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Q1: Department of Chemical Engineering Process Integration 2023 - 2024 Coursework Introduction The purpose of the coursework is to provide you with an opportunity of demonstrating the application of knowledge acquired in the unit to a larger scale industrially related problem. You will make use of knowledge gained in lectures and problem solving and apply it to produce a feasible, validated heat exchanger network. You have a certain period of time to produce the coursework. You will also be expected to apply your own background skills as Chemical Engineers. You will be expected to produce an appropriately structured, written, and presented report, with a limited number of pages. You are provided with some guidance in relation to the structure of the report to be produced, but part of the assessment is to evaluate your skills in relation to reporting the work that you have performed, its validity, and relevance. - The coursework is group based with groups comprising three members. You are required to choose the members of the group and register the group and members in Blackboard. Marks are awarded for group contributions and for individual contributions. For group contributions, all members of the group are awarded the same mark. Individual contributions MUST be labelled with the member making the contribution (student ID). Introduction Stream data for a chemical process are given in Table 1.1. Table 1.1 Stream data Stream Ts (°C) TT (°C) CP(kW °C-1) HTC (kW m² K-1) Hot1 430 300 5 0.8 Hot2 285 40 1.4 0.8 Hot3 280 25 2.0 0.6 Hot4 230 70 11.0 0.6 Hot5 140 50 23 0.8 Hot6 120 35 30 0.8 Cold1 180 350 12 0.6 Cold2 110 210 12 0.8 Cold3 30 150 18 0.8 A Maximum Energy Recovery Heat Exchanger Network (MER HEN), using the Pinch Design method, is to be designed for this chemical process using a minimum approach temperature (AT MIN) of 20°C. The MER HEN is to be designed in three parts (above the utility pinch, above the process pinch, and below the process pinch). There are three utilities available to provide additional process heating and cooling (Table 1.2). The specific heat capacity of the hot oil is 1.5 kJ kg¯¹ K−¹. The final developed MER HEN and its component parts (above the utility pinch, above the process pinch, and below the process pinch) are required to be validated and tested for feasibility, by comparing their features with targeted values. Table 1.2 Utility data Utility Ts (°C) Hot Oil 390 TT (°C) 310 Cost (£/kWh) HTC (kW m² K-1) 0.6 1.5 MP Steam 241 Cooling Water 5 240 10 0.35 3.0 0.05 1.0 Task 1 (Group Task – 40 marks) Using a minimum approach temperature (ATMIN) of 20°C, determine the overall hot utility requirement (QHmin), overall cold utility requirement (Qcmin), and overall heat recovery (QREC) for the chemical process given in Table 1.1. These results should be supported by the appropriate graphical and tabular information. In addition, and making use of the utilities that are available for additional heating and cooling (Table 1.2), determine the duty of the hot oil to be provided (kW), the MP steam (kW), and the cooling water (kW). The use of two hot utilities (hot oil and MP steam) produces a utility pinch at shifted temperature of 231°C. Your results need to confirm this utility pinch shifted temperature value. (Note that MP steam will be used in preference to hot oil due to its lower cost of supply). Task 2 (Individual Task – Member 1 – 30 marks) Produce a feasible, validated Maximum Energy Recovery Heat Exchanger Network (MER HEN) for the Above Utility Pinch Design region using the Pinch Design method for the chemical process (Table 1.1), using a minimum approach temperature (AT MIN) of 20°C. In this design region you should be using only hot oil as a utility. The report should contain all the information required to demonstrate the Maximum Energy Recovery Heat Exchanger Network (MER HEN) for this design region using is feasible and validated. The report should contain a table of all of the heat exchangers used in this design region which includes the hot stream entry and exit temperatures, the cold stream entry and exit temperatures, and the duty of the heat exchangers. Task 3 (Individual Task - Member 2 - 30 marks) Produce a feasible, validated Maximum Energy Recovery Heat Exchanger Network (MER HEN) for the Above Process Pinch Design region (and below the utility pinch) using the Pinch Design method for the chemical process (Table 1.1), using a minimum approach temperature (AT MIN) of 20°C. In this design region you should be using only MP steam as a utility. The report should contain all the information required to demonstrate the Maximum Energy Recovery Heat Exchanger Network (MER HEN) for this design region using is feasible and validated. The report should contain a table of all of the heat exchangers used in this design region which includes the hot stream entry and exit temperatures, the cold stream entry and exit temperatures, and the duty of the heat exchangers. Task 4 (Individual Task - Member 3 - 30 marks) Produce a feasible, validated Maximum Energy Recovery Heat Exchanger Network (MER HEN) for the Below Process Pinch Design region using the Pinch Design method for the chemical process (Table 1.1), using a minimum approach temperature (ATMIN) of 20°C. In this design region you should be using only cooling water as a utility. The report should contain all the information required to demonstrate the Maximum Energy Recovery Heat Exchanger Network (MER HEN) for this design region using is feasible and validated. The report should contain a table of all of the heat exchangers used in this design region which includes the hot stream entry and exit temperatures, the cold stream entry and exit temperatures, and the duty of the heat exchangers. Task 5 (Group Task – 10 marks) Produce a feasible, validated Maximum Energy Recovery Heat Exchanger Network (MER HEN) using the Pinch Design method for the chemical process (Table 1.1), using a minimum approach temperature (ATMIN) of 20°C, and the utilities provided in Table 1.2. This is essentially the final MER HEN Design combining the designs from Region 1 (above the Utility Pinch), Region 2 (above the Process Pinch), and Region 3 (below the Process Pinch). You can refer to information that you have provided in Tasks 2,3, and 4, but you are required to comment and discuss the feasibility and validity of the final MER HEN. There will be help available from myself and Dr. Salman Shahid and the GTA's. However, this help is related to general guidance only. You are being assessed on your own ability to design the required Heat Exchanger Networks. Marking scheme and Report Submission It is up to you to decide the exact format of your report and what should be included to support the work you have done. A marking sheet and a marking scheme will be made available. However, the report should include the following sections; Task 1 (Group based - maximum 40 marks) Task 2 (Member 1 - maximum 30 marks) Task 3 (Member 2 - maximum 30 marks) Task 4 (Member 3 - maximum 30 marks) Task 5 (Group – maximum 10 marks) - Marks