US20130299425A1

US20130299425A1 - Process for enhanced total organic carbon removal while maintaining optimum membrane filter performance

Info

Publication number: US20130299425A1
Application number: US13/912,604
Authority: US
Inventors: Gregg A. McLeod
Original assignee: Siemens Water Technologies LLC
Current assignee: H2O Innovation Inc
Priority date: 2007-10-23
Filing date: 2013-06-07
Publication date: 2013-11-14
Also published as: US20100300970A1; US20090101578A1; US8540882B2; US8491788B2

Abstract

One embodiment of a method to system for enhancing TOC removal while maintaining membrane filter performance is the implementation of a dual pH control system. This embodiment will enhance the ability to maximize TOC removal while maintaining optimum membrane filter performance. By adjusting pH, dosing a chemical coagulant and incorporating liquid-solids separation, a considerably higher degree of TOC removal is possible. By adjusting pH again after liquid-solids separation this embodiment can drastically increase the efficiency of the membrane microfiltration/ultrafiltration system.

Thus pH control for soluble organic removal is critical. This pH level however may not be the ideal set point for minimizing membrane fouling which is the basis for this embodiment. An example: the pH set point for optimum soluble organic removal is designated to be 5.5. However, the optimum pH set point for optimum membrane performance is 7.0. This embodiment will show the reader that a two stage approach can accomplish the desired result. Stage 1 involves coagulant dosing, pH control, mixing and liquid-solids separation followed by Stage two which involves pH control, mixing and membrane filtration.

Description

CROSS-REFERENCE TO RELATED APPLICATIONS

Not Applicable

FEDERALLY SPONSORED RESEARCH

Not Applicable

BACKGROUND

Prior Art

Increasingly, municipal drinking, water and wastewater filtration facilities utilize membrane microfiltration or ultrafiltration as a means of filtering ground water, surface water and wastewater sources. Membranes are used as a method to filter or reject organic, inorganic and microscopic particulates. By passing water through a membrane filter barrier under pressure, particulate debris accumulates on the membrane surface. Periodically, the filter will backwash off the contaminants, then return to filtration. Accumulated organic and inorganic contaminants that do not backwash off are removed by chemical cleaning with various chemicals such as chlorine, caustic soda, and various acids. The performance of the membrane is dictated by the “fouling” rate of the influent contaminants. (Fouling is described as the build up of organic and inorganic contaminants on the membrane surface which are not readily removed during periodic backwashing) Numerous contaminants can increase the fouling rate of membranes including Total Organic Carbon (TOC).
Most membrane filtration facilities operate without any additional processes or chemical treatment. Mostly, insoluble contaminants sized larger than 0.04-0.1 microns are filtered or rejected. Solubles or particulates and ions less than 0.04-0.1 microns will pass through the membrane.
This embodiment pertains specifically to the removal of Total Organic Carbon (TOC) utilizing membrane filtration. TOC consists of both soluble and insoluble compounds. TOC levels vary in water supplies from very pristine (low levels of TOC) to very contaminated (high levels of TOC). Higher organic levels will contribute to problems such as taste and odor and Disinfection By Products (DBP). Taste and odor can occur when higher levels of soluble organic compounds are not removed and pass through the membrane filter. DBP's are categorized as Halo Acetic Acids (HAA) and Tri Halo Methanes (THM). HAA's and THM's are created when chlorine reacts with soluble organics to form these regulated compounds. These compounds are formed in the distribution system, which is a collection of underground pipes that deliver filtered water to homes and businesses. Out of compliance DBP's can be controlled by reducing the level of TOC in the raw water. Membrane filtration alone can only remove the insoluble component of TOC. A common method to increase soluble organic removal is to introduce a chemical coagulant into the water stream and provide adequate mixing/detention prior to membrane filtration. Metal salt based coagulants can react via a process known as “charge neutralization” thus precipitating a portion of the soluble organic compounds. The metal base of these coagulants is generally aluminum or iron. Several chemical coagulants can provide this chemical reaction, namely: aluminum sulfate, ferric chloride, ferric sulfate, poly aluminum chloride and aluminum chlorhydrate. Coagulant removal of TOC can be increased by adjusting pH. Generally, the lower the pH, the higher TOC removal. This embodiment provides primary and secondary pH control while incorporating liquid-solids separation and membrane filtration. It has been assumed that the pH set point for a higher degree of organic removal will also be the optimum set point for optimum membrane performance.
Optimum membrane performance can be defined as continuous filtration with 1) lowest pressure rise across the membrane, measured as trans membrane pressure or TMP, and 2) lowest chemical cleaning requirement. Chemicals such as caustic soda, sodium hypochlorite (chlorine), various acids and other chemical products are exposed to the membrane in a clean in place (CIP) and/or maintenance wash procedure to remove the build-up of organic and inorganic compounds. When a coagulant is dosed into a water stream, and the pH is depressed chemically to a desired level and maintained (example: pH: 5.5), a higher level of TOC removal can be achieved.
Presently, all membrane filtration systems heretofore known operate accordingly:
(a) Municipal systems will address additional TOC removal by installing a process after membrane filtration such as
Granular Activated Carbon Adsorption (GAC).
(b) Municipal systems will dose a chemical coagulant prior to membrane filtration without any pH control.
(c) Municipal systems will dose a chemical coagulant and possibly control pH ahead of a liquid-solids separator prior to membrane filtration.
(d) pH will only be controlled for organic removal. It has been assumed that the optimum pH control for organic removal and membrane filtration will be the same.

