CN104086679A - High polymer resin, and apparatus and method for removing oil by using it - Google Patents
High polymer resin, and apparatus and method for removing oil by using it Download PDFInfo
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- CN104086679A CN104086679A CN201410269759.XA CN201410269759A CN104086679A CN 104086679 A CN104086679 A CN 104086679A CN 201410269759 A CN201410269759 A CN 201410269759A CN 104086679 A CN104086679 A CN 104086679A
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Abstract
The invention relates to an oil-containing wastewater oil removal technology, and especially discloses a coalescence material used in a coalescence process oil removal technology, an oil removal method and an oil removal apparatus. The purposes of the invention comprise provision of a polymer resin simple to prepare, provision of an oil removal apparatus using the polymer resin and having a high oil removal rate and obvious energy and water saving benefits, and provision of a high-oil-content wastewater oil removal method using the above synthetic resin and the oil removal apparatus. The polymer resin is highly stable and firm in a subsequently introduced lipophilic group, can be repeatedly used, and is simple to prepare without amination. The oil removal apparatus comprises an aggregation device and an oil-water separating device, and also comprises a differential pressure detection device, and a resin layer is loosened through the automatic control of a pressure inductor in order to reduce the operation differential pressure; and the upper end of the aggregation device is provided with a wash water inlet, and the lower end of the aggregation device is provided with a wash water outlet.
Description
Technical field
The present invention relates to the degreasing technique of oily(waste)water, the coalescence material in a kind of coalescent method degreasing technique particularly, and deoiling method and device.
Background technology
Oily(waste)water mainly comprises oil field waste, the waste water of refinery and petroleum chemical plant, the water ballast of oil tanker, washwater, engine room water, the rinse water of tank wagon etc.This is the main source that causes environment oil pollution, particularly marine oil pollution (as petroleum pollution).
The degreasing technique of current oily(waste)water mainly comprises By Bubble-floating Method, membrane separation process, absorption method, biochemical process and coalescent method etc.By Bubble-floating Method and biochemical process can produce secondary pollution in treating processes, also need subsequent technique, and water outlet oleaginousness are still relatively high; The problem that membrane separation process exists film to pollute, thus cause operating pressure to increase, and film is expensive, and cost is higher; Absorption method is exactly mainly with gac oil suction, although effect is better, gac reaches absorption needs regeneration after saturated, and regenerative operation is loaded down with trivial details, and the waste water that regeneration produces still pollutes the environment.
Coalescent method is to utilize the residence time difference of profit two-phase on coalescence material to reach the method for separated object, when oily(waste)water passes through coalescence material, the residence time of elaioleucite on coalescence material is greater than the residence time of water, thereby elaioleucite is temporarily adsorbed on and on coalescence material, forms oil film, when oil film reaches certain thickness, under hydraulic action, depart from again coalescence material coalescence and become large elaioleucite, finally utilize profit density variation that profit is separated.
Application number is 201110246699.6 to disclose a kind of synthetic resins, preparation method and application thereof, the stoste that is 10-100mg/L for oleaginousness, and oil removal rate is more than 99%, and oil recovery rate is greater than 90%.The resin oil removing stable performance that this invention provides, reach more than 5 years the work-ing life of resin.The oil removing application process that it provides, steam condenses is down to below 1mg/L the content of oil in water by being filled with the resin column of oil-absorbing resin.But because the common flow of trade effluent is larger, 99% oil removal rate and 90% oil recovery rate still have the greasy dirt of a greater number not to be removed, and except preparation technology's more complicated of oleo-resinous, be subject to the restriction of sewage stoste oleaginousness.
Therefore, adopt preparation simpler, have the sorbing material of better performance and more the oil removal plant of high-efficiency long-life be the key breakthrough point that utilizes coalescent method degreasing technique.
Summary of the invention
One of the object of the invention is to provide a kind of simple macromolecule resin of preparing, two of object is to provide that a kind of oil removal rate is high, energy-saving and water-saving benefit is obvious, apply the oil removal plant of this macromolecule resin, three of object is to provide the method for this synthetic resins of application and oil removal plant oil removing in high oil-containing wastewater.
The present invention solves the problems of the technologies described above adopted technical scheme:
A macromolecule resin, by following methods, made:
Step 1, mixes matrix polymer with water, with sodium hydroxide, regulate pH to 8～14;
Step 2, is warming up to 60 ℃～90 ℃ by the product of step 1;
Step 3 adds modifying agent in the product of step 2, and the mass ratio of modifying agent, matrix polymer and water is 0.05～0.25:1:1, is incubated 3 hours～8 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin;
Described matrix polymer is cross-linking type polystyrene gel-type strongly acidic cation exchange resin;
Described modifying agent is quaternary ammonium salt cationic surfactant.
Above step of preparation process is simple, easily realizes, lower to the requirement of reaction, and product is stable.
As preferably, the degree of crosslinking of described cross-linking type polystyrene gel-type strongly acidic cation exchange resin is 3～14.
