CN101835954B - Process for removing silica in heavy oil recovery - Google Patents
Process for removing silica in heavy oil recovery Download PDFInfo
- Publication number
- CN101835954B CN101835954B CN200880113363.9A CN200880113363A CN101835954B CN 101835954 B CN101835954 B CN 101835954B CN 200880113363 A CN200880113363 A CN 200880113363A CN 101835954 B CN101835954 B CN 101835954B
- Authority
- CN
- China
- Prior art keywords
- salt solution
- evaporimeter
- concentrated salt
- directed
- oil
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 title claims abstract description 142
- 239000000377 silicon dioxide Substances 0.000 title claims abstract description 69
- 238000000034 method Methods 0.000 title claims abstract description 62
- 230000008569 process Effects 0.000 title abstract description 28
- 238000011084 recovery Methods 0.000 title abstract description 13
- 239000000295 fuel oil Substances 0.000 title description 22
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 151
- 239000000203 mixture Substances 0.000 claims abstract description 30
- 239000012267 brine Substances 0.000 claims abstract description 21
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims abstract description 21
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 10
- 239000003153 chemical reaction reagent Substances 0.000 claims abstract description 7
- 239000003129 oil well Substances 0.000 claims abstract description 7
- 238000002156 mixing Methods 0.000 claims abstract 6
- 239000012266 salt solution Substances 0.000 claims description 81
- 238000005516 engineering process Methods 0.000 claims description 56
- CPLXHLVBOLITMK-UHFFFAOYSA-N Magnesium oxide Chemical compound [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 claims description 46
- 239000007787 solid Substances 0.000 claims description 45
- TWRXJAOTZQYOKJ-UHFFFAOYSA-L Magnesium chloride Chemical compound [Mg+2].[Cl-].[Cl-] TWRXJAOTZQYOKJ-UHFFFAOYSA-L 0.000 claims description 32
- 238000004821 distillation Methods 0.000 claims description 26
- 239000012528 membrane Substances 0.000 claims description 26
- 239000000919 ceramic Substances 0.000 claims description 25
- 239000000395 magnesium oxide Substances 0.000 claims description 23
- 239000012141 concentrate Substances 0.000 claims description 20
- VTHJTEIRLNZDEV-UHFFFAOYSA-L magnesium dihydroxide Chemical compound [OH-].[OH-].[Mg+2] VTHJTEIRLNZDEV-UHFFFAOYSA-L 0.000 claims description 18
- 239000000347 magnesium hydroxide Substances 0.000 claims description 18
- 229910001862 magnesium hydroxide Inorganic materials 0.000 claims description 18
- 229910001629 magnesium chloride Inorganic materials 0.000 claims description 16
- 239000011777 magnesium Substances 0.000 claims description 12
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 claims description 10
- 238000000975 co-precipitation Methods 0.000 claims description 10
- 229910052749 magnesium Inorganic materials 0.000 claims description 10
- 238000009833 condensation Methods 0.000 claims description 8
- 230000005494 condensation Effects 0.000 claims description 8
- 238000011144 upstream manufacturing Methods 0.000 claims description 8
- 238000004064 recycling Methods 0.000 claims description 6
- 239000012466 permeate Substances 0.000 claims description 5
- 239000000047 product Substances 0.000 claims description 4
- 230000001376 precipitating effect Effects 0.000 claims description 3
- 239000000725 suspension Substances 0.000 claims description 3
- 239000002244 precipitate Substances 0.000 claims description 2
- 238000002347 injection Methods 0.000 abstract description 2
- 239000007924 injection Substances 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 46
- 235000019198 oils Nutrition 0.000 description 41
- 238000010521 absorption reaction Methods 0.000 description 29
- 238000002425 crystallisation Methods 0.000 description 24
- 230000008025 crystallization Effects 0.000 description 24
- 238000001704 evaporation Methods 0.000 description 23
- 239000013078 crystal Substances 0.000 description 21
- 230000008020 evaporation Effects 0.000 description 20
- 239000002002 slurry Substances 0.000 description 20
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 18
- 239000010408 film Substances 0.000 description 15
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 14
- 150000001875 compounds Chemical class 0.000 description 14
- 239000000463 material Substances 0.000 description 12
- 238000010438 heat treatment Methods 0.000 description 10
- 230000004888 barrier function Effects 0.000 description 8
- 239000000126 substance Substances 0.000 description 8
- 229910000019 calcium carbonate Inorganic materials 0.000 description 7
- 238000005755 formation reaction Methods 0.000 description 7
- 238000004513 sizing Methods 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- 230000008859 change Effects 0.000 description 6
- 238000002474 experimental method Methods 0.000 description 6
- 235000019476 oil-water mixture Nutrition 0.000 description 6
- 239000000356 contaminant Substances 0.000 description 5
- 238000012360 testing method Methods 0.000 description 5
- 239000002699 waste material Substances 0.000 description 5
- OYPRJOBELJOOCE-UHFFFAOYSA-N Calcium Chemical compound [Ca] OYPRJOBELJOOCE-UHFFFAOYSA-N 0.000 description 4
- UQSXHKLRYXJYBZ-UHFFFAOYSA-N Iron oxide Chemical compound [Fe]=O UQSXHKLRYXJYBZ-UHFFFAOYSA-N 0.000 description 4
- 229910004298 SiO 2 Inorganic materials 0.000 description 4
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 4
- 239000003513 alkali Substances 0.000 description 4
- 239000011575 calcium Substances 0.000 description 4
- 229910052791 calcium Inorganic materials 0.000 description 4
- BRPQOXSCLDDYGP-UHFFFAOYSA-N calcium oxide Chemical compound [O-2].[Ca+2] BRPQOXSCLDDYGP-UHFFFAOYSA-N 0.000 description 4
- 239000000292 calcium oxide Substances 0.000 description 4
- ODINCKMPIJJUCX-UHFFFAOYSA-N calcium oxide Inorganic materials [Ca]=O ODINCKMPIJJUCX-UHFFFAOYSA-N 0.000 description 4
- 239000003518 caustics Substances 0.000 description 4
- 238000007872 degassing Methods 0.000 description 4
- 239000002270 dispersing agent Substances 0.000 description 4
- 239000011552 falling film Substances 0.000 description 4
- 238000001556 precipitation Methods 0.000 description 4
- 238000001179 sorption measurement Methods 0.000 description 4
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 description 3
- 239000000920 calcium hydroxide Substances 0.000 description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 description 3
- 239000002131 composite material Substances 0.000 description 3
- 229910000765 intermetallic Inorganic materials 0.000 description 3
- -1 metal-oxide compound Chemical class 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 239000013049 sediment Substances 0.000 description 3
- 238000002834 transmittance Methods 0.000 description 3
- 101100352919 Caenorhabditis elegans ppm-2 gene Proteins 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 229940037003 alum Drugs 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 230000006835 compression Effects 0.000 description 2
- 238000007906 compression Methods 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 239000003651 drinking water Substances 0.000 description 2
- 235000020188 drinking water Nutrition 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229910044991 metal oxide Inorganic materials 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000000741 silica gel Substances 0.000 description 2
- 229910002027 silica gel Inorganic materials 0.000 description 2
- 235000017550 sodium carbonate Nutrition 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- RBORURQQJIQWBS-QVRNUERCSA-N (4ar,6r,7r,7as)-6-(6-amino-8-bromopurin-9-yl)-2-hydroxy-2-sulfanylidene-4a,6,7,7a-tetrahydro-4h-furo[3,2-d][1,3,2]dioxaphosphinin-7-ol Chemical compound C([C@H]1O2)OP(O)(=S)O[C@H]1[C@@H](O)[C@@H]2N1C(N=CN=C2N)=C2N=C1Br RBORURQQJIQWBS-QVRNUERCSA-N 0.000 description 1
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 description 1
