CN108609793A - A kind of acidity water degasification deoiling method and its device - Google Patents
A kind of acidity water degasification deoiling method and its device Download PDFInfo
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- CN108609793A CN108609793A CN201810703462.8A CN201810703462A CN108609793A CN 108609793 A CN108609793 A CN 108609793A CN 201810703462 A CN201810703462 A CN 201810703462A CN 108609793 A CN108609793 A CN 108609793A
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 122
- 238000007872 degassing Methods 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000002253 acid Substances 0.000 claims abstract description 61
- 239000012071 phase Substances 0.000 claims abstract description 45
- 238000005119 centrifugation Methods 0.000 claims abstract description 35
- 238000000926 separation method Methods 0.000 claims abstract description 24
- 238000005192 partition Methods 0.000 claims abstract description 19
- 239000007788 liquid Substances 0.000 claims abstract description 18
- 239000000835 fiber Substances 0.000 claims abstract description 11
- 239000007791 liquid phase Substances 0.000 claims abstract description 11
- 238000004581 coalescence Methods 0.000 claims abstract description 8
- 239000004519 grease Substances 0.000 claims abstract description 8
- 239000012530 fluid Substances 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 37
- 238000005238 degreasing Methods 0.000 claims description 10
- 239000007792 gaseous phase Substances 0.000 claims description 10
- 238000004945 emulsification Methods 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 6
- 230000009471 action Effects 0.000 claims description 5
- 230000008859 change Effects 0.000 claims description 3
- 238000005728 strengthening Methods 0.000 claims description 3
- 230000009194 climbing Effects 0.000 claims description 2
- 238000013461 design Methods 0.000 claims description 2
- 230000008676 import Effects 0.000 claims description 2
- 239000003305 oil spill Substances 0.000 claims description 2
- 240000007594 Oryza sativa Species 0.000 claims 1
- 235000007164 Oryza sativa Nutrition 0.000 claims 1
- 235000013339 cereals Nutrition 0.000 claims 1
- 239000000839 emulsion Substances 0.000 claims 1
- 235000009566 rice Nutrition 0.000 claims 1
- 238000007701 flash-distillation Methods 0.000 abstract description 5
- 239000008267 milk Substances 0.000 abstract description 2
- 210000004080 milk Anatomy 0.000 abstract description 2
- 235000013336 milk Nutrition 0.000 abstract description 2
- 239000003921 oil Substances 0.000 description 89
- 229930195733 hydrocarbon Natural products 0.000 description 11
- 150000002430 hydrocarbons Chemical class 0.000 description 11
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 9
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 8
- 230000000694 effects Effects 0.000 description 7
- 238000009826 distribution Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 230000008569 process Effects 0.000 description 5
- 239000004215 Carbon black (E152) Substances 0.000 description 4
- 239000005864 Sulphur Substances 0.000 description 4
- 230000002378 acidificating effect Effects 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 230000003014 reinforcing effect Effects 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- 238000007667 floating Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000008213 purified water Substances 0.000 description 2
- 239000002516 radical scavenger Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 150000001412 amines Chemical class 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000009954 braiding Methods 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000003749 cleanliness Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
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- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000013527 degreasing agent Substances 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001125 extrusion Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
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- 230000009467 reduction Effects 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/06—Flash evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/32—Hydrocarbons, e.g. oil
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Physical Water Treatments (AREA)
Abstract
The invention discloses a kind of acid water degasification deoiling method and its devices, and the solution gas for carrying gas and pressure drop release to acid water first detaches；Acid water is handled using the method for centrifugation flash distillation, in flash tank liquid inlet, centrifugation flash distillation injector is set, the gas dissolved under flash tank operating pressure is further detached, by rotary fluid qi leel from centrifugal field micro-bubble is effectively removed, gas enters gas vent from gas-phase space；Liquid phase enters coarse coalescence module, and oil droplet carries out sinusoidal flowing with the flowing of liquid, and oil phase is moved upwards from top, and water phase is moved downward from bottom, forms the quick separating of grease.The unsegregated small oil droplet of part emulsified state carries out physics break milk separation using hydrophobe nona modified fiber module；The oil detached has been arrived the upper layer of liquid phase, device is gone out after overflow plate enters oil partition tank, water is flowed through from oil removal trench bottom, and the partition board for passing through water phase controls oil water interface height.