are also awarded for presentation of the report (Group based) – maximum 10 marks. Marks are also awarded to contribution from group members. This is done via Peer Assessment (method of awarding this mark will be released nearer to submission date). Maximum 10 marks. Total 100 marks maximum per group member As the space is limited, present information that you think is relevant and reflects the work that has been done and the points that you are attempting to make to an audience. Not all information can be presented as space is not sufficient. Part of the skill is deciding what is relevant and how to express it. DO NOT BE VERBOSE. The mark sheet to be used for assessment and the marking scheme will be available in separate documents. The report should be completed in MS Word, and should not contain more than 18 pages (which does not include a front page). Pages above this limit will be penalised by a reduction of 5% per additional page in your overall mark. Late submission of the coursework will also result in a penalty of a reduction in your overall mark. The later the submission the larger the reduction!!!! Late submission penalties are set by the Department. Mitigating circumstances can be submitted to support late submissions. Again, this has been set by the Department and further information can be found in the Student Handbook and Virtual Common Room. A pdf version of the report should be produced (CutePDFWriter is a good PDF production tool and is available online or on the CEAS computers), and this PDF should be uploaded into Blackboard. There will be an area in the Energy Systems Blackboard space for doing this and appropriate instructions a week prior to the submission date. The submitted report in Blackboard will be checked by TURNITINUK for plagiarism and collusion. BE WARNED!!!!!! If you are unsure of the meaning academic malpractice including plagiarism or collusion, please ask.See Answer
Q2: Clean Technologies and Environmental Policy https://doi.org/10.1007/s10098-020-01893-0 ORIGINAL PAPER Recycling of used lubricating oil by solvent extraction: experimental results, Aspen Plus simulation and feasibility study Nancy Zgheib¹D. Hosni Takache¹ Received: 30 September 2019 / Accepted: 27 June 2020 © Springer-Verlag GmbH Germany, part of Springer Nature 2020 Check for updates Abstract This study investigates the recycling of used lubricating oil (ULO) by solvent extraction using a ternary solvent consist- ing of 2-propanol, 1-butanol and methyl ethyl ketone (MEK) followed by a vacuum distillation unit. In order to select the best combination of solvents for the liquid–liquid extraction process, many parameters were first evaluated on a laboratory scale such as the effect of the solvent composition, the solvent-to-oil ratio and the temperature. The oil recovery efficiency and the physicochemical properties of the oil obtained from the extraction process were measured, and the results showed that a ternary system consisting of 50% 1-butanol/25% isopropanol/25% MEK is the best mixture for effectively reducing the contaminants in ULO with a good sludge separation prior to the fractionation. Also, a solvent-to-oil ratio of 3:1 and a temperature of 25 °C are the optimal parameters for the extraction when the aforementioned solvent mixture is used. The whole re-refining process including the vacuum distillation unit was then simulated for a plant capacity of 2125 kg/h using Aspen Plus™. Four pseudo-components (saturate, monoaromatic, diaromatic and polyaromatic) together with the nonrandom two-liquid (NRTL) and universal quasichemical activity coefficient (UNIQUAC) were used to describe the liquid-liquid equilibrium (LLE) in the system solvent/lubricating oils during the extraction phase. The calculated yields on the extraction unit performed for different solvent composition, solvent-to-oil ratio and temperature showed a good agreement with the experimental data performed at the laboratory scale which verifies the right choice of the solvent mixture. The investiga- tion of the amount and composition of oil loss inside the sludge obtained from the simulation showed that the contaminant reduction and the oil recovery depend on the percentage of 1-butanol in the solvent mixture. Also, the results confirmed that the amount of MEK and 2-propanol in the solvent mixture should not exceed 25% and the best results were obtained when 1-butanol was used as a base solvent with an amount of 50%. Finally, to check the feasibility of the process, the investment payback time and the return on investment of the re-refining process were evaluated. Based on the economic study results, the production process was found to be highly profitable with a return on investment equal to 55% and a payout period of 1.9 years in the worst-case scenario where the price of lubricating oil is 2.5 $/L. ☑ Nancy Zgheib 1 nancyzgheib@usek.edu.lb Department of Chemical and Petroleum Engineering, School of Engineering, Holy Spirit University of Kaslik (USEK), Jounieh, Lebanon Published online: 14 July 2020 Springer Graphic abstract ULO Re-Refining of ULO Transport ✓ Experimental Study Dehydration ✓ Process Simulation ✓ Sensitivity Analysis Feasibility Study Solvent Extraction Solvent Recycling Fractionation N. Zgheib, H. Takache Recycled Lubricating oil . . . Keywords Recycling · Used lubricating oil · Solvent extraction Aspen plus simulation · Feasibility study Introduction Used motor oil is a hazardous material and harmful for the environment and for the human health because of the pres- ence of pollutants, for instance heavy metals, polychlo- rinated biphenyls and polycyclic aromatic hydrocarbons (Kanokkantapong et al. 2009). In the absence of an appro- priate treatment, used motor oil is normally discarded in the ground and into waterways including sewers making it an environmental hazard (Hamad et al. 2005). At the same time, ULOS are considered as valuable resources since the recycling of such materials will reduce the imports of oil products and will have a positive impact on the environ- ment as well (Totten and Bruce 2006). Numerous studies have reported the recycling of lube oil; however, there has been very little research reported on the re-refining of used lubricating oil (Boadu et al. 2019). ULO can be recycled and used as an alternative fuel in a variety of engine con- figurations and furnaces or as an important component in road paving asphalt. The most preferred option by experts in terms of energy requirements, cost and environment is the re-refining process (Jafari and Hassanpour 2015). Springer . Re-refining is a process that removes all contaminants for the purpose of reusing the base oil as lube oil. The conventional methods of contaminants removal that have been used on an industrial scale either require the use of toxic materials such as sulfuric acid or implies high cost technologies such as vacuum distillation. The acid pro- cess followed by clay treatment is the oldest one. This process is capable of producing high-quality base oil with the lowest cost but have the highest environmental risk. Membrane technology is another