrations and used in the EOR process.

2 is a conceptual diagram of a smart water production system according to an embodiment of the present invention.

According to this, the smart water production system according to an aspect of the present invention includes a first separation unit 100, a crystallization unit 200, an electrolysis unit 300, a second separation unit 400, an RO processing unit 500, It is configured to include a storage unit 600 , and a recovery unit 700 .

The first separation unit 100 is a device for removing solid substances contained in the production water generated in the crude oil extraction process, and by maintaining the turbidity of the production water below a certain level, a physical treatment device for increasing the efficiency of the subsequent process. One, it functions as a pre-treatment facility to remove foreign substances contained in the produced water. Specifically, a filter device, a disk filter device, a sand filter device, an ultrafiltration device, an activated carbon filter device, a biological water treatment device using only pure microorganisms, an aeration device, and a membrane device or method may be used. In this case, a disk filter device capable of backwashing is preferable. .

The crystallization unit 200 is a device for removing salts contained in the produced water that has passed through the separation unit 100 . In order to reuse the produced water, salts must be maintained at an appropriate concentration. As a first step to maintain the salts at an appropriate concentration, all salts contained in the produced water are removed.

3 is a schematic diagram of a crystallization unit according to an embodiment of the present invention. An embodiment of the crystallization unit will be described in detail with reference to this. The crystallization unit 200 according to an embodiment of the present invention includes a reaction tank 210 , a separation tank 220 , a settling tank 230 , a production water inlet 240 , a drug inlet 250 , and an internal return pipe. 260 , and a discharge unit 270 .

The reaction tank 210 , the separation tank 220 , and the settling tank 230 are each cylindrical, and the diameter of the reaction tank 210 is smaller than the diameter of the separation tank 220 , and the diameter of the separation tank 220 is that of the settling tank 230 . It is preferable that the diameter smaller than the crystallization reaction efficiency and separation efficiency can be maximized in the present invention.

The reaction tank 210 is filled with a seed in the crystallization unit 200 according to an embodiment of the present invention, and the production water containing salt supplied through the production water inlet 240 and the chemical inlet 250 . Chemicals such as a crystallizing agent supplied through the reactor react in the turbulent flow phase to crystallize on the seed surface, and the reactants that are not crystallized on the seed correspond to the base reactor in which the crystallization reaction occurs as fine particles.

The seed of the reactor 210 gradually decreases in size from the bottom to the top.

The fine particles present on the seed of the reactor 210 are crystallized on the surface of the fine particles over time to grow as a seed.

That is, the first crystals formed by chemical reaction with elements at appropriate pH are fine particles of the order of several μm, and stay at the point where buoyancy and gravity are balanced by upflow. The fine particles continuously react with the injected element or surrounding fine particles, and as the particle size gradually increases, the buoyancy force becomes smaller than gravity and moves downward. If wastewater or liquid substances and chemicals containing contaminants to be treated are continuously injected, fine grain crystals are formed, and the growth and movement of these particles to the bottom continuously occurs within one device.

When the particle size continues to increase due to the reaction with liquid substances, production water, and injected chemicals in the lower part of the reaction tank of the crystallization device, the crystals that have moved to the bottom grow and grow while adsorbing the crystallized fine particles. A one-time injection of , the crystallization reaction occurs continuously without a separate seed injection.

When the seed reaches a certain size (or a certain period), the crystals generated through the lower part of the crystallizer are extracted and the amount and volume of the filling material in the reactor are kept constant.

For a stable and efficient crystallization operation in the aforementioned crystallization reaction, a device capable of stably maintaining the fine particles in the reactor, which is the base for the crystallization reaction, is required. The present invention can prevent excessive presence of fine particles in the separation tank, which is a section in which solid-liquid separation occurs in the fluid transferred from the reaction tank, and stably maintain the microparticles in the reaction tank.

Specifically, the fine particles _{settle or rise according to the sedimentation force (Fg = π/6D p} ³ (ρ _p -ρ _w )g) of the particle itself and the buoyancy force of the fluid moving from the bottom to the top (F=3πμDpv) do. Therefore, in order to prevent the outflow of fine particles, the sedimentation force must be greater than the buoyancy force. Among them, it is effective to weaken the buoyancy force because the weight increase of the particles cannot be achieved in a short time.

