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Представлено дослидження ттеграци теплових пототв багатокорпусног випарног установки для концентрування сиропу сорго. Актуальтсть робо-ти визначаеться технологieю процесу, який вимагае високих витрат енерги. Тому вы дослгдження, спря-моват на зниження споживання зовтшньог енерги i пгдвищення ефективностi роботи, актуальн i мають практичну цттсть.
Головною метою роботи е створення науково обгрунтованого проекту з полтшеними економiчни-ми показниками роботи, забезпечення економи споживання гарячого теплоноыя (пари) i охолоджую-чог води.
Ршення проблеми було проведено з викорис-танням методу пинч-аналiзу. Були гдентифтова-н тепловi потоки, що вимагають нагрiвання та охолодження, i створений альтернативний проект, заснований на виборi значення м^мальног рiзницi температур ^ТтП. Це значення було розраховане i обгрунтовано на основi даних по тепловим потокам. У систему був доданий потж конденсату ретурног пари, надлишок тепла якого не використовувався доы. Для альтернативного проекту була запропоно-вана схема розмiщення теплообмтного обладнання, проведенорозрахунок пластинчастих теплообмтни-кв. Запроектована мережа теплообмтних апаратiв дозволила знизити рiчнi витрати пари на 18 %.
Аналiз економiчног ефективностi проводився порiвнянням показнитв для двох проектiв вiддiлен-ня попереднього нагрiву сиропу для випарног станци. Запропонований альтернативний проект забезпечуе економю споживаног потужностi охолоджуючог води 35,9 кВт, пари, що грiе - 60,5 кВт. При процентнш ставщ податку 18 %реалiзацiя альтернативного проекту окупиться через 4 м^ящ. В результатi чистий рiчний дохiд пгдприемства плануеться бшьше на 16 %, при практично однаковому термiнi окупностi проек-тiв. Застосування методiв ттеграци теплових пото-кгв дозволило розробити ефективний проект попереднього пiдiгрiву сиропу сорго перед випаровуванням та забезпечити економю зовнштх утилт
Ключовi слова: рекуперащя енерги, пiнч-аналiз, випарна установка, пластинчастi теплообмтники,
концентрування сиропу сорго
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UDC 66.012.4
|DOI: 10.15587/1729-4061.2018.133655]
THE INNVESTIGATION OF THE PROCESS STREAMS INTEGRATION IN THE MULTI-EFFECT EVAPORATION PLANT FOR THE CONCENTRATION OF SORGHUM SYRUP
T. Babak
Associate professor* E-mail: tgbabak@gmail.com O. Gol u bki na
Senior Lecturer* E-mail: oalgolubkina@gmail.com Y. Ponomarenko
Associate Professor* E-mail: yevgeniya.ponomarenko@gmail.com
L. Solovey Senior Lecturer* E-mail: ludsol@ukr.net G. Khavin Doctor of Technical Sciences, Professor, Leading researcher Join-stock Company "Sodrugestvo-T" Kaplunovsky lane, 2, Kharkiv, Ukraine, 61002 E-mail: gennadii.khavin@ gmail.com *Department of integrated technologies, processes and apparatus National Technical University "Kharkiv Polytechnic Institute" Kyrpychova str., 2, Kharkiv, Ukraine, 61002
1. Introduction
Evaporation is currently the only actual industrial method of concentration of aqueous solutions, widely used in the chemical and food industries. Principles of construction of evaporating stations are common to all industries, concentrating liquid products, regenerating solvents or particular liquid crystal mixtures. Designing the technological processes of evaporation and the use of different types of equipment for evaporating stations are the focus of a large number of studies, among which we can highlight the practical applications in papers [1-3].
The relevance of the research in this direction is determined, first of all, by the technology of the process, which requires high energy costs. That is why the research, aimed at a decrease in consumption of external energy and an increase in efficiency of evaporating stations, is relevant and has practical value.