method for recycling the used motor oils where hollow fiber membranes such as polyethersulfone, polyvinylidene fluoride and polyacry- lonitrile are used (Cao et al. 2009). Solvent extraction has been employed as an alternate method to treat the used oil and the solvent chosen should have maximum solubility for the base oil and minimum for additives and impuri- ties. Vacuum distillation is also used to separate asphalts, additives and breakdown products from the base oil. This process operates at high temperature above 300 °C and proved to be impractical because of coking and fouling of processing equipment. The extraction process using liq- uid-liquid solvent performed prior to distillation of the Recycling of used lubricating oil by solvent extraction: experimental results, Aspen Plus... used lubricating oil is an alternative solution to the sepa- ration of asphalts and additives by vacuum distillation. Many studies have been conducted on the re-refining of used oil using solvent extraction (Whisman et al. 1978; Dos Reis and Jeronimo 1988; Alves dos Reis and Jeronimo 1990; Martins 1997; Elbashir et al. 2002; Hamad et al. 2005; Daham et al. 2017). Supercritical fluids propane and ethane are used as extracting solvents for recycling used motor oils but give low yield 72–80% (Rincón et al. 2003). According to Reis et al. (Dos Reis and Jeronimo 1988; Alves dos Reis and Jeronimo 1990), ketones and alcohols are the most effi- cient solvents for extraction since they are miscible with the base oil on the one hand and flocculate some of the additives and carbonaceous compounds by applying an antisolvent effect on the other hand. The capability to segregate sludge is closely related to the difference between the solubility of the solvent and the polyisobutylene, a viscosity improver additive. Whisman et al. (1978) showed that a ternary sys- tem consisting of 25% 2-propanol, 25% butanone and 50% 1-butanol is reasonably effective to reduce contaminants in the oil with a good sludge separation. They indicated that 2-propanol rich systems produce high ash reduction but poorly separated sludge, while butanone-rich systems lead to a good sludge separation, but re-dissolve the contaminants. To adjust the ash reduction and oil recovery properties, an equal percentage of 2-propanol and butanone was employed and 1-butanol was chosen as a base solvent. Few studies have reported the simulation of an extraction process using vacuum distillates as main feed (Coto et al. 2006a, b; Espada et al. 2008), and only one study (Botas et al. 2017) has reported the simulation and design of the re-refining process of ULO using propane as a solvent for the extraction process. In fact, the simulation of the extrac- tion process of such systems is complex due to the huge number of components present in the lubricating oil. To be able to properly reproduce the equilibrium properties dur- ing the extraction operation, an appropriate thermodynamic model must be used. Also, the number, the composition and the properties of each component that are taken into con- sideration to describe the system should be well defined. The approach usually used to describe the components pre- sent in petroleum product is based on distillation curves. This method is not suitable for extraction processes since the chemical structure of the oil and the solvents used has a much bigger effect than the boiling temperatures. In order to estimate the LLE of the systems furfural/lubricating, Coto et al. (2006a, b) used a model based on a correlation of pseudo-component properties (specific gravity, density, refractive index and sulfur content) and NRTL parameters with the oil average boiling temperature. This method has proved to be highly effective for any lubricating oil cut and needs only the average boiling point and three physical prop- erties as experimental data. In this study, three mixtures of composite solvents con- taining 2-propanol, 1-butanol and MEK were first investi- gated on a laboratory scale to treat the used oil. The choice of the solvent and the ratio of the ternary system were based on a literature investigation (Whisman et al. 1978; Dos Reis and Jeronimo 1988; Alves dos Reis and Jeronimo 1990). The objective of this investigation is to select the best combina- tion of solvents as well as the optimal operating conditions for the extraction unit. In fact, solvent selection is critical for the development of an economical extraction system and the optimal solvent selection is based on laboratory effort before starting the design or the selection of the extraction unit. For this purpose, the effect of the solvent type and composi- tion, the solvent-to-oil ratio and the temperature on the oil recovery efficiency and the physicochemical properties of the oil obtained from the extraction process will be studied. Then, the whole re-refining process will be simulated with Aspen plus™, and the yields of the extraction unit obtained by varying the solvent type and composition as well as the solvent-to-oil ratio and the temperature will be compared to the experimental results. The detailed composition of the oil in the sludge obtained from the simulation will be inves- tigated in order to study the effect of the solvent type and concentration on the contaminant reduction and the oil loss. Finally, a profit and loss analysis of the recycling process will be performed to explore if the application of the process at industrial scale could be recommended. Experimental section Materials Virgin lubricating oil was purchased from the local mar- ket. The used lubricating oil samples were collected from Mercedes-Benz lube change center in Lebanon. The sam- ple used in this study is a mixture of used oil coming from automobiles operating with different engine conditions. The sample was stored in a suitable tank away from light and at room temperature. Solvents used for extraction were 2-pro- panol, 1-butanol and MEK. The solvents purchased from Sigma-Aldrich were of analytical grade with 99.5% purity. Solvent extraction process The oil was first filtered and then dehydrated using a rotary evaporator. This operation was carried out to remove water and some light hydrocarbons. The dehydrated used oil was collected and then used for the next step of solvent extrac- tion. Three different compositions of a ternary system con- taining 2-propanol, 1-butanol and MEK were used in this study, and the composition of the three mixtures is reported in Table 1. Springer N. Zgheib, H. Takache Table 1 Composition (vol%) of the solvent mixtures used in the extraction process Mixture composition 2-propanol 1-butanol (%) MEK (%) (%) Mixture A 25 50 Mixture B 25 40 Mixture C 40 35 25 535 25 5355 The used oil was weighed (mo) and mixed for 20 min with the composite solvent mixture using an electrical stirrer at 500 rpm. The solvent-to-oil ratios employed in this study were 2:1, 3:1 and 4:1, and the extraction temperatures used were 25, 40 and 60 °C. The mixture was then left unshaken for a period of 24 h to allow extraction-flocculation. Then, solvent-oil solution was separated from the sludge by decan- tation