{"id":2140,"date":"2026-01-09T06:10:57","date_gmt":"2026-01-09T06:10:57","guid":{"rendered":"https:\/\/palegreen-baboon-853405.hostingersite.com\/?p=2140"},"modified":"2026-01-09T12:33:53","modified_gmt":"2026-01-09T12:33:53","slug":"mastering-chemical-process-design","status":"publish","type":"post","link":"https:\/\/instrontechnologies.com\/ca\/mastering-chemical-process-design\/","title":{"rendered":"Mastering Chemical Process Design"},"content":{"rendered":"\t\t
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Mastering Chemical Process Design: A Comprehensive Guide to Efficiency and Sustainability<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
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by Milind Saindane | Jan 11, 2024 | Uncategorized<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
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Introduction<\/h2>\t\t\t\t<\/div>\n\t\t
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Process design and optimization play a vital role in creating and improving the manufacturing processes for chemicals and related products. Chemical process design includes several stages, including conceptual design, process development, detailed design, construction, and operation. The ultimate goal of chemical process design is to develop a cost-effective and safe process that can produce high-quality products at a high yield.<\/p>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t<\/div>\n\t\t\t\t<\/div>\n\t\t\t\t<\/div>\n\t\t\t\t

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Importance of Chemical Process Design:<\/h2>\t\t\t\t<\/div>\n\t\t
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  • Cost reduction:\u00a0It can help reduce production costs by identifying and eliminating inefficiencies in the production process. By optimizing the process, manufacturers can produce more with fewer resources, reducing the cost of production.<\/span><\/li>
  • Improved product quality: Manufacturers can improve the quality of the product. The process can be designed to produce products that meet specific quality standards, resulting in fewer defects and customer complaints.<\/span><\/div><\/li>
  • Increased safety :By identifying potential hazards and mitigating them during the design stage, manufacturers can reduce the risk of accidents during production and ensures the safety of workers.<\/span><\/div><\/li>
  • Environment Sustainability : Minimize waste and energy consumption and promote the reuse of materials, manufacturers can reduce their carbon footprint and contribute to a more sustainable future.<\/span><\/li>
  • Competitive Advantage : Manufacturers can get a competitive advantage by improving their efficiency, quality, and sustainability. This can help them gain market share and increase profitability.<\/span><\/li>
  • Innovation : Manufacturers can lead to the development of new products\/technologies and processes that are more efficient and sustainable.<\/span><\/li><\/ul>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t<\/div>\n\t\t\t\t
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    Chemical Process Design:<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
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    Creating of manufacturing process in cost effective and safe manner involves several steps including basic engineering package, detailed engineering packages, construction and operation. Process engineers are professional who play a vital role to design a process which can produce high quality products efficiently.<\/p>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t

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    Basic Engineering Design Services:<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
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    Basic Engineering Design (BED) or Front-End Engineering Design (FEED) services is most important engineering design activity for working on any Greenfield or Brownfield projects. BED will establish the specific set of process operating conditions and equipment necessary to achieve the level of reliability, efficiency, and safety required. This design phase sets the direction for the rest of the project. At the completion of this phase, a cost estimate of +40%\/-20% can typically be developed for the project. BED puts great emphasis on the development of the Design Basis at the initiation of design. When the design basis is complete, we typically have the following information defined:<\/p>

    • Raw material specifications<\/li>
    • Plant capacity requirements<\/li>
    • Product specifications<\/li>
    • Critical plant operating parameters<\/li>
    • Available utilities specifications<\/li>
    • Individual unit operations performance requirements<\/li>
    • Process regulatory requirements<\/li>
    • All other operating goals and constraints desired by the plant<\/li><\/ul>


      Once the design basis is in place, and agreed upon with the client, process engineer works to create, analyze, and optimize the many aspects of the plant design. The end result is process documentation that clearly defines the process.Typical Process Engineering Deliverables for BED package can include the following or a smaller subset of these items:<\/p>