Description
Technical field
It is specifically a kind of de- using centrifugation flash distillation the present invention relates to a kind of method and apparatus of acid water degasification oil removing
Gas device will be originally used for split type degassing with tandem coalescing separator compact device and degreasing unit is integrated into complete set of equipments,
The advantage for having given full play to centrifugation flash liberation device and tandem coarse separation, realizes depth flash separation and the grease of gas
The process of separation efficiently, quickly removes dispersed gas and emulsification state oil droplet, and eliminates conventional settling tank and use interfacial meter
The inaccurate problem of oil water interface is measured, the steam stripped requirement of subsequent acidic water is met.
Background technology
Durings oil work, gas chemical industry, coal chemical industry etc., sulfur recovery facility is an essential device,
Its effect is that the sour gas containing hydrogen sulfide to being generated in chemical process is realized using process Recovered sulphur appropriate
Clean manufacturing, the purpose of environmental protection, and meet product quality requirement simultaneously, corrosion is reduced, realization device long period is raw safely
All multiple requirements such as production.And the hydrogen sulfide in acid water is one of the important sources of sulphur recovery sour gas, sour gas it is clear
The more high then sulfur recovery facility of cleanliness runs more stable.
Sour water of the raw water from each device of the whole audience of usual acidic water stripping device processing, due to making in pressure
Part lighter hydrocarbons substance, light oil, heavy oil is had under to be dissolved in inside sour water, if degassing deoiling effect is bad,
It will influence subsequent operation.Hydro carbons in raw water enters hydrocarbon in stripper if not being removed, in raw water
Matter will be stripped out, to influence H2The extrusion rate of S affects the quality of sour gas.Hydro carbons, light oil substance and H2S
Together enter subsequent sulphur unit can inside burner carbon distribution influence sulphur burner service life.Hydrocarbons calorific value compares
Height, into sulphur unit after can lead to the overtemperature of reacting furnace.Hydro carbons, light oil type can increase a large amount of pairs instead after entering sulfur reaction stove
It answers, or even will produce " black sulphur ", generating the substances such as COS, CS2 will not be got off by amine absorption, eventually enter into incinerator burning
At SO2, lead to discharge consumption that is exceeded, or entering flue gas desulfurization device increase absorbing liquid.
In addition, the oil in acid water will be brought in stripper if not removing, heating forms oil on tower tray
Envelope pushes up the insufficient top pressure fluctuation of temperature, influences sour gas quality, heavy oil, which enters in purified water, causes purified water unqualified.Raw material simultaneously
Water band oil can cause it is regular rush tower, cause the fluctuation of stripper temperature, pressure, liquid level, seriously affect steam stripped stable behaviour
Make.
Chinese invention patent CN104310685A discloses a kind of acid water treatment facilities and method, and it is single to pass through oil removing degassing
Member, acid water storage element change method and are effectively detached to the gas dissolved in acid water by voltage reduction method, sub-department
Gas be divided into gas phase and liquid phase by the method for gravitational settling, but be still dissolved in gas and the portion of acid water at this pressure
Divide micro-bubble that cannot be detached, still can be brought to downstream unit, downstream unit load is caused to increase.
Chinese invention patent CN105174520A discloses a kind of Acidulous water oil removing processing method, passes through homogeneous floating oil
Device goes out to swim, and carrying out oil-water separator again by the water being discharged after precipitation and separation carries out water-oil separating,.But the technique
Method is complicated, needs to set homogeneous floating oil collector, take up a large area, and degreaser cyclone can only partition density difference it is bigger and
The not serious grease system of emulsification, cannot efficiently separate the oil droplet of emulsification state.
In current acid water pretreatment deaerates oil removing, be badly in need of wanting it is a kind of realizes the depth separation of oil removing of deaerating, low energy consumption,
The low complete set of equipments of operating cost.
