Heat and Mass Transfer in Food Engineering

ISSN(Online) : 2319-8753

ISSN (Print) : 2347-6710

International Journal of Innovative Research in Science,

Engineering and Technology

(An ISO 3297: 2007 Certified Organization)

Website: www.ijirset.com

Vol. 6, Issue 7, July 2017

Heat and Mass Transfer in Food Engineering

Kirti Bhushan Zare

, Dr.Utkarsh Maheshwari

, D.P.Deshpande

, Pankaj Vardhe

Dept. of Chemical Engineering, Dr.D.Y.Patil Institute of Engineering Management and Research, Akurdi,

Pune, India

,2,3,4

ABSTRACT: Heat transfer in food processing is simultaneous heat and mass transfer in drying and frying, free

convection heat transfer in thermal sterilization of cans, and phase change in freezing and thawing. Air drying, freeze

drying, spray drying, and steam drying are accompanied by moisture transfer, which also undergoes phase change

(evaporation). Heat transfer, together with moisture and vapor transfer, controls these processes. There is a need for

deeper qualitative and quantitative understanding of the heat and mass transfer mechanisms underlying various

techniques for food production, processing, preservation and storage. Several classes of food-processing problems are

presented where advances can be made on the basis of improved understanding of heat and mass transfer mechanisms.

This is important for the development of new food sources, for more economical and energy-efficient processing of

food from existing sources, for better food quality and quality control, and for adherence to new regulations.Microwave

(MW) drying is a rapid dehydration technique that can be applied to specific foods increasing concerns over product

quality and production costs have motivated the researchers to investigate and the industry to adopt microwave drying

technology.

KEYWORDS: Heat transfer, mass transfer, food processes, microwave drying.

I.INTRODUCTION

1.1 Heat Transfer Principles:Air during retort come-up and for draining (D), outlet ports for venting the retort at the

end of thecycle (C), and a safety and pressure relief valve (F). A pocket for instruments, a thermometer, temperature-

recording probe, and a pressure gauge is located on the side of the vessel. The operating cycle of this type of a retort

involves bringing the retort up to a temperature of around 121◦C. Steam is then allowed to pass through the vessel so

that all air in the retort and between the cans is removed (venting) before the retort is finally brought up to the operating

pressure and processing temperature . At the end of the processing time, the steam is turned off, and a mixture of

cooling water and air is introduced into the retort to cool the cans. The purpose of the air is to maintain the pressure in

the retort, following the condensation of the residual steam after the initial introduction of cooling water. The

containers may deform because of the pressure difference between inside and outside of the container if this pressure is

not maintained.

The recent focus on thermal sterilization of foods is to improve the rates of heating, in order to increase production

rates and minimize damage to product quality.In most applications these two types of heat transfer occur

simultaneously, but one type may be more important than the other. Steady-state heat transfer takes place when there is

no change in temperature with time.

1.2. Unsteady-State Heat Conduction: In food processing, there are many situations where temperature is a function

of time. The calculations of unsteady-state heat transfer are usually complicated and involve solving the Fourier

equation, written in terms of the partial differential equation in three dimensions. In unsteady-state heat transfer, the

temperature within a food during processing depends on the time and position. The temperature changes are influenced

1. the initial temperatures of the heated body

2. the temperature of the heating medium

3. the surface heat transfer coefficient (heat transfer coefficient at all interfaces as well as whereconvection is involved)

4. the thermal conductivity, specific heat, and density of the food and their variation withtemperature and composition

ISSN(Online) : 2319-8753

ISSN (Print) : 2347-6710

International Journal of Innovative Research in Science,

Engineering and Technology

(An ISO 3297: 2007 Certified Organization)

Website: www.ijirset.com

Vol. 6, Issue 7, July 2017

The basic equation for unsteady-state heat conduction in one-space dimension (x) is

--------------------------------------------------------------------------------------------------(1)

where ∂T/∂t is the change of temperature with time, ρ is the density (kg m−3), Cp is the specific heat capacity (J

kg−1K−1), and k is the thermal conductivity (W m−1K−1).

When a solid piece of food is heated or cooled by a fluid, the resistance to heat transfer is mainly controlled by the

surface heat transfer coefficient (h) and the thermal conductivity of the food (k)

[1]

These two factors are related by the Biot number (Bi):

-----------------------------------------------------------------------------------------------------------(2)

where δ is the characteristic dimension or heat transfer path length in the solid (m). At small Bi values (>0.2), the

surface film is the main resistance to heat flow; in this case, the assumption of anegligible internal (conductive) heat

transfer resistance in the solid food is valid .However, in most applications the thermal conductivity of the food limits

the rate of heat transfer (Bi >1).

[2]

1.3. Free Convection

When a fluid’s temperature changes, the resulting changes in density establish natural convection currents, which occur

as a result of bulk movement of the fluid, such as the movement of liquid inside a can during sterilization. Obviously,

heat transfer by conduction occurs simultaneously but is generally negligible compared to convection heat transfer

(Karl et al., 1975). The rate of convection heat transfer is governed by Newton’s law of cooling. This law states that the

rate of heat transfer by convection is directly proportional to the heat transfer area and the temperature difference

between the fluid and heating/cooling surface:

-----------------------------------------------------------------------------------------------(3)

where Q is the rate of heat transfer (W), a is the surface area (m2), Ts is the surface

temperature, Tbu is the bulk fluid temperature, and hs is the surface or film heat transfer coefficient (W m−2 K−1).