SUMMARY

In accordance with one embodiment of higher TOC removal while minimizing membrane fouling can be achieved in a two stage process. Controlling pH and coagulant feed prior to liquid-solids separation will substantially increase TOC removal while also improving the separation process. Also, adjusting pH and mixing will substantially increase membrane filter performance.
Adjusting pH prior to said separation of liquids and solids, in addition to said prior treatment, will substantially increase TOC removal and substantially decrease membrane fouling.

DRAWINGS Figures

In the drawing, FIG. 1 shows the complete process.

REFERENCE NUMERALS


10	Raw water flow	12	Flow meter
14	Primary mixing tank	16	Coagulant dosing
18	Primary acid/base dosing	20	Primary rapid mixer
22	Primary maturation Mixer	24	Primary pH probe
26	Separator	28	Secondary mixing tank
30	Secondary acid/base dosing	32	Secondary rapid mixer
34	Secondary maturation mixer	36	Secondary pH probe
38	Membrane microfiltration
	or ultrafiltration system

DETAILED DESCRIPTION—FIG. 1

Preferred Embodiment

One embodiment of the process is the primary coagulant dosing 16, pH control 24 and mixing system 14 illustrated in FIG. 1. (this vessel can be a steel, fiberglass or concrete tank) A chemical metering system 16 (pump) with feed lines doses the coagulant in an automated mode based on flow rate, by receiving a signal from a flow meter 12. A primary chemical metering system 16 (pump) with feed lines doses either acid or base depending on the desired pH set point. A pH probe 24 is installed which sends a signal to a pH set point controller. The probe controls the optimum pH set point by introducing the required acid or base 18. A variable speed mixer 20 is mounted into this tank to provide adequate mixing of the chemical coagulant and pH acid and/or base chemical. This mixer would be a rapid mix type. The chemical mixing system 14 would be divided into a separate compartment which would be mounted with a slower speed flocculation or maturation mixer 22.
Another embodiment of the process is a liquid-solids separator 26. This unit can be one of several types such as a Plate Separator, Sedimentation Tank, Solids-Contact Clarifier, Dissolved Air Flotation Unit or other type separator.
Another embodiment of the process is a secondary pH control and mixing system 28. This vessel can be a steel, fiberglass or concrete tank. A chemical metering system 30 (pump) with feed lines doses either acid or base depending on the desired pH set point. A pH probe 36 is installed which sends a signal to a pH set point controller. The probe controls the optimum pH set point by introducing the required acid or base 30. A variable speed mixer 32 is mounted into this tank to provide adequate mixing of the pH acid or base depending on the desired pH set point. This mixer would be a rapid mix type. The secondary chemical mixing system 28 would be divided into a separate compartment which would be mounted with a slower speed flocculation or maturation mixer 34.
A final embodiment of the process is a membrane microfiltration/ultrafiltration system 38.

