CN104086679B - A kind of apparatus and method of its oil removing of macromolecule resin and application - Google Patents
A kind of apparatus and method of its oil removing of macromolecule resin and application Download PDFInfo
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- CN104086679B CN104086679B CN201410269759.XA CN201410269759A CN104086679B CN 104086679 B CN104086679 B CN 104086679B CN 201410269759 A CN201410269759 A CN 201410269759A CN 104086679 B CN104086679 B CN 104086679B
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Abstract
The present invention relates to the degreasing technique of oily waste water, the coalescence material in particularly a kind of coalescence method degreasing technique, and deoiling method and device.One of the object of the invention is to provide one kind and prepares simple macromolecule resin, it is obvious that the second purpose is to provide a kind of oil removal rate height, energy-saving and water-saving benefit, using the degreasing unit of the macromolecule resin, the third purpose is to provide the method using the oil removing in high oil-containing wastewater of the synthetic resin and degreasing unit.The macromolecule resin is stablized and firm the most in the lipophilic group subsequently introduced, and can recycle, and preparation process is more simple, without carrying out amination.The degreasing unit, includes agglomerator, oily-water seperating equipment, and its design feature is, also includes：Pressure test device, automatically controls progress loosening resin bed by pressure inductor, reaches the purpose of reduction operation pressure；The agglomerator upper end is provided with flushing water inlet, and the agglomerator lower end is provided with flushing water out.
Description
Technical field
The present invention relates to the degreasing technique of oily waste water, the coalescence material in particularly a kind of coalescence method degreasing technique, and
Deoiling method and device.
Background technology
Oily waste water mainly includes the waste water of oil field waste, oil plant and petrochemical plant, water ballast, the washing of tanks of oil tanker
Water, engine room water, rinse water of oil truck etc..This is to cause environment oily pollution, particularly marine oil pollution (such as oil pollution)
Main source.
The degreasing technique of current oily waste water mainly includes Bubble-floating Method, membrane separation process, absorption method, biochemical process and coalescence method
Deng.Bubble-floating Method and biochemical process can produce secondary pollution in processing procedure, in addition it is also necessary to subsequent technique, and water outlet oil content still phase
To higher；The problem of there is fouling membrane in membrane separation process, so that cause operating pressure to increase, and film is expensive, cost is higher；Inhale
Attached method is exactly mainly with activated carbon oil suction, although effect preferably, but activated carbon reach needed after adsorption saturation regeneration, and regenerate behaviour
Make cumbersome, and the waste water that regeneration is produced still pollutes the environment.
Coalescence method is the method that separation purpose is reached using residence time difference of the water-oil phase on coalescence material, is contained
When oily waste water is by coalescence material, residence time of the elaioleucite on coalescence material is more than the residence time of water, so that elaioleucite is temporary transient
It is adsorbed on coalescence material and forms oil film, disengaging coalescence material gathers when oil film reaches certain thickness, then under hydraulic action
And into big elaioleucite, it is final to be separated profit using profit density variation.
Application No. 201110246699.6 discloses a kind of synthetic resin, preparation method and applications, for oil content
For 10-100mg/L stoste, oil removal rate is more than 99%, and oil recovery rate is more than 90%.The resin that the invention is provided removes oiliness
Can be stable, the service life of resin as long as five years more than.Its oil removing application process provided, steam condensate passes through filled with suction
The resin column of oleoresin makes content oily in water be down to below 1mg/L.But it is due to that the usual flow of industrial wastewater is larger, 99%
Oil removal rate and 90% oil recovery rate still have greater number of greasy dirt to be removed, and except the preparation technology ratio of oleoresin
It is more complicated, limited by raw sewage oil content.
Therefore, using preparing the simpler, sorbing material with more preferable performance and the more degreasing unit of high-efficiency long-life
It is to utilize the key breakthrough point for coalescing method degreasing technique.
The content of the invention
One of the object of the invention is to provide one kind and prepares simple macromolecule resin, and the second purpose is to provide a kind of oil removal rate
High, energy-saving and water-saving benefit substantially, using the degreasing unit of the macromolecule resin, the third purpose be to provide using the synthetic resin and
The method of degreasing unit oil removing in high oil-containing wastewater.
The present invention solves the technical scheme that is used of above-mentioned technical problem：
A kind of macromolecule resin, is made up of following methods：
Step one, matrix polymer is mixed with water, pH to 8~14 is adjusted with sodium hydroxide；
Step 2,60 DEG C~90 DEG C are warming up to by the product of step one；
Step 3, modifying agent is added into the product of step 2, and the mass ratio of modifying agent, matrix polymer and water is
0.05~0.25：1：1, it is incubated 3 hours~8 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin；
The matrix polymer is cross-linking type polystyrene gel-type strongly acidic cation exchange resin；
The modifying agent is quaternary ammonium salt cationic surfactant.
Processing step made above is simple, easily realizes, the requirement to reaction is relatively low, and product is stable.
Preferably, the degree of cross linking of the cross-linking type polystyrene gel-type strongly acidic cation exchange resin is 3~14.
Preferably, the quaternary ammonium salt cationic surfactant is hexadecyltrimethylammonium chloride, octadecyl
Trimethyl ammonium chloride, dodecyl benzyl dimethyl ammonium chloride, dodecyl dimethyl benzyl ammonium bromide and hexadecyl
One or more in pyridine.
