Team:DTU-Denmark/Kinetic Model

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Latest revision as of 19:37, 4 October 2013

Kinetic model of the Pathway

Summary

In order to determine the practicality of our solution, we are applying kinetic modeling to investigate how much time our engeneered E. coli cells will take to convert a certain amount of ammonia to nitrous oxide. For ammonia concentrations typically encountered in wastewater, our modelling shows that our transformed E. coli cells will be able to do this within less than 15 minutes.

Methods

The reactions of the pathway we are trying to integrate in E. coli are:

We constructed a kinetic model of our transformants based on literature research. To describe product formation by the enzymes we used the Michaelis-Menten approach (also the iGEM team from Taipei in 2012 was looking into kinetic modelling of Nir and Nos):

Some of the necessary parameters can be found in literature, they are listed in Table 1.

It is necessary to know or estimate the enzyme concentration if k_cat values are used. Based on a paper we found that gives typical protein concentrations in E. coli [4] we chose to use four different enzyme concentrations in our model: 100, 500, 1000 and 100 000 enzymes per cell corresponding to low, medium, high and very high concentrations of enzyme.

To be consistent in units we converted the vmax value of AMO and HAO to a k_cat value in the following way: In [5] the amount of HAO in cell extract is given as 2.6% so for our conversion we assume 2% of the protein mass corresponds to AMO and another 2% correspond to HAO, summing up to 4%. This leads to a value of 39.75μmol min⁻¹ mg of enzyme⁻¹ . The molecular weight of AMO is given in [6] as 283 kDa and the molecular weight of HAO is given in [5] as 189 kDa. Summing those numbers leads to a molecular weight of 472 kDa corresponding to 7.838 · 10⁻¹⁶ mg. With this number we convert the vmax to 3.116 · 10⁻¹⁴ μmol min⁻¹ . Then using the Avogadro number we derive a k_cat value of 18765 min⁻¹.

We also need to know how much ammonia the water we want to treat will contain. The ammonia concentration in different types of waste water is given in [7] as 1 mg/L in aquatic cultures, 10 mg/L for municipal waste water and more than 100 mg/L for industrial waste water. So the concentrations we want to look at in our model are: 1 mg/L (58.72μM), 10 mg/L (587.2μM), 100 mg/L (5.872 mM) and 500 mg/L (29.358 mM) ammonia.

The equations of the two models for Mutant 1 and Mutant 2 are:

The modeling was done in MATLAB using the Systems Biology Toolbox [8] and the scripts are uploaded in the section scripts below.

Results and Discussion

Concentration versus time plots of ammonia and nitrous oxide are shown in Figures 1-2 for different enzyme concentrations. There should at least be around 500 copies of each enzyme in the cell to convert the ammonia in a reasonable time. Especially in Mutant 2 the conversion takes long but with 1000 enzymes per cell the converion times is little more than 20 minutes for an extreme concentration of 500 mg/L ammonia. The plots shown here are estimations based on literature research and will be corrected once we have experimental data.

Figure 1: Kinetic modeling of Mutant 1. Nitrite concentration over time based on kinetic parameters found in literature and for different enzyme and substrate (here NO₂) concentrations. Click on the pictures to see them larger.

Figure 2: Kinetic modeling of Mutant 2. Nitrous oxide concentration over time based on kinetic parameters found in literature and for different enzyme and substrate (here NO₂) concentrations. Click on the pictures to see them larger.

References

[1] WK Keener and DJ Arp. Kinetic studies of ammonia monooxygenase inhibition in Nitrosomonas europaea by hydrocarbons and halogenated hydrocarbons in an optimized whole-cell assay. Applied and Environmental Microbiology, 59(8): 2501–2510, 1993.

[2] Serena Rinaldo. Biology of the Nitrogen Cycle. Francesca Cutruzzola, 2007 (37-55).

[3] SW Snyder and TC Hollocher. Purification and some characteristics of nitrous oxide reductase from paracoccus denitrificans. Journal of Biological Chemistry, 262: 6515–6525, 1987.

[4] Y Ishihama, T Schmidt, J Rappsilber, M Mann, FU Hartl, MJ Kerner, and D Frishman. Protein abundance profiling of the escherichia coli cytosol. BMC genomics, 9, 2008.

[5] AB Hooper, PC Maxwell, and KR Terry. Hydroxylamine oxidoreductase from nitrosomonas: Absorption spectra and content of heme and metal. Biochemistry, 17:2984–2989, 1978.

[6] S Gilch, O Meyer, and I Schmidt. A soluble form of ammonia monooxygenase in nitrosomonas europaea. Biological Chemistry, 390(9):863–873, 2009.

[7] T.C. Jorgensen and L.R. Weatherley. Ammonia removal from wastewater by ion exchange in the presence of organic contaminants. Water Research, 37:723–1728, 2003.