      • Process design basis<\/li>
      • Material & Energy Balance (M&EB)<\/li>
      • Process Flow Diagrams (PFDs)<\/li>
      • Process descriptions<\/li>
      • Utility balances and Utility Flow Diagrams (UFDs)<\/li>
      • Preliminary Piping & Instrumentation Diagrams (P&IDs)<\/li>
      • Process control description<\/li>
      • Preliminary line\/pipe list<\/li>
      • Preliminary instrument list<\/li>
      • Process equipment list<\/li>
      • Preliminary Tie-in list<\/li>
      • Equipment process datasheets<\/li>
      • Instrument process datasheets<\/li>
      • Hydraulic design reports.<\/li><\/ul>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t
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        Case studies on chemical process<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
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        Let us assume a homogeneous liquid phase non-catalytic reaction. In this reaction two organic raw materials, chemical \u2018A\u2019 and chemical \u2018B\u2019 reacts to form chemical \u2018C\u2019. This is an exothermic reaction and raw material \u2018A\u2019 is limiting reactant. Chemical \u2018B\u2019 consumption is 1.25 times of reactant \u2018A\u2019. Heat of reaction is 150 kcal\/kg of reacted \u2018A\u2019.<\/p>

        In this process equilibrium conversion of the reaction is 85% on the mass basis for reactant \u2018A\u2019. This reaction takes place at 85 \u00b0C and atmospheric conditions. Selectivity of the reaction is 95% on mass basis. And remaining 5% of reacted \u2018A\u2019 converts into high boiling tar like material. This residue composition is as below which is sent for incineration. The calorific value for residue is 7500 kcal\/kg approximately.<\/p><\/div><\/div><\/div><\/div>

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        \n\t\t\t\t\t\t\t\t\t\t\t\t\t\tSr. No.<\/span><\/th>\n\t\t\t \t\t\t\t \n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\tComponent<\/span><\/th>\n\t\t\t \t\t\t\t \n\t\t\t\t\t\t\t\t\t\t\t\t\t\tComposition (wt%)<\/span><\/th>\n\t\t\t \t\t\t\t <\/tr>\n\t\t\t <\/thead>\n\t\t\t \t
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        \n\t\t\t\t\t\t\t\t\t\t\t\t\tChemical B\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
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        \n\t\t\t\t\t\t\t\t\t\t\t\t\t3\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
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        \n\t\t\t\t\t\t\t\t\t\t\t\t\tChemical C\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
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        \n\t\t\t\t\t\t\t\t\t\t\t\t\t4\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
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        Physical and Chemical Properties:<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
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        For our batch reactor process calculations, we need physical and chemical properties for the chemicals are in below table.<\/p>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t

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        \n\t\t\t\t\t\t\t\t\t\t\t\t\t\tSr. No.<\/span><\/th>\n\t\t\t \t\t\t\t \n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\tComponent<\/span><\/th>\n\t\t\t \t\t\t\t \n\t\t\t\t\t\t\t\t\t\t\t\t\t\tNormal Boiling Point (\u2103)<\/span><\/th>\n\t\t\t \t\t\t\t \n\t\t\t\t\t\t\t\t\t\t\t\t\t\tHeat Capacity (kcal\/kg\u2103)<\/span><\/th>\n\t\t\t \t\t\t\t \n\t\t\t\t\t\t\t\t\t\t\t\t\t\tDensity (kg\/m3)<\/span><\/th>\n\t\t\t \t\t\t\t \n\t\t\t\t\t\t\t\t\t\t\t\t\t\tHeat of Vapourization (kcal\/kg)<\/span><\/th>\n\t\t\t \t\t\t\t <\/tr>\n\t\t\t <\/thead>\n\t\t\t \t
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        \n\t\t\t\t\t\t\t\t\t\t\t\t\tChemical B\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
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        \n\t\t\t\t\t\t\t\t\t\t\t\t\t90\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t0.35\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t900\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t100\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t<\/tr>\n\t\t\t \t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t3\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\tChemical C\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t100\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t0.35\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t1000\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t90\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t<\/tr>\n\t\t\t \t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t4\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\tHeavies\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t120\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t0.35\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t1000\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t \t\t\t\t\t\t\t\t\t\t\t
        		\n\t\t\t\t\t\t\t\t\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t–\t\t\t\t\t\t\t\t\t\t\t\t<\/div><\/div>\n\t\t\t\t\t\t\t\t\t\t\t<\/td>\n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t<\/tr>\n\t\t\t \t\t\t <\/tbody>\n\t\t\t<\/table>\n\t\t<\/div>\n\t \t\t\t\t\t<\/div>\n\t\t\t\t
        \n\t\t\t\t\t

