Treatment and Energy Recovery for Municipal Waste Water Using Forward Osmosis Process
Table of Contents
Abstract
TREATMENT AND ENERGY RECOVERY FOR MUNICIPAL WASTE WATER USING FORWARD OSMOSIS PROCESS
Background and motivation
Method
Future Work
References
Footnotes
Tables
Figures
Abstract
Treatment of wastewater has become necessary and treatment using membrane is flourishing widely. Forward osmosis process is one such process. The main aim of this study is to investigate wastewater treatment system using forward osmosis membrane. The research reveal a proof study on the feasibility of forward osmosis membrane in two ways: (1) to treat municipal wastewater and (2) to concentrate wastewater for energy recovery using algae biomass. The results will demonstrate how wastewater/seawater forward osmosis system would operate and show the operational cost.
Keywords: Wastewater, forward osmosis, treatment, energy
Treatment and Energy Recovery for Municipal Waste Water Using Forward Osmosis Process
Introduction
Modernization is the reason for both – development as well as environmental problems. Swelling numbers of effluents in wastewater has become a global issue. Handful of freshwater resources are not enough to feed increasing population demand. Thus need for wastewater treatment has become necessary. Conventional wastewater treatment plants are designed for treating household and industrial wastewater and to protect environmental from its adverse effect.
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Nowadays many treatment techniques like adsorption, activated sludge, ultrafiltration, coagulation have been applied to treat the wastewater. Membrane separation is an innovative way of treating wastewater. Forward osmosis membrane helps to concentrate suspended solids and nutrients in wastewater. Osmosis is a process in which water passes through the semipermeable membrane to balance the solute concentration. Using FO membrane to treat municipal wastewater is an innovative way which could help to achieve the same results as that of tertiary and advanced treatment (McGinnis and Elimelech 2007; Cornelissen 2008; Achilli 2009). Moreover, FO is a suggested method for algae biomass production and treat wastewater simultaneously if incorporated together (Buckwalter 2013; Wang 2016). Algae produce more energy per area and use less water than terrestrial crops; but, the infrastructure necessary to produce and harvest microalgae is still expensive (Demirbas 2011).
Objective
The objective of this study is to determine the feasibility of forward osmosis process into wastewater treatment plant and harvest algae at the same time. This study proposes a treatment process to harvest the algae with forward osmosis membrane to both create a byproduct revenue and reduce environmental problem caused due to effluents in wastewater. The osmosis system will harvest the algae by utilizing the osmotic gradient between seawater and wastewater.
Municipal Wastewater Treatment
Every day, millions of cubic meter of wastewater from homes, institutions, commercial and industries is flushed into the sewer system. Municipal wastewater contain sanitary sewage and sometimes it even contain stormwater. Municipal wastewater is one of the largest source of pollution in water in Canada (Government of Canada).
Figure:1 Water treatment level 1983 – 2009.
(Adopted from Municipal wastewater treatment- Canada)
The operating condition and methodology depends on the level of effluents. Pretreatment, Primary treatment, secondary treatment, tertiary treatment and haulage are the main treatment process followed by the wastewater treatment plants. The percentage of Canadians on municipal sewers with secondary treatment has improved from 40% in 1983 to 69% in 2009, which is approximately 18% done by primary treatment and 13 % by household septic tanks (Government of Canada). Pretreatment removes solid particles while primary treatment reduces the amount of organic solids and inorganic solids.
Compared to these process the secondary treatment and advanced treatment methods require more energy as they have to remove phosphorous, nitrogen and organic matter up to certain extent. Biological treatment is a part of secondary treatment in which dissolved oxygen is added to remove organic impurities by removing impurities and disinfecting them. Usually, secondary process are designed in such a way that it remove 20-35% 0f nitrogen and 80-95% of BOD5 from wastewater.
Tertiary and advanced treatment methods remove the remaining suspended solids and pathogenic microorganisms.