A kind of degreasing unit using above-mentioned macromolecule resin, its design feature is, includes agglomerator, water-oil separating
Device,
It is provided with the agglomerator in resin bed, the resin bed and is provided with pressure test device and flusher, institute
State pressure test device with the top layer and bottom of the resin bed to be connected, the flushing water inlet of the flusher is arranged on described
Resin bed upper end, the flushing water out of the flusher is arranged on the resin bed lower end, and the flusher is in the pressure
The pressure difference that device for detecting difference is measured exceedes clean resin bed pressure difference 0.35kg/cm2Shi Qidong；The agglomerator bottom, which is provided with, to be contained
Oil-polluted water outlet is provided with the top of greasy dirt water inlet, the agglomerator；
The oil-polluted water outlet is communicated with the processing water inlet of the oily-water seperating equipment, and the processing water inlet is set
In the bottom of the oily-water seperating equipment, the oily-water seperating equipment bottom is additionally provided with processing water out, the water-oil separating
Device top is provided with overflow oil-out and pneumostome.
Preferably, it is described processing water inlet be higher than the processing water out, processing water inlet and processing water out it
Between be provided with porous oil isolated from water plate, the water by water-oil separating is discharged from the delivery port of the lower partition, porous oil isolated from water plate
The separation for assembling oil and condensate can further be realized.
Preferably, the processing water inlet end is additionally provided with water-locator, the water-locator and is provided with air inlet pipe, should
The principle that method with reference to Bubble-floating Method oil removing draws its strong point, is combined by bubble with oil droplet, further improves oil droplet
Rise separating rate and separating effect.
Preferably, the device of falling infundibulate is provided with the oily-water seperating equipment, on big under the device of falling infundibulate
Small, in the case where overall flow is constant, processing water flow velocity is constantly accelerated from the bottom to top, so as to the wholly liquid state of its feed liquor side
System produces suction, ingenious to make use of this principle so that the oil droplet of oil removing resin surface absorption is easier to be pulled away.
A kind of method that oil removing is carried out using above-mentioned macromolecule resin and degreasing unit, step is：
Step one, oil-polluted water is pumped into from bottom to top from the oil-polluted water entrance, is flowed through and is fixed in the resin bed
Macromolecule resin, by the surface tension effects between grease and the macromolecule resin, make grease in the macromolecule resin
Upper aggegation forms film, realizes the demulsification enrichment of grease, the droplet size of the oil-polluted water is between 10~130 microns, institute
Maximum must be reached by stating resin surface product；
Step 2, as grease is continuously adsorbed on macromolecule resin, the thickness of the film reaches critical value, containing greasy dirt
The impulse force of water current, the difference of profit density can tear film from macromolecule resin surface, by described in the resin bed
The apical cap of agglomerator realizes the aggegation of grease, and then exports outflow from oil-polluted water as processing water, and the agglomerator is in stable state
Lower operation, the oil mass of oil mass and the processing water disengaged into the resin bed oil-polluted water is balanced, when pressure differential detection dress
Put the pressure difference measured and exceed clean resin bed pressure difference 0.35kg/cm2Shi Suoshu flushers start；
Step 3, the processing water is pumped into after air enters the water-locator by the processing water inlet, and then from institute
State water-locator and flow into the oily-water seperating equipment bottom, the processing water flow velocity must be limited by climbing speed in STOKE laws,
Larger oil droplet is gathered into assembly oil on the oily-water seperating equipment top, from oil-out export；Processing water through oil removing passes through
Turn into condensate after the porous oil isolated from water plate, from the processing water out export.Preferably, when the oil-polluted water enters
When oil-polluted water oil content is 1mg/L at mouthful, flow velocity is 100m3/ h, the deoiling effect under this flow velocity is best.
Preferably, the size of larger oil droplet is more than 150 microns in the step 2, oil droplet aggegation becomes big and is conducive to oily richness
Collection and separation.
The present invention compared with the existing technology has advantages below and effect：1st, because matrix polymer is cross-linking type styrene
It is gel-type strongly acidic cation exchange resin, stablizes the most and firm in the lipophilic group subsequently introduced, and can be anti-
It is multiple to utilize；2nd, preparation process is more simple, without carrying out amination；3rd, it is provided with pressure test device in degreasing unit and flushing is opened
Close, the impurity in resin bed can be removed in time, loosen resin bed, increase the service life, when entering coolant-temperature gage≤120 DEG C, fortune
5 to 10 years row time；4th, degreasing unit be divide into integral type and split type two kinds, is conducive to the installation in different places；5th, should
The deoiling method that oleoresin is removed with this is also up to more than 99.5% to the oil removal rate of big oil mass oil-polluted water, and not by raw sewage
Oil content and oil-containing species limitation, maximum oil content can reach 1000mg/L.
Brief description of the drawings
In order to illustrate more clearly about the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or existing
There is the accompanying drawing used required in technology description to be briefly described, it should be apparent that, drawings in the following description are only this
Some embodiments of invention, for those of ordinary skill in the art, without having to pay creative labor, may be used also
To obtain other accompanying drawings according to these accompanying drawings.
Fig. 1 is integral type oil removing system structural representation of the invention.
Fig. 2 is split type oil removing system structural representation of the invention.
Fig. 3 is the apparatus structure schematic diagram of falling infundibulate of the invention.
Fig. 4 is porous oil isolated from water plate structure schematic diagram of the invention.
