In this lesson we will learn about the thermodynamics and kinetics of microbe-mediated redox reactions, the biogeochemical redox ladder in natural systems, and setting up microbe-mediated reactions in well-mixed batch reactors.
By the end of this lesson, you should be able to:
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If you have any questions, please post them to our Questions? discussion forum (not e-mail), located in Canvas. The TA and I will check that discussion forum daily to respond. While you are there, feel free to post your own responses if you, too, are able to help out a classmate.
Microorganisms are everywhere in the Earth surface environment. Their presence has significant influence in the natural and engineered environments. They play a key role in the biogeochemical cycling of elements such as carbon (C), oxygen (O) and nitrogen (N). For example, primary production involves photosynthetic microorganisms that transform CO2 in the atmosphere into organic (cellular) materials of vegetation in terrestrial systems. Planktonic algae and cyanobacteria on the other hand, are the “grass of the sea”. They account for ~ 50% of the primary production on the planet and are the primary carbon source for marine life. The fixation of N from the N2 gas also occurs through N-fixing microorganisms. Microorganisms are believed to be critical in the origin of life and in the transformation of rocks to soils that create life-accommodating environments on Earth. In the modern time when humans generated large quantities of waste and contaminants, microorganisms have overtaken the daunting tasks of cleaning up and recycling wastes in engineered systems such as wastewater treatment plants. They have also been indispensable in remediating contaminated water, soils, and aquifers.
For any redox reactions to occur, we need an electron donor and electron acceptor. The oxidation state of the electron donor increases during redox reactions, whereas that of the electron acceptor decreases. In natural environments, organic carbon often serves as the electron donor in microbe-mediated reactions and become oxidized from organic carbon to inorganic form (e.g., CO2), while multiple electron acceptors often co-exist, including oxygen, nitrate, manganese, iron oxides, among others. There are typically multiple functioning microbial groups that use different electron acceptors.
Microorganisms typically do not use multiple electron acceptors simultaneously. Instead they use electron acceptors in the order of biogeochemical redox ladder, as shown in Figure 1 for some of the naturally-occurring electron acceptors. Different redox reactions release different amount of energy. For example, aerobic oxidation reactions generate much more energy than other redox reactions. The oxidation of glucose can produce 2,880 kJ / mol of C6H12O6; sulfate reduction can produce 492 kJ /mol of C6H12O6, as shown in Figure 2, a much smaller amount. The microorgnanisms that use high-energy-output redox reactions therefore has growth advantage and can outgrow other species.
Reactions | Chemical Formula | Free Energy kJ/mol glucose |
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Aerobic Oxidation | $\mathrm{C}_{6} \mathrm{H}_{12} \mathrm{O}_{6}+6 \mathrm{O}_{2} \rightarrow 6 \mathrm{CO}_{2}+6 \mathrm{H}_{2} \mathrm{O}$ | -2,880 |
Denitrification | $5\ \mathrm{C}_6\mathrm{H}_{12}\mathrm{O}_6+24\mathrm{\ NO^-}_3+24\mathrm{\ H}^+\rightarrow\ 30\mathrm{\ CO}_2+42\mathrm{\ H}_2\mathrm{O}+12\mathrm{\ N}_2$ | - 2,720 |
Sulfate reduction | $6\mathrm{\ C}_6\mathrm{H}_{12}\mathrm{O}_6\ +\ 6\mathrm{\ SO}_4^{2-}+9\mathrm{\ H}^+\rightarrow\ 12\mathrm{\ CO}_2+12\ \mathrm{H}_2\mathrm{O}+3\mathrm{H}_2\mathrm{S}+3\mathrm{HS}^-$ | - 492 |