and the solvent mixture was recovered. This proce- dure was repeated in all experiments for three times. The oil recovered was weighed (mp), and the percentage of lubricat- ing oil extracted was calculated using Eq. (1). %R = 100 × mp то (1) where % R is the percentage of lubricating oil extracted, то is the mass of the ULO, and mp is the mass of the oil obtained after the separation of the solvent in the extract. Analysis of samples The ULO was tested for ASTM D-1160 method. The recy- cled oil obtained from the extraction was analyzed for differ- ent physical properties such as: Flash points by ASTM D56, pour point by ASTM D97-02, viscosity index by ASTM D445-18, density (specific gravity) by ASTM 1298, ash con- tent by ASTM 482-13 and sulfur content by ASTM D4294. Kinematic viscosity The kinematic viscosity is the measure of the resistive flow of a fluid under the influence of gravity. A fixed volume of oil was charged into the capillary of a calibrated viscometer which has a flow time above 200 s. The diameter of the capillary was chosen by considering the expected viscosity. The viscometer was placed into a constant temperature bath maintained at the temperature on which the viscosity is to be determined. A chronometer was used to determine the time the oil takes to progress between two points highlighted inside the capillary. The viscosity is determined by multiply- ing the efflux time by the viscometer constant. Pour point The pour point of petroleum products is the lowest temper- ature at which the oil will flow under cooling prescribed conditions of test. A specific amount of oil was placed in a test jar which is closed with a cork engulfing a thermom- eter. The oil was heated in a bath at 48 °C, then cooled at intervals of 3 °C and tilted to determine the flow charac- teristics. The pour point is reached when the fuel no longer moves upon holding the specimen horizontally for 5 s. Flash point The flash point is the lowest temperature at which vapors of the material will ignite under the application of an igni- tion source. The test cup was filled with oil to the required volume, and both the test cup and the specimen were main- tained at a temperature that is at least 23 ±5 °C below the flash point expected. The temperature of the specimen was increased, and the ignition source is applied to the vapor area in the cup. The sample is considered to have reached the flash point when a large flame occurs and instantane- ously propagates over the whole surface of the specimen. Ash content This method consists of measuring the amount of ash- forming material in the oil which provides an idea about the quality of the product and the adequacy for any application since the ash represents the impurities and unwanted components. The sample was placed in a suit- able vessel and was burned until only ash was left behind. The evaporating crucible was heated at 775 °C, cooled to room temperature and weighed. The mass of the ash was then calculated as a percentage of the original sample. Sulfur content This test measures the sulfur content in petroleum prod- ucts. The sample was placed in the beam emitted from an X-ray source, and the resulting fluorescent X-rays were measured and the sulfur concentration in mass% was deter- mined by comparing the accumulated count with counts from previously prepared calibration samples. Vacuum distillation of used lubricating oil ASTMD 1160-13 standard method was used to determine at reduced pressures the range of boiling points for used motor oil. The sample of ULO was vacuum distilled at Springer Recycling of used lubricating oil by solvent extraction: experimental results, Aspen Plus... about 65 mm mercury and over a temperature range of 272-400 °C. Experimental results Oil recovery is an important parameter to be considered, and it represents the economy of the process since it accounts for the oil yield obtained from the extraction process. The ash reduction is also a vital parameter in the extraction process since it accounts for the reduction of the concentration of the contaminants in the oil such as dirt, iron oxide, wear metals and corrosion products as well as the concentration of ash- producing additives. The sulfur reduction also accounts for the removal of sulfur compounds and additives. The recov- ered oil obtained from the extraction experiments performed with mixtures A, B and C using a solvent-to-oil ratio of 3:1 was tested for oil recovery, ash reduction % by means of ASTM 482-13 and sulfur reduction % by means of ASTM D4294. The results obtained for different compositions of the ternary solvents used are shown in Table 2. As it is shown in Table 2, the optimum solvent mixture that produces maximum oil recovery (96%) with maximum ash reduction (28%) and an acceptable sulfur reduction (16.7%) was achieved with solvent mixture B. These results indicate that mixture B is capable of reducing contaminants in the oil with a good contaminant separation. The high per- cent oil recovery obtained for mixture B is in good agree- ment with Whisman et al. (1978) who reported that using higher percentage of MEK than 25% produces good sludge separation and thus high oil recovery since MEK has a lower solubility parameters value than the two alcohols. However, increasing the amount of 2-propanol does not decrease the ash forming material as reported in the literature. This differ- ence might be associated with the nature of the base oil and to the fact that these days ash-less materials are used in the additive package instead of ash forming materials. The solvent-to-oil ratio investigation was conducted on mixture B. The investigated solvent-to-oil ratios were 2:1; 3:1 and 4:1, and the extraction temperature used was 25 °C. The oil recovery results in relation to solvent-to-oil ratio are shown in Fig. 1. It can be seen that the best condition after which a further increase in the solvent oil ratio bring no Table 2 Oil recovery %, ash reduction % and sulfur reduction % val- ues obtained from the solvent composition experiments performed at the laboratory scale Oil recovery (%) 100 90 80 70 60 50 40 30 20 10 0 2 3 Solvent to oil ratio 4 Fig. 1 Percentage of oil recovery for optimum solvent-to-oil ratio experiments performed on mixture B using an extraction temperature of 25 °C change in the percent oil recovery values is above a solvent- to-oil ratio equal to 3:1. This can be attributed to the fact that increasing the solvent-to-oil ratio improves the solubility of the oil in the solvent resulting in decreasing the oil loss in the sludge and increasing the oil recovery values. Solvent- to-oil ratios higher than 3:1 are not considered economically feasible by industry, and the experimental results showed no improvement in terms of oil recovery. Thus, a solvent-to-oil ratio of 3:1 will be considered to be the optimum ratio in this work. To study the effect of the temperature on the extraction- flocculation process, the extraction was performed on mix- ture B at three different temperatures (25, 40 and 60 °C) using a solvent-to-oil ratio of 3:1. The oil recovery results in relation to the extraction temperature are shown in Fig. 2. No significant change in percent oil loss was shown with increasing the extraction temperature. Thus, the extraction process at a temperature higher than 25 °C does not lead to a higher yield of oil recovery. Oil recovery (%) 100 90 80 70 60 50 40 30 20 Mixtures Oil recovery (%) Ash reduction Sulfur 10 (%) reduction 0 (%) 25 40 60 Temperature (°C) Mixture A 90 27 20 Mixture B 96 28 16.7 Mixture C 84 20 14.3 Fig. 2 Percentage of oil recovery for optimum extraction temperature experiments performed on mixture B using a solvent/feed ratio of 3:1 SpringerSee Answer