Forward osmosis
Various methods are being studied for the treatment of wastewater; out of which osmotic membrane technology is being researched to produce energy and desalinate water. The phenomenon of forward osmosis occur when water begin to move from feed solution to draw solution to reach osmotic equilibrium. Here the municipal wastewater is termed as feed solution and seawater as draw solution. Feed solution has low osmotic pressure while the draw solution has high pressure. FO do not require any hydraulic pressure as an input energy, instead it work on osmotic pressure of the solution which create osmotic gradient. The membrane separates the two solution and behaves as a physical barrier for suspended solids and many salts. The figure below shows a the flow of the forward osmosis process.
Figure 2: Flow of forward osmosis process
Forward Osmosis Theory
Assume that the following equation completely rejects the feed and draw solute and water transport through a FO membrane is generally described as:
JW = A(D,b – F,b)
Where,
Jw is the water flux
A is the pure water permeability of the membrane
D,b is the bulk osmotic pressure of draw solution and,
F,b is the bulk osmotic pressure of the feed solution.
The bulk osmotic pressure is given by Van’t Hoff equation for both the solution:
= Rg T i M
Where,
Rg is a gas constant
T is the temperature in Kelvin
I is the Van’t Hoff factor for specific ion
M is the molarity of the specific ion.
Concentration polarization
As water passes through the membrane, the surface of the membrane is blocked by the solute facing the feed solution which cause the pressure on the surface of the feed solution to be larger compared to the osmotic pressure of the bulk feed solution. This phenomenon is termed as concentrative external concentration polarization for a dense symmetric membrane ( McCutcheon and Elimelech 2007). It is given by
Jw = A( D,b – F,b exp (Jw,e/ Kf))
The exponential term is the concentrative ECP modulus and is the function of Jw,e .
Jw,e is water flux and Kf is the mass transfer coefficient on the feed side of the membrane.
On the draw solution side of the membrane dilutive ECP takes place. The water that passed through the membrane weakens the effective draw solution osmotic pressure at the membrane surface. The equation for the combination of both the phenomena is given as under:
Jw = A(D,b exp (-Jw,e/ KD) – F,b exp (Jw,e/ KF))
Where,
KD is the mass transfer coefficient on the draw solution side of the membrane.
The negative sign at the dilutive ECP modulus indicates the reduction of the osmotic pressure on the draw solution side. The above equation is for dense symmetric membrane while FO system works effective using asymmetric membrane i.e., porous support layer and dense layer. However, in FO the concentration inside the membrane has larger effect on water flux.
Internal concentration polarization (ICP) is caused when the salts get accommodated in the porous support layer. The draw solution is in contact with the porous layer. The salt which is on porous layer should allow to generate the osmotic driving force. Once it is generated the water will pass through the membrane and as a result it will decrease the concentration of the draw solution. The dilutive effect in the membrane is referred to as dilutive ICP and is given as:
Jw = A(D,b exp (-Jw,e KD) – F,b exp (Jw,e/ KF))
Where,
exp (-Jw,e KD) is the dilutive ICP modulus and,
k is the resistance to the diffusion by the solute
Solute Transport
In ideal case of forward osmosis membrane completely block the way of salts; but with current FO reverse salt diffusion is going to happen. Due to this, it is increases the risk to the economy of industrial FO system. If NaCl transfer across the membrane it will be against the strict water quality standards. Furthermore, the bidirectional transfer of the solutes must be considered. For an example, the transfer of solutes like pathogens and other organic compound from wastewater treatment to treated salt water may not meet the water quality standards. An equation to predict the amount of reverse salt diffusion is given by (Philip and Yong 2010):
Jw / Js = A/B nRgT
Where,
Js is the total draw solute flux
B is the draw solute permeability coefficient
N is the number of dissolved species
Fouling concerns
Membrane fouling is a general problem in FO. It occur mainly due to two reasons (1) organisms use the membrane to attach themselves to (2) due to hydrodynamic force of an osmosis system foultants are drawn into membrane. It decreases the speed of flow rate across the membrane. There are several ways to reduce the effect of fouling like backflushing, increasing the cross-section area, pretreatment and chemical cleaning.
Recent Developments and advantages
Treating complex water like municipal wastewater using forward osmosis membrane has increased over 12 years (Cath 2006; Achilli 2009; Buckwalter 2013 and Ansari 2017). Many of the significant discoveries related to the wastewater treatment using FO membrane and algae separation as described below.