For this, the linear velocity (v) of the fluid needs to be reduced. When the cross-sectional area increases when the flow rate is the same, the linear velocity decreases (Q = A ₁ V ₁ = A ₂ V _{2 ,} where A ₁ <A ₂ V ₁ > V ₂ ), so the buoyancy force can be weakened, and the larger the difference in linear velocity (ie, V ₁ >> V ₂ ), the smaller particles can be separated.

As for the fluid flow in the reaction tank 210, it is preferable that the value calculated by the following Equation 1 is greater than 4,000 so that the fine particles generated by the crystallization reaction can be effectively maintained inside the device without external leakage and can grow into fine crystals.

[Equation 1]

Re ₁ = D ₁ V ₁ ρ/μ

(Where D ₁ is the diameter (m) _{of the reactor, V 1} is the flow rate (m/sec) of the reactor, ρ is the density (kg/m ³ ), and μ is the viscosity (kg/ms).)

^{As used herein, the terms density and viscosity refer to 998.23 kg/m 3} , which is the density of water at 20° C., and viscosity refers to 0.001016 kg/ms, unless otherwise specified.

Materials removed by the crystallization unit include, but are not limited to, fluorine, ammonia, Ca ²⁺ , Mg ²⁺ , F ⁻ and the like.

The separation tank 220 is provided on the upper part of the reaction tank 210 , and laminar and turbulent flows coexist to return some of the fine particles rising by buoyancy to the reaction tank 210 , and the transferred fine particles are transferred to the reaction tank 210 . ) to be used in the crystallization reaction again.

The fine particles settle or rise according to the sedimentation force due to the weight of the particle itself and the buoyancy force of the fluid moving from the bottom to the top.

In order to increase the sedimentation force, it is necessary to increase the particle weight (increase the density) or to weaken the buoyancy force.

In order to weaken the buoyancy force, the linear velocity (v) of the fluid must be reduced. If the cross-sectional area increases when the flow rate is the same, the linear velocity decreases, so the buoyancy can be weakened. The larger the difference in linear velocity, the smaller the particles can be separated do.

The separation tank 220 is preferably configured so that a turbulent flow region (or a transition region) and a laminar flow region coexist using this principle.

In the separation tank 220, the fluid flow from the portion connected to the reaction tank 210 to the portion connected to the settling tank 230, the laminar flow has a larger flow gradient than the turbulent flow or has an alternating layer flow to maximize the separation efficiency It is preferable to

That is, as for the fluid flow in the separation tank, it is preferable that the value calculated by the following Equation 2 is greater than 2,100 and less than or equal to 4,000, so that the fine particles generated by the crystallization reaction can be effectively maintained inside the device without external leakage and can be grown into fine crystals. .

[Equation 2]

Re ₂ = D ₂ V ₂ ρ/μ

(Where D ₂ is the diameter (m) _{of the separation tank, V 2} is the flow rate (m/sec) of the separation tank, ρ is the density (kg/m ³ ), and μ is the viscosity (kg/ms).)

Alternatively, as for the fluid flow in the connection portion between the separation tank and the settling tank, it is preferable that the value calculated by the following Equation 4 is 2,100 or less so that the microparticles generated by the crystallization reaction can be effectively maintained inside the device without external leakage and can grow into microcrystals. .

[Equation 4]

Re ₄ = D ₄ V ₄ ρ/μ

(Here, D ₄ is the diameter (m) _{of the connection site, V 4} is the flow rate (m/sec) of the connection site, ρ is the density (kg/m ³ ), and μ is the viscosity (kg/ms). )

The separation tank may be provided with an internal conveying pipe 260 for circulating some fluid discharged from the separation tank 220 to the chemical inlet 250 . In this case, it is more preferable that the internal conveyance pipe 260 is provided at the upper end of the separation tank 220 so as not to prevent the recirculation of the fine particles separated in the separation tank 220 to the reaction tank 210 .

The pipe connecting the separation tank 220 and the internal conveyance pipe 260 may have a drain valve, and in this case, there is an effect of facilitating the circulation of fine particles.

The settling tank 230 is provided above the separation tank 220, and generates a laminar flow so that some of the fine particles rising by buoyancy do not flow out to precipitate the fine particles.