Q3: UO 09 STEAM GENERATOR 1. INTRODUCTION In many engineering processes the first step is the production of heat energy by combustion. One way to distinguish between combustion processes is according to whether the energy produced by combustion is intended to be retained in the products of combustion or transferred to an external fluid (such as water). In boilers for electricity generation, space heating or raising of process stream, the usefulness of the combustion process depends on the proportion of the calorific value of the fuel transferred as heat energy to the external working fluid; any heat retained in the flue gases is largely wasted. The steam generator pilot plant uses water as the feed fluid and propane as the combustion fuel to produce steam. The steam vapour is subsequently condensed and recycled back around to the steam generator. The Air/Fuel ratio and flowrate of gas can be moderated. The water feed flowrate using the positive displacement pump can be varied. The output combustion gases can be analysed, allowing the calculation of an energy balance over the unit. Various key temperature, pressure, flowmeter indicators are fitted. The steam pressure can also be moderated using a control valve (adjustable PRV, V7, see Figures 1 & 2). 27 30 31 34 36 37 38 225 2333353 28 29 1 Cooling water inlet valve V10 26 Waste gas analysis device 2 Cooling water flow meter F2 27 Flow safeguard 3 Cooling water feed 28 Exhaust pipe 4 Condensate return 29 Exhaust gas measuring point O2, CO₂. CO 5 Condensate return valve V11 30 Temperature measuring point T7 6 Process schematic 31 Steam boiler A2 26 25 24 23 22 21 20 19 18 17 16 15 14 7 Switch for condensate pump 32 Live steam pressure sensor P1 8 Main switch 33 Condensate trap 9 Steam connection for consumer units 34 Ignition electrodes 10 Main steam shut-off valve V8 35 Air feed to the boiler 13 11 Steam temperature controller for 36 Feedwater pump P1 12 superheater 11 12 Temperature selector 37 Fine adjustment valve for gas V1 10 13 Measurement readouts 38 9 Gas connection and gas main valve with thermal cutout 8 7 14 Signal lamps 39 Lockable roller 6 15 Reset button 40 Valve for draining (pipe) 5 # 16 Pressure sensor for condenser P2 41 4 Differential pressure sensor Feedwater level L1 3 2 17 Condenser A1 42 Valve for draining (feedwater tank) 18 Condenser pressure controller 43 Concentrate pump P2 19 Non-return valve V6 44 Valve for draining (condenser) 20 Live steam pressure controller 45 Water jet pump P3 21 Pressure retention valve V7 46 Shut-off valve for water jet pump V9 22 Steam safety valve V5 47 Power supply connection 23 Ventilation 40 41 42 43 44 45 46 47 48 49 50 48 Cooling water discharge 24 Feedwater tank B1 49 USB connector 25 Superheater W1 with water trap A3 50 Table frame 2. AIMS Figure 1: Steam generator module (Boxhammer, 2012) 1. To understand the operating principles of a steam generator plant. 2. Experimental determination of the turndown ratio of the burner for propane. 3. Calculation of the stoichiometric air/fuel ratios and net combustion heat release. 4. To understand the importance of determining a heat balance for a chemical reaction (combustion). 5. To understand the principles and calculation of combustion efficiency. 1 3. OPERATING PROCEDURE KTC Superheater W1 Water trap (T5 A3 P1 V5 X1 P3 V8 Main steam Water jet pump CO₂ 0₁₂ Condensate Vent pipe Boiler trap ☑ ☑IV9 V6 (T3) Feed- T1 T6 Conden water A2 ser tank B1 P2 A1 Cool- T2F2 ing (L1) 山 L V10 (P3 5 2 V1 V3 (F3 V4 -- Gas F1 T4 V12 P1 Feedwater pump Condensate return L V11 P2 Condensate pump V13 on the gas cylinder Figure 2: P&ID of steam generator (Boxhammer, 2012) Al Condenser A2 Boiler A3 Water trap B1 Feedwater tank P1 Feedwater pump P2 Condensate pump P3 Water jet pump X1 Condensate trap V1 Fine adjustment valve for gas V2 Gas solenoid valve V3 Gas pressure regulator V4 Gas main valve with thermal cutout V5 Steam safety valve V6 Non-return valve V7 Pressure retention valve V8 Live steam shut-off valve V10 Cooling water inlet valve V11 Condensate return valve V12 Feedwater non-return valve F1 Feedwater flow F2 Cooling water flow F3 Gas flow L1 Feedwater level P1 Live steam pressure P2 Pressure in the condenser P3 Gas pressure T1 Temperature in the condenser T2 Cooling water inlet temperature T3 Cooling water outlet temperature T4 Feedwater temperature T5 Live steam temperature superheater T6 Saturated steam temperature T7 Exhaust gas temperature Table 1: Key to P&ID V9 Shut-off valve for the water jet pump 2 NOTE: The exhaust chamber surface of the burner is extremely hot, this can reach in excess of 250 °C. Start-Up (refer to Figure 2 and panel): 1. Ensure that all valves are closed (especially check that V8 and V11 are fully closed, this is essential for safety), except V7 which should be fully open. 2. Switch on the power supply. 3. Open V10 (cooling water) and adjust the flowrate to 80 l/hr at F2. 4. Check that the feed water level in vessel B exceeds 2200 ml. If lower than 2200 ml ask academic staff to top this up. 5. Check that the level in condenser (A1) does not exceed 300 ml. If more than 300 ml in A1, excess liquid can be transferred to vessel B using the condensate pump, P2 (the start switch for P2 is on the panel next to the main power supply). 6. Ask Academic Staff to Do: Open main valve on gas cylinder, and open and adjust the pressure regulator to 1 bar. 7. Open V3 (yellow handled valve on gas cylinder line under the desk). 8. Open V1, by turning anticlockwise 3 complete turns. 9. Start feed pump P1 and set flowrate to 8 l/hr (visual display on pump) and start condensate pump P2. 10. Ignition stage: Maintain a distance of at least 30 cm from the burner housing. Press reset button on panel and then press reset burner button on panel. If the burner does not ignite wait 3 minutes before attempting to re-start. 11. Check ignition (look for flame in burner), adjust V1 to set a gas flowrate of approximately 5.0 1/min at F3 (note adjust slowly as valve is sensitive). 12. Fully open V9 and adjust V10 to the keep flowrate at 80 l/hr at F2. 13. Adjust V7 to set the steam pressure to 8 bar at P1 (Note: there is a lag between adjusting V7 and the pressure change so do this slowly). 