CN203820559U - Device for solid removal and oil removal of quenching water and washing water in process of producing olefins from methanol - Google Patents
Device for solid removal and oil removal of quenching water and washing water in process of producing olefins from methanol Download PDFInfo
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- CN203820559U CN203820559U CN201420208889.8U CN201420208889U CN203820559U CN 203820559 U CN203820559 U CN 203820559U CN 201420208889 U CN201420208889 U CN 201420208889U CN 203820559 U CN203820559 U CN 203820559U
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Abstract
The utility model relates to a device for solid removal and oil removal of quenching water and washing water in a process of producing olefins from methanol. The device comprises a quenching water tower and a washing water tower, wherein the bottom of the quenching water tower is connected with an inlet of a first ultrafiltration membrane component, the permeation side of the first ultrafiltration membrane component is connected with a quenching water inlet of the quenching water tower, the interception side of the first ultrafiltration membrane component is connected to a first three-phase cyclone separator, an oil phase outlet is formed at the top of the first three-phase cyclone separator, a catalyst outlet is formed at the side part of the first three-phase cyclone separator, a water outlet is formed at the bottom of the first three-phase cyclone separator, and the bottom is connected to the inlet of the first ultrafiltration membrane component; the bottom of the washing water tower is connected with the inlet of a second ultrafiltration membrane component, the permeation side of the second ultrafiltration membrane component is connected to a washing water inlet of the washing water tower, the interception side of the second ultrafiltration membrane component is connected to a second three-phase cyclone separator, an oil phase outlet is formed at the top of the second three-phase cyclone separator, a catalyst outlet is formed at the side part of the second three-phase cyclone separator, a water outlet is formed at the bottom of the second three-phase cyclone separator, and the bottom is connected to the inlet of the second ultrafiltration membrane component.
Description
Technical field
The utility model relates to quenched water and the de-device of oil removing admittedly of washing water in a kind of MTO technology, relate in particular to a kind of art breading MTO/MTP quenched water and washing water that adopts membrane sepn and the integrated coupling of three-phase cyclone separator, and reach the device of the object of internal system water cycle, belong to process water treatment and reuse field in Coal Chemical Industry process.
Background technology
MTO/MTP be take methyl alcohol as raw material, by the fluidized-bed reaction form of similar catalytic cracking unit, produces the Chemical Engineering Technology of low-carbon alkene.This technique mainly comprises that reactive moieties (reactor and revivifier), product purify part (quench tower, water wash column, soda-wash tower and drying tower) and product separation part.
US6166282 discloses a kind of MTO fluidized-bed reactor, in reactor head, one group of cyclonic separator is installed.US0234281 and CN1942558A disclose a kind of one or more solid-liquid cyclonic separators or hydrocyclone recycle catalyzer that adopts a set of serial or parallel connection combined running.CN200810042662.X discloses a kind of micro-cyclone concentrating method and device of removing trickle catalyzer in quenched water, washing water.All there is the shortcomings such as separation accuracy is low, catalyst recovery is thorough, function singleness in above utility model.CN101962235A discloses the wastewater treatment of a kind of MTO process high-temperature and reuse method, this utility model has been reported tune alkali, aeration, filter, micro-filtration or ultrafiltration membrane system, high temperature reverse osmosis system is processed the method for a small amount of high-temperature technology waste water of discharging at the bottom of stripping tower reactor, methyl alcohol in main removal waste water, dme, acetic acid, propionic acid etc., but in processing MTO technique a large amount of quenched waters and water coolant reclaim catalyzer and oily aspect do not study and report, and the method complex process, reagent consumption is large, when temperature is high, there is methyl alcohol, dme, acetic acid, propionic acid volatilization.
In MTO/MTP reaction process, except object product low-carbon alkene, the by product such as a large amount of water vapors, mixed alkanes, aromatic hydrocarbon, coke also, when catalyzer and by product coexist in quench tower and water wash column, catalyzer plays bridging action and forms large particulate matter, and pore is stopped up in wearing and tearing; Quenched water and washing water are unprocessed, and recycle meeting causes catalyzer enrichment in reactor; Quenched water and washing water are unprocessed, and directly discharge causes water treatment system paralysis; Enter in water wash column, after heat exchange, temperature reduces, and oily matter is separated out, and stops up pore.Adopt ultrafiltration/three-phase cyclone separator integrated technique to process MTO/MTP quenched water and washing water, can effectively remove catalyzer and by product, reach the object of internal system water cycle.
Utility model content
The utility model, for the problem existing in quenched water in MTO technology (MTO/MTP) and washing water treating processes, proposes method and the device of the de-solid oil removing of a kind of new MTO/MTP quenched water and washing water.Concrete technical scheme is:
The method of the de-solid oil removing of quenched water and washing water in MTO technology, comprise the steps: that the process water in MTO technology is sent into ultra-filtration membrane to be concentrated, concentrated solution enters three-phase cyclone separator and carries out separation, top discharge is refiltered oil, sidepiece discharging is catalyzer, and bottom discharge is back to the entrance of ultra-filtration membrane; Described process water refers to quenched water or washing water.
Methanol-to-olefins described in the utility model is to put forward MTO (Methanol ethene) or MTP (preparing propylene from methanol) technique.
In above-mentioned steps, the filtrate of ultra-filtration membrane is back to carries out reuse in process water.
In above-mentioned steps, the transmembrane pressure of ultrafiltration is 0.2～0.6MPa preferably, more preferably 0.3～0.4MPa.
In above-mentioned steps, the crossflow velocity of ultrafiltration is preferably 0.5～6m/s, more preferably 3～4m/s.
In above-mentioned steps, the mean pore size of ultrafiltration is preferably 5～200nm, more preferably 20～50nm.
In above-mentioned steps, described process water is quenched water, preferably 80～130 ℃ of the temperature of ultrafiltration, more preferably 90～120 ℃; Cycles of concentration is preferably 5～50 times, more preferably 10～20 times.
In above-mentioned steps, described process water is washing water, 30～60 ℃ of the temperature of ultrafiltration; Preferably concentrated 5～50 times.
In above-mentioned steps, the kickback pressure in ultrafiltration step is 0.4～1.0MPa preferably, and optimum is 0.6～0.8MPa; The recoil cycle is 20～120min preferably, and optimum is 45～60min; The recoil time is 3～10s preferably, and optimum is 5～8s.