Methanogenesis | $\mathrm{C}_6\mathrm{H}_{12}\mathrm{O}_6\ \rightarrow\ 3\mathrm{\ C}\mathrm{O}_2+\ 3\mathrm{\ CH}_4$ | -428 |
Ethanol Fermentation | $\mathrm{C}_6\mathrm{H}_{12}\mathrm{O}_6\ \rightarrow\ 2\mathrm{CO}_2\ +\ 2\mathrm{CH}_3\mathrm{CH}_2\mathrm{OH}$ | -244 |
*Table modified from Rittman and McCarthy, 2001. Used with Permission
Redox reactions written in the form shown in Figure 2, do not consider microorganisms or biomass as part of the reaction products. In order to do so, we need to consider reaction energetics and metabolic pathways. The catabolic pathway breaks down the electron donor (e.g., organic carbon) into smaller molecules and generates energy. The anabolic pathway uses organic carbon and energy harnessed in the catabolic pathway to synthesize large cell molecules. The two pathways complement each other in that the energy released from one is used up by the other. The degradative process of a catabolic pathway provides the energy required to conduct a biosynthesis of an anabolic pathway. Both pathways use electrons from the electron donor. Therefore, electrons from the electron donor partition into the two pathways. To write the full reaction equations, we will need to know the fractions of electrons being used for energy production (fe) and for cell synthesis (fs). The summation of $\ f_e\ and\ f_s\ is\ 1.0$. For different redox reactions, these fractions differ. Those higher in the biogeochemical redox latter generate more energy per electron flow so they need smaller fractions of electrons for energy production (smaller fe) and can channel more electron into cell synthesis. Therefore, values of fe increase and fs decrease as we go from aerobic oxidation that is high in the redox ladder to those lower in the redox ladder. That is, less microbial cells are being produced as we go down the redox ladder with the same amount of electron donor. To write the full reaction equation, we also need chemical formula for microbial cells. A commonly used one is C5H7O2N, approximating the ratios of major elements C, N, O, H, in biomass without including trace elements such as phosphorous, sulfur, metals, etc. Other examples include C8H13O3N2, often used to represent microbial sludge produced in waste water treatment plants. Details of how to write such reaction equations are given in Chapter 2 of Rittmann and McCarthy (2001). Here we show a few examples of reaction equations with biomass as the product using acetate as the electron donor (Cheng et al., 2016; Li et al., 2010). Note that for the text below, the overall reactions R is developed using half reactions of electron donor (Rd), electron acceptor (Ra) and cell synthesis (Rc). The energy production reaction Re = Ra - Rd and cell synthesis reaction Rs = Rc - Rd, respectively. The overall reaction $\ R\ =\ f_e\ R_e+f_s\ R_s=\ f_e\ \left(R_a-R_d\right)+f_s\ \left(R_c-R_d\right)=f_e\ R_a+f_s\ R_c-R_d$. A few examples are shown below.
$R_a\ \left(Reaction\ of\ electron\ acceptor\right):\frac{1}{4}O_2+H^++e^-=\frac{1}{2}H_2O$
$\mathrm{R_d\ \left(Reaction\ of\ electron\ donor\right)}:\ \frac{1}{4}\mathrm{HCO}_3^-+\frac{9}{8}\mathrm{H}^++e^-=\frac{1}{8}\mathrm{CH}_3\mathrm{COO}^-+\frac{1}{2}\mathrm{H}_2\mathrm{O}$
$R_c\ \left(Cell\ synthesis\ reaction\right):\ \frac{1}{4}HCO_3^-+\frac{1}{20}NH_4^++\frac{6}{5}H^++e^-=\frac{1}{20}C_5H_7O_2N_{AOB}+\frac{13}{20}H_2O$
Here AOB represent aerobic oxidating bacteria.
The catabolic pathway Re = -Ra - Rd that yields: $\frac{1}{8}CH_3COO^-+\frac{1}{4}O_2=\frac{1}{4}HCO_3^-+\frac{1}{8}H^+$