14. Allow system time to stabilise (this occurs when you have a consistent flame in boiler, and instrument measurements level out) before commencing experiments. Note: Ensure A1 level does not exceed 400ml, and feed tank does not empty. Operation: Experiment 1 (Varying Gas Feed Flow): Start the equipment as described in the start-up procedure. Vary the gas fuel flowrate at F3 at values of approximately 4, 5, and 6 l/min. Keep the water feed flow at 8 l/hr and steam pressure at 8 bar. Experiment 2 (Varying Steam Pressure): With a fuel flowrate of 5 l/min, water feed flow rate of 8 1/hr, vary the steam pressure at values of 7, 7.5 and 8 bar by adjusting V7. Experiment 3 (Varying Feed Water Flow): With a fuel flowrate of 5 l/min, steam pressure of 8 bar, vary the water feed flow at values of 7, 7.5 and 8 1/hr. Experiment 4 (Varying Air Flow): With a fuel flowrate of 5 l/min, steam pressure of 8 bar, and feed flow of 8 1/hr, vary the air flow (ask staff to help do this). Experiment 5 (Turndown Ratio): Determine the turndown ratio of the boiler. Starting with the conditions described in the start-up procedure, adjust V1 until the maximum gas flowrate is obtained at F3. Then adjust V1 slowly until the flame in the boiler goes out. Make a note of the high and low gas flowrates. For experiments 1-4 you will need to record the temperature of the feed water in, the steam temperature and pressure, the feed water flow rate, the gas flow rate, the ambient air temperature, the flue gas temperature, the % by vol of O2 in the flue gas, the % by volume of CO2 in the flue gas, the air/fuel ratio (2) value (1.0 indicates stoichiometric air, 1.2 indicates 20% excess air) and the combustion efficiency 3 (n). These final values are obtained using the DRAGER gas analyser, the use of which is explained in the video (but will be recapped on the day). Shut down: 1. Close V1. 2. Close V3. 3. Switch of gas bottle (Staff to do this). 4. Switch off P1 and P2. 5. Wait 5 minutes. 6. Close V9 and V10. 7. Switch off power. 8. Close all valves except V7 which should be opened fully. 4. THEORY 4.1 Turndown ratio Turndown ratio refers to the width of the operational range of a device and is defined as the ratio of the maximum capacity to minimum capacity. For the steam generator the turndown ratio can be defined as: TD=max gas flow / gas flow when flame goes out 4.2 Heat Balances (see Felder and Rousseau (2016); Smith et al., (1996)) The stoichiometric equation for the complete combustion of propane is given as: C3H8 (g) +502 (g) → 3CO2 (g) + 4H₂O (1) (4.1) (4.2) In order to calculate the heat given out by this reaction equation (4.3) is used: AHReact Σni Hfi products - Σni Hfi reactants (4.3) where AHReact is the heat of reaction, n; is the number of moles of component i and Hƒ¡ is the heat of formation of component i (Note: All of this data is usually obtained at 25 °C and can be found in Appendix 1). In this case the heat of reaction is also known as the heat of combustion. There are different heats of combustion available in the literature as some reactions have the water product as a gas whilst others have the water product as a liquid (as in this case). The gross calorific value or standard enthalpy of combustion at 298 K is when the water product of combustion is in the liquid state (as in equations 4.2 and 4.3), whilst the net calorific value is found by taking into account the heat of vaporization of water at 298 K e.g. AHReact NetΣni Hfi products - Σni Hfi reactants + NH2O H20@298K (4.4) so that, C3H8 (g) +502 (g) → 3CO2 (g) + 4H₂O (g) (4.5) We now need to consider the overall heat balance in the steam generator, In the generator, propane and air are taken in (remember air is 21% by mol (or vol) O2 and 79% by mol N2) at room temperature and are then combusted to give out heat. This heat is taken up by the feedwater so that the water boils to create steam. The rest of the heat is either taken up by the flue gases or is lost to the environment. In order to calculate the amount of heat available for uptake by the boiler water we need to construct a van't Hoff box on the combustion system as shown in Figure 3. The heat balance over the box gives: AHoverall = AH1 + ▲H2+ AH3 (4.6) 4 Ti AHoverall Reactants AH₁ 298 K ΔΗΣ Figure 3: The van't Hoff box where, AH₁ = Σni Cpi, Ti (298 – Ti) AH₂ = AHReact Net AH3 = Σni Cpi, Tf (Tƒ – 298) AH3 Products 298 K (4.7) (4.8) (4.9) and Cpi is the specific heat of component i, T; is the ambient temperature and Tƒ is the flue gas temperature. Note: Values for heats of formation of individual species and specific heat capacities of gases are given in Appendix 1. A positive value of AH; signifies that heat is added to the system, while a negative value indicates that heat is lost by the system. The heat taken up by the water, which becomes steam can be determined from the enthalpy of the water feed subtracted from the enthalpy of the steam out: Qsteam-m (hg-hf) (4.10) where m is the mass flow rate of water into the system, hg is the enthalpy of steam at the given temperature and pressure and hƒ is the enthalpy of the feed water in at the given temperature of the feed. 4.3 Characteristic Values of the Steam Generator 4.3.1 Evaporation rate The boiler's evaporation rate (mst) is calculated from the supplied quantity of feedwater (Vw) and its density at the feedwater temperature. mst Vfwp@Tfeed (4.11) 4.3.2 Combustion efficiency The combustion efficiency indicates how much of the energy contained in the fuel is used during combustion by the steam generator. The remaining energy is lost in the form of exhaust gas losses. It is defined as follows: η = 1 - (ΔΗ3 / ΔΗ2) (4.12) Note: (i) When using the efficiency equations remember to use the magnitude for AH; not the +/- value. (ii) This value can be compared to the value given by the DRAGER gas analyser(eta [n] value). 5See Answer
Q4:a) %Excess air and Fuel Ratio [20 Marks] The Orsat flue gas analysis from a boiler house chimney by volume is provided as below If there is complete combustion takes place, Answer the following CO₂ = 12.5%; O₂-4.5%; N2=83% (i) Calculate the % Excess air (10 Marks) (ii) Calculate the C to H ratio in the fuel (10 Marks) Note: Carbon and Hydrogen gas fuel are used in boilerSee Answer
Q5:b) Energy balance with chemical reaction Perform energy balance calculation for following chemical reaction. SO2 (g) +(1/2)02 (g) SO3(g) [13 Marks] (i) Obtain an empirical equation relating the heat of reaction and the temperature. (10 Marks) (ii) Using the same expression in task 2b(i), calculate the heat of reaction at 773 C as per table 3 data. (3 Marks) Data Given ΔΗ = -98910 kJ/km ole cp=a = a + bT + cT² + dT³, kJ/(kmole.K) or J/(mole.K) Gas a b x 103 cx 106 d x 109 SO2 (g) 24.7706 62.9481 -44.2582 11.122 Oz (g) 26.0257 11.7551 -2.3426 -0.5623 SO3 (g) 22.0376 121.624 -91.8673 24.3691 [Table 3: C constants for task 2]See Answer
Q6:a) Enthalpy Balance of gas stream Analyze enthalpy balance calculation for the gas stream having composition as per table 1. calculate the heat content of 1 km ole gas mixture from 298 C to 775 C using given components as per table 2. data of Gas Composition (Mole %) SO₂ 7.09 SO3 FFF 10.55 0.45 81.91 [Table 1: Gas mixture composition for task 2a)] Co= a + bT + CT² + dT³, kJ/(kmole.K) or J/(mole.K) Gas a b x 103 cx 106 d x 10⁹ SO2 (g) 24.7706 62.9481 -44.2582 11.122 Oz (g) 26.0257 11.7551 -2.3426 -0.5623 SO3 (g) 22.0376 121.624 -91.8673 24.3691 N2 (g) 29.5909 -5.141 13.1829 -4.968 [Table 2: Co constants for task 2a)]See Answer