As preferably, described quaternary ammonium salt cationic surfactant is one or more in palmityl trimethyl ammonium chloride, octadecyl trimethyl ammonium chloride, dodecyl benzyl dimethyl ammonium chloride, dodecyl dimethyl benzyl ammonium bromide and cetylpyridinium chloride.
Use an oil removal plant for above-mentioned macromolecule resin, its constructional feature is, includes agglomerator, oily-water seperating equipment,
In described agglomerator, be provided with resin bed, in described resin bed, be provided with pressure test device and flushing arrangement, described pressure test device is connected with bottom with the top layer of described resin bed, the wash-down water entrance of described flushing arrangement is arranged on described resin bed upper end, the wash-down water outlet of described flushing arrangement is arranged on described resin bed lower end, and the pressure reduction that described flushing arrangement records at described pressure test device surpasses clean resin bed pressure reduction 0.35kg/cm
2shi Qidong; Described agglomerator bottom is provided with oily(waste)water entrance, and described agglomerator top is provided with oily(waste)water outlet;
Described oily(waste)water outlet communicates with the processing water inlet of described oily-water seperating equipment, described processing water inlet is arranged on the bottom of described oily-water seperating equipment, described oily-water seperating equipment bottom is also provided with processing water out, and described oily-water seperating equipment top is provided with and overflows hydraulic fluid port and pneumostome.
As preferably, described processing water inlet is higher than described processing water out, between processing water inlet and processing water out, be provided with porous oil isolated from water plate, water through oily water separation is discharged from the water outlet of the lower partition, and porous oil isolated from water plate can be realized further and assemble the separated of oil and condensed water.
As preferably, described processing water inlet end is also provided with water distributor, in described water distributor, is provided with inlet pipe, and the method is drawn its strong point with reference to the principle of By Bubble-floating Method oil removing, by bubble, combine with oil droplet, further promoted rising velocity of separation and the separating effect of oil droplet.
As preferably, in described oily-water seperating equipment, be provided with the device of falling doline, due to large little under the device of falling doline, the in the situation that of whole constant flow, processing water flow velocity constantly accelerates from the bottom to top, thereby the whole liquid system to its feed liquor side produces suction, ingenious this principle of having utilized is more easily pulled away the oil droplet of oil removing resin surface absorption.
A method of utilizing above-mentioned macromolecule resin and oil removal plant to carry out oil removing, step is:
Step 1, oily(waste)water pumps into from bottom to top from described oily(waste)water entrance, flow through and be fixed on the macromolecule resin in described resin bed, by the surface tension effects between grease and described macromolecule resin, make grease aggegation on described macromolecule resin form film, realize the breakdown of emulsion enrichment of grease, the droplet size of described oily(waste)water is between 10～130 microns, and described resin surface is long-pending must reach maximum value;
Step 2, along with grease continuous adsorption on macromolecule resin, the thickness of described film reaches threshold value, the difference of the impulse force of oily(waste)water current, profit density can be torn film from macromolecule resin surface, by the apical cap of agglomerator described in described resin bed, realize the aggegation of grease, and then become processing water from oily(waste)water outlet outflow, described agglomerator moves under stable state, enter the oil mass of described resin bed oily(waste)water and the oil mass balance of the processing water disengaging, the pressure reduction recording when described pressure test device surpasses clean resin bed pressure reduction 0.35kg/cm
2shi Suoshu flushing arrangement starts;
Step 3, described processing water enters described water distributor through described processing water inlet after pumping into air, and then flow into described oily-water seperating equipment bottom from described water distributor, described processing water flow velocity must be subject to the restriction of climbing speed in STOKE law, larger oil droplet is gathered on described oily-water seperating equipment top assembles oil, from described oil outlet, derives; Through becoming condensed water except oil handling water after described porous oil isolated from water plate, from described processing water out, derive.As preferably, when described oily(waste)water ingress oily(waste)water oleaginousness is 1mg/L, flow velocity is 100m
3/ h, the deoiling effect under this flow velocity is best.
As preferably, in described step 2, the size of larger oil droplet is greater than 150 microns, and oil droplet aggegation becomes and is conducive to greatly oily enrichment with separated.
The present invention compared with the existing technology has the following advantages and effect: 1, because matrix polymer is cross-linking type polystyrene gel-type strongly acidic cation exchange resin, the most stable and firm when the lipophilic group of follow-up introducing, and can recycle; 2, preparation process is more simple, without carrying out amination; 3, in oil removal plant, be provided with pressure test device and flush switch, can remove in time the impurity in resin bed, loosening resin layer, increases the service life, when entering water temp≤120 ℃, and 5 to 10 years working times; 4, oil removal plant has been divided into integral type and split type two kinds, has been conducive to the installation in different places; 5, apply this except deoiling method of oleo-resinous to the oil removal rate of large oil mass oily(waste)water also up to more than 99.5%, and not limited by sewage stoste oleaginousness and oil-containing kind, maximum oil content can reach 1000mg/L.
Accompanying drawing explanation
In order to be illustrated more clearly in the embodiment of the present invention or technical scheme of the prior art, to the accompanying drawing of required use in embodiment or description of the Prior Art be briefly described below, apparently, accompanying drawing in the following describes is only some embodiments of the present invention, for those of ordinary skills, do not paying under the prerequisite of creative work, can also obtain according to these accompanying drawings other accompanying drawing.