Operation—FIG. 1

The process of my invention shows raw untreated water 10 flowing into the first chemical dosing, mixing and pH control system. The author envisions this water source passing through a flow meter 12. This flow meter will send an electronic signal to a coagulant dosing system. This method of “flow rate” coagulant dosing will provide for accurate metering of coagulant. The chemical coagulant is dosed into the primary mixing basin 14 although the author notes that this coagulant could be dosed further upstream of the process. This mixing basin can be a single or multiple mixing zone unit. Multiple mixing zones utilize rapid mixing in the first cell 20 which assists in quickly dispersing the chemical introduced and flocculation or maturation mixing 22 in the second zone which promotes flocculation of chemically precipitated particles. The author notes that other types of maturation mixers are also suitable. pH is controlled in this mixing basin by means of a pH control/monitoring probe 24. This pH probe will send a signal to a pH set point controller which activates a chemical metering pump 18. This chemical feed system can dose either acid or base 18 depending on the pH set point desired.
The water flow then enters the flocculation or maturation mixing zone 22. Another vertically mounted propeller type agitator 22 operates at a lower speed to promote a flocculated particle which can enhance the performance of a liquid-solid separator. The author notes that other types of maturation mixers are also suitable.
Water flows to a liquid-solids separator 26. This unit can be one of several types including a Plate Settler, a Sedimentation Type Clarifier, a Solids Contact Clarifier or Dissolved Air Flotation. Author notes that another type of adsorption unit such as an Ion Exchange Unit could be utilized. Different types of liquid-solids separators can have benefits depending upon the quality of the raw water source. This unit separates the chemically flocculated particles from the water and removes them from the system. Chemically precipitated TOC removal occurs in this unit.
However, the optimum pH of this water will probably be lower than that which would promote optimum membrane performance.
The water flows from the liquid-solids separator 26 to a secondary pH control and mixing system 28 which is similar in operation to the first mixing system 14. The process of pH control and mixing is repeated. pH is controlled in this secondary mixing basin by means of a pH control/monitoring probe 36. The pH probe signal feeds to a set point controller which controls the operation of the chemical feed system 30. This chemical feed system can dose either acid or base 30 depending on the pH set point desired.
Mixing in this basin is achieved via a vertically mounted, propeller type agitator 32. However, the author notes that other types of mixers are also suitable. The water flow then enters the flocculation or maturation mixing zone. Another vertically mounted propeller type agitator 34 operates at a lower speed to promote a flocculated particle which can enhance the performance of a membrane filtration system. The author notes that other types of maturation mixers are also suitable. This mixer may have a variable speed drive to regulate and fine tune membrane filter performance. Water then flows to a membrane filter 38. The membrane filtration system provides the final process step before disinfection and distribution to homes and businesses.

Advantages

From the description above, a number of advantages of some embodiments of my process for organic removal via membrane filtration become evident:
(a) Single pH control to provide for organic removal, liquid-solids separation and membrane filtration does not provide for the most efficient total operating system. By providing a second chemical mixing and pH control system, allows the total system operates more effectively.
(b) By setting a single pH set point which will address coagulant and membrane performance, there will be an efficiency loss for both processes. The primary pH control and mixing system will not only provide for optimum TOC removal but also lower the amount of coagulant required.
(c) The ability to control a desired pH set point for optimum organic removal. Organics precipitate at specific set points.
(d) Since the optimum pH set point for TOC removal will probably be lower than that for membrane filtration.
Example: Higher TOC removal can be achieved by depressing the pH to a range of 5.0-6.0 (sometimes lower depending on water source characteristics). Optimum membrane performance could be achieved at the desired pH set point for finished water sent to distribution to homes and businesses (normally neutral or 7.0 and above). This provides the advantages of fewer pH control adjustments through the process.
(e) pH control and efficient mixing can provide maximum separation at the liquid-solids separator ensuring a higher degree of TOC removal from the system.
(f) A secondary pH control/mixing system will increase the performance of the membrane filtration system including:

- 1. Higher membrane filtration rate.
- 2. Longer membrane filtration intervals.
- 3. Smaller system requirements, lower capital cost.
- 4. Water conservation. Less membrane backwash waste.
- 5. Lower membrane chemical cleaning requirements.
- 6. Longer membrane life.

(g) The process can be set up to provide for gravity flow throughout the process, thus minimizing additional water pumping requirements
(h) The liquid-solids separator and the membrane filtration system can perform positively or negatively depending on flocculation. The flocculation/maturation step allows for optimization by utilizing the variable speed drive.
(i) The process can be a stand aloe system or be in addition to other processes to further enhance the contaminant removal process.
(j) The process can improve membrane filtration performance when incorporating certain types of chemical coagulants that historically have increased fouling, such as ferric chloride and aluminum sulfate.
(k) The process can be utilized with different membrane material types such as polymeric and ceramic membranes.

CONCLUSIONS, RAMIFICATIONS, AND SCOPE

Accordingly, the reader will see that the method for TOC removal and minimal membrane fouling is a two stage process. Stage 1 represents chemical coagulant dosing and pH control to maximize TOC removal via a non membrane type separator. Stage 2 represents pH control prior to final membrane filtration.

Advantages

From the description above, a number of advantages of some embodiments of my treatment process become evident:
a) Stage 1 coagulant addition, pH adjustment and mixing will provide for the highest economical degree of TOC removal.
b) Higher TOC removal will result in lower taste and odor issues related to the final filtered drinking water product.
c) Higher TOC removal will satisfy regulatory requirements for DBP Rules as well as other organic related requirements.
d) Higher TOC removal will result in lower fouling rates on the membrane filtration process
e) Stage 2 pH adjustment and mixing will provide for lower fouling rates on the membrane filtration process.
f) Lower membrane fouling will result in the following benefits

- 1. Higher throughput or flux
- 2. Lower capital cost
- 3. Lower energy requirements
- 4. Longer filter run times
- 5. Less backwash waste, water conservation
- 6. Longer membrane life
- 7. Fewer membrane chemical clean

Although the description above contains many specifities, these should not be construed as limiting the scope of the embodiment but as merely providing illustrations of some of the presently preferred embodiments. For example, the process for maximizing a higher degree of TOC removal and membrane filtration performance can include controlling other constituents in the water stream as well such as alkalinity adjustment, varying types of dual stage chemical coagulants, powdered activated carbon (PAC) dosing, among other examples. Other technologies can be added to this process such as Ion Exchange and Granular Activated Carbon Adsorption. An Ion Exchange process could be added ahead of this process. Granular Activated Carbon Adsorption could be added after this process. The process described can be a stand alone process for drinking water filtration or placed ahead or behind other technologies. The flexibility of the process also allows for newer types of liquid-solids type separators and newer, more advanced membrane materials. Thus the scope of the embodiment should be determined by the appended claims and their legal equivalents, rather than by the examples given.

Claims

1. (canceled)

2. A membrane filtration system, comprising:

a first treatment stage, comprising:

a first mixing tank;

a first pH probe configured to measure a first pH level of water in the first mixing tank;

a metering system configured to disperse a coagulant into the water in the first mixing tank;

a first mechanical mixing device configured to mix the water in the first mixing tank; and

a liquid-solid separator device in fluid communication downstream of the first mixing tank for receiving water from the first mixing tank;

a second treatment stage, comprising:

a second mixing tank, the second mixing tank in fluid communication downstream of the liquid-solid separator device, and configured to receive water that has passed through the liquid-solid separator device;

a second pH probe configured to measure a second pH level of the water in the second mixing tank;

a second mechanical mixing device configured to mix the water in the second mixing tank; and

