CN104071910A - MTO/MTP (Methanol to Olefins/Methanol to Propylene) product separating tower bottom solution dewaxing and deoiling method and device - Google Patents
MTO/MTP (Methanol to Olefins/Methanol to Propylene) product separating tower bottom solution dewaxing and deoiling method and device Download PDFInfo
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Abstract
The invention relates to an MTO/MTP (Methanol to Olefins/Methanol to Propylene) product separating tower bottom solution dewaxing and deoiling method and device. The device comprises an ultrafiltration membrane facility, a biphase cyclone separator and an oil groove. The MTO/MTP product separating tower bottom solution is firstly subjected to ultrafiltration membrane separation, and the ultrafiltrate returns to the product separating tower for cyclic utilization; the ultrafiltration membrane concentrated solution enters the biphase cyclone separator; an oil/emulsified paraffin mixture separated from the top of the biphase cyclone separator enters the oil groove; and the biphase cyclone separator bottom water returns to the ultrafiltration membrane system. The invention also relates to a cleaning scheme of the MTO/MTP product separating tower bottom solution dewaxing and deoiling ultrafiltration membrane device. The method can effectively remove the oil and emulsified paraffin in the product separating tower bottom solution, thereby implementing the continuous stable operation of the device; the membrane flux can be completely recovered by cleaning; and the oil and paraffin in the tower bottom solution are simultaneous recovered, thereby avoiding the waste of resources and reducing the environmental pollution.
Description
Technical field
The device and method that the present invention relates to liquid dewaxing oil removing at the bottom of a kind of MTO/MTP product separation tower tower, belongs 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 MTO charging vaporization unit and lighter hydrocarbons recovery upgrading unit.In MTO/MTP reaction process, product is mainly low-carbon alkene, but also generates the by products such as large water gaging, mixed alkanes, alkene, aromatic hydrocarbon and yellowish brown oily liquids.When water recycles in product separation tower as refrigerant, some heavy hydrocarbons in water are known from experience continuous enrichment as the paraffin of emulsification shape and yellowish brown oily liquid, when after interchanger heat exchange, water temperature declines, paraffin in water and oil can be adsorbed in interchanger, cause heat transfer effect to decline, even stop up interchanger, have a strong impact on the steady running of system.Therefore, at the bottom of the effective removal of exploitation MTO/MTP product separation tower tower, the oil in liquid and the technology of emulsification shape paraffin seem particularly important.
CN101962235A discloses the wastewater treatment of a kind of MTO process high-temperature and reuse method, the method of adjusting alkali, aeration, filtration, micro-filtration or ultrafiltration membrane system, high temperature reverse osmosis system to process a small amount of high-temperature technology waste water of discharging at the bottom of stripping tower reactor has been reported in this invention, methyl alcohol, dme, acetic acid, propionic acid etc. in main removal waste water, but the aspect that removes for the paraffin in liquid at the bottom of product separation tower tower in MTO technique and oil is not studied and reports, and the method complex process, reagent consumption are large.CN101139117A and CN101139118A disclose a kind of waste water treatment process containing methyl alcohol and dme, CN102060347A discloses a kind of recovery low-carbon (LC) hydro carbons and the organic sewage treatment process of low-carbon oxygen-containing, but above-mentioned 2 pieces of patents only reclaim low-carbon (LC) hydrocarbons and low-carbon oxygen-containing organism sewage from the angular separation of process optimization, do not relate to the paraffin in water and oily removal method.
CN103768955A provides a kind of hyperfiltration membrane cleaning agent, clean-out system main component is Sodium dodecylbenzene sulfonate, fatty alcohol-polyoxyethylene ether sodium sulfonate, Walocel MT 20.000PV, Trisodium Citrate, sodium carbonate, sodium hydroxide, polygalacturonase, aliphatics polyoxy Vinyl Ether, potassium silicate, and this patent also proposes cleaning process and divides pickling, alkali cleaning, rinsing three steps.CN103041709A provides a kind of ultra-filtration membrane purging method, first uses NaOH solution and the alkali cleaning of PC-98 solution difference 1 time, then uses 1% oxalic acid solution pickling 1 time.Above-mentioned 2 pieces of patents all exist that clean-out system complicated component, cleaning step are loaded down with trivial details, need a large amount of pure water in cleaning process, cleaning reagent expense is high, cleaning reagent cannot reuse etc. shortcoming.