Fig. 1 is integral type oil removing system structural representation of the present invention.
Fig. 2 is split type oil removing system structural representation of the present invention.
Fig. 3 is the apparatus structure of falling doline schematic diagram of the present invention.
Fig. 4 is porous oil isolated from water plate structure schematic diagram of the present invention.
Fig. 5 is water distributor structure schematic diagram of the present invention.
Label declaration: agglomerator 10, resin bed 11, oily(waste)water entrance 12, oily(waste)water outlet 13, screen cloth 14, dress resin mouth 15, unload resin mouth 16, water cap 17, apical cap 18, dividing plate 19, oily-water seperating equipment 20, process water inlet 21, process water out 22, the device of falling doline 23, bottom surface steel ring 231, round table surface 232, contraction mouth 233, bracing frame 234, oil outlet 24, pneumostome 25, porous oil isolated from water plate 26, disengaging zone 27, flush switch 30, wash-down water entrance 31, wash-down water outlet 32, pressure test device 40, observe visor 41, inspection manhole 42, water distributor 43, link pipeline 44, inlet pipe 45.
Embodiment
Below in conjunction with embodiment, the present invention is described in further detail, and following examples are explanation of the invention and the present invention is not limited to following examples.
Embodiment 1:
The following part of the present embodiment has been described a kind of macromolecule resin:
This macromolecule resin is made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 3 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 8;
Step 2, is warming up to 60 ℃ by the product of step 1;
Step 3 adds palmityl trimethyl ammonium chloride 50g in the product of step 2, is incubated 3 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
The following part of the present embodiment has been described a kind of oil removal plant:
As Fig. 1, shown in 3, this oil removal plant, by agglomerator 10, resin bed 11, oily(waste)water entrance 12, oily(waste)water outlet 13, screen cloth 14, dress resin mouth 15, unload resin mouth 16, water cap 17, apical cap 18, dividing plate 19, oily-water seperating equipment 20, process water inlet 21, process water out 22, the device of falling doline 23, bottom surface steel ring 231, round table surface 232, contraction mouth 233, bracing frame 234, oil outlet 24, pneumostome 25, porous oil isolated from water plate 26, disengaging zone 27, flush switch 30, wash-down water entrance 31, wash-down water outlet 32, pressure test device 40, observe visor 41, inspection manhole 42, water distributor 43, link pipeline 44, inlet pipe 45 forms.
Agglomerator 10 bottom inlets communicate with oily(waste)water entrance 12 and wash-down water outlet 32, and at agglomerator, 10 bottom inlet places are provided with screen cloth 14, and oily(waste)water flows into agglomerator 10 through screen cloth 14.In agglomerator 10, be filled with the resin bed 11 of macromolecule resin, resin bed 11 upper and lower ends are respectively arranged with dividing plate 19, are provided with water cap 17 on dividing plate 19, and oily(waste)water flows in resin bed 11 through water cap 17.Water cap 17 is metal winding, and material is that 316L has stronger erosion resistance, and gap is that 0.2mm can effectively avoid resin leakage.Between the upper and lower ends of resin bed 11, be provided with the inductor block of pressure test device 40, in order to detect the pressure reduction of resin bed 11.Oily(waste)water flows out from oily(waste)water outlet 13 through the apical cap 18 of agglomerator 10.Wash-down water entrance 31 is arranged on agglomerator 10 upper ends, and wash-down water outlet 32 is arranged on agglomerator 10 lower ends, at wash-down water entrance 31 and wash-down water outlet 32, is respectively arranged with wash-down water switch 30.
Oily(waste)water outlet 13 communicates with the processing water inlet 21 of oily-water seperating equipment 20, processing water inlet 21 is arranged on the bottom of oily-water seperating equipment 20, oily-water seperating equipment 20 bottoms are also provided with processes water out 22, process water out 22 higher than processing water inlet 21, between is provided with the device of falling doline 23, the device of falling doline 23 is up-small and down-big, bottom surface steel ring 231 closely cooperates oily-water seperating equipment 20 is divided into upper and lower two portions with oily-water seperating equipment 20 walls, only with contraction mouth 233, communicate, top is disengaging zone 27.Process water out 22 and be positioned at bottom surface steel ring 231 tops, process water inlet 21 and be positioned at bottom surface steel ring 231 belows.The contraction mouth 233 of round table surface 232 ends is connected with oily-water seperating equipment 20 by the bracing frame 234 of outer.Oily-water seperating equipment 20 tops are provided with oil outlet 24 and pneumostome 25.
In top, the bottom of oil removal plant and position that resin bed 11 is set, be provided with inspection manhole 42 and observe visor 41.