- ZOXJGFHDIHLPTG-UHFFFAOYSA-N Boron Chemical compound [B] ZOXJGFHDIHLPTG-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- BIVQBWSIGJFXLF-UHFFFAOYSA-N PPM-18 Chemical compound C=1C(=O)C2=CC=CC=C2C(=O)C=1NC(=O)C1=CC=CC=C1 BIVQBWSIGJFXLF-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Natural products OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 1
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical class [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 229910052796 boron Inorganic materials 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005553 drilling Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000008398 formation water Substances 0.000 description 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 1
- 239000010931 gold Substances 0.000 description 1
- 229910052737 gold Inorganic materials 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 229910001410 inorganic ion Inorganic materials 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 210000000056 organ Anatomy 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 239000011591 potassium Substances 0.000 description 1
- 229910052700 potassium Inorganic materials 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000004088 simulation Methods 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
Images
Classifications
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH DRILLING; MINING
- E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/16—Enhanced recovery methods for obtaining hydrocarbons
- E21B43/24—Enhanced recovery methods for obtaining hydrocarbons using heat, e.g. steam injection
-
- E—FIXED CONSTRUCTIONS
- E21—EARTH DRILLING; MINING
- E21B—EARTH DRILLING, e.g. DEEP DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
- E21B43/34—Arrangements for separating materials produced by the well
Abstract
A process for recovery oil includes recovering an oil/water mixture from an oil well. Thereafter, the method includes separating oil from the oil/water mixture to produce an oil product and produced water having dissolved silica therein. The produced water is directed to an evaporator and produces steam and a concentrated brine. The method or process entails mixing a precipitant or crystallizing reagent with the produced water or the concentrated brine and causing the silica to precipitate from the produced water or the concentrated brine. Steam produced by the evaporator is condensed to form a distillate which is directed to steam generator. At the steam generator the distillate is heated to produce steam which is injected into an injection well, giving rise to the formation of the oil/water mixture.
Description
The cross reference of related application
According to 35U.S.C. § 119 (e), the claimed following U.S. Provisional Application No. of the application: the provisional application No.60/968 that submits on August 27th, 2007,180.This application is attached to herein by quoting in full.
Technical field
The present invention relates to be used to reclaim the technology of heavy oil, more specifically, the present invention relates to oil and reclaim technology, this technology utilization mechanical vapour Compression Evaporation system handles output water.
Background technology
Conventional oil reclaims and relates to drilling well and extract mixture oily and water from this well.With oil and moisture from, and usually water is injected in the subsurface formations.Conventional recovery is very effective for light viscosity oil.But it is not very effective for viscosity higher or heavy oil that conventional oil reclaims technology.
Improving oil recovery process using by the use of thermal means improves from underground reservoir recovery heavy oil.Water vapour is injected into contains the raising oil recovery method that heavy-oil formation is a broad practice.Usually, need several tons of water vapours to reclaim oil per ton.Oil in the water vapour heating reservoir, this has reduced oil viscosity and has allowed oil to flow to the collection well.Water vapour condensation and mix with oil, the water vapour of condensation is known as output water.Flow to the oil of collection well and the mixture of output water and be drawn into the surface.Utilize the common process that adopts in the conventional oily reclaimer operation with oil and output moisture from.
For economy and environment reason, need recycling to inject and improve the used output water of oil recovery at water vapour.This finishes by following operation: handle output water; Produce feedwater; And, the feedwater of handling is directed to steam generator or boiler, steam generator or boiler produce water vapour.Complete water circulation may further comprise the steps:
Water vapour is injected into oil bearing bed;
Condensed steam is to add deep fat, so the water vapour of condensation mixes with oil to form oil water mixture;
In well, collect oil water mixture;
Oil water mixture is drawn into the surface;
Oil is separated to obtain output water from oil water mixture;
Handling output water makes it become the feedwater of steam generator or boiler; And
Convert feedwater to water vapour, this water vapour has the quality that is fit to be injected in the oil bearing bed.
Handling output water is challenging with the feedwater that preparation is used for the water vapour generation.Be known that output water is carried out chemical treatment and make output water stand evaporation technology being used for water vapour and feeding water to form distillation.Especially, be known that use evaporimeter and mechanical vapour compressor produce distillation.But output water contains the compound of a large amount of silica-based usually.By silica fouling or deposition on treatment surface, the compound of these silica-based will be easy to stop up evaporimeter and other treatment surface.These foulings have reduced the conductibility of heat transfer element in the equipment, thereby have reduced evaporation and steam generation efficient.In order to prevent or to block the evaporimeter heating surface and stop up, routinely, be enhanced to keep silica solubility to the pH of the feed of evaporimeter because of the silica-based fouling.
But current technology exists defective and shortcoming.Add caustic alkali and represent significant running cost to improve pH.Usually do not wish to contain in the waste streams caustic alkali of high concentration.In addition, though mechanical vapour Compression Evaporation device reclaims about 95% water from output water, be difficult to handle residue and concentrate stream.Residue concentrates the pH of stream usually above 12.This stream that neutralizes causes solid precipitation, and is difficult to separate these solids from the aqueous solution.Sometimes discharge gas with technology in also known, such as hydrogen sulfide.These systems tend to operate comparatively expensive and safeguard that cost is higher.In addition, output water usually comprises a large amount of calcium and the magnesium that hardness is provided.Higher pH can promote the precipitation of hardness component (calcium and magnesium).If do not controlled, this can cause the possibility of the hardness fouling of evaporimeter heating surface.Can reduce the fouling risk that hardness causes by the chemicals that adds the dispersing agent form.The dispersing agent suspended particles make that they are also non-caked and stop up evaporator surface.How much as if not at this moment, determine to use dispersing agent can control hardness, because existing heavy oil reclaimer operation system seldom has the very low output water hardness.But, estimate that output water will comprise that higher brackish water composition and the hardness concentration in the output water are with higher in the heavy oil recovery technology in future.Utilize the higher pH technology of dispersing agent may be not too effective for output water with higher hardness concentration.