[8] Systems biology toolbox for matlab: A computational platform for research in systems biology. Bioinformatics, 22(4):514–515, 2006.

Scripts

Model of Mutant 1

Plot time series Mutant 1

Model of Mutant 2

Plot time series of Mutant 2

@@ Line 4: / Line 4: @@
 == Kinetic model of the Pathway ==
-We are applying kinetic modeling to investigate how long it takes a cell to produce a certain amount of nitrous oxide.
+=== Summary ===
+In order to determine the practicality of our solution, we are applying kinetic modeling to investigate how much time our engeneered ''E. coli'' cells will take to convert a certain amount of ammonia to nitrous oxide. For ammonia concentrations typically encountered in wastewater, our modelling shows that our transformed ''E. coli'' cells will be able to do this within less than 15 minutes.
+=== Methods ===
 The reactions of the pathway we are trying to integrate in ''E. coli'' are:
@@ Line 11: / Line 15: @@
 [[File:1a.png|400px|center]]
-The iGEM team from [https://2012.igem.org/Team:NYMU-Taipei Taipei] in 2012 was using Nir and Nos in their project as well and did some kinetic modeling based on literature research. To describe product formation by the enzymes they used the Michaelis-Menten approach:
+We constructed a kinetic model of our transformants based on literature research. To describe product formation by the enzymes we used the Michaelis-Menten approach (also the iGEM team from [https://2012.igem.org/Team:NYMU-Taipei Taipei in 2012] was looking into kinetic modelling of Nir and Nos):
 [[File:DTU_mod_1b.png|330px|center]]
@@ Line 20: / Line 24: @@
 Some of the necessary parameters can be found in literature, they are listed in Table 1.
-It is necessary to know or estimate the enzyme concentration if k<sub>cat</sub> values are used. The [https://2012.igem.org/Team:NYMU-Taipei Taipei] Team did this with another kinetic model, but we are missing information about many of this models parameters so the result would be very inexact. Therefore we chose to use four different enzyme concentrations in our model: 100, 500, 1000 and 100 000 enzymes per cell corresponding to low, medium, high and very high concentrations of enzyme. These numbers are based on [4].
-[[File:DTU_mod_1d.png|550px|center]]
+[[File:DTU_modeling_Tab_1.png|600px|center]]
+It is necessary to know or estimate the enzyme concentration if k<sub>cat</sub> values are used. Based on a paper we found that gives typical protein concentrations in ''E. coli'' [4] we chose to use four different enzyme concentrations in our model: 100, 500, 1000 and 100 000 enzymes per cell corresponding to low, medium, high and very high concentrations of enzyme.
+[[File:DTU_modeling_Enz_no.png|450px|center]]
-[[File:DTU_mod_1e.png|560px|center]]
+To be consistent in units we converted the vmax value of AMO and HAO to a k<sub>cat</sub>
+value in the following way:
+In [5] the amount of HAO in cell extract is given as 2.6% so for our conversion we
+assume 2% of the protein mass corresponds to AMO and another 2% correspond to
+HAO, summing up to 4%. This leads to a value of 39.75μmol min<sup>−1</sup> mg of enzyme<sup>−1</sup> .
+The molecular weight of AMO is given in [6] as 283 kDa and the molecular weight
+of HAO is given in [5] as 189 kDa. Summing those numbers leads to a molecular
+weight of 472 kDa corresponding to 7.838 · 10<sup>−16</sup> mg. With this number we convert
+the vmax to 3.116 · 10<sup>−14</sup> μmol min<sup>−1</sup> . Then using the Avogadro number we derive a
+k<sub>cat</sub> value of 18765 min<sup>−1</sup>.
-We also need to know how much ammonia the water we want to treat will contain. The ammonia concentration in different types of waste water is given in [5] as 1 mg/l in aquatic cultures, 10 mg/l for municipal waste water and more than 100 mg/l for industrial waste water. So the concentrations we want to look at in our model are: 1 mg/l, 10 mg/l, 100 mg/l and 500 mg/l ammonia.
-The modeling was done in MATLAB using the Systems Biology Toolbox [6] and the models equations are given below. Results are shown in Figures 1-2.
+We also need to know how much ammonia the water we want to treat will contain.
+The ammonia concentration in different types of waste water is given in [7] as 1 mg/L
+in aquatic cultures, 10 mg/L for municipal waste water and more than 100 mg/L for
+industrial waste water. So the concentrations we want to look at in our model are: 1
+mg/L (58.72μM), 10 mg/L (587.2μM), 100 mg/L (5.872 mM) and 500 mg/L (29.358
+mM) ammonia.
-[[File:DTU_mod_1f.png|350px|center]]