2. Literature review and problem statement
Evaporation in a multi-effect evaporator is typically the most energetically expensive process of obtaining a sugar
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solution. That is why the research, aimed at decreasing power consumption and increasing a recovery level are still relevant, both in terms of reducing the cost value of the product and in terms of decreasing emissions and of environmental security. Possibilities of optimal and rational design of multi-effect evaporators, the ways of energy saving have been carefully studied in regard to plants in the sugar producing industry [1-3]. Paper [1] presents the algorithm, based on the methods of process streams integration to optimize evaporator steams, widely used in the chemical and food industries. The main idea of the authors is that to develop new technological processes, implemented for evaporators, it is necessary to optimize the whole flow sheet, rather than separate parts of the system. However, it is not shown in the paper how and why the internal optimization of separate subsystems contradicts to the optimization of the system in general. Paper [2] addresses the integration processes of the evaporator station in the pulp and paper industry. The method for thermoeconomic analysis of the evaporator station, used to study the process of repeated evaporation of calcium bisulfite was proposed. Several variants of modeling the process for different values of minimum temperature difference were obtained. As a result, consumption of external energy can be reduced by 20 %, and in the case of the integration of the system of public services, their corresponding cost can be reduced by 23 % compared with the original scheme. It is not clear from the paper how it is supposed to integrate the system of municipal heat and hot water supply, having a pronounced seasonal and daily irregularity, into a new more efficient scheme of the evaporator operation. Paper [3] deals with the problem of using extra steam during sugar production as a source of heating sugar juice before evaporation and efficiency of their use in the thermal integration. This study presented the equation, which, according to the authors, can be used as a benchmark for thermal plants, including the integration of multi-effect evaporators. However, the presented analysis and the reference equation do not take into consideration the possibility of changes in the number of stages and the tendency of increasing the boiling point for stages with a simultaneous decrease in the time a solution stays in them.
Articles [4, 5] present the basic theoretical principles and practical guidance on application of the method of pinch-analysis. The methods of pinch-analysis make it possible to set the targets of design (optimal values of selected objective-functions, such as minimum values of the capacity of external utilities) before designing the network of recuperative heat exchangers and guarantee that these targets will be met during designing. The issues of thermal integration of multi-effect evaporators and cost-effectiveness of the obtained design solutions were considered.
To identify the ways of saving energy when operating the evaporating stations at sugar factories [6-8], researchers published the data on the overall analysis of the thermal scheme of the sugar factory in general. Thus, paper [6] presents the study of the heat integration of Savannah Sugar Company using the methods of pinch-analysis and software HENSAD. The obtained results showed significant saving of hot and cold utilities at minimal temperature difference of 7 °C.
In articles [7-9], examination of the sugar plant with the capacity of 3,000 tons of sugar beet processing per day was presented. The use of one of the methods of process streams integration (pinch-analysis) identified bottlenecks
in the thermal plant network and its reconstruction project was developed. While implementing this project, specific consumption of thermal power can be reduced by 16 %. The payback period of the proposed modernization does not exceed the duration of the sugar beet processing campaign. The authors predict the possibility of further decrease in the power consumption at the rate of ~30 %.
Typical shortcomings of papers [6-8] may include the fact that the considered thermal scheme of the whole sugar factory does not take into consideration the reciprocal location of streams, that is, it is impossible to connect physically the streams, selected for heat integration, due to their location in different branches of production.
In the course of research, it was found that implementation of thermal integration of heat power for particular sections of a plant, specifically, those preparing or ensuring compliance with the technological process, is not less important in the general scheme. Examples of studying such enterprises, ensuring functioning of the main technological process are presented in articles [9, 10]. These papers deal with the issues of practical modernization of the system of sugar juice heating before evaporation. The operation of the system of heaters for the season of 2012-2013 was analyzed. Conducted monitoring of the operation of the installed heat exchangers proved that there is contamination of heat exchange surface and pressure losses in the first years of the operation of the system. Despite high efficiency of calculated and installed equipment, which was proved by the field observations, the authors could not establish the pattern of emergence and development of deposits on heat transfer surface, quality of sugar juice and temperature mode of the heaters' operation.
