Magaly Herrera Relatorio Final

Study of Kinetic Parameters in a Fed-Batch

Alcoholic Fermentation with Cell Recycle

Scholar Magaly Herrera Garca

Student of Biochemical Engineering at Technological Institute of Veracruz

Supervisor Dr. Elmer Ccopa Rivera / PAT-CTBE

Co-Supervisor

Celina Kiyomi Yamakawa / PIN-CTBE

Study of Kinetic Parameters in a Fed-

Batch Alcoholic Fermentation with Cell Recycle

Scholar Magaly Herrera Garca

Student of Biochemical Engineering at Technological Institute of Veracruz

Technical-Scientific Report presented as a Partial requirement for the 22nd Program of

Summer Grants of Brazilian Center for Research in Energy and Materials (CNPEM)

Supervisor Dr. Elmer Ccopa Rivera / PAT-CTBE

Co-Supervisor

Celina Kiyomi Yamakawa / PIN-CTBE

Campinas, SP - 2013

RELATRIO FINAL DE BOLSISTA 22 PROGRAMA BOLSAS DE VERO DO CNPEM

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Agradecimientos

A mis padres, Myriam Garca Sierra y Norberto M. Herrera Tapia, de quienes he recibido todo el amor, el apoyo y la disciplina. Ellos son los cimientos de todos mis proyectos realizados y los que pretendo realizar. A mi hermano, Norbertt Herrera Garca, por ser autntico, apoyarme y desearme lo mejor siempre, a pesar de los desacuerdos. A mi familia, por celebrar a lo grande cada uno de mis logros y acompaarme muy de cerca en los estresantes das de espera; abuelos, tos y primos sin los cuales no habra tenido tanta confianza, especialmente a Michelle, que vivi todo el proceso conmigo y sin quien no habra sido posible.

A Mario, por esa confianza ciega desde el inicio. Por ser siempre la voz del realismo, por su apoyo an desde lejos y sobre todo, por estos 5 maravillosos aos juntos.

A Mara y Karen, por seguir aqu sin importar el paso de los aos, celebrando nuestros logros. A mis amigos Rolando, Myriam y Risela, por los nimos y el apoyo todos los das, hacen mi vida cotidiana mucho ms fcil y entretenida.

A mis profesores, el Dr. M. A. Salgado Cervantes y la Dra. Dolores Reyes Duarte, su apoyo fue fundamental en la realizacin de esta experiencia. Especiales agradecimientos al Profesor Alejandro Gonzlez Valdz por presentarme esta gran oportunidad e impulsarme a aprovecharla, por su apoyo y comprensin durante todo el proceso.

A mi asesor Elmer A. Ccopa Rivera y co-asesora Celina Kiyomi Yamakawa, por todas sus enseanzas, dedicacin y tiempo durante mi estancia en CTBE, gracias por la confianza depositada; fue para m una experiencia muy grata el haber podido trabajar con ustedes. A Fernanda Keile Gabrielli por toda la paciencia y su apoyo en mis primeros das. A Victor Coelho, Lucas Pavanello y Sayonara Soares, por su amistad y compaerismo todos los das.

A mis colegas Becarios, por hacer de esta una experiencia de vida completa, pero en especial a Thiago (Alberto), Fi, Paola (mostri), Dulcinea, Patricio (Pato) e Izabel, por haber sido mi familia durante 2 meses, por las risas y noches de desvelo compartidas, por su empata en momentos de crisis y porque son lazos que conservar toda la vida.

A Tatiane Madruga Morais y Roberto Pereira Medeiros por su hospitalidad y cuidados durante todo el proceso. Por ltimo agradezco al CNPEM por la gran oportunidad que me fue brindada a travs del 22 Programa de Becas de Verano para desarrollarme en el campo de la investigacin en un centro tan importante como lo es el CTBE.


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Resumo

A configurao de plantas de fermentao industrial no Brasil predominantemente em batelada alimentada com reciclo de clulas. Neste modo de operao, a levedura exposta a inibidores atravs de longos perodos de tempo e a concentraes elevadas de clulas, bem como a flutuaes na qualidade da matria-prima, com impacto na cintica do processo e no desempenho operacional. Neste contexto, para a implementao de estratgias de operao adequadas, necessrio dispor de modelos cinticos capazes de descrever o processo em batelada alimentada, o mais realista possvel. Assim, neste trabalho, avaliou-se um processo de fermentao em batelada alimentada com reciclo de clulas, utilizando levedura industrial e caldo de cana como substrato..

A preciso da previso de um modelo cintico avaliada no apenas por sua preciso na descrio de observaes experimentais, mas, essencialmente, pelos desafios envolvidos na estimativa de seus parmetros. Fermentaes sucessivas de experimentos em batelada alimentada foram realizadas para desenvolver o mtodo para a estimativa de parmetros cinticos. O modelo foi capaz de prever com preciso as fermentaes em batelada alimentada, aps a etapa de tratamento de levedura. Observou-se medidas de desempenho aceitaveis (RSD e R2) para a previso das concentraes de clulas, substrato e etanol. Abstract

The configuration of industrial fermentation plants in Brazil is predominantly fed-batch culture with cell recycle. In this mode of operation, yeast is exposed to inhibitors through long time periods and under high cell concentrations as well as fluctuations in the quality of the raw material, with impact on process kinetic and operating performance.