Invention content
In order to overcome the above-mentioned deficiencies of the prior art, the present invention proposes a kind of utilize and centrifuges flash liberation and substep classification
The technology of oil removing coupling to the size oil droplet that is carried in solution gas under gas entrained by acid water with pressure and the partial pressure and acid water into
The method and apparatus that row efficiently separates.It is not sufficiently effective that the present invention compensates for current acid water degassing tank, and the big tank sedimentation time is long, accounts for
The oil water interface meter circle position of the problems such as ground area is big and conventional degassing oil removing pot measures inaccurate problem.
The specific technical solution of the present invention is as follows：
The first aspect of the present invention provides acid water degasification deoiling method, step 1, the band gas oil-containing acid water first step
The solution gas for carrying gas and pressure drop release to acid water first under gravity field action into flash liberation device detaches；Step
2, acid water is handled using the method for centrifugation flash distillation, centrifugation flash distillation injector is set in flash tank liquid inlet, is relied on
Rotary fluid qi leel from barometric gradient field (pressure continuously decreases radial section from the outside to the core) will be dissolved under flash tank operating pressure
Gas further detach, by rotary fluid qi leel from centrifugal field micro-bubble is effectively removed, gas from gas phase sky
Between enter gas vent；Step 3, liquid phase enter coarse coalescence module, and the probability for increasing small oil droplet collision makes oil droplet
Grain size constantly grow up, oil droplet after growing up carries out sinusoidal stream by strengthening gravitational settling module, oil droplet with the flowing of liquid
Dynamic, oil phase is moved upwards from top, and water phase is moved downward from bottom, forms the quick separating of grease.Part emulsified state
Unsegregated small oil droplet carries out physics break milk separation using hydrophobe nona modified fiber module；Step 4, the oil detached are just
The upper layer for having arrived liquid phase goes out device after overflow plate enters oil partition tank, and water is flowed through from oil removal trench bottom, by water phase every
Plate controls oil water interface height, eliminates the use of oil water interface meter.
Further, described：
Step 1：The solution gas for carrying gas and pressure drop release to acid water first under gravity field action detaches, gassiness
The pressure of acid water with oil is 0.1~20MPa, and pressure is reduced to 0.01~19.95MPa, and treatment temperature is 5~99 DEG C；
Step 2：The barometric gradient field generated by centrifugal force using centrifugation flash liberation method carries out acid water secondary
Gas-liquid separation, the pressure difference in the centrifugal force are 0.01~0.2MPa, and treatment temperature is 5~99 DEG C；
Step 3：Using coalescence physical oil-removing separation method to the free state in the acid water after degassing, suspended state, emulsification
State oil droplet is detached；The pressure drop of the separation process is in 0.001~0.05MPa；
Step 4：Grease after being detached by step 3, oil spill stream enter oil phase collecting tank, are periodically arranged by fluid level controller
It puts, water is flowed through from the bottom of oil phase collecting tank, is discharged by Liquid level after climbing over water phase partition board later, and water phase partition board control is passed through
Oil water interface before liquefaction phase collecting tank.
Another aspect of the present invention, provides a kind of acid water degasification degreasing unit, the centrifugation flash liberation waste-oil scavenger,
Including shell, the national anthem parallel connection centrifugation flash liberation core pipe being set in shell, the multilevel oil removal module being set in shell, if
Entrance, liquid level gauge, differential manometer, liquid-phase outlet and the gaseous phase outlet being placed on shell, it includes a chamber to change centrifugation flash liberation core pipe
Body, the cavity are equipped with the import of core pipe liquid gas, core pipe gaseous phase outlet and core pipe liquid-phase outlet, oil and water separation bygranulation module distance centrifugation
Flash liberation device distance strengthens distance of the gravitational settling module apart from oil and water separation bygranulation module and exists between 300-2000mm
50mm, hydrophobe nona modified fiber module are exported apart from oil phase between 200-1800mm.