During work, for utilizing oily buoyancy, oily(waste)water pumps into from bottom to top from oily(waste)water entrance 12, flow through and be fixed on the macromolecule resin in resin bed 11, the lipophilic group of macromolecule resin can attract the dispersed oil droplets in water, by the surface tension between oil and oleophilic resin, make oil aggegation on round resin particle form film.Along with oil continuous adsorption on resin, the thickness of film reaches threshold value.The difference of the impulse force of oily(waste)water current, profit density can be torn oil film from resin surface.The oil droplet disengaging, because density is less, enters apical cap 18 by resin bed 11 and top water cap 17, finally becomes and processes water from oily(waste)water outlet 13 outflows.According to material balance, agglomerator 10 moves under stable state, enters the oil mass of resin bed 11 and the oil mass balance of disengaging.
In order to protect the interior arrangement of agglomerator 10, must monitor the pressure reduction of resin bed 11, pressure test device 40 obtains pressure difference data by the inductor block being arranged between resin bed 11 upper and lower ends, when pressure reduction surpasses clean resin bed pressure reduction 0.35kg/cm
2when (5 pounds/square inch), just by pressure test device 40, report to the police.Flush switch 30 starts simultaneously, and wash-down water flows into from wash-down water entrance 31, from wash-down water outlet 32, flows out, and rinses from top to bottom; Current flow into from wash-down water outlet 32 afterwards, from wash-down water entrance 31, flow out, and carry out backwash, so alternately 10～30 minutes, can very soon pressure reduction be returned to normal value.Rinse frequency and determine with suspended impurity content in oily(waste)water, according to service experience, be about 7 to 40 days once.Rinse institute's water consumption and only account for 0.1～0.3% of processing water inventory.
Oily-water seperating equipment 20 is arranged on directly over agglomerator 10, process water and enter oily-water seperating equipment 20 bottoms from processing water inlet 21, because the device of falling doline is gone up greatly little 23 times, the in the situation that of whole constant flow, processing water flow velocity constantly accelerates from the bottom to top, thereby the whole liquid system to its below produces suction, is more conducive to take away the oil droplet of oil removing resin surface absorption.Process water and flow into disengaging zone 27 from contraction mouth 233, enter behind disengaging zone 27, process water flow velocity and reduce, water (flow) direction also changes, and because oil droplet density is little and size increases, oil droplet will be separated from process water.The processing water speed that enters disengaging zone 27 must be subject to the restriction of climbing speed in STOKE law, do not make these the oil droplet of increased in size from processing water out 22, flow out.Water in processing water is because density is larger, and it is 27 bottoms, disengaging zone that sedimentation is condensed in to round table surface 232 outsides, becomes condensed water.Disengaging zone 27 bottom condensed water are static substantially, along round table surface 232 inclined-planes, upwards gradually become dynamically, and the top that oil droplet is collected in disengaging zone 27 becomes assembly oil.Finally, assemble oil and derive from oil outlet 24, condensed water derives from processing water out 22.Assembling oil is pure oil substantially, and moisture content is no more than 0.5%.
The effect of pneumostome 25 is the air for remover apparatus top, the pressure equilibrium of conditioning equipment inside and outside.Oil outlet 24 is closing condition when flat, when assembling when oil reaches certain limit in oily-water seperating equipment 20, discharges.
The oil mass of collecting at oily-water seperating equipment 20 tops is the function of oily(waste)water oleaginousness, and as oily(waste)water oleaginousness 1mg/L, flow velocity is 100m
3/ h, maximum collection every day oil mass is 2.5L.Under normal circumstances, the oil mass that oily-water seperating equipment 20 reclaims is also little, as refinery heating unit leaks, will make a large amount of oil enter oily(waste)water, and at this moment oily(waste)water oleaginousness will reach 100mg/L, collect oily volume every day and will reach 0.25m
3.
Condensed water oleaginousness after processing generally can be lower than 1mg/L, if oleaginousness is less than 100mg/L when oily(waste)water flows into, condensed water oleaginousness and oily(waste)water oleaginousness are irrelevant.Average condensed water oleaginousness can maintain 0.3～0.5mg/L.
The following part of the present embodiment has been described a kind of deoiling method of applying above-mentioned oil removal plant and macromolecule resin:
Step 1, pumps into agglomerator by oil-containing water, at oil-containing water, passes through in the process of resin layer, the lipophilic group of resin layer is collected in oil molecule on resin surface, realize the breakdown of emulsion enrichment of grease, the droplet size of oily(waste)water is between 10～130 microns, and described resin surface is long-pending must reach maximum value;
Step 2, the aggegation of grease forms oily film, and oily film constantly accumulates, and when reaching the threshold value that impulsive force peels off, oily film departs from from the resin layer surface being fixedly installed, and forms larger oil droplet, realizes the aggegation of grease, and the size of larger oil droplet is greater than 150 microns;
Step 3, the processing water process agglomerator outlet with larger oil droplet, enters oily-water seperating equipment, controls the speed of current in oily-water seperating equipment, and larger oil droplet rises and forms oil reservoir, has realized oil removing.
Oil removing according to the method described above, not limited by oleaginousness and oil-containing kind, maximum oil content can reach 1000mg/L, contains the various operating modes such as steam condenses, petroleum chemical enterprise's recirculated water, trade effluent, oilfield sewage, oil removal rate is more than 99.0%, and oil recovery rate reaches 95%.Resin need to fill up resin bed substantially, and travelling speed is 5～8BV/h, when entering water temp≤120 ℃, and 5 to 10 years working times.