Summary of the invention
The present invention is directed to and in MTO/MTP product separation tower operational process, have emulsification shape paraffin and the constantly enrichment in interchanger of yellowish brown oily liquids, even stop up the problems such as interchanger, propose method and the device of liquid dewaxing oil removing at the bottom of a kind of new MTO/MTP product separation tower tower.Meanwhile, be directed to body series and propose a kind of new cleaning program and cleaning reagent.
Technical scheme:
According to an aspect of the present invention, liquid dewaxing deoiling method at the bottom of MTO/MTP product separation tower tower, comprises the steps: at the bottom of product separation tower tower that liquid is sent into ultra-filtration membrane to filter, and obtains seeing through liquid and concentrated solution; See through liquid and return product separation tower, concentrated solution is sent into two-phase cyclone separator, obtains water and oil phase, and water is back to ultra-filtration membrane and filters, and after oil phase stratification, obtains oil reservoir and paraffin.
According to another aspect of the present invention, liquid dewaxing oil removal plant at the bottom of MTO/MTP product separation tower tower, include ultra-filtration membrane membrane module, two-phase cyclone separator, layering groove, the side of holding back of ultra-filtration membrane membrane module is connected with the entrance of two-phase cyclone separator, the top of two-phase cyclone separator is connected with the import of ultra-filtration membrane membrane module, and the bottom of two-phase cyclone separator is connected with layering groove.
According to another aspect of the present invention, the film purging method of liquid dewaxing oil removing process at the bottom of MTO/MTP product separation tower tower, soaks, washs by membrane module being carried out to polar solvent immersion, washing and non-polar solvent successively.
Invention effect
At the bottom of 1.MTO/MTP product separation tower tower, liquid adopts ultrafiltration membrane separation concentration, and water rate of recovery >97%, and oily and paraffin total content < 80ppm in water, have significant economic benefit.
2. adopt water-and-oil separator refiltered oil and paraffin, oil and paraffin total yield >99%, have significant economic benefit.
3. the method can prevent paraffin and oil enrichment in recirculated water, reduces paraffin and oily matter in heat exchanger surface enrichment, improves the stability of heat exchange efficiency and system.
4. the advantages such as membrane element adopts tubular ultra-filtration membrane, and this film has long service life (2～10 years), and easy cleaning and cleaning interval are long, working cost is low.The mode that adopts ultra-filtration membrane per-meate side back pressure, range of application is wider, and temperature is 70～95 ℃.
5. material out directly enters ultrafiltration membrane system from system, and without regulating temperature and pH, energy consumption and reagent consumption are little again.
6. to realize the two-phase of oil-water simultaneously separated for water-and-oil separator, compares with common waste-oil scavenger, and water-and-oil separator has that volume is little, efficiency is high, it is little to invest and the feature such as energy consumption is low.
7. adopt polar solvent, small molecules non-polar solvent, macromole non-polar solvent to clean film pipe, three kinds of reagent are all from raw materials for production or product, and cleaning charge is low.
8. cleaning process only comprises cross-flow cleaning, soaking and washing stage, total scavenging period 1～2h, and scavenging period is short, step is simple.
9. while cleaning, do not need to add pure water or the allotment of other reagent, after cleaning finishes, do not need pure water rinsing, saved great lot of water resources.
10. clean-out system can reuse, and after use, can enter system recovery system, to environment, can not cause any harm, has saved cleaning charge use simultaneously.
11. these clean-out systems are no acidic, alkaline matter, all corrosion-free to film pipe and equipment, greatly reduce facility investment, maintenance and replacement cost.
Accompanying drawing explanation
Fig. 1 is process flow sheet of the present invention
Wherein, 1-quench tower, 2-product separation tower, 3-ultra-filtration membrane membrane module, 4-two-phase cyclone separator, 5-layering groove, 6-purge tank, 7-quench tower recycle pump, 8-product separation tower recycle pump, 9-ultra-filtration membrane fresh feed pump, 10-quench tower interchanger, 11-product separation tower interchanger.