The anabolic pathway RS = Rc - Rd that yields:
$\frac{1}{8}CH_3COO^-+\frac{1}{20}NH_4^++\frac{3}{40}H^+=\frac{1}{20}C_5H_7O_2N_{AOB}+\frac{1}{20}H_2O$
Combining the two pathways using $R\ =f_e\cdot\left(R_a-R_d\right)+f_s\cdot\left(R_c-R_d\right)=f_e\cdot R_a+f_s\cdot R_c-R_d,$
with $\ f_e=0.4\ and\ f_s=0.6$, we have the following:
$\begin{array}{l}R:0.100\mathrm{O}_2(aq)+0.125\mathrm{CH}_3\mathrm{COO}^-+0.030\mathrm{NH}_4^+\rightarrow\\
0.030\mathrm{C}_5\mathrm{H}_7\mathrm{O}_2\mathrm{~N}_{\mathrm{AOB}}+0.100\mathrm{HCO}_3^-\ +0.090\mathrm{H}_2\mathrm{O}+0.005\mathrm{H}^+\end{array}$
$R a: \frac{1}{5} N O_{3}^{-}+\frac{6}{5} H^{+}+e^{-}=\frac{1}{10} N_{2}+\frac{3}{5} H_{2} O$
$\mathrm{Rd}: \frac{1}{4} \mathrm{HCO}_{3}^{-}+\frac{9}{8} \mathrm{H}^{+}+e^{-}=\frac{1}{8} \mathrm{CH}_{3} \mathrm{COO}^{-}+\frac{1}{2} \mathrm{H}_{2} \mathrm{O}$
$R c: \frac{1}{4} H C O_{3}^{-}+\frac{1}{20} N H_{4}^{+}+\frac{6}{5} H^{+}+e^{-}=\frac{1}{20} C_{5} H_{7} O_{2} N_{N R B}+\frac{13}{20} H_{2} O$
$\text{ Following }R=f_e\cdot R_a+f_s\cdot R_c-R_d,\text{ using a higher }f_e=0.45,\ f_s=0.55,$ we have:
$\begin{array}{l}R:\ 0.090\mathrm{NO}_3^-+0.125\mathrm{CH}_3\mathrm{COO}^-+0.0275\mathrm{NH}_4^++0.075\mathrm{H}^+\rightarrow\\
0.0275\mathrm{C}_5\mathrm{H}_7\mathrm{O}_2\mathrm{N}_{NRB}+0.1125\mathrm{HCO}_3^-+0.1275\mathrm{H}_2\mathrm{O}+0.015\mathrm{N}_2(aq)\end{array}$
$\mathrm{Ra}:\mathrm{\ FeOOH}(s)+3\mathrm{H}^++e^-=\mathrm{Fe}2^+2\mathrm{H}_2\mathrm{O}$
$\mathrm{Rd}:\ \frac{1}{4}\mathrm{HCO}_3^-+\frac{9}{8}\mathrm{H}^++e^-=\frac{1}{8}\mathrm{CH}_3\mathrm{COO}^-+\frac{1}{2}\mathrm{H}_2\mathrm{O}$
$Rc:\frac{\ 1}{4}HCO_3^-+\frac{1}{20}NH_4^++\frac{6}{5}H^++e^-=\frac{1}{20}C_5H_7O_2N_{\mathrm{Fe}RB}+\frac{13}{20}H_2O$
$\text { Following } R=f_{e} \cdot R_{a}+f_{s} \cdot R_{c}-R_{d}, \text { where } f_{e}=0.60, f_{s}=0.40$
$\begin{array}{l}\mathrm{R}:\mathrm{\ FeOOH}(\mathrm{s})+0.208\mathrm{CH}_3\mathrm{COO}^-+0.033\mathrm{NH}_4^++1.925\mathrm{H}^+\rightarrow\\
\mathrm{R}:\mathrm{\ FeOOH}(\mathrm{s})+0.208\mathrm{CH}_3\mathrm{COO}^-+0.033\mathrm{NH}_4^++1.925\mathrm{H}^+\end{array}$
$\mathrm{Ra}:\ \frac{1}{8}\mathrm{SO}_4^{2-}+\frac{9}{8}\mathrm{H}^++e^-=\frac{1}{8}\mathrm{HS}^-+\frac{1}{2}\mathrm{H}_2\mathrm{O}$
$\mathrm{Rd}:\ \frac{1}{4}\mathrm{HCO}_3^-+\frac{9}{8}\mathrm{H}^++e^-=\frac{1}{8}\mathrm{CH}_3\mathrm{COO}^-+\frac{1}{2}\mathrm{H}_2\mathrm{O}$
$Rc:\ \frac{1}{4}HCO_3^-+\frac{1}{20}NH_4^++\frac{6}{5}H^++e^-=\frac{1}{20}C_5H_7O_2N_{\mathrm{Fe}RB}+\frac{13}{20}H_2O$
$\text{ Following }R=f_e\cdot R_a+f_s\cdot R_c-R_d,\text{ where }f_e=0.92,\ \ f_s=0.08,$
$\begin{array}{l}R:\ 0.125\mathrm{SO}_4^{2-}+0.13525\mathrm{CH}_3\mathrm{COO}^-+0.004375\mathrm{NH}_4^++0.0065\mathrm{H}^+\rightarrow\\
R:\ 0.125\mathrm{SO}_4^{2-}+0.13525\mathrm{CH}_3\mathrm{COO}^-+0.004375\mathrm{NH}_4^++0.0065\mathrm{H}^+\end{array}$
In each of these reactions, the ratio of the biomass carbon number (C) in the biomass formula (C5H7O2N) produced per C of organic C is called yield coefficient. For example, for aerobic oxidation, the yield coefficient is 0.030*5/(0.125*2) = 0.60; for denitrification, the yield coefficient is 0.0275*5/(0.125*2) = 0.55; for the FeOOH reduction reaction, the yield coefficient is 0.033*5/(2*0.208) = 0.40; for the sulfate reduction reaction, the yield coefficient is 0.004375*5/(2*0.13525) = 0.08 C biomass /C organic. In general, large fs values leads to high yield coefficients. Values of fs are typically in the range of 0.6 – 0.75 for aerobic oxidation, 0.55 – 0.7 for denitrification, and 0.08 – 0.30 for sulfate reduction. For typical values of different types of redox reactions, please refer to Rittmann and McCarthy (2001).