Fig. 5 is water distributor structure schematic diagram of the invention.
Label declaration：Agglomerator 10, resin bed 11, oil-polluted water entrance 12, oil-polluted water outlet 13, screen cloth 14, dress tree
Fat mouthfuls 15, unload resin mouthful 16, water cap 17, apical cap 18, dividing plate 19, oily-water seperating equipment 20, processing water inlet 21, processing water out
22nd, the device of falling infundibulate 23, bottom surface steel ring 231, round table surface 232, contraction mouth 233, support frame 234, oil-out 24, pneumostome
25th, porous oil isolated from water plate 26, Disengagement zone 27, flush switch 30, flushing water inlet 31, flushing water out 32, pressure differential detection dress
Put 40, observation visor 41, inspection manhole 42, water-locator 43, link pipeline 44, air inlet pipe 45.
Embodiment
With reference to embodiment, the present invention is described in further detail, following examples be explanation of the invention and
The invention is not limited in following examples.
Embodiment 1：
The present embodiment following section describes a kind of macromolecule resin：
The macromolecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 3 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 8 is adjusted with sodium hydroxide；
Step 2,60 DEG C are warming up to by the product of step one；
Step 3, hexadecyltrimethylammonium chloride 50g is added into the product of step 2, is incubated 3 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
The present embodiment following section describes a kind of degreasing unit：
As shown in Figure 1,3, the degreasing unit, is gone out by agglomerator 10, resin bed 11, oil-polluted water entrance 12, oil-polluted water
Mouthfuls 13, screen cloth 14, dress resin mouthful 15, unload resin mouthful 16, water cap 17, apical cap 18, dividing plate 19, oily-water seperating equipment 20, processing water
Entrance 21, processing water out 22, the device of falling infundibulate 23, bottom surface steel ring 231, round table surface 232, contraction mouth 233, support frame 234,
Oil-out 24, pneumostome 25, porous oil isolated from water plate 26, Disengagement zone 27, flush switch 30, flushing water inlet 31, flushing water go out
Mouth 32, pressure test device 40, observation visor 41, inspection manhole 42, water-locator 43, link pipeline 44, air inlet pipe 45 are constituted.
The bottom inlet of agglomerator 10 is communicated with oil-polluted water entrance 12 and flushing water out 32, in the bottom inlet of agglomerator 10
Place is provided with screen cloth 14, and oil-polluted water flows into agglomerator 10 by screen cloth 14.The tree of macromolecule resin is filled with agglomerator 10
Fat bed 11, the upper and lower side of resin bed 11, which is respectively arranged with dividing plate 19, dividing plate 19, is provided with water cap 17, and oil-polluted water passes through water cap 17
Flow into resin bed 11.Water cap 17 is metal winding, and material is that 316L has a stronger corrosion resistance, and gap is that 0.2mm can be with
Effectively avoid resin leakage.The inductor of pressure test device 40 is provided between the upper and lower side of resin bed 11, to examine
Survey the pressure difference of resin bed 11.Oil-polluted water flows out by the apical cap 18 of agglomerator 10 from oil-polluted water outlet 13.Rinse water inlet
31 are arranged on the upper end of agglomerator 10, rinse water out 32 and are arranged on the lower end of agglomerator 10, go out in flushing water inlet 31 and flushing water
Mouth 32 is respectively arranged with flushing taps 30.
Oil-polluted water outlet 13 is communicated with the processing water inlet 21 of oily-water seperating equipment 20, and processing water inlet 21 is arranged on oil
The bottom of water separation device 20, the bottom of oily-water seperating equipment 20 is additionally provided with processing water out 22, and processing water out 22 is higher than place
Water inlet 21 is managed, the device of falling infundibulate 23 is provided with therebetween, the device of falling infundibulate 23 is up-small and down-big, bottom surface steel ring 231
With the wall of oily-water seperating equipment 20 be fitted close by oily-water seperating equipment 20 be divided into above and below two parts, only communicated with contraction mouth 233, on
Portion is Disengagement zone 27.Handle water out 22 and be located at the top of bottom surface steel ring 231, processing water inlet 21 is located at the lower section of bottom surface steel ring 231.
The contraction mouth 233 of the end of round table surface 232 is connected by the support frame 234 of outer with oily-water seperating equipment 20.Oily-water seperating equipment
20 tops are provided with oil-out 24 and pneumostome 25.
Inspection manhole 42 and observation visor are provided with the position at the top of degreasing unit, bottom and setting resin bed 11
41。
During work, for using the buoyancy of oil, oil-polluted water is pumped into, flows through and be fixed on from bottom to top from oil-polluted water entrance 12
Macromolecule resin in resin bed 11, the lipophilic group of macromolecule resin can attract the dispersed oil droplets in water, pass through oil and oleophylic
The surface tension of interlaminar resin, makes oil aggegation on round resin particle form film.As oil is continuously adsorbed on resin, the thickness of film
Reach critical value.The impulse force of oil-polluted water current, the difference of profit density can tear oil film from resin surface.The oil disengaged
Drop is smaller due to density, enters apical cap 18 by resin bed 11 and top water cap 17, eventually becomes processing water and goes out from oil-polluted water
Mouth 13 flows out.According to material balance, agglomerator 10 is run in the steady state, and the oil mass and the oil mass disengaged into resin bed 11 are put down
Weighing apparatus.
