METHOD FOR FOULING REDUCTION ON THE SURFACE OF CERAMIC MEMBRANES USING STEAM FAST-FLUSHING

Abstract

The inventions discloses a method for reducing fouling on the surface of a ceramic membrane or filter with a recalcitrant filtration cake thereon that is non-responsive to regular back-flushing or other physical means of removal, where the ceramic membrane or filter is subjected to steam fast-flushing by injecting steam directly in feed channel of the ceramic membrane or filter while back-flushing the ceramic membrane or filter at the same time to heat and remove fouled layer on the ceramic membrane or filter while cooling a selective layer of the ceramic membrane or filter to avoid thermal shocking of the ceramic membrane or filter, the surface is cleaned with the ceramic membrane or filter being stationary.

Claims

1. A method for reducing fouling on the surface of a ceramic membrane or filter, the ceramic membrane or filter has a recalcitrant filtration cake on its surface that is non-responsive to removal by regular back-flushing or other physical means of removal, wherein the ceramic membrane or filter is subjected to steam fast-flushing by injecting steam directly in feed channel of the ceramic membrane or filter while back-flushing the ceramic membrane or filter at the same time to heat and remove the fouled layer on the ceramic membrane or filter while cooling a selective layer of the ceramic membrane or filter to avoid thermal shocking of the ceramic membrane or filter, wherein the surface of ceramic membrane or filter is cleaned with the ceramic membrane or filter being stationary.

2. The method of claim 1, wherein a permeate is resulted from fluid that has initially passed through ceramic membrane or filter, and wherein the selective layer of the ceramic membrane or filter is back-flushed and cooled by a difference in pressure of the permeate and a depressurized feed stream.

3. The method of claim 1, wherein the steam is injected in the feed channel from the top of a module of the ceramic membrane or filter, and wherein the feed channel at the bottom of the ceramic membrane or filter is connected to a feed tank.

4. The method of claim 1, wherein the steam is injected in the feed channel without isolating a module from a circulation loop.

5. The method of claim 1, wherein the steam cleaning process is performed on a membrane that is not in a feed and bleed loop.

6. The method of claim 1, wherein the selective layer of the ceramic membrane or filter is back-flushed and cooled by the difference in pressure of the permeate and the depressurized feed stream.

7. The method of claim 1, wherein the ceramic membrane or filter is in the form of a flat sheet, multi-pleated sheet, a single tubular lumen or multi-lumen tube.

8. The method of claim 1, wherein material of ceramic membrane or filter and its support is a ceramic.

9. The method of claim 8, wherein the ceramic is one selected from an oxide of aluminium, titanium, zirconium, or mixtures thereof.

10. The method of claim 1, wherein material in the selective layer of the ceramic membrane or filter is different from the membrane support material.

11. The method of claim 1, wherein material in the selective layer of the ceramic membrane or filter is identical to the membrane support material.

12. The method of claim 1, wherein material of the ceramic membrane or filter membrane is a ceramic and its support is a metal.

13. The method of claim 12, wherein the ceramic is one selected from an oxide of aluminium, titanium, zirconium, or mixtures thereof.

14. The method of claim 1, wherein the filter is metallic, the pore size is 0.1 to 1000 microns.

15. The method of claim 1, wherein the pore size of the ceramic membrane or filter is 1 nm to 10 microns.

16. The method of claim 1, wherein the ceramic membrane or filter is inorganic.

17. The method of claim 1, wherein the ceramic membrane or filter is a sintered inorganic.

18. The method of claim 1, wherein the recalcitrant filtration cake is formed in treating any wastewater.

19. The method of claim 1, wherein the recalcitrant filtration cake is formed in treating oily wastewater.

20. The method of claim 1, wherein the recalcitrant filtration cake is formed in treating bituminous and oily wastewater.

21. The method of claim 1, wherein the recalcitrant filtration cake is formed in treating steam assisted gravity drainage (SAGD) produced water or process water.

Description

BRIEF DESCRIPTION OF THE DRAWINGS

[0036] By way of example only, preferred embodiments of the present invention are described hereinafter with reference to the accompanying drawings, wherein:

[0037] FIG. 1 is a flow diagram according to an embodiment of the present invention showing a membrane loop equipped with valves for steam fast-flushing and permeate back-flushing.

[0038] FIG. 2 is a graph showing permeate flux and operating pressure versus time for two membranes treating SAGD process water according to the present invention.

DETAILED DESCRIPTION OF THE INVENTION

[0039] It is to be understood that the disclosure is not limited in its application to the details of the embodiments as set forth in the following description. The invention is capable of other embodiments and of being practiced or of being carried out in various ways.

[0040] Furthermore, it is to be understood that the terminology used herein is for the purpose of description and should not be regarded as limiting. Contrary to the use of the term “consisting”, the use of the terms “including”, “containing”, “comprising”, or “having” and variations thereof is meant to encompass the items listed thereafter and equivalents thereof as well as additional items. The use of the term “a” or “an” is meant to encompass “one or more”. Any numerical range recited herein is intended to include all values from the lower value to the upper value of that range.