In above-mentioned steps, three-phase cyclone separator pressure drop is preferably 0.1～0.25Mpa, and optimum is 0.15～0.2MPa; Excellent 1～the 6m/s of being falls in inlet velocity, and optimum is 3～5m/s.
In above-mentioned step, concentrated solution enters to microfiltration membrane and again concentrates, and obtains micro-filtration concentrated solution, then micro-filtration concentrated solution is delivered to three-phase cyclone separator and carry out separation.
Another object of the present utility model has been to provide the device of the de-solid oil removing of process water in a kind of MTO technology, include quenching water column, washing water tower, the bottom of quenching water column is connected with the import of the first hyperfiltration membrane assembly, the per-meate side of the first hyperfiltration membrane assembly is connected to the quenched water ingress of quenching water column, the side of holding back of the first hyperfiltration membrane assembly is connected to the first three-phase cyclone separator connection, the top of the first three-phase cyclone separator is that oil phase outlet, sidepiece are that catalyst outlet, bottom are water outs, and bottom is connected to the import of the first hyperfiltration membrane assembly; The bottom of washing water tower is connected with the import of the second hyperfiltration membrane assembly, the per-meate side of the second hyperfiltration membrane assembly is connected to the washing water ingress of washing water tower, the side of holding back of the second hyperfiltration membrane assembly is connected to the second three-phase cyclone separator connection, the top of the second three-phase cyclone separator is that oil phase outlet, sidepiece are that catalyst outlet, bottom are water outs, and bottom is connected to the import of the second hyperfiltration membrane assembly.
Improvement as said apparatus, the side of holding back of the first hyperfiltration membrane assembly is connected in the first micro-filtration membrane module, the side of holding back of the first micro-filtration membrane module is connected with the first three-phase cyclone separator, and the per-meate side of the first micro-filtration membrane module is connected in the ingress of the first hyperfiltration membrane assembly; The side of holding back of the second hyperfiltration membrane assembly is connected in the second micro-filtration membrane module, and the side of holding back of the second micro-filtration membrane module is connected with the second three-phase cyclone separator, and the per-meate side of the second micro-filtration membrane module is connected in the ingress of the second hyperfiltration membrane assembly.
Beneficial effect
1. adopt ultra-filtration membrane from MTO/MTP quenched water and washing water catalyst concentration, three-phase cyclone separator reclaims catalyzer, and rate of recovery >98%, has significant economic benefit.
2. adopt ultra-filtration membrane from MTO/MTP quenched water and the concentrated oily matter of washing water, three-phase cyclone separator refiltered oil, oil recovery rate >95%, has significant economic benefit.
3. the method can be stopped catalyzer enrichment in quench tower and water wash column, reduces catalyst bridging and forms macrobead probability, reduces pore plugging rate, increases the equipment cycle of operation, reduces equipment maintenance cost, greatly improves stabilization of equipment performance and continuous production.
4. reduce oily matter in heat exchanger surface enrichment, improve heat exchange efficiency, reduce energy consumption.
5. adopt tubular ultra-filtration membrane, have that film is stable, film long service life (3～10 years), film replacement charge is low, film cleaning charge is low, quality product is excellent and the advantage such as stable.
6. adopt the de-solid oil removing from a large amount of quenched waters and washing water of ultra-filtration membrane/three-phase cyclone separator, water can direct reuse in quenched water and washing water system, reduce circulation amount of makeup water, there is good economic benefit, social benefit.
7. after treatment, in water body, catalyzer and oil-contg reduce greatly for quenched water and washing water, can effectively prevent after directly discharge follow-up water treatment system paralysis.
8. adopt totally-enclosed system, water treatment system is used the pressure of reactor own, and energy consumption reduces greatly; Without regulating pH, reagent consumption is little; Adopt ultra-filtration membrane infiltration to survey the mode of back pressure, range of application is wider, and temperature is 80～130 ℃.
9. Gu to realize oil-water-three-phase simultaneously separated for three-phase cyclone separator, to compare with desanding formula swirler with common oil removing, three-phase cyclone utensil has that volume is little, efficiency is high, investment and the feature such as process cost is lower.
10. adopt microfiltration membrane further concentrated, greatly improve the water rate of recovery, water rate of recovery >90%.
Accompanying drawing explanation
Fig. 1 is the de-schema of oil removal plant admittedly that the utility model provides.
Fig. 2 is the schema of another kind of improved de-solid oil removal plant.
Wherein, 1, reactor; 2, quench tower; 3, water wash column; 4-1, the first ultra-filtration membrane fresh feed pump; 4-2, the second ultra-filtration membrane fresh feed pump; 5-1, the first hyperfiltration membrane assembly; 5-2, the second hyperfiltration membrane assembly; 6-1, the first three-phase cyclone separator; 6-2, the second three-phase cyclone separator; 7-1, First Heat Exchanger; 7-2, the second interchanger; 8-1, the first topping-up pump; 8-2, the second topping-up pump; 9-1, the first micro-filtration membrane module; 9-2, the second micro-filtration membrane module.
Embodiment
In the related MTO technology of the utility model, the method for the de-solid oil removing of process water is mainly that the process water in this technological process mainly refers to quenched water and washing water for MTO (Methanol ethene) or MTP (preparing propylene from methanol) technique.Quenched water temperature is generally 80～130 ℃, and catalyst content is 50～5000mg/L, oil-contg 50～500mg/L; Washing water temperature is generally 30～80 ℃, and catalyst content is 50～500mg/L, oil-contg 1000～10000mg/L.
As shown in Figure 1, the utility model relates to device and flow process.Methyl alcohol enters reactor 1, and under the effect of catalyzer, reaction generates product and by product.Product and by product are carried partially catalyzed agent secretly with gas form and are entered quench tower 2, and in quench tower 2, most of catalyzer enters water.Quench tower 2 bottoms water is out under the promotion of the first ultra-filtration membrane fresh feed pump 4-1, enter the first hyperfiltration membrane assembly 5-1, ultra-filtration membrane concentrated solution enters the first three-phase cyclone separator 6-1, the first three-phase cyclone separator 6-1 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, bottom discharge returns the first ultra-filtration membrane fresh feed pump 4-1 and advances into ceramic membrane system, after the quenched water that discharge ultra-filtration membrane clear liquid and quench tower 2 middle and upper parts merges, enter First Heat Exchanger 7-1, the quenched water after heat exchange is transmitted back to quench tower 2 by the first topping-up pump 8-1.Quench tower 2 top gas enter water wash column 3, water body tower 3 bottoms water is out under the promotion of the second ultra-filtration membrane fresh feed pump 4-2, enter the second ultra-filtration membrane membrane element 5-2, ultra-filtration membrane concentrated solution enters the second three-phase cyclone separator 6-2, top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, bottom discharge returns the second ultra-filtration membrane fresh feed pump 4-2 and advances into ceramic membrane system, after the quenched water that discharge ultra-filtration membrane clear liquid and water wash column 3 middle and upper parts merges, enter the second interchanger 7-2, the washing water after heat exchange is transmitted back to water wash column 3 by the second topping-up pump 8-2.