In this context, for implementation of suitable operational strategies, it is necessary to have fed-batch kinetic models able to describe the process as much realistic as possible. Bearing this in mind, in this work the alcoholic fermentation by industrial yeast strain and sugarcane juice in fed-batch with cell recycle was assessed. The accuracy of prediction of a mechanistic kinetic model is evaluated not only by their precision in describing experimental observations, but essentially by the challenges involved in the estimation of their parameters. Fed-batch experiments in successive fermentations were performed to develop the method for estimation of kinetic parameters. The model was able to accurately predict the fed-batch fermentations after the yeast treatment step. It was observed an acceptable performance measures (RSD and R2) for prediction of cell, substrate and ethanol concentrations.


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Summary

Resumo/Abstract ......................................................................................................................... 2 1. Introduction ......................................................................................................................... 4 1.1 Background. ............................................................................................................................ 4 1.2 First and Second Generation Ethanol.....................................................................................6 1.3 Ethanol Production in Brazil...................................................................................................7

1.4 The Melle-Boinot Process ......................................................................................................8

1.5 Bacterial and Yeast Contamination.......................................................................................10

2. Objectives ........................................................................................................................... 11 2.1 General Objective ................................................................................................................. 11 2.2 Specific Objectives ................................................................................................................ 11 3. Methodology ....................................................................................................................... 12 3.1 Fed Batch Fermentation: Experimental Part ....................................................................... 12 3.1.1 Materials and methods ................................................................................................. 12 3.2 Analytical Determinations.....................................................................................................15 4. Results .................................................................................................................................... 16 5. Mathematical Modeling........................................................................................................18

5.1 Kinetic model ...................................................................................................................................18

5.2 Fed-Batch Model ............................................................................................................................19

5.3 Parameter Estimation ....................................................................................................................20

5.4 Mathematical Modeling: Results...................................................................................................21

6. Conclusions............................................................................................................................24 7.References...............................................................................................................................25


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1. Introduction

For the last few years, the alternative energy field has been expanding in order to

compensate the fuel demand worldwide dealing with fossil fuels problems such as

unavailability of resources and high greenhouse emissions.

Nowadays, ethanol has been established as the best fuel alternative and a fair

competition to gasoline, replacing approximately 50% of the gasoline that would be

used in Brazil if there wasnt another option (Goldemberg, 2013).

The cultivation of sugarcane in Brazil is one of the most notorious worldwide,

this makes it a highly available resource for exploitation.

The total use of sugarcane (bagasse and straw included) as raw cellulosic

material has become an important alternative for ethanol industrial production processes

by depolymerizing, through hydrolysis, the cellulose and hemicelluloses fractions into

fermentable sugars (Andrade, 2013).

In Brazil, ethanol has been produced by industrial fermentation processes since

the 20th century. Currently there are 432 mills and distilleries processing about 625

million tons of sugarcane per crop, resulting in a production about 27 billion liters of

ethanol and 38.7 tons of sugar (Amorim and Lopes, 2011).

Even though Brazil is a pioneer and a leader in fermentative processes for

biofuels production, there are still a lot of problems that need to be taken care of, such

as the cost of production, the complete exploitation of sugarcane and the yeast cell

recycling, which is not yet explored as much.

The main purpose of this work is to generate a mathematical model that can

adjust and predict the effects, advantages and disadvantages of cell recycling in fed-

batch fermentation for ethanol industrial production processes.

It is also intended that it can be applied to the processes already being used in

order to improve the efficiency and lower the costs.


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1.1 Background

Due to the fossil energy depletion and the need to reduce green house gas

emissions and their effects on global warming, alternative energy sources must be

developed. Biofuels, derived from renewable resources are realistic and viable

substitutes to fossil fuels.

At the present time, bioethanol, the main biofuel produced by fermentation of

several feedstocks, constitutes a rapid and significant answer to these problems which is

already being taken into account (Amillastre et al., 2012).

Among all forms of producing ethanol, the fermentation route is the most

economically profitable to Brazil. This fact is due mainly to Brazilian geographic

location, type of soil, variety of feedstock and possibility of nationwide cultivation

(Basso et al., 2011).

Brazil is one of the largest producers of sugarcane worldwide and responsible of

sugar accounting for approximately a quarter of the entire worlds production

(Goldemberg, 2013). Thus, Brazil is the most competitive producer of bioethanol from

sugarcane in the world with a well developed domestic market thats also being

increasingly stimulated by growing sales of flex fuel cars.

At the beginning the priority was to produce anhydrous bioethanol so that it

could be mixed with gasoline; after the world oil crisis that took place in the late 70s

this objective turned into the initiation of ethanol-powered vehicles. This plan was

successful and it culminated in an increase of vehicles that functioned on hydrated

ethanol in Brazil to the point where the occupation of these cars occurred in almost

100% of the country.

In 2008 bioethanol consumption as a fuel exceeded the consumption of gasoline

in Brazil; currently more than 95% of all the cars sold in Brazil are flex-fuel (meaning

they can run either on ethanol or gasoline).

