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Article

The Physical Optimum as an Ideal Reference Value for Balancing Thermodynamic Processes Integrating the Exergetic Evaluation by the Example of Heat Supply

Department of Energy and Biotechnology, Flensburg University of Applied Sciences (FUAS), 24943 Flensburg, Germany
*
Author to whom correspondence should be addressed.
Academic Editor: Xiaolin Wang
Energies 2021, 14(15), 4426; https://doi.org/10.3390/en14154426
Received: 16 June 2021 / Revised: 16 July 2021 / Accepted: 19 July 2021 / Published: 22 July 2021
(This article belongs to the Topic Exergy Analysis and its Applications)

Abstract

This paper contains the basic definition and application of the physical optimum as a method for process evaluation and optimization. By means of the exemplary balance of a wood pellet-fired boiler, the conventional efficiency is compared to the PhO. Furthermore, this study demonstrates the possibility of applying the thermodynamic state variable exergy as a physical reference property of a system within the PhO method. To explain the approach, the heat generation in the wood pellet-fired boiler is compared to the supply from a heat pump, which itself is connected to a power plant. Furthermore, the process-independent PhO is explained in order to illustrate the limitations of feasible optimization. Additionally, possible research topics such as the integration of dynamic behavior in the method are approached. As a conclusion, the differences between the methods outline the advantage of the PhO in the optimization process.
Keywords: physical optimum; PhO; reference process; exergy; energy efficiency; energy optimization; method comparison physical optimum; PhO; reference process; exergy; energy efficiency; energy optimization; method comparison

1. Introduction

Technical analysis often uses comparison models in order to describe a process in a simplified manner, and, additionally, to compare the model to a real process with a certain degree of energy loss. The literature provides different terms for the reference process. The following list illustrating the existing variety shows a range of possibilities for process evaluation [1]:
  • BDP: best demonstrated practice;
  • OEO: operational energy optimum;
  • PEO: plant energy optimum;
  • TEO: theoretical energy optimum;
  • Best practice observed;
  • BAT: best available technology;
The method of the physical optimum (PhO) was primarily described in the dissertation of Volta [1]. Keichel provided an additional consideration in his dissertation [2] in 2017 as well as the resulting VDI 4663 [3], which is mainly based on these studies. Wenzel [4] provided a systematic comparison of the PhO to the exergy method. Kerpen [5] provided a differentiation between the PhO and exergetic evaluation.
This study explains the physical optimum and the PhO factor FPhO as the corresponding indicators and integrates the already common methods of efficiency and exergy analysis, using the methods in combination. The particularity of the application of the PhO is the reference to an ultimate value. This allows the analysis of losses, aiming to distinguish whether they are avoidable or not because an optimization can only reduce avoidable losses. Other studies such as [4,5] outlined the differences between the PhO and other evaluation methods, while this study aims to integrate, in particular, the state value exergy into the PhO.

2. Materials and Methods

Below, the approaches to energy optimization relevant to this study are explained, namely, efficiency, exergy analysis and the PhO. The distinct characteristics of the methods are outlined.

2.1. Efficiency

The efficiency is defined as the output-to-input ratio of a certain process:
η = output input
The efficiency does not specify the conditions under which a process operates. Without further information, it is not possible to draw conclusions on whether the process operates under ideal conditions or not. An efficiency below one only indicates that a part of the expense is not gained as a benefit from the process. Therefore, the degree to which any losses result, in general, becomes evident.
Thus, the efficiency is a fundamental application of the first law of thermodynamics, namely, energy conservation.