This enabled taking into consideration the specific features of sugar production with application of the principles of integration of thermal scheme of evaporation stations, considering the operation of auxiliary equipment, which was reflected, for example, in papers [11, 12]. Paper [11] contains the analysis of contemporary approaches to energy saving in the processes of the multi-effect evaporation. The extraction of data of the evaporator station of sugar syrup concentration (analysis of the technological scheme and identification of the process streams, requiring heating or cooling [4, 5]), was performed and weaknesses in organization of system's energy recovery were identified. Using the methods of heat integration, reconstruction of the existing technological scheme was performed: the network of exchangers, ensuring the maximum possible energy recovery in the system was planned and parameters of heat exchange equipment were calculated for economically reasonable value ATmin. It may be noted as shortcomings that process streams from other branches of production were not considered in these papers, and it was not shown how they affect the operation and thermal integration of the evaporation station.
In article [12], a universal technique for modeling food processes with the methods of pinch-analysis and the exergy analysis was proposed. The methodology was applied to the process of production of sugar from beets. Using software ProSimPlus®, the model of operation of the sugar factory with deviations within uncertainties of the industrial data on industrial enterprises of this type was constructed.
The considered studies on thermal integration of evaporating stations prove the fact that these objects are unique and need to be considered in each particular case. It is connected not only with the number of stages and the kind
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of the evaporated product, but also the operation modes (under pressure or vacuum). The main goal of any project is to minimize extraction of extra steam and maximum recovery of thermal energy. In fact, it is possible to say that the use of the classical schemes when designing such facilities does not provide sufficient heat recovery and cost savings. Designing evaporating stations with the preheating department requires a separate approach to calculation of thermal scheme and energy integration in each specific case. The need for research is related to the development of a new approach to designing the juice preheating department, based on maximum heat recovery to reduce operating costs.
3. The aim and objectives of the study
The aim of the present research is the search for an alternative solution in creation of a project of an evaporation station of sorghum syrup concentration, based on heat recovery, due to designing a new network of the heat exchange equipment. This will make it possible to improve the performance of the station by the criterion of minimization of hot and cold utilities consumption.
To accomplish the aim, the following tasks have been set:
- construction and analysis of composite curves of technology streams;
- selection of economically reasonable ATmin, determining minimal required power of hot and cold utilities for an alternative project, location of heat exchange equipment;
- evaluation of forecasted economic efficiency of the alternative project.
were selected as evaporators. For preheating of syrup to the temperature equal to boiling point before feeding to stage 1 (evaporator 1), it is proposed to use a two-stage steam heating. Preheating of syrup up to the temperature of 80 °C is carried out by steam from the last evaporator (stage 3) and then up to 125.5 °C by return steam. Heat exchangers M6-MFG - E1 and H are selected for heating. Condensation of residual secondary steam from stage 3 was performed in the plate condenser M6-MFG (E2, Fig. 1), in this case, technical water was heated. Cooling of secondary steam condensate is produced in the heat exchanger M6-MFG (C, Fig. 1). All calculated heat exchangers are produced by company "Alfa Laval". The total mass flow rate of return steam with temperature of 140 °C by estimation will make up 692.6 kg/h.
Complete condensation of heating vapors was performed in all heat exchangers - evaporators and condensers. Secondary steam condensate enters the condensate line, is cooled, and collected in a storage container. Condensate of return steam returns to the boiler to generate steam. In this case, the used vapor-condensate system is open that is a condensate after the condensate remover enters the condensate collection tank. This tank is connected to the atmosphere and is not under excessive pressure, and the condensate is pumped into the boiler. In this case, the temperature of condensate in the tank does not exceed 100 °C.
To improve the performance of the technological scheme and to save steam and cooling water, we set the task to study the thermal scheme for possible improvement of energy recovery and reduction of energy consumption from external utilities. To accomplish this, pinch-analysis was selected [9, 11] as one of the most effective methods for studying thermal processes.
4. Calculation scheme of the object and research procedure
It is necessary to design an evaporation station for concentration of sorghum syrup of initial concentration of DS=16 % to the concentration of DS=70 %. The original solution (sorghum syrup) has an initial temperature of 20 °C and mass flow rate of 2,000 kg/h. Saturated steam with the temperature of 140 °C is supposed to be used as the main hot utility. Thermophysical parameters and properties of sorghum syrup were accepted according to reference data and properties from paper [13].