In addition, utilizing the heavy oil of evaporimeter to reclaim technology produces to concentrate salt solution and suitably dispose these concentrated salt solution and has problem sometimes.Especially true for high pH salt solution.High pH salt solution need reduce silica levels to allow disposal and to guarantee that the silica precipitating reagent will can not stop up disposal well.This treatment process relates to a large amount of acid, because existing must the neutralization in order to increase all caustic alkali that pH adds.Along with pH reduces, form silica gel, must remove this silica gel from salt solution.Operating experience for this saline treatment technology is limited, but it was reported the obstruction that equipment and pipeline usually can occur.If high pH salt solution is injected deep-well, this treatment process is than difficult, and cost is higher and unreliable.Exist alternative that deep-well injects and its to be the disposal of salt cave.But this selects to inject more expensive than deep-well significantly.
Therefore reclaiming at heavy oil needs to have more cost-benefit vapo(u)rization system and handles output water and produce pure relatively feedwater flow and be used for the water vapour generation systems in the technology.
Summary of the invention
The present invention relates to be used to clean and purify the technology that reclaims the output water that heavy oil generated from oil bearing bed.This technology comprises evaporation output water and forms the absorption slurry to prevent the silica fouling of evaporator surface.Can be by adding compound (it reacts to form the absorption suspended solid) to output water or this output water absorption suspended solid being formed this absorption slurry.Thereby suspended solid forms crystal slurry and the silica preferential adsorption device fouling that avoids evaporating to the crystal.The evaporimeter distillation forms and is suitable for purifying waste water of water vapour generation, and its generation is used to be injected into the water vapour of oil bearing bed.
In a kind of special process, from oil well recovered oil/aqueous mixtures.Afterwards, to produce oil product and output water, the output glassware for drinking water has contaminants from oil/aqueous mixtures separating oil, such as silica, hardness or the residual oil of dissolving.Mix with output water such as the such metallic compound of magnesia or magnesium chloride or any or alum in the multiple metal-oxide compound.When magnesia or magnesium chloride mix with output water, form magnesium hydroxide.In this example, this method comprises and makes magnesium hydroxide and silica co-precipitation.Afterwards, the output water that will have precipitated silica is directed to evaporimeter, and evaporimeter produces water vapour and concentrated salt solution.This method or technology also comprise condensed steam forming distillation and distillation is directed to steam generator, and add distillation among the hot water steam generator to produce water vapour.Afterwards, water vapour is injected into the injection well, causes the formation of oil/aqueous mixtures.
In another special process, from oil well recovered oil/aqueous mixtures.Afterwards, to produce oil product and output water, the output glassware for drinking water has contaminants from oil/aqueous mixtures separating oil, such as silica, hardness or the residual oil of dissolving.Mix with output water such as the oxide of Ti, Al or Si or the compound of composite oxides.These surface naturies of these compounds make and remove most of silica from solution.Afterwards, the output water that only has a small amount of solvable silica is directed to evaporimeter, and evaporimeter produces steam and concentrated salt solution.This method or technology comprise that also condensed steam is directed to steam generator with the formation distillation and with distillation, and the distillation in the heating steam generator is to produce water vapour.Afterwards, steam is injected into and injects into well, and causes the formation of oil/aqueous mixtures.
By research following description and accompanying drawing, other purpose of the present invention and advantage will become apparent, and accompanying drawing just illustrates the present invention.
Description of drawings
Fig. 1 is schematically illustrating according to the basic technology of heavy oil recovery technology of the present invention.
Fig. 2 utilized crystallization reactor to remove the illustrative that reclaims technology such as the heavy oil of the such contaminants of silica from the output current before the output current arrive one or more evaporimeters.
Fig. 3 is the explanation and the schematic diagram of the similar technology of technology shown in Figure 2, but wherein only a film be associated with evaporimeter.
Fig. 4 comprises that the heavy oil of crystallization processes reclaims the illustrative of technology, and this crystallization processes is used to handle the part around the concentrated salt solution of evaporimeter circulation.
Fig. 5 reclaims the illustrative that the similar heavy oil of technology reclaims technology with heavy oil shown in Figure 4, but wherein provides film in the downstream in crystallization reactor or zone, such as ceramic membrane.
The specific embodiment
The present invention needs a kind of heavy oil to reclaim technology, wherein, uses the absorption slurry to purify output water by evaporation technology.The distillation formation feedwater that comes from evaporation technology is used to generate water vapour and contains in the heavy oil subsurface formations to be injected into.Absorption slurry avoids evaporating the device heating surface because silica compounds in the output water and silica and durometer compound and fouling in certain embodiments, thereby keeps evaporator effectiveness.
Heavy oil is recycled the heat that discharges from condensed steam and is discharged oil from the oil-containing deposit.Collect resulting oil water mixture and it is drawn into the surface, wherein oil separates with this mixture, stays so-called output water.Reusing output water generates water vapour and presents and get back to oil bearing bed.The present invention also points to use absorption slurry and the method for output water with formation water vapour generation feedwater handled in evaporation, thereby recycling is reclaimed the most of water that uses in the technology at heavy oil.
Output water comprises the inorganic ions of dissolving, the organic compound of dissolving, the inorganic and organic solid of suspension, and dissolved gases.Total suspended solid in output water can change.Suspended solid in the common output water is less than about 100ppm, and in some cases, the suspended solid in the output water is in the scope of about 100ppm to about 150ppm.Except suspended solid, the output water that reclaims technology from heavy oil comprises the organic and inoganic solids of dissolving in varing proportions.The solid that dissolves in output water (comprise hardness and the compound of silica-based) especially has may by what make that the heating surface fouling stops up evaporation equipment.Therefore, wishing to carry out extra process removes silica-based from output water before evaporation compound after the water-oil separating.Use term " silica " to refer to the compound of silica-based substantially hereinafter.
Can use any evaporation device in the multiple evaporimeter to realize evaporation technology, include, but is not limited to mechanical vapour recompression evaporimeter, multi-effect evaporator and falling film evaporator.In addition, that the heating surface of evaporimeter can be template or cast and can be level or vertical, and on these surperficial either sides, evaporate.
Usually adopt various pretreating process to guarantee the efficient and the usefulness of evaporation technology.Especially, owing in output water, exist a large amount of silicas (to be generally 175ppm to 300ppm, as SiO
2), the present invention includes the absorption slurry to prevent silica fouling in equipment.