[0041] Oil production operations produce a large amount of oily wastewaters that contain ultrafine clay particles, solvents, resins, bitumen and other complex organics. These mixtures of fine particulates combined with oils and bitumen is particularly difficult to treat. When such a mixture is treated by traditional membrane filtration, fouling deposits form on the surface of the membrane. These deposits must be removed by chemical or physical means. The deposits can be removed with solvents or detergents; however this method produces cleaning and rinse wastewaters that must be disposed of.

[0042] Alternatively, the deposits can be removed by physical means; where permeate (fluid that has initially passed through the membrane) is pressurized and forced back through the pores of the membrane. This flow reversal is effective in removing deposits or filter cakes on the surface of the membrane when the cakes do not adhere to its surface or do not form structured networks that reinforce the cake.

[0043] Filter cakes containing materials that can coalesce and bridge can form cakes having very low permeabilities. An example of such cakes is observed when wastewaters containing fine particles, oil and bitumen are treated such as in the recycling of SAGD process waters. These cakes are also found in oil and gas operations, flotation mining, food chemical, and biotech industries to name a few. In many cases, the presence of a high concentration of suspended solids and the possibility of ionic binding or the slight polymerization of species in the cake makes them quite recalcitrant.

[0044] These recalcitrant filter cakes are difficult to back-flush and gradually increase in thickness which greatly reduces permeate flow through the membrane. The resistance of these cakes to flow is extremely high and the flux of the membrane eventually decreases to a level where the operation of the system comprising the membrane is no longer economical.

[0045] In addition to this problem, it is advantageous to treat process waters at a high temperature when they originate from operations where steam is used in the extraction process. This has the advantage of treating the wastewater when its viscosity is reduced at the higher temperatures of 80 to 100° C. and to eliminate the cooling requirements needed prior to treatment when conventional membrane materials are used in the treatment process. Avoiding the need to cool and then reheat the wastewater reduces the CO.sub.2 emissions of the oil production process.

[0046] The present invention discloses the use of two simultaneous physical approaches in order to reduce the accumulation of oily particulates and bitumen on the surface of the ceramic membrane and remove recalcitrant cakes from its surface.

[0047] According to the present invention, the recalcitrant filter cake is directly heated using steam, while back-flushing the membrane with permeate.

[0048] This is done by decoupling the membrane module from the loop and injecting steam directly on the feed side of the membrane.

[0049] The outlet of the feed channel is open to atmosphere and permits the fast-flushing of the feed channel with steam. This rapid heating of the filter cake prevents the selected layer of the membrane from being exposed to a sudden heat transient that could crack the ceramic selective layer.

[0050] Fast-flushing has a scouring effect on the surface of the membrane. The initial cake released in the feed channel accumulates as a plug that scours and cleans the inside of the membrane lumen while permeate back-flushes the selected layer of the membrane to remove the cake and cool the surface of the membrane. These combined effects permit the continuous operation of the membrane system at flux levels that is 3 to 4 times that of non-steam back-flushed systems.

[0051] By combining these two actions, steam above 100° C. can be used to heat treat a membrane system operating at 80° C. The viscosity of bitumen decreases substantially with increasing temperature. The advantage of using direct steam injection is seen by the reduction in viscosity of the bitumen found in processed water filter cakes.

[0052] Table 1 below lists the viscosity of Athabasca bitumen as a function of temperature. When increasing the temperature from 20 to 80° C., the viscosity is reduced 1333 times and when increasing the temperature from 80 to 126° C., the viscosity is reduced 23 times.

TABLE-US-00001 TABLE 1 Viscosity of Athabascan Bitumen as a Function of Temperature Viscosity Temp C. Pa .Math. s  20° C. 4000  80° C. 3.0 1333 times lower than at 20° C. 126° C. 0.13  23 times lower than 80° C.

[0053] The reduction that facilitates the removal of the filter cake accumulated on the surface of the ceramic membrane. The selective layer of the membrane however, must not be exposed to heat transients as it may crack.

[0054] Heating of the selective layer while back-flushing was achieved using a system shown in FIG. 1. The system is meant to be an illustrative and non-limiting example.

[0055] Referring to FIG. 1, the system comprises a feed and bleed loop with a membrane module 1, a membrane 2, a circulation pump 3, a feed pump 4, and seven (7) pneumatically actuated valves V1 to V7. Membrane concentrate accumulating in the loop is continuously returned to the feed tank by a separate bleed line (not shown in FIG. 1) connecting the circulation loop to the feed tank.

[0056] Under normal operation, valves V2, V3, V5 and V7 are closed; and valves V1, V4 and V6 are open.

[0057] For steam fast-flushing, at first, membrane module 1 is isolated from the process loop by closing valves V1, V6 and opening valve V7.