        Reaction:<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t

        A (liq.) + B (liq.) \u2014-> C (liq.)<\/b>\u00a0at 85 \u00b0C and atmospheric pressure<\/p>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t

        \n\t\t\t\t\t

        \nProcess Flow Diagram (PFD)\n<\/h2>\t\t\t\t<\/div>\n\t\t
        \n\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t\"\"\t\t\t\t\t\t\t\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t

        Here,<\/b>
        RM \u2013 Raw Material , CWS \u2013 Cooling Water Supply, CWR \u2013 Cooling Water Return, Cond. \u2013 Steam Condensate<\/p>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t

        \n\t\t\t\t\t

        Material Balance for the Batch Reactor System<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
        \n\t\t\t\t\t\t\t\t\t

        This process includes two steps first is reaction and second is batch distillation. The material balance for per batch will be as below.<\/p>

        • Charge of RM \u2013 A, 2000 kgs\/batch<\/li>
        • Charge of RM \u2013 B, 2500 kgs\/batch (since B is charged 1.25 times of A)<\/li>
        • Total mass of in reactor (RM \u2013 A + RM \u2013 B = 4500 kgs\/batch)<\/li>
        • Equilibrium conversion is 85% hence unreacted RM \u2013 A in crude product = 2000*(100 \u2013 85)\/100 = 300 kg.<\/li>
        • Unreacted RM \u2013 B in crude will be = 300*1.25 =375 kg.<\/li>
        • Product C in crude will be (2000 + 2500) *0.85*0.95 = 3633 kg (since selectivity is 95% for the product C.)<\/li>
        • Heavies\u2019 generation in reaction will be = (2000 + 2500) *0.85*0.05 = 181.7 kg\/batch. Since the composition of heavies in residue is 95% hence residue generation per batch will be = 181.7 *100\/95 = 191.3 kg.<\/li>
        • Loss of RM \u2013 A in residue will be 191.3 *1\/100 = 1.91 kg\/batch<\/li>
        • Loss of RM \u2013 B in residue will be 191.3 *2\/100 = 3.83 kg\/batch<\/li>
        • Loss of Product C in residue will be 191.3 *2\/100 = 3.82 kg\/batch<\/li><\/ul>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t
          \n\t\t\t\t\t\t\t\t\t

          The recovered quantities from distillation based on 90% recovery will be as below<\/p>

          • RM \u2013 A recovered = 300 *90\/100 = 270 kg\/batch<\/li>
          • RM \u2013 B recovered = 375 *90\/100 = 337.5 kg\/batch<\/li>
          • Product \u2013 C recovered = 3633 *90\/100 = 3269.7 kg\/batch<\/li>
          • Intercut quantity of A & B = 45.5 kg\/batch (66% A and 34% B) \u2013 from R&D package<\/li>
          • Intercut quantity of B & C = 44.0 kg\/batch (50% B and 50% C) \u2013 from R&D package<\/li><\/ul>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t
            \n\t\t\t\t\t\t\t\t\t

            Total production of product \u2013 C will be = product in crude \u2013 loss in intercut \u2013 loss in residue = 3633 \u2013 22 \u2013 3.82 = 3607.2 kg\/batch.<\/b>
            Total RM \u2013 A consumed = Charged \u2013 Recovered = 2000 \u2013 270 = 1730 kg\/batch<\/b>
            Total RM \u2013 B consumed = 2500 \u2013 337.5 = 2162.5 kg\/batch<\/b><\/p>

            Energy Balance for the Batch Reactor System<\/p>

            Heating utility for our process is 3.5 bar steam at saturated conditions. The temperature of the steam is 139 \u00b0C and latent heat is 513.5 kcal\/kg.<\/p>