In Brazilian ethanol production industry, the fermentation is a biochemical

process in which glucose, fructose and sucrose (from sugarcane juice and sugarcane

molasses in varying proportion) is metabolized to ethanol by yeast Saccharomyces

cerevisiae in fermentors containing millions of liters. Ethanol yields in the order of 90


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92% of the theoretical sugar conversion into ethanol were achieved in the last decade

(Della-Bianca et al., 2012).

Gasoline sold in Brazil nowadays contains 25% anhydrous bioethanol. The

expansion of ethanol consumption due to the growing fleet of light vehicles, mainly flex

fuel cars, and increased exports have opened new opportunities for industrial growth.

However, the success of these industries depends on how they solve and face the

challenges that this new fuel brings to the table.

1.2 First and Second Generation Ethanol At present, there are two main streams in biofuels production: First and Second

generation biofuels (see Figure 1).

First generation biofuels

First generation or conventional biofuels are the ones produced from raw

materials ready for fermentation; these raw materials dont mandatorily need a

pretreatment. Some examples of these feedstocks are mainly crops rich in starch such as

grains, sugarcane and corn.

Starch is a glucose-containing polymer which can readily be hydrolyzed by

industrially produced enzymes and fermented by yeast strains. This process is well

known and is being currently applied for industrial production of bioethanol in many

parts of the world, especially in the USA (whit corn as feedstock) and Brazil (with

sugarcane as feedstock).

Second Generation Biofuels.

Second-generation biofuels are the ones produced from sustainable feedstock.

These feedstocks are usually lignocellulosic materials which need to be pre-treated for

the fermentation (hydrolysis or thermo-chemical pretreatments). After this additional

step, the sugar released during the pretreatment is fermentation ready to produce

ethanol. Wood, bagasse and straw are the most common lignocellulosic resources for

this type of fermentation.


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Figure 1: Flowchart for first and second generation ethanol production processes (Tan et al., 2008)

1.3 Ethanol production in Brazil

Current production process of ethanol from biomass can be divided into four

phases: preparation of raw materials, obtaining of substrate for fermentation,

fermentation and distillation. The first two phases represent significant differences with

respect to each of the three types of products that are usually processed (saccharine,

starchy and cellulosic) (Macedo, 1993)

The current setting of industrial fermentation plants in Brazil in present time is

predominantly fed-batch culture with cell recycle, this process is also known as the

Melle-Boinot process, being that 70-80% of distilleries utilize this mode of operation

(Brethauer and Wyman, 2010).

Here, 90-95% of the yeast cell is reused from several successive fermentations

(intensive recycling). This allows high cell densities inside the fermentors, which

contributes to reduce the fermentation time to 6-11 h (Basso et al. 2008; Della-Bianca et

al., 2013).

Nowadays there are many apparently minor, but important, industrial problems

associated to the ethanol production process using fed-batch culture with cell recycle.

The most important and less studied are those related to the yeast treatment step. Thus, a

study and description of the influence that cell recycling has on fermentation kinetics is

essential for a reliable mathematical model adequate to be used for process optimization


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by predicting the behavior of the fermentation for it to perform in a more efficient way

and thus reduce the costs and time of production, as well as determinate the optimal

conditions for the process to work at its highest levels of performance.

In this work an alcoholic fermentation by an industrial yeast strain

(Saccharomyces cerevisiae from LEB-UNICAMP) and sugarcane juice in fed-batch

with cell-recycle was performed. These experiments were assessed in order to study and

analyze the kinetic model with focus on a method that may be used always a re-

estimation of parameters is required. In this sense, the performance of a mechanistic

kinetic model, considering the effect of cell recycling on the kinetic, is evaluated not

only by their accuracy in describing experimental data, but mainly by the difficulties

involved in the adaptation of their parameters. Fed-batch experiments with cell recycle

were performed to develop the method for estimation of kinetic parameters.

1.4 The Melle-Boinot process The actual fermentation process was developed in the 1930s by Firmino Boinot and

this technology was patented in 1937. Melle-Boinot Process is the most popular

fermentation technology being used in Brazil; this process involves yeast recovery for

cell recycling by wine centrifuging.

Yeast cell recycling represents an advantage for the industry because the re-

utilization of the living cell biomass saves sugar and increases the fermentation yield

because, according to Amorim and Lopez (2005), instead of the yeast converting sugar

into the cellular biomass, more sugar is converted into ethanol. For this reason, other

processes worldwide without cell recycle cannot compete with Brazilian distilleries

ethanol yields (Amorim et al., 2011). Typical configuration of a Melle-Boinot fermentation process is presented in

Table 1.


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Table 1: Data table of Melle-Boinot process traditional configuration (Johnson and Seebaluck, 2012)

In the last 30 years this process has been improved allowing Brazilian distilleries

to achieve yields up to 92-93%.This yield refers specifically to ethanol produced from

sugar, nonetheless there are various sub-products such as glycerol, cellular biomass,

succinate and malate (Amorim et al., 2011); now every industrial fermentation plant in

Brazil uses modified Melle-Boinot processes to produce ethanol on an industrial scale.

Disadvantages of the Melle-Boinot process

Despite the high level yields that this process achieves, it presents a few

significant problems such as contamination risks and loss of activity because of cell

recycling and stressful conditions.