Q7:a) Reverse Osmosis Cell with Recycle Sea water is to be desalinized by reverse osmosis with brine recycling at following plant scheme shown figure 1. For the given plant scheme and data, answer the following [12 Mar Feed (F) (M) 1000 kg/h sea water 3.3% salt 3.9% Salt Recycle Brine (R) 6% Salt Reverse Osmosis Cell (W) Brine waste (B) 6% Salt Desalinised water (D) 475 ppm Salt [Figure 1: Recycled plant schematic for task 1a)] (i) Calculate the rate of brine waste (B) (4 Marks) (ii) Calculate the rate of desalinized water (D) (4 Marks) (!!!) Calculate the ratio of Recycled stream (R) to the Reverse osmosis cell outlet (W) flow (4 Marks)See Answer
Q8:8. Consider the following reaction: CH4 + O2 → HO2 + CH3. The rate coefficient is k = 3.8 x 10⁹ x T x exp (-20000/T) cm³/gmol.s. The CH4 and O2 mole fractions are 0.02 and 0.03 respectively. What is the activation energy of the reaction? Calculate the characteristic time of the reaction at 2100 K and P = 2 bar.See Answer
Q9:6. Explain in your own words with examples the law of mass action, order and molecularit of a reaction. (5 pointsSee Answer
Q10:5. Write the Fick's Law for a Binary Mixture and explain the different terms in the equation. (4 points)See Answer
Q11:3. What is a Global reaction? What is an Elementary Reaction? Explain the differences between the two reactions (Global vs Elementary). (5 points)See Answer
Q12:2. Calculate the mass fraction and volume fraction of O2 and N2 in Air (O2 + 3.76 N2). (6 points)See Answer
Q13:5. Ethylene oxide (C2H4O) is a high volume chemical intermediate that is used to produce glycol and polyethylene glycol. Ethylene oxide is produced by the partial oxidation of ethylene (C2H4) using a solid catalyst in a fixed bed reactor: 2C2H4 + 02 → 2C2H4O Unfortunately, a portion of the ethylene reacts completely to CO2 and H2O: C2H4+302 → 2CO2 + 2H2O (1) The product gas leaving a fixed bed ethylene oxide reactor has the following water free composition: 20.5% C2H4O, 72.7% N2, 2.3 % O2, and 4.5% CO2. Determine the percent excess air used in the reactor, based on the desired reaction (1) and the mass of ethylene feed (in lbs/hr) required to produce 100,000 tons/year of ethylene oxide.See Answer
Q14:4. A synthesis gas analyzing 6.4% CO2, 0.2% O2, 40.0% CO, and 50.8% H2 (the balance is N2) is burned with 40% dry excess air. What is the composition of the flue gas?See Answer
Q15:9.3. What power is required for the mixing operation of Prob. 9.1 if a propeller 360 mm in diameter turning at 15 r/s is used and if four baffles, each 120 mm wide, are installed?See Answer
Q16:9.2, What is the maximum speed at which the agitator of the tank described in Prob. 9.1 may be driven if the liquid is replaced by one having a viscosity of IP and the same density?See Answer
Q17:9.1. A tank 1.2 m in diameter and 2 m high is filled to a depth of 1.2 m with a latex having a viscosity of 10 P and a density of 800 kg/m³. The tank is not baffled. A three-blade 360-mm-diameter propeller is installed in the tank 360 mm from the bottom. The pitch is 1:1 (pitch equals diameter). The motor available develops 8 kW. Is the motor ade- quate to drive this agitator at a speed of 800 r/min?See Answer
Q18: AU الجامعة الأسترالية AUSTRALIAN UNIVERSITY الكويت - KUWAIT Advanced process simulation (PBL) / 21SPTE323 Spring 2024 Project Title: Gasification in the Oil and Gas Industry for Sustainable Resource Management Project statement: In the dynamic oil and gas industry landscape, effective waste management is paramount to ensure environmental sustainability and resource efficiency. The oil and Gas Industry generates diverse waste streams, ranging from coal and petroleum coke to biomass, plastics, and refinery residues. The treatment and utilization of these materials present both challenges and opportunities. It is within this context that gasification emerges as a pivotal solution. Gasification, a sustainable and versatile process, is vital to transforming waste products into valuable syngas, aligning with the industry's commitment to cleaner energy production and resource optimization. In the following questions and tasks, students will delve into the multifaceted realm of gasification, exploring its technical intricacies and broader implications within the oil and gas sector. 1. Literature Review: - Evaluate the technologies currently used to treat Oil and Gas Industry Wastes. Investigate the current state of gasification technology. Explore recent advancements and innovations in gasification processes. Review case studies or projects that have successfully implemented gasification in the oil and gas industry for different applications. 2. Process Design Using Promax Software: - Design a gasification process using Promax software. Simulate the key reactions in a gasifier and analyze the composition of the produced syngas. 3. Environmental Impact Assessment: Assess the environmental impact of gasification, particularly in terms of carbon dioxide emissions. Explore methods to minimize environmental impact, such as carbon capture and storage (CCS) technologies. Explore ways to integrate renewable energy sources into gasification to enhance sustainability and reduce dependence on non-renewable resources. 4. Feedstock Flexibility: Investigate the suitability of different feedstocks (petroleum coke, petroleum sludge, biomass, waste streams) for gasification. Analyze how the choice of feedstock influences the composition and characteristics of the syngas. AU الجامعة الأسترالية AUSTRALIAN UNIVERSITY الكويت - KUWAIT 5. Product Flexibility and Polygeneration: Advanced process simulation (PBL) / 21SPTE323 Explore the possibilities of polygeneration plants using gasification. Spring 2024 Consider the production of various products like hydrogen, ammonia, and gasoline from the same gasification process. 6. Infrastructure Requirements: Analyze the infrastructure needed for implementing gasification on a large scale. Consider transportation and storage logistics for syngas and its by-products. 7. Techno-Economic Analysis: Conduct a techno-economic analysis of a gasification plant, considering factors such as capital and operating costs. 8. Outlook and Market Potential: Explore the potential growth of gasification in the global energy and industrial sectors. Consider how advancements in technology and changes in market dynamics may impact the future of gasification.See Answer
Q19:2:43 1 HW3_Individual.pdf : 71 Problem 1 ⚫Jacketed Non-adiabatic CSTR. The reaction A→B takes place in a jacketed non-adiabatic CSTR reactor. The reaction is a single first-order exothermic and irre- versible reaction. The reactant A is converted into b, the product. The initial concentration of component A is CA,= 15 kmol/m³. The inlet volumetric flow rate is F, 200m³/h, the volume of the reactor is V = 380 m³, the inlet temperature is 250 K, the liquid density is 600 kg/m³, and the fluid heat capacity is Cp=3 kJ(kg.K). • Develop Degree of Freedom. • Derive a model that represents the given scenario. Solve that problem mathematically and compare your results by SIMULINK. Results will be evaluated thru your laptop in the class.See Answer