+The equations of the two models for Mutant 1 and Mutant 2 are:
-== The reactor ==
+[[File:DTU_modeling_Equations_kin.png|350px|center]]
-===Continuous stirred tank reactor CSTR===
+The modeling was done in MATLAB using the Systems Biology Toolbox [8] and
+the scripts are uploaded in the section scripts below.
-With our genetically engineered ''E. coli'' we want to treat ammonia polluted waste water. The fastest way to do this would be in a continuous process like a continuous stirred tank reactor (CSTR). Ideally this process would generate an amount of nitrous oxide that is so large that the energy needed for running the system can be delivered by catalytically decomposing the nitrous oxide. We are planing to test a simple CSTR system but hold the engineered ''E. coli'' back in the reactor, so that the outgoing water is free of bacteria. Also we will need to use two CSTRs in sequence because the second mutant requires anaerobic conditions. A picture of two CSTR reactors in series can be found in Figure 3. Another interesting solution would be to grow a bacterial bioﬁlm on solid carriers as shown in Figure 4, a technology known as moving bed bioﬁlm reactor.
+=== Results and Discussion ===
-A CSTR can be balanced using the following equation [7]:
+Concentration versus time plots of ammonia and nitrous oxide are shown in Figures 1-2 for different enzyme concentrations. There should at least be around 500 copies of each enzyme in the cell to convert the ammonia in a reasonable time. Especially in Mutant 2 the conversion takes long but with 1000 enzymes per cell the converion times is little more than 20 minutes for an extreme concentration of 500 mg/L ammonia. The plots shown here are estimations based on literature research and will be corrected once we have experimental data.
-[[File:DTU_mod_2a.png|200px|center]]
 [[File:DTU-NO2_1mg_ammonia.jpg‎|330px]][[File:DTU-NO2_10mg_ammonia.jpg‎|330px]][[File:DTU-NO2_100mg_ammonia.jpg‎|330px]][[File:DTU-NO2_500mg_ammonia.jpg‎|330px]]
-Figure 1: Kinetic modeling of Mutant 1. Nitrite concentration over time based on kinetic parameters found in literature and for different enzyme and substrate (here NO<sub>2</sub>) concentrations.
+<b>Figure 1:</b> Kinetic modeling of Mutant 1. Nitrite concentration over time based on kinetic parameters found in literature and for different enzyme and substrate (here NO<sub>2</sub>) concentrations. Click on the pictures to see them larger.
 [[File:DTU-N2O_1mg_nitrite.jpg‎|330px]][[File:DTU-N2O_10mg_nitrite.jpg‎|330px]][[File:DTU-N2O_100mg_nitrite.jpg‎|330px]][[File:DTU-N2O_500mg_nitrite.jpg‎|330px]]
-Figure 2: Kinetic modeling of Mutant 2. Nitrous oxide concentration over time based on kinetic parameters found in literature and for different enzyme and substrate (here NO<sub>2</sub>) concentrations.
+<b>Figure 2:</b> Kinetic modeling of Mutant 2. Nitrous oxide concentration over time based on kinetic parameters found in literature and for different enzyme and substrate (here NO<sub>2</sub>) concentrations. Click on the pictures to see them larger.
+=== References ===
+[1] WK Keener and DJ Arp. Kinetic studies of ammonia monooxygenase inhibition in ''Nitrosomonas europaea'' by hydrocarbons and halogenated hydrocarbons in an optimized whole-cell assay. ''Applied and Environmental Microbiology'', 59(8): 2501–2510, 1993.
-[[File:DTU_mod_2b.png|300px|center]]
+[2] Serena Rinaldo. ''Biology of the Nitrogen Cycle''. Francesca Cutruzzola, 2007 (37-55).
+[3] SW Snyder and TC Hollocher. Purification and some characteristics of nitrous oxide reductase from paracoccus denitrificans. ''Journal of Biological Chemistry'', 262: 6515–6525, 1987.
+[4] Y Ishihama, T Schmidt, J Rappsilber, M Mann, FU Hartl, MJ Kerner, and D Frishman. Protein abundance profiling of the escherichia coli cytosol. ''BMC genomics'', 9, 2008.
-Figure 3: Two CSTRs in series taken from http://www.umich.edu/elements/a-syLearn/bits/cstr/.
+[5] AB Hooper, PC Maxwell, and KR Terry. Hydroxylamine oxidoreductase from
+nitrosomonas: Absorption spectra and content of heme and metal. ''Biochemistry'',
+:2984–2989, 1978.
+[6] S Gilch, O Meyer, and I Schmidt. A soluble form of ammonia monooxygenase in
+nitrosomonas europaea. ''Biological Chemistry'', 390(9):863–873, 2009.
+[7] T.C. Jorgensen and L.R. Weatherley. Ammonia removal from wastewater by ion exchange in the presence of organic contaminants. ''Water Research'', 37:723–1728, 2003.
-[[File:DTU_mod_2c.png|300px|center]]
+[8] Systems biology toolbox for matlab: A computational platform for research in systems biology. ''Bioinformatics'', 22(4):514–515, 2006.
