Detailed design of Filtration unit to purify crude glycerol to pure glycerol for use in glycerol steam reforming process
Abstract
The design project’s goal is to design a plant capable of producing hydrogen sustainably at an industrial scale. After preliminary design the plant designed was split into sections for which was split between the members tasked to conclude this design, for which each member is to produce a detailed design of their section.
The detailed design in this report concludes a safe and efficient design for the filtration unit to be used as part of the purification process used to convert the crude glycerol feed to pure glycerol to be used in the glycerol steam reforming process to form the required hydrogen. Due to the coupled and interlinked nature of the design parameters of the filtration unit the theory and design equations are outlined prior to an application of an optimisation algorithm to determine the optimum design parameters. Furthermore, as due to the fact that parameters are present that are to be determined experimentally, a summary of the experimental procedures and theory needed to determine these parameters are outlined, in addition to the equations and assumption used to determine the values theoretically.
In addition, a control and safety instrumented system was developed to conserve optimum and efficient operation as well as the capability to adapt to changes in conditions and production rate as well as safeguard safe operation.
Table of Contents
1.3 Filter press type selection
2 Detailed design and optimisation of filtration unit
2.1 Particle size distribution
2.2 Fixed and known parameters
2.3 Reynold Number and flow regime
2.5 Determining specific cake resistance and filter medium resistance
2.9 Capital and operating costs formulas
2.10 Optimisation of filtration unit
2.12 Summary of operating parameters
3 Assumptions made during detailed design and optimisation
3.1 Management of solids output assumptions
4.3 Summary of final estimated costing
5 Mechanical Engineering design
5.3 Dimensions of filter press and summary of mechanical design
8 Control systems and manning requirements
8.1 Operation Control system design
8.2 Sensitivity studies and relationship to control system
11 P & ID diagram with outline of additions to system
Nomenclature
| Ri | Percentage retained in the sieve with opening size i | % | ki | The permeability of i | m2 |
| WS,i | The mass of solids present in the sieve with opening size i | kg | Lc | The thickness of the filter cake | M |
| WT | The total mass of solids placed at the start in the top sieve screen | kg | Lm | The filter medium thicknes | M |
| Dp | Average particle diameter | µm | kc | thefilter cake permeability | m2 |
| dpavg | The average particle diameter for the solids present in the slurry | µm | km | The filter medium permeability | m2 |
| μ | The viscosity of the liquid phase of the feed and the filtrate | Pa.s | V | The volume of filtrate output from the filter media | m3 |
| pvap | Vapour pressure of liquids in feed | Pa | t | the period of time the filtrate was collected in | s |
| Re | Reynold number for flow through a packed bed | dVdt | The filtration rate | m3 s-1 | |
| ρs | Average density of the dry solids | kg m-3 | Rm | Filter medium’s resistance | m-1 |
| ρl | Average density of the liquids in the slurry | kg m-3 | Rc | Filter cake’s resistance | m-1 |
| dpse | The equivalent spherical diameter | µm | α | Specific cake resistance | mkg-1 |
| εb | The porosity of the bed | W | Mass of the filter cake | kg | |
| ρ | The density of the fluid flowing through the packed bed | kg m-3 | C | The mass of solids per unit volume of filtrate | kgm-3 |
| us | The superficial velocity | m s-1 | αo |
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