Now go to according to general technology of the present invention, this technology is schematically described in Fig. 1.Output water is directed to preheating step from the water-oil separating step, is the degassing afterwards, and adsorption compound adds, and evaporation and water vapour take place.The preheating and the degassing are not necessarily but optionally.Water vapour from the water vapour generation step is directed to oil bearing bed, and water vapour condensation here discharges heat to emit oil from the stratum.Collect resulting oil water mixture then and it is drawn into the water-oil separating step, finish the water circulation that heavy oil reclaims technology.
Each all can be finished by method known to those skilled in the art to should be appreciated that water-oil separating, preheating, the degassing and steam generation.For example, can use Gravity Separation to realize water-oil separating.Preheating output water has improved the CO that dissolves in the subsequent degassifying
2Remove efficient.Preheating (if use) can be reclaimed hot finishing from one or more waste streams or from distillating stream by using heat interchanger.Sometimes before evaporation, remove the CO of dissolving
2Be used to avoid CO
2In evaporator shell, assemble.This CO
2Gathering can be covered the part of evaporimeter heat exchange area and influence evaporability unfriendly.The degassing can be used for removing oxygen to reduce the corrosion in the evaporimeter.Can realize that water vapour takes place by using boiler or various forms of steam generator.
Now go to absorption slurry and evaporation technology, the present invention prevents or reduces evaporimeter heating surface hardness and silica-based fouling.Prevent fouling by adding chemicals, chemicals comprises that trickle suspended solid is to form the absorption slurry in the salt solution of circulation again of evaporation technology.Suspended solid forms crystal, and crystal provides the preferential adsorption site of silica.Silica is adsorbed onto absorption slurry and therefore is pulled out on the crystal rather than is deposited on the heating surface of evaporimeter from solution.Therefore reduce or the device surface scale that avoids evaporating, thus the efficient of reservation evaporation technology.
Generally speaking, evaporation step converts at least 90% output water to output steam, and its condensation is to form distillation.Distillation is formed for the feedwater of water vapour generation equipment.The part of Qi Hua output water is not known as concentrate or salt solution.The absorption slurry forms the part of concentrate or salt solution.Concentrate or salt solution is circulation again in evaporimeter.All solids basically in evaporator feedwater is stayed in the concentrate.From the discharge material or the evaporimeter discharge stream of flow cycle are discarded the part of circulate again concentrate or salt solution to keep selected brine strength again.Evaporimeter discharge stream can convert solid to or place and inject well in zero liquid-discharging system (ZLD).
Now go to the more detailed consideration of absorption pulp material and absorption slurry development, should be appreciated that and before output water enters evaporimeter or enters the brine loop of circulation again in the evaporimeter, to add compound to output water.The material that adds evaporimeter to can be oxide, such as magnesia, calcium oxide, calcium hydroxide or other metal oxide, such as alumina or iron oxide.In addition, the material through adding to form the absorption slurry can be metallic compound, such as magnesium chloride.In addition, the material through adding to form the absorption slurry can be alum.In addition, this material can be such as the oxide of Ti, Al or Si or the compound of composite oxides, and they have specific surface property.Add this material and obtain absorption slurry in the brine loop that circulates again of evaporimeter.Absorption slurry comprises the preferential adsorption site, makes silica in the output water preferably adsorb or with the crystal co-precipitation but not form the scale deposition thing on the heating surface of evaporimeter.
Using under the magnesian situation, adding magnesium to keep the weight ratio between about 0.5: 1 and 3: 1 of the magnesium and silica in output water or the salt solution.In a kind of technological design, magnesium (Mg) and silica (SiO
2) ratio be about 1.0.When adding output water to, magnesia and water react to form magnesium hydroxide crystal.Magnesia will improve the pH of output water.The magnesium hydroxide crystal magnitude range usually about 0.5 to about 10 μ.For the ease of the absorption silica, the pH of concentrate or salt solution should be at least 9.2 and preferably in 10.2 to 11.2 scope.Because the rising pH that interpolation magnesia causes has reduced the solubility of magnesium hydroxide.Because magnesium hydroxide absorption is extracted a large amount of silicas out from solution.The silica of extracting out from solution is adsorbed onto on the magnesium hydroxide.Therefore the silica concentration with dissolving is reduced to relatively low level.Remaining a small amount of silica is easy to stay in the solution and does not produce fouling.
Adding calcium oxide or calcium hydroxide to output water, also should add material to keep calcium and the weight ratio of silica between about 0.5: 1 and 3: 1 in the output water to form under the situation of adsorbing pulp material.Calcium oxide or calcium hydroxide and output water react to form the calcium carbonate crystal slurry.The magnitude range of calcium carbonate crystal is between about 5 microns to about 20 microns.For the ease of the absorption silica, the pH of concentrate or salt solution should at least 9.5 and preferably in 10.2 to 11.2 scope.Some mixtures of the chemicals of interpolation such as soda ash or NaOH or these chemicals are to adjust the precipitation that pH promotes calcium carbonate crystal.Usually, about 90% silica adsorbed by calcium carbonate crystal and with the calcium carbonate crystal co-precipitation.
The oxide that adds Ti, Al, Si to output water or composite oxides or similar compound with the situation that forms the absorption slurry under, also should add material with keep the output underwater gold and belong to and about 0.5: 1 and 5: 1 of silica between weight ratio.The surface nature of compound makes and removes silica from solution.The magnitude range of suspended solid is between about 5 to 100 microns.Be convenient to adsorb among the embodiment of silica, the pH of concentrate or salt solution should at least 9.5 and preferably in 10.2 to 11.2 scope.Some mixtures of the chemicals of interpolation such as soda ash or NaOH or these chemicals promote absorption to adjust pH.Usually, about 90% silica adsorbed by calcium carbonate crystal and with the calcium carbonate crystal co-precipitation.
Fig. 2 illustrates the method for handling output water, and wherein, this method is utilized absorption sizing process mentioned above in conjunction with a pair of evaporimeter and a pair of film.Under the situation of Fig. 2 technology, provide two evaporimeters 110,112 that place substantially between crystallization generator and boiler or the steam generator.Each evaporimeter 110,112 comprises salt solution flow line 114,116 again.In addition, evaporimeter 110,112 comprises distillation outlet line 118,120.Should be appreciated that evaporimeter 110,112 produces water vapour in a usual manner, to form distillation, derive from evaporimeter 110,112 via outlet line 110 and 120 then by distillation through condensation for water vapour. Distillation outlet line 118 and 120 is communicatively connected to steam generator feed line 40, and steam generator feed line 40 will be directed to steam generator by evaporimeter 110,112 distillations that produced then.