(1) No need for pre-treatment
(2) Low energy required due to lack of hydraulic pressure needed.
(3) As the pore radius is between 0.25-0.37 nm, there is high rejection of salt, pathogens and TDS.
(4) The process holds excellent working records in terms of durability and water quality.
(5) The process is easy to apply and very flexible.
(6) Membrane replacement rates are less
Disadvantages
(1) Low water fluxes and reverse salt diffusion
(2) Incomplete rejection of organic contaminants
(3) Low water flux
Bioenergy from algae
Microalgae have a simple cellular structure. They are the plants which do not have roots, stems and leaves containing chlorophyll. Algae carry out photosynthesis by using solar system to split water and fix carbon dioxide which gives oxygen and storable chemical energy as output. Microalgae have the potential to decrease the water footprint of biofuel production.
Figure 3: Comparison of microalgae’s footprint to other crops
(adapted from Yang, 2011)
According to new findings algae biofuel could compete with conventional energy production if wastewater is utilized as water resource. Anaerobic digestion is a biological process used to convert biodegradable materials into methane and carbon dioxide. Compared to normal electricity production costs, anaerobic digestion of microalgae using wastewater produce energy at high cost.
During the process, the organic material is broken down into insoluble organic polymers. Acidogenic bacteria break the sugars and amino acids into carbon dioxide, ammonia, hydrogen and organic acids. Acidogenic bacteria further breaks organic acids into ammonia and carbon dioxide. Lastly, methanogens convert the remaining products into carbon dioxide and methane that can be used for bioenergy production.
Bioenergy produced from wastewater has two benefits. (1) Sufficient concentration of nitrogen, phosphorous, carbon, etc. are present in the abundant amount in wastewater.
(2) There is no need to construct a new infrastructure to transport wastewater to centralized wastewater treatment plant.
The only drawback of this process is to use algae to supply oxygen and remove nutrients is the removal. According to a study 20-40% of the total algae production cost is due to separation of algae from its aqueous environment ( Grima 2003; Pragya, Sahoo 2013). Harvesting microalgae by FO might be less expensive than other methods, only if the leakage through membrane is controlled and seawater is readily available (Buckwalter 2013).
Method
This section describes the source of data, the necessary assumptions and the economic theory to study the feasibility of the process economically.
Forward osmosis system
Forward osmosis process have following components: a housing structure, feed pumps, storage tanks, flush pumps, FO membrane, valves, piping structure, hangers, FO instrumentation and control system. The FO system was designed based on the advanced treatment system using the reverse osmosis for the wastewater treatment (AWP 2013). The working of the system is shown below by flow diagram.
Wastewater is termed as feed solution and the seawater is termed as a draw solution. Both the solution enter the FO system and are stored in a tank so that the flow is gravitational flow. To prevent both the solutions sulfuric acid and antiscalant is added to them. Feed pumps are used to pump both solutions across the forward osmosis membranes. We get diluted seawater or a concentrated algae when both the solution exit the membrane. Once a month, the flush pumps are used to remove fouling from the membrane. The figure below shows the flow diagram of forward osmosis system.
Figure 4: Flow diagram of forward osmosis process.