The kinetics of microbe-mediated reactions are often described by Monod rate laws in the following form:
Here $\mu$ is the rate constant (mol/s/microbe cell), $C_{C_{5} H_{7} O_{2} N}$ is the concentration of microbe cells (cells/m3), Cd and Ca are the concentrations of electron donor and acceptor of the reaction (mol/m3). The Km,D and Km,A are the half-saturation coefficients of the electron donor and acceptors (mol/m3), respectively. These coefficients are the concentrations at which half of the maximum rates are reached for the electron donor and acceptor, respectively. If the electron donor is not limiting, it means that $C_{D} ? K_{m, D}$, so that the term $\frac{C_{D}}{K_{m, D}+C_{D}}$ is essentially 1.
In order to represent the biogeochemical redox ladder, we will need to introduce an additional term in the dual Monod rate law, the inhibition term. A Monod rate law with an inhibition term looks as follows:
Here the KI,H is the inhibition coefficient for the inhibiting chemical H. In contrast to the Monod terms, the inhibition terms become 1 (not inhibiting) only when KI,H?CH.
As an example, in a system where oxygen and nitrate coexist, which is very common in agricultural soils, aerobic oxidation will occur first before denitrification occurs. The sequence of that can be represented by the following:
These two rate laws, with proper parameterization, will ensure that denitrification reaction occurs only when O2 is depleted to a certain extent that the term $\frac{K_{I, O_{2}}}{K_{I, O_{2}}+C_{O_{2}}}$ approaches 1.0. If other electron acceptors that are lower than nitrate in the redox ladder also occur, then multiple inhibition terms are needed. For example, if there is also iron oxide in the system, we will need the following for the iron reduction rate law:
Where the additional litrate inhibition term will allow iron reduction to occur at sufficiently significant rates only when nitrate level is low compared to the inhibition constant value.
The system: I have a 200 ml bottle in my kitchen. I accidentally drop some recently-fertilized soil grains from my backyard into the bottle. I close the bottle after the accident. The soil has some microbial cells, along with some organic carbon (assuming the formula of acetate), and nitrate. The initial acetate and NO3 concentration in the bottle are 5.0 and 1.0 mmol/L, respectively. Assume initially there are some dissolved O2 in the water at the concentration of 0.28 mmol/L while all other chemicals in the soil are not reactive. The initial biomass concentration of O2-reducing and nitrate-reducing biomass are 2.0×10-6 and 1.5×10-6 mol-biomass/L, respectively. In the bottle, I put in some magic powders (to be invented in the future by my daughter Melinda Wu!) that would automatically show the concentrations of chemical species without the need of measurements (that would be my dream come true!). The microbe-mediated reactions advance as the follows:
Aerobic oxidation $\left(f_{s}=0.6 \text { and } f_{e}=0.4\right)$:
$\begin{array}{l} 0.500 \mathrm{O}_{2(a q)}+0.417 \mathrm{CH}_{3} \mathrm{COO}^{-}+0.067 \mathrm{NH}_{4}^{+} \rightarrow \\ 0.067 \mathrm{C}_{5} \mathrm{H}_{7} \mathrm{O}_{2} \mathrm{~N}_{\mathrm{AOB}}+0.500 \mathrm{HCO}_{3}^{-}+0.200 \mathrm{H}_{2} \mathrm{O}+0.150 \mathrm{H}^{+} \end{array}$
Denitrification $\left(f_{s}=0.55 \text { and } f_{e}=0.45\right)$:
$\begin{array}{l} 0.090 \mathrm{NO}_{3}^{-}+0.125 \mathrm{CH}_{3} \mathrm{COO}^{-}+0.0275 \mathrm{NH}_{4}^{+}+0.075 \mathrm{H}^{+} \rightarrow \\ 0.0275 \mathrm{C}_{5} \mathrm{H}_{7} \mathrm{O}_{2} \mathrm{~N}_{\mathrm{NRB}}+0.1125 \mathrm{HCO}_{3}^{-}+0.1275 \mathrm{H}_{2} \mathrm{O}+0.045 \mathrm{~N}_{2(a q)} \end{array}$
Reactions | $\mu_{\max }(\text { mol/mol-biomass/yr) }$ | $\begin{array}{c} K_{m, \text { acceptor }} \\ \text { (mol/kgw) } \end{array}$ | $\begin{array}{c} K_{m, \text { donor }} \\ \text { (mol/kgw) } \end{array}$ | $\begin{array}{r} K_{I, O 2(a q)} \\ (\mathrm{mol} / \mathrm{kg} \mathrm{w}) \end{array}$ |
---|---|---|---|---|
Aerobic | 50000 | 1.00x10-4 | 1.00x10-3 | |
Denitrification | 20000 | 1.00x10-3 | 1.00x10-3 | 1.00x10-6 |
*Range of relevant parameters is from Cheng et al., 2016; Li et al., 2010.