Two ceramic membranes 130 and 132 are associated with evaporimeter 110,112.The details of ceramic membrane will not describe in detail in this article, because this itself is not that material of the present invention and other ceramic membrane are as known in the art.About the commentary of general ceramic membrane technology, with reference to U.S. Patent No. 6,165,553 and No.5,611,931 disclosure, the content of these patents is attached to herein clearly by reference.Ceramic membrane 130 places between evaporimeter 110 and 112, and ceramic membrane 132 places the downstream of evaporimeter 112.Salt solution feed line 122 extends to ceramic membrane 130 from brine stream stylet 114.Salt solution feed line 124 from salt solution again flow line 116 extend to ceramic membrane 132.Return line 140 will be in ceramic membrane 130,132 one or both barrier stream are directed to one or more points of first evaporimeter, 110 upstreams.See that in Fig. 2 the part of the concentrated salt solution of circulation is directed to film 130 and 132 again in pipeline 114 and 116. Film 132 and 132 each all produce and intercept logistics and permeate stream.The permeate stream of ceramic membrane 130 is directed to evaporimeter 112, and other point that is used for further process for purifying is discarded or be directed to the permeate stream of ceramic membrane 132.Return line 140 is divided into section 140A and 140B.Section 140A makes the obstruct logistics turn back to evaporimeter 110.That is, section 140A makes barrier turn back to evaporimeter 110 or to the point of vaporizer upstream and crystal region or reactor downstream.Section 140B makes barrier turn back to crystal region or reactor.This return can be directed to crystal region or crystal region upstream and preferably oil/moisture from the point in downstream, unit.In case solid concentration and the solid concentration in the return line that can monitor in the return line 140 arrive threshold value, the part that intercepts logistics can be directed to waste streams 28, and waste streams 28 is led to dewatering process.As shown in Figure 2 dewatering process produces thickened waste materials flow 60 and low concentration stream 29, low concentration stream 29 be recycled in this technology of crystal region upstream a bit.In some cases, preferably only recycling from the obstruct logistics of first ceramic membrane 130.Under the sort of situation, can discard or be directed to other point or zone in this technology from the obstruct logistics 142 of ceramic membrane 132.Should note bypass line 144, it extends around first ceramic membrane 130.This allows salt solution or its part in the pipeline 122 to walk around first ceramic membrane and be introduced directly into second evaporimeter 112.
In the technology of Fig. 2, as discussed above, in crystallization reactor, mix with output water such as magnesia or the such metallic compound of magnesium chloride.In one example, this causes magnesium hydroxide to form, magnesium hydroxide in output water with the silica co-precipitation.That is, silica is adsorbed onto on the magnesium hydroxide crystal that precipitates in crystallization reactor.Therefore, precipitated silica finally terminates in salt solution again in the flow line 114 again in the salt solution of circulation.Remove most of precipitated silica by first ceramic membrane 130.To finally terminate in the salt solution of circulation in pipeline 116 at the remaining solvable silica in the permeate stream of film 130.From the salt solution of pipeline 116 filter by second ceramic membrane 132 and therefore the obstruct logistics of second film also can comprise precipitated silica and other suspended solid.
If have a large amount of suspended solids in the output water in crystallization reactor, supposition absorption slurry is more effective so.Therefore, one of effect of playing from the obstruct logistics of ceramic membrane 130,132 by recycling is that output water in crystallization reactor adds suspended solid.Suppose in the output water in crystallization reactor 5,000 to 10, the suspended sediment concentration of 000Mg/L is favourable.Also supposition more wishes 20,000 to 30, the suspended sediment concentration of 000Mg/L magnitude.Therefore, can provide various monitorings and control device to system and the technology that Fig. 2 described, it is used for the suspended sediment concentration of crystallization control reactor output water routinely in waste water industry.
Fig. 3 illustrates and above discusses and the similar sizing process of sizing process shown in Figure 2.But in the embodiments of figure 3, only provide a ceramic membrane 130 and its to be located at the downstream of second evaporimeter 112.In the case, flow through from the barrier of ceramic membrane 130 and be recycled to the point of evaporimeter 110 or evaporimeter 110 upstreams by pipeline 140 and 140A.In addition, some that intercept in the logistics can be recycled to the point of crystallization reactor or crystallization reactor upstream via pipeline 140B.
In above institute's discussion and Fig. 2 and technology shown in Figure 3, film 130,132 serves as separator.In a particular embodiment, film is a ceramic membrane.But should be appreciated that and understand these separators can be other type form membrane or or even the strainer or the separator of other type, such as cyclone hydraulic separators.
In Fig. 2 and technology shown in Figure 3, the time of staying in the crystallization reactor can change.In one embodiment, the time of staying is about ten minutes to about 40 minutes, and during this period of time, output water fully mixes with one or more crystallization reagent.And in these process implementing examples, the pH of output water can change, but under representative condition, can change between about 10.5 the pH at about 9.2 pH, and in a selection process, the pH of output water can be changed to about 10.0 from about 9.7.At crystallization reagent is under the situation of magnesia or magnesium chloride, for example, and magnesium and SiO
2Ratio as ppmMg than ppm SiO
2For about 0.5 to 3.0 and be preferably about 1.0.The amount of the barrier of circulation can change again in Fig. 2 and technology shown in Figure 3.In an exemplary processes, about 60% barrier can be circulated to the point of upstream again.Suppose that preferably flow rate will be about 20% to 40% again.
Go to Fig. 4, another absorption sizing process shown in it.Utilize this absorption sizing process in conjunction with evaporimeter.But under the situation of Fig. 4 technology, crystallization reactor places evaporimeter 202 downstreams and is arranged in especially and is connected to the salt solution tributary 210 of flow line 206 again.That is,, be directed to evaporimeter 202 from the output water that obtains by pipeline 204 from oil/moisture as in Fig. 4, seeing.Evaporimeter 202 produces water vapour, and water vapour is condensed and is directed to steam generator as distillation by pipeline 208.And evaporimeter 202 produces and concentrates salt solution, and concentrated salt solution is passing through evaporimeter in the flow line 206 constantly more again.Tributary 210 is connected to flow line 206 again and is used for and will be directed to crystallization reactor in the part of the salt solution of pipeline 206 circulation.At the crystallization reactor place, add such as the such crystallization reagent of magnesia or magnesium chloride and such as the such caustic alkali of NaOH, and mix with salt solution.In this process implementing example, all ingredients can mix with concentrated salt solution with from concentrating the various contaminants of salt water sedimentation, such as silica.For example, can add all cpds,, make the contaminants precipitation such as magnesia, magnesium chloride, calcium oxide, alumina, iron oxide and other precipitating reagent.As discussed above, under the situation of magnesia or magnesium chloride, form magnesium hydroxide and with the silica co-precipitation, significantly reduce the silica concentration of dissolving in the salt solution.The salt solution that comprises precipitated silica is derived by tributary 210 from crystallization reactor.Some that have in the salt solution of precipitated silica can be discarded via pipeline 218.The state-variable of being discussed above can change between technology such as the time of staying, pH etc.Generally speaking, the state-variable of above being discussed is identical substantially with the state-variable that can be applicable to Fig. 4 technology.