Know-why of the present utility model is as follows: owing to being to contain a certain amount of catalyzer in quenched water and washing water, if after being sent into Waste Water Treatment, can cause the waste of catalyzer, first after concentrating by ultra-filtration membrane, can obtain comparatively pure ultrafiltration and see through liquid, and catalyzer, oil etc. all can reside in the concentrated solution of ultrafiltration, again further by three-phase cyclone separator to oil, catalyzer carries out separation, in three-phase cyclone separator, top is isolated oily matter, sidepiece is isolated catalyzer, and bottom is for containing a certain amount of catalyzer, the water of grease, the water of these bottoms can be back to again and in ultrafiltration membrance filter system, carry out reuse.
Quenched water and washing water are being carried out in ultra-filtration process, if the transmembrane pressure of ultrafiltration is excessive, can cause oily matter to be squeezed through ultra-filtration membrane, and can easily cause more serious film surface pollution; If the transmembrane pressure of ultrafiltration is too small, can cause cycles of concentration to improve, under low cycles of concentration, three-phase cyclone separator is cannot be preferably separated by catalyzer, water, oily matter, has caused that separation efficiency is low, the rate of recovery is low.Transmembrane pressure is preferably 0.2～0.6MPa, more preferably 0.3～0.4MPa.。Because the pressure and temperature of quenched water can be higher, in order to maintain transmembrane pressure in rational scope, can be in the back pressure side pressurization of ultra-filtration membrane, to control transmembrane pressure.
If the crossflow velocity in ultra-filtration process is excessive, can cause face cannot form good cake layer, these cake layers can play the effect of holding back further oily matter, can cause oily matter to see through ultra-filtration membrane; If crossflow velocity is too small, can cause the flux of ultrafiltration too small, cycles of concentration cannot be improved further, make the water-content in concentrated solution too high, and then cause the separation efficiency of three-phase cyclone separator low, inferior separating effect.Crossflow velocity is preferably 0.5～6m/s, more preferably 3～4m/s.
If the mean pore size of the ultra-filtration membrane using is too small, can cause that permeation flux is low, cannot to meet engineering required, make cycles of concentration low, make the Efficiency Decreasing in three-phase cyclone separation; If mean pore size is excessive, can cause having more oily matter and catalyzer to see through rete, the rate of recovery of oil and catalyzer is incurred loss.Mean pore size is preferably 5～200nm, more preferably 20～50nm.
In ultra-filtration process, if excess Temperature can cause the solvability of oily matter in water and dispersed raising, the rejection of ultra-filtration membrane is declined, and easily destroy the external phase of the water forming in fenestra, make oil enter per-meate side; If temperature is too low, can cause the viscosity of feed liquid too low, and then can make filtration flux on the low side, make cycles of concentration less than normal.In ultrafiltration for quenched water, filtration temperature is 80～130 ℃, more preferably 90～120 ℃; In ultrafiltration for washing water, filtration temperature is preferably 30～60 ℃.
For preferably concentrating 5～50 times in the ultrafiltration of quenched water, more preferably 10～20 times.For preferably concentrating 5～50 times in the ultrafiltration of washing water.
In the process of ultrafiltration, can carry out recoil measure, for decelerating membrane pollution and recover flux.For example, if backwashing strength too high (: kickback pressure is too high, the recoil cycle is too short or recoil time length), can cause film surface cannot form stable cake layer, make oily rejection on the low side.If backwashing strength is too small, can causes that filtration flux is little, cycles of concentration is little, and then make the efficiency of three-phase cyclone separation not high.Kickback pressure is 0.4～1.0MPa preferably, and optimum is 0.6～0.8MPa; The recoil cycle is 20～120min preferably, and optimum is 45～60min; The recoil time is 3～10s preferably, and optimum is 5～8s.
In three-phase cyclone separator, the concentrated solution of membrane sepn is to enter from the side separator, the top of separator can make oil obtain separation, on the sidewall on the other hand of separator, can isolate catalyzer, and in bottom, be water, in water, still containing some oil and catalyzer, the entrance that therefore need to send into ultra-filtration membrane carries out reuse.Three-phase cyclone separator pressure drop is preferably 0.1～0.25Mpa, and optimum is 0.15～0.2MPa; Inlet velocity is preferably 1～6m/s, and optimum is 3～5m/s.
Improvement as such scheme, device as shown in Figure 2, be the import that side is connected in the first micro-filtration membrane module (9-1) of holding back of the first hyperfiltration membrane assembly (5-1) with the difference of Fig. 1, the side of holding back of the first microfiltration membrane is connected with the first three-phase cyclone separator (6-1), and the per-meate side of the first micro-filtration membrane module (9-1) is connected with the import of the first hyperfiltration membrane assembly (5-1) again; The second hyperfiltration membrane assembly (5-1) hold back the import that side is connected in the second micro-filtration membrane module (9-1), the side of holding back of the second microfiltration membrane is connected with the second three-phase cyclone separator (6-1), and the per-meate side of the second micro-filtration membrane module (9-1) is connected with the import of the second hyperfiltration membrane assembly (5-1) again.After needing in this improvement technique that the concentrated solution of ultra-filtration membrane is carried out to micro-filtration, then the concentrated solution of micro-filtration is sent into three-phase cyclone separator and carry out separation.Because the rejection of ultra-filtration membrane is higher, in its concentrated solution, also include the impurity such as a certain amount of paraffin, these impurity can make separation efficiency not high in being introduced into three-phase cyclone separator, the grease of some and catalyzer can reside in the bottom from cyclone separator in concentrated solution and flow out, and make the rate of recovery can not get improving.Because the aperture of microfiltration membrane is greater than ultra-filtration membrane, it has lower working pressure, and can see through a part of feed liquid, the cycles of concentration of concentrated solution is improved further, and exclude a part of impurity, the concentrated solution of micro-filtration is carried out to three-phase cyclone when separated, with respect to direct, with ultrafiltration and concentration liquid, can make oil that separation obtains and the rate of recovery of catalyzer be improved.The mean pore size of preferred microfiltration membrane is 200nm～500nm; The transmembrane pressure of micro-filtration is 0.05MPa～0.3MPa, and crossflow velocity is 4～5m/s.
