# Team:Valencia/Modeling

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<b>All in all:</b> | <b>All in all:</b> | ||

<br><br>Our modeling team has developed tools to understand and predict better the processes involved in our biosystem, and approach an estimate for the optimum design for a continuous culture bioreactor.<br> | <br><br>Our modeling team has developed tools to understand and predict better the processes involved in our biosystem, and approach an estimate for the optimum design for a continuous culture bioreactor.<br> |

## Revision as of 16:18, 26 September 2012

Modeling

**All in all:**

Our modeling team has developed tools to understand and predict better the processes involved in our biosystem, and approach an estimate for the optimum design for a continuous culture bioreactor.

The main goal of the modeling in this project is to integrate the relevant processes implied in the powering and functioning of the combined symbiotic system.

To achieve this, we entwined two complex models, a metabolic network for Synechococcus sp. and a hybrid regulation model based on highly non-linear differential equations for Aliivibrio fischeri.

We ran the model for a wide range of values for input parameters, such as relative volumes and cell densities. Then, by the means of conditional applications to the cloud of solutions, we retrocalculate the input values of culture design for stable day/night luminescence oscillation, high luminescence yield and balanced energy flow.

Other basic goals are to assess the maximum luminescence production form Synechococcus, to give us an estimate of the suitability of this organism for biolamp applications.

**1)**In first place we adapted a metabolic model of Synechococcus with the functions we included with our constructs. The model is an algorithm applied to a metabolic network of reactions, originally designed for Synechocystis sp. by Lopo et al 2012 and recently adapted for Synechococcus sp.,where optimization of determined fluxes with constraints on certain reactions which make it behave like a living cell. We transformed a wildtype Synechococcus elongatus with the luciferase genes (luxAB) regulated by the promoter psbA. The reactions of bioluminescence expressed by the LuxAB construct were introduced as follows:

- LuxE8 : octanoic acid + ATP + NADPH -> octanal + AMP + NADP+ + diphosphate
- LuxAB8 : octanal + FMNH
_{2}+ oxygen -> FMN + H_{2}O + octanoic acid + light - LuxE14 : tetradecanoic acid + ATP -> tetradecanal + AMP + NADP+ + diphosphate
- LuxAB14 : tetradecanal + FMNH
_{2}+ oxygen -> FMN + H_{2}O + tetradecanoic acid + light - LuxE16 : hexadecanoic acid + ATP -> hexadecanal + AMP + NADP+ + diphosphate
- LuxAB16 : hexadecanal + FMNH2 + O
_{2}-> FMN + H_{2}O + hexadecanoic acid + luz - FMN_red : FMNH
_{2}+ NADP+ <-> FMN + NADPH

May be noted that the luciferin (FMNH

_{2}) is reduced (regenerated) by the reaction FMN_red, which is not naturally present in Synechococcus, but which we added to our model to ensure light production in a persistent way. As a future aim, we plan to include luciferin regeneration gene cassettes to this wildtype. If we didn’t insert this adjustment, the model would calculate flow 0, as luminescence would extinguish in a few seconds with the scarce FMNH

_{2}, so the model has no solutions for infinite time flow. This helped us to notice (and then assured from bibliographic support) this handicap of cyanobacteria as light producers. This partly triggered the reorientation of our research towards the bispecific coculture idea.

Moreover, we programmed bioluminescence functions with 3 types of fatty acid (8, 14 and 16 carbon chain length) which are most abundant in the cyanobacterial cell so could be used as ‘fuel’ with greatest probability, and lied between the operational chain-lenght limits for the luciferase.

This yielded results as we optimized the model’s algorithm to maximize light production, by adjusting the flow rates of the other reaction of the metabolism under certain restrictions which make it a biologically reasonable maximum value. This is the principle of operation for every result we obtained from the algorithm.

In second place, we adapted the wildtype model with the sucrose export induced by the expression of the cscB transporter gene included in the transformed strain from Harvard. Here we modeled the maximum values of sucrose export for 2 different growth restrictions, 0.09mmol Biomass/gDCW*/h (a value near to the maximum growth, similar to an averaged exponential phase culture) and 1x10

^{-6}mmol Biomass/gDCW/h (a negligible growth value which will keep all the vital reactions working but not divert a significant amount of fixed carbon to increasing biomass, as in an averaged dynamic equilibrium of a stationary phase culture).