(Adapted from thesis by Patrick Buckwalter, 2017)
Assumptions, parameters and cost
System operation parameters
System parameter
Value
Units
Reference
System size
1
MGD
Plant life
20
years
Forward osmosis operating inputs
System parameter
Value
Units
Reference
FO membrane replacement
5
years
Linares, 2016
Membrane water Flux
5
L m-2 hr-1
Wang, 2016
Usable membrane module area
9
m2
Kim, 2015
Concentration factor
5
n/a
Wang, 2016
Feed/ Draw flow rate
ratio
1:1
n/a
Hancock and Cath, 2009
Membrane cleaning rate
2
#/month
Wang, 2016
Energy consumption
0.23
kWh/m3
Jackson, 2014
Capital Cost assumption
System parameter
Value
Units
Reference
Membrane cost
$56
m-2
Forward Osmosis Facility structure
$2,653,680
21.2 MGD
AWP 2013
FO feed pump
$1,153,144
21.2 MGD
AWP 2013
FO Flush pump
$96,847
21.2 MGD
AWP 2013
Tank
$191,517
21.2 MGD
AWP 2013
Hangers and supports
$127,910
21.2 MGD
AWP 2013
Valves
$634,422
21.2 MGD
AWP 2013
Piping
$132,652
21.2 MGD
AWP 2013
Instrumentation and controls (I & C)
8
%
AWP 2013
Permitting
$25,000
4 MGD
Lundquist, 2010
Mobilization/ demobilization
$452,500
4 MGD
Lundquist, 2010
Construction Insurance
$181,500
4 MGD
Lundquist, 2010
Engineering, Legal & Administration
$317,500
4 MGD
Lundquist, 2010
Construction Management
$545,000
4 MGD
Lundquist, 2010
Contingency
$452,500
4 MGD
Lundquist, 2010
Annual Operation Cost Assumptions
System parameter
Value
Units
Reference
FO Feed Pump
$333,301
21.2 MGD
AWP 2013
FO Flush pump
$178
21.2 MGD
AWP 2013
Antiscalant Feed pump
$1,119
21.2 MGD
AWP 2013
Sulfuric acid feed pump
$1,119
21.2 MGD
AWP 2013
Antiscalant
$132,359
21.2 MGD
AWP 2013
Sulfuric Acid
$298,191
21.2 MGD
AWP 2013
Maintenance cost
$851,458
21.2 MGD
AWP 2013
Labor cost
$1,418,271
21.2 MGD
AWP 2013
Economic rate assumption
System parameter
Value
Units
Reference
Electricity cost
$0.12
kWh
AWP 2013
Inflation rate
3
%
Hickenbottom, 2015
Discount rate
6
%
Gomez 2011
All the above tables are taken from the thesis presented by Patrick Buckwalter.
Cost analysis of FO system
The main assumption in the design is that it is similar to the design of reverse osmosis process. The components which are necessary in RO for hydraulic pressure are omitted. System design, operational costs and membrane componentry are proposed based on advanced water purification facility study report (AWPFSR) using reverse osmosis process (AWP 2013).
FO membrane cost is taken as $1500 per 27 m2 (Linares 2016).
Cost of the membrane (FO cost) = AFO Cm
Where, AFO is the area of membrane
Cm is the cost of membrane per square meter.
Membrane area can be given as:
AFO = QFS / Jw
Where, QFS is the membrane permeation rate of feed solution
Jw is the water flux through the membrane.
Costs associated with the pumping and pretreatment were taken double the cost of reverse osmosis process as the FO system require two flow streams across the membrane.
Cost of construction, engineering, permitting, legal, Construction management was taken from a report by Lundquist, 2010.
Results and discussion
Initial capital cost of the FO system was about $3.2 million dollars per million gallons of capacity. It is broken down into various compartments. Membrane cost is the largest cost contributor with $2,000,000 for 32,000 m2 of membrane. Indirect costs include engineering, construction, legal and administration.
Figure 5: Capital cost components for forward osmosis system (Buckwalter, 2017)
Annual operational cost for the system is about $600,000 per one million gallons of the capacity per year. Osmosis replacement cost is largest contributor to annual operations cost. Compared to other technologies like microfiltration, activated carbon; FO provides an estimated cost of construction, operation and maintenance.
Figure 6: Operational cost break down of forward osmosis system (Buckwalter, 2017)
Conclusion
Forward osmosis process is not only an advanced wastewater treatment technology but it can simultaneously harvest algae for biofuel and reduce the volume of the wastewater. The FO facility was found to have a lifecycle cost of approximately $10 million/MGD of feed solution.
All in all, forward osmosis concept using feed and draw solution can be considered as a future wastewater treatment concept.
Future Work
Following is the future work to be carried out for this system:
(1) To remove the total nitrogen demand for large wastewater treatment plants, the solute rejection of ammonium should be rejected and for that membrane improvement becomes necessary.
(2) Mechanical pre-treatment for the FO process should be investigated for its operational and economic advantages and disadvantages.