Questions:
Please watch the following video: Microbe Mediated Reactions (24:50)
Please watch the following video (29:51):
In addition to the chemicals and biomass specified in example 5.1, assume there is also sulfate in the water at the concentration of 3.0 mmol/L. The initial sulfate reducing bacteria has the concentration of 1.0×10-6 mol-biomass/L.
Sulfate reduction (Fs = 0.08 and Fe = 0.92) goes as follows:
$\begin{array}{l}
0.125 \mathrm{SO}_{4}^{2-}+0.13525 \mathrm{CH}_{3} \mathrm{COO}^{-}+0.004375 \mathrm{NH}_{4}^{+}+0.0065 \mathrm{H}^{+} \rightarrow \\
0.004375 \mathrm{C}_{5} \mathrm{H}_{7} \mathrm{O}_{2} \mathrm{~N}_{S R B}+0.250 \mathrm{HCO}_{3}^{-}+0.013 \mathrm{H}_{2} \mathrm{O}+0.125
\end{array}$
Sulfate reduction rate parameters are specified in Table 2. Note that it has two inhibition terms because it has both O2 and NO3 above in the redox ladder.
Reactions | $\mu_{\max }(\mathrm{mol} / \mathrm{mol}-\mathrm{biomass/yr})$ | $\begin{array}{l} K_{m, \text { acceptor }} \\ \text { (mol/kgw) } \end{array}$ | $\begin{array}{c} K_{m, \text { donor }} \\ \text { (molkgw) } \end{array}$ | $\begin{array}{c} K_{I, O 2(a q)} \\ \text { (molkgw) } \end{array}$ | $\begin{array}{c} K_{I, \mathrm{NO} 3(a q)} \\ (\mathrm{molkgw}) \end{array}$ |
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Sulfate reduction | 35000 | 1.25x10-3 | 1.25x10-3 | 1.00x10-6 | 1.00x10-3 |
*Range of relevant parameters is from Cheng et al., 2016; Li et al., 2010.
Questions:Extension: In Problem 1, we mainly discuss how O2(aq) affects the microbe-mediated reactions. Other thermodynamics and kinetic parameters, including maximum biomass grow rate, half saturation of the electron donor and acceptor, and the concentrations of electron donor and acceptor, also affect the biomass reactions. Please use the input and database files from Problem 1 as the base case to do the following analysis comparing N2(aq) and sulfide evolution:
In this lesson, we have learned to write microbe-mediated reactions, the Monod rate law, the set up of reactions in CrunchFlow, and the importance of different parameters in controlling the rates and onset of different reactions using the biogeochemical redox ladder.
Borch, T., Kretzschmar, R., Kappler, A., Cappellen, P.V., Ginder-Vogel, M., Voegelin, A. and Campbell, K. (2010) Biogeochemical Redox Processes and their Impact on Contaminant Dynamics. Environmental Science & Technology 44, 15-23.
Cheng, Y., Hubbard, C.G., Li, L., Bouskill, N., Molins, S., Zheng, L., Sonnenthal, E., Conrad, M.E., Engelbrektson, A., Coates, J.D. and Ajo-Franklin, J.B. (2016) Reactive Transport Model of Sulfur Cycling as Impacted by Perchlorate and Nitrate Treatments. Environmental Science & Technology 50, 7010–7018.
Li, L., Steefel, C.I., Kowalsky, M.B., Englert, A. and Hubbard, S.S. (2010) Effects of physical and geochemical heterogeneities on mineral transformation and biomass accumulation during biostimulation experiments at Rifle, Colorado. J. Contam. Hydrol. 112, 45-63.
Rittmann, B.E. and McCarty, P.L. (2001) Environmental Biotechnology: Principles and Applications. McGraw-Hill, New York.