a membrane filter in fluid communication downstream of the second mixing tank configured to receive water from the second mixing tank,

wherein the second treatment stage comprises no metering system for dispersing a coagulant into the second mixing tank; and

a pH set point control system in communication with the first and second pH probes and configured to:

adjust the first pH level of the water in the first mixing tank, prior to the water being directed through the liquid-solid separator device, to a first pH set point selected for optimum TOC removal in response to a signal from the first pH probe, and to

adjust the second pH level of the water in the second mixing tank, prior to the water being directed through the membrane filter, to a second pH set point selected for optimum performance of the membrane filter in response to a signal from the second pH probe, the second pH set point being higher than the first pH set point.

3. The membrane filtration system of claim 2, wherein the pH set point control system comprises a first acid/base dosing system in fluid communication with the first mixing tank and a second acid/base dosing system in fluid communication with the second mixing tank.

4. The membrane filtration system of claim 2, wherein the first treatment stage further comprises a flow meter for determining a flow rate of water flowing into the first mixing tank, and wherein the metering system for dispersing the coagulant is configured to determine an amount of coagulant to dose based upon the flow rate of the water flowing into the first mixing tank.

5. The membrane filtration system of claim 2, wherein the liquid-solid separator device is selected from the group consisting of a plate separator, a sedimentation tank, a solids-contact clarifier, an ion exchange unit and a dissolved air flotation unit.

6. The membrane filtration system of claim 2, wherein the coagulant is an aluminum or iron metal salt based coagulant.

7. The membrane filtration system of claim 2, wherein the first pH set point is about 5.0 to about 6.0, and wherein the second pH set point is neutral or about 7.0 or higher.

8. The membrane filtration system of claim 2, wherein the membrane system comprises microfiltration or ultrafiltration membranes made of polymeric or ceramic materials.

9. The membrane filtration system of claim 2, further comprising an ion exchange operation upstream of the first treatment stage.

10. The membrane filtration system of claim 2, further comprising a disinfection or a granular activated carbon adsorption operation downstream of the second treatment stage.

11. A process for treating water, comprising:

dispersing an effective amount of coagulant into a volume of water in a first tank;

adjusting a pH level of the water in the first tank to a first pH set point selected for optimum total organic carbon removal;

mixing the water in the first tank;

directing the water at the first pH set point through a liquid-solid separator device and into a second tank downstream of the liquid-solid separator device;

adjusting a pH level of the water in the second tank to a second pH set point selected for optimum performance of a downstream membrane filter, the second pH set point being higher than the first pH set point;

mixing the water in the second tank; and

directing the water at the second pH set point through the membrane filter.

12. The process of claim 11, wherein the dispersing step includes metering the coagulant based upon a signal which corresponds to a flow rate of water into the first tank.

13. The process of claim 11, wherein the effective amount of coagulant is determined based upon the volume, TOC level and temperature of the water in the first tank.

14. The process of claim 11, further comprising suppressing the pH level of the water prior to the coagulant dispersing step.

15. The process of claim 11, wherein the first pH set point ranges from 5.0 to 6.0 standard units and the second pH set point is at least 7.0 standard units.

16. The process of claim 11, further comprising performing an ion exchange operation upstream of the first tank.

17. The process of claim 11, further comprising performing a disinfection or a granular activated carbon adsorption operation downstream of the membrane filter.

18. A process for treating water, comprising:

mixing the water in the first tank;

directing the water at the first pH set point through a liquid-solid separator device and into a second tank downstream of the liquid-solid separator device, wherein no coagulant is dispersed downstream of the liquid-solid separator device;

adjusting a pH level of the water in the second tank to a second pH set point selected for optimum performance of a downstream membrane filter;

mixing the water in the second tank; and

directing the water at the second pH set point through the membrane filter.

19. The process of claim 11, wherein the effective amount of coagulant is determined based upon the volume, TOC level and temperature of water in the first tank.

20. The process of claim 2, further comprising suppressing the pH level of the water prior to the coagulant dispersing step.