            Steam Requirement<\/p>

            Heat load for reaction mass heating after charging of RM \u2013 B will be Q1 = mass RM-B * Cp * (initial temp \u2013 final temp) = 2500*0.35*(80-35) = 39375 kcal\/batch. Hence steam requirement will be\u00a0m1 = Q1\/513.5 = 76.7 kg\/batch.<\/b><\/p>

            Heat load and steam requirement in distillation will as follows:<\/p>

            For recovery of RM \u2013 A, heat load will be Q2 = mass recovered * (1 + reflux ratio) * latent heat = 270*(1 + 5) *100 = 162000 kcal\/batch. Steam requirement will be\u00a0m2 = Q2\/513.5 = 162000\/513.5 = 315.5 kg\/batch<\/b>.<\/p>

            Similarly, for RM \u2013 B recovery Q3 = 337.5*(1 + 10)*100 = 371250 kcal\/batch. Steam requirement will be\u00a0m3 = Q3\/513.5 = 723.0 kg\/batch.<\/b><\/p>

            For product recovery Q4 = 3269.7*(1 + 10)*90 = 3237003 kcal\/batch. Steam requirement will be\u00a0m4 = Q4\/513.5 = 3237003\/513.5 = 6303.8 kg\/batch.<\/b><\/p>

            For first intercut Q5 = 44.5*(1 + 25)*100 = 115700 kcal\/batch. Steam required will be\u00a0m5 = Q5\/513.5 = 225.3 kg\/batch.<\/b><\/p>

            Heat load for second intercut Q6 = 44.0*(1 + 40)*100 = 180400 kcal\/batch. Hence steam requirement will be\u00a0m6 = Q6\/513.5 = 351.3 kg\/batch.<\/b><\/p>

            Therefore, total steam requirement for total batch processing will be Q = Q1 + Q2 + Q3 + Q4 + Q5 + Q6 = 76.7+315.5+723.0+6303.8+225.3+351.3 = 7995.6 kg\/batch. Considering 5% steam loss actual steam requirement will be\u00a0Q\u2019 = 1.05*Q = 8395 kg\/batch.<\/b><\/p>

            Cooling Water Requirement<\/p>

            Cooling water flow rate requirement will be based on when our reaction is going on and pure product draw is going on. As this will be maximum requirement any point of time during the process.<\/p>

            • Hence, heat load on jacket during reaction q1 = rate of addition A * heat of reaction = 500 * 150 = 7500 kcal\/h (for calculation we are considering 100% conversion). Cooling water supply and return temperature are 32 and 40 \u00b0C respectively. Hence, cooling water flow will be\u00a0w1 = q1\/(Cpw*(40-32)) = 7500\/(1*(40-32)) = 937.5 kg\/h.<\/b><\/li>
            • Heat load during pure product draw (3269.7\/10 = 327 kg\/h) will be q2 = 327*(1 + 10) *90 = 323730 kcal\/h. Therefore, cooling water requirement at column condenser will be\u00a0w2 = q2\/(Cpw*(40-32)) = 323730\/(1*(40-32)) = 40466 kg\/h.<\/b><\/li>
            • Water circulation in reactor condenser w3 = 5000 kg\/h. Total flow rate for cooling water pump will be\u00a0W = w1 + w2 + w3= 937.5 + 40466 + 5000 = 46403.5 kg\/h or 46.4 m3\/h.<\/b><\/li><\/ul>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t
              \n\t\t\t\t\t

              Conclusion<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
              \n\t\t\t\t\t\t\t\t\t

              You can use this procedure to carry out the material and energy balance for the batch reactor plant. For your work you will get a technology package from your R&D department. In this you will get all the information regarding reaction and downstream requirement.<\/p>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t

              \n\t\t\t\t\t

              Instron Technologies LLP<\/h2>\t\t\t\t<\/div>\n\t\t\t\t
              \n\t\t\t\t\t\t\t\t\t