2.2. Exergy Analysis

For the state variable exergy E, the determination of a ratio in analogy to the efficiency is typical. The exergetic efficiency is defined as the exergetic benefit in relation to the exergetic expense of a specific process.
ζ = E o u t p u t E i n p u t = 1 E l o s s E i n p u t
with E i n p u t = E o u t p u t + E l o s s .
This study distinguishes between avoidable and unavoidable losses.
E l o s s = E l o s s , a v o i d a b l e + E l o s s , u n a v o i d a b l e
If an unavoidable energy flow exits the balance with a temperature differing from the ambient state, an unavoidable exergy flow is transferred to the surroundings in the form of exergy loss. A practical example is a heating process, in which the temperature of a product to be heated is increased over the ambient temperature using a material-bound energy carrier. The following approach considers the exergy of fuels and the exergy of heat for an analytic balance.
Kerpen [5] considered a combustion process as well. The focus in Kerpen’s [5] work, however, lies on the explicit difference between the exergy and energy contents of the fuel. The aim of this study is to explain the principle of integrating exergy into the PhO method. Furthermore, the focus of this study lies on the generation of useful heat including the integration of further applications for energy conversion, not exclusively on the combustion process. Therefore, the example is kept deliberately simple. Thus, in this study, the exergy content of a fuel is described as the fuel performance in a good approximation.
E B Q B
The exergy of heat depends on the amount of heat as well as the ambient temperature in relation to the temperature at which the heat passes the system border [6] (p. 156).
E q = ( 1 T a m b T ) × Q = η C × Q
If the heat is not exchanged at a constant temperature level, meaning the heat transfer is sensible, the average thermodynamic temperature Tm of the heat transfer is used to calculate the amount of exergy transferred with the heat. For ideal gases, as well as incompressible fluids with an approximately constant specific isobaric heat capacity, the average thermodynamic temperature can be calculated as follows [6] (pp. 119–120).
T m 1 , 2 = Q 12 S q 12 = m × c p × ( T 2 T 1 ) m × c p × l n ( T 2 T 1 ) = T 2 T 1 l n ( T 2 T 1 )

2.3. Physical Optimum

Below, the PhO is described based on [1,3]. The value of the PhO is ultimate for a specific process. To determine the PhO, an ideal thermodynamic reference process must be established for which the application of the laws of thermodynamics is essential. The process can be reversible as well as irreversible. The PhO is applicable to energy types as well as material and information. Figure 1 shows the PhO in comparison to common reference processes.
As an ideal threshold value, the PhO separates the perpetuum mobile from the processes feasible in reality. The laws of thermodynamics refute the feasibility of a perpetuum mobile. Thus, the perpetuum mobile is also a theoretical concept to define an ideal process, though it is—even as a threshold—not feasible. As an example for the necessity of changing reference points, the efficiency classes of electric motors can be taken into account. Following technical progress, the electric motors according to efficiency class Eff1 were redefined as IE2 to enable the evaluation of further improved motors with IE3 and IE4 [7].
The PhO factor puts the real amount of energetic expense B in relation to the corresponding physical minimum expense BPhO, resulting in a value higher than one at all times (according to the initial approach in [1] to focus on the demand of processes, the symbol “B” is used, as in [3]).
It is therefore necessary to measure the expense B, in order to establish it with a simulation, in case the examined process is not running yet. On the other hand, the physical minimum expense BPhO is defined and calculated based on an ideal reference process.
F P h O B = B B P h O 1
The difference between the PhO factor and the physically optimal case ( F P h O B  = 1) returns the avoidable losses ∆ΩB:
Δ Ω B = F P h O B 1
In contrast to the efficiency, the PhO outlines the avoidable losses, which represents the only possible starting point of process optimization. The efficiency provides the overall loss of a process consisting of avoidable and unavoidable losses. Just for the exceptional case in which the ideal efficiency can reach 1 (ηideal 1), the efficiency outlines only the avoidable loss ∆ΩB because the unavoidable loss equals zero. In any other case (for ηideal < 1), the efficiency does not enable conclusions regarding the degree to which the process can be optimized because unavoidable losses are included in the overall loss. Below, a practical example of a wood pellet-fired boiler illustrates this problem.

3. Results

As an exemplary process, a wood pellet fired-boiler is considered, which provides warm water for space heating with a heat exchanger in the exhaust system. The following calculations are described in a typical way and can be found, e.g., in [6,8].