In fermentation process with cell recycling the yeast cells are being constantly

submitted to stressful conditions such as high ethanol levels, low pH, temperature,

excess of salts and mineral deficiency among others; due to this the first challenge

nowadays for process improvements is the comprehension of how this parameters affect

the yeast cells and the fermentation. Although several laboratories are now working in

the reproduction of these conditions at bench scale, its still very difficult to understand

how the yeast is being affected at an industrial scale since the results of other

fermentation processes cant be applied to the Brazilian distilleries because of the

difference in the conditions between sugar cane and other feedstocks such as wheat,

corn, etc (Amorim et al, 2011).


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1.5 Bacterial and yeast contamination

As it was mentioned earlier, one of the problems that the fed-batch industrial

fermentation process presents is the high risk of contamination, which can be by

bacteria and wild yeast that end up competing with the selected yeast to survive in the

fermentors.

Among the main contaminants of alcoholic fermentations we can find species

such as Lactobacillus and Bacillus. Between the factors that allow the contaminating

microorganisms to enter into the process are the successive recycling of tons of yeast

cells everyday and the difficulties to sterilize large volumes of juice and water. At the

present time, these bacterial populations are being controlled with acid treatments,

antibiotics and chemical biocides that arent harmful for the yeast cells.


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2. Objectives

2.1 General Objective:

The main purpose of this work is to evaluate the prediction accuracy of a

mechanistic kinetic model not only by its precision in describing experimental

observations, but essentially by the challenges involved in the estimation of their

parameters.

2.2 Specific Objectives:

1. Development of experiments for a fed-batch fermentation process with cell recycles using industrial yeast strain and sugarcane juice.

2. Development and testing of a modeling approach for the kinetic parameter estimation with focus on a method that may be used when a re-estimation or

comparison of parameters is required.

2.1 Evaluate optimization criteria expressions to find optimal values for the

parameters that result in the closest fit between the experimental

observations and the simulated response variables.

2.2 Evaluate the performance of the model considering the effect of cell

recycling on the kinetic.


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3. Methodology

3.1 Fed Batch Fermentation: Experimental Part

For the first part of this study a fed-batch fermentation experiment was assessed

to produce the appropriate conditions to emulate the industrial conditions of the

Brazilian industrial alcoholic fermentation.

The characteristics of this experiment are presented in Figure 2.

Figure 2: Flowsheet of the yeast treatment with operational specifications

3.1.1 Materials and methods Microorganism

The Saccharomyces cerevisiae strain used in this work was an un-named strain

cultivated in the Development Bioprocess Laboratory at CTBE (see Figure 3) and

obtained from the Faculty of Food Engineering/ State University of Campinas,

originally coming from an industrial ethanol distillery. The strain was maintained on

agar plates that were prepared per liter of desmineralized water: yeast extract, 10 g;

peptone, 20 g; glucose, 20 g; and agar, 20 g.

Figure 3: Saccharomyces cerevisiae Experiment 401.13.00.001.004 Time 1 and Time 6 photographed with 100X objective

Bioflo Fermentor 115 - 3L (0.8-2.2 L)

Agitation: 100 rpmTemperature: 33.0CTime: ~10 hours.pH: 5Fermentor final total volume: 2000 mL.Inoculum Volume: 500 mLTotal must volume: 1500 mL.Volume per Fermentation: 1500 mLNumber of recycles: 5

Must

Glucose SolutionPA 500g/L: 1800.00 mLWater: 7200.00 mL


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Previous the inoculum preparation, three slopes from agar plate were transferred

to liquid complex medium containing per liter of desmineralized water: yeast extract, 10

g; peptone, 20 g; and glucose, 20 g. This step named pre inoculum aimed cells

activation that was performed in flask shaker culture for 24 hours at 33C and 250 rpm.

Inoculum and cultivation

The complex medium used for inoculum and cultivation contained the following

per liter of desmineralized water: K2SO4, 6.6 g; KH2PO4, 3 g; MgSO4, 0.5 g;

CaCl2.2H2O, 1.0; and yeast extract, 5.0 g. After autoclaving at 121C for 15 minutes, the

medium was cooled to room temperature. Thereafter, filter-sterilized elements were

added in the following concentration per liter: urea, 2.3 g; thiamine, 3.0 g; EDTA, 15

mg; ZnSO4.7H2O, 4.5 mg; CoCl2.6H2O, 0.3 mg; MnCl2.4H2O, 0.84 mg; CuSo4.5H2O,

0.3; FeSO4.7H2O, 3 mg; NaMoO4.2H2O, 0.4 mg; H3BO3, 1 mg; and KI, 0.1 mg. The

carbon source, 80 g/ L of glucose, was sterilized separately at 121C for 15 minutes.

The inoculum culture was performed in Erlenmeyer flask for 24 hours, 33C and

250 rpm in an orbital shaker incubator (Innova 44 New Brunswick). After that the

inoculum was centrifuged in a Sorvall centrifuge at 8000 rpm for 20 minutes, then the

supernatant was discarded and the cells were suspended in sterilized water up to 200 mL

and transferred to the cultivation bioreactor aseptically. The cultivation was performed

at 33C in a bioreactor (Bioflo 115; New Brunswick Scientific) (as shown in Figure 4)

in fed batch configuration in cascade control with agitation and air flow to maintain the

dissolved) O2 concentration above 60% of saturation with air. Thereafter, the yeast

culture was centrifuged in a Sorvall centrifuge at 8000 rpm for 20 minutes, then the

supernatant was discarded and the cells were suspended in sterilized water (quantity

sufficient for 800 mL) and transferred to the bioreactor for alcoholic fermentations.