In following examples, adopt above-mentioned device and device to take off solid oil removal treatment to the process water in MTO technology, wherein need to investigate the rate of recovery of oil recovery rate, catalyzer and the rate of recovery of water, oil recovery rate refers to the oily weight that obtains in three-phase cyclone separator and the ratio of the oily weight in process water, the rate of recovery of catalyzer is the ratio of the weight of catalyzer in the weight of the catalyzer that obtains in three-phase cyclone separator and process water, and the rate of recovery of water is the ratio of ultra-filtration membrane penetrating fluid and feeding liquid volume.
Embodiment 1
Device flow process as shown in Figure 1, methyl alcohol enters reactor 1, and under the effect of catalyzer, reaction generates product and by product.Product and by product are carried partially catalyzed agent secretly with gas form and are entered quench tower 2, and quench tower 2 bottoms quenched water water quality is out 115 ℃ of temperature, catalyst content 189mg/L, oil-contg 510mg/L.Under the promotion of the first ultra-filtration membrane fresh feed pump 4-1, enter the first hyperfiltration membrane assembly 5-1, the inner ultra-filtration membrane of installing is oxidation titanium film, ultra-filtration membrane is worked under different pressures condition, also can add back pressure and form transmembrane pressure, crossflow velocity 5m/s, aperture 5nm simultaneously, 87 ℃ of temperature, per-meate side back pressure 0.2MPa; Recoil condition is 0.8MPa, recoil cycle 45min, recoil time 6s.Titanium oxide ultra-filtration membrane concentrated solution enters the first three-phase cyclone separator 6-1, pressure drop is 0.15Mpa, inlet velocity is 3m/s, the first three-phase cyclone separator 6-1 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, bottom discharge returns the first ultra-filtration membrane fresh feed pump 4-1 and advances into the first hyperfiltration membrane assembly, after the quenched water that discharge ultra-filtration membrane clear liquid and quench tower 2 middle and upper parts merges, enters First Heat Exchanger 7-1, and the quenched water after heat exchange is transmitted back to quench tower 2 by the first topping-up pump 8-1.Oil recovery rate under different transmembrane pressure conditions, catalyst recovery yield are as shown in table 1-1.
Oil recovery rate, catalyst recovery yield under the different transmembrane pressure conditions of table 1-1
| Transmembrane pressure MPa | 0.05 | 0.1 | 0.3 | 0.5 |
| Cycles of concentration | 9 | 14 | 20 | 25 |
| Oil recovery rate % | 72.6 | 84.3 | 88.6 | 82.7 |
| Catalyst recovery yield % | 86.4 | 88.2 | 94.6 | 93.5 |
| Water rate of recovery % | 92 | 91 | 93 | 91 |
As can be seen from the table, when transmembrane pressure is less than normal, cycles of concentration can not be improved, and concentrated solution can not obtain separated preferably in three-phase cyclone separator, makes the rate of recovery of oil and catalyzer less than normal.When if transmembrane pressure is excessive, can cause ultra-filtration membrane to decline to oily rejection, the whole rate of recovery is also reduced.
Quench tower 2 top gas enter water wash column 3,115 ℃ of water wash column 3 bottoms washing water temperature out, catalyst content 189mg/L, oil-contg 5200mg/L.Under the promotion of the second ultra-filtration membrane fresh feed pump 4-2, enter the second hyperfiltration membrane assembly 5-2, material is titanium oxide, ultra-filtration membrane is worked under different transmembrane pressures, crossflow velocity 5m/s, aperture 5nm, 57 ℃ of temperature; Recoil condition is 0.6MPa, recoil cycle 45min, recoil time 6s.Ceramic membrane concentrated solution enters the second three-phase cyclone separator 6-2, the second three-phase cyclone separator 6-2 pressure drop is 0.15Mpa, inlet velocity is 3m/s, the second three-phase cyclone separator 6-2 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, and bottom discharge returns the second ultra-filtration membrane fresh feed pump 4-2 and advances into ceramic membrane system.After the washing water that discharge ceramic membrane clear liquid and water wash column 3 middle and upper parts merges, enter the second interchanger 7-2, the washing water after heat exchange is transmitted back to water wash column 3 by the second topping-up pump 8-2.
Oil recovery rate under different transmembrane pressure conditions, catalyst recovery yield are as shown in table 1-2.
Oil recovery rate, catalyst recovery yield under the different transmembrane pressure conditions of table 1-2
| Transmembrane pressure MPa | 0.05 | 0.1 | 0.3 | 0.5 |
| Cycles of concentration | 12 | 17 | 26 | 28 |
| Oil recovery rate % | 75.8 | 82.5 | 89.6 | 86.7 |
| Catalyst recovery yield % | 82.4 | 84.6 | 94.8 | 93.1 |
| Water rate of recovery % | 92 | 92 | 91 | 93 |
Embodiment 2
Device flow process as shown in Figure 1, methyl alcohol enters reactor 1, and under the effect of catalyzer, reaction generates product and by product.Product and by product are carried partially catalyzed agent secretly with gas form and are entered quench tower 2, and quench tower 2 bottoms quenched water water quality is out 115 ℃ of temperature, catalyst content 189mg/L, oil-contg 510mg/L.Under the promotion of the first ultra-filtration membrane fresh feed pump 4-1, enter the first hyperfiltration membrane assembly 5-1, the inner ultra-filtration membrane of installing is oxidation titanium film, ultra-filtration membrane is worked under different pressures condition, also can add back pressure and form transmembrane pressure, transmembrane pressure is 0.4Mpa, aperture 20nm simultaneously, 87 ℃ of temperature, per-meate side back pressure 0.2MPa; Recoil condition is 0.8MPa, recoil cycle 45min, recoil time 6s.Titanium oxide ultra-filtration membrane concentrated solution enters the first three-phase cyclone separator 6-1, pressure drop is 0.15Mpa, inlet velocity is 3m/s, the first three-phase cyclone separator 6-1 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, bottom discharge returns the first ultra-filtration membrane fresh feed pump 4-1 and advances into the first hyperfiltration membrane assembly, after the quenched water that discharge ultra-filtration membrane clear liquid and quench tower 2 middle and upper parts merges, enters First Heat Exchanger 7-1, and the quenched water after heat exchange is transmitted back to quench tower 2 by the first topping-up pump 8-1.Oil recovery rate under different crossflow velocity conditions, catalyst recovery yield are as shown in table 2-1.