Embodiment 2:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1, and difference is the preparation method of structure and the macromolecule resin of oily-water seperating equipment.
As shown in Fig. 2,4,5, the processing water inlet 21 of oily-water seperating equipment 20 is connected with oily(waste)water outlet 13 by link pipeline 44, processing water inlet 21 is arranged on the middle and lower part of oily-water seperating equipment 20, process water inlet 21 pipe ends and be provided with water distributor 43, water distributor 43 belows are 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, inspection manhole 42 diameter 400mm, bottom is used 10 channel-section steels to make bracing frame and is fixed.On link pipeline 44, be provided with inlet pipe 45, process water out 22 and be arranged on below porous oil isolated from water plate 26 planes.
During work, process water and from water distributor 43, flow into oily-water seperating equipment 20 along link pipeline 44, before entering oily-water seperating equipment 20, by inlet pipe 45, to processing in water, pump into air, oil droplet is combined with air.Enter oily-water seperating equipment 20 aftertreatment water flow velocities and reduce, water (flow) direction also changes, and owing to combining the little and size of the oil droplet density of air, increases, and oil droplet will speed up from process water separated.Through the processing water speed of oily-water seperating equipment 20, must be subject to the restriction of climbing speed in STOKE law, do not make these the oil droplet of increased in size from processing water out 22, flow out, the condensed water of porous oil isolated from water plate below 26 is static substantially, on it, be that dynamically oil droplet is collected in the top of oily-water seperating equipment 20.Finally, assemble oil and derive from oil outlet 24, condensed water derives from processing water out 22.Assembling oil is pure oil substantially, and moisture content is no more than 0.5%.
This macromolecule resin is made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 4 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 8;
Step 2, is warming up to 60 ℃ by the product of step 1;
Step 3 adds octadecyl trimethyl ammonium chloride 60g in the product of step 2, is incubated 4 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 260mg/L, and water outlet oleaginousness is≤0.83mg/L.
Embodiment 3:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 5 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 8;
Step 2, is warming up to 70 ℃ by the product of step 1;
Step 3 adds octadecyl trimethyl ammonium chloride 70g in the product of step 2, is incubated 5 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin need to fill up resin bed substantially, and travelling speed is 6BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 280mg/L, and water outlet oleaginousness is≤0.76mg/L.
Embodiment 4:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 6 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 9;
Step 2, is warming up to 75 ℃ by the product of step 1;
Step 3 adds dodecyl dimethyl benzyl ammonium bromide 80g in the product of step 2, is incubated 6 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 260mg/L, and water outlet oleaginousness is≤0.73mg/L.
Embodiment 5:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 7 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 9;
Step 2, is warming up to 80 ℃ by the product of step 1;
Step 3 adds octadecyl trimethyl ammonium chloride 90g in the product of step 2, is incubated 7 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 260mg/L, and water outlet oleaginousness is≤0.63mg/L.
Embodiment 6:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 8 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 9;
Step 2, is warming up to 85 ℃ by the product of step 1;
Step 3 adds palmityl trimethyl ammonium chloride 50g in the product of step 2, and octadecyl trimethyl ammonium chloride 50g is incubated 8 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 6BV/h, and inflow temperature is 60 ℃, water inlet oil-containing 180mg/L, and water outlet oleaginousness is≤0.65mg/L.
Embodiment 7:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 9 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 10;
Step 2, is warming up to 90 ℃ by the product of step 1;
Step 3 adds dodecyl benzyl dimethyl ammonium chloride 50g, octadecyl trimethyl ammonium chloride 60g in the product of step 2, is incubated 3 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 260mg/L, and water outlet oleaginousness is≤0.72mg/L.
Embodiment 8:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 10 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 10;
Step 2, is warming up to 60 ℃ by the product of step 1;
Step 3 adds dodecyl benzyl dimethyl ammonium chloride 40g, dodecyl dimethyl benzyl ammonium bromide 80g in the product of step 2, is incubated 4 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 98%.Resin need to fill up resin bed substantially, and travelling speed is 7BV/h, and inflow temperature is 70 ℃, water inlet oil-containing 260mg/L, and water outlet oleaginousness is≤0.66mg/L.
Embodiment 9:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 11 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 10;
Step 2, is warming up to 65 ℃ by the product of step 1
Step 3 adds dodecyl dimethyl benzyl ammonium bromide 60g, cetylpyridinium chloride 70g in the product of step 2, is incubated 5 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 5BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 270mg/L, and water outlet oleaginousness is≤0.61mg/L.
Embodiment 10:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 12 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 11;
Step 2, is warming up to 70 ℃ by the product of step 1
Step 3 adds cetylpyridinium chloride 70g, palmityl trimethyl ammonium chloride 70g in the product of step 2, is incubated 6 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 98%.Resin need to fill up resin bed substantially, and travelling speed is 5BV/h, and inflow temperature is 25 ℃, water inlet oil-containing 268mg/L, and water outlet oleaginousness is≤0.53mg/L.