The acidity water degasification degreasing unit, including such as lower component：
(1) it is used to be dissolved in hydrocarbon gas, the H of acid water2S and NH3Equal gases by rotary fluid qi leel from barometric gradient
The centrifugation flash liberation device that field (pressure continuously decreases radial section from the outside to the core) is detached；
(2) it is used to the oil droplet of free state, dispersed, suspended state passing through the filling that is made of the solid matter of surface oleophylic
Bed quickly coalesces the coarse module grown up；
(3) oil droplet after being used to grow up does variable motion along corrugated plating, is then opened with certain ratio by wave crest, trough
Aperture quick separating reinforcing gravitational settling module；
(4) it is used to carry out the hydrophobe nano modification fibre that braiding combination is suitable for 0.1-20 μm of drop separation by Ω forms
Tie up module；
(5) it is used to control the baffle for receiving oil, the front apron of oil trap is less than rear baffle, before water phase partition board is less than oil trap
Baffle.
Further, the entrance in equipment is arranged in the centrifugation flash liberation device, away from pot bottom 800mm-1500mm；
Further, flow velocity is 0.8m/s-1.2m/s in the centrifugation flash liberation device；
Further, the centrifugation flash liberation device core pipe inlet diameter is 50-100mm, a diameter of 10- of gaseous phase outlet
30mm
Further, the coarse module material therefor is the substance of surface oleophilic drainage, i.e. oil, solid surface contact
Angle should be less than 70 °, and contact angle is smaller, and oleophylic wettability is better；
Further, the reinforcing gravitational settling module is arranged after coarse module, by wave crest, trough with one
The aperture that fixed-ratio is opened, oil float up to last layer folded plate, so carry out, can float or decline layer by layer；
Further, the hydrophobe nona modified fiber module is arranged after strengthening gravitational settling module, boundary
The design value of surface current speed is between 0.002-0.2m/s；
Further, the oil trap front apron is less than rear baffle about 100-600mm, and water phase partition board is less than oil trap
Front apron 50-300mm.
Compared with prior art, a kind of method and apparatus of acid water degasification oil removing provided by the invention has following excellent
Point：
(1) with traditional degassing tank ratio, degassing equipment processing speed provided by the invention is fast, degassing efficiency is high；Overcome acid
Property gas band hydrocarbon enter follow-up stripper plant, cause follow up device to fluctuate larger problem；
(2) with traditional oil removing pot ratio, waste-oil scavenger oil removal efficiency provided by the invention is high, easy to operate, equipment volume is small；
Overcome the big tank sedimentation time long, takes up a large area, the problems such as deoiling effect is bad.
Description of the drawings
Fig. 1 is the structural schematic diagram of acid water degasification oil removing.
In figure：1- gaseous phase outlets；2- gas-liquid two-phase entrances；3- centrifuges flash liberation device distribution pipe；4- centrifuges flash liberation
Device；5- coarse modules；6- strengthens gravitational settling module；7- hydrophobe fibre modules；8- oil traps；9- liquid level gauges；10- oil phases
Outlet；11- partition boards；12- water phases export；13- tank bodies.
Specific implementation mode
The present inventor has found afterwards after extensive and in-depth study, the flash liberation oil removing for acid water, compared with
It is the method that oil removing is settled using gravitational settling flash liberation tank and big tank for conventional method.In actual production, gravity is heavy
The problems such as dropping flash liberation tank there are degassing efficiencies low, acid water and bad oil phase layered effect.Therefore, invention is dodged using centrifugation
The technology of degassing plus coalescent deoiling is steamed, and centrifugation flash liberation device and oil removing module group are built in acid water degasification oil removing pot
Portion is flashed using the centrifugal force and decompression of eddy flow field, strengthens the degassing of acid water, utilize three layers of quick oil removing of oil removing module.
Low to efficiently solve current degassing tank degassing efficiency, oil removing pot oil removing is incomplete, the problems such as taking up a large area, improves acid
The degassing oil removal efficiency of property water.
The method of above-mentioned acidity water degasification oil removing, step：
Step 1：The solution gas for carrying gas and pressure drop release to acid water first under gravity field action detaches, gassiness
The pressure of acid water with oil is 0.1~20MPa, and pressure is reduced to 0.05~19.95MPa, and treatment temperature is 5~99 DEG C；
Step 2：The barometric gradient field generated by centrifugal force using centrifugation flash liberation method carries out acid water secondary
Gas-liquid separation, the pressure difference in the centrifugal force are 0.02~10.02MPa, and treatment temperature is 5~99 DEG C；
Step 3：Using coalescence physical oil-removing separation method to the free state in the acid water after degassing, suspended state, emulsification
State oil droplet is detached；The pressure drop of the separation process is in 0.001~0.05MPa.