Go to the technology of Fig. 5, this absorption sizing process and technology shown in Figure 4 are similar, are located at except film 214 in the tributary 210 in crystallization reactor downstream.In the case, the concentrated salt solution that has precipitated silica is directed to film 214, such as ceramic membrane.Film 214 produces and intercepts logistics, and intercepting logistics derives via pipeline 216 from film.Barrier in the pipeline 216 is can be by pipeline 216C optionally discarded or can turn back to any or two section 216A or 216B.Intercept logistics 216 and concentrate suspended solid is arranged, and all obstruct logistics or its part can turn back to the entrance side of film 214.All or part of turned back to crystallization reactor of identical barrier is so that increase the concentration of suspended solid in the crystallization reactor.
Example
The output water sample is carried out intermediate experiment.The purpose of test is in order to determine scaling tendency.The dosage of magnesia and NaOH mixes with output water with simulation absorption sizing process.Carry out test with about 97% the rate of recovery, the expression time per unit is about 97% of the time per unit output water quality that is fed into evaporimeter 202 by the distillation quality that used single evaporimeter produced.Use comprises the single tube falling film evaporator of steam main body, and circulation pump, the surface condenser that is used for process steam, steam and process condensate thing receiver, feeding groove and the feed pump that has a variable speed drives are carried out intermediate experiment again for falling film heat exchanger, salt solution with variable speed drives.
The charging that is used for intermediate experiment is the output water sample.Analysis to the output water sample is provided in the table 1 below.
Table 1
| Describe | Unit | The charging of 97% rate of recovery | |
| Ph | 7.68 | ||
| Total suspended solid | ppm | 138 | |
| About the sample that filters | |||
| Total solid (105C) | ％ | 0.23 | |
| Ash content (dry solids basis) | ％ | 34.7 | |
| Sulfate | ppm | N.D (color interference) | |
| Chloride | ppm | 260 | |
| Fluoride | ppm | 2 | |
| Sulfide as S | ppm | ＜1 | |
| TOC | ppm | 596 | |
| COD | ppm | 2000 | |
| Extractible hexane (HEM) | ppm | 26 | |
| As C
6H
5Total oxybenzene compound of | ppm | 116 | |
| TIC | ppm | 31 | |
| As CaCO 3Total alkalinity | ppm | 333 | |
| Ammonium (NH 4) | ppm | 66 | |
| Calcium | ppm | 2 | |
| Magnesium | ppm | 0.6 | |
| Sodium | ppm | 321 | |
| Potassium | ppm | 18 | |
| As SiO 2Total silica | ppm | 255 | |
| Boron (via AA) | ppm | ＜10 |
Carried out intermediate experiment in continuous several days.Utilize 510ppm MgO and 25ppm NaOH to handle the output water sample.Equally, target recovery rate is 97%.
Tentative evaporimeter utilizes magnesia and the pre-slurrying of NaOH.Resulting slurry comprises 1.3% as Mg (OH)
2Magnesium.Use the part of this mixture to come to tentative evaporimeter reinforced.
Carry out intermediate experiment and during this period of time in about 340 hours period, the thermal transmittance slight modification of falling liquid film interchange of heat but as one man be defined as beginning about 0.9 to 1.0 of thermal transmittance.After test in about 340 hours, check the falling film evaporation organ pipe.Find that remainder that the pipe top has normal variable color and a pipe shows as cleaning.By carrying out chemically cleaning in three hours at 160 times weak acid solutions that in evaporimeter, circulate.After pickling, access tube finds to have removed variable color once more.Observed thermal transmittance and manage spatter property and show that all magnesia provides effective control to the silica scaling tendency with the output water sample of the nominal distillation rate of recovery 97% after test.
Concentrate based on magnesian intermediate experiment is analyzed.Silica (SiO in the duration of test dissolving
2) concentration is in 4 to 21ppm scope.The pH of concentrate is changed to about 10.24 from about 9.86.Total suspended solid as the percentage of concentrate in about scope of 1.5 to 3.9.
Be used in this article to describe and the term " guiding " of a material or a movement-oriented part to technology contained directly and guiding indirectly.For example, term is directed to second evaporimeter with at least a portion of brine stream and represents that brine stream is directed to second evaporimeter directly or indirectly.
Certainly under the situation that does not depart from essential characteristic of the present invention, the present invention certainly alternate manner outside the specifically statement mode of this paper carries out.It is illustrative and not restrictive that current embodiment is considered in all respects, and be covered by among the present invention in the meaning and the intention of all changes in the equivalent scope of appended claims.
Claims (21)
1. method from the oil well recovered oil, it may further comprise the steps:
A. from described oil well recovered oil/aqueous mixtures;
B. from described oil/aqueous mixtures separating oil to produce oil product and wherein to have the output water that dissolves silica;
C. output water is directed to evaporimeter and produces water vapour and concentrated salt solution;
D. magnesia or magnesium chloride are mixed with described output water or described concentrated salt solution and form magnesium hydroxide, to keep the weight ratio of magnesium and silica be 0.5: 1 to 3.0: 1 thereby wherein quantitatively add magnesia or magnesium chloride;
E. from described output water or described described magnesium hydroxide of concentrated salt solution co-precipitation and silica;
The concentrated salt solution that f. will have the output water of precipitated silica or have a precipitated silica is directed to eliminator and produces low suspended solid stream and higher suspension efflux of solids;
G. at least a portion of the described higher suspension efflux of solids of recycling is 5000Mg/L or higher to described output water or described concentrated salt solution so that keep the concentration of suspended solid in described output water or the concentrated salt solution.
H. the described water vapour that produced by described evaporimeter of condensation is to form distillation;
I. described distillation is directed to steam generator and heats described distillation in the described steam generator to produce water vapour; And
J. described water vapour is injected into and injects into well, cause the formation of described oil/aqueous mixtures.
2. method according to claim 1, it comprises that the pH that keeps described output water or concentrated salt solution is 9.8 to 12.0.
3. method according to claim 2, thus it comprises and quantitatively adds magnesia or magnesium chloride to described output water or concentrated salt solution to keep the weight ratio of magnesium and silica be 1: 1.