Embodiment 11:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 13 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 11;
Step 2, is warming up to 75 ℃ by the product of step 1
Step 3 adds octadecyl trimethyl ammonium chloride 80g, cetylpyridinium chloride 70g in the product of step 2, is incubated 7 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 98%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 60 ℃, water inlet oil-containing 180mg/L, and water outlet oleaginousness is≤0.43mg/L.
Embodiment 12:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 14 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 11;
Step 2, is warming up to 80 ℃ by the product of step 1
Step 3 adds dodecyl dimethyl benzyl ammonium bromide 60g, dodecyl benzyl dimethyl ammonium chloride 50g, cetylpyridinium chloride 50g in the product of step 2, is incubated 8 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 97%.Resin need to fill up resin bed substantially, and travelling speed is 6BV/h, and inflow temperature is 50 ℃, water inlet oil-containing 230mg/L, and water outlet oleaginousness is≤0.58mg/L.
Embodiment 13:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 7 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 12;
Step 2, is warming up to 85 ℃ by the product of step 1
Step 3 adds dodecyl dimethyl benzyl ammonium bromide 60g in the product of step 2, and cetylpyridinium chloride 50g, palmityl trimethyl ammonium chloride 70g are incubated 3 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96.8%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 60 ℃, water inlet oil-containing 300mg/L, and water outlet oleaginousness is≤0.72mg/L.
Embodiment 14:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 8 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 12;
Step 2, is warming up to 90 ℃ by the product of step 1
Step 3 adds octadecyl trimethyl ammonium chloride 60g, cetylpyridinium chloride 70g, palmityl trimethyl ammonium chloride 60g in the product of step 2, is incubated 4 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 98%.Resin need to fill up resin bed substantially, and travelling speed is 6BV/h, and inflow temperature is 60 ℃, water inlet oil-containing 260mg/L, and water outlet oleaginousness is≤0.53mg/L.
Embodiment 15:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 9 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 12;
Step 2, is warming up to 60 ℃ by the product of step 1
Step 3 adds dodecyl benzyl dimethyl ammonium chloride 50g in the product of step 2, and palmityl trimethyl ammonium chloride 80g, octadecyl trimethyl ammonium chloride 70g are incubated 5 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96.3%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 280mg/L, and water outlet oleaginousness is≤0.61mg/L.
Embodiment 16:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 10 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 13;
Step 2, is warming up to 65 ℃ by the product of step 1
Step 3 adds dodecyl dimethyl benzyl ammonium bromide 40g in the product of step 2, octadecyl trimethyl ammonium chloride 110g, dodecyl benzyl dimethyl ammonium chloride 60g, insulation 6 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 100mg/L, and water outlet oleaginousness is≤0.45mg/L.
Embodiment 17:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 11 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 13;
Step 2, is warming up to 70 ℃ by the product of step 1
Step 3 adds palmityl trimethyl ammonium chloride 40g, octadecyl trimethyl ammonium chloride 80g, dodecyl benzyl dimethyl ammonium chloride 70g, dodecyl dimethyl benzyl ammonium bromide 30g in the product of step 2, is incubated 7 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 98%.Resin need to fill up resin bed substantially, and travelling speed is 5BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 200mg/L, and water outlet oleaginousness is≤0.66mg/L.
Embodiment 18:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 12 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 13;
Step 2, is warming up to 75 ℃ by the product of step 1
Step 3 adds octadecyl trimethyl ammonium chloride 60g, dodecyl benzyl dimethyl ammonium chloride 70g, dodecyl dimethyl benzyl ammonium bromide 40g, cetylpyridinium chloride 60g in the product of step 2, is incubated 8 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 60 ℃, water inlet oil-containing 100mg/L, and water outlet oleaginousness is≤0.43mg/L.
Embodiment 19:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 13 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 14;
Step 2, is warming up to 80 ℃ by the product of step 1
Step 3 adds palmityl trimethyl ammonium chloride 70g, octadecyl trimethyl ammonium chloride 65g, dodecyl benzyl dimethyl ammonium chloride 85g, cetylpyridinium chloride 20g in the product of step 2, is incubated 3 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 97%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 20 ℃, water inlet oil-containing 160mg/L, and water outlet oleaginousness is≤0.60mg/L.
Embodiment 20:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 14 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 14;
Step 2, is warming up to 65 ℃ by the product of step 1
Step 3, in the product of step 2, add palmityl trimethyl ammonium chloride 30g, octadecyl trimethyl ammonium chloride 75g, dodecyl benzyl dimethyl ammonium chloride 40g, dodecyl dimethyl benzyl ammonium bromide 50g, cetylpyridinium chloride 55g, be incubated 5 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin need to fill up resin bed substantially, and travelling speed is 6BV/h, and inflow temperature is 60 ℃, water inlet oil-containing 250mg/L, and water outlet oleaginousness is≤0.60mg/L.