Fig. 1. General flow sheet of the proposed project of evaporation station for the concentration of sorghum syrup
The following flow sheet of evaporation was proposed - a three-stage evaporator under pressure with an equal amount of evaporated water for stages. The boilers of M10-MFG type, manufactured by company "Alfa Laval" (V1-V3, Fig. 1)
5. Analysis of data on heat streams, substantiation of selection of minimum temperature difference and design of a heat exchange network
To analyze the performance of the station operation and to determine the ways of creating an alternative project, the data examination and extraction was performed. In addition to the streams, considered in the original project, the stream of return steam condensate was taken into consideration. This stream is not involved in energy recovery but does not require the use of external utilities for cooling. The data on these streams are given in Table 1.
In the above Table, the following designations were accepted: Ts and Tt are the supply temperature and target temperature of a stream; g is the mass flow rate; CP is the heat capacity flow rate of the stream, determined as c-g; where c, kJ/(kg-°C), is the specific heat capacity; AH=CP\Ts-Tt\ is the required change in heat content of the stream (stream enthalpy [4, 5]), otherwise, heat load of the stream.
Total heat recovery, proposed for implementation in the original project, is equal to 962.5 kW. The composite curves of the streams of the system were constructed (without taking into consideration the stream of return steam condensate) and located on the temperature-enthalpy diagram so that the region of their overlapping by abscissa should be equal to heat recovery (Fig. 2).
This location of the components of the curve corresponds to the value ATmin=16.5°C, that is, the temperature difference in the heat exchangers, must not exceed this value, if they were placed in accordance with the rules of
the pinch-analysis. However, it is not so, specifically, in the heat exchanger E1, minimum temperature difference of heat carriers is equal to 4 °C. To illustrate the shortcomings of the proposed project, its grid diagram is shown (Fig. 3), the analysis of which shows the heat transfer through the pinch, which leads to an increase in power of hot and cold utilities.
Table 1
Data on process streams of the evaporation plant
No Name Type Ts, "C T, °C g, kg/s CP, kW/°C AH, kW
1 Secondary steam of evaporator 1 Hot 124.5 124.5 0.142 - 310,8
2 Secondary steam of evaporator 2 Hot 107 107 0.144 - 322.3
3 Secondary steam of evaporator 3 Hot 84 84 0.143 - 329.4
4 Condensate of return steam Hot 140 100 0.145 0.617 24.7
5 Mixture of condensates Hot 105.1 30 0.429 1.803 135.5
6 Evaporation in evaporator 1 Cold 125.5 125.5 0.556 - 310.8
7 Evaporation in evaporator 2 Cold 108 108 0.413 - 310.8
8 Evaporation in evaporator 3 Cold 85 85 0.269 - 322.3
9 Original mixture (feed) Cold 20 125.5 0.556 2.177 229.7
10 Technical water Cold 25 55 1.587 6.626 198.8
QH=409,9 kW A-►
1
/ 1
1
/ 1
ATm 11=16,5 °C 1
/
/
f .
QC= 135,5 kW •i-
800 1000 S.H, kW
Qrec=962,5 kW
Fig. 2. Composite curves of the streams for the flow sheet in Fig. 1
To improve the existing project, the following actions can be proposed:
- selection of the value of ATmin that is reasonable from the point of view of economy and specificity of production;
- addition to the system of considered streams, the stream of return steam condensation, the excessive heat of which has not been used so far;
- location of heat exchange equipment in accordance with the rules of the pinch- analysis to minimize consumption of external utilities;
- calculation and installation of new plate heat exchange devices.
67,5 °C 198,8 kW Fig. 3. Grid diagram for the flow sheet in Fig. 1
The calculations that predict the value of ATm;n, which provides a minimum of annualized total cost of the project, were performed. Fig. 4 shows dependences of capital investments, cost of external utilities and the annualized total cost, obtained using the Hint Version 2.2 software. The optimal value of ATm;n is approximately equal to 4 °C.
Fig. 4. Cost curves depending on ATmin. Dash line is capital investments, dot line is the cost of utilities, continuous line is the annualized total cost
To implement the project, we selected the value ATm;n= =5 °C, which, on the one hand, is implemented in the plate heat exchangers, and on the other hand, does not lead to an increased heat transfer surface and, correspondingly, to a decrease in a linear velocity of heat carriers' motions in the channels. It is essential in this process, where one of the heat carriers is sorghum syrup, which by analogy with sugar syrup, tends to fairly intense contamination of the heat exchange surface at low velocities of heat carriers in the channels.
For the selected value ATmin=5 °C, composite curves were constructed (Fig. 5), already taking into consideration the stream of return steam condensate, the power of which can be used.
Pinch temperature of the hot streams is 84 oC, of the cold streams - 79 oC. The grid diagram after location of heat exchange devices takes the following form, Fig. 6.
For the project, the flow sheet of which is shown in Fig. 1, the heat transfer equipment, the cost specifications for which are given in Table 2, was proposed.
Fig. 5. Composite curves for streams in Table 1, constructed for value A7"min=5 °C
Fig. 6. Grid diagram with installed heat exchangers for value of A7min=5 °C
Table 2
Type, number of plates and cost of heat exchangers, accepted for installation for the flow sheet in Fig. 1
and evaporation) is based on step-by-step procedure of changing the mass flow rate of vapor content. To determine the pressure drop in the steam, the method of Lokkart-Martinelli for turbulent flow is used. When determining the cost of heat exchangers, we used the linear dependence of
where C, is the cost of the
the form C,U!=Cpl ■
i i +C,
pl frame '
device, Cpl is the cost of one plate with gaskets, Cframe is the cost of frame, npl is the number of plates in the device. All calculated heat exchangers are single-pass, the plates are made of stainless steel AISI 316, gasket material is the rubber EPDM. The cost was determined according to the price-lists of company "Alfa Laval Potok", producing heat exchangers.
Fig. 7. Flow sheet of evaporation station for sorghum syrup concentration with preheating, designed based on pinch-analysis
Table 3
Type, number of plates and cost of heat exchangers, accepted for installation for the alternative design in Fig. 7
Purpose Type Number of plates Price with a 20 % VAT, USD
Recuperative E1 M6-MFG 12 2,668.1
Recuperative E2 M3-FG 11 1,487.9
Recuperative E3 M3-FG 10 1,465.3
Recuperative E4 M6-MFG 22 3,144.3
Recuperative E5 M3-FG 40 2,181.9
Recuperative E6 M6-MFG 14 2,720.4
Cooler C M6-MFG 12 2,615.9
Heater H M6-MFG 10 2,511.0
Purpose Type Number of plates Price with a 20 % VAT, USD
Heater H M6-MFG 12 2,615.9
Cooler C M6-MFG 12 2,615.9
Recuperative E1 M6-MFG 46 4,407.3
Recuperative E2 M6-MFG 22 3,144.3
For the alternate installation scheme for heat exchangers, presented in Fig. 7 and the corresponding grid diagram in Fig. 6, calculation of plate heat exchangers was conducted, the results of which are shown in Table 3. Calculation of the plate heat exchangers was performed using mathematical toolkit, developed with the use of the technique, presented in [14, 15]. Heat exchangers were selected form the nomenclature of gasketed heat exchangers, manufactured by company "Alfa Laval". Calculation of "liquid - liquid" devices was produced by the method of LMTD. Calculation of heat exchangers with phase transition in channels (condensation
As a result of analysis and design of two thermal schemata, two solutions that differ significantly in composition of the used equipment (plate heat exchangers) were obtained. This solution is characteristic when using the methods of pinch analysis [1-3]. Substantiation of the choice for implementation of a project is determined by cost-benefit analysis of equipment operation, which is presented below.
6. Discussion of results: cost-benefit analysis of the projects
For calculation of the economic indicators of the process, the following data were used: the price per 1,000 m3 of gas is USD 422, IRPT (interest rate of profit tax) is 18 %, the number of working hours per year is 6,000. Based on these data, the calculated cost of steam was obtained -
USD 272.7 kWh/year, the cost of water is estimated as 10 % of the cost of steam.
Without energy recovery, the plant must consume the steam power of 739.3 kW, cooling water power of 464.9 kW. The scheme with heat recovery of the original project reduces the power of consumed steam up to 409.9 kW, of cooling water - up to 135.5 kW. The project using the principles of pinch-analysis gives a decrease in power of steam consumption up to 349.3 kW, of water - up to 99.5 kW. Thus, saving of steam power for the original and the alternative projects will amount to 329.4 kW and 389.9 kW, of water -329.4 kW and 365.3 kW, respectively. The data on annual saving of steam and cooling water AS due to heat integration of the process streams and, consequently, a decrease in consumption of external energy sources are shown in Table 4.
Table 4
Indicators of annual saving of external utilities, capital and operating costs, annual net profit and payback period for flow sheets of evaporation station: 1 — Fig.1; 2 — Fig. 6
AS, I, AOC, NAG,
No. USD USD USD USD PP, years
thousand thousand thousand thousand
1 98.8 21.3 5.1 76.8 0.27
2 116.2 31.3 7.5 89.1 0.35
Equipment costs included the cost of heat exchangers with VAT and installation cost (30 % of the cost of the heat exchangers). Design costs were determined in the amount of 15 % of the equipment cost. Design and equipment costs are capital expenditure (I) (Table 4). AOC (annual operating cost) included amortization (15 % of the capital costs of an enterprise) and maintenance costs (15 % of the equipment cost). ANI (annual net income) of an enterprise was calculated as ANI=AS-AOC. NAG (net annual gain) of an enterprise was determined as NAG =ANI.(1-IRPT/100). PP (payback period) was calculated as PP=I/NAG. Comparative analysis of technical and economic indicators of the projects are shown in Table 4.
Thus, the use of a new alternative scheme, for which calculations were performed, makes it possible to significantly save costs of thermal energy. This was achieved through the installation of additional heat exchange equipment, enabling maximization of heat recovery in the juice preheating department.
The results of the conducted technical analysis of the projects show high efficiency and simplicity of the use of the proposed approach in evaluating the process of thermal integration of the systems of the interconnected heat exchange equipment. The main merit of the proposed approach is its consistent analysis when designing (from calculation of minimum temperature difference to economic efficiency assessment) combined with the use of different techniques (tools) for this evaluation. This approach uses high accuracy in calculation of each method, enables a wide variation in
designed parameters, providing for direct and credible assessment of economic efficiency. Possible shortcomings are the requirements for high qualification in designing using the methods of heat integration and calculation of plate heat exchangers.
The presented research can be used when designing evaporation stations regardless of the type of feed for concentration, the number of evaporators and the quantity of steam to be remove. This approach is especially useful when designing new plants.
This study is a continuation of the studies on the development of methods for heat integration and their practical applications in various industries, including the food industry. Further direction of development is to create techniques, algorithms and mathematical toolset for automated assessment of the obtained alternative solutions between themselves and selection the optimal one by the specified criteria.
7. Conclusions
1. Based on a comprehensive analysis of the thermal scheme of the evaporation station, we compiled the table of the data of all thermal streams, which formed the basis for further research on their integration. To implement the syrup preheating, the composite curves of process streams were constructed, the pinch point and minimum temperature difference ATmin=5 °C was determined.
2. Based on the available data, the minimum required power of hot and cold utilities of the two projects was determined and the network of recuperative plate heat exchangers, ensuring maximum heat recovery, was designed. The proposed alternative project provides a decrease in consumed steam power up to 349.3 kW, of water - up to 99.5 to kW.
3. The presented cost-effectiveness analysis showed that the alternative project ensures saving in cold utility (cooling water) consumption of 35.9 kW, of hot utility (steam), of 60.5 kW in relation to the original project. At the interest rate of profit tax of 18 %, the project implementation will be pay off after about 4 months. When implementing an alternative project, due to increased heat recovery in the system, we achieve annual saving of steam and cooling water by 18 %. Net annual net gain of an enterprise is planned to increase by 16 % at a short payback period.
Acknowledgments
All design calculations of the plate two-phase evaporators and condensers, plate heat exchangers "liquid-liquid", as well as some techniques of process streams integration were made using software, developed by the company JSC "Sodruzhestvo-T" (Kharkov, Ukraine) and the Department of Integrated Technologies, Processes and Apparatuses of the National Technical University "KhPI".
References
1. Westphalen D. L., Wolf Maciel M. R. Optimization of bleed streams in evaporation systems based on pinch analysis: new approach // Computer Aided Chemical Engineering. 2000. P. 997-1002. doi: 10.1016/s1570-7946(00)80168-6
2. Perin-Levasseur Z., Palese V., Marechal F. Energy integration study of a multi-effect evaporator // PRES08: 11th Conference Process Integration, Modelling and Optimisation for Energy Saving and Pollution Reduction. Praha, 2008.
3. Thermal integration of multiple effect evaporator in sugar plant / Higa M., Freitas A. J., Bannwart A. C., Zemp R. J. // Applied Thermal Engineering. 2009. Vol. 29, Issue 2-3. P. 515-522. doi: 10.1016/j.applthermaleng.2008.03.009
4. Kemp I. C. Pinch Analysis and Process Integration. A User Guide on Process Integration for the Efficient Use of Energy. Butterworth-Heinemann, 2007. 416 p. doi: 10.1016/b978-0-7506-8260-2.x5001-9
5. Osnovy integracii teplovyh processov / Smit R., Klemesh Y., Tovazhnyanskiy L. L., Kapustenko P. A., Ul'ev L. M. Kharkiv: NTU «KhPI», 2000. 458 p.
6. Barambu N. U. A., El-Nafaty U. A., Saeed I. A. Energy Integration of Sugar Production Plant Using Pinch Analysis: A Case Study of Savanah Sugar Company Yola // Advances in Applied Science Research. 2017. Vol. 8, Issue 2. P. 20-29.
7. Heat Integration Improvement for Eastern European Countries Sugar-Plant / Tovazhnyanski L. L., Kapustenko P. A., Ulyev L. M., Boldyryev S. A. // Proceedings of 15th International Congress of Chemical and Process Engineering, CHISA'2002. Prague, 2002. P. 251.
8. Teplovaya integraciya i energosberezhenie v saharnoy promyshlennosti / Tovazhnyanskiy L. L., Kapustenko P. A., Ul'ev L. M., Boldyrev S. A. // Vestnik NTU «KhPI». 2002. Vol. 1, Issue 9. P. 95-105.
9. Modernizaciya sistemy posledovatel'no ustanovlennyh podogrevateley saharnogo soka / Arsen'eva O. P., Babak T. G., Demirskiy A. V., Havin G. L. // Nauchnye trudy ONAHT. 2011. Vol. 2, Issue 39. P. 151-155.
10. Analiz raboty sistemy podogrevateley saharnogo soka s uchetom zagryazneniy teploobmennoy poverhnosti / Demirskiy A. V., Tovazhnyanskiy L. L., Arsen'eva O. P., Havin G. L., Kapustenko P. A. // Integrirovannye tekhnologii i energosberezhenie. 2013. Issue 2. P. 14-18.
11. Povyshenie energoeffektivnosti raboty stancii uparivaniya saharnogo siropa / Babak T. G., Golubkina O. A., Korol' D. S., Ponoma-renko E. D. // Vestnik NTU «KhPI». 2017. Issue 18 (1240). P. 46-52.
12. Simulation of a sugar beet factory using a chemical engineering software (ProSimPlus ®) to perform Pinch and exergy analysis / Lambert C., Laulan B., Decloux M., Romdhana H., Courtois F. // Journal of Food Engineering. 2018. Vol. 225. P. 1-11. doi: 10.1016/ j.jfoodeng.2018.01.004
13. Eggleston G., Cole M., Andrzejewski B. New Commercially Viable Processing Technologies for the Production of Sugar Feedstocks from Sweet Sorghum (Sorghum bicolor L. Moench) for Manufacture of Biofuels and Bioproducts // Sugar Tech. 2013. Vol. 15, Issue 3. P. 232-249. doi: 10.1007/s12355-013-0229-6
14. Plastinchatye teploobmenniki v teplosnabzhenii / Tovazhnyanskiy L. L., Kapustenko P. A., Havin G. L., Arsen'eva O. P.; G. L. Havin (Ed.). Kharkiv: NTU «KhPI», 2007. 448 p.
15. Mathematical Modeling and optimal Design of Plate-and-Frame Heat Exchangers / Arsenyeva O. P., Tovazhnyanski L. L., Kapustenko P. A., Khavin G. L. // Chemical Engineering Transactions. 2009. Vol. 18. P. 791-796. doi: 10.3303/cet0918162