Another aspect of the present invention, provides a kind of device of acid water degasification oil removing, which includes：
13 entrance of tank body is built-in with distribution pipe 3, enters centrifugation flash liberation device 4 and gaseous phase outlet 1 for distributing acid water；
The tank body 13 is built-in with coarse module 5, strengthens gravitational settling module 6, hydrophobe fibre module 7；Built in the tank body 13
It is useful for the oil partition tank 8 and oil discharge outlet 10 of separation oil phase；The tank body 13 further includes the partition board 11 and water phase for water phase overflow
Outlet 12；The centrifugation flash liberation device 4 of 13 entrance of the tank body is mounted in distribution pipe 3, and entrance is connected to distribution pipe.
In certain petrochemical industry acidic water stripping device technical process, the method according to the invention, using acid water degasification oil removing
Method and apparatus, centrifugation reinforcing carried out to the flash process of acid water, the hydro carbons that deep removal is wherein carried secretly is removed by coalescence
The method of oil efficiently separates oil in acid water.Its specific operation and effect are described as follows：
1. material properties and relevant parameter
Acid water treating capacity 140m3/ h, 40 DEG C of operation temperature, acid water density 700kg/m under operating condition3, operating condition
Lower oil content 3000-5000ppm, operating pressure 1.1MPa.
2. implementation process
Implement with reference to the method for the present invention, it is specific as follows：
Acid water enters centrifugation flash liberation device distribution pipe by acid water degasification oil expeller entrance, to being dissolved in liquid phase
Gas phase carry out centrifugation flash separation, the gas phase flashed off via gas-phase space from acid water degasification oil expeller gaseous phase outlet into
Enter gas pipe network.
Grease is layered after acid water after degassing enters coalescent deoiling module, and oil phase is on upper layer by overflowing to oil removal
In slot, oil is exported from oil partition tank oil phase and is discharged, and the water phase that water phase then enters degassing oil expeller by partition board exports, then goes to downstream
Device.
3. implementation result
(1) hydro carbons removal effect
After acid water centrifugation flash liberation device processing, gas phase hydrocarbon removal efficiency reaches 98% in acid water.
(2) oily removal effect
After the acid water coalescent deoiling resume module, the petroleum content in water phase outlet is less than or equal to 80ppm.
It is only the preferred embodiment of the present invention, implementation model not for the purpose of limiting the invention in summary
It encloses.Equivalence changes and modification made by the content of i.e. every claim according to the present invention should all belong to the skill of the present invention
Art scope.
Claims (9)
1. a kind of method of acidity water degasification oil removing, which is characterized in that steps are as follows：
Step 1, the band gas oil-containing acid water first step enter flash liberation device and carry gas to acid water first under gravity field action
And the solution gas of pressure drop release is detached；
Step 2, the centrifugal pressure that the gas dissolved under the degassing tank operating pressure is generated using centrifugation flash liberation method
Gradient fields carry out secondary separation so that the micro-bubble carried secretly in acid water can effectively remove, and the gas separated enters
Go out device after gas-phase space；
Acid water after step 3, degassing enters liquid Space from centrifugation flash liberation device bottom, first passes around coarse coalescence
Module, oil droplet are constantly grown up by continuous collision coalescence grain size, and the oil droplet after growing up is carried out using gravitational settling module is strengthened
Quick water-oil separating, the oil emulsion that part does not detach enter the laggard one-step physical demulsification of hydrophobe nona modified fiber module
Separation；
Step 4, detached by step 3 after grease, the oil detached arrived the upper layer of liquid phase, by overflow plate enter every
Go out device after oil groove, water is flowed through from oil removal trench bottom, and oil water interface height is controlled by the partition board of water phase.