Embodiment
Technique of the present invention is applicable to the dewaxing oil removing of liquid at the bottom of product separation tower tower in Methanol ethene or propylene (MTO/MTP) process.In MTO or MTP technique, first the gas product obtaining in reactor enters quench tower, the gas phase of chilling tower top is sent in product separation tower, gas product in product separation tower with two bursts of recirculation water condensations, the olefin product of product separation top of tower is sent into olefin recovery unit, compress fractionation and purification.From product knockout tower bottom, material major part is out got back to product separation tower in intermediate condenser with after fresh feed heat exchange, and small part is sent into water stripper, and residual lighter hydrocarbons by stripping out.At the bottom of knockout tower tower, liquid is generally 70～95 ℃, oil-contg 500～50000mg/L.
The device that the present invention adopts as shown in Figure 1, from the gas product of quench tower 1, enter to the entrance of product separation tower 2, a part of kettle base solution of product separation tower 2 (mainly containing organism and the yellowish brown oily matter such as emulsification shape paraffin) enters ultra-filtration membrane membrane module 3 by ultra-filtration membrane fresh feed pump 9, the clear liquid of ultra-filtration membrane membrane module 3 returns to 2 recycles of product separation tower, the concentrated solution of membrane module enters two-phase cyclone separator 4, the import of ultra-filtration membrane fresh feed pump 9 is returned in the 4 bottom water outlets of two-phase cyclone separator, again enters ultrafiltration membrane system; The 4 top dischargings of two-phase cyclone separator are oil and the mixture of emulsification shape paraffin, and this mixture enters that oil groove 5 is standing, after layering, and the oil of upper strata yellow flows in oil-collecting bucket, then recovery; And the paraffin of lower floor flows in collection wax bucket, then reclaim.
Owing to having mixed alkanes, alkene, aromatic hydrocarbon and yellowish brown oily liquids in product separation tower, water temperature declines, and the paraffin in water and oil can be adsorbed in interchanger, causes heat transfer effect to decline, and even stops up interchanger, has a strong impact on the steady running of system.First after concentrating by ultra-filtration membrane, can obtain comparatively pure ultrafiltration and see through liquid, and oil, paraffin etc. all can reside in the concentrated solution of ultrafiltration, by two-phase cyclone separator, oil, paraffin are carried out to separation further again, in two-phase cyclone separator, top is isolated oily matter, and bottom is the water after purifying, and the water of these bottoms can be back to again and in ultrafiltration membrance filter system, carry out reuse.In this technique, water rate of recovery >97%, and oily and paraffin total content < 80ppm in water; With two-phase cyclone separator refiltered oil and paraffin, oil and paraffin total yield >99%, by after oil and paraffin removal, can prevent paraffin and oil enrichment in recirculated water, reduce paraffin and oily matter in heat exchanger surface enrichment, improve the stability of heat exchange efficiency and system.In addition, it is simultaneously separated that two-phase cyclone separator can be realized the two-phase of oil-water, compares with common waste-oil scavenger, and two-phase cyclone separator has that volume is little, efficiency is high, it is little to invest and the feature such as energy consumption is low.
Liquid carries out in ultra-filtration process at the bottom of to product separation tower tower, 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, two-phase cyclone separator is cannot be preferably separated by 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 0.3～0.5MPa, optimum 0.4MPa.
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 two-phase cyclone separator low, inferior separating effect.Crossflow velocity is preferably 0.5～6m/s, more excellent 3～5m/s, optimum 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 two-phase cyclone separator; If mean pore size is excessive, can cause having more oily matter to see through rete, the rate of recovery of oil and catalyzer is incurred loss.Mean pore size is preferably 5～200nm, more preferably 20～200nm.Ultra-filtration membrane preferably adopts ceramic membrane.