[0058] Valves V2 and V5 are then opened and steam is injected directly in the feed channel of membrane module 1 and sent to a feed tank.

[0059] In one instance, permeate is back-flushed at 80 psi by closing valve V4 and opening valve V3.

[0060] In another instance, valves V3 and V4 are closed and the permeate is back-flushed naturally, as the feed channel is depressurized from 50 psig to 0 psig.

[0061] The outlet of the feed channel of module 1 is open to atmosphere allowing for the return of the filter cake to the feed tank. The feed tank is blanketed with an inert gas and kept at atmospheric pressure.

[0062] After steam fast-flushing, the system is returned to its normal operation by closing valves V2, V3, V5 and V7 and opening V1, V4 and V6.

[0063] An example of the benefits of this process is provided in FIG. 2 where two membranes, placed in parallel in a circulation loop, treated a feed obtained from a steam assisted gravity drainage (SAGD) operation in Alberta Canada.

[0064] The arrangement of the valves is identical for both membrane modules. Only one membrane module with its set of valves is shown in FIG. 1. The membrane is a multi-lumen ceramic tube 2.5 cm in diameter with 19-3.5 mm diameter lumens. Over 2000 liters of SAGD produce water were treated using membranes made from alumina and titania.

[0065] The membranes have the following characteristics: pore size 5 nm, selective layer TiO.sub.2 and support layer Al.sub.2O.sub.3 (Ti—Al) or pore size 5 nm, selective layer TiO.sub.2 and the support layer TiO.sub.2 (Ti—Ti).

[0066] The flux of both membranes in Litres/m.sup.2/h (Lmh) and the operating pressures with time are shown in FIG. 2.

[0067] FIG. 2 illustrates 7 days of operation at 4 h/day. Steam fast-flushing was performed every 15 minutes of the run while conventional permeate back-flushing was performed on the membranes at five-minute intervals between steam fast-flushing.

[0068] The first part of FIG. 2, 0 to 7.2 hours, represents the flux when no steam fast-flushing was performed and conventional permeate back-flushing was performed every 5 minutes.

[0069] The second part of FIGS. 2, 7.2 to 15.5 hours, represents the flux when steam fast-flushing was performed every 15 minutes and conventional permeate back-flushing performed every 5 minutes.

[0070] The third part of FIG. 2, from 15.5 to 17.5 hours, represents the flux when no steam fast-flushing was performed and conventional permeate back-flushing performed every 5 minutes.

[0071] The final section of FIGS. 2, 17.5 to 26 hours, represents the flux when steam fast-flushing was performed at every 15 minutes and conventional permeate back-flushing performed every 5 minutes.

[0072] The effect of steam fast-flushing on permeate flux is shown. It successfully increased the permeate flux by of 150 Lmh for the Ti—Al membrane and 120 Lmh for the Ti—Ti membrane.

[0073] On average for both membranes, with conventional permeate back-flushing (without steam fast-flushing), the permeate flux rapidly declined to 48 Lmh, which is well below the acceptable limit for the economical operation a ceramic membrane in treating oily wastewater.

[0074] With steam fast-flushing, the permeate flux was maintained at a level above 156 Lmh. This represents a 3.2-time improvement in permeate flux.

[0075] In another scenario, membrane module 1 is not isolated from the process loop for the steam fast flushing operation. Here valves V3, V5 and V7 are closed; and valves V1, V4 and V6 are open.

[0076] The circulation velocity in the loop is decreased and steam injected directly in the feed channel of the membranes via valve V2. The surge in pressure on steam injection is accounted for by sufficient vapor or inert gas space in the loop (not shown).

[0077] The filter cake released from the surface of the membrane is integrated into the contents of the loop and exits via the bleed line of the loop.

[0078] Permeate is back-flushed at a pressure greater than the loop pressure by closing valve V4 and opening valve V3.

[0079] The steam fast-flushing process is a clean in place method, as the modules are not removed from the system in order to clean them. No cleaning wastewaters or residues are produced as the cake from the steam fast-flushing process is recycled to the feed tank of the membrane loop.

[0080] The present invention provides a significant advantage in operating a membrane system particularly in remote areas where cleaning fluids produced when the membranes are chemically cleaned would have to be trucked out and treated off-site. The combination of heating the selective surface of the membrane while back-flushing with permeate offers the continuous and optimal removal of the bituminous cake without the use of chemical cleaning.

[0081] While the present invention has been described in considerable detail with reference to certain preferred and/or exemplary embodiments, it will be understood by those skilled in the art that various changes may be made and equivalents may be substituted for elements thereof without departing from the scope of the invention. In addition, many modifications may be made to adapt a particular situation or material to the teachings of the present invention without departing from the essential scope thereof. Therefore, the scope of the appended claims should not be limited by the preferred embodiments set forth in the examples, but should be given the broadest interpretation consistent with the description as a whole.