Maximum export values yielded:

With minimal growth constraint: 0.3075mmol/g DCW/h

With maximal growth constraint: 0.027mmol/g DCW/h

As we planned to transform this cscB strain to express luxI, the protein that synthesizes AHL (Vibrio autoinducer molecule), we introduced the reaction in the model as follows:

ahl: Hexanoyl-(acyl carrier protein) + S-adenosyl-L-methionine -> ahl + S-methyl-5'-thioadenosine + an acyl-carrier protein

As we know, this biomachine has 2 functions inserted, for which we have an interest of flow maximization. Unfortunately, export of sucrose and export of AHL, both carbon based molecules, sets a biochemical competition for carbon redirection. Therefore we came out with 3 modeled outputs: Parabolic curve of maximization of AHL+Sucrose (fig a), and the linear functions of AHL vs. sucrose export in both growth scenarios (fig b, c). All units are expressed in mmol/g DCW/h.

**Fig a.**Parabolic curve representing the product of AHL·Sucrose export flows

versus net sucrose export constraint, at the maximum growth constrain.

The maximum value, of near 0.016mmol/g DCW/h, corresponds

to the 0.013mmol/g DCW/h sucrose export constraint.

**Fig b.**Linear equation representing AHL export versus sucrose export

constraint, at the minimum growth constraint.

**Fig c.**Linear equation representing AHL export versus sucrose export constraint,

at the maximum growth constraint. In this scenario, the value of AHL export

for a sucrose export of 0.049 mmol/g DCW/h (units adapted from Ducat et

al, 2012, at the experimental conditions of our setting) is 0.221mmol/g

DCW/h, which is a very high value, near to the the maximum

(0.2633mmol/g DCW/h).

We just require 1 or 2 molecules per cell of Aliivibrio fischeri to induce the system – (reference). In Fig c we can see the how small sucrose export values, such as our real fluxes affect very little the export of AHL. This was tested on a maximal growth restriction, as the forward idea is to keep the bioreactor in a continuous exponential phase, which corresponds to a flow of 0.00974 mmol/g DCW/h . This imposes a constant flux of sucrose and AHL, which is optimum for our system. The answer of the model to this constant export of sucrose is a flow of 0.015mmol/g DCW/h, which is a pretty high value. As you will see later, this value of AHL export is fundamental for the development of our next model.

-*: DCW=Dry Cell Weight, where an average Synechococcus cell has a dry weight of 1.53pg.

**2)**We achieved our main goal of integrating and connecting all the system into a single model capable of predicting the luminescence of the consortium system in different bioreactor setting scenarios, assuming fast diffusion mechanisms of substances in the medium with a pump system and a pump-filter-return control of population density in both Synechococcus and Aliivibrio modules.

The main part is based on the model of bioluminescence regulation developed by Belta et al. 2001, a hybrid model of 9 differential equations which predicts the behavior of the whole regulatory mechanism of luciferase expression (including cAMP, AHL, LuxR and LuxI expression) in Aliivibrio fischeri.

We modified this model to restrict the growth of the Aliivibrio population to a constrained volume (biolamp compartment) meanwhile we adopted a greater volume for the dilution of the autoinducer (AHL). Such volume represents the annexing of the photobioreactor of Synechococcus and the extra volume from tubing and pumping systems where the medium flows.

We gave the system a new input of AHL derived from the Synechococcus population, which has a Ks (constant rate of AHL production/cell resultant from our modified Syenchococcus metabolic network model) multiplying the number of cells (culture density x culture volume – of the photobioreactor compartment). The model still counts with the AHL produced by the Aliivibrio population, and the degradation half-life in the cells. As we said above, the diffusion speed of AHL is considered instantaneous (as the rate’s scale is very high compared with other variables, such as cell growth or gene expression).

The application of this model is focused in the optimization in the design of the future bioreactor which may contain the system. We are looking for the values of compartment volumes, relative volume, population densities and total volume which can assure a diel control of luminescence (in 12h cycles, considering export rates and the AHL half-life of 10h) by the light induced activity of our Synechococcus biomachine; and, within those values, the settings with maximum luminescence values.

A second filter is be applied to the group of solutions obtained from these premises, with the result of our further model on export and consumption rates of sucrose. This filter aims to discard the settings where insufficient sucrose is exported to the culture to sustain the growth of the Aliivibrio population. We managed to adapt some experimental values of sucrose export and consumption from the literature:

The export of sucrose from our cyanobacteria is: 2.07x10

^{-11}nmol/cell/s (units adapted from Ducat et al, 2012)

The consumption of sucrose by Aliivibrio fischeri is: 0.00000150 nmol/cell/s (units adapted from oxygen consumption rates at maximum bioluminescent activity, at normal glycolytic route assumptions in aerobic conditions, from Makemson 1985).

This amendment model sets the total volume of dilution, the compartmental volumes of occupation and the cell densities for S. elongatus cscB and for A. fischeri (cell densities in a range between 0 and 10

^{9}cell/ml) as controlled variables.

The output gives the multivariate scenarios where the rate of change of sucrose concentration in the common broth is 0 or positive, so that the energy budget is not a shortfall.