Embodiment 21:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 4 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 10;
Step 2, is warming up to 60 ℃ by the product of step 1;
Step 3 adds octadecyl trimethyl ammonium chloride 100g in the product of step 2, is incubated 4 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 60 ℃, water inlet oil-containing 150mg/L, and water outlet oleaginousness is≤0.46mg/L.
Embodiment 22:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 5 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 12;
Step 2, is warming up to 70 ℃ by the product of step 1;
Step 3 adds octadecyl trimethyl ammonium chloride 120g in the product of step 2, is incubated 5 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 260mg/L, and water outlet oleaginousness is≤0.53mg/L.
Embodiment 23:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 6 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 11;
Step 2, is warming up to 75 ℃ by the product of step 1;
Step 3 adds dodecyl dimethyl benzyl ammonium bromide 120g in the product of step 2, is incubated 6 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 360mg/L, and water outlet oleaginousness is≤0.83mg/L.
Embodiment 24:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 7 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 10;
Step 2, is warming up to 80 ℃ by the product of step 1;
Step 3 adds octadecyl trimethyl ammonium chloride 130g in the product of step 2, is incubated 7 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 230mg/L, and water outlet oleaginousness is≤0.73mg/L.
Embodiment 25:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 8 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 12;
Step 2, is warming up to 85 ℃ by the product of step 1;
Step 3 adds palmityl trimethyl ammonium chloride 50g in the product of step 2, and octadecyl trimethyl ammonium chloride 80g is incubated 8 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 230mg/L, and water outlet oleaginousness is≤0.81mg/L.
Embodiment 26:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 9 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 11;
Step 2, is warming up to 90 ℃ by the product of step 1;
Step 3 adds dodecyl benzyl dimethyl ammonium chloride 70g, octadecyl trimethyl ammonium chloride 90g in the product of step 2, is incubated 3 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96.5%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 240mg/L, and water outlet oleaginousness is≤0.66mg/L.
Embodiment 27:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 10 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 11;
Step 2, is warming up to 60 ℃ by the product of step 1;
Step 3 adds dodecyl benzyl dimethyl ammonium chloride 90g, dodecyl dimethyl benzyl ammonium bromide 80g in the product of step 2, is incubated 4 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 97%.Resin need to fill up resin bed substantially, and travelling speed is 7BV/h, and inflow temperature is 40 ℃, water inlet oil-containing 100mg/L, and water outlet oleaginousness is≤0.31mg/L.
Embodiment 28:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 11 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 10;
Step 2, is warming up to 65 ℃ by the product of step 1
Step 3 adds dodecyl dimethyl benzyl ammonium bromide 100g, cetylpyridinium chloride 70g in the product of step 2, is incubated 5 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 97%.Resin need to fill up resin bed substantially, and travelling speed is 9BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 280mg/L, and water outlet oleaginousness is≤0.83mg/L.
Embodiment 29:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 12 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 11;
Step 2, is warming up to 70 ℃ by the product of step 1
Step 3 adds cetylpyridinium chloride 80g, palmityl trimethyl ammonium chloride 110g in the product of step 2, is incubated 6 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 6BV/h, and inflow temperature is 80 ℃, water inlet oil-containing 200mg/L, and water outlet oleaginousness is≤0.57mg/L.
Embodiment 30:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 13 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 12;
Step 2, is warming up to 75 ℃ by the product of step 1
Step 3 adds octadecyl trimethyl ammonium chloride 80g, cetylpyridinium chloride 120g in the product of step 2, is incubated 7 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 98%.Resin need to fill up resin bed substantially, and travelling speed is 6BV/h, and inflow temperature is 60 ℃, water inlet oil-containing 200mg/L, and water outlet oleaginousness is≤0.63mg/L.
Embodiment 31:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 3 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 8;
Step 2, is warming up to 60 ℃ by the product of step 1;
Step 3 adds octadecyl trimethyl ammonium chloride 80g in the product of step 2, is incubated 7 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 25 ℃, water inlet oil-containing 260mg/L, and water outlet oleaginousness is≤0.73mg/L.
Embodiment 32:
The oil removal plant that the present embodiment is used and deoiling method are identical with embodiment 1 or embodiment 2, and difference is that macromolecule resin made by following methods:
The cross-linking type polystyrene gel-type strongly acidic cation exchange resin that step 1 is 3 by 10kg degree of crosslinking mixes with 10kg water, with sodium hydroxide, regulates pH to 9;
Step 2, is warming up to 90 ℃ by the product of step 1;
Step 3 adds dodecyl benzyl dimethyl ammonium chloride 90g, octadecyl trimethyl ammonium chloride 70g in the product of step 2, is incubated 8 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin.
Oil removing according to the method described above, is not limited by oleaginousness and oil-containing kind, and maximum oil content can reach 1000mg/L, and oil removal rate is more than 99.5%, and oil recovery rate reaches 96%.Resin need to fill up resin bed substantially, and travelling speed is 8BV/h, and inflow temperature is 40 ℃, water inlet oil-containing 360mg/L, and water outlet oleaginousness is≤0.33mg/L.