In order to protect the interior arrangement of agglomerator 10, the pressure difference of resin bed 11 must be monitored, pressure test device 40 is by setting
The inductor put between the upper and lower side of resin bed 11 obtains pressure difference data, when pressure difference exceedes clean resin bed pressure difference 0.35kg/cm2
When (5 pounds/square inch), just alarmed by pressure test device 40.Flush switch 30 starts simultaneously, and flushing water enters from flushing water
Mouth 31 is flowed into, and is flowed out, is rinsed from top to bottom from water out 32 is rinsed；Current are flowed into from water out 32 is rinsed afterwards, from flushing water
Entrance 31 flows out, and carries out backwash, so alternately 10~30 minutes, quickly can recover pressure difference to normal value.Rinse frequency with containing
In oily water depending on suspended impurity content, according to operating experience, about 7 to 40 days once.It is total that flushing institute water consumption only accounts for processing water
The 0.1~0.3% of amount.
Oily-water seperating equipment 20 is arranged on directly over agglomerator 10, and processing water enters water-oil separating from processing water inlet 21 and filled
20 bottoms are put, due to upper small greatly under the device of falling infundibulate 23, water flow velocity is handled from the bottom to top in the case where overall flow is constant
Constantly accelerate, so as to produce suction to wholly liquid state system below, be more beneficial for taking away the oil of oil removing resin surface absorption
Drop.Handle water and flow into Disengagement zone 27 from contraction mouth 233, into after Disengagement zone 27, processing water flow velocity reduction, water (flow) direction also changes
Become, because oil droplet density is small and size increases, oil droplet will be separated from processing water.Processing water speed rate into Disengagement zone 27 must be by
The limitation of climbing speed in STOKE laws, do not make these increased in size oil droplet from processing water out 22 flow out.Handle in water
Water due to density it is larger, sedimentation is condensed in into the outside of the round table surface 232 i.e. bottom of Disengagement zone 27, as condensate.Disengagement zone 27
Bottom condensate is essentially static state, and dynamic is gradually become upwards along the inclined-plane of round table surface 232, and oil droplet is collected in Disengagement zone 27
Top, which turns into, assembles oil.Finally, assemble oil to export from oil-out 24, condensate is exported from processing water out 22.Assemble oil base sheet
On be pure oil, moisture is no more than 0.5%.
The effect of pneumostome 25 is the air at the top of remover apparatus, the pressure balance of adjustment equipment inside and outside.Oil-out
24 be closed mode when flat, is discharged when assembling oil and reaching certain limit in oily-water seperating equipment 20.
It is the function of oil-polluted water oil content, such as oil-polluted water oil content in the oil mass of the collected overhead of oily-water seperating equipment 20
1mg/L, flow velocity is 100m3/ h, oil mass of collecting maximum daily is 2.5L.Under normal circumstances, oily-water seperating equipment 20 is reclaimed
Oil mass is simultaneously little, such as oil plant heater leakage, and substantial amounts of oil will be made to enter oil-polluted water, and at this moment oil-polluted water oil content will
Up to 100mg/L, the volume that oil is collected daily is up to 0.25m3。
Condensate oil content after processing can typically be less than 1mg/L, if oil content is less than 100mg/ during oil-polluted water inflow
L, then condensate oil content is unrelated with oil-polluted water oil content.Average condensate oil content can maintain 0.3~0.5mg/L.
The present embodiment following section describes a kind of deoiling method for applying above-mentioned degreasing unit and macromolecule resin：
Step one, oil-containing water is pumped into agglomerator, during oil-containing water is by resin bed, the lipophilic group of resin bed
Oil molecule is collected on resin surface, the demulsification enrichment of grease is realized, the droplet size of oil-polluted water 10~130 microns it
Between, the resin surface product must reach maximum；
Step 2, the aggegation of grease forms oily film, and oily film is constantly accumulated, when the critical value for reaching impulsive force stripping
When, oily film departs from from the resin layer surface being fixedly installed, and forms larger oil droplet, realizes the aggegation of grease, the size of larger oil droplet is big
In 150 microns；
Step 3, is exported with the processing water of larger oil droplet by agglomerator, into oily-water seperating equipment, controls water-oil separating
The speed of current in device, larger oil droplet rises to form oil reservoir, realizes oil removing.
Oil removing according to the method described above, is not limited by oil content and oil-containing species, and maximum oil content can reach 1000mg/L, is contained
The various operating modes such as lid steam condensate, petroleum chemical enterprise's recirculated water, industrial wastewater, oilfield sewage, oil removal rate is more than 99.0%, oil
The rate of recovery reaches 95%.Resin needs to be essentially filled with resin bed, and the speed of service is 5~8BV/h, when entering coolant-temperature gage≤120 DEG C,
Run time 5 to 10 years.
Embodiment 2：
Degreasing unit and deoiling method used in the present embodiment is same as Example 1, and difference is that water-oil separating is filled
The construction and the preparation method of macromolecule resin put.
As shown in Fig. 2,4,5, the processing water inlet 21 of oily-water seperating equipment 20 is gone out by linking pipeline 44 with oil-polluted water
Mouth 13 is connected, and processing water inlet 21 is arranged on the middle and lower part of oily-water seperating equipment 20, and the processing pipe end of water inlet 21 is provided with
Water-locator 43, the lower section of water-locator 43 is provided with porous oil isolated from water plate 26, and porous oil isolated from water plate 26 is by carbon steel line with rubber, thickness of slab 20
~30mm, aperture diameter 20mm, the diameter 400mm of inspection manhole 42, bottom is made support frame using 10 channel-section steels and is fixed.Chain is taken over
Air inlet pipe 45 is provided with line 44, processing water out 22 is arranged on below the porous plane of oil isolated from water plate 26.