References
Achili, Andrea and Amy Childress. 2009. ‘The forward osmosis membrane bioreactor: a low fouling alternative to MBR processes’ Desalination.
Ansari, Ashley J, William E Price, Jorg E Drewes, and Long D Nghiem. 2017
‘Forward osmosis as a platform for resource recovery from municipal wastewater’ Journal of membrane science.
Advanced Water Purification Facility Study Report (AWP), San Diego Water Purification Demonstration Project. 2013. ‘ Indirect Potable Reuse/ Reservoir Augmentation Demonstration Project Advanced Water Purification Facility.’
Buckwalter, Patrick; Shrewin Gormly, and Jonathan D Trent. 2013. ‘ Dewatering microalgae by forward osmosis’, Desalination.’
Buckwalter, Patrick. 2017. ‘Forward osmosis for Wastewater Treatment and energy recovery.’
Cath, Tzahi y, Amy E Childress, and Menachem Elimelech. 2006.’ Forward osmosis: Principles, applications, and recent developments’, Journal of membrane science.
Cornelissen, ER, CJ Ruiken, Jian-Jun Qin, H Oo, and LP Wessels. 2008. ‘ Membrane fouling and process performance of forward osmosis membranes on activated sludge’, Journal of membrane science.
Demirbas, Ayhan, and M Fatih Demirbas. 2011. ‘Importance of algae oil as a source of biodiesel’, Energy conservation and management.
Gomez, J. 2011 ‘ Assessment of osmatic Mechanisms Pairing Desalination Concentrate and Wastewater treatment’, Texas Water Development Board.
Grima, E Molina, A Robles Medina, and Yusuf Chisti. 2003. ‘ Recovery of microalgal biomass and metabolites: process option and economics’, Biotechnology Advances.
Hancock and Cath. 2009. Solute coupled diffusion in osmotically driven membrane processes’, Environmental science and technology.
Hickenbottom and Tzahi Y Cath. 2015. ‘Assessing the current state of commercially available membranes and spacers for energy production with PRO: An experimental investigation’, development and assessment of a novel osmotic heat engine for energy generation from low-grade heat.
Jackson, M., 2014. Evaluation of an osmotic dilution process for tertiary wastewater treatment. Master Thesis, Humboldt State University.
Kim, Jung Eun, Sherub Phuntsho, Fezeh Lotfi, and Ho Kyong Shon. 2015. ‘Investigation of pilot-scale 8040 FO membrane module under different operating conditions for brackish water desalination’, Desalination and Water Treatment.
Linares, Rodrigo Valladares, Zhenyu Li, Muhannad Abu-Ghdaib, Chun-Hai Wei, Gary Amy, and Johannes S Vrouwenvelder. 2013. ‘Water harvesting from municipal wastewater via osmotic gradient: an evaluation of process performance’, Journal of membrane science.
Lundquist, Tryg J, Ian C Woertz, NWT Quinn, and John R Benemann. 2010. ‘A realistic technology and engineering assessment of algae biofuel production’, Energy Biosciences Institute
McCutcheon, Jeffrey R, Robert L McGinnis, and Menachem Elimelech. 2005. ‘A novel ammonia-carbon dioxide forward (direct) osmosis desalination process’, Desalination.
Phillip, William A, Jui Shan Yong, and Menachem Elimelech. 2010. ‘Reverse draw solute permeation in forward osmosis: modeling and experiments’, Environmental science & technology.
Pragya, Namita, Krishan K Pandey, and PK Sahoo. 2013. ‘A review on harvesting, oil extraction and biofuels production technologies from microalgae’, Renewable and Sustainable Energy Reviews.
Wang, Zhiwei, Junjian Zheng, Jixu Tang, Xinhua Wang, and Zhichao Wu. 2016. ‘A pilot-
scale forward osmosis membrane system for concentrating low-strength
municipal wastewater: performance and implications’, Scientific reports
Yang, Jia, Ming Xu, Xuezhi Zhang, Qiang Hu, Milton Sommerfeld, and Yongsheng
Chen. 2011. ‘Life-cycle analysis on biodiesel production from microalgae: water
footprint and nutrients balance’, Bioresource technology.
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