In addition, it should be noted that, the specific embodiment described in this specification sheets, the shape of its parts and components, institute's title of being named etc. can be different.All equivalence or simple change of doing according to described structure, feature and the principle of patent design of the present invention, are included in the protection domain of patent of the present invention.Those skilled in the art can make various modifications or supplement or adopt similar mode to substitute described specific embodiment; only otherwise depart from structure of the present invention or surmount this scope as defined in the claims, all should belong to protection scope of the present invention.
Claims (10)
1. a macromolecule resin, is characterized in that, by following methods, is made:
Step 1, mixes matrix polymer with water, with sodium hydroxide, regulate pH to 8～14;
Step 2, is warming up to 60 ℃～90 ℃ by the product of step 1;
Step 3 adds modifying agent in the product of step 2, and the mass ratio of modifying agent, matrix polymer and water is 0.05～0.25:1:1, is incubated 3 hours～8 hours;
Step 4, by product washing, the discharging of step 3, the end product that collection granularity is 0.3mm～1.25mm, obtains macromolecule resin;
Described matrix polymer is cross-linking type polystyrene gel-type strongly acidic cation exchange resin;
Described modifying agent is quaternary ammonium salt cationic surfactant.
2. macromolecule resin according to claim 1, is characterized in that, the degree of crosslinking of described cross-linking type polystyrene gel-type strongly acidic cation exchange resin is 3～14.
3. macromolecule resin according to claim 1, it is characterized in that, described quaternary ammonium salt cationic surfactant is one or more in palmityl trimethyl ammonium chloride, octadecyl trimethyl ammonium chloride, dodecyl benzyl dimethyl ammonium chloride, dodecyl dimethyl benzyl ammonium bromide and cetylpyridinium chloride.
4. use an oil removal plant for above-mentioned macromolecule resin, it is characterized in that, include agglomerator, oily-water seperating equipment,
In described agglomerator, be provided with resin bed, in described resin bed, be provided with pressure test device and flushing arrangement, described pressure test device is connected with bottom with the top layer of described resin bed, the wash-down water entrance of described flushing arrangement is arranged on described resin bed upper end, the wash-down water outlet of described flushing arrangement is arranged on described resin bed lower end, and the pressure reduction that described flushing arrangement records at described pressure test device surpasses clean resin bed pressure reduction 0.35kg/cm
2shi Qidong; Described agglomerator bottom is provided with oily(waste)water entrance, and described agglomerator top is provided with oily(waste)water outlet;
Described oily(waste)water outlet communicates with the processing water inlet of described oily-water seperating equipment, described processing water inlet is arranged on the bottom of described oily-water seperating equipment, described oily-water seperating equipment bottom is also provided with processing water out, and described oily-water seperating equipment top is provided with and overflows hydraulic fluid port and pneumostome.
5. oil removal plant according to claim 4, is characterized in that, described processing water inlet, higher than described processing water out, is provided with porous oil isolated from water plate between processing water inlet and processing water out.
6. oil removal plant according to claim 5, is characterized in that, described processing water inlet end is also provided with water distributor, connects on the pipeline of described processing water inlet and described water distributor and is provided with air intake structure.
7. oil removal plant according to claim 4, is characterized in that, in described oily-water seperating equipment, is provided with the device of falling doline.
8. utilize the method that described in macromolecule resin and claim 6, oil removal plant carries out oil removing described in claim 1, it is characterized in that, step is:
Step 1, oily(waste)water pumps into from bottom to top from described oily(waste)water entrance, flow through and be fixed on the macromolecule resin in described resin bed, by the surface tension effects between grease and described macromolecule resin, make grease aggegation on described macromolecule resin form film, realize the breakdown of emulsion enrichment of grease, the droplet size of described oily(waste)water is between 10～130 microns, and described resin surface is long-pending must reach maximum value;
Step 2, along with grease continuous adsorption on macromolecule resin, the thickness of described film reaches threshold value, the difference of the impulse force of oily(waste)water current, profit density can be torn film from macromolecule resin surface, by the apical cap of agglomerator described in described resin bed, realize the aggegation of grease, and then become processing water from oily(waste)water outlet outflow, described agglomerator moves under stable state, enter the oil mass of described resin bed oily(waste)water and the oil mass balance of the processing water disengaging, the pressure reduction recording when described pressure test device surpasses clean resin bed pressure reduction 0.35kg/cm
2shi Suoshu flushing arrangement starts;
Step 3, described processing water enters described water distributor through described processing water inlet after pumping into air, and then flow into described oily-water seperating equipment bottom from described water distributor, described processing water flow velocity must be subject to the restriction of climbing speed in STOKE law, larger oil droplet is gathered on described oily-water seperating equipment top assembles oil, from described oil outlet, derives; Through becoming condensed water except oil handling water after described porous oil isolated from water plate, from described processing water out, derive.
9. deoiling method according to claim 8, is characterized in that, when described oily(waste)water ingress oily(waste)water oleaginousness is 1mg/L, flow velocity is 100m
3/ h.
10. deoiling method according to claim 8, is characterized in that, in described step 2, the size of larger oil droplet is greater than 150 microns.
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| 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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| CN104086679B (en) | 2017-07-21 |
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