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Alcoholic fermentation medium

Figure 4: Fed-batch fermentation in Bioflo fermentor 115.

The substrate used for alcoholic fermentations was slight the same of cultivation but

glucose concentration was per liter of desmineralized water 198.53 g in the first recycle,

197.78 g in the second recycle and 136.44 g in the third recycle. The alcoholic

fermentations were performed with cells recycling in the fed batch configuration as is

usual in industrial Brazilian process (Melle-Boinot). However the cell density was not

high as at industrial process (approximately 30 g/ L in the end of must feed) whereas the

main aim in these experiments was to obtain many data to obtain kinetic tendency in fed

batch.

The yeast cells required were obtained previously in the cultivation step. The batch

feeding using must was performed in nine hours (flow of 2.26 mL/min) up to the final

volume of 2 L. After that, the wine was then centrifuged meaning not ensure that all

sugar was consumed. The fermented wine was centrifuged at 8000 rpm for 20 minutes

in a Sorvall centrifuge then the yeast was suspended with sterilized water and

centrifuged again in the same condition above. The centrifuged yeast biomass was

carried back to the bioreactor for treatment with H2SO4 under pH of 3.0 and aeration

during one hour. This treatment was performed before each fermentative cycle during

yeast cell recycling in other words fermentation and yeast recover step and recycle were

carried out for four cycles (see figure 5).

Samples were taken on every hour of each fermentation cycle in triplicates, for them

to be analyzed later and determinate the products and the yields of the fermentation and


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discuss how does the cell recycling affects the yeast cells and impact on the

fermentation kinetics.

Figure 5: Yeast treatment flow sheet with condition specifications.

3.2 Analytical determinations

Concentrations of glucose and ethanol were detected by high-performance liquid

chromatography (HPLC) Dionex Ultimate 3000 with IR detector Shodex RI-101,

Aminex column HPX-87H 300 mm x 7.8 mm at 50C and 0.5 mL/min of sulfuric acid 5

mM as eluent phase. Measurements of the dry weight mass were carried out in triplicate

and determined gravimetrically after centrifuging, washing two times with water and

drying at 80C until constant weight in the analytical balance.

1st. Recovery

Fermentation

Reinvigoration

2nd Recovery

De-yeasted wine

Detoxification

Cells

must

Yeast Treatment

H2SO4pH=3

T=30 min.150 rpm0.1 vvm


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4. Results The first part of this study includes data obtained from 5 fed-batch fermentations (4

cell recycles) in which the triplicate samples of each fermentation cycles were weight to

determine the dry mass data contained in 2 mL eppendorfs: MA (empty eppendorfs

weight), MD (eppendorfs weight with dry cell weight) and MC (dry cell weight).

These data were analyzed in order to obtain concentration values for the samples.

As it was previously mentioned, the samples were taken in triplicates and to avoid any

probabilistic error, the standard deviation between the 3 samples was calculated. The

results of this analysis werent significant, meaning that the difference between the

samples of each time wasnt even enough to plot them.

After performing these analyses, the profiles of X (cell concentration, g/L) in

function of the time (hours) were plotted, as shown in Figure 6.

a)* b)

c) d)*

Figure 6: X against time for first (a), second (b), third (c) and forth (d) recycle. (*The fluctuations in concentration values can be considered as a result of a decalibration of the analytical balance between samples.)

0.00

2.00

4.00

6.00

8.00

10.00

12.00

0 1 2 3 4 5 6 7 8 9 10

Conc

entrat

ion (g/L

)

Time (h)

Concentration X (g/L) - all values

Concentration X (g/L) -all values

0.00

2.00

4.00

6.00

8.00

10.00

12.00

14.00

-2 0 2 4 6 8 10

Conc

entration X (g/L

)

Time (h)

Concentration X (g/L)


0.00

2.00

4.00

6.00

8.00

10.00

12.00

-2 0 2 4 6 8 10

Conc

entration X (g/L

)

Time (h)



0.00

2.00

4.00

6.00

8.00

10.00

12.00

-2 0 2 4 6 8 10

Conc

entrat

ion X (g/L

)

Time (h)

Concentration X (g/L)Concentration X (g/L)


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Figure 7 shows the concentration values obtained from the HPLC analysis for ethanol,

glucose, and cells concentrations (g/L):

a) b)

c) d)

Figure 7: Graphics that represent the concentration of Ethanol (), Glucose (), and Cells () in g/L plotted against time (hours).

Ethanol concentration was expected to be higher for this particular fermentation,

but their low yield can be considered a result for a lack of nutrients (such as salts and

minerals) in the fermentation medium. However, the concentration of ethanol, glucose

and cells show a typical behavior to a fed-batch process.