-------------------------------------------------------------(4)

where his the heat transfer coefficient at the solid liquid interface(Wm−2 K−1); dv is the characteristic dimension (m),

which may be the height or diameter of the can, as will be discussed later; k is the thermal conductivity of the fluid (W

m−1K−1); ρ is the density (kg m−3); Cp is the specific heatcapacity (J kg−1K−1); μ is the viscosity (N s m−2); g is the

acceleration due to gravity (m s−2); β is the thermal expansion coefficient (K−1); and _T is the temperature difference

(◦C).

[4]

II.RELATED WORK

2.1Thermal properties of food:Knowledge of the thermal properties of food is required in order to evaluate the heat

transfer in food products. Therefore, a composition-based prediction method was used to obtain the thermal properties

of food. The thermal properties are described by major components found in food such as: proteins, fat, carbohydrate,

fibers, ash and water/ice. The composition data is stated as mass fraction and given in [1] and [2] for different food

products such as vegetables, fruits, meat, etc. The thermo physical properties of each component are subsequently

ISSN(Online) : 2319-8753

ISSN (Print) : 2347-6710

International Journal of Innovative Research in Science,

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Vol. 6, Issue 7, July 2017

described by temperature dependent mathematical models in the temperature range of -40oC to 150oC. The properties

were evaluated in the global expression window in Comsol. Knowing the composition as well as the thermal properties

of the different components makes it possible to find the apparent properties of the food product. A different approach

is used for the evaluation of the properties in the unfrozen and frozen region of the food. In order to evaluate which

approach is to be used, determination of the initial freezing point is required. Pham Q.T. [3] has suggested the

following equation for evaluation of the initial freezing point based on the composition data of the product:

[5]

------------------------------------------(5)

Whether the temperature of the product is above or below the initial freezing point the thermal properties of the food

are calculated according to one of the following approaches:

Unfrozen food (T > Tf) The density of the food product is calculated according to the following equation:

-------------------------------------------------------------------------------------------------------(6)

The specific heat capacity in the unfrozen part of the food is obtained from the mass average of the heat capacities of

the components in the food product

------------------------------------------------------------------------------------(7)

The thermal conductivity is described by means of a Maxwell type model. The dispersed phase is air (if present) and

the continuous phase in the equation is obtained from the mass average of the conductivities of the remaining

components in the food product

[7]

--------------------------------------------------------(8)

Frozen food (T ≤ Tf) The ice fraction during freezing is determined by the

following equation given by [1]:

---------------------------------------------------------------------------------(9)

Knowing the fraction of ice, the thermal properties of the food during freezing can be obtained. The density of the food

product is calculated according to equation 2, however, now including the mass fraction of ice.

The latent heat of fusion is accommodated in the description of the

apparent specific heat of food during freezing.

----------------------------------------------------------------------(10)

Thermal conductivity is determined in two steps and is based on equation 4. First, ice is used as a dispersed phase (if

ISSN(Online) : 2319-8753

ISSN (Print) : 2347-6710

International Journal of Innovative Research in Science,

Engineering and Technology

(An ISO 3297: 2007 Certified Organization)

Website: www.ijirset.com

Vol. 6, Issue 7, July 2017

present). Secondly, air is used as dispersed phase (if present) and continuous phase is the previously obtained

conductivity.

2.2 Heat transfer and reactions in foods:Foods are physically complex fluids and soft solids, with rheological and

material propertiesthat are time- and process-dependent and which have a natural variation. It is thus difficult tospecify

the physics in such a way as to allow accurate prediction of the process. Some safety marginis added to ensure that

every part of the material is safe.

2.3 Milk protein:Unlike tomato paste, milk deposit cannot be removed by water alone. The force required to disrupt

and remove the milk protein deposit has been measured without chemical being used and with cleaning chemical

containing 0.5 wt% NaOH, used.

2.4Cohesive and adhesive structures

It is possible, by setting the micromanipulation probe to pass above the disc, to leave deposit onthe surface. In this case

the force measured by the probe will corresponds to that required to breakthe cohesive forces between parts of the

deposit. This has been done for both types of deposit. For tomato, the force required for partial removal of the deposit

exceeds that for the total removal,

III.EXPERIMENTAL WORK

In all experiments, the microwave oven was brought to the operating temperature by heating 1000 ml of distilled water

in a glass beaker for 5 min before the first run of the day .The potato samples was placed on Petri dishes in the center of

the microwave oven cavity. Throughout the experimental run the sample weights were continuously recorded at

predetermined time intervals until no discernible difference between subsequent readings was observed. The moisture

content value was determined as

[12]

Where M is moisture content, Wt is the weight of sample (g) at any time and Wdis

the weight of the dried sample.

Figure No: 3 Microwave drying systems

ISSN(Online) : 2319-8753

ISSN (Print) : 2347-6710

International Journal of Innovative Research in Science,

Engineering and Technology

(An ISO 3297: 2007 Certified Organization)

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Vol. 6, Issue 7, July 2017

IV.RESULT AND DISCUSSION

Throughout the experimental run the sample weights were continuously recorded at regular time intervals until no

discernible difference between subsequent readings was observed.

Graph No: 4.1 Drying Curve

V. CONCLUSION

Based on the results of this study, the conclusions were drawn. Drying took place mainly in the falling rate period

followed by a constant rate period after a short heating period. The drying rate increases with increasing the microwave

power or sample diameter. An increase in slab diameter results an increase in the drying coefficient It is because of

sudden and volumetric heating, generating high pressure inside the potato samples, resulted in boiling and bubbling of

the samples.

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