Oil recovery rate, catalyst recovery yield under the different crossflow velocity conditions of table 2-1
| Crossflow velocity m/s | 0.5 | 1 | 3 | 5 |
| Cycles of concentration | 4 | 11 | 16 | 21 |
| Oil recovery rate % | 51.6 | 71.7 | 84.9 | 79.5 |
| Catalyst recovery yield % | 66.5 | 69.5 | 75.2 | 74.3 |
| Water rate of recovery % | 90 | 90 | 91 | 90 |
As can be seen from the table, when crossflow velocity is less than normal, cycles of concentration can not be improved, and concentrated solution can not obtain separated preferably in three-phase cyclone separator, makes the rate of recovery of oil and catalyzer less than normal.When if crossflow velocity is excessive, can cause ultra-filtration membrane to decline to oily rejection, the whole rate of recovery is also reduced.
Quench tower 2 top gas enter water wash column 3,115 ℃ of water wash column 3 bottoms washing water temperature out, catalyst content 189mg/L, oil-contg 5200mg/L.Under the promotion of the second ultra-filtration membrane fresh feed pump 4-2, enter the second hyperfiltration membrane assembly 5-2, material is titanium oxide, ultra-filtration membrane is worked under different transmembrane pressures, transmembrane pressure 0.4MPa, aperture 20nm, 57 ℃ of temperature; Recoil condition is 0.6MPa, recoil cycle 45min, recoil time 6s.Ceramic membrane concentrated solution enters the second three-phase cyclone separator 6-2, the second three-phase cyclone separator 6-2 pressure drop is 0.15Mpa, inlet velocity is 3m/s, the second three-phase cyclone separator 6-2 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, and bottom discharge returns the second ultra-filtration membrane fresh feed pump 4-2 and advances into ceramic membrane system.After the washing water that discharge ceramic membrane clear liquid and water wash column 3 middle and upper parts merges, enter the second interchanger 7-2, the washing water after heat exchange is transmitted back to water wash column 3 by the second topping-up pump 8-2.
Oil recovery rate under different crossflow velocity conditions, catalyst recovery yield are as shown in table 2-2.
Oil recovery rate, catalyst recovery yield under the different crossflow velocity conditions of table 2-2
| Crossflow velocity m/s | 0.5 | 1 | 3 | 5 |
| Cycles of concentration | 5 | 14 | 22 | 26 |
| Oil recovery rate % | 56.9 | 67.8 | 84.3 | 82.7 |
| Catalyst recovery yield % | 82.4 | 84.6 | 94.8 | 93.1 |
| Water rate of recovery % | 90 | 90 | 93 | 92 |
Embodiment 3
Device flow process as shown in Figure 1, methyl alcohol enters reactor 1, and under the effect of catalyzer, reaction generates product and by product.Product and by product are carried partially catalyzed agent secretly with gas form and are entered quench tower 2, and quench tower 2 bottoms quenched water water quality is out 115 ℃ of temperature, catalyst content 189mg/L, oil-contg 510mg/L.Under the promotion of the first ultra-filtration membrane fresh feed pump 4-1, enter the first hyperfiltration membrane assembly 5-1, the inner ultra-filtration membrane of installing is oxidation titanium film, ultra-filtration membrane is worked under different pressures condition, also can add back pressure and form transmembrane pressure, transmembrane pressure is 0.4Mpa, crossflow velocity 3m/s simultaneously, 87 ℃ of temperature, per-meate side back pressure 0.2MPa; Recoil condition is 0.8MPa, recoil cycle 45min, recoil time 6s.Titanium oxide ultra-filtration membrane concentrated solution enters the first three-phase cyclone separator 6-1, pressure drop is 0.15Mpa, inlet velocity is 3m/s, the first three-phase cyclone separator 6-1 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, bottom discharge returns the first ultra-filtration membrane fresh feed pump 4-1 and advances into the first hyperfiltration membrane assembly, after the quenched water that discharge ultra-filtration membrane clear liquid and quench tower 2 middle and upper parts merges, enters First Heat Exchanger 7-1, and the quenched water after heat exchange is transmitted back to quench tower 2 by the first topping-up pump 8-1.Oil recovery rate under different membrane pore size conditions, catalyst recovery yield are as shown in table 3-1.
Oil recovery rate, catalyst recovery yield under the different membrane pore size conditions of table 3-1
| Membrane pore size nm | 5 | 20 | 50 | 200 |
| Cycles of concentration | 6 | 14 | 23 | 26 |
| Oil recovery rate % | 61.2 | 68.5 | 78.6 | 72.4 |
| Catalyst recovery yield % | 72.5 | 78.9 | 82.9 | 81.4 |
| Water rate of recovery % | 91 | 91 | 93 | 92 |
As can be seen from the table, when membrane pore size is less than normal, cycles of concentration can not be improved, and concentrated solution can not obtain separated preferably in three-phase cyclone separator, makes the rate of recovery of oil and catalyzer less than normal.When if membrane pore size is excessive, can cause ultra-filtration membrane to decline to oily rejection, the whole rate of recovery is also reduced.
Quench tower 2 top gas enter water wash column 3,115 ℃ of water wash column 3 bottoms washing water temperature out, catalyst content 189mg/L, oil-contg 5200mg/L.Under the promotion of the second ultra-filtration membrane fresh feed pump 4-2, enter the second hyperfiltration membrane assembly 5-2, material is titanium oxide, ultra-filtration membrane is worked under different transmembrane pressures, transmembrane pressure 0.4MPa, crossflow velocity 3m/s, 57 ℃ of temperature; Recoil condition is 0.6MPa, recoil cycle 45min, recoil time 6s.Ceramic membrane concentrated solution enters the second three-phase cyclone separator 6-2, the second three-phase cyclone separator 6-2 pressure drop is 0.15Mpa, inlet velocity is 3m/s, the second three-phase cyclone separator 6-2 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, and bottom discharge returns the second ultra-filtration membrane fresh feed pump 4-2 and advances into ceramic membrane system.After the washing water that discharge ceramic membrane clear liquid and water wash column 3 middle and upper parts merges, enter the second interchanger 7-2, the washing water after heat exchange is transmitted back to water wash column 3 by the second topping-up pump 8-2.