Q20: Swansea University Prifysgol Abertawe EG-208 Process Design and Simulation Assignment 1 (25%): Pinch Analysis EG-208 is a continually assessment module. This assignment will contribute 25% towards module grade. your overall The aim of this assignment is for you to demonstrate the following: ● Your ability to apply the Pinch Analysis Technique using EXCEL to identify the pinch temperature and the potential maximum heat recovery that could be achieved. • • Your ability to design a Heat Exchanger Network that identifies which streams could potentially be used to achieve the identified maximum heat recovery. Your understanding of practical considerations that need to be made when trying to actually implement the proposed heat exchanger network design, as well the importance of Pinch Analysis as a tool for Chemical Engineers. Submission Guidance Your submission will comprise of two files as described below: File 1. A spreadsheet containing the Pinch Analysis calculations, related charts and the heat exchanger network diagram you have developed to answer Part A. File 2. A PDF file which contains the following. • • A section that contains a summary that the data generated in the Excel File against the criteria outlined in Part A. This summary should be presented in the same manner as shown in the solution document provided in Week 20 for the Class Exercise. (https://canvas.swansea.ac.uk/courses/45029/pages/pinch-technology-exercise- answers?module item id=2541658) A section that contains your written discussion that answers Part B of the of the Assignment. Each file will have its own Canvas Submission point. You only be allowed to make 1 submission for each file. Please ensure you submit the final version of your files, and to the correct submission point. For each file, please use your student number as the file name. Once you have made your submission, go back into the submission links and check that the correct files have been submitted. Please be aware when viewing your spreadsheet file using the preview function in Canvas, you may find the formatting appears incorrect. Download the file to check that it is correct. 1 Please note: Zero tolerance for late submission applies. Academic Misconduct This is an individual assessment; working in groups, helping or receiving help from other students or third parties is not permitted. The spreadsheet for part A which contains your pinch analysis must be your own work and generated by you from first principles. The University regulations regarding academic misconduct apply. For further information regarding Academic Misconduct please use the following link: Academic Misconduct Procedure Be wary of using Al Tools to develop your answers to this assignment. Please speak with Dr Richard Butterfield for further guidance on this matter. Further guidance can be found here: Artificial Intelligence Guidance - Swansea University 2 Part A: Pinch Analysis (30 Marks) The data provided Table 1 lists streams that have been identified as suitable for heat exchange recovery. Table 1: Details of Hot and Cold Streams to be used in the Pinch Analysis Heat Capacity Flowrate CP(kW/K) Initial Temp Ts(°C) Final Temp T+(°C) Cold Stream 1 60 30 180 Cold Stream 2 20 80 160 Cold Stream 3 10 80 160 Hot Stream 4 40 180 40 Hot Stream 5 30 150 60 Hot Stream 6 15 210 80 Based on the assumption that you must maintain a minimum temperature difference of 20°C, and achieve maximum heat recovery, develop an EXCEL spreadsheet to apply the pinch technology techniques and produce the following: • The "Composite Curves" for the hot and cold streams. • The "Shifted Composite Curves" for the hot and cold streams. • The "Problem Table" and "Infeasible & Feasible Heat Cascades" for this analysis. • The "Grand Composite" curve for this process. • Clearly identify the minimum hot & cold utilities required for this process. • Clearly identify the pinch temperature for this process. Your design of a heat exchanger network compliant with maximum heat recovery. The network diagram should clearly show which streams are interchanging heat, the magnitude of the heat being exchanged, and the inlet & outlet temperatures of the streams passing through the heat exchangers used to facilitate the heat interchange. Note: You must ensure the minimum temperature difference is maintained. You may split process streams as outlined in the literature. You should then produce a PDF document in which you formally present the findings of your pinch analysis, including the number of heat exchangers required by the network you have designed. The summary of the findings from your EXCEL file should be presented in the manner shown in the solution to the class exercise in Week 20 of the course material. The summary table provided on Page 5 can be used as part of your submission. 3 IMPORTANT- Please note: You are expected to perform the pinch analysis in this assignment using a spreadsheet that you personally have created from first principles. It should be an active spreadsheet with all the relevant calculations developed and presented logically within the spreadsheet. If your spreadsheet is not an active spreadsheet, i.e. the data values have not been calculated within the spreadsheet, then you will receive ZERO MARKS for Part A of the assignment. Graphs should be plotted in Excel and when inspected should link to the data you have generated within the spreadsheet. Your heat exchanger network diagram should be presented clearly on a separate tab within your spreadsheet file. It is preferred that you use appropriate software tools to present your network diagram. Please see the Pinch Analysis Class Exercise solution document from Week 20 to see how you should present your findings for Part A in your PDF Document. General Breakdown of Marks for Part A • The "Composite Curves" for the hot and cold streams. [3 marks] • The "Shifted Composite Curves" for the hot and cold streams. [3 marks] • The "Problem Table” and “Infeasible & Feasible Heat Cascades” for this analysis. [5 marks] • The "Grand Composite" curve for this process. [3 marks] • Clearly identify the minimum hot utility required for this process. [2 marks] • Clearly identify the minimum cold utility required for this process. [2 marks] • Clearly identify the pinch temperature for this process. [2 marks] • Your design of a heat exchanger network compliant with maximum heat recovery. [10 marks] Total Marks Available for Part A = 30 Marks 4 Answer Summary Sheet for Part A Student Name Measure Minimum Heating Utility kW Minimum Cooling Utility kW Pinch Temperature °C Number of Heat Exchangers Required Summary of Heat Exchanger Duty Streams Heat Interchanged Exchanged kW Student Number Answer Hot Stream Inlet Temperature Hot Stream Outlet Cold Stream Cold Stream Inlet Temperature Temperature Outlet Temperature N.B. The number of rows in this table is no indicator of the expected number of heat exchanges required in this problem. 5See Answer

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