-Figure 4: In moving bed bioﬁlm reactors the bioﬁlm is grown on carriers as shown above. The picture is taken from http://www.hydrotech-group.com/en/products/industrial-wwtp/mbbr/.
+===Scripts===
+[https://2013.igem.org/wiki/index.php?title=Team:DTU-Denmark/model_mutant1 Model of Mutant 1]
-[[File:DTU_mod_2d.png|550px|center]]
+[https://2013.igem.org/wiki/index.php?title=Team:DTU-Denmark/plot_mutant1 Plot time series Mutant 1]
-For a CSTR perfect mixing is assumed, which means that the concentrations of all compounds are the same everywhere in the reactor and also at the exit point. If the system is run in steady state the so called design equation can be used to calculate the necessary volume of the reactor:
-[[File:DTU_mod_2e.png|190px|center]]
-We can split the molar ﬂow rate of species j into concentration of species j times ﬂow. The reaction rate is dependent on the substrate concentration and can be described with Michaelis-Menten kinetics in our case: [[File:DTU_mod_2f.png|100px]]. So we can calculate the volume of the first reactor for series of different ﬂow rates and substrate concentrations.
-To include the right enzyme concentration we need to estimate how many cells per litre we will have in the reactor and how many enzymes each cell will contain. It was estimated that the cells take up 40% of the volume in the reactor and that they contain 750 copies of each protein of the pathway (see above) resulting in a enzyme concentration of 2.4917x10<sup>-4</sup> mmol/l.
-However this equation does not allow a complete removal of the substrate ammonia from the system.
-The MATLAB function describing the design equation and the script to evaluate it for different flows and substrate concentrations are stored on google drive in Modeling/reactor/CSTR/steadystate. The result of evaluating the design equation for different flows and substrate concentrations is shown in Figure 5.
-[[File:DTU-fig5.jpg|400px|center]]
-Figure 5: CSTR volume for different flow rates and substrate (ammonia) concentrations. The volume was calculated for a steady state application using the design equation.
-In a different approach the reactors were was not assumed to be in steady state but modelled by using the mass balance equation given above. The equations of the model are shown below and the plots of substrate and product concentration for different flows and volumes of the reactors can be found in Figures 6-7. The system was simulated for 1000 min (which corresponds to several cell generations) to assure it to be very close to steady state (or in steady state).
-[[File:DTU_mod_2g.png|450px|center]]
-[[File:DTU-fig6a.jpg|330px]][[File:DTU-fig6b.jpg|330px]]
-Figure 6: Substrate and product concentration in CSTR reactor 1 (ammonia to nitrite) for different flow rates and reactor volumes. The simulation time was 1000 min to assure that the system is very close to steady state.
-== References ==
-[1] WK Keener and DJ Arp. Kinetic studies of ammonia monooxygenase inhibition in ''Nitrosomonas europaea'' by hydrocarbons and halogenated hydrocarbons in an optimized whole-cell assay. ''Applied and Environmental Microbiology'', 59(8): 2501–2510, 1993.
-[[File:DTU-fig7a.jpg|330px]][[File:DTU-fig7b.jpg|330px]]
-Figure 7: Substrate and product concentration in CSTR reactor 2 (from nitrite to nitrous oxide) for different flow rates and reactor volumes. The simulation time was 1000 min to assure that the system is very close to steady state.
-[2] Serena Rinaldo. ''Biology of the Nitrogen Cycle''. Francesca Cutruzzola, 2007 (37-55).
-[3] SW Snyder and TC Hollocher. Purification and some characteristics of nitrous oxide reductase from paracoccus denitrificans. ''Journal of Biological Chemistry'', 262: 6515–6525, 1987.
-[4] Y Ishihama, T Schmidt, J Rappsilber, M Mann, FU Hartl, MJ Kerner, and D Frishman. Protein abundance profiling of the escherichia coli cytosol.''BMC genomics'', 9, 2008.
-[5] T.C. Jorgensen and L.R. Weatherley. Ammonia removal from wastewater by ion exchange in the presence of organic contaminants. ''Water Research'', 37:723–1728, 2003.
+[https://2013.igem.org/wiki/index.php?title=Team:DTU-Denmark/model_mutant2 Model of Mutant 2]
-[6] Systems biology toolbox for matlab: A computational platform for research in systems biology. ''Bioinformatics'', 22(4):514–515, 2006.
+[https://2013.igem.org/wiki/index.php?title=Team:DTU-Denmark/plot_mutant2 Plot time series of Mutant 2]
-[7] H. Scott Fogler. ''Essentials of Chemical Reaction Engineering''. Prentice Hall, 2010.
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