0.00

10.00

20.00

30.00

40.00

50.00

60.00

70.00

80.00

90.00

0 2 4 6 8 10

Ethanol

Glucose

Cells

0.00

20.00

40.00

60.00

80.00

100.00

120.00

0 2 4 6 8 10

Ethanol

Glucose

Cells

0.00

20.00

40.00

60.00

80.00

100.00

120.00

0 2 4 6 8 10

Ethanol

Glucose

Cells

0.00

20.00

40.00

60.00

80.00

100.00

120.00

0 2 4 6 8 10

Ethanol

Glucose

Cells


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5. Mathematical modeling This section presents the considerations required to develop a model-based

technique for the estimate of the kinetic parameters.

5.1 Kinetic model

The state variables involved in this fed-batch process were concentration of total

cell mass, X (kg/m3), concentration of substrate, S (kg/m3) and concentration of ethanol,

P (kg/m3).

Experimental observations have shown that cell, substrate and product inhibitions

are significant for ethanol fermentation (Rivera et al., 2007; Andrade et al., 2013). Eq

(1) shows the cell growth rate equation, rx, which includes terms for such types of

inhibitions:

XPP1

XX1S)Kexp(

SKSr

n

max

m

maxi

smaxx

+= (1)

where max is the maximum specific growth rate (h1), Ks the substrate saturation

constant (kg/m3), Ki the substrate inhibition parameter (m3/kg), Xmax the cell

concentration where the growth ceases (kg/m3), Pmax the ethanol concentration where

the cell growth ceases (kg/m3), and m and n are empirical parameters.

In this study, a modified Luedking-Piret expression was used to account for the ethanol

formation rate, rp, as shown in Eq (2). This rate depended on the specific growth rate

and cell concentration (X). Yp/x (kg/kg) is the product yield based on cell growth, m

(kg/kg h) is a parameter associated with maintenance, and Ks (kg/m3) a saturation

parameter.

XSKS

rrs

mxp/xp ++= (2)

The substrate consumption rate, rs, was expressed as follows:

Xm)/(rr sxxs += (3) Were Yx (kg/kg) and ms (kg/kg h) denote the limit cellular yield and maintenance

parameter.


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5.2 Fed-batch model

Mechanistic models comprise the mass balance differential equations, with

microorganism growth, substrate consumption and ethanol formation for a fed-batch

reactor described as follows:

- Total biomass

VXFr

dtdX A

x = (4)

- Substrate

sAA rV

)(SFdtdS

=S

(5)

- Ethanol

VPF

rdtdP A

p = (6)

- Volume

AFdtdV

= (7)

The mass balance differential equations were solved with the using the

Livermore Solver for Ordinary Differential Equations (LSODE, Radhakrishnan and

Hindmarsh 1993).

Figure 8: General framework of the model-based approach used to estimate the kinetic parameters

Fed-batch model

State variables(Xn, Sn, Pn)

Fixed kinetic parameters

Guess to the influential kinetic parameters

Re-estimate the influentialkinetic parameters byoptimization algorithms

- Initial conditions values: X0,S0,P0(kg/m3)- Feeding time (h)- Feed stream flow rate (m3/h)- Feed substrate concentration (kg/m3)

Minimize cost function: E()

Experimental data (Xen,Sen,Pen)

Stop?

End

Optimization step

Initial dataset


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5.3 Parameter estimation method

The proposed method for estimation of kinetic parameters is shown in Figure 1.

First the kinetic parameters are initialized (including fixed parameters and the

parameters to be estimated) as well as the operational conditions values for the fed-

batch process (Feeding time tF; Feed stream flow rate, FA and Feed substrate

concentration, SA). After this step, the method proposed can find optimal values for the

parameters that produce the best fit between the experimental observations and the

simulated response variables by minimizing cost functions, Eq (8), Eq (9).

=

+

+

=np

1n2max

2nn

2max

2nn

2max

2nn

Pe)Pe(P

Se)Se(S

Xe)Xe(X

)(E

=

+

+

=np

1n2

nn

2nn

2nn

2nn

2nn

2nn

2PeP

)Pe(P

2SeS

)Se(S

2XeX

)Xe(X)(E

Where is the vector of kinetic parameters constrained by bounds within a

realistic range, i.e, biological meaning. Xen, Sen and Pen are the experimental

observations of cell; substrate and ethanol concentrations at the sampling time n. Xn, Sn

and Pn are the concentrations computed by the model at the sampling time n. Xemax,

Semax and Pemax are the maximum measured concentrations.

If a stopping criterion is reached, the estimation is finished. If not, the algorithm

re-estimates the parameters using an optimization technique based on Genetic

Algorithm and Quasi-Newton method. The determination of the feasible region of the

total search space in the multi-parameter optimization of a mechanistic model is not a

trivial procedure. For that reason, in this study, the optimization procedure is based on

the combination of two optimization techniques. Initially, the potential of global

searching of Genetic Algorithm (GA) was explored for simultaneous estimation of the

initial guesses for a set of kinetic parameter in the model. Subsequently, the quasi-

Newton algorithm (QN), which converges much more quickly than GA to the optimal

values, was used to continue the optimization of the kinetic rate constants near to the

global optimum region.