Water is handled during work and flows into oily-water seperating equipment 20 along link pipeline 44 from water-locator 43, is entering water-oil separating dress
Air is pumped into processing water by air inlet pipe 45 before putting 20, oil droplet is combined with air.Locate after into oily-water seperating equipment 20
The reduction of water water velocity is managed, water (flow) direction also changes, because the oil droplet density for combining air is small and size increases, oil droplet will add
Speed is separated from processing water.It must be limited by the processing water speed rate of oily-water seperating equipment 20 by climbing speed in STOKE laws,
Do not make these increased in size oil droplet from processing water out 22 flow out, condensate of the porous oil isolated from water plate below 26 is essentially
Static state, is thereon dynamic, oil droplet is collected in the top of oily-water seperating equipment 20.Finally, assemble oil to export from oil-out 24, coagulate
Bear water from processing water out 22 and export.It is substantially pure oil to assemble oil, and moisture is no more than 0.5%.
This macromolecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 4 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 8 is adjusted with sodium hydroxide；
Step 2,60 DEG C are warming up to by the product of step one；
Step 3, OTAC 60g is added into the product of step 2, is incubated 4 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 260mg/L of intaking, water outlet oil content is≤0.83mg/L.
Embodiment 3：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 5 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 8 is adjusted with sodium hydroxide；
Step 2,70 DEG C are warming up to by the product of step one；
Step 3, OTAC 70g is added into the product of step 2, is incubated 5 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin needs to be essentially filled with resin bed, and the speed of service is 6BV/h, is entered
Coolant-temperature gage is 80 DEG C, and oil-containing 280mg/L of intaking, water outlet oil content is≤0.76mg/L.
Embodiment 4：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 6 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 9 is adjusted with sodium hydroxide；
Step 2,75 DEG C are warming up to by the product of step one；
Step 3, dodecyl dimethyl benzyl ammonium bromide 80g is added into the product of step 2, is incubated 6 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 260mg/L of intaking, water outlet oil content is≤0.73mg/L.
Embodiment 5：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 7 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 9 is adjusted with sodium hydroxide；
Step 2,80 DEG C are warming up to by the product of step one；
Step 3, OTAC 90g is added into the product of step 2, is incubated 7 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 260mg/L of intaking, water outlet oil content is≤0.63mg/L.
Embodiment 6：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 8 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 9 is adjusted with sodium hydroxide；
Step 2,85 DEG C are warming up to by the product of step one；
Step 3, hexadecyltrimethylammonium chloride 50g, octadecyl trimethyl chlorination are added into the product of step 2
Ammonium 50g, is incubated 8 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 6BV/h, water inlet
Temperature is 60 DEG C, and oil-containing 180mg/L of intaking, water outlet oil content is≤0.65mg/L.
Embodiment 7：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 9 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 10 is adjusted with sodium hydroxide；
Step 2,90 DEG C are warming up to by the product of step one；
Step 3, dodecyl benzyl dimethyl ammonium chloride 50g, octadecyl trimethyl are added into the product of step 2
Ammonium chloride 60g, is incubated 3 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 260mg/L of intaking, water outlet oil content is≤0.72mg/L.
Embodiment 8：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 10 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 10 is adjusted with sodium hydroxide；
Step 2,60 DEG C are warming up to by the product of step one；
Step 3, dodecyl benzyl dimethyl ammonium chloride 40g, dodecyl dimethyl are added into the product of step 2
Benzylphosphonium Bromide ammonium 80g, is incubated 4 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 98%.Resin needs to be essentially filled with resin bed, and the speed of service is 7BV/h, water inlet
Temperature is 70 DEG C, and oil-containing 260mg/L of intaking, water outlet oil content is≤0.66mg/L.
Embodiment 9：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 11 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 10 is adjusted with sodium hydroxide；
Step 2,65 DEG C are warming up to by the product of step one
Step 3, dodecyl dimethyl benzyl ammonium bromide 60g, hexadecyl pyrrole are added into the product of step 2
Pyridine 70g, is incubated 5 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 5BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 270mg/L of intaking, water outlet oil content is≤0.61mg/L.
Embodiment 10：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 12 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 11 is adjusted with sodium hydroxide；
Step 2,70 DEG C are warming up to by the product of step one
Step 3, cetylpyridinium chloride 70g, hexadecyltrimethylammonium chloride are added into the product of step 2
70g, is incubated 6 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 98%.Resin needs to be essentially filled with resin bed, and the speed of service is 5BV/h, water inlet
Temperature is 25 DEG C, and oil-containing 268mg/L of intaking, water outlet oil content is≤0.53mg/L.
Embodiment 11：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 13 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 11 is adjusted with sodium hydroxide；
Step 2,75 DEG C are warming up to by the product of step one
Step 3, OTAC 80g, cetylpyridinium chloride are added into the product of step 2
70g, is incubated 7 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 98%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 60 DEG C, and oil-containing 180mg/L of intaking, water outlet oil content is≤0.43mg/L.
