User talk:Yazbo91

From 2011.igem.org

(Difference between revisions)
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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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----
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==Tables for Yassen==
 +
 +
{| class="wikitable centredtext"
 +
|-
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!Equipment
 +
!Size (m<sup>3</sup>)
 +
!Cost constant (&pound;)
 +
!Index
 +
!Purchase cost (&pound;)
 +
!Number required
 +
!Total cost (&pound;)
 +
|-
 +
|Boiler
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|8
 +
|70
 +
|0.8
 +
|13,218.33
 +
|4
 +
|52,873.31
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|-
 +
|Reactor 1
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|4
 +
|18,5000
 +
|0.45
 +
|47,158.74
 +
|1
 +
|47,158.74
 +
|-
 +
|Reactor 2
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|4
 +
|18,500
 +
|0.45
 +
|34,522.22
 +
|1
 +
|34,522.22
 +
|-
 +
|Reactor 3
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|4
 +
|18,500
 +
|0.45
 +
|34,522.22
 +
|1
 +
|34,522.22
 +
|-
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|Reactor 4
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|4
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|18,500
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|0.45
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|34,522.22
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|1
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|34,522.22
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|-
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|Reactor 5
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|4
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|18,500
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|0.45
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|34,522.22
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|1
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|34,522.22
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|-
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|Reactor 6
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|4
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|18,500
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|0.45
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|34,522.22
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|1
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|34,522.22
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|-
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|Tank 100-102
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|3.3
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|1,400
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|0.55
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|2,699.67
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|3
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|8099.01
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|-
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|Tank 103
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|93.2
 +
|1,400
 +
|0.55
 +
|16,955.35
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|1
 +
|16,955.35
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|-
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|Tank 104
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|40
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|1,400
 +
|0.55
 +
|10,647.83
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|1
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|10,647.83
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|-
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|Tank 105
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|147
 +
|1,400
 +
|0.55
 +
|21,784.75
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|1
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|21,784.75
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|-
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|Tank 106
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|17
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|1,400
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|0.55
 +
|6,650.82
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|1
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|6,650.82
 +
|}
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 +
{| class="wikitable centredtext"
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|-
 +
!Factorial number
 +
!Item
 +
!Factor
 +
|-
 +
|f1
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|Equipment erection
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|0.45
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|-
 +
|f2
 +
|Piping
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|0.45
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|-
 +
|f3
 +
|Instrumentation
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|0.15
 +
|-
 +
|f4
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|Electrical
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|0.1
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|-
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|f5
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|Buildings, process
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|0.1
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|-
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|f6
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|Ancillary buildings
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|0.2
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|-
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|colspan="2"
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|'''Total = 1.45'''
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|-
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|f10
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|Design and Engineering
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|0.25
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|-
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|f11
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|Contractor’s Fee
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|0.05
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|-
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|f12
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|Contingency
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|0.1
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|-
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|colspan="2"
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|'''Total = 0.4'''
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|}
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 +
{| class="wikitable centredtext"
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|-
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!Type
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!