As for the fluid flow in the sedimentation tank, it is preferable that the value calculated by the following Equation 3 is 2,100 or less so that the fine particles generated by the crystallization reaction can be effectively maintained inside the device without external leakage and can be grown into microcrystals.

[Equation 3]

Re ₃ = D ₃ V ₃ ρ/μ

(Here, D ₃ is the diameter (m) _{of the sedimentation tank, V 3} is the flow rate (m/sec) of the sedimentation tank, ρ is the density (kg/m ³ ), and μ is the viscosity (kg/ms).)

As described above, in order to stably maintain the fine particles in the reaction tank 210 of the present invention, the diameter of the reaction tank 210 is smaller than the diameter of the separation tank 220, and the diameter of the separation tank 220 is It is preferable that they are sequentially connected from the top while satisfying a relationship smaller than the diameter of the settling tank 230 . In the case of having such a structure and diameter, even if the fine particles float upstream by buoyancy, they are circulated through the reaction tank multiple times, which is advantageous for growing into microcrystals.

The diameter of the separation tank 220 may be 2 to 4 times larger than the diameter of the reaction tank 210 . In addition, the diameter of the settling tank 230 may be 4.5 times or more larger than the diameter of the reaction tank 210 , and at the same time, it may be larger than twice the diameter of the separation tank 220 .

Here, the upper diameter of the separation tank 220 may be the same as or smaller than the diameter of the settling tank 300 , and the diameter of the reaction tank 210 may be based on 5 to 20 cm as a specific example, but is variable.

In addition, the linear speed of the separation tank 220 may be, for example, 4.5 times or more and less than 20 times the linear speed of the settling tank, and the linear speed of the reaction tank 210 is 10-25, for example, based on the linear speed of the settling tank 230 . can be a boat

The upper linear speed of the separation tank 220 may be the same as or greater than the linear speed of the settling tank 230 , and the linear speed of the settling tank 230 may be, for example, 1 to 7 m/hr.

3 illustrates a structure in which the connection part 215 of the reaction tank 210 and the separation tank 210 and the connection part 225 of the separation tank 200 and the settling tank 300 have a linear tapered shape, but is limited thereto. no. The connecting portions 215 and 225 may have a curved tapered shape or a cross curved tapered shape. The connecting portions 215 and 225 are easy to change the fluid flow as described above. For example, the taper angle may be an angle of 45° to 90°.

The chemical inlet 250 injects a crystallizing agent, and is supplied to the lower side of the reaction tank 210 but is preferably injected together with sand, and the crystallizing agent is variable depending on the type of contaminants or ions contained in the produced water. , NH ₄ ⁺ , Ca ²⁺ , Mg ²⁺ , F ^{- When} including ions such as sodium compound (NaOH), calcium compound (eg CaCl ₂ ), magnesium compound (eg MgCl ₂ ) and phosphate Compounds (eg, AlPO ₄ ) It is preferable to use at least one selected from the group consisting of suitable pH control and crystallization. NaOH can be injected and flowed as a pH adjuster. Usually, when the pH is about 10, crystallization proceeds.

On the other hand, the treated water from which the ionic material has been removed from the settling tank of the crystallization unit is discharged through the production water discharge unit 270, and the seeds at the bottom are accumulated and discharged at regular intervals, which is referred to as crystallization sludge. Crystallization sludge contains ionic components.

2, the electrolysis unit 300 is a device for stabilizing particulate matter such as suspended particles, emulsion particles, insoluble particles, etc. by applying an electric current to the treated water to aggregate. The electric current applied to the arranged metal plate acts as an electric driving force that causes a chemical reaction, and the dissolved metal is hydrolyzed to form suspended, soluble and colloidal hydroxides. For example, the applied current ^{generates an iron (Fe 3+} ) component in the disposed iron plate, which acts as a coagulant for ferric sulfate and ferric chloride. At this time, the metal hydroxide produced has excellent agglomeration, adsorption and sedimentation properties because of its stronger activity and lower potential than the chemically prepared hydroxide, and it causes particulate matter such as suspended particles, emulsion particles, and insoluble particles in treated water to agglomerate and float.