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 product separation tower, be 70～95 ℃, more excellent is 75～90 ℃, optimum 90 ℃.For cycles of concentration in the ultrafiltration of product separation tower, be 5～60 times, more excellent is 10～30 times, optimum 20 times.
In two-phase cyclone separator, the concentrated solution of membrane sepn is to enter from the side separator, and the top of separator can make oil obtain separation, and bottom is that the entrance that water is directly sent into ultra-filtration membrane carries out reuse.The pressure drop of two-phase cyclone separator is 0.05～0.25Mpa, and more excellent is 0.1～0.2MPa, optimum 0.15MPa; Inlet velocity is 1～6m/s, and more excellent is 3～5m/s, optimum 3m/s.
In this application, the filter cake that the pollution type on film surface mainly can include Pore Blocking pollution and film surface pollutes, and due to complicated component in the kettle base solution of product separation tower, include mixed alkanes, alkene, aromatic hydrocarbon, yellowish brown oily liquids, paraffin, suspended solid (for example some granules of catalyst), make the washing effect of conventional cleaning agents of membrane poor, be difficult for membrane flux to recover.The present invention is by first soaking, clean with polar solvent, then soaks, cleans with non-polar solvent, effectively can recover membrane flux.Such cleaning way is that the type of polluting with film is closely related, and cake layer, hole plug can be polluted and removes.The polar solvent adopting can be methyl alcohol, ethanol, propyl alcohol etc., and optimum is to adopt methyl alcohol; The non-polar solvent adopting can be the alkane of C4～C8, and optimum is to adopt octane.First adopt polar solvent soak and clean, can effectively remove the pollution of cake layer, after cake layer is removed, non-polar solvent can directly contact with the blocking pollution thing (may be some greases, paraffin etc.) in fenestra, to these hole plug pollution clean-up better effects if.In a preferred embodiment, with polar solvent, soak and clean constantly, preferably 40～50 ℃ of temperature, optimum 45 ℃, soak time is 30～60min preferably; When soaking and cleaning with non-polar solvent, preferably 50～60 ℃ of temperature, optimum is 55 ℃, and soak time is 40～80min preferably, and optimum is 60min; Clean-out system that this purging method is used is no acidic, alkaline matter, all corrosion-free to film pipe and equipment, greatly reduces facility investment, maintenance and replacement cost.
In following examples, adopt above-mentioned device and device to carry out de-oiling processing to the tower bottoms of product separation tower, wherein need to investigate the rate of recovery of oil recovery rate, paraffin, oil recovery rate refers to the oily weight that obtains in two-phase cyclone separator and the ratio of the oily weight in kettle base solution, the ratio of the weight of paraffin in the weight of the paraffin obtaining in the rate of recovery two-phase cyclone separator of paraffin and kettle base solution.
Embodiment 1
At the bottom of the tower of product separation tower, liquid passes through under the promotion of product separation tower recycle pump 8 and ultra-filtration membrane fresh feed pump 9 successively, enter ultra-filtration membrane membrane module 3, hyperfiltration membrane assembly adopts titanium oxide ceramics ultra-filtration membrane, aperture 20nm, crossflow velocity 5m/s, adopt respectively 0.05,0.1,0.3, the working pressure of 0.5MPa, 75 ℃ of temperature.The clear liquid of ultra-filtration membrane returns to recycle in product separation tower 2.Ultra-filtration membrane concentrated solution enters two-phase cyclone separator 4, and 4 pressure drops of two-phase cyclone separator are 0.20Mpa, and inlet velocity is 6m/s.The import of ultra-filtration membrane fresh feed pump 9 is returned in the 4 bottom water outlets of two-phase cyclone separator, again enters recycle in ultrafiltration membrane system.The 4 top dischargings of two-phase cyclone separator are emulsification shape paraffin and oily mixture; The oil of separating and emulsification shape mineral wax mixture enter oil groove 5.Oil and emulsification shape mineral wax mixture is standing, after layering, the oil reservoir of upper strata yellow flows in oil-collecting bucket, then recycling; And the paraffin of lower floor flows in collection wax bucket, then recycle.The service data of this technique is as shown in table 1.
Service data under the different transmembrane pressure conditions of table 1
| Transmembrane pressure MPa | 0.05 | 0.1 | 0.3 | 0.5 |
| Cycles of concentration | 10 | 20 | 30 | 40 |
| Oil and paraffin total content ppm in water | 80 | 92 | 97 | 121 |
| Oil recovery rate % | 80.1 | 83.4 | 88.7 | 82.7 |
| Solvent recovery with paraffin rate % | 90.1 | 92.5 | 94.6 | 93.5 |
As can be seen from the table, along with the increase of transmembrane pressure, in penetrating fluid, oil and paraffinicity also there will be increase, and this may be due to after increasing pressure, and a part of oily matter can enter to per-meate side through fenestra to be caused.In addition, in the situation that transmembrane pressure is less, there will be the situation that cycles of concentration is not high, in ultrafiltration and concentration liquid, can retain and have more water, these moisture are being difficult for obtaining effectively separatedly with oily components when the cyclonic separation, and paraffin and oil recovery rate are on the low side in the situation that of low transmembrane pressure.When transmembrane pressure is 0.3MPa left and right, the rate of recovery obtaining is higher.
Embodiment 2
At the bottom of the tower of product separation tower, liquid passes through under the promotion of product separation tower recycle pump 8 and ultra-filtration membrane fresh feed pump 9 successively, enter ultra-filtration membrane membrane module 3, hyperfiltration membrane assembly adopts titanium oxide ceramics ultra-filtration membrane, aperture 200nm, crossflow velocity is respectively 0.5,3,4,6m/s, 0.3MPa working pressure, 80 ℃ of temperature.The clear liquid of ultra-filtration membrane returns to recycle in product separation tower 2.Ultra-filtration membrane concentrated solution enters two-phase cyclone separator 4, and 4 pressure drops of two-phase cyclone separator are 0.15Mpa, and inlet velocity is 5m/s.The import of ultra-filtration membrane fresh feed pump 9 is returned in the 4 bottom water outlets of two-phase cyclone separator, again enters recycle in ultrafiltration membrane system.The 4 top dischargings of two-phase cyclone separator are emulsification shape paraffin and oily mixture; The oil of separating and emulsification shape mineral wax mixture enter oil groove 5.Oil and emulsification shape mineral wax mixture is standing, after layering, the oil reservoir of upper strata yellow flows in oil-collecting bucket, then recycling; And the paraffin of lower floor flows in collection wax bucket, then recycle.The service data of this technique is as shown in table 1.
Service data under the different crossflow velocity conditions of table 2
| Crossflow velocity m/s | 0.5 | 3 | 4 | 6 |
| Cycles of concentration | 7 | 15 | 24 | 30 |
| Oil and paraffin total content ppm in water | 83 | 89 | 77 | 124 |
| Oil recovery rate % | 83.3 | 84.5 | 87.3 | 81.6 |
| Solvent recovery with paraffin rate % | 88.1 | 89.5 | 93.7 | 92.9 |
As can be seen from the table, under the condition of lower crossflow velocity, the pollution of ultra-filtration process is comparatively serious, cannot improve further cycles of concentration, make in concentrated solution moisture more, these concentrated solutions can cause making moisture and oiliness component separating in the process of carrying out cyclonic separation, in the water outlet of bottom, can, with more oiliness composition, make paraffin and oil recovery rate lower.Under the condition of higher crossflow velocity, can cause forming the cake layer that enough plays auxiliary centrifugation on film surface, part oily matter can see through rete and enter to per-meate side, cause the amount of oil-containing in the water of penetrating fluid and paraffin higher, when crossflow velocity is 4m/s left and right, can effectively improve the yield of oil and paraffin.