4. method according to claim 1, wherein, described magnesia or magnesium chloride mix with described output water, make the co-precipitation in described output water of described magnesium hydroxide and silica; And wherein said evaporimeter is first evaporimeter, and wherein said method comprises: at least a portion that described concentrated salt solution is directed to second evaporimeter and evaporates described concentrated salt solution is to produce second brine stream and after-fractionating logistics.
5. method according to claim 4, it comprises described second brine stream is separated into filtered stream and concentrated suspended solid stream, and at least a portion that will described concentrated suspended solid flows is recycled to described first evaporimeter.
6. method according to claim 4, it comprises that the concentration factor of keeping the output water that is directed to described first evaporimeter is lower than the concentration factor of the concentrated salt solution that is directed to described second evaporimeter.
7. method according to claim 4, it comprises described second brine stream is directed to ceramic membrane and described second brine stream is separated into filtered stream and concentrated suspended solid stream, and at least a portion that will concentrate suspended solid stream is recycled to described first evaporimeter or is recycled to and concentrates the point that suspended solid stream mixes with described output water described in this technology.
8. method according to claim 1, wherein, described evaporimeter is first evaporimeter, and second evaporimeter wherein is provided and places first separator between described first and second evaporimeters, and described method comprises:
A. described output water is directed to described first evaporimeter and produces first brine stream and first distillating stream,
B. described first brine stream is directed to described first separator and described first brine stream is separated into filtered stream and concentrated suspended solid stream;
At least a portion that c. will concentrate suspended solid stream is recycled to described first evaporimeter; And,
D. will be directed to second evaporimeter and produce second brine stream and the after-fractionating logistics by the filtered stream that described first separator produces.
9. method according to claim 8, wherein, described first separator comprises at least one ceramic membrane.
10. method according to claim 8, wherein, second separator that places the described second evaporimeter downstream is provided, and described method comprises that at least a portion with described second brine stream is directed to described second separator and produces second filtered stream and the second concentrated suspended solid stream; And, second at least a portion that concentrates suspended solid stream is directed to described first evaporimeter.
11. method according to claim 10, it comprises that at least a portion that makes described first brine stream walks around first separator that places between described first and second evaporimeters, makes the part of described first brine stream not be directed to described second evaporimeter under the situation of not filtered by described first separator.
12. method according to claim 1, it comprises that by described magnesia or magnesium chloride are mixed the pH that improves described salt solution or output water with output water be 9.8 to 12.0.
13. method according to claim 4, it comprises described concentrated salt solution or second brine stream is directed to film and generation intercepts logistics, and at least a portion of described obstruct logistics is recycled to described first evaporimeter or is recycled to the point that the logistics of obstruct described in this technology mixes with described output water.
14. method according to claim 1, it comprises:
A. by the salt solution that is associated with the described evaporimeter flow line described concentrated salt solution that circulates again again;
B. with in the described concentrated salt solution at least some from described salt solution again flow line be directed to the tributary;
C. described magnesia or magnesium chloride are mixed with described concentrated salt solution in the described tributary and the described concentrated salt solution in described tributary in form magnesium hydroxide; And,
D. from described described magnesium hydroxide of concentrated salt solution co-precipitation and silica.
15. method according to claim 14, it comprises that at least some that make described concentrated salt solution turn back to described salt solution flow line again from described tributary.
16. method according to claim 14, it comprises magnesia or magnesium chloride and described concentrated salt solution to be directed to the film that places described tributary and to filter described concentrated salt solution to form permeate stream and concentrated suspended solid obstruct logistics with after described concentrated salt solution in the described tributary mixes.
17. the method from the oil well recovered oil, it comprises:
A. from described oil well recovered oil/aqueous mixtures;
B. from described oil/aqueous mixtures separating oil to produce oil product and wherein to have the output water that dissolves silica;
C. described output water is directed to evaporimeter and produces water vapour and concentrated salt solution;
D. by the salt solution of the circulation again pipeline that is associated with the described evaporimeter described concentrated salt solution that circulates again;
E. with salt solution from described salt solution again flow line be directed to tributary with mixing tank;
F. mixed precipitant and described concentrated salt solution in the described mixing tank in described tributary;
G. in described tributary, precipitate the silica in the described concentrated salt solution;
H. at least a portion that has the described concentrated salt solution of precipitated silica in the described tributary is back to described salt solution flow line again;
I. the water vapour that produced by described evaporimeter of condensation is to form distillation;
J. the distillation that described distillation is directed to steam generator and heats in the described steam generator produces water vapour; And
K. described water vapour is injected into and injects well, cause the formation of described oil/aqueous mixtures.
18. method according to claim 17, its be included in the described mixing tank in the described tributary with magnesia or magnesium chloride mixes with described concentrated salt solution and described concentrated salt solution in described tributary in form magnesium hydroxide; And, magnesium hydroxide and silica in described tributary in the described concentrated salt solution of co-precipitation.
19. method according to claim 17 wherein, after mixing described precipitating reagent and described concentrated salt solution, is directed to film with described concentrated salt solution and filters described concentrated salt solution and produce filtered stream and the obstruct logistics of concentrated suspended solid.
20. method according to claim 19, it comprises at least a portion of the described obstruct logistics of recycling and in described film upstream described obstruct logistics is mixed with described concentrated salt solution, thereby increases the concentration of suspended solid in the described concentrated salt solution.