3.1. Application of PhO to Boiler Process

Figure 2 illustrates the boiler system. Fuel mB and combustion air ml are fed to the system. In this model, a complete combustion is assumed.
Resulting from mB, the combustion heat QB is fed to the system. Apart from the useful heat QN, the following losses leave the system:
  • Qfg  exhaust loss;
  • Qash ash loss;
  • QCO losses by incompletely burned material;
  • QS   surface loss.
Q B = Q N + Q f g + Q a s h + Q C O + Q s
A simplified approach to determine the system efficiency is—neglecting the surface loss Qs—the combustion efficiency ηf
η f = 1 q f g q C O q a s h
with
q f g = Q f g Q B ;   q C O = Q C O Q B ;   etc .
The ash losses as well as the losses by unburned material can typically be neglected in an energetic balance (qCO ⟶ 0, qash ⟶ 0). The combustion efficiency is simplified to
η f = 1 q f g
Under the condition of a complete combustion, the exhaust loss is a function of the air ratio λ, the oxygen concentration in the flue gas and the exhaust temperature:
q f g = f ( O 2 f g ,   ϑ f g )
Furthermore, for complete combustion, the air ratio for fuels with high gross calorific values can be determined in a good approximation according to [8]
λ = C O 2 m a x f g C O 2 f g = O 2 m a x f g O 2 m a x f g O 2 f g = 0.2093 0.2093 O 2 f g
The specific exhaust loss qgf is defined as
q f g , c o n d , H i = [ ( v i · C m p , i ) ] × ( ϑ f g ϑ a m b ) w c o n d × r H i
with
i = 1 n ( v i × c ) = v C O 2 × c m p , C O 2 + v N 2 × c m p , N 2 + v H 2 O × c m p , H 2 O + v O 2 × c m p , O 2
It is also possible to refer to the gross calorific value for the combustion efficiency.
η f , c o n d , H s = η f , c o n d , H i × H i H s
The specific molar heat capacity of the components in the flue gas cmp,i is approximated for 100 °C and the condensation enthalpy of water for 25 °C of rH2O, 25 °C = 2411 kJ/kg.
Moreover, the specific flow of condensed water is defined as the flow of the condensate in relation to the supplied flow of the fuel.
w c o n d = m ˙ c o n d m ˙ B