2. a kind of method of acid water degasification oil removing according to claim 1, which is characterized in that described：
Step 1：The solution gas for carrying gas and pressure drop release to acid water first under gravity field action detaches, gassiness band oil
The pressure of acid water be 0.1~20MPa, pressure is reduced to 0.01~19.95MPa, and treatment temperature is 5~99 DEG C；
Step 2：Secondary gas-liquid is carried out to acid water by the barometric gradient field that centrifugal force generates using centrifugation flash liberation method
It detaches, the pressure difference in the centrifugal force is 0.01~0.2MPa, and treatment temperature is 5~99 DEG C；
Step 3：Using coalescence physical oil-removing separation method to free state, suspended state, the emulsification state oil in the acid water after degassing
Drop is detached；The pressure drop of the separation process is in 0.001~0.05MPa；
Step 4：Grease after being detached by step 3, oil spill stream enter oil phase collecting tank, are periodically discharged by fluid level controller,
Water is flowed through from the bottom of oil phase collecting tank, is discharged by Liquid level after climbing over water phase partition board later, is controlled by water phase partition board
Oil water interface before oil phase collecting tank.
3. a kind of acid water degasification degreasing unit realized as described in claims 1 or 2 method, including the centrifugation flash liberation remove
Oily device housings, each centrifugation flash liberation core pipe in parallel being set in shell, the multilevel oil removal module being set in shell,
Entrance, liquid level gauge, differential manometer, liquid-phase outlet and the gaseous phase outlet being set on shell, it includes one to change centrifugation flash liberation core pipe
Cavity, the cavity be equipped with the import of core pipe liquid gas, core pipe gaseous phase outlet and core pipe liquid-phase outlet, oil and water separation bygranulation module distance from
Heart flash liberation device distance strengthens distance of the gravitational settling module apart from oil and water separation bygranulation module and exists between 300-2000mm
50mm, hydrophobe nona modified fiber module are exported apart from oil phase between 200-1800mm, after the front apron of oil trap is less than
Baffle about 100-800mm, water phase partition board are less than the front apron 50-600mm of oil trap.
4. acidity water degasification degreasing unit according to claim 3, which is characterized in that the centrifugation flash liberation device is set
The entrance in equipment is set, away from pot bottom 800mm-1500mm.
5. acidity water degasification degreasing unit according to claim 3, which is characterized in that the coalescent deoiling form is thick
It is granulated module, strengthens gravitational settling module, hydrophobe nona modified fiber module using concatenated mode, the design of interface flow velocity
Value is between 0.002-0.2m/s.
6. acidity water degasification degreasing unit according to claim 3, which is characterized in that the centrifugation flash liberation device core
Pipe is combined using parallel mode, and flanged joint between core pipe and concetrated pipe, core pipe gaseous phase outlet is connected with tank body gas-phase space
It connects, circulation passage is centrifugation flash liberation core pipe pipe group.
7. acidity water degasification degreasing unit according to claim 3, which is characterized in that the centrifugation flash liberation device core
Pipe inlet diameter is 50-300mm, a diameter of 10-100mm of gaseous phase outlet.
8. acidity water degasification degreasing unit according to claim 3, which is characterized in that centrifugation flash liberation device entrance and acid
Property water inlet connection, coarse module is built in inside equipment, and strengthening gravitational settling module is built in inside equipment, and hydrophobe is received
Rice modified fibre module is built in inside equipment, and three modules are sequentially arranged, between it is separated by a distance.
9. acidity water degasification degreasing unit according to claim 3, which is characterized in that the front apron of oil trap is kept off after being less than
Plate, water phase partition board are less than the front apron of oil trap, and the front apron of oil trap is less than rear baffle about 100-800mm, and water phase partition board is low
In the front apron 50-600mm of oil trap.
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| CN201810703462.8A CN108609793A (en) | 2018-06-29 | 2018-06-29 | A kind of acidity water degasification deoiling method and its device |
| PCT/CN2019/090061 WO2020001246A1 (en) | 2018-06-29 | 2019-06-05 | Method and apparatus for degassing and oil removal of acidic water |
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| WO2020001246A1 (en) * | 2018-06-29 | 2020-01-02 | 上海米素环保科技有限公司 | Method and apparatus for degassing and oil removal of acidic water |
| CN113457190A (en) * | 2021-06-15 | 2021-10-01 | 中石化南京化工研究院有限公司 | Gas-liquid separator for synthesizing age resister 6PPD |
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| WO2020001246A1 (en) | 2020-01-02 |
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