21. method according to claim 20, it comprises that the concentration of keeping suspended solid in the described mixing tank is 10,000Mg/L or higher.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US96818007P | 2007-08-27 | 2007-08-27 | |
| US60/968180 | 2007-08-27 | ||
| PCT/US2008/074442 WO2009029653A1 (en) | 2007-08-27 | 2008-08-27 | Process for removing silica in heavy oil recovery |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101835954A CN101835954A (en) | 2010-09-15 |
| CN101835954B true CN101835954B (en) | 2013-07-31 |
Family
ID=40387762
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200880113363.9A Active CN101835954B (en) | 2007-08-27 | 2008-08-27 | Process for removing silica in heavy oil recovery |
Country Status (4)
| Country | Link |
|---|---|
| CN (1) | CN101835954B (en) |
| BR (1) | BRPI0815845B1 (en) |
| RU (1) | RU2479713C2 (en) |
| WO (1) | WO2009029653A1 (en) |
Families Citing this family (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2954950B1 (en) | 2010-01-06 | 2012-02-24 | Total Sa | STEAM PRODUCTION AND ITS APPLICATION TO ASSISTED HYDROCARBON RECOVERY |
| WO2013142764A2 (en) * | 2012-03-22 | 2013-09-26 | E. I. Du Pont De Nemours And Company | Produced water treatment in oil recovery |
| CA2794356C (en) * | 2012-09-13 | 2018-10-23 | General Electric Company | Treatment of produced water with seeded evaporator |
| GB2510159B (en) * | 2013-01-27 | 2015-04-22 | Ide Technologies Ltd | Evaporator array for a water treatment system |
| CA2860277C (en) * | 2014-06-02 | 2016-10-25 | Veolia Water Solutions & Technologies North America, Inc. | Oil recovery process including enhanced softening of produced water |
| CA2958071C (en) | 2014-08-13 | 2019-01-15 | Veolia Water Technologies, Inc. | Method and apparatus of flash-cooling produced water and heating steam generator feedwater |
| CN107032515A (en) * | 2016-02-04 | 2017-08-11 | 通用电气公司 | Technique and system for preparing the method and apparatus of steam and oil recovery comprising it from output current |
| US10807895B2 (en) | 2016-04-14 | 2020-10-20 | Veolia Water Technologies, Inc. | Process for treating produced water with magnesium oxide |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3193009A (en) * | 1963-02-28 | 1965-07-06 | Shell Oil Co | Use of low-grade steam containing dissolved salts in an oil production method |
| US4663367A (en) * | 1984-08-30 | 1987-05-05 | The Borden Company Limited | Compositions and methods for reducing the permeability of underground strata |
| US4877536A (en) * | 1981-04-23 | 1989-10-31 | Bertness Enterprises, Inc. | Method of treating saline water |
| US5611931A (en) * | 1995-07-31 | 1997-03-18 | Media And Process Technology Inc. | High temperature fluid separations using ceramic membrane device |
| US6733636B1 (en) * | 1999-05-07 | 2004-05-11 | Ionics, Inc. | Water treatment method for heavy oil production |
| CN1902437A (en) * | 2003-11-26 | 2007-01-24 | 水技术国际股份有限公司 | Method for production of high pressure steam from produced water |
Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6536523B1 (en) * | 1997-01-14 | 2003-03-25 | Aqua Pure Ventures Inc. | Water treatment process for thermal heavy oil recovery |
| CA2296357C (en) * | 1997-07-23 | 2006-07-04 | Cleansorb Limited | Methods for deposition of materials in underground reservoirs |
| US6165553A (en) * | 1998-08-26 | 2000-12-26 | Praxair Technology, Inc. | Method of fabricating ceramic membranes |
| US6734144B2 (en) * | 2000-04-25 | 2004-05-11 | Exxonmobil Upstream Research Company | Solids-stabilized water-in-oil emulsion and method for using same |
| US6447577B1 (en) * | 2001-02-23 | 2002-09-10 | Intevep, S. A. | Method for removing H2S and CO2 from crude and gas streams |
| RU2215871C2 (en) * | 2001-05-03 | 2003-11-10 | Аква-Пьюэр Вентчерс Инк. | Method of removal of polluting impurities from incoming flow |
| US20030127391A1 (en) * | 2001-07-26 | 2003-07-10 | Craft Frank S. | Method for treatment of circulating cooling water |
| CA2414949C (en) * | 2002-12-20 | 2010-04-13 | Imperial Oil Resources Limited | Integrated water treatment and flue gas desulfurization process |
-
2008
- 2008-08-27 WO PCT/US2008/074442 patent/WO2009029653A1/en active Application Filing
- 2008-08-27 RU RU2010111793/03A patent/RU2479713C2/en active
- 2008-08-27 BR BRPI0815845-2A patent/BRPI0815845B1/en not_active IP Right Cessation
- 2008-08-27 CN CN200880113363.9A patent/CN101835954B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3193009A (en) * | 1963-02-28 | 1965-07-06 | Shell Oil Co | Use of low-grade steam containing dissolved salts in an oil production method |
| US4877536A (en) * | 1981-04-23 | 1989-10-31 | Bertness Enterprises, Inc. | Method of treating saline water |
| US4663367A (en) * | 1984-08-30 | 1987-05-05 | The Borden Company Limited | Compositions and methods for reducing the permeability of underground strata |
| US5611931A (en) * | 1995-07-31 | 1997-03-18 | Media And Process Technology Inc. | High temperature fluid separations using ceramic membrane device |
| US6733636B1 (en) * | 1999-05-07 | 2004-05-11 | Ionics, Inc. | Water treatment method for heavy oil production |
| CN1902437A (en) * | 2003-11-26 | 2007-01-24 | 水技术国际股份有限公司 | Method for production of high pressure steam from produced water |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101835954A (en) | 2010-09-15 |
| BRPI0815845B1 (en) | 2018-06-12 |
| RU2479713C2 (en) | 2013-04-20 |
| RU2010111793A (en) | 2011-10-10 |
| BRPI0815845A2 (en) | 2015-02-24 |
| WO2009029653A1 (en) | 2009-03-05 |
| BRPI0815845A8 (en) | 2015-12-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7905283B2 (en) | Process for removing silica in heavy oil recovery | |
| CN101835954B (en) | Process for removing silica in heavy oil recovery | |
| US8047287B2 (en) | Process for recovering heavy oil utilizing one or more membranes | |
| CN101835957B (en) | Process for recovering heavy oil utilizing one or more membranes | |
| US7681643B2 (en) | Treatment of brines for deep well injection | |
| US7150320B2 (en) | Water treatment method for heavy oil production | |
| CA2307819C (en) | Water treatment method for heavy oil production | |
| US20030127226A1 (en) | Water treatment method for heavy oil production | |
| CN205740622U (en) | A kind of percolate coagulating sedimentation, evaporation joint processing system | |
| CN102659197B (en) | Water treatment process for recovering heavy oil recovery produced water to serve as boiler feed water | |
| CA2818176C (en) | Method of recovering oil and producing produced water that is concentrated and dried by a double drum dryer | |
| RU2705684C2 (en) | Method of extracting oil, which includes improved softening of formation water | |
| CN104128080A (en) | Method for recovering calcium salt by treating high Cl high CO2 burning flue gas and waste burning fly ash water washing lotion | |
| Heins et al. | Achieving zero liquid discharge in SAGD heavy oil recovery | |
| CA2448680A1 (en) | Water treatment method for heavy oil production | |
| US9127540B2 (en) | Method of recovering oil and producing produced water that is concentrated and dried by a double drum dryer | |
| CA2640421C (en) | Process for removing silica in heavy oil recovery | |
| CA2567171C (en) | Treatment of brines for deep well injection | |
| RU2247232C2 (en) | Method for processing water for extraction of oil by thermal methods | |
| CN108883950A (en) | With the method for magnesia processing recovered water |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| ASS | Succession or assignment of patent right |
Owner name: VEOLIA WATER TREATMENT TECHNOLOGY NORTH AMERICA CO Free format text: FORMER OWNER: HPD LLC Effective date: 20130703 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20130703 Address after: American Pennsylvania Applicant after: Veolia Water Solutions & Technologies North America Inc. Address before: Illinois State Applicant before: HPD LLC |
|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |