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Optimización energética industrial con recuperadores de calor y un ciclo de Rankine orgánico regenerativo

Industrial energy optimization with heat recuperat= ors and a regenerative organic Rankine cycle

= ¹=	Saúl David Valdez Rosales=	<= /span>	https://orci= d.org/0000-0001-6129-5170
<= /span>	Esc= uela Superior Politécnica de Chimborazo (ESPOCH) saul.valdez@espoch.edu.ec=
= ²=	Paúl Gustavo Palmay Paredes=	<= /span>	https://orci= d.org/0000-0002-9172-4113
<= /span>	Escuela Superior Politécnica de Chimborazo (ESPO= CH) paul.palmay= @espoch.edu.ec=
= ³=	Mónica Lilián Andrade Avalos=	<= /span>	https://orcid.org/0000-0001-5736-5607
<= /span>	Escuela Superior Politécnica de Chimborazo (ESPO= CH) moandrade@espoch.edu.ec=

Artículo de Investigación Científica y Tecnológica

Enviado: 07/01/2022

Revisado: 22/02/2022

Aceptado: 03/03/2022

Publicado:25/04/2022

DOI: https://doi.org/10.33262/concie= nciadigital.v5i2.2144 <= o:p>

<= o:p> <= /p>

=

Cítese: <= /o:p>

&= nbsp;

Valdez Rosales, S. D., Palmay Paredes, P. G., & Andrade Avalos, M. L. (2022). Optimización energética industrial con recuperadores de calor y un ciclo = de Rankine orgánico regenerativo. ConcienciaDigital, 5(2), 140-161. <= /span>https://doi.org/10.33262/concienciadigital.v5i2.= 2144 =

CONCIENCIA DIGITAL, es una r= evista multidisciplinar, trimestral, que se publicará en soporte electrónico tiene como misión contribuir a la formación de profesionales competentes con visión humanística y crítica q= ue sean capaces de exponer sus resultados investigativos y científicos en la misma medida que se promueva mediante su intervención cambios positivos e= n la sociedad. https:/= /concienciadigital.org =

La revi= sta 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 r= evista está protegida bajo una licencia Creative Commons Attribution Non Commerc= ial No Derivatives 4.0 International. Copia de la licencia: http://= creativecommons.org/licenses/by-nc-nd/4.0/

Palabras claves:

optimiz= ación energética; balance de masa y energía; recuperadores de calor; ciclo de r= ankine orgánico regenerativo.

Resumen

En el Ecuador, la Industria de extracción de aceite rojo de palma africana, = en las provincias de Santo Domingo de los Tsáchilas y Esmeraldas ha tenido un crecimiento en los últimos ańos con un promedio de producción de 19 a 25 = tn/h de fruto. El proceso de extracción de aceite rojo de palma africana se lo realiza principalmente p= or digestión de la fruta en un cilindro calentado con vapor, en donde la fru= ta digerida es prensada para extraer aceite bruto y el licor de prensa que se dirige al clarificador para clarificar el aceite y posteriormente secarlo, por lo tanto, la necesidad energética de la planta industrial es elevada.= El objetivo principal del presente trabajo de investigación es realizar la <= span style=3D'color:black;mso-themecolor:text1'>optimización energética de un proceso industrial de extracción de aceite de palma, mediante el uso de recuperadores de calor y un ciclo de Rankine orgánico regenerativo. Para = lo cual se realizó un balance de masa y energía a partir de los datos recopilados de la extractora San Daniel, Cantón la Concordia, Provincia Santo Domingo de = los Tsáchilas de varios meses de producción a condiciones estacionarias, para cuantificar la energía residual generada en el proceso. Se determinaron varios puntos potenciales de energía residual aprovechable, los cuales corresponden a la purga de la caldera que tiene un flujo de 0,592 tn/h y = un calor residual de 424,3 KW, los gases de escape de la chimenea de la cald= era un flujo de 10,18 tn/h y un calor residual de 1543 KW, la operación de se= cado un flujo de 0,244 tn/h y un calor residual de 211,1 KW, la digestión del fruto de palma 0,448 tn/h y un calor residual de 35,82 KW y la esteriliza= ción de los racimos de palma africana un flujo de 1,47 tn/h y un calor residua= l de 1723 KW. A partir de los datos encontrados se realizó la simulación de cu= atro recuperadores de calor y un ciclo de Rankine orgánico regenerativo en el software DWSIM. Co los resultados obtenidos se concluye que a través de e= stos dispositivos se podrá generar una reducción del consumo de vapor producido por la caldera de 5,86 a 4,61 tn/h y además se producirán 227,68 KW/h de energía eléctrica.

Keywords:

energy optimi= zation; mass and energy balance; heat recovery units; regenerative organic rankin= e cycle.

Abstract=

In Ecuador, the industry for the extraction of red African palm oil in the provinces of Santo Domingo de Los Tsáchilas and Esmeraldas has grown in recent years with an average production of 19 to 25 tn/h of fruit. The red African palm oil extraction process is conducted by digesting the fruit i= n a cylinder heated with steam, where the digested fruit is pressed to extract crude oil and the press liquor is directed to the clarifier to clarify the oil. oil and subsequently dry it, therefore, the energy need of the industrial plant is high. The main objective of this research work is to perform the energy optimization of an industrial palm oil extraction proc= ess, using heat recuperators and a regenerative organic Rankine cycle. For whi= ch a mass and energy balance was made from the data collected from the San Dan= iel extractor, the Concordia, Santo Domingo de Los Tsáchilas Province of seve= ral months of production at stationary conditions, to quantify the residual energy generated in the process. Several potential points of usable resid= ual energy were determined, which correspond to the purge of the boiler that = has a flow of 0.592 tn/h, and a residual heat of 424.3 KW, the exhaust gases = from the boiler chimney a flow of 10.18 tn/h and a residual heat of 1543 KW, t= he drying operation a flow of 0.244 tn/h and a residual heat of 211.1 KW, the digestion of the palm fruit 0.448 tn/h and a residual heat of 35.82 KW and the sterilization of the African palm bunches a flow of 1.47 tn/h and a residual heat of 1723 KW. From the data found, the simulation of four heat recuperators and a regenerative organic Rankine cycle was conducted in the DWSIM software. With the results obtained, it is concluded that through t= hese devices it will be possible to generate a reduction in the consumption of steam produced by the boiler from 5.86 to 4.61 tn/h, and in addition, 227= .68 KW/h of electrical energy will be produced.

Introducción

= El desarrollo industrial se ha incrementado considerablemente en los últimos ańos lo que = ha ocasionado el agotamiento de los combustibles fósiles por tal razón la búsq= ueda de fuentes de energías alternativas que sean renovables se hace cada vez más imperiosa de tal manera que se logre reducir la dependencia de los recursos= no renovables como lo son los combustibles de uso común (Aranguren, 2015). El cont= inuo encarecimiento del combustible, así como una mayor necesidad de aumentar la eficiencia energética en la industria, ha provocado que, en los últimos ańo= s, se busque poner en valor la energía “residual” que hasta ahora era lanzada = a la atmosfera sin ningún tipo de aprovechamiento (Habibi et al., 2018).

De las fuentes de energías alternativas una de las= más comunes es el uso de biomasas como combustible que resulta una oportunidad = para palear la problemática energética, sin embargo, el exceso de su incineración puede resultar peligrosa debido a la generación progresiva de sustancias tóxicas, por lo que su uso debe ser realizado bajo un control estricto de t= al manera que se eviten productos no deseados en el medio (Borja, 2018).<= /o:p>

En los procesos industriales se generan grandes pérdidas de energía en forma de calor residual, ésta es una fuente de energ= ía alternativa que puede ser aprovechada como combustible en algunos procesos,= a pesar de ello, la realidad es que, en la mayoría de las empresas, actualmen= te esta energía residual es desaprovechada y es expulsada al ambiente (Guo &am= p; Jiang, 2019). El calor residual po= dría ser empleado como reemplazo de los combustibles fósiles en ciertas etapas o procesos, debido a las características que presenta y a los ahorros energét= icos y económicos que representaría, estas son algunas de las razones que han ido despertando paulatinamente el interés de investigadores y empresas (Banda &= amp; Gutiérrez, 2016).

La necesidad de incrementar la eficiencia energética en la industria ha ocasionado que, en = los últimos ańos, se busque revalorizar la energía “residual” que actualmente es emitida a la atmosfera sin ningún tipo de aprovechamiento (Valdez, 2021). <= /span>Las pérdi= das de energía que se producen en la planta industrial estudiada son elevadas, = ya que cuenta con un flujo continuo de aproximadamente 10 tn/h y una temperatu= ra de 250 şC la cual no es aprovechada. La misma puede ser una fuente útil de energía que se puede aprovechar en beneficio de la industria, mediante el incremento de la eficiencia térmica del sistema de generación de vapor con = el que cuenta la planta y por ende varias etapas del respectivo proceso (Cengel & Boles, 2015), de tal manera que se pueda revalorizar esta energía que actualmente es desperdiciada y emitida hacia la atmósfera. Esta investigaci= ón, estima realizar el aprovechamiento de la energía residual producida, optimizando el proceso energético y como resultado generar un ahorro económ= ico.=

El desarrollo de = esta investigación tiene un gran aporte a la industria, debido a que se aprovech= ará la energía residual generada en este sector, logrando mejores rendimientos = de producción, mitigando la destrucción de la capa de ozono como consecuencia = del uso excesivo de biomasas y expulsión de gases de escape a elevadas temperat= uras hacia el medio en forma de calor y generando un mayor rendimiento en la elaboración de sus productos (Valdez, 2021).

La extracción de aceite rojo de palma africana incluye varias etapas y por ende requiere una alta demanda energética, una vez que la fruta es recepta esta es llevada al esterilizador, seguidamente es conducida a un desfrutador con la finalidad = de separar los frutos esterilizados de los racimos de palma, los frutos sueltos son llevados al digestor en donde estos son macerados. La fruta digerida pa= sa a un proceso de prensado en el cual se obtiene el aceite bruto, el mismo es dirigido al tamizador y posteriormente a un clarificador en el cual el acei= te de palma es separado por diferencia de densidades, el aceite separado es llevado al secador para posteriormente ser almacenado y listo para su comercialización, cabe indicar que las etapas de esterilización, digestión,= y secado se utiliza como energía vapor de agua el cual es producido por la caldera de la planta (Paz, 2017). El combustible utilizado en la caldera es= una biomasa conformada en su totalidad por fibra la cual es subproducto de la t= orta remanente del proceso de extracción del fruto de palma.

Metodología

Material y Métodos

Para llevar a cabo el desarrollo del presente trab= ajo de investigación se revisaron los datos correspondientes al último ańo de producción de la planta, de los cuales para el desarrollo de los cálculos de ingeniería se tomó como referencia los promedios semanales de producción a condiciones estacionarias de las últimas doce semanas. Se desarrolló el diagnóstico del funcionamiento actual del proceso a mejorar, mediante la ejecución de un balance de masa y energía del proceso estudiado con la finalidad de identificar cada uno de los focos calientes de la planta. A pa= rtir de los datos obtenidos se desarrolló la simulación en el software DWSIM de = las dos propuestas planteadas las cuales consisten en implementar ya sea Recuperadores de Calor o un Ciclo de Rankine Orgánico Regenerativo. Posteriormente se realizó el análisis técnico y económico de los resultados obtenidos en la simulación y se hizo la validación con varias fuentes bibliográficas.

Recuperador del calor

Se plantea agregar intercambiadores de calor al proceso industrial estudiado con la finalidad = de incrementar la eficiencia energética de la planta mediante el aprovechamien= to de la energía residual producida en la planta, para lo cual a partir de los datos obtenidos en los cálculos de ingeniería y la simulación efectuada en = el software DWSIM de los dispositivos descritos se analizará los puntos potenciales de energía residual aprovechable.

Las condiciones de operación que se utilizarán para realizar la simulación de estos dispositiv= os se muestran en las tablas de resultados de balance de masa y energía.<= /o:p>

Figura 1

Propuesta recuperadores de calor

=

Nota: = Esquema gráfico del proceso de recuperación de cal= or en el proceso de extracción de aceite de palama africana<= /span>

Fuente: Valdez (2021)

<= span style=3D'mso-bookmark:_Hlk81985521'>Para aprovechar la energía residual en la extractora también se propone la implementación de un Ciclo de Rankine Orgánico (ORC) el cual es un sistema cuyo fluido de trabaj= o es un compuesto orgánico y utiliza flujos de baja y media temperatura para gen= erar energía eléctrica. De acuerdo con los resultados obtenidos del balance de d= el proceso, el vapor de purga proveniente de los gases de escape derivados de = la chimenea de la caldera tiene flujos másicos elevados y temperaturas convenientes para activar un ORC.

Figura 2

Propuesta Ciclo de Rankine Orgánico (ORC)

Nota: Esquema general de la implementación de un Ciclo Orgánico de Rankine = en la recuperación de calor del proceso de obtención de aceite de palma africa= na

Fuente: Valdez (2021)

Por lo tanto, con= los datos mostrados en las tablas de resultados de los balances se realizará la simulación del ciclo termodinámico descrito, para la misma se utilizará el modelo termodinámico Peng Robinson y como fluido de trabajo el ciclohexano debido a que su temperatura de ebullición se ajusta a las condiciones del proceso industrial.

Figura 3

Ciclo de Rankine

=

=

=

=

=

=



=

Nota: = Esquema gráfico general de un Ciclo de Rankine

Fuente: Valdez (2021)

=

=

=

=

=

Resultados y Discusión

Balance de Masa

El desarrollo del balance de masa permitió determinar los flujos másicos de cada una de las operaciones del proceso estudiado, a continuación, se presentan los datos m= ás importantes en la siguiente tabla
= Tabla 1

Resultados del Balance de Masa

Sistema de Generación de Vapor (Cald= era)

Corrientes

Nomenclatura

Flujo másico (tn/h)

Agua

W1

5,86

Vapor Proceso

V

5,86

Gases de Escape

G

10,18

Vapor Purga=

VP

0,592

Fibra

FP

2,188

Esterilizador<= /span>

Vapor Esterilizador

V2

4,11

Palma Africana Cruda

R

19,55

Palma Africana Cocida

R2

17,87

Purga Esterilizador

P1

1,47

Condensados=

C

4,32

Desfrutamiento

Frutos Sueltos

F

14,299

Raquiz

RQ

3,575

Digestor

Vapor Digestor

V3

0,733

Frutos Digeridos

D

14,584

Purga Digestor

PD

0,448

Tabla 1

Resultados del Balance de Masa = (continuación)

Sistema de Generación de Vapor (Cald= era)

Corrientes

Nomenclatura

Flujo másico (tn/h)

Prensa =

Aceite Bruto

P

10,755

Torta

T

3,829

Prensa Raquiz<= /span>

Aceite Raquiz

ARQ

0,552

Raquiz Desecho

RQ2

3,023

Desfibración

Fibra

FP

2,188

Nueces

N

1,642

Clarificación<= /span>

Aceite Húmedo

L

7,396

Aceite Lodoso

AL

3,359

Secador=

Vapor Secador

V4

0,244

Aceite Terminado

A

5,7

Purga Secador

AP

0,244

Centrifugador<= /span>

Aceite Recuperado<= /span>

AR

1,246

Aguas Lodosas

TE

2,113

                  =       Fuente: Valdez (2021)

Balance de Energía

El balance de ene= rgía es efectuado con la finalidad de conocer la energía requerida y desechada en cada operación del proceso, las etapas analizadas en el presente proyecto s= on: sistema de generación de vapor, esterilización, digestión y secado, las cua= les son sistemas abiertos por que existe un intercambio de masa y energía entre= el sistema y sus alrededores. Además, se considera que cada etapa trabaja en un régimen estacionario, en donde las temperaturas y presiones del proceso permanecen constantes, el combustible empleado en la caldera es la fibra de palma la cual está compuesta en su mayoría por celulosa y tiene un poder calorífico de 12150.8 KJ/Kg (Torres & Quintero, 2019).

De acuerdo con Ba= tty et al. (1990), los valores pertinentes son calculados a las capacidades caloríficas de la fruta de palma africana y aceite de palma africana en cada una de las etapas estudiadas.

Mediante el balan= ce de energía se calculó la energía residual en cada operación del proceso com= o se describe en la siguiente tabla:

Tabla 2

Resultados del Balance de Energía

= Sistema de Generación de Vapor (Caldera)

Corrientes

Nomenclatura

Flujo (KW)

Calor del Agua

Qagua

5842

Calor del Combustible

Qcomb

7385

Calor Gases de Escape

Qperdido

1543

Calor de la purga caldera

Qpurgacal

424,3

Esterilizador

Calor del Esterilizador

Qester

4614

Calor de la purga

Qpester

1723

Digestor

Calor del Digestor

Qdig

569,9

Calor de la purga

Qpdig

35,82

Secador

Calor del Secador

Qsec

281,2

Calor de la purga

Qpsec

211,1

                  =       Fuente: Valdez (2021)

Resultados de propuestas<= span style=3D'mso-bookmark:_Hlk81985521'> analizadas

Para aprovechar la mayor cantidad de energía residual producida en la planta industrial en la optimización de su respectivo proceso se plantean dos propuestas.

Recuperadores de calor

Las purgas de eta= pas como el sistema de generación de vapor, esterilización, digestión y secado contienen una gran cantidad de energía residual que actualmente no es aprovechada en la planta, por tal razón se pretende recuperar esta energía = para reingresarla al proceso mediante varios recuperadores de calor, a continuac= ión, se presentan los resultados obtenidos de la simulación efectuada de los recuperadores en el software DWSIM:

Tabla 3

Resultados propuesta I.C. – ORC regenerativo

Recuperadores de Calor

Eficiencia (%)

Vapor reingresado (tn/h)<= /span>

I. C. 1

63,46

0,592

I.C. 2

94,12

0,244

I.C. 3

70,01

0,240

I.C.4

81,04

0,478

                        = Fuente: Valdez (2021)

Ciclo de Rankine Orgánico Regenerativo

El flujo continuo de los gases de escape = de la chimenea se aprovecha para llevar a cabo una simulación de un Ciclo de Rankine Orgánico Regenerativo en el cual el fluido de trabajo se mantiene c= omo un fluido supercrítico homogéneo a lo largo del ciclo en donde la presión de trabajo es mayor a la presión crítica (Martínez, 2020).

Antes de ingresar= a la turbina el fluido de trabajo es precalentado con la energía residual del flujo de salida de la turbina mediante un recuperador de calor, con la finalidad de reducir el calor de entrada del sistema e incrementar la eficiencia del ciclo, en donde se obtuvieron los siguientes resultados:

Tabla 4

Resultados Ciclo de Rankine Orgánico (ORC) Regenerativo

= Sistema de generación de vapor

Parámetro

Valor

Unidades

Nomenclatura

Eficiencia del ciclo

20,86

%

n ciclo

Calor de entrada

1074,21

KW

Q adicionado

Trabajo neto

224,17

KW

W neto

Trabajo turbina

227,68

KW

W turbina

Trabajo bomba

3,5125

KW

W bomba

Calor de salida

298,47

KW

Q salida

Fuente: Valdez (2021)

Recuperadores de calor - ORC regenerativo

Se combinarán las propuestas para evaluar si es posible obtener mejores rendimientos que   con las propuestas individuales. Debid= o a que se cuentan con cuatro recuperadores de calor que corresponden a los úni= cos puntos en donde existe generación de energía residual aprovechable, se debe analizar el punto más favorable para poder activar un ORC regenerativo que = para el efecto corresponde a los gases de escape provenientes de la chimenea del sistema de generación de vapor, por tanto, se reemplazará el recuperador de calor 2 por el ORC regenerativo. <= o:p>

Tabla 5

Resultados propuesta I.C. – ORC regenerativ<= span style=3D'mso-bookmark:_Hlk81985521'>o

Propuesta

Eficiencia (%)

Producto generado

I. C. 1

63,46

0,59 tn/h

ORC Regenerativo

20,86

227,68 KW/h

I.C. 3

70,01

0,24 tn/h

I.C.4

81,04

0,47 tn/h

                        Fuente: Valdez (2021)

Análisis económic= o

Recuperadores de Calor

El combustible utilizado en la planta industrial es la fibra la cual es un subproducto del proceso de extracción de aceite de palma africana y tiene un poder calórico= de 12150.8 KJ/Kg. Actualmente se requieren 2,18 tn/h de fibra para generar 7385 KW, energía necesaria para la producción de 5,86 tn/h de vapor. De acuerdo = con los datos proporcionados en la simulación se puede hacer una estimación de costos.

Tabla 6

Costo del combustible

Costo del Combustible

Producto

Cantidad

Valor

Fibra

1 tn

$ 6

                        = Fuente: Valdez (2021)

La caldera de la planta actualmente genera 5,86 tn/h de vapor para procesar 19,55 tn/h de racimos de fruta fresca de palma africana, para lo cual utiliza 2,188 tn/h = de fibra como combustible, el mismo representa un gasto para la empresa de $13,13/h. Cabe indicar que de las 5,86 tn/h de vapor producidas existe un 8= ,33 % de perdidas lo cual es equivalente a 0,50 tn/h.<= /p>

Tabla 7

Costos actuales de operación

Etapa

Vapor usado proveniente de la Caldera (tn/h)

Combustible Usado =

(tn/h)

Costo ($/h)=

Precalentamiento

0,29

0,108

0,65

Secado

0,24

0,089

0,54

Digestión

0,73

0,273

1,64

Esterilización

4,11

1,535

9,21

Pérdidas del proceso

0,49

0,183

1,09

PROCESO=

5,86

2,188

13,13

            = Fuente: Valdez (2021)

Tabla 8

Costos proceso optimizado

Etapa

Vapor usado proveniente de la Caldera (tn/h)

Combustible Usado =

(tn/h)

Costo ($/h)=

Precalentamiento

0

0

0

Secado

0

0

0

Digestión

0,49

0,18

1,09

Esterilización

3,63

1,35

8,13

Perdidas del proceso

0,49

0,18

1,09

PROCESO=

4,61

1,72

10,33

            Fuente: Valdez (2021)

En la tabla 8 pod= emos apreciar que la cantidad de vapor usado proveniente de la caldera en cada u= na de las etapas del proceso disminuye debido a la recuperación y reingreso de energía residual a cada una de las operaciones a través de los recuperadore= s de calor, de esta manera se logra generar un ahorro de energía térmica y por e= nde económico ya que solo se necesitarán 4,61 tn/h de vapor para procesar 19,55 tn/h de racimos de fruta fresca de palma africana, para lo cual el uso de combustible disminuirá a 1,721 tn/h lo que representará ahora para la empre= sa un gasto de $10,33/h.

La propuesta de recuperadores de calor al proceso de extracción estudiado permitirá consegu= ir un ahorro económico de $ 24528 anuales.

Tabla 9

Costos recuperadores de calor

Intercambiadores de Calor=

Numero

Tipo

Área (m2)

Intercambio de calor (KW)=

Costo ($)

I. C. 1

Tubo y carcasa

2,51

230,81

2621,22

I. C. 2

Tubo y carcasa

4,45

245,71

3782,65

I. C. 3

Tubo y carcasa

6,32

237,13

5425,14

I. C. 4

Tubo y carcasa

5,12

556,32

4879,87

Total

16708,88

            Fuente: Valdez (2021)

La inversión inic= ial para llevar a cabo esta propuesta es de 16708,88 $ misma que de acuerdo con= el ahorro generado se recuperará en un periodo aproximado de nueve meses.=

Ciclo de Rankine Orgánico Regenerativo<= /a>

De acuerdo con el balance de masa y energía realizado a todo el proceso se determinó que la energía residual contenida en los gases de escape de la chimenea tiene la capacidad para activar un ORC, en la simulación efectuada en el software DW= SIM se determinó que podrá generar 227,68 KW de energía eléctrica.

Tabla 10<= span style=3D'mso-bookmark:_Hlk81985521'>

Costo energía eléctrica

Energía Eléctrica<= /span>

Cantidad

Precio (sector industrial)

1 KW

$ 0,0902

El consumo de energía eléctrica en la planta actualmente es de 172546 KW mensuales los cuales representan alrededor de $15563,65 dólares.

La energía eléctrica producida por el ORC representará un ahorro económico de $177437,4 anuales debido a que el valor a cancelar por consumo eléctrico mensual se reducirá de $15563,65 a $777,2 el cual representa un ahorro económico del 95,01% del valor actual saldado mensualmente.

Tabla 11<= /span>

Costo componentes OR= C

Número

Dispositivos

Costos ($)<= /p>

1

Bomba

2190

1

Caldera

38900

1

Turbina

65600

1

Condensador=

8450

1

Intercambiador de Calor

2844

1

Accesorios<= /p>

2150

Total

120134

                        Fuente: Valdez (2021)

El costo de inver= sión del ORC es de $120134 el mismo se calcula que se podrá recuperar en un perí= odo de nueve meses aproximadamente.

Recuperadores de calor - ORC regenerativo

Tabla 12<= /span>

Propuesta combinada I.C. – ORC regenerativo<= /span>

Propuesta

Ahorro económico ($/ańo)

I. C. 1

5694

I. C. 3

4747,9

I. C. 4

9443,3

ORC Regenerativo

177437,4

Total

197322,6

Fuente: Valdez (2021)<= o:p>

El ahorro económico total que representaría emplear esta propuesta es de aproximadamente $197322,6/ańo.=

Validación de la Optimización

La validación de la optimización del se realizó mediante la comparac= ión de los resultados obtenidos con los de varias fuentes bibliográficas. Las eficiencias de los recuperadores de calor expuestas por Barreto (2015), coinciden con los del presente proyecto de investigación al igual que las manifestadas por Imbert (2011).

=

Tabla 13<= /span>

Validación de resultados recuperadores de calor=

Eficiencias Intercambiadores de calor=

Autor

Otras investigaciones

Investigación actual

Rango: 50 - 70 %

63,46%

Barreto (2015)<= !--[if supportFields]>

70,01%

81,04%

Otras investigaciones

Investigación actual

Autor

Rango: 60 - 80 %

63,46%

Imbert (2011)

70,01%

81,04%

Fuente: Valdez (2021)

Para validar el Ciclo de Rankine Orgánico se tomó = como referencia los modelos realizados por Andrade (2019) y Tzivanidis et al. (2016) en el software EES, en donde= la eficiencia del ORC desarrollado en el software DWSIM del presente trabajo de investigación se ajusta a la de los modelos elaborados por los autores cita= dos anteriormente.

Tabla 14<= /a>

Validación de resultados ORC<= /span>

Investigación actual

Software utilizado

Eficiencia

Autor

DWSIM

20,86%

Valdez (2021)

Otras investigaciones

Software utilizado

Eficiencia

Autor

Desviación

EES

19,63%

Andrade (2019)<= !--[if supportFields]>

6,27%

EES

22,36%

Tzivanidis et al. (2016)

6,71%

                        Fuente: Valdez (2021)

=

=

=

=

=

=
Selección de propuesta

Tabla 15

Matriz de selección de propuest<= /span>a análisis técnico

CRITERIO

PROPUESTA

Viabilidad Técnica=

Viabilidad Económica

Reducción De Contaminación Térmica

Reducción De Emisión De Gases De Invernadero

Total

Microturbinas

1

1

1

0

3

Recuperadores de calor

2

1

2

2

7

ORC

1

2

1

0

4

R.C - Microturbina

1

2

1

1

5

R.C. – ORC<= /p>

2

2

2

2

8

            Fuente: Valdez (2021)

Propuesta

Ahorro Económico ($)

Inversión Inicial ($)

Periodo De Recuperación Inversión (Meses)

Microturbinas

116899,2

18551,6

2 - 3

Recuperadores de calor

24528

16708,88

8 – 9

Ciclo de Rankine Orgánico

177437,4

120134

8 – 9

RC - Microturbina

89749,8

31477,83

4 - 5

RC - ORC Regenerativo

197322,6

133060,23

9 – 10

Los recuperadores= de calor resultan una opción muy favorable para incrementar la eficiencia térm= ica de un proceso industrial ya que permiten reutilizar la energía residual generada, de esta forma se obtiene un ahorro energético considerable y grac= ias a ello se puede evidenciar que existe ahorro económico, sin embargo, este no resulta tan significativo en comparación con otras propuestas. <= /span>

Tabla 16

Matriz de selecci= ón análisis económico

Fuente: Valdez (2021)

Por su parte el C= iclo de Rankine Orgánico Regenerativo (ORC) produce energía eléctrica a partir de fuentes cuyas temperaturas son bajas, en el cual el fluido de trabajo emple= ado se trata de un compuesto orgánico de elevado peso molecular mientras, el ah= orro económico generado es realmente significativo sin embargo éste por sí solo = no logra cumplir con la hipótesis planteada puesto que no se lograría reducir = la contaminación térmica provocada por los gases que actualmente son expulsado= s al medio a elevadas temperaturas contribuyendo al calentamiento del planeta.

La propuesta combinada entre un ORC Regenerativo y Recuperadores de calor permite obtene= r el mayor beneficio tanto económico como energético, por lo que fue seleccionad= a como la más factible, para esta propuesta combinada se eligió el ORC Regenerativ= o en lugar del convencional debido a que en la simulación efectuada se obtuvo un mayor porcentaje de eficiencia. La propuesta consiste en implementar estos = dos sistemas para optimizar el proceso mediante el aprovechamiento de la energía residual emitida en la misma.

La combinación de estas dos propuestas permitirá disminuir el consumo de combustible (fibra) = de 2,188 tn/h a 1,721 tn/h y el consumo de energía eléctrica de 172546 KW/mes a 8616,41 KW/mes. De acuerdo con el análisis económico efectuado anteriormente esto representará un ahorro económico de:

El capital por invertir para llevar a cabo la implementación de la propuesta seleccionada = es de $ 133060,23 valor que se podrá recuperar en un periodo de nueve meses de acuerdo con el ahorro económico calculado.

Figura 4

Propuesta seleccionada para optimización de proceso=

Nota: Esquema gráfico d= e la implementación de un ciclo orgánico de Rankine con regeneración para la obtención de energía eléctrica a partir de calor residual de proceso de obtención de aceite de palma.=

         Fuente: Valdez (2021)

Conclusiones

·      La cantidad de energía residual producida en cada una de las etapas del proceso es la siguiente, la purga de la caldera tiene un flujo 0,592 tn/h y un calor resi= dual de 424,3 KW, los gases de escape de la chimenea de la caldera un flujo de 1= 0,18 tn/h y un calor residual de 1543 KW, la operación de secado de aceite un fl= ujo de 0,244 tn/h y un calor residual de 211,1 KW, la digestión del fruto de pa= lma 0,448 tn/h y un calor residual de 35,82 KW y la esterilización de los racim= os de palma africana un flujo de 1,47 tn/h y un calor residual de 1723 KW; los mismos se determinaron mediante el balance de masa y energía efectuado al proceso de extracción de aceite de palma africana.=

·      La optimización d= el proceso a través de la implementación de la propuesta seleccionada permitirá tener un ahorro energético en la generación de vapor de aproximadamente 1,25 tn/h de vapor gracias a los recuperadores de calor, por su parte el Ciclo de Rankine Orgánico regenerativo generará 163929,6 KW/mes, finalmente la propu= esta combinada representará un ahorro económico total de $197305,1 anuales.=

·      Los resultados obtenidos de la optimización del proceso fueron validados con varias fuentes bibliográficas, las eficiencias obtenidas de los recuperadores de calor se ajustan a las expuestas por Barreto e Imbert. De igual manera la eficiencia del Ciclo de Rankine Orgánico Regenerativo desarrollad= o en el software DWSIM con un porcentaje bajo de desviación coincide con la manifestada por Andrade y Tzivanidis, ambas obtenidas en el software EES.

Referencias Bibliográficas

Andrade, = M. (2019). Modelación matemática de un Ciclo de Rankine Orgánico híbrido con energía solar para el aprovechamiento de energía residual del horno B&T de la empresa Ecuacerámica. [Tesis de maestría, Escuela Superior Politécnica = de Chimborazo] Repositorio institucional ESPOCH. http://dspace.espoch.edu.ec/handle/123456789/13025=

Aranguren Garacochea, P. (2015). Estudio y optimización de los sistemas de interca= mbio de calor en generación termoeléctrica aplicada al aprovechamiento del calor residual. [Tesis doctoral, Universidad Técnica de Navarra] Dialnet. = https://dialnet.unirioja.es/servlet/tesis?codigo=3D110871

Banda, P., & Gutiérrez, C. (2016). Simulación de un Sistema Recuperador de Calor p= ara Gases de Escape de Motogeneradores a Crudo. Revista Técnica “Energía,” 1= 2(1), 230–238. https://doi.org/10.37116/revistaenergia.v12.n1.2016.48<= /span>

Barreto, = W. (2015). Diseńo, construcción y pruebas de un intercambiador de serpentín= y coraza para un banco de trampas de vapor. [Tesis de pregrado, Universid= ad Nacional de San Agustín de Arequipa] Repositorio institucional UNAS. = http://repositorio.unsa.edu.pe/handle/UNSA/3239

Batty, J., Clair, & Folkman, S. (1990). Fundament= os de la Ingeniería de los Alimentos. México: Compańía Editorial Continental=

Borja, M. (2018). Aprovechamiento de la Biomasa para uso energético. Editorial Reverté

Cengel, Y. A., & Boles, M. A. (2015). Termodinámica. Editorial Mc Graw Hill Education.

Paz Feijóo, A. (2017). Diseńo de recuperador en planta de cogeneración. [Tesis de grado. Universidad de la Coruńa] Repositorio Institucional UDC. https://ruc.udc.es/dspace/bitstream/handle/2183/19734/PazFeijoo_Adrian_TFG_= 2017.pdf?sequence=3D2

Guo, J., & Jiang, F. (2019). The performance of finite-time refrigerators wi= th Rankine cycles. Physical A: Statistical Mechanics and Its Applications. Elsevier 536(C). https://doi.org/10.1016/j.physa.2019.122529

Habibi, H= ., Chitsaz, A., Javaherdeh, K., Zoghi, M., & Ayazpour, M. (2018). Thermo-e= conomic analysis and optimization of a solar-driven ammonia-water regenerative Rankine cycle and= LNG cold energy. Energy, 149, 147–160. https://doi.org/10.1016/j.energy.2018.01.157

Imbert, J. (2011). Evaluación de un intercambiador de calor. estudio de su empleo como= recuperador de calor. Tecnología Química, XXXI (3),37-44. https://www.redalyc.or= g/pdf/4455/445543774005.pdf

Martínez, D. A. (2020). Estudio y caracterización del ciclo orgánico Rankine en plantas termosolares con receptor de torre. [Tesis de Maestría, Univers= idad Pública de Navarra]. Repositorio institucional upna. https://academica-e.unavarra.es/handle/2454/38647<= /p>
Torres Pérez, C. I., & Quintero López, L. A. (2019). Análisis de residuos sóli= dos de palma africana, como alternativa de aprovechamiento de energías renovabl= es en el departamento del Cesar. Ingenierías USBMed, 10(1), 8–18. https://doi.org/10.21500/20275846.3662

Tzivanidi= s, C., Bellos, E., & Antonopoulos, K. A. (2016). Energetic and financial investigation of a stand-alone solar-thermal Organic Rankine Cycle power plant. Energy Conversion and Management, 126, 421–433. https://doi.org/10.1016/j.enconman.2016.08.033

Valdez, S. (2021). Optimización del proceso de extracción de aceite de palma africana de la planta San Daniel mediante el aprovechamiento de energ= ía residual para generar un ahorro energético. [Tesis = de maestría, Escuela Superior Politécnica de Chimborazo] Repositorio instituci= onal ESPOCH. http://dspace.espoch.edu.ec/handle/123456789/14704

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

&nbs= p;

El artículo queda en propiedad de la revista y, por tanto, su publicación parcial y/o total en otro medio tiene que ser autoriz= ado por el director de la Revista Conc= iencia Digital.

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ISSN: 2600-5859

Vol. 5 No 2, pp. 140 – 161 , abril-junio 2022

www= .concienciadigital.org

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                                     Gestión y Procesos                Página 1401

	Artículo de Investigación Científica y Tecnológica Enviado: 07/01/2022 Revisado: 22/02/2022 Aceptado: 03/03/2022 Publicado:25/04/2022 DOI: https://doi.org/10.33262/concie= nciadigital.v5i2.2144 <= o:p>
<= o:p> <= /p>	=
Cítese: <= /o:p>		&= nbsp; Valdez Rosales, S. D., Palmay Paredes, P. G., & Andrade Avalos, M. L. (2022). Optimización energética industrial con recuperadores de calor y un ciclo = de Rankine orgánico regenerativo. ConcienciaDigital, 5(2), 140-161. <= /span>https://doi.org/10.33262/concienciadigital.v5i2.= 2144 =
		CONCIENCIA DIGITAL, es una r= evista multidisciplinar, trimestral, que se publicará en soporte electrónico tiene como misión contribuir a la formación de profesionales competentes con visión humanística y crítica q= ue sean capaces de exponer sus resultados investigativos y científicos en la misma medida que se promueva mediante su intervención cambios positivos e= n la sociedad. https:/= /concienciadigital.org = La revi= sta 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 r= evista está protegida bajo una licencia Creative Commons Attribution Non Commerc= ial No Derivatives 4.0 International. Copia de la licencia: http://= creativecommons.org/licenses/by-nc-nd/4.0/
Palabras claves: optimiz= ación energética; balance de masa y energía; recuperadores de calor; ciclo de r= ankine orgánico regenerativo.		Resumen En el Ecuador, la Industria de extracción de aceite rojo de palma africana, = en las provincias de Santo Domingo de los Tsáchilas y Esmeraldas ha tenido un crecimiento en los últimos ańos con un promedio de producción de 19 a 25 = tn/h de fruto. El proceso de extracción de aceite rojo de palma africana se lo realiza principalmente p= or digestión de la fruta en un cilindro calentado con vapor, en donde la fru= ta digerida es prensada para extraer aceite bruto y el licor de prensa que se dirige al clarificador para clarificar el aceite y posteriormente secarlo, por lo tanto, la necesidad energética de la planta industrial es elevada.= El objetivo principal del presente trabajo de investigación es realizar la <= span style=3D'color:black;mso-themecolor:text1'>optimización energética de un proceso industrial de extracción de aceite de palma, mediante el uso de recuperadores de calor y un ciclo de Rankine orgánico regenerativo. Para = lo cual se realizó un balance de masa y energía a partir de los datos recopilados de la extractora San Daniel, Cantón la Concordia, Provincia Santo Domingo de = los Tsáchilas de varios meses de producción a condiciones estacionarias, para cuantificar la energía residual generada en el proceso. Se determinaron varios puntos potenciales de energía residual aprovechable, los cuales corresponden a la purga de la caldera que tiene un flujo de 0,592 tn/h y = un calor residual de 424,3 KW, los gases de escape de la chimenea de la cald= era un flujo de 10,18 tn/h y un calor residual de 1543 KW, la operación de se= cado un flujo de 0,244 tn/h y un calor residual de 211,1 KW, la digestión del fruto de palma 0,448 tn/h y un calor residual de 35,82 KW y la esteriliza= ción de los racimos de palma africana un flujo de 1,47 tn/h y un calor residua= l de 1723 KW. A partir de los datos encontrados se realizó la simulación de cu= atro recuperadores de calor y un ciclo de Rankine orgánico regenerativo en el software DWSIM. Co los resultados obtenidos se concluye que a través de e= stos dispositivos se podrá generar una reducción del consumo de vapor producido por la caldera de 5,86 a 4,61 tn/h y además se producirán 227,68 KW/h de energía eléctrica.
Keywords: energy optimi= zation; mass and energy balance; heat recovery units; regenerative organic rankin= e cycle.		Abstract= In Ecuador, the industry for the extraction of red African palm oil in the provinces of Santo Domingo de Los Tsáchilas and Esmeraldas has grown in recent years with an average production of 19 to 25 tn/h of fruit. The red African palm oil extraction process is conducted by digesting the fruit i= n a cylinder heated with steam, where the digested fruit is pressed to extract crude oil and the press liquor is directed to the clarifier to clarify the oil. oil and subsequently dry it, therefore, the energy need of the industrial plant is high. The main objective of this research work is to perform the energy optimization of an industrial palm oil extraction proc= ess, using heat recuperators and a regenerative organic Rankine cycle. For whi= ch a mass and energy balance was made from the data collected from the San Dan= iel extractor, the Concordia, Santo Domingo de Los Tsáchilas Province of seve= ral months of production at stationary conditions, to quantify the residual energy generated in the process. Several potential points of usable resid= ual energy were determined, which correspond to the purge of the boiler that = has a flow of 0.592 tn/h, and a residual heat of 424.3 KW, the exhaust gases = from the boiler chimney a flow of 10.18 tn/h and a residual heat of 1543 KW, t= he drying operation a flow of 0.244 tn/h and a residual heat of 211.1 KW, the digestion of the palm fruit 0.448 tn/h and a residual heat of 35.82 KW and the sterilization of the African palm bunches a flow of 1.47 tn/h and a residual heat of 1723 KW. From the data found, the simulation of four heat recuperators and a regenerative organic Rankine cycle was conducted in the DWSIM software. With the results obtained, it is concluded that through t= hese devices it will be possible to generate a reduction in the consumption of steam produced by the boiler from 5.86 to 4.61 tn/h, and in addition, 227= .68 KW/h of electrical energy will be produced.

Sistema de Generación de Vapor (Cald= era)
Corrientes	Nomenclatura	Flujo másico (tn/h)
Agua	W1	5,86
Vapor Proceso	V	5,86
Gases de Escape	G	10,18
Vapor Purga=	VP	0,592
Fibra	FP	2,188
Esterilizador<= /span>
Vapor Esterilizador	V2	4,11
Palma Africana Cruda	R	19,55
Palma Africana Cocida	R2	17,87
Purga Esterilizador	P1	1,47
Condensados=	C	4,32
Desfrutamiento
Frutos Sueltos	F	14,299
Raquiz	RQ	3,575
Digestor
Vapor Digestor	V3	0,733
Frutos Digeridos	D	14,584
Purga Digestor	PD	0,448

= Sistema de Generación de Vapor (Caldera)
Corrientes	Nomenclatura	Flujo (KW)
Calor del Agua	Qagua	5842
Calor del Combustible	Qcomb	7385
Calor Gases de Escape	Qperdido	1543
Calor de la purga caldera	Qpurgacal	424,3
Esterilizador
Calor del Esterilizador	Qester	4614
Calor de la purga	Qpester	1723
Digestor
Calor del Digestor	Qdig	569,9
Calor de la purga	Qpdig	35,82
Secador
Calor del Secador	Qsec	281,2
Calor de la purga	Qpsec	211,1

Recuperadores de Calor	Eficiencia (%)	Vapor reingresado (tn/h)<= /span>
I. C. 1	63,46	0,592
I.C. 2	94,12	0,244
I.C. 3	70,01	0,240
I.C.4	81,04	0,478

= Sistema de generación de vapor
Parámetro	Valor	Unidades	Nomenclatura
Eficiencia del ciclo	20,86	%	n ciclo
Calor de entrada	1074,21	KW	Q adicionado
Trabajo neto	224,17	KW	W neto
Trabajo turbina	227,68	KW	W turbina
Trabajo bomba	3,5125	KW	W bomba
Calor de salida	298,47	KW	Q salida

Propuesta	Eficiencia (%)	Producto generado
I. C. 1	63,46	0,59 tn/h
ORC Regenerativo	20,86	227,68 KW/h
I.C. 3	70,01	0,24 tn/h
I.C.4	81,04	0,47 tn/h

Etapa	Vapor usado proveniente de la Caldera (tn/h)	Combustible Usado = (tn/h)	Costo ($/h)=
Precalentamiento	0,29	0,108	0,65
Secado	0,24	0,089	0,54
Digestión	0,73	0,273	1,64
Esterilización	4,11	1,535	9,21
Pérdidas del proceso	0,49	0,183	1,09
PROCESO=	5,86	2,188	13,13

Intercambiadores de Calor=
Numero	Tipo	Área (m2)	Intercambio de calor (KW)=	Costo ($)
I. C. 1	Tubo y carcasa	2,51	230,81	2621,22
I. C. 2	Tubo y carcasa	4,45	245,71	3782,65
I. C. 3	Tubo y carcasa	6,32	237,13	5425,14
I. C. 4	Tubo y carcasa	5,12	556,32	4879,87
			Total	16708,88

Energía Eléctrica<= /span>
Cantidad	Precio (sector industrial)
1 KW	$ 0,0902

Número	Dispositivos	Costos ($)<= /p>
1	Bomba	2190
1	Caldera	38900
1	Turbina	65600
1	Condensador=	8450
1	Intercambiador de Calor	2844
1	Accesorios<= /p>	2150
	Total	120134

Propuesta	Ahorro económico ($/ańo)
I. C. 1	5694
I. C. 3	4747,9
I. C. 4	9443,3
ORC Regenerativo	177437,4
Total	197322,6

Eficiencias Intercambiadores de calor=	Autor
Otras investigaciones	Investigación actual
Rango: 50 - 70 %	63,46%	Barreto (2015)<= !--[if supportFields]>
70,01%
81,04%
Otras investigaciones	Investigación actual	Autor
Rango: 60 - 80 %	63,46%	Imbert (2011)
70,01%
81,04%

Investigación actual
Software utilizado	Eficiencia	Autor
DWSIM	20,86%	Valdez (2021)
Otras investigaciones
Software utilizado	Eficiencia	Autor	Desviación
EES	19,63%	Andrade (2019)<= !--[if supportFields]>	6,27%
EES	22,36%	Tzivanidis et al. (2016)	6,71%

Propuesta	Ahorro Económico ($)	Inversión Inicial ($)	Periodo De Recuperación Inversión (Meses)
Microturbinas	116899,2	18551,6	2 - 3
Recuperadores de calor	24528	16708,88	8 – 9
Ciclo de Rankine Orgánico	177437,4	120134	8 – 9
RC - Microturbina	89749,8	31477,83	4 - 5
RC - ORC Regenerativo	197322,6	133060,23	9 – 10

Figura 1

Propuesta recuperadores de calor

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Nota: = Esquema gráfico del proceso de recuperación de cal= or en el proceso de extracción de aceite de palama africana<= /span>

Fuente: Valdez (2021)

Fuente: Valdez (2021)

Recuperadores de calor - ORC regenerativo

Recuperadores de Calor

Ciclo de Rankine Orgánico Regenerativo<= /a>

Recuperadores de calor - ORC regenerativo

Validación de la Optimización