The electrolysis device has a coagulation effect but also a decomposition effect, so it decomposes an emulsion type sample into water and oil. Oxygen generated from the anode can oxidize organic matter in the water, and bubbles from hydrogen and oxygen gas generated from the cathode and anode can be used for flotation. That is, by applying an electric current, the ions generated from the electrode cause a chemical reaction and precipitation, or the colloidal particles are aggregated and ionized to remove contaminants. Electric current is applied to the electrolysis device at all times during operation, and the residence time (RT) in the reaction tank is 1 to 5 minutes.

The electrocoagulation treatment method has excellent effects on various wastewater, dyeing factories, ink factories, slaughterhouses, leather factories, textile factories, paper factories, etc., especially color treatment, treatment of various harmful heavy metals, and removal of fat, oil and grease. It is very effective in destroying and treating viruses and cystis (blue-green algae), and can treat iron, magnesium, calcium, nitrate, etc. contained in groundwater.

Residual particles are additionally removed in the second separation unit 400 . Since the particles contained in the produced water that have passed through the first separation unit 100, the crystallization unit 200, and the electrolysis unit 300 are small in size, it is preferable to use a dissolved air flotation device.

Dissolved Air Flotation (DAF) is a device that blows fine air bubbles into the production water to float and separate suspended matter, oil, insoluble matter, etc. In the smart water production system, it plays a role of additionally flotation and separation of particulate matter and oil components that are primarily agglomerated and separated in the electrolysis device.

4 is a schematic diagram of a dissolved air flotation device according to an embodiment of the present invention. When the produced water that has passed through the electrolysis unit is introduced through the inlet pipe 410 , the micro-air injection device 420 is operated to float the micro-air along the guide plate 430 , and the dissolved air floatation device is operated. The sludge of oil components and particulate matter floated and separated in the treatment water tank 440 is stored in the sludge collection tank 4450 over the baffle 441 at the top of the treatment water tank 440, and then discharged through the sludge discharge pipe 460, The treated water introduced into the water collecting tank 480 through the lower connection pipe 470 of the floating device is discharged from the device through the discharge pipe 490 .

The RO treatment unit 500 additionally removes the ionic material of the produced water in a reverse osmosis method. The RO treatment unit is a device using reverse osmosis, and uses pressure energy to separate fresh water by pressurizing a reverse osmosis membrane that allows water to pass through but hardly transmits solutes (ionic substances). Sexual substances (Cl ^- ,Na ⁺ ,SO4 ^2- ,Mg ²⁺ , Ca ²⁺ ,K ⁺ etc.) are almost excluded. At this time, the membrane uses a special membrane (membrane) that almost excludes ionic substances dissolved in water and allows only pure water to pass through.

The electrolysis unit, the second separation unit, and the membrane treatment unit described above may be selectively included, and the product water passing through the crystallization unit and the electrolysis unit, the second separation unit, and the membrane treatment unit optionally included is stored in the storage unit 300 . is saved

The storage unit 300 is finally stored in the production water passing through the RO processing unit 500, and is provided with a transfer pipe for delivering the production water to the storage unit.

5 shows a recovery unit according to an embodiment of the present invention. Referring to this, the recovery unit 700 recovers the ion component from the crystallization sludge generated in the crystallization unit and sends it to the storage unit or a transfer pipe that sends the above-mentioned production water to the storage unit, and the dissociation unit 710 and the extraction unit 720 ) is included.

The dissociation unit 710 reacts the crystallization sludge discharged from the crystallization unit with acidic water, and the extraction unit 720 extracts the dissociated ionic component contained in the crystallization sludge in the dissociation unit 710 . The dissociation unit 710 dissociates ionic components, for example, Ca ²⁺ , Mg ²⁺ ions, and these ionic components are injected at an appropriate concentration into the storage unit or the transfer line where the product water is recovered to the storage unit to make the produced water smart. reformed with water

That is, the produced water is in a state close to zero as the ionic material is removed while passing through the crystallization unit, the RO treatment unit, and the like, which is an advantageous state for controlling the concentration. At this time, smart water is manufactured by extracting ionic components from the crystallization sludge containing ionic substances discharged from the crystallization unit and injecting it into the production unit at an appropriate concentration. Smart water produced at this time varies slightly by region and season, but TDS is 1,500 mg/L to 2,100 mg/L, and the concentration of salt is 20 mg/L to 40 mg/L ^{for Ca 2+ , and 40 mg/L for Mg 2+} It is preferable that it is L - 60 mg/L.