(8)

(9)


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5.4 Mathematical modeling: Results and Discussion

Experiments used in this study were obtained following the methodology as

describe in Section 3. The difference lays in the fact that for the first experimental study

(Section 3) the sampling process and the data correspond only to the fed-batch part of

the process because the fermentation was stopped right after the must feeding emptied

completely. On the other hand, the experimental results for the mathematical modeling

study also include the batch part of the process and the natural curse of the fermentation

as can be seen in Figures 9 and 10.

Table 2: Initial values and operational conditions of the experiments

Fermentation 1

Fermentation 2

Fermentation 3

Fermentation 4

Initial values X0 (kg/m3) 17.95 3.37 15.52 4.22 S0 (kg/m3) 9.84 14.55 14.56 11.13 P0 (kg/m3) 40.55 44.15 44.83 44.65

Operational conditions

V0 (m3) 0.5 0.5 0.5 0.5 SA (kg/m3) 171.7 171.7 171.7 171.7 FA (m3/h) 0.43 0.26 0.22 0.23 tF (h) 2 3 3 3

The parameter estimation process requires appropriate initial guess values to start

the optimization process. This step is critical to find the optimal values of the

parameters that minimize the error between the experimental and simulation data.

Fortran routines was used to accomplish this procedure. Two cost functions were

compared (Equations 8 and 9) and the results are show in Table 3.

The parameters shaded in green were the only ones varied during the adjustment.

In this study, mp, m, Ks also were studied. The remaining ones were fixed in the

previous values used in several studies (Atala et al., 2001; Rivera et al., 2007, Andrade

et al., 2013 ), as follows: Ks = 4.1 (kg/m3), Ki = 0.004 m3/kg, m = 1.0 and n = 1.5.


22

Table 3: Estimated parameters values using cost function in Equations 8 (Obj. Eqn. 1) and Equation 9 (Obj. Eqn. 2).

Obj. Eqn. 1 Obj. Eqn. 2 Obj. Eqn. 1 Obj. Eqn. 2 Obj. Eqn. 1 Obj. Eqn. 2 Obj. Eqn. 1 Obj. Eqn. 2Ks (Kg/m

3) Substrate Saturation parameter. 4.1 4.1 4.1 4.1 4.1 4.1 4.1 4.1

Ki (m3/kg) Substrate inhibition coefficient. 0.02 0.02 0.02 0.02 0.02 0.02 0.02 0.02

Pmax (g/L) Product concentration whe cell growth ceases. 75.61201899 92.7767951 72.459508 71.67815207 128.0495434 104.7110895 76.4021715 78.12817597

Xmax (g/L) Biomass concentration when cell growth ceases.100.8944462 93.39447076 98.176 94.17771218 45.27023103 69.85805492 63.20667339 76.22623341n Product inhibition parameter. 1.5 1.5 1.5 1.5 1.5 1.5 1.5 1.5m Cellular inhibition parameter. 1 1 1 1 1 1 1 1

Ypx (kg/kg) Product yield based on cell growth. 9.6993 10.23472122 5.5924 5.53461521 9.840849015 9.809487592 9.079148271 9.356566396

max (h-1) Maximum specific growth rate. 0.3057 0.365345316 0.3484 0.432892842 0.03555624 0.262421984 0.229800896 0.212278924

ms (kg/[kg h] Maintenance parameter. 1 1 1 1 0.85 0.85 0.84 0.84

m (kg/[kg h]) Growth associated Ethanol production. 0.795 0.795 0.917 0.917 0.482 0.482 0.55 0.55

Ks (kg/m3) Saturation Parameter. 12.75 12.75 13.65 13.65 5.96 5.96 5.84 5.84

Yx (kg/kg) Limit cellular yield. 1.1328 0.015177643 0.100301138 0.012840896 0.076578042 0.077629355 0.076861025 0.077082446

Ferm. 1 Ferm. 2 Ferm. 3 Ferm. 4Parameter Description

Figure 9: Cell (X), substrate (S) and ethanol (P) concentrations plotted against time, being the dotted line (---) the plot corresponding to equation (8) and the continuous line corresponding to equation (9). a), b), and c) correspond to Recycle 1; d), e) and f) correspond to recycle 2.

a)

b)

c)

d)

f))

e)


23

Figure 10: cell (X), substrate (S) and ethanol (P) concentrations plotted against time, being the dotted line (---) the plot corresponding to equation (8) and the continuous line corresponding to equation (9). g), h), and i) correspond to Recycle 3; j), k) and l) correspond to recycle 4. Table 4: Statistical Criteria to characterize the prediction quality of the fed batch model:

X S P X S PRSD(%) 5.03 12.22 3.02 5.96 8.35 6.35

R2 0.97 1.00 1.00 0.99 1.00 1.00RSD(%) 11.56 22.96 6.52 7.94 23.98 4.99

R2 0.98 0.98 1.00 0.98 0.98 1.00RSD(%) 6.37 7.83 7.82 4.81 10.42 9.36

R2 0.99 0.99 0.99 0.98 0.99 0.98RSD(%) 7.20 4.90 7.12 6.21 6.00 7.19

R2 1.00 1.00 1.00 1.00 0.99 1.00

Obejctive equation 2.

RECYCLE 4

RECYCLE 1

RECYCLE 2

RECYCLE 3

Objective equation 1.