Oil recovery rate under different membrane pore size conditions, catalyst recovery yield are as shown in table 3-2.
Oil recovery rate, catalyst recovery yield under the different membrane pore size conditions of table 3-2
| Membrane pore size nm | 5 | 20 | 50 | 200 |
| Cycles of concentration | 8 | 15 | 24 | 28 |
| Oil recovery rate % | 64.5 | 68.9 | 75.4 | 73.1 |
| Catalyst recovery yield % | 654.8 | 71.5 | 77.8 | 73.5 |
| Water rate of recovery % | 91 | 93 | 93 | 92 |
Embodiment 4
Device flow process as shown in Figure 1, methyl alcohol enters reactor 1, and under the effect of catalyzer, reaction generates product and by product.Product and by product are carried partially catalyzed agent secretly with gas form and are entered quench tower 2, and quench tower 2 bottoms quenched water water quality is out 115 ℃ of temperature, catalyst content 189mg/L, oil-contg 510mg/L.Under the promotion of the first ultra-filtration membrane fresh feed pump 4-1, enter the first hyperfiltration membrane assembly 5-1, the inner ultra-filtration membrane of installing is oxidation titanium film, ultra-filtration membrane is worked under different pressures condition, also can add back pressure and form transmembrane pressure, transmembrane pressure is 0.4Mpa, crossflow velocity 3m/s simultaneously, membrane pore size is 50nm, per-meate side back pressure 0.2MPa; Recoil condition is 0.8MPa, recoil cycle 45min, recoil time 6s.Titanium oxide ultra-filtration membrane concentrated solution enters the first three-phase cyclone separator 6-1, pressure drop is 0.15Mpa, inlet velocity is 3m/s, the first three-phase cyclone separator 6-1 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, bottom discharge returns the first ultra-filtration membrane fresh feed pump 4-1 and advances into the first hyperfiltration membrane assembly, after the quenched water that discharge ultra-filtration membrane clear liquid and quench tower 2 middle and upper parts merges, enters First Heat Exchanger 7-1, and the quenched water after heat exchange is transmitted back to quench tower 2 by the first topping-up pump 8-1.Oil recovery rate under different filtration temperature conditions, catalyst recovery yield are as shown in table 4-1.
Oil recovery rate, catalyst recovery yield under the different filtration temperature conditions of table 4-1
| Temperature ℃ | 80 | 90 | 110 | 130 |
| Cycles of concentration | 16 | 21 | 26 | 27 |
| Oil recovery rate % | 65.4 | 67.8 | 77.1 | 73.2 |
| Catalyst recovery yield % | 71.3 | 75.8 | 77.8 | 75.1 |
| Water rate of recovery % | 91 | 91 | 93 | 92 |
As can be seen from the table, when membrane pore size is less than normal, cycles of concentration can not be improved, and concentrated solution can not obtain separated preferably in three-phase cyclone separator, makes the rate of recovery of oil and catalyzer less than normal.When if membrane pore size is excessive, can cause ultra-filtration membrane to decline to oily rejection, the whole rate of recovery is also reduced.
Quench tower 2 top gas enter water wash column 3,115 ℃ of water wash column 3 bottoms washing water temperature out, catalyst content 189mg/L, oil-contg 5200mg/L.Under the promotion of the second ultra-filtration membrane fresh feed pump 4-2, enter the second hyperfiltration membrane assembly 5-2, material is titanium oxide, ultra-filtration membrane is worked under different transmembrane pressures, transmembrane pressure 0.4MPa, crossflow velocity 3m/s, 57 ℃ of temperature; Recoil condition is 0.6MPa, recoil cycle 45min, recoil time 6s.Ceramic membrane concentrated solution enters the second three-phase cyclone separator 6-2, the second three-phase cyclone separator 6-2 pressure drop is 0.15Mpa, inlet velocity is 3m/s, the second three-phase cyclone separator 6-2 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, and bottom discharge returns the second ultra-filtration membrane fresh feed pump 4-2 and advances into ceramic membrane system.After the washing water that discharge ceramic membrane clear liquid and water wash column 3 middle and upper parts merges, enter the second interchanger 7-2, the washing water after heat exchange is transmitted back to water wash column 3 by the second topping-up pump 8-2.
Oil recovery rate under different filtration temperature conditions, catalyst recovery yield are as shown in table 4-2.
Oil recovery rate, catalyst recovery yield under the different filtration temperature conditions of table 4-2
| Temperature ℃ | 40 | 50 | 50 | 60 |
| Cycles of concentration | 17 | 19 | 23 | 25 |
| Oil recovery rate % | 65.8 | 66.7 | 75.4 | 71.7 |
| Catalyst recovery yield % | 62.7 | 68.7 | 80.7 | 75.4 |
| Water rate of recovery % | 90 | 90 | 93 | 92 |
Embodiment 5
Device flow process as shown in Figure 1, methyl alcohol enters reactor 1, and under the effect of catalyzer, reaction generates product and by product.Product and by product are carried partially catalyzed agent secretly with gas form and are entered quench tower 2, and quench tower 2 bottoms quenched water water quality is out 115 ℃ of temperature, catalyst content 189mg/L, oil-contg 510mg/L.Under the promotion of the first ultra-filtration membrane fresh feed pump 4-1, enter the first hyperfiltration membrane assembly 5-1, the inner ultra-filtration membrane of installing is oxidation titanium film, ultra-filtration membrane is worked under different pressures condition, also can add back pressure simultaneously and form transmembrane pressure, and transmembrane pressure is 0.4Mpa, crossflow velocity 3m/s, membrane pore size is 50nm, 87 ℃ of temperature, per-meate side back pressure 0.2MPa; Recoil condition is 0.8MPa, recoil time 6s.Titanium oxide ultra-filtration membrane concentrated solution enters the first three-phase cyclone separator 6-1, pressure drop is 0.15Mpa, inlet velocity is 3m/s, the first three-phase cyclone separator 6-1 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, bottom discharge returns the first ultra-filtration membrane fresh feed pump 4-1 and advances into the first hyperfiltration membrane assembly, after the quenched water that discharge ultra-filtration membrane clear liquid and quench tower 2 middle and upper parts merges, enters First Heat Exchanger 7-1, and the quenched water after heat exchange is transmitted back to quench tower 2 by the first topping-up pump 8-1.Oil recovery rate under difference recoil cycle interval condition, catalyst recovery yield are as shown in Table 5-1.