On the other hand, the acidic water used in the dissociation unit is preferably prepared by mixing _{CO 2 and water generated in the crude oil extraction process.} In general, water, oil, and gas are generated in oil fields. Of these, the main components of gas are methane and carbon dioxide. The separated methane is used as a main material for gas power generation or fuel, but carbon dioxide is directly emitted into the atmosphere because it is a substance that causes global warming. cause environmental problems.

However, it is used to dissociate ^{Ca 2+} , Mg ²⁺ ions in the crystallization sludge by dissolving difficult-to-treat carbon dioxide in water to make acidic water with a pH of about 5. In this case, it is significant in that it reduces the emission of carbon dioxide that causes air pollution.

On the other hand, in the smart water production system of the present invention, not only the step of injecting a chemical into the treated water, but also sensors for measuring TDI, ion concentration, etc. are provided in the input/exit piping of each device constituting the system. Based on the measured values, the control unit controls whether each processing unit passes or not and a valve control unit for flow adjustment.

Assuming that emergency measures are required during operation, the control unit may be composed of a control unit for controlling each device and a control unit monitoring it, or select any one of a control unit for each device and a control unit for integrated control configurable.

Another aspect of the present invention is a smart water oil recovery promotion system using smart water manufactured in the smart water production system described above.

The smart water oil recovery promotion system uses smart water having a salt concentration suitable for oil recovery promotion. It is a system that realizes the maximum residual oil recovery rate by arbitrarily adding ^{Ca 2+} , Mg ^{2+ ions to the re-injected production water.}

Another aspect of the present invention is the smart water production method described above. The smart water production method includes a separation step, a crystallization step, and a recovery step.

The separation step is a pretreatment step for removing the solid substances contained in the production water, and filtering, sand filtration, ultrafiltration, activated carbon filtration, biological water treatment, aeration, and membrane methods may be used.

The crystallization step is a step of removing the ionic material contained in the produced water that has undergone the separation step, and the ionic material is removed to control the concentration to change the produced water to smart water. In the crystallization step, the produced water is separated into production water from which ionic substances have been removed and ionic sludge containing ionic substances, and proceeds to the next step.

The product water discharged from the crystallization step selectively passes through the electrolysis step through the above-described electrolysis section, the second separation step through the second separation section, and the RO treatment step through the RO treatment section to further remove particulate matter or ionic materials. can

Meanwhile, the crystallization sludge discharged from the crystallization step is transferred to the recovery step. In the recovery step, crystallization sludge is a step in which ionic components are extracted. In the recovery step, crystallization sludge and acidic water are mixed to dissociate the ionic components and then extracted. At this time, the acidic water in the recovery step _{is preferably prepared by collecting CO 2} generated in the crude oil extraction process and mixing it with water.

The smart water generation step is a step of mixing the production water after the crystallization step and the ionic component obtained in the recovery step and mixing it again with smart water of an appropriate concentration to promote oil recovery to generate smart water.

In the above, an example of the system of the present invention has been shown and described, but the present invention is not limited to the specific example described above, and it is common in the technical field to which the present invention belongs without departing from the gist of the present invention as claimed in the claims. Various modifications may be made by those having the knowledge of, of course, and these modifications should not be individually understood from the technical spirit or perspective of the present invention.

100: first separation unit
200: crystallization unit
210: reaction tank
215: first connection part
220: separation tank
225: second connection part
230: sedimentation tank
260: inner return pipe
300: electrolysis unit
400: second separation unit
410: inlet pipe
420: micro air injection device
430: guide plate
440: treatment tank
441: baffle
450: sludge collecting tank
460: sludge discharge pipe
470: connector
480: catchment tank
490: discharge pipe
500: RO processing unit
600: storage
700: recovery unit
710: dissociation
720: extraction unit

Claims (14)

