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Mejoramiento de extracción de aceite de palma en u= na planta industrial

 

Improvement of the extraction rate of red oil in the

 

 


1=

Jeffer= son Geovanny Navarro Alcívar

https://orcid.org/= 0000-0002-1664-7904

 

 

Escuela Superior Politécnica de Chimborazo (ESPOCH), Ciencias, Química, Riobamba, jefferson.navarro@espoch.= edu.ec

2=

Luis Santiago Carrera Almendáriz=

 <= /span>

https://orcid.org/= 0000-0002-3262-5895

 

 

Escuela Superior Politécnica de Chimborazo (ESPOCH), Ciencias, Química, Riobamba, luissantiago.carrera@= espoch.edu.ec  

3

Ana Gabriela Flores Huilcapi                                  https://orcid.= org/0000-0001-8748-7859

Escuela Superior Politécnica de Chimborazo (ESPOCH), Ciencias, GAIBAQ, Riobamba, ana.flores@espoch.edu.ec  

 

 

 

 

 

 

 

 

 

 <= /span>

Artículo de Investigación Científica y Tecnológica

Enviado: 09/04/2022=

Revisado: 25/05/2022

Aceptado: 23/06/2022

Publicado:08/07/2022

           DOI: https://doi.org/10.33262/concienciadigi= tal.v5i3.2206<= /o:p>

 

 

&= nbsp;

Cítese= :

&= nbsp;

 =

Navarro Alcívar, J. G., Carrera Almendáriz, L. S., & Flores Huilcapi, A. G. (2022). Mejoramiento de extracción = de aceite de palma en una planta industrial. Conciencia= Digital, 5(3), 68-84. https://doi.org/10.33262/concienciadigital.v5i3.2206

 =

 

3Deditorial1.png<= !--[if gte vml 1]>

 

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La rev= ista es editada por la Editorial Ciencia Digital (Editorial de prestigio registrada en la Cámara Ecuatoriana de Libro con No de Afiliación 663) www.celibro.org.ec

 

 

Esta revista está protegida bajo una licencia Cr= eative Commons Attribution Non Commercial No Derivatives 4.0 International. Copia de la licencia: http://creativecommons.org/licenses/by-nc-nd/4.0= /

 

Palabras claves:Autoclave, Extracción Soxhlet, Tricanter, Pérdidas de Aceite, <alma Aceitera (E= . Guineensis).

 

Resumen

Introducción: Las plantas extractoras de aceite crudo de palm= a en el Ecuador representan un eslabón importante para la industria alimentari= a. El aceite se extrae principalmente de los racimos de fruta fresca varieda= d Elaeis guineensis Jacq por su alto contenido, sin embargo, existen otras variedades que aportan en menor grado. La eficiencia de recuperación del aceite en las plantas depende de= la variedad y calidad de la fruta y sus condiciones de procesamiento.  Objetivo: Esta investigación bu= sca mejorar la tasa de extracción de aceite rojo a través de la evaluación de= la materia prima y sus procesos. Metodología: Se establece 2 meses de monitoreo en la planta industrial tanto de materia prima como procesos de producción. Durante el primer mes se establece las condiciones de operaci= ón y al siguiente se ajusta sus parámetros. Utilizando el método de extracción= Soxhlet se evaluó el potencial de aceite de cuatro variedades de racimos de palma aceitera y las pérdidas de aceite en la pl= anta de extracción. Por el método de centrifugación se determinó el porcentaje= de dilución del licor de prensa en el proceso de prensado-digestión y clarificación, además, se registró la temperatura de los digestores, del tanque de agua que alimenta las prensas y del licor de prensa antes de ingresar al Tricanter. Para la identificación= de las condiciones de operación en el proceso de esterilización se registró = el número de autoclaves procesadas, la presión de sostenimiento y el tiempo = de cocción. Resultados: La extracción de aceite de la variedad E. guineensis resultó en 20 % y estadísticamente = es significativamente diferente a las demás variedades. El balance de masa registró mayores pérdidas de aceite durante el primer mes. Conc= lusión: En cuanto a la materia prima los racimos E. guine= ensis, producen mayor cantidad de aceite. Se produjo mejores resultados cuan= do los racimos son esterilizados a 45 psi durante 50 min, y las condiciones = de temperatura de los digestores, tanque de agua y licor de prensa se encuen= tran a 95 C.

 

 

Keywords:

Auto= clave, Soxhlet Extraction, Tric= anter, Oil Loss, Oil Palm (E. Guineensis).

&= nbsp;

Abstract

Introduction: Extraction companies oversee extracting as much oil as possible from oil palm bunches and producing high quality oil. Objective: This study is called Improvement of the extraction rate of red oil in the Extractor "Atahualpa" Extracata S.A. The objective is to improve the extr= action rate of red oil by evaluating the raw material and the processes. = Methodology:= Using the Soxhlet extraction method, the oil potential of four varieties of oil palm cluste= rs and the oil losses in the extraction plant was evaluated. Using the centrifugation method, the dilution percentage of the press liquor was determined in the pressing-digestion and clarification process. In additi= on, the temperature of the digesters, the water tank that feeds the presses a= nd the press liquor was recorded before entering the Tr= icanter. To identify the operating conditions in the sterilization process, the nu= mber of autoclaves processed was recorded. holding pressure and cooking time. = Results:= For the statistical analysis of the four varieties of clusters, the Tukey test was performed, resulting in a significant difference between the Taisha var= iety and E. guineensis. According to the mass bala= nce, greater oil losses were recorded during the first month. Conclusion:<= /b> Concerning the raw material, the bunches of E= . guineensis produce a greater quantity of oil. Best results were produced when the bunches are sterilized at 45 psi for 50 min and the temperature conditions of the water tank and press liquor digeste= rs are at 95 degrees Celsius.

&= nbsp;

 

 

 

Introducción

La palma aceitera (Elaeis<= /i> guineensis) es una planta tropical, propia = de climas cálidos, en Ecuador tiene una trayectoria productiva por más de 60 a= ños, el cultivo actualmente representa el 5 % de la superficie total destinada a= la producción agropecuaria del país, siendo el segundo cultivo en extensión después del arroz. Existen 257.120,93 hectáreas sembradas en 8.149 plantaciones, siendo la provincia de Esmeraldas la de mayor superficie semb= rada con 116.430,48 hectáreas, seguida por Los Ríos con 39.146,08 hectáreas, otr= as 101.387,92 hectáreas y Santa Elena la menor superficie con 156,45 hectáreas= (Navarrete, 2020).<= /span>

Las plantas extractoras son empresas agroindustria= les cuya función principal es extraer la mayor cantidad posible de aceite de los racimos de fruta fresca (RFF), y producir aceite de alta calidad, ya que la extracción de aceite de palma se realiza en el campo, la planta extractora = solo puede optimizar sus operaciones de extracción (Tan et al., 1997; Carter et al., 2007; De Graef et al., 2006).<= /span>

Los racimos que se reciben en las plantas extracto= ras se clasifican conforme a la madurez y otros criterios que podrían afectar el proceso y la tasa de extracción de aceite, sin embargo, no hay un estimativo del contenido de aceite en el racimo recibido. Las plantas extractoras proc= esan racimos de frutos frescos provenientes de muchas fuentes y cuyo contenido de aceite se desconoce, y después calculan la tasa de extracción con base a la cantidad de aceite que se obtiene (Cock et al., 2015; Santosa, 2008; Gibon et al., 2007).

El control de proceso en una planta extractora de aceite tiene como fin la producción de productos de la mejor calidad y mantener la pérdida de productos al mínimo,= por lo tanto, se debe tomar muestras de rutina siempre que se considere necesar= io. Los puntos de muestreo y la frecuencia deben ser determinados por la determinación de la planta extractora (A. NGAN, 1998; Basiron, 2007).

La presente investigación busca evaluar principalm= ente la materia prima que está ingresando al área de recepción de fruta fresca, = las condiciones de operación que se aplican y las pérdidas que se generan duran= te el proceso de extracción de aceite rojo con la finalidad de optimizar los procesos y mejorar la tasa de extracción de aceite (TEA) (Uribe, 1999).

Metodología

Los datos obtenidos para esta investigación fueron tomados del área de recepció= n de fruta fresca y en la planta de extracción en las secciones más importantes = del proceso tales como esterilización, prensado-digestión y clarificación.=

Determinación del potencial de aceite de racimos de palma aceitera<= /span>

Se analizó el potencial de aceite de cuatro variedades de palma aceitera que ingresa al área de recepción de fruta fresca, tales como: palma híbrida Taisha, palma híbrida Coarí, palma híbrida Brunca y palma E. guineensis. Se realizó un diseño experimental en = cuadro latino 4x4, seguidamente un ANOVA y la prueba de Tukey= con la finalidad de identificar la variedad de mayor potencial de aceite que ingresa a la empresa y que pueda contribuir en el mejoramiento de la tasa de extracción de aceite (TEA) (Yáñez, 2= 008).

Se tomó un racimo de fruta fresca (RFF) al azar de la variedad a analizar, se = retiró todas las espigas del racimo, y se recolectó una muestra de 3000 g de espig= as con frutos, se clasificó en frutos normales externos e internos, frutos partenocárpicos rojos, frutos pa= rtenocápicos blancos y flores abortadas según se observa en la figura 1. Para el análisi= s se consideró únicamente los frutos normales externos e internos y se tomó una muestra de 10 frutos de ambas clases sin el mesocarpio. Para la técnica de = extracción soxhlet se tomó una muestra de 10 g de mesocarp= io fresco aceitoso de frutos externos e internos y se secó a 105 °C durante 24 horas. Se utilizó la cantidad de 200 mL de clor= oformo como solvente. El aceite recolectado fue colocado en la estufa por 2 horas a 105 °C para eliminar trazas de solvente que aún están presentes en el aceit= e.

Figura 1

Diagrama gener= al para la determinación del potencial de aceite de los racimos de palma aceit= era por el método de extracción Soxhlet<= /span>

3D"Interfaz

 

Tabla 1

Ecuaciones para la determinación del potencial de aceite

Ecuaciones

Porcentaje de espigas sobre racimo de fruta fresca (RFF)

Porcentaje de frutos externos sobre espigas

=

Porcentaje de frutos internos sob= re espigas

Porcentaje de mesocarpio de frutos externos

 

=

 

Porcentaje de mesocarpio de frutos internos

 

=

 

Porcentaje de aceite sobre muestra de mesocarpio= de frutos externos

 

Tabla 1

Ecuaciones para la determinación del potencial de aceite (continuación)

Ecuacio= nes=

Porcentaje de aceite de mesocarpio= de frutos externos sobre racimo de fruta fresca

=  

=

 

Porcentaje de aceite sobre muestra de mesocarpio= de frutos internos

 

=  

Porcentaje = de aceite de mesocarpio de frutos internos sobre racimo de fruta fresca=

=  

=

 

Porcentaje de aceite total sobre racimo de fruta fresca.

 

  Ec.10

=  

     Fuente: Cenipalma (1999)

Muestreo y elaboración del balance de masas

Se determinó un balance de masa para aquellas fuentes de pérdidas de aceite más importantes en la planta de extracción según el esquema de la figura 2 como: pérdidas de aceite en raquis, frutos adheridos, fibras, aguas efluentes y nueces. Este estudio se llevó a cabo durante dos meses.  

Para determinar pérdidas de aceite en fibras y nueces cada hora se tomó muestras= de 1000 g durante toda la jornada laboral. Al final del día se tomó una muestr= a de 10 g de fibras y 50 g de nueces para su posterior análisis.

Para el caso de pérdidas de aceite en raquis se tomó cada hora un raquis a la sa= lida de la banda transportadora y al final del día se tomó una muestra de 15 g. = También tomar 10 frutos adheridos a los raquis para su posterior análisis.

Para las pérdidas de aceite en las descargas líquidas del proceso, se almacenó 2= 00 mL de muestra cada hora durante toda la jornada labor= al. Al final del día se tomó 50 g de aguas efluentes.

Para el balance de masa se conoce los aforos en cada una de las corrientes de sa= lida de la planta de extracción según la tabla 2.

 

Tabla 2

Valores de aforo de la planta extractora

Punto de aforo

Valor de control

Raquis

                 20 % Raquis/RFF

Fibra

                 15 % Fibra/RFF

Nuez

                 11,24 % Nuez/RFF<= /o:p>

Aguas efluentes

                  0,79 =

 

Figura 2

Procedimiento general para la extracción de aceite rojo y fuentes de pérdidas de aceite en cada corriente de salida=

3D"Diagrama

Descripción

 

 

 

 

 

 

 

 

Tabla 3

Ecuaciones para la elaboración del balance de masa= s

Ecuaciones

Ecuaciones para la determinación d= e pérdida de aceite en raquis

&nbs= p;

  Ec.11

 

=

 

 

 

SSNA: Sólido seco no aceitoso.=

 

SSA: Sólido seco aceitoso.

 

A.E: Aceite extraído.

 

<= !--[if gte msEquation 12]>= % ACRFF: Porcentaje de pérdida de aceite sobre racimo de fruta fresca.

 

<= !--[if gte msEquation 12]>= %  R= aquisRFF: Porcentaje de raquis sobre racim= o de fruta fresca.

 

Ecuaciones para la determinación = de pérdida de aceite en frutos adheridos

 

 

=

 

Ecuaciones para la determinación de pérdida de aceite en fibras

 

 

=

 

 

=

Tabla 3<= /b>

Ecuaciones para la elabora= ción del balance de masas (continuación)

= Ecuaciones

Ecuaciones para la determinación = de pérdida de aceite en aguas efluentes

 

<= ![if !msEquation]>

 

: Porcentaje de pérdida de aceite = en efluentes líquidos sobre racimo de fruta fresca.=

 

: Volumen en metros cúbicos de efluentes sobre toneladas de racimos de fruta fresca procesada.

 

: gramos de aceite perdido por cada litro de aguas efluentes.

 

Ecuaciones para la determinación = de pérdida de aceite en nueces

 

 

: Porcentaje de pérdida de aceite impregnado en nueces sobre racimo de fruta fresca.

 

:  Porcentaje de nueces sobre racimo de fruta fresca.

           Fuente: Cala et al. (2011)

Identificación= de las condiciones de operación para una óptima extracción de aceite rojo=

Las tres secciones más importantes de la planta de extracción son: esterilizaci= ón, prensado -digestión y clarificación según se observa en la figura 3. Para la sección de esterilización se consideró dos evaluaciones durante el proceso = de 100 ton RFF de cada variedad al ser sometidas a diferentes condiciones de presión y tiempo de cocción. La primera evaluación consiste en comparar la = tasa de extracción de aceite que la empresa obtuvo dos meses antes de la investigación cuando las variedades fueron sometidas a 50 psi durante 60 mi= n de cocción para el primer mes y 50 min de cocción para el segundo mes. En la segunda evaluación se comparó la tasa de extracción cuando las variedades s= on sometidas a 45 psi durante 60 min de cocción para el primer mes y 50 min de cocción para el segundo mes, con la finalidad de identificar a qué condicio= nes de operación existe un incremento de la tasa de extracción de aceite y adem= ás comprobar cuál de las cuatro variedades produce mayor cantidad de aceite.

Para la determinación de la tasa de extracción de aceite (TEA) se aplicó la siguiente ecuación:

En la sección de prensado - digestión se determinó el porcentaje de dilución d= el licor de prensa a la salida del tamiz vibratorio cuando los digestores y el agua que alimenta la prensa se encuentran en condiciones de temperatura de = 85 y 95 °C. Durante cada hora en tubos de ensayos se tomó 10 mL de licor de prensa e inmediatamente se llevó a centrifugación a 4200 rpm y finalmente se registró el porcentaje del volumen de aceite, porcentaje de l= odo ligero, porcentaje de agua y porcentaje de lodo pesado.

En la sección de clarificación se determinó el porcentaje de dilución del lico= r de prensa antes del ingreso al tricanter o separad= or de tres fases cuando el licor se encuentra en condiciones de temperatura de 85= y 95 °C. Cada hora en tubos de ensayos se tomó 10 mL de licor de prensa e inmediatamente se llevó a centrifugación a 4200 rpm y finalmente se registró el porcentaje de volumen de aceite, porcentaje de lo= do ligero, porcentaje de agua y porcentaje de lodo pesado.

Para la determinación del porcentaje de dilución en el proceso de presado – digestión y clarificación se aplicó la siguiente ecuación:

<= /span>

Figura 3=

Puntos de muestreo en las tres secciones más importantes del proceso de extracción de aceite rojo

3D"Diagrama

Descripción

Resultados

Al determinar el potencial de aceite de cuatro variedades de palma aceitera por el método de extracción Soxhlet, se puede observar en los cuatro tratamientos de la Tabla 4, que la variedad= E. guineensis contiene mayor porcentaje de ace= ite residual, mientras que, las variedades de palma híbrida presentan menores porcentajes de aceite, en especial los racimos híbridos Brunca considerada como la variedad de menor calidad.

Tabla 4<= /o:p>

Resultados del potencial de aceite de racimos de palma aceitera

Contenido de aceite variedades de palma

(%)

TRAT.

Palma híbrida Taisha=

Palma híbrida Coarí<= /p>

Palma híbrida Brunca=

Palma

E. guineensis

1

14,68

23,58

13,58

29,47

2

20,27

22,18

13,27

28,63

3

14,05

19,08

11,30

27,08

4

16,47

20,32

13,05

26,56

 

Aplicando ANOVA a los resultados del contenido de aceite a las variedades de palma mostrados en la tabla 4 se, determina que existen diferencias significativas entre las diferentes variedades. En la prueba de Tukey que se realizó se identificó diferencia de medias entre el tratamiento 1 y tratamiento 3, es decir, las mayores diferencias se presentan ent= re la Palma híbrida Taisha y la Palma E. guineensis.

Tabla 5

Resultados de las pérdidas de aceite en las fuentes más importantes de la planta de extracción


MES 1

&n= bsp;

PÉRIDAS EN:

PARAMET= ROS

SEM 1

SEM 2

SEM 3

SEM 4

PROMEDI= O

CANT (t= on)

Raquis

% AC/RFF (impregnado en raquis)

0,53=

0,56=

0,59=

0,61=

0,57=

2,280<= /o:p>

Frutos adheridos

%AC/RFF (en fruto adherido al raquis)

0,09=

0,07=

0,05=

0,03=

0,06=

0,240<= /o:p>

Fibras

% AC/RFF (impregnado en fibra)

0,82=

0,51=

0,62=

0,59=

0,64=

2,560<= /o:p>

Aguas efluentes

% AC/RFF (por efluentes líquidos)

1,36=

1,41=

1,31=

1,47=

1,39=

5,560<= /o:p>

Nueces

% AC/RFF (impregnado en nueces)

0,07=

0,04=

0,04=

0,05=

0,05=

0.200<= /o:p>

TOTAL, PÉRDIDAS (%AC/RFF)

2,87

2,59

2,61

2,75

2,71

10,840=

MES 2<= /o:p>

 =

PÉRDIDAS EN:

   PARAM= ETROS

SEM 1<= /o:p>

SEM 2<= /o:p>

SEM 3<= /o:p>

SEM 4<= /o:p>

PROMEDIO

CANT (ton)<= o:p>

Raquis

% AC/RFF (impregnado en raquis)

0,59

0,59

0,60

0,53

0,58

2,320<= /o:p>

Frutos adheridos

%AC/RFF (en fruto adherido al raquis)=

0,05

0,04

0,06

0,07

0,05

0,200<= /o:p>

Fibras

% AC/RFF (impregnado en fibra)=

0,57

0,52

0,57

0,59

0,56

2,240<= /o:p>

Aguas efluentes

% AC/RFF (por efluentes líquidos)

1,47

1,42

1,23

1,14

1,32

5,280<= /o:p>

Nueces

% AC/RFF (impregnado en nueces)

0,06

0,04

0,06

0,04

0,05

0,200<= /o:p>

TOTAL, PÉRDIDAS (%AC/RFF)

2,74=

2,61=

2,52=

2,37=

2,56=

10,240=

 

El control de pérdidas de aceite en la planta de extracción se llevó a cabo a través de un balance de masa según tabla 5, en= el cual se identificó una pérdida promedio de aceite en raquis de 0,57 % en el primer mes y 0,58 % durante el segundo mes de proceso, encontrándose dichas pérdidas dentro de los límites permisibles. Durante el desfrutamiento en el interior del tambor desfrutador, el raquis entra en contacto con los frutos y otros racimos generando que el aceite se impregne en el raquis, la norma admite un valor de pérdida en raquis de 0,4= 0 a 0,60 %, es decir, se cumple la norma establecida (Uribe, 1999).

En la tabla 5, el porcentaje promedio de pérdidas = de aceite en frutos adheridos en el primer mes es de 0,06 % y el segundo mes de 0,05 %. No todos los frutos del racimo son desprendidos del raquis, y por e= nde se produce la pérdida del aceite contenido, la norma establece un valor permisible para la pérdida en un rango de 0,03-0,05 %, es decir, solo el segundo mes cumple la norma establecida (Uribe, 1999).

De acuerdo con la tabla 5, la pérdida prome= dio de aceite en fibras en el primer mes es 0,64 % y 0,56 % para el segundo mes. Durante el prensado, algunas celdas que contienen el aceite no se rompen, ocasionan= do una pérdida en el residuo, la norma permite un máximo para la pérdida en un rango de 0,50 - 0,60 %, de tal manera, que la pérdida promedio de aceite en fibras durante el primer mes se encuentra dentro de los límites permisibles= .

Las pérdidas de aceite en aguas efluentes debe est= ar en el rango de 0,5 al 0,7 %. En la Tabla 5, se puede apreciar una pérdida promedio de 1,39 % en el primer mes y un 1,32 % en el segundo mes, es decir, son las pérdidas de aceite más altas que se producen en la planta de extrac= ción con un rango promedio de 5,280 - 5,560 Ton de aceite rojo aproximadamente <= /span>(Yan & Lai, 2006).

Los residuos de mesocarpio y el aceite impregnado = en las nueces constituyen pérdidas de aceite en este subproducto, la norma establece un máximo permisible en el rango de 0,05 - 0,06 % (Uribe, 1999). En la tabla 6 se puede apreciar una pérdida prom= edio de aceite impregnado en nueces de 0,05 % en los dos meses de proceso, es de= cir, se encuentra dentro de los límites permisibles en el rango de 0,05 – 0,06 %= .

De acuerdo a l= a tabla 5, en el primer mes se obtuvo una pérdida total de 2,71 %, eso significa qu= e el 2,71 % del total de racimos procesados durante dicho mes equivale a la cant= idad de aceite perdido, es decir, durante el primer mes se procesó en total 400,= 000 ton de RFF, entonces, se estima que se perdió 10,849 ton de aceite rojo aproximadamente, mientras tanto, en el segundo mes al procesar 400,000 ton = de RFF con un 2,56 % de pérdidas totales, se produjo una pérdida de 10,240 ton= de aceite rojo aproximadamente. El porcentaje de pérdida total de aceite debe = ser como máximo 1,86 % (A. NGAN, 1998). Sin embargo, el porcentaje de pérdidas totales de aceite en la Extractora es del 2,71 % y 2,56 %.

Tabla 6

Porcentajes de extracción = de aceite según el tipo de variedad de fruta procesada

Tasa de= extracción de aceite (%)

Varieda= des

Evaluac= ión 1

Evaluac= ión 2

Promedi= o

Mes 1

Mes 2

Mes 1

Mes 2

Taisha

15,83

15,88

16,19

16,22

16,03

Coarí=

16,10

16,89

17,22

17,50

16,93

Brunca

11,43

12,00

12,50

13,64

12,39

E. guineensis=

20,25

20,93

21,05

21,43

20,92 <= o:p>

 

Según la tabla= 6 la evaluación 1 corresponde al período antes de la investigación. Durante el periodo de investigación que corresponde a la evaluación 2 se observa un incremento de la tasa de extracción de aceite durante el segundo mes condiciones de operación en la esterilización a 45 psi durante 50 min, mien= tras que, el primer mes es inferiores mantuvo una esterilización a 45 psi durant= e 60 min.

Tabla 7

Porcentajes de dilución = del licor de prensa en el proceso de prensado-digestión

Mes 1

Mes 2

T °C Digestor #1

T °C Digestor #2

T °C Del Agua

% Dilución

T °C Digestor #1

T °C Digestor #2

T °C Del Agua

% Dilución

85,00

85,00

85,00

0,93

95,00

95,00

95,00

1,58

85,00

85,00

85,00

0,94

95,00

95,00

95,00

1,40

85,00

85,00

85,00

0,91

95,00

95,00

95,00

1,27

85,00

85,00

85,00

0,93

95,00

95,00

95,00

1,30

Promedio

 

 

0,93

 

 

 

1,38

 

En el proceso de prensado – digestión descrita en la tabla 7, durante el primer mes se obtuvo un porcentaje de dilución promedio de 0,93 % cuando los digestores que maceran los frutos y el agua que se agrega en la etapa de prensado se encuentran en condiciones de temperatura de 85 °C, sin embargo,= en el segundo mes el porcentaje de dilución promedio incrementa a 1,38 % al es= tar operando los digestores y el agua de prensa a 95 °C. Experimentalmente han comprobado que el porcentaje de dilución de 1,40 % vol. aceite / % vol. agu= a es óptima para el licor de prensa, pues permite una rápida separación del acei= te, un incremento global en la eficiencia del proceso y la reducción del impacto ambiental por disminución en el consumo de agua y generación de efluentes <= /span>(Yáñez, 2= 008). La carga dentro del digestor debe mantenerse en un rango de temperaturas entre los 9= 2 - 95 °C y mantener siempre lleno el digestor u operar al menos a ¾ de lleno <= /span>(Mohamad = et al., 2008).

Tabla 8

Porcentajes de dilución del licor de prensa en el proceso de clarificación

Mes 1

Mes 2<= /o:p>

T °C <= /o:p>

Licor De Pr= ensa

% Dilución<= o:p>

T °C <= /o:p>

Licor De Pr= ensa

%

Dilución

85,00<= /o:p>

0,92

95,00<= /o:p>

1,24

85,00<= /o:p>

0,90

95,00<= /o:p>

1,23

85,00<= /o:p>

0,89

95,00<= /o:p>

1,23

85,00<= /o:p>

0,93

95,00<= /o:p>

1,19

Promedio

0,91

 =

1,22

 

En la tabla 9, se puede apreciar un incremento del porcentaje de dilución en un 1,22 % cuando la temperatura del licor de pren= sa antes de ingresar al Tricanter o Separador de t= res fases se encuentra a 95 °C, esto indica que en el segundo mes hubo una mejor separación del aceite del resto de productos tales como agua, lodos ligeros= y lodos pesados. El porcentaje de dilución óptimo es de (1,40 % vol. aceite /= % vol. agua) (Matthäus, 2007), y la temperatura del licor de prensa debe manten= erse en un rango entre los 92 y los 97 °C (Lumor & Akoh, 2005).

Conclusiones<= /b>

·&nb= sp;        A = nivel industrial se puede obtener una tasa de extracción de aceite rojo mínimo de= l 20 % cuando la mayor parte de materia prima que se procese sea variedad E. guineensis. En la evaluación se registra una pérdida = de aceite en aguas efluentes de 2,71% en el primer mes y 2,56 % en el segundo.= El cambio de parámetros en los procesos de esterilización a 45 psi y 50 min; e= n el prensado - digestión a 95 C y clarificación a 95 C logran mejorar la recuperación de aceite. El estudio sugiere incrementar la temperatura del l= icor de prensa en el tanque homogeneizador para que ingrese con mayor temperatur= a al tricanter y permita una separación rápida del a= ceite.

 

 

Refe= rencias bibliográficas

 

A. NGAN, M. (1998). La pla= nta extractora de aceite de palma. Control del proceso. XII Conferencia Internacional de Palma Aceitera. Fedepalma., 19.

Basiron, Y. (2007). Palm oil production through sustainable plantations. European Journal of Lipid Science and Technology, 109(4), 289–295. https://doi.org/10.1002/ejlt.200600223

Cala, S. L. A., Yáñez, E. = E. A., & García, J. A. N. (2011). Manual de procedimientos de laborator= io en plantas de beneficio - Cenipalma.

Carter, C., Finley, W., Fry, J., Jacks= on, D., & Willis, L. (2007). Palm oil markets and future supply. European Journal of Lipid Science and Technology, 109(4), 307–314. https://doi.org/10.1002/ejlt.200600256

Cock, J., Program, S. A., Donough, C. = R., Program, S. A., Program, S. A., Indrasuara, K., & Dolong, T. (2015). Aumento de los rendimientos de aceite de palma mediante el campo hasta las plantas procesadoras * Increasing Palm Oil Yields by Measuring Oil Recovery Efficie= ncy from the Fields to the Mills. 36(1), 63–77.

De Graef, = V., Dewettinck, K., Verbeken, D., & Foubert, I. (2006). Rheological behavio= r of crystallizing palm oil. European Journal of Lipid Science and Technology= , 108(10), 864–870. https://doi.org/10.1002/ejlt.200600102<= /span>

Gibon, V., De Greyt, W., & Kellens, M. (2007). Palm oil refining. European Journal of Lipid Science and Technol= ogy, 109(4), 315–335. https://doi.org/10.1002/ejlt.200600307

Lumor, S. E., & Akoh, C. C. (2005). Incorporation of γ-linolenic and linoleic acids into a palm kernel oil/palm olein blend. European Journal of Lipid Science and Technology, 107(7–8), 447–454. https://doi.org/10.1002/ejlt.200501157

Matthäus, B. (2007). Use of palm oil for fryin= g in comparison with other high-stability oils. European Journal of Lipid Sci= ence and Technology, 109(4), 400–409. https://doi.org/10.1002/ejlt.200600294

Mohamad Ibrahim, M. N., Nadiah, M. Y. = N., Norliyana, M. S., Sipaut, C. S., & Shuib, S. (2008). Separation of vani= llin from oil palm empty fruit bunch lignin. Clean - Soil, Air, Water, 36(3), 287–291. https://doi.org/10.1002/clen.200700141

Navarrete, M. (2020). Evaluation of the efficiency of three oil extraction equipments with different oil palm genot= ypes (Elaeis sp.). Scientific Engineering Journal.

Santosa= , S. J. (2008). Palm oil boom in Indonesia: From plantation to downstream products and biodiesel. Clean - Soil, Air, Water, 36(5–6), 453–465. https://doi.org/10.1002/clen= .200800039

Tan, Y. A., Chong, C. L., & Low, K= . S. (1997). Crude palm oil characteristics and chlorophyll content. Journal = of the Science of Food and Agriculture, 75(3), 281–288. https://doi.org/10.1002/(SICI)1097-0010(199711)75:3<281: AID-JSFA875>= 3.0.CO;2-A

Uribe, L. (1999). Eficienc= ia en la recuperación de aceite. Efecto de las prácticas agronómicas y el proc= eso industrial en la tasa de recuperación de aceite (tea). Palmas, 20(2), 31–40.

Yan, H. M., & Lai, T. P. (2006). CFD modeling of biomass combustion in palm oil was= te boiler. Developments in Chemical Engineering and Mineral Processing,= 14(1–2), 259–276. https://doi.org/10.1002/apj.5500140123

Yáñez A., É. (2008). Determinación del nivel de dilución apropiado en el proceso de clarificació= n y diseño de un sistema de control automático. Palmas, 29(4), 21= –30.

3Deditorial1.png

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

 

El artículo que se publica es de exclusiva responsabilidad de los autor= es y no necesariamente reflejan el pensamiento de la Revista Conciencia Digital.

3Deditorial1.png

 

 

 

El artículo queda en propiedad de la revista= y, por tanto, su publicación parcial y/o total en otro medio tiene que ser autorizado por el director de la R= evista Conciencia Digital.

 

3D"logo_catalogo3b.jpg"

 

 

 


 

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