Oil recovery rate, catalyst recovery yield under the different recoil of table 5-1 periodic condition
| Recoil cycle interval min | 20 | 40 | 60 | 120 |
| Cycles of concentration | 27 | 28 | 30 | 29 |
| Oil recovery rate % | 75.8 | 78.9 | 89.7 | 85.4 |
| Catalyst recovery yield % | 78.5 | 81.2 | 93.4 | 91.7 |
| Water rate of recovery % | 92 | 92 | 95 | 93 |
As can be seen from the table, when partially long in the recoil cycle, cycles of concentration can not be improved, and concentrated solution can not obtain separated preferably in three-phase cyclone separator, makes the rate of recovery of oil and catalyzer less than normal.If the recoil cycle when less than normal, can cause ultra-filtration membrane to decline to oily rejection, the whole rate of recovery is also reduced.
Quench tower 2 top gas enter water wash column 3,115 ℃ of water wash column 3 bottoms washing water temperature out, catalyst content 189mg/L, oil-contg 5200mg/L.Under the promotion of the second ultra-filtration membrane fresh feed pump 4-2, enter the second hyperfiltration membrane assembly 5-2, material is titanium oxide, ultra-filtration membrane is worked under different transmembrane pressures, transmembrane pressure 0.4MPa, crossflow velocity 3m/s, 57 ℃ of temperature; Recoil condition is 0.6MPa, recoil time 6s.Ceramic membrane concentrated solution enters the second three-phase cyclone separator 6-2, the second three-phase cyclone separator 6-2 pressure drop is 0.15Mpa, inlet velocity is 3m/s, the second three-phase cyclone separator 6-2 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, and bottom discharge returns the second ultra-filtration membrane fresh feed pump 4-2 and advances into ceramic membrane system.After the washing water that discharge ceramic membrane clear liquid and water wash column 3 middle and upper parts merges, enter the second interchanger 7-2, the washing water after heat exchange is transmitted back to water wash column 3 by the second topping-up pump 8-2.
Oil recovery rate under difference recoil periodic condition, catalyst recovery yield are as shown in table 5-2.
Oil recovery rate, catalyst recovery yield under the different recoil of table 5-2 periodic condition
| Recoil cycle interval min | 20 | 40 | 60 | 120 |
| Cycles of concentration | 25 | 27 | 34 | 31 |
| Oil recovery rate % | 77.4 | 83.4 | 92.1 | 85.4 |
| Catalyst recovery yield % | 79.9 | 86.7 | 94.7 | 87.4 |
| Water rate of recovery % | 90 | 90 | 93 | 92 |
Embodiment 6
Device flow process as shown in Figure 2, methyl alcohol enters reactor 1, and under the effect of catalyzer, reaction generates product and by product.Product and by product are carried partially catalyzed agent secretly with gas form and are entered quench tower 2, and quench tower 2 bottoms quenched water water quality is out 115 ℃ of temperature, catalyst content 189mg/L, oil-contg 410mg/L.Under the promotion of the first ultra-filtration membrane fresh feed pump 4-1, enter the first hyperfiltration membrane assembly 5-1, the inner ultra-filtration membrane of installing is oxidation titanium film, ultra-filtration membrane is worked under different pressures condition, also can add back pressure and form transmembrane pressure, crossflow velocity 5m/s, aperture 5nm simultaneously, 87 ℃ of temperature, per-meate side back pressure 0.2MPa; Recoil condition is 0.8MPa, recoil cycle 45min, recoil time 6s.Titanium oxide ultra-filtration membrane concentrated solution enters the first micro-filtration membrane module and filters, the mean pore size of microfiltration membrane is 500nm, transmembrane pressure is 0.1MPa, crossflow velocity is 1m/s, the concentrated solution of micro-filtration assembly enters to the first three-phase cyclone separator 6-1, the penetrating fluid of micro-filtration is back to the import of the first hyperfiltration membrane assembly 5-1, the pressure drop of the first three-phase cyclone separator 6-1 is 0.15Mpa, inlet velocity is 3m/s, the first three-phase cyclone separator 6-1 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, bottom discharge returns the first ultra-filtration membrane fresh feed pump 4-1 and advances into the first hyperfiltration membrane assembly, after merging, the quenched water that discharge ultra-filtration membrane clear liquid and quench tower 2 middle and upper parts enters First Heat Exchanger 7-1, quenched water after heat exchange is transmitted back to quench tower 2 by the first topping-up pump 8-1.Oil recovery rate under different transmembrane pressure conditions, catalyst recovery yield are as shown in Table 6-1.
Oil recovery rate, catalyst recovery yield under the different transmembrane pressure conditions of table 6-1
| Transmembrane pressure MPa | 0.05 | 0.1 | 0.3 | 0.5 |
| Ultrafiltration and concentration multiple | 10 | 13 | 21 | 24 |
| Oil recovery rate % | 77.1 | 87.7 | 93.2 | 87.4 |
| Catalyst recovery yield % | 89.2 | 94.7 | 98.7 | 94.9 |
| Water rate of recovery % | 90 | 91 | 90 | 91 |
As can be seen from the table, compare with embodiment 1, by by ultra-filtration membrane concentrated solution through micro-filtration further after concentration, can effectively improve cycles of concentration, and make a part of impurity see through microfiltration membrane, separated with feed liquid, feed liquid enters to can be better separated in three-phase cyclone separator, and the rate of recovery of oil recovery rate and catalyzer is high.
Quench tower 2 top gas enter water wash column 3,115 ℃ of water wash column 3 bottoms washing water temperature out, catalyst content 189mg/L, oil-contg 5200mg/L.Under the promotion of the second ultra-filtration membrane fresh feed pump 4-2, enter the second hyperfiltration membrane assembly 5-2, material is titanium oxide, ultra-filtration membrane is worked under different transmembrane pressures, crossflow velocity 5m/s, aperture 5nm, 57 ℃ of temperature; Recoil condition is 0.6MPa, recoil cycle 45min, recoil time 6s.Ceramic membrane concentrated solution enters the second micro-filtration membrane module 9-2, the mean pore size of microfiltration membrane is that 500nm, transmembrane pressure are that 0.1MPa, crossflow velocity are 1m/s, the concentrated solution of micro-filtration is sent into the second three-phase cyclone separator 6-2, micro-filtration see through the import that liquid is back to the second hyperfiltration membrane assembly, the second three-phase cyclone separator 6-2 pressure drop is 0.15Mpa, inlet velocity is 3m/s, the second three-phase cyclone separator 6-2 top discharging refiltered oil, catalyzer is reclaimed in sidepiece discharging, and bottom discharge returns the second ultra-filtration membrane fresh feed pump 4-2 and advances into ceramic membrane system.After the washing water that discharge ceramic membrane clear liquid and water wash column 3 middle and upper parts merges, enter the second interchanger 7-2, the washing water after heat exchange is transmitted back to water wash column 3 by the second topping-up pump 8-2.
Oil recovery rate under different transmembrane pressure conditions, catalyst recovery yield are as shown in table 6-2.
Oil recovery rate, catalyst recovery yield under the different transmembrane pressure conditions of table 6-2
| Transmembrane pressure MPa | 0.05 | 0.1 | 0.3 | 0.5 |
| Ultrafiltration and concentration multiple | 11 | 17 | 25 | 29 |
| Oil recovery rate % | 82.9 | 88.4 | 96.6 | 90.7 |
| Catalyst recovery yield % | 86.8 | 87.6 | 97.9 | 95.6 |
| Water rate of recovery % | 90 | 91 | 90 | 91 |
As can be seen from the table, compare with embodiment 1, using microfiltration membrane after further concentrating, can improve the rate of recovery of oil and catalyzer to ultrafiltration and concentration liquid.
Claims (5)
1. in a MTO technology, process water takes off the device of oil removing admittedly, it is characterized in that: include quenching water column (2), washing water tower (3), the bottom of quenching water column (1) is connected with the import of the first hyperfiltration membrane assembly (5-1), the per-meate side of the first hyperfiltration membrane assembly (5-1) is connected to the quenched water ingress of quenching water column (2), the side of holding back of the first hyperfiltration membrane assembly (5-1) is connected to the first three-phase cyclone separator (6-1) connection, the top of the first three-phase cyclone separator (6-1) is oil phase outlet, sidepiece is catalyst outlet, bottom is water out, bottom is connected to the import of the first hyperfiltration membrane assembly (5-1), the bottom of washing water tower (3) is connected with the import of the second hyperfiltration membrane assembly (5-2), the per-meate side of the second hyperfiltration membrane assembly (5-2) is connected to the washing water ingress of washing water tower (3), the side of holding back of the second hyperfiltration membrane assembly (5-2) is connected to the second three-phase cyclone separator (6-2) connection, the top of the second three-phase cyclone separator (6-2) is that oil phase outlet, sidepiece are that catalyst outlet, bottom are water outs, and bottom is connected to the import of the second hyperfiltration membrane assembly (5-2).
2. in MTO technology according to claim 1, process water takes off the device of oil removing admittedly, it is characterized in that: the side of holding back of the first hyperfiltration membrane assembly (5-1) is connected in the first micro-filtration membrane module (9-1), the side of holding back of the first micro-filtration membrane module (9-1) is connected with the first three-phase cyclone separator (6-1), and the per-meate side of the first micro-filtration membrane module (9-1) is connected in the ingress of the first hyperfiltration membrane assembly (5-1); The side of holding back of the second hyperfiltration membrane assembly (5-2) is connected in the second micro-filtration membrane module (9-2), the side of holding back of the second micro-filtration membrane module (9-2) is connected with the second three-phase cyclone separator (6-2), and the per-meate side of the second micro-filtration membrane module (9-2) is connected in the ingress of the second ultra-filtration membrane group (5-2) part.
3. the device of the de-solid oil removing of process water in MTO technology according to claim 1, is characterized in that: the mean pore size of the first hyperfiltration membrane assembly (5-1) and the second hyperfiltration membrane assembly (5-2) is 5～200nm.
4. the device of the de-solid oil removing of process water in MTO technology according to claim 3, is characterized in that: described mean pore size is 20～50nm.
5. the device of the de-solid oil removing of process water in MTO technology according to claim 2, is characterized in that: the mean pore size of microfiltration membrane is 200 nm～500 nm.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103951098A (en) * | 2014-04-25 | 2014-07-30 | 江苏久吾高科技股份有限公司 | Solid and oil removal method and device for chilled water and washed water in MTO (methanol to olefin) process |
| CN106542589A (en) * | 2015-09-21 | 2017-03-29 | 波特膜过滤与分离技术(石家庄)有限公司 | MTO chilled water (chw)s and washing water purification process technique |
| CN109205859A (en) * | 2018-11-14 | 2019-01-15 | 湖南泰山石环境科技有限公司 | A kind of methanol-to-olefins device generation water treatment system |
| CN110015800A (en) * | 2019-04-23 | 2019-07-16 | 国家能源投资集团有限责任公司 | Methanol-to-olefins water system and its processing method |
-
2014
- 2014-04-25 CN CN201420208889.8U patent/CN203820559U/en not_active Withdrawn - After Issue
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103951098A (en) * | 2014-04-25 | 2014-07-30 | 江苏久吾高科技股份有限公司 | Solid and oil removal method and device for chilled water and washed water in MTO (methanol to olefin) process |
| CN103951098B (en) * | 2014-04-25 | 2015-12-30 | 江苏久吾高科技股份有限公司 | In MTO technology, quenched water and washing water take off method and the device of solid oil removing |
| CN106542589A (en) * | 2015-09-21 | 2017-03-29 | 波特膜过滤与分离技术(石家庄)有限公司 | MTO chilled water (chw)s and washing water purification process technique |
| CN109205859A (en) * | 2018-11-14 | 2019-01-15 | 湖南泰山石环境科技有限公司 | A kind of methanol-to-olefins device generation water treatment system |
| CN109205859B (en) * | 2018-11-14 | 2022-06-17 | 湖南泰山石环境科技有限公司 | Methanol-to-olefin device generates water treatment system |
| CN110015800A (en) * | 2019-04-23 | 2019-07-16 | 国家能源投资集团有限责任公司 | Methanol-to-olefins water system and its processing method |
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