Embodiment 3
At the bottom of the tower of product separation tower, liquid passes through under the promotion of product separation tower recycle pump 8 and ultra-filtration membrane fresh feed pump 9 successively, enter ultra-filtration membrane membrane module 3, hyperfiltration membrane assembly adopts titanium oxide ceramics ultra-filtration membrane, mean pore size adopts respectively 5,20,50,200nm, 4,6m/s, 0.4MPa working pressure, 90 ℃ of temperature.The clear liquid of ultra-filtration membrane returns to recycle in product separation tower 2.Ultra-filtration membrane concentrated solution enters two-phase cyclone separator 4, and 4 pressure drops of two-phase cyclone separator are 0.15Mpa, and inlet velocity is 4m/s.The import of ultra-filtration membrane fresh feed pump 9 is returned in the 4 bottom water outlets of two-phase cyclone separator, again enters recycle in ultrafiltration membrane system.The 4 top dischargings of two-phase cyclone separator are emulsification shape paraffin and oily mixture; The oil of separating and emulsification shape mineral wax mixture enter oil groove 5.Oil and emulsification shape mineral wax mixture is standing, after layering, the oil reservoir of upper strata yellow flows in oil-collecting bucket, then recycling; And the paraffin of lower floor flows in collection wax bucket, then recycle.The service data of this technique is as shown in table 1.
Service data under the different film mean pore size of table 3 condition
| Mean pore size nm | 5 | 20 | 50 | 200 |
| Cycles of concentration | 8 | 17 | 35 | 38 |
| Oil and paraffin total content ppm in water | 13 | 53 | 71 | 137 |
| Oil recovery rate % | 52.3 | 78.1 | 96.1 | 83.1 |
| Solvent recovery with paraffin rate % | 55.2 | 79.2 | 95.2 | 84.1 |
As can be seen from the table, in the situation that use the film of smaller aperture due, can cause cycles of concentration less, can make paraffin and oil recovery rate less than normal; If in larger aperture, the oily matter in kettle base solution can see through rete and enter to per-meate side, equally also can cause concentrated solution cannot obtain good separation in two-phase cyclone separator, makes oil recovery rate on the low side.
Embodiment 4
To completing the ultra-filtration membrane of filter operation in embodiment 3, carry out film cleaning, purging method adopts respectively following 4 kinds:
Cleaning program 1: adopt methyl alcohol as clean-out system, soak 90min at 45 ℃ after, with the working pressure of 0.05MPa, the crossflow velocity of 5m/s cleans 1h.
Cleaning program 2: adopt octane as clean-out system, soak 90min at 45 ℃ after, with the working pressure of 0.05MPa, the crossflow velocity of 5m/s cleans 1h.
Cleaning program 3: first use methyl alcohol as clean-out system, soak 50min at 45 ℃ after, with the working pressure of 0.05MPa, the crossflow velocity of 5m/s cleans 0.5h; Use octane as clean-out system, soak 40min at 55 ℃ after, with the working pressure of 0.05MPa, the crossflow velocity of 5m/s cleans 0.5h again.
Cleaning program 4: first use octane as clean-out system, soak 50min at 45 ℃ after, with the working pressure of 0.05MPa, the crossflow velocity of 5m/s cleans 0.5h; Use methyl alcohol as clean-out system, soak 40min at 55 ℃ after, with the working pressure of 0.05MPa, the crossflow velocity of 5m/s cleans 0.5h again.
Under 4 kinds of conditions, the membrane flux recovery rate calculating is as shown in table 4 respectively.
The recovery rate of table 4 membrane flux
| Cleaning program | 1 | 2 | 3 | 4 |
| Membrane flux recovery rate % | 72 | 65 | 98 | 82 |
As can be seen from the table, when employing scheme 1 and scheme 2, the cleaning performance that adopts polar solvent to pollute for film is slightly better than non-polar solvent, this is due in pollution layer, particularly in filter cake pollution layer, some are contained with the impurity of polarity in surface, can remove, after destroying cake layer, again the pollutent in fenestra is cleaned, non-polar solvent is bad for the pollution cleaning performance of cake layer, cake layer is stayed on film surface, its pollution cleaning performance for fenestra inside is affected.By scheme 3 and scheme 4, can find out, when first adopting polar solvent to clean, clean with non-polar solvent again, can first cake layer be polluted and effectively be removed, make octane more effective in the ensuing cleaning that Pore Blocking is polluted.And if while just first cleaning with non-polar solvent, cause cake layer to be first eliminated, the follow-up cleaning performance that fenestra is polluted is affected.So employing scheme 3 is comparatively suitable, may reach 98% flux recovery.
Claims (10)
- At the bottom of 1.MTO/MTP product separation tower tower, liquid dewaxing deoiling method, is characterized in that, comprises the steps: at the bottom of product separation tower tower that liquid is sent into ultra-filtration membrane to filter, and obtains seeing through liquid and concentrated solution; See through liquid and return product separation tower, concentrated solution is sent into two-phase cyclone separator, obtains water and oil phase, and water is back to ultra-filtration membrane and filters, and after oil phase stratification, obtains oil reservoir and paraffin.
- 2. liquid dewaxing deoiling method at the bottom of MTO/MTP product separation tower tower according to claim 1, is characterized in that: described ultra-filtration membrane is ceramic super-filtering film; The mean pore size of described ceramic super-filtering film is 5～200nm.
- 3. liquid dewaxing deoiling method at the bottom of MTO/MTP product separation tower tower according to claim 1, is characterized in that: the transmembrane pressure of described ultra-filtration membrane is 0.2～0.6MPa.
- 4. liquid dewaxing deoiling method at the bottom of MTO/MTP product separation tower tower according to claim 1, is characterized in that: the crossflow velocity of described ultra-filtration membrane is preferably 0.5～6m/s.
- 5. liquid dewaxing deoiling method at the bottom of MTO/MTP product separation tower tower according to claim 1, is characterized in that: 70～95 ℃ of the service temperatures of described ultra-filtration membrane.
- 6. liquid dewaxing deoiling method at the bottom of MTO/MTP product separation tower tower according to claim 1, is characterized in that: described two-phase cyclone separator pressure drop is 0.05～0.25Mpa; Two-phase cyclone separator inlet velocity is 1～6 m/s.
- 7. liquid dewaxing deoiling method at the bottom of MTO/MTP product separation tower tower according to claim 1, is characterized in that, the purging method of described ultra-filtration membrane is: by membrane module being carried out to polar solvent immersion, washing and non-polar solvent, soak, wash successively.
- 8. liquid dewaxing deoiling method at the bottom of MTO/MTP product separation tower tower according to claim 1, is characterized in that: described polar solvent is selected from methyl alcohol, ethanol, propyl alcohol; Described non-polar solvent is the alkane of C4～C8.
- 9. liquid dewaxing deoiling method at the bottom of MTO/MTP product separation tower tower according to claim 1, is characterized in that: while adopting polar solvent to soak, soaking temperature is 40～50 ℃, soak time 30～60 min; While adopting non-polar solvent to soak, soaking temperature is 50～60 ℃, soak time 40～80 min.
- Liquid dewaxing oil removal plant at the bottom of 10.MTO/MTP product separation tower tower, include ultra-filtration membrane membrane module (3), two-phase cyclone separator (4), layering groove (5), the side of holding back of ultra-filtration membrane membrane module (3) is connected with the entrance of two-phase cyclone separator (4), the top of two-phase cyclone separator (4) is connected with the import of ultra-filtration membrane membrane module (3), and the bottom of two-phase cyclone separator (4) is connected with layering groove (5).
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| CN1397501A (en) * | 2001-07-18 | 2003-02-19 | 中国科学院生态环境研究中心 | Process and equipment for reclaing sewage generated by wiping paper money printing plate |
| CN101962246A (en) * | 2009-07-24 | 2011-02-02 | 中国石油化工股份有限公司 | Method for treating and recycling MTO process wastewater |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107502441A (en) * | 2017-09-06 | 2017-12-22 | 烟台智本知识产权运营管理有限公司 | A kind of lubricating oil mechanical delamination constant temperature dewaxing device |
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Address after: 211806 No. 195 Buyue Road, Pukou Economic Development Zone, Nanjing City, Jiangsu Province Patentee after: Jiangsu Jiuwu High-Tech Co., Ltd. Address before: 211808, No. 9 Hu Dong Road, Pukou Economic Development Zone, Jiangsu, Nanjing Patentee before: Jiangsu Jiuwu High-Tech Co., Ltd. |