Embodiment 12：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 14 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 11 is adjusted with sodium hydroxide；
Step 2,80 DEG C are warming up to by the product of step one
Step 3, dodecyl dimethyl benzyl ammonium bromide 60g, dodecyl dimethyl are added into the product of step 2
Benzyl ammonium chloride 50g, cetylpyridinium chloride 50g, are incubated 8 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 97%.Resin needs to be essentially filled with resin bed, and the speed of service is 6BV/h, water inlet
Temperature is 50 DEG C, and oil-containing 230mg/L of intaking, water outlet oil content is≤0.58mg/L.
Embodiment 13：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 7 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 12 is adjusted with sodium hydroxide；
Step 2,85 DEG C are warming up to by the product of step one
Step 3, dodecyl dimethyl benzyl ammonium bromide 60g, hexadecyl pyrrole are added into the product of step 2
Pyridine 50g, hexadecyltrimethylammonium chloride 70g, are incubated 3 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96.8%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, is entered
Coolant-temperature gage is 60 DEG C, and oil-containing 300mg/L of intaking, water outlet oil content is≤0.72mg/L.
Embodiment 14：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 8 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 12 is adjusted with sodium hydroxide；
Step 2,90 DEG C are warming up to by the product of step one
Step 3, OTAC 60g, cetylpyridinium chloride are added into the product of step 2
70g, hexadecyltrimethylammonium chloride 60g, are incubated 4 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 98%.Resin needs to be essentially filled with resin bed, and the speed of service is 6BV/h, water inlet
Temperature is 60 DEG C, and oil-containing 260mg/L of intaking, water outlet oil content is≤0.53mg/L.
Embodiment 15：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 9 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 12 is adjusted with sodium hydroxide；
Step 2,60 DEG C are warming up to by the product of step one
Step 3, dodecyl benzyl dimethyl ammonium chloride 50g, cetyl trimethyl are added into the product of step 2
Ammonium chloride 80g, OTAC 70g, are incubated 5 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96.3%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, is entered
Coolant-temperature gage is 80 DEG C, and oil-containing 280mg/L of intaking, water outlet oil content is≤0.61mg/L.
Embodiment 16：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 10 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 13 is adjusted with sodium hydroxide；
Step 2,65 DEG C are warming up to by the product of step one
Step 3, dodecyl dimethyl benzyl ammonium bromide 40g, octadecyl trimethyl are added into the product of step 2
Ammonium chloride 110g, dodecyl benzyl dimethyl ammonium chloride 60g, insulation 6 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 100mg/L of intaking, water outlet oil content is≤0.45mg/L.
Embodiment 17：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 11 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 13 is adjusted with sodium hydroxide；
Step 2,70 DEG C are warming up to by the product of step one
Step 3, hexadecyltrimethylammonium chloride 40g, octadecyl trimethyl chlorination are added into the product of step 2
Ammonium 80g, dodecyl benzyl dimethyl ammonium chloride 70g, dodecyl dimethyl benzyl ammonium bromide 30g, are incubated 7 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 98%.Resin needs to be essentially filled with resin bed, and the speed of service is 5BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 200mg/L of intaking, water outlet oil content is≤0.66mg/L.
Embodiment 18：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 12 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 13 is adjusted with sodium hydroxide；
Step 2,75 DEG C are warming up to by the product of step one
Step 3, OTAC 60g, dodecyl dimethyl benzyl are added into the product of step 2
Ammonium chloride 70g, dodecyl dimethyl benzyl ammonium bromide 40g, cetylpyridinium chloride 60g, are incubated 8 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 60 DEG C, and oil-containing 100mg/L of intaking, water outlet oil content is≤0.43mg/L.
Embodiment 19：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 13 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 14 is adjusted with sodium hydroxide；
Step 2,80 DEG C are warming up to by the product of step one
Step 3, hexadecyltrimethylammonium chloride 70g, octadecyl trimethyl chlorination are added into the product of step 2
Ammonium 65g, dodecyl benzyl dimethyl ammonium chloride 85g, cetylpyridinium chloride 20g, are incubated 3 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 97%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 20 DEG C, and oil-containing 160mg/L of intaking, water outlet oil content is≤0.60mg/L.
Embodiment 20：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 14 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 14 is adjusted with sodium hydroxide；
Step 2,65 DEG C are warming up to by the product of step one
Step 3, hexadecyltrimethylammonium chloride 30g, octadecyl trimethyl chlorination are added into the product of step 2
Ammonium 75g, dodecyl benzyl dimethyl ammonium chloride 40g, dodecyl dimethyl benzyl ammonium bromide 50g, hexadecyl pyrrole
Pyridine 55g, is incubated 5 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin needs to be essentially filled with resin bed, and the speed of service is 6BV/h, is entered
Coolant-temperature gage is 60 DEG C, and oil-containing 250mg/L of intaking, water outlet oil content is≤0.60mg/L.
Embodiment 21：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 4 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 10 is adjusted with sodium hydroxide；
Step 2,60 DEG C are warming up to by the product of step one；
Step 3, OTAC 100g is added into the product of step 2, is incubated 4 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 60 DEG C, and oil-containing 150mg/L of intaking, water outlet oil content is≤0.46mg/L.
Embodiment 22：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 5 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 12 is adjusted with sodium hydroxide；
Step 2,70 DEG C are warming up to by the product of step one；
Step 3, OTAC 120g is added into the product of step 2, is incubated 5 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 260mg/L of intaking, water outlet oil content is≤0.53mg/L.