Separation unit for removing the solid material contained in the production water generated in the crude oil extraction process;
a crystallization unit for removing the ionic material contained in the produced water that has passed through the separation unit;
^{an electrolysis unit generating iron (Fe 3+} ) components in the produced water discharged from the crystallization unit to stabilize and aggregate particulate matter;
a storage unit for storing the produced water discharged from the electrolysis unit; and
A dissociation unit that recovers ionic components from the crystallization sludge discharged from the crystallization unit, _{collects CO 2} generated in the crude oil extraction process, and mixes acidic water prepared by mixing with water with the crystallization sludge to dissociate the ionic components and a recovery unit including an extraction unit for extracting the ionic component dissociated from the dissociation unit;
A smart water production system for producing smart water by injecting the recovered ion component into the storage unit or a transfer line connected to the storage unit with the production water.
The method of claim 1,
The ionic component is Ca ²⁺ , Mg ²⁺ Smart water production system including.
3. The method of claim 2,
The crystallization part is filled with a seed inside, and the crystallizing agent reacts with the water to be treated including contaminants or ions in a turbulent flow to crystallize on the surface of the seed, and the reactant that is not crystallized on the seed is a reaction tank in which fine particles are generated ;
a separation tank provided above the reaction tank, in which laminar and turbulent flows coexist to return some of the fine particles rising by buoyancy to the reaction tank; and
A smart water production system comprising a; a sedimentation tank provided at the upper part of the separation tank and generating a laminar flow to precipitate the microparticles so that some of the microparticles rising by buoyancy do not flow out.
4. The method of claim 3,
The crystallization unit smart water production system including an internal conveying pipe for recirculating a portion of the fluid from the separation tank to the lower part of the reaction tank.
5. The method of claim 4,
The crystallization unit is a smart water production system that uses at least one selected from a sodium compound (NaOH), a calcium compound, a magnesium compound, and a phosphate phosphorus compound as a crystallizing agent according to the type of contaminants contained in the produced water.
5. The method of claim 4,
The separation unit is a smart water production system using at least one selected from the group consisting of a filter, a disc filter, a sand filter, an ultrafiltration device, an activated carbon filter, a biological water treatment device, an aeration device, and a membrane device .
7. The method of claim 6,
In the separation tank, the value calculated by Equation 2 below is greater than 2,100 and the value calculated by Equation 4 is less than or equal to 2,100 for the production water in which the fluid flow is calculated by Equation 4 below. Smart water production system including.
[Equation 2]
Re ₂₁ = D ₂ V ₂ ρ/μ
(Here, D ₂ is the diameter (m) _{of the separation tank, V 2} is the flow rate (m/sec) of the separation tank, ρ is
Density (kg/m ³ ), μ is viscosity (kg/ms))
[Equation 4]
Re ₄₂ = D ₄ V ₄ ρ/μ
(Here, D ₄ is the diameter (m) _{of the connection part, V 4} is the flow rate (m/sec) of the connection part, ρ is the density (kg/m ³ ), μ is the viscosity (kg/ms) to be.)
8. The method of claim 7,
The electrolysis unit applies a current to the produced water discharged from the crystallization unit, and a smart water production system for generating ^{the iron (Fe 3+ ) component from the disposed iron plate.}
9. The method of claim 8,
Smart water production system further comprising a second separator for additionally removing particulates from the produced water discharged from the electrolysis unit.
10. The method of claim 9,
The second separation unit is a micro-air injection device;
a sludge collection tank for collecting oil components and sludge floated by the micro-air injection device; and
A smart water production system comprising a; a water collecting tank for temporarily storing the treated water discharged through the lower end of the sludge collecting tank.
11. The method of claim 10,
Smart water production system further comprising an RO processing unit for additionally removing ionic substances from the produced water discharged from the second separation unit.
12. The method of claim 11,
The smart water has a TDS of 1,500 mg/L to 2,100 mg/L, and a salt concentration of 20 mg/L to 40 mg/L ^{of Ca 2+ , and a smart water production system that has Mg 2+} of 40 mg/L to 60 mg/L.
A smart water oil recovery promotion system comprising the smart water production system of any one of claims 1 to 12.
Separation step of removing the solid material contained in the production water;
a crystallization step of removing the ionic material contained in the produced water that has undergone the separation step;
an electrolysis step of removing particulate matter by generating an ^{iron (Fe 3+} ) component in the produced water discharged in the crystallization step; and
A recovery step of dissociating, extracting, and recovering the ionic components by mixing the crystallized sludge generated in the crystallization step and the CO _{2 generated in the crude oil extraction process, mixing it with water and acidic water prepared by mixing,}
A smart water production method comprising a; a smart water generation step of manufacturing smart water by injecting the recovered ionic component into the production water after the crystallization step.

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