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User talk:Yazbo91
From 2011.igem.org
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[[User:Allancrossman|Allancrossman]] 16:38, 9 September 2011 (CDT) | [[User:Allancrossman|Allancrossman]] 16:38, 9 September 2011 (CDT) | ||
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|Pre-treatment reactor | |Pre-treatment reactor | ||
| - | |Capacity:8 m<sup>3, 140 C, 20 bar | + | |Capacity:8 m<sup>3</sup>, 140 C, 20 bar |
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|R-2 | |R-2 | ||
Revision as of 17:08, 12 September 2011
Yassen's talk page
Oh hai.
Some comments:
- When you define steady state as meaning 99% of the cellulose is used up, it becomes unclear what it means for cellobiose or glucose.
- You say Figure 3 shows cellobiose doesn't reach a steady state. But it goes to zero. If you mean it goes negative, you'll have to replot the graph to show that...
- You say "Analysing steady state is important to find out whether a system accumulates excess mass or energy" - but we know it can't in reality, right, since this violates physics? Do you mean analysing steady state is important as a way of testing if the model is sane?
Allancrossman 16:38, 9 September 2011 (CDT)
Tables
| Equipment | Size (m3) | Cost constant (£) | Index | Purchase cost (£) | Number required | Total cost (£) |
|---|---|---|---|---|---|---|
| Boiler | 8 | 70 | 0.8 | 13,218.33 | 4 | 52,873.31 |
| Reactor 1 | 4 | 18,5000 | 0.45 | 47,158.74 | 1 | 47,158.74 |
| Reactor 2 | 4 | 18,500 | 0.45 | 34,522.22 | 1 | 34,522.22 |
| Reactor 3 | 4 | 18,500 | 0.45 | 34,522.22 | 1 | 34,522.22 |
| Reactor 4 | 4 | 18,500 | 0.45 | 34,522.22 | 1 | 34,522.22 |
| Reactor 5 | 4 | 18,500 | 0.45 | 34,522.22 | 1 | 34,522.22 |
| Reactor 6 | 4 | 18,500 | 0.45 | 34,522.22 | 1 | 34,522.22 |
| Tank 100-102 | 3.3 | 1,400 | 0.55 | 2,699.67 | 3 | 8099.01 |
| Tank 103 | 93.2 | 1,400 | 0.55 | 16,955.35 | 1 | 16,955.35 |
| Tank 104 | 40 | 1,400 | 0.55 | 10,647.83 | 1 | 10,647.83 |
| Tank 105 | 147 | 1,400 | 0.55 | 21,784.75 | 1 | 21,784.75 |
| Tank 106 | 17 | 1,400 | 0.55 | 6,650.82 | 1 | 6,650.82 |
| Factorial number | Item | Factor |
|---|---|---|
| f1 | Equipment erection | 0.45 |
| f2 | Piping | 0.45 |
| f3 | Instrumentation | 0.15 |
| f4 | Electrical | 0.1 |
| f5 | Buildings, process | 0.1 |
| f6 | Ancillary buildings | 0.2 |
| colspan="2" | Total = 1.45 | |
| f10 | Design and Engineering | 0.25 |
| f11 | Contractor’s Fee | 0.05 |
| f12 | Contingency | 0.1 |
| colspan="2" | Total = 0.4 |
| Type | Amount | Unit price | Cost |
|---|---|---|---|
| Steam | 200 kg/h | £7/t | £9811.2 |
| Cooling water | 3,000 kg/h | 1.5p/t | £315.36 |
| Power | 100 kwh/d | 1.2p/mj | £43,200 |
| Equipment number | Equipment name | Comment |
|---|---|---|
| Tank 100,101,102 | Feed storage tanks | Capacity: 3.3 m3 |
| Tank 103 | Product storage tank | Capacity: 93.2 m3 |
| Tank 104 | Product storage tank | Capacity: 40 m3 |
| Tank 105 | Product storage tank | Capacity: 147 m3 |
| Tank 106 | Product storage tank | Capacity: 17 m3 |
| R-1 | Pre-treatment reactor | Capacity:8 m3, 140 C, 20 bar |
| R-2 | Thermal depolymerisation of hemicellulose | Capacity: 4 m3 |
| R-3 | Hydrous pyrolysis of lignin | Capacity: 4 m3 |
| R-4 | Degradation of cellulose | Capacity: 4 m3 |
| R-5 | Conversion of glucose to sorbitol | Capacity: 4 m3 |
| R-6 | Conversion of glucose to fructose syrup | Capacity 4 m3 |
| P-1, P-2 | Pumps | |
| D-1 | Recovery column | 1 bar |
| HE-1, 2, 3, 4 | Heat exchangers | |
| LI-1, 2, 3, 4, 5, 6, 7, 8, 9 | Level indicators | PID control |
| TI-1, 2, 3, 4, 5, 6 | Temperature indicators | PID control |
| FI-1 to FI-15 | Flow indicators | PID control |
| V-1, 2, 3, 6, 7, 8 | Mixing valve | |
| V-4, 5 | Angle valve | |
| V-9 to V-42 | Gate valve | |
End of tables.