Embodiment 23：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 6 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 11 is adjusted with sodium hydroxide；
Step 2,75 DEG C are warming up to by the product of step one；
Step 3, dodecyl dimethyl benzyl ammonium bromide 120g is added into the product of step 2, is incubated 6 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate is up to 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, enters water temperature
Spend for 80 DEG C, oil-containing 360mg/L of intaking, water outlet oil content is≤0.83mg/L.
Embodiment 24：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 7 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 10 is adjusted with sodium hydroxide；
Step 2,80 DEG C are warming up to by the product of step one；
Step 3, OTAC 130g is added into the product of step 2, is incubated 7 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, is entered
Coolant-temperature gage is 80 DEG C, and oil-containing 230mg/L of intaking, water outlet oil content is≤0.73mg/L.
Embodiment 25：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 8 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 12 is adjusted with sodium hydroxide；
Step 2,85 DEG C are warming up to by the product of step one；
Step 3, hexadecyltrimethylammonium chloride 50g, octadecyl trimethyl chlorination are added into the product of step 2
Ammonium 80g, is incubated 8 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, is entered
Coolant-temperature gage is 80 DEG C, and oil-containing 230mg/L of intaking, water outlet oil content is≤0.81mg/L.
Embodiment 26：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 9 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 11 is adjusted with sodium hydroxide；
Step 2,90 DEG C are warming up to by the product of step one；
Step 3, dodecyl benzyl dimethyl ammonium chloride 70g, octadecyl trimethyl are added into the product of step 2
Ammonium chloride 90g, is incubated 3 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, is entered
Coolant-temperature gage is 80 DEG C, and oil-containing 240mg/L of intaking, water outlet oil content is≤0.66mg/L.
Embodiment 27：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 10 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 11 is adjusted with sodium hydroxide；
Step 2,60 DEG C are warming up to by the product of step one；
Step 3, dodecyl benzyl dimethyl ammonium chloride 90g, dodecyl dimethyl are added into the product of step 2
Benzylphosphonium Bromide ammonium 80g, is incubated 4 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 97%.Resin needs to be essentially filled with resin bed, and the speed of service is 7BV/h, water inlet
Temperature is 40 DEG C, and oil-containing 100mg/L of intaking, water outlet oil content is≤0.31mg/L.
Embodiment 28：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 11 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 10 is adjusted with sodium hydroxide；
Step 2,65 DEG C are warming up to by the product of step one
Step 3, dodecyl dimethyl benzyl ammonium bromide 100g, hexadecyl are added into the product of step 2
Pyridine 70g, is incubated 5 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 97%.Resin needs to be essentially filled with resin bed, and the speed of service is 9BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 280mg/L of intaking, water outlet oil content is≤0.83mg/L.
Embodiment 29：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 12 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 11 is adjusted with sodium hydroxide；
Step 2,70 DEG C are warming up to by the product of step one
Step 3, cetylpyridinium chloride 80g, hexadecyltrimethylammonium chloride are added into the product of step 2
110g, is incubated 6 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 6BV/h, water inlet
Temperature is 80 DEG C, and oil-containing 200mg/L of intaking, water outlet oil content is≤0.57mg/L.
Embodiment 30：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 13 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 12 is adjusted with sodium hydroxide；
Step 2,75 DEG C are warming up to by the product of step one
Step 3, OTAC 80g, cetylpyridinium chloride are added into the product of step 2
120g, is incubated 7 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 98%.Resin needs to be essentially filled with resin bed, and the speed of service is 6BV/h, water inlet
Temperature is 60 DEG C, and oil-containing 200mg/L of intaking, water outlet oil content is≤0.63mg/L.
Embodiment 31：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 3 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 8 is adjusted with sodium hydroxide；
Step 2,60 DEG C are warming up to by the product of step one；
Step 3, OTAC 80g is added into the product of step 2, is incubated 7 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 25 DEG C, and oil-containing 260mg/L of intaking, water outlet oil content is≤0.73mg/L.
Embodiment 32：
Degreasing unit and deoiling method used in the present embodiment is identical with embodiment 1 or embodiment 2, and difference is height
Molecule resin is made up of following methods：
Step one, by the 10kg degrees of cross linking for 3 cross-linking type polystyrene gel-type strongly acidic cation exchange resin with
10kg water is mixed, and pH to 9 is adjusted with sodium hydroxide；
Step 2,90 DEG C are warming up to by the product of step one；
Step 3, dodecyl benzyl dimethyl ammonium chloride 90g, octadecyl trimethyl are added into the product of step 2
Ammonium chloride 70g, is incubated 8 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm~1.25mm, obtains height
Molecule resin.
Oil removing according to the method described above, is not limited, maximum oil content can reach 1000mg/L by oil content and oil-containing species, is removed
Oil cut rate is more than 99.5%, and oil recovery rate reaches 96%.Resin needs to be essentially filled with resin bed, and the speed of service is 8BV/h, water inlet
Temperature is 40 DEG C, and oil-containing 360mg/L of intaking, water outlet oil content is≤0.33mg/L.
Furthermore, it is necessary to explanation, the specific embodiment described in this specification, is named the shape of its parts and components
Title etc. can be different.The equivalent or simple change that all construction, feature and principles according to described in inventional idea of the present invention are done, is wrapped
Include in the protection domain of patent of the present invention.Those skilled in the art can be to described specific implementation
Example is made various modifications or supplement or substituted using similar mode, structure without departing from the present invention or surmounts this
Scope as defined in the claims, all should belong to protection scope of the present invention.