3.1.1. Example

The efficiency of the heat generator depends on λ and the exhaust temperature. To determine λ, a measurement of the following parameters in the flue gas is required (this example is used parallely in a similar form in [3]): O2,fg = 7%; ϑfg = 130 °C. The real λ results in being
λ = O 2 m a x f g O 2 m a x f g O 2 f g = 0.2093 0.2093 0.07 = 1.5
However, in the case of physically optimal conditions, λPhO would be 1 (complete combustion):
λ P h O = O 2 m a x f g O 2 m a x f g O 2 f g = 0.2093 0.2093 0 = 1
In addition, the exhaust temperature would equal the lowest temperature in the system (in this case, the return flow temperature at 60 °C), resulting in a higher efficiency.
The following applies: ϑ1 = ϑfg = 60 °C, terminal temperature difference TTD = 0. Figure 3 shows the temperature of the two fluids over the surface of the heat exchanger in the real case and the PhO.
A combustion efficiency of 100% would be impossible to achieve even if the flue gas were cooled back to ambient temperature (in this case, 20 °C). The combustion efficiency for a specific temperature with regard to λ is shown in Figure 4. (The relative humidity φ of the flue gas is about 100%, unlike the relative humidity of the combustion air (60%). This is why the combustion efficiency does not reach 100% in the diagram, even at 20 °C.)
In the PhO, the combustion efficiency amounts to 90.75%. This corresponds to an exhaust loss which cannot fall below qa,Hs,PhO = 9.25% for this case. Thus, in the PhO, if 100 units of fuel are fed to the system, QN,PhO = 90.75 units of useful heat can be provided. For the real case, the standard operating point (SOP) is shown in Figure 4. The exhaust loss sums up to qa,Hs = 13.64%, which means that it is qa,Hs,ΔΩ = 4.39% higher than the ideal case. This equals the potential for optimization. Figure 5 and Figure 6 illustrate the losses. If the input is assumed to be constant, a higher amount of useful heat can be gained for the PhO. Furthermore, the distinction between unavoidable and avoidable losses is shown.
A more detailed analysis considering further losses would be possible, as indicated in Figure 6.
For the gross calorific value, the following applies:
F P h O , H s B = B B P h O = η f , H s , P h O η f , H s , S O P = 1.0508
The avoidable losses equal the potential for optimization. For a specific demand, 105.08% of the optimal demand is used. In accordance with this, the energy input of the boiler could be reduced by
Δ Ω B = F P h O , H s B 1 = 1.0508 1 = 5.08 % points
Thus, the avoidable losses do not equal the overall losses:
1 − ηf,Hs,SOP = 1 − 0.8636 → Potential for optimization ≠ 13.64%
It is also possible to determine the PhO factor for the lower calorific value. For the sampled wood pellets, the ratio of gross and lower calorific values was determined as Hs/Hi = 1.084. The combustion efficiency amounts to
F P h O , H i B = η f , H i , P h O η f , H i , S O P = η f , H s , P h O × H s H i η f , H s , S O P × H s H i = η f , H s , P h O η f , H s , S O P = 1.0508 Δ Ω B , H i = F P h O , H i B 1 = 5.08 % points
Again, the overall losses are higher than the avoidable losses: 1 η f , H i , S O P = 1 η f , H i , S O P × H s H i = 1 0.8636 × 1.084 = 1 0.9359   → Potential for optimization ≠ 6.41%
However, for both approaches, the potential for optimization amounts to 5.08%-points. Using the PhO factor, a distinction between the gross and lower calorific values for the evaluation of a combustion process becomes unnecessary. The evaluation of the efficiency with the PhO factor is valid in general.

3.1.2. PhO Factor Based on Exergy Analysis

The ambient temperature is estimated to be Tamb = 293 K. In this study, the outlet temperature of hot water was set to ϑ2 = 80 °C, and the return flow temperature was set to ϑ1 = 60 °C. Thus, the resulting thermodynamic middle temperature is
T m = 353   K 333   K l n ( 353   K 333   K ) = 343   K = 69.9   ° C
Real Process:
Explicitly, the exergy of the useful heat in the given example amounts to
E ˙ x , N = ( 1 T a m b T m ) × Q ˙ N = ( 1 293   K 343   K ) × 86.36   units = 12.57   units
Physical Optimum:
The amount of exergy of the flow of useful heat is
E ˙ x , N , P h O = ( 1 T a m b T ) × Q ˙ N , P h O = ( 1 293   K 343   K ) × 90.75   units = 13.21   units
In the real process, the exergetic efficiency is 12.57%. In the case of the PhO, a higher flow of useful heat can be gained at the same temperature level, resulting in a higher exergetic efficiency of 13.21%. Assuming the process conditions are in accordance with the energetic analysis, the same PhO factor, namely, the same potential for optimization results for the exergetic analysis, is shown in Figure 7.
The PhO-Factor based on exergy analysis results in
F P h O , H s , E x B = B E x B E x , P h O = ζ P h O ζ = 0.1321 0.1257 = 1.0508
The avoidable losses sum up to
Δ Ω B , E x = F P h O , H s , E x B 1 = 1.0508 1 = 5.08 % points
If the temperature levels are not changed during the optimization (as in this example), the amount of avoidable losses does not depend on the method used to determine this value. The exergetic and energetic balances return the same result. Thus, the determination of the avoidable losses is valid in general: Δ Ω B , H i = Δ Ω B , H s = Δ Ω B , E x = Δ Ω B .

3.2. Comparison of Boiler and Heat Pump with PhO

Comparing the resulting two PhO factors of the two different processes, the option that is closer to its own ideal consumption is outlined. In this case, the PhO factor indicates the potential for the optimization of each individual process. It is also possible to use the PhO to compare different processes with the same benefit, as long as a common ideal comparison process (according to the PhO) can be specified for both processes.
In this study, a heat pump process is compared to the wood pellet-fired boiler. The heat pump (HP) is connected to a power plant (PP). Both overall processes are supplied with fuel. Both deliver the same amount of useful energy at the same temperature level.

3.2.1. PhO Factor and Efficiency

On the left, Figure 8 shows the boiler process again. Meanwhile, on the right, a simple model of an HP is illustrated. The PhO for this process can be determined according to Carnot.
  • For BPhO: Assuming a TTD of 0 K, the ideal HP operates between 20 and 80 °C, with a COP of 5.88.
  • For Δ Ω 1 : For the real HP, the liquefaction temperature is set to 85 °C, and the evaporation temperature is set to 15 °C (TTD = 5 K). With a Carnot grade of approximately 0.6, the COP of the real HP would be 3.07.
  • For Δ Ω 2 : Furthermore, the efficiency of the power plant (PP) delivering the electric energy is assumed to be 40%.
In Figure 8, the PhOind is shown in the middle representing the absolute minimum exergy input for the boiler as well as the HP. The anergy of the useful heat is added in white. In the case of the HP, this anergy is taken from the environment. For the boiler, it is exergy turned into anergy in the process. On the left and right in gray, the consumption in the real case is given for each option. In between, the losses are given as a cascade adding to the PhOind until the real expense is reached. Thus, the impact of a specific loss on the total losses can be quantified with this form of presentation.
For this process, the PhO factor sums up to 4.793. As a significant amount of losses are caused by the conversion of fuel to electric energy, the supply with renewable sources should be considered instead. With the losses of the PP practically reduced to zero, the further advantages of the HP for this application are evident. The PhOind is explained below.
The overall energy efficiency of the heating considered in this study shall be defined as the ratio of useful heat to input exergy.
η t o t = Q N E i n ;   η t o t , b o i l e r = η f ;   η t o t , H P = C O P H P × η P P
If the PhO factors alone are taken into account, the boiler shows little potential for further optimization. However, while the PhO factor of 1.102 indicates that only 10.2% of the losses are avoidable, the overall energy efficiency shows that just 89.8% of the initial energy input can be gained as useful heat from the process. Therefore, the overall fuel demand for the HP is lower, which can be determined by the overall efficiency of 1.421, meaning that the amount of useful heat generated is higher than the fuel input, due to the additional input of pure anergy from the environment. Figure 9 further enhances this.

3.2.2. Process-Independent PhO

The PhO can also be used to compare different processes when referring to an ultimate, process-independent PhO (PhOind), which is also shown in Figure 8. The minimum amount of exergy needed to increase the temperature from 60 to 80 °C can be determined by the exergy in the transferred heat of 12.57 units. This equals the amount of exergy transferred to the flow of heating water in both options. In relation to the PhOind, it is possible to determine a process-independent PhO factor FPhO,ind. In this case, the HP is the more efficient option while simultaneously consuming less energy, as shown by the factors.
F P h O ,   i n d , E x , b o i l e r = B b o i l e r , E x B P h O , i n d , E x   = 100 12.57 = 7.96 F P h O ,   i n d , E x , H P = B H P , E x B P h O , i n d , E x   = 70.36 12.57 = 5.60
However, the PhO for a specific process exclusively provides valid information on the degree of possible optimization. Figure 10 compares the temperature levels (of the two fluids) of the real heat transfer (I.), the PhO (II.) and the process PhOind (III.).
The process-independent ideal heat transfer is reversible, meaning the temperature difference between the two fluids in the heat exchanger is zero at all times. Even in theory, this is only possible if the thermal capacity flow W ˙ = m ˙ × c p of the heat supply (fluid 1) equals that of the heat demand (fluid 2), as shown in Figure 10. The temperature ϑcond,PhOind therefore has to change during condensation to reach ϑ2. As this is not feasible for a phase-changing single-component fluid at constant pressure in reality, the difference between the PhO of this process and the PhOind is an unavoidable loss. A heat pump operating between ambient temperature and the thermodynamic middle temperature ϑm returns the result for the exergetic expense. Yet, ϑm is below the required temperature ϑ2. A condensation at ϑm = const. cannot supply the system. It becomes clear that in this case, the PhOind is over-idealized, outlining the reversible heat transfer, which is not feasible in reality.
To sum up, the PhOind is suitable for a process comparison and, as with the efficiency, determines the process with a lower total energy consumption. The PhO factor, in addition, outlines the efficiency of each specified process as well as the potential for optimization.

4. Discussion

Many indicators for the evaluation of processes exist. To evaluate the efficiency of a process, the PhO is one of those indicators. The following section discusses the advantages and particularities of the PhO in order to put the method into the context of research on optimization.

4.1. Degree of Idealization

To determine the PhO, a certain process is idealized. Some improvements can only be reached with infinite expense through optimization, such as the TTD of 0 K. The surface of the heat exchanger would have to be infinite. In some cases, it can be reasonable to use a realistic TTD instead. If specific parameters are definite, the PhO can be determined taking them into account. An example would be a safety margin or a minimum temperature requested (keyword legionella). The system boundaries as well as the idealization of the process must be executed considering the purpose of determining the feasible minimum input. When over-idealized, as in Figure 10, the outcome of the analysis is not valid anymore. While the perfect heat exchanger would run as a reversible process, the user of the PhO method should consider finding a more realistic model.
It would have been possible to compare the real HP to a model according to Carnot, which takes into account the TTD of 5 K for each heat exchanger. Then, of course, the minimum temperature for the flue gas of the boiler should also be determined with a realistic TTD. Yet, the TTD should not be changed once specified. The PhO must be an ultimate value. Therefore, the determination of the boundary conditions is decisive. Overall, the definition of the PhO depends on the purpose of the analysis. The heat exchanger can thus be defined in different ways, as shown in the example in Figure 10. A reason for the chosen description should be given at all times. The distinction between avoidable and unavoidable losses shows the effect of the PhO being defined closer to the actual process conditions: losses which are avoidable for the idealized version are unavoidable for the more realistic one. Losses occur in both cases. Thus, the consideration must always be whether this categorization has been performed according to the aim of the analysis.

4.2. Description of the Benefit of a Process

It is important to define the benefit of a process. Especially for the efficiency, the definition becomes difficult if a process does not generate useful energy, but rather, e.g., a material product. For the heating purpose in this study, the minimum input is easily outlined by the demand as the specific or absolute amount of exergy needed to raise the temperature of the heating water. However, for example, in a baking process, heat is also required. Still, the benefit is the baking of the product, not necessarily the exergy it contains leaving the oven. If the exergy in the product is evaluated as a loss, the energetic and exergetic efficiency would be zero, although the benefit is achieved. The PhO, on the other hand, can be defined, in this case, as the minimum requested energy, for example, to reach a specific temperature. Thus, the PhO factor would return a distinctive value, unlike the efficiency, enabling the evaluation of the efficiency. The PhO allows analysis of a wide range of different applications and is not bound to specific processes, as with some other existing indicators.

4.3. Using Exergy to Describe the PhO

Taking the exergy into account as a state variable enables a more detailed description of a process in some cases. As it was shown for the boiler, the PhO evaluation by means of the exergy confirms the results of the energetic evaluation. Anyway, comparing the HP to the boiler, the exergy analysis shows the absolute minimum input in both cases, which allows a direct comparison. If the energy stored in the fuel is directly compared to the electric energy fed to the HP, the quality of the energy is not regarded. The exergetic content of a specific form of energy can be of high significance for a process comparison. Comparing heat to electric energy means comparing a combination of exergy and anergy to pure exergy. For some applications, the consideration of the exergetic content is highly essential. Thus, the exergy analysis should be integrated into the PhO when necessary.

4.4. Research Directions: Change in Load

The given examples for the PhO describe stationary processes. A change in load was not taken into account in this study. Though it is possible to consider this state as well, this only makes sense if the process is indeed dynamic. If the essential period of time can be outlined, the description of the dynamics in an ideal model is possible again, meaning a PhO can be defined for the change in load as well. The losses caused by the change in load show up in the efficiency of a process over a longer period as well (e.g., seasonal COP). The loss can be significant in a certain instant, and yet be small in the long term due to the short period of time in which it occurs. For a dynamic process such as transport, an optimization of the dynamic behavior can be reasonable. If the dynamics are not taken into account for the PhO, they would show up as avoidable losses in the PhO factor. Therefore, again, the application determines the required level of detail of the analysis.

4.5. Application of the PhO to Other Examples

For a process, the description of the PhO depends on the aim of the analyses, as it has been shown. There are several possibilities for ideal reference processes. The PhOind in comparison to the PhO of each process is an example for this circumstance. However, this study is limited to the example of two options for the supply of heat. In general, the principle can be transferred to other processes. The VDI 4663-1 [3] provides further examples for the application of the PhO as well as the references [1,2,4,5]. As for any other method, the application of the PhO is limited. An example is a process which does not need any input in the ideal case: Considering a room with a temperature differing from the ambient state, an expense of energy would be needed to balance the heat transfer between the environment and the room and maintain the temperature. For an ideal case, the room would be ideally isolated, resulting in an adiabatic system border. The temperature in the room would not change. Thus, the ideal input is zero. The PhO factor is not applicable, F P h O . This particular case could be a potential for improvement in the PhO method.

5. Conclusions

This study presented the potentials of the PhO as well as some particularities and research opportunities. In particular, the advantages of the PhO as a method for energetic analysis were outlined.
Firstly, the PhO establishes the principle of a distinction between avoidable and unavoidable losses. The efficiency only indicates the occurrence of losses in general. The comparison between the efficiencies for the two calorific values outlines one of the advantages of the PhO. While the efficiency depends on the reference to the gross or lower heating value, the PhO method indicates the same degree of avoidable losses in both cases.
Secondly, the integration of exergy as a state variable enables a more precise description of the process for the determination of the PhO. The limits of energy conversion are taken into account by evaluating a type of energy by its exergy content. For the boiler, most of the exergy of the fuel was turned into anergy. Meanwhile, pure anergy was turned into useful heat by a certain amount of exergy in the HP. The distinction between exergy and anergy allows, in this case, a more detailed comparison of the HP to the boiler.
Thirdly, the PhOind enables a direct comparison of different processes in order to outline not only the potential for optimization but also an overall energy input. For the PhO factor, a real demand is considered in relation to an ideal input, which means that, for example, the type of energy is the same for both. The COP of an HP compares heat to pure exergy, and the combustion efficiency compares useful heat to the exergy of the fuel. On the other hand, for the PhO factor, the exergy content of the real input energy type equals that of the ideal input. Thus, the PhOind factors can be compared directly. This also outlines the limits of optimization. For an over-idealized reference, unavoidable losses are categorized as avoidable ones.
Additionally, the PhO allows the consideration of upstream processes, such as the PP providing the electric energy for the HP. The HP process itself might not enable further optimization, while the upstream processes do. In this case, the option of integrating renewables was illustrated for the HP. The example in this study was kept deliberately simple to demonstrate the principle which can be applied to more complex systems.
Lastly, this study pointed out the perspective of further research projects of the PhO such as a change in load.
The significance of reducing the environmental impact of processes is not only evident in inhibiting climate change but also under all conditions. For process optimization, it is inevitable to determine the avoidable losses. The method of PhO is particularly suitable for this. The PhO defines a practical and user-oriented method for the application to a wide range of processes. Therefore, the PhO contributes to the progress in optimization in particular, and the primary objective of resource efficiency in general.

Author Contributions

Conceptualization, D.V. and S.A.W.; methodology, D.V. and S.A.W.; software, D.V. and S.A.W.; validation, D.V. and S.A.W.; formal analysis, D.V. and S.A.W.; investigation, D.V. and S.A.W.; resources, D.V.; data curation, D.V.; writing—original draft preparation, D.V. and S.A.W.; writing—review and editing, D.V. and S.A.W.; visualization, D.V. an S.A.W.; supervision, D.V.; project administration, D.V.; funding acquisition, D.V. All authors have read and agreed to the published version of the manuscript.

Funding

This research was funded by the Evangelical Lutheran Deaconess Hospital Flensburg and the Society for Energy and Climate Protection Schleswig-Holstein (Gesellschaft für Energie und Klimaschutz Schleswig-Holstein GmbH, EKSH), and the Evangelic-Lutheran Deaconesses’ Hospital Flensburg, grant number 8/12-40.

Institutional Review Board Statement

Not applicable.

Informed Consent Statement

Not applicable.

Data Availability Statement

This study did not report any data.

Acknowledgments

The authors gratefully acknowledge the support of the proofreaders, in particular, for language support.

Conflicts of Interest

The authors declare no conflict of interest.

Nomenclature

Roman Symbols
SymbolUnitDescription
Be.g., J, WDemand
cpJ/(kgK)Specific isobaric heat capacity
EJExergy
F P h O B -PhO factor, based on demand
HJEnthalpy
HiJ/kgLower calorific value
HsJ/kgGross calorific value
mkgMass
QJHeat
rJ/kgSpecific condensation enthalpy
SJEntropy
TKKelvin temperature
TTDKTerminal temperature difference
Greek Symbols
ζ -Exergy efficiency
η -Efficiency
λ-Air ratio
v i -Stoichiometric number
Δ Ω B e.g., J, WAvoidable losses
Sub- and Superscript
SymbolDescription
ambAmbient
ashAshes
BFuel, demand
CCarnot
cgCombustion gas
COIncompletely burned
condCondensate
ExExergy
fgFlue gas (exhaust)
fCombustion
HPHeat pump
indProcess-independent
irrIrreversible
lLoss; for air: dry air
mMean, average
NUseful part (e.g., of heat)
PhOPhysical optimum
qHeat
SSurface
SOPStandard operating point
totTotal, overall
˙   Differentiation by time

References

  1. Volta, D. Das Physikalische Optimum als Basis von Systematiken zur Steigerung der Energie- und Stoffeffizienz von Produktionsprozessen. Ph.D. Thesis, TU Clausthal, Clausthal-Zellerfeld, Germany, 5 December 2014. [Google Scholar]
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Figure 1. The PhO in comparison to common reference processes [1].
Figure 1. The PhO in comparison to common reference processes [1].
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Figure 2. System definition for boiler process.
Figure 2. System definition for boiler process.
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Figure 3. Temperature profile inside the heat exchanger of the heat generator.
Figure 3. Temperature profile inside the heat exchanger of the heat generator.
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Figure 4. Combustion efficiency for wood pellets, with reference to the gross calorific value.
Figure 4. Combustion efficiency for wood pellets, with reference to the gross calorific value.
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Figure 5. Energy balance.
Figure 5. Energy balance.
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Figure 6. Cascade of losses for boiler.
Figure 6. Cascade of losses for boiler.
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Figure 7. Exergy balance for boiler, real process vs. PhO.
Figure 7. Exergy balance for boiler, real process vs. PhO.
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Figure 8. Cascade of losses—comparison of heat supply for boiler and HP.
Figure 8. Cascade of losses—comparison of heat supply for boiler and HP.
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Figure 9. Sankey—comparison of heat supply for boiler and HP.
Figure 9. Sankey—comparison of heat supply for boiler and HP.
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Figure 10. Temperature profile of the heat transfer in the condenser of the HP (real vs. PhO, PhOind).
Figure 10. Temperature profile of the heat transfer in the condenser of the HP (real vs. PhO, PhOind).
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