The performance of the model in describing the experimental observations for

Fermentations is shown in Figures 9 and 10 and quantified through the RSD(%)

(Residual Standard Deviation) and R2 (correlation coefficient) (Rivera et al., 2007).

From these criteria, it was concluded that the model described the experimental data

accurately, as evaluated by RSD(%) values. Furthermore, in all cases R2 was close to

unity, indicating a good fit of the model, as can be seen in Table 4.

g)

h)

i)

j)

k)

l)


24

6. Conclusions

This work presents results from the development and testing of a modeling approach

for the estimation parameters in fed-batch fermentation with high cell densities

intensively recycled. Even considering that the kinetic rate expressions are known in the

mechanistic model, the estimation problem is complex and time consuming.

This suggests that using a model in a situation where frequent parameter re-

estimation is necessary, such as the studied system could be a limitation. In this work, a

model-based approach has been developed using a mechanistic model and optimization

algorithms that have been widely used for modeling and optimization purposes in

engineering application.

Based on this approach, a mechanistic model was obtained and its performance in

describing the dynamic behavior of cell, substrate and ethanol concentrations during

fed-batch fermentation was assessed. Model predictions using the experimental

observations provided acceptable performance measures (RSD and R2). Finally, it can

be said that the use of this approach enables a rapid determination of a mathematical

description of fed-batch fermentation processes that can be used for optimization and

control.


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7. References

Amillastre E., Aceves-Lara C.A., Uribelarrea J.L., Alfenore S., Guillouete S.E, 2012. Dynamic model of temperature impact on cell viability and major product formation during fed-batch and continuous ethanolic fermentation in Saccharomyces cerevisiae. Bioresour Technol; 117C :242-250.

Amorim Henrique V., Lopez L. Mario., 2005. Yeast Selection for fuel ethanol

production in Brazil. FEMS Yeast Research. Volume 8, Issue 7. Andrade R.R, 2007., Procedimento Para o Desenvolvimento De Um Modelo

Mstemtico Robusto Para o Processo De Fermentacao alcolica. Dissertao de Mestrado. Campinas 2007.

Andrade R.R., Rivera E.C., Atala, D.I.P., Maciel Filho R., Maugeri Filho F., Costa,

A.C., 2009. Study of kinetic parameters in a mechanistic model for bioethanol production through a screening technique and optimization, Bioprocess Biosyst. Eng. 32, 673-680.

Andrade R.R., Maugeri Filho F., Maciel Filho, R., Costa A.C., 2013. Kinetic of ethanol

production from sugarcane bagasse enzymatic hydrolysate concentrated with molasses under cell recycle, Bioresource Tech. 130, 351-359.

Atala D.I.P., Costa A.C., Maciel Filho R., Maugeri Filho F., 2001. Kinetics of ethanol

fermentation with high biomass concentration considering the effect of temperature, App. Biochem. Biotechnol. 91-93, 353-366.

Basso L.C., Amorin H.V., Oliveira A.J., Lopes M.L., 2008. Yeast selection for fuel

ethanol production in Brazil, FEMS Yeast Res. 8, 1155-1163. Basso L.C., Basso T.O., Rocha S.N., 2011. Ethanol production in Brazil: The industrial

process and its impact on yeast fermentation. In: Biofuel Production Recent developments and prospects, Eds. Bernardes M.A.D.S., InTech, Rijeka, Croatia.

Brethauer S., E. Wyman C.,2010, Review: Continuous hydrolysis and fermentation for

cellulosic ethanol production, Bioresource Technology. Della-Bianca B.E., Basso T.O., Stambuk B.U., Basso L.C., Gombert A.K., 2013. What

do we know about the yeast strains from the Brazilian fuel ethanol industry?, Appl. Microbiol. Biotechnol. 97, 979-991.


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Henrique V. Amorim, Lopes M.L., Velasco de Castro J., Buckeridge M.S., Henrique G.G., 2011, Scientific challenges of Bioethanol Production in Brazil., Appl. Microbiol. Biotechnol. 91, 1267-1275.

J. Goldemberg., 2013. Sugarcane Ethanol: Strategies to a successful program in Brazil.

Advanced Biofuels and Bioproducts Part 1, Chapter 2. Johnson and Seebaluck, 2012. Bioenergy for Sustainable Development and

International Competitiveness: The Role of Sugarcane in Africa. Experimental Agriculture Vol. 49.

Macedo et. al., 1993. Sugarcane etanol: Contributions to climate challenge mitigation

and the environment. Chapter 4. Oliveira L. M., Valdes Serra J.C., Magalhes K.B., 2012 Estudo Comparativo Das

Diferentes Tecnologias Utilizadas Para Producao De Etanol. Geo-Ambiente on-line. 1,4-6.

Rivera E.C., Costa A.C., Andrade R.R., Atala D.I.P, Maugeri Filho F., Maciel Filho R.,

2007. Development of adaptive modeling techniques to describe the temperature-dependent kinetics of biotechnological process, Biochem. Eng. J. 36, 157-166.

Tan T.K., Lee K.T. Mohamed, A.R., Role of energy policy in renewable energy

accomplishment: The case of second-generation bioethanol, Energy Policy 36, 3360-3365.

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