Claims (7)
1. a kind of degreasing unit of use macromolecule resin, it is characterised in that include agglomerator, oily-water seperating equipment, described
It is provided with agglomerator in resin bed, the resin bed and is provided with pressure test device and flusher, the pressure differential detection dress
Put and be connected with the top layer and bottom of the resin bed, the flushing water inlet of the flusher is arranged on the resin bed upper end,
The flushing water out of the flusher is arranged on the resin bed lower end, and the flusher is surveyed in the pressure test device
The pressure difference obtained exceedes the clean kg/cm of resin bed pressure difference 0.352Shi Qidong；The agglomerator bottom is provided with oil-polluted water entrance,
Oil-polluted water outlet is provided with the top of the agglomerator；
The oil-polluted water outlet is communicated with the processing water inlet of the oily-water seperating equipment, and the processing water inlet is arranged on institute
The bottom of oily-water seperating equipment is stated, the oily-water seperating equipment bottom is additionally provided with processing water out, the oily-water seperating equipment
Top is provided with overflow oil-out and pneumostome；
Described macromolecule resin is made up of following methods：
Step one, matrix polymer is mixed with water, pH to 8 ~ 14 is adjusted with sodium hydroxide；
Step 2,60 DEG C ~ 90 DEG C are warming up to by the product of step one；
Step 3, modifying agent is added into the product of step 2, the mass ratio of modifying agent, matrix polymer and water is 0.05
~0.25：1：1, it is incubated 3 hours ~ 8 hours；
Step 4, by product washing, the discharging of step 3, collects the end-product that granularity is 0.3mm ~ 1.25mm, obtains macromolecule
Resin；
The matrix polymer is cross-linking type polystyrene gel-type strongly acidic cation exchange resin；
The modifying agent is quaternary ammonium salt cationic surfactant.
2. degreasing unit according to claim 1, it is characterised in that the processing water inlet goes out higher than the processing water
Mouthful, it is provided with porous oil isolated from water plate between processing water inlet and processing water out.
3. degreasing unit according to claim 2, it is characterised in that the processing water inlet end is additionally provided with water distribution
Air intake structure is provided with device, the pipeline for connecting the processing water inlet and the water-locator.
4. degreasing unit according to claim 1, it is characterised in that be provided with down infundibulate in the oily-water seperating equipment
Device.
5. a kind of method that oil removing is carried out using degreasing unit described in claim 3, it is characterised in that step is：
Step one, oil-polluted water is pumped into from bottom to top from the oil-polluted water entrance, flows through the height being fixed in the resin bed
Molecule resin, by the surface tension effects between grease and the macromolecule resin, makes grease be coagulated on the macromolecule resin
Collection forms film, realizes the demulsification enrichment of grease, the droplet size of the oil-polluted water is between 10 ~ 130 microns, the resin
Surface area must reach maximum；
Step 2, as grease is continuously adsorbed on macromolecule resin, the thickness of the film reaches critical value, oil-polluted water water
The impulse force of stream, the difference of profit density can tear film from macromolecule resin surface, pass through aggegation described in the resin bed
The apical cap of device realizes the aggegation of grease, and then exports outflow from oil-polluted water as processing water, and the agglomerator is transported in the steady state
OK, into the resin bed oil-polluted water oil mass and the oil mass of the processing water disengaged is balanced, when the pressure test device is surveyed
The pressure difference obtained exceedes the clean kg/cm of resin bed pressure difference 0.352Shi Suoshu flushers start；
Step 3, the processing water is pumped into after air enters the water-locator by the processing water inlet, and then from the cloth
Hydrophone flows into the oily-water seperating equipment bottom, and the processing water flow velocity must be limited by climbing speed in STOKE laws, big oil
Drop in the oily-water seperating equipment top and be gathered into assembly oil, from oil-out export；Processing water through oil removing is by described
Turn into condensate after porous oil isolated from water plate, from the processing water out export.
6. deoiling method according to claim 5, it is characterised in that when the oil-polluted water porch oil-polluted water oil-containing
When measuring as 1mg/L, flow velocity is 100 m3/h。
7. deoiling method according to claim 5, it is characterised in that the size of larger oil droplet is more than 150 in the step 3
Micron.
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| CN104826578B (en) * | 2015-05-29 | 2017-03-22 | 浙江海洋学院 | Fly ash modified adsorbent and preparing method thereof and method of treating oily sewage |
| CN106943771B (en) * | 2017-03-07 | 2019-07-02 | 深圳市富益达材料科技有限公司 | A kind of degreaser and preparation method thereof of temperature-resistant high-efficient oily wastewater |
| CN116212976A (en) * | 2023-01-10 | 2023-06-06 | 江苏金杉新材料有限公司 | Modified cation exchange resin and preparation method thereof |
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| CN101298058A (en) * | 2008-06-13 | 2008-11-05 | 华东理工大学 | Modified cation-exchange resin and preparation and use thereof |
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| CN101781040B (en) * | 2010-03-12 | 2011-12-21 | 余金海 | Treatment device of oily sewage of oil field |
| CN102875717B (en) * | 2011-08-26 | 2014-06-04 | 中化化工科学技术研究总院 | Synthetic resin, and preparation method and application thereof |
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