              We provide basic engineering design service optimized to the process requirements based on our experience in various industries, such as pharma, food and chemical as skid-mounted unit or for any greenfield & brownfield projects. Rest assured, the contents of the basic engineering can be customized according to your preferred scope of supply, whether it\u2019s limited to key equipment or extends to a complete skid-mounted unit.<\/p>\t\t\t\t\t\t\t\t<\/div>\n\t\t\t\t<\/div>\n\t\t\t\t\t<\/div>\n\t\t\t\t<\/div>\n\t\t

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              \n\t\t\t\t
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              \n\t\t\t
              <\/div>\n\t\t<\/div>\n\t\t\t\t\t\t<\/div>\n\t\t\t\t\t<\/div>\n\t\t\t\t<\/div>\n\t\t\t\t<\/div>\n\t\t","protected":false},"excerpt":{"rendered":"

              Mastering Chemical Process Design: A Comprehensive Guide to Efficiency and Sustainability by Milind Saindane | Jan 11, 2024 | Uncategorized Introduction Process design and optimization play a vital role in creating and improving the manufacturing processes for chemicals and related products. Chemical process design includes several stages, including conceptual design, process development, detailed design, construction, and operation. The ultimate goal of chemical process design is to develop a cost-effective and safe process that can produce high-quality products at a high yield. Importance of Chemical Process Design: Cost reduction:\u00a0It can help reduce production costs by identifying and eliminating inefficiencies in the production process. By optimizing the process, manufacturers can produce more with fewer resources, reducing the cost of production. Improved product quality: Manufacturers can improve the quality of the product. The process can be designed to produce products that meet specific quality standards, resulting in fewer defects and customer complaints. Increased safety :By identifying potential hazards and mitigating them during the design stage, manufacturers can reduce the risk of accidents during production and ensures the safety of workers. Environment Sustainability : Minimize waste and energy consumption and promote the reuse of materials, manufacturers can reduce their carbon footprint and contribute to a more sustainable future. Competitive Advantage : Manufacturers can get a competitive advantage by improving their efficiency, quality, and sustainability. This can help them gain market share and increase profitability. Innovation : Manufacturers can lead to the development of new products\/technologies and processes that are more efficient and sustainable. Chemical Process Design: Creating of manufacturing process in cost effective and safe manner involves several steps including basic engineering package, detailed engineering packages, construction and operation. Process engineers are professional who play a vital role to design a process which can produce high quality products efficiently. Basic Engineering Design Services: Basic Engineering Design (BED) or Front-End Engineering Design (FEED) services is most important engineering design activity for working on any Greenfield or Brownfield projects. BED will establish the specific set of process operating conditions and equipment necessary to achieve the level of reliability, efficiency, and safety required. This design phase sets the direction for the rest of the project. At the completion of this phase, a cost estimate of +40%\/-20% can typically be developed for the project. BED puts great emphasis on the development of the Design Basis at the initiation of design. When the design basis is complete, we typically have the following information defined: Raw material specifications Plant capacity requirements Product specifications Critical plant operating parameters Available utilities specifications Individual unit operations performance requirements Process regulatory requirements All other operating goals and constraints desired by the plant Once the design basis is in place, and agreed upon with the client, process engineer works to create, analyze, and optimize the many aspects of the plant design. The end result is process documentation that clearly defines the process.Typical Process Engineering Deliverables for BED package can include the following or a smaller subset of these items: Process design basis Material & Energy Balance (M&EB) Process Flow Diagrams (PFDs) Process descriptions Utility balances and Utility Flow Diagrams (UFDs) Preliminary Piping & Instrumentation Diagrams (P&IDs) Process control description Preliminary line\/pipe list Preliminary instrument list Process equipment list Preliminary Tie-in list Equipment process datasheets Instrument process datasheets Hydraulic design reports. Case studies on chemical process Let us assume a homogeneous liquid phase non-catalytic reaction. In this reaction two organic raw materials, chemical \u2018A\u2019 and chemical \u2018B\u2019 reacts to form chemical \u2018C\u2019. This is an exothermic reaction and raw material \u2018A\u2019 is limiting reactant. Chemical \u2018B\u2019 consumption is 1.25 times of reactant \u2018A\u2019. Heat of reaction is 150 kcal\/kg of reacted \u2018A\u2019. In this process equilibrium conversion of the reaction is 85% on the mass basis for reactant \u2018A\u2019. This reaction takes place at 85 \u00b0C and atmospheric conditions. Selectivity of the reaction is 95% on mass basis. And remaining 5% of reacted \u2018A\u2019 converts into high boiling tar like material. This residue composition is as below which is sent for incineration. The calorific value for residue is 7500 kcal\/kg approximately. \u00a0 Sr. No. Component Composition (wt%) 1 Chemical A 1% 2 Chemical B 2% 3 Chemical C 2% 4 Heavies 95% Physical and Chemical Properties: For our batch reactor process calculations, we need physical and chemical properties for the chemicals are in below table. Sr. No. Component Normal Boiling Point (\u2103) Heat Capacity (kcal\/kg\u2103) Density (kg\/m3) Heat of Vapourization (kcal\/kg) 1 Chemical A 70 0.35 900 100 2 Chemical B 90 0.35 900 100 3 Chemical C 100 0.35 1000 90 4 Heavies 120 0.35 1000 – Reaction: A (liq.) + B (liq.) \u2014-> C (liq.)\u00a0at 85 \u00b0C and atmospheric pressure Process Flow Diagram (PFD) Here,RM \u2013 Raw Material , CWS \u2013 Cooling Water Supply, CWR \u2013 Cooling Water Return, Cond. \u2013 Steam Condensate Material Balance for the Batch Reactor System This process includes two steps first is reaction and second is batch distillation. The material balance for per batch will be as below. Charge of RM \u2013 A, 2000 kgs\/batch Charge of RM \u2013 B, 2500 kgs\/batch (since B is charged 1.25 times of A) Total mass of in reactor (RM \u2013 A + RM \u2013 B = 4500 kgs\/batch) Equilibrium conversion is 85% hence unreacted RM \u2013 A in crude product = 2000*(100 \u2013 85)\/100 = 300 kg. Unreacted RM \u2013 B in crude will be = 300*1.25 =375 kg. Product C in crude will be (2000 + 2500) *0.85*0.95 = 3633 kg (since selectivity is 95% for the product C.) Heavies\u2019 generation in reaction will be = (2000 + 2500) *0.85*0.05 = 181.7 kg\/batch. Since the composition of heavies in residue is 95% hence residue generation per batch will be = 181.7 *100\/95 = 191.3 kg. Loss of RM \u2013 A in residue will be 191.3 *1\/100 = 1.91 kg\/batch Loss of RM \u2013 B in residue will be 191.3 *2\/100 = 3.83 kg\/batch Loss of Product C in residue will be 191.3 *2\/100 = 3.82 kg\/batch The recovered quantities from<\/p>\n","protected":false},"author":2,"featured_media":2141,"comment_status":"closed","ping_status":"open","sticky":false,"template":"","format":"standard","meta":{"_acf_changed":false,"footnotes":""},"categories":[1],"tags":[],"class_list":["post-2140","post","type-post","status-publish","format-standard","has-post-thumbnail","hentry","category-uncategorized"],"acf":[],"_links":{"self":[{"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/posts\/2140","targetHints":{"allow":["GET"]}}],"collection":[{"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/posts"}],"about":[{"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/types\/post"}],"author":[{"embeddable":true,"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/users\/2"}],"replies":[{"embeddable":true,"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/comments?post=2140"}],"version-history":[{"count":64,"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/posts\/2140\/revisions"}],"predecessor-version":[{"id":2320,"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/posts\/2140\/revisions\/2320"}],"wp:featuredmedia":[{"embeddable":true,"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/media\/2141"}],"wp:attachment":[{"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/media?parent=2140"}],"wp:term":[{"taxonomy":"category","embeddable":true,"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/categories?post=2140"},{"taxonomy":"post_tag","embeddable":true,"href":"https:\/\/instrontechnologies.com\/ca\/wp-json\/wp\/v2\/tags?post=2140"}],"curies":[{"name":"wp","href":"https:\/\/api.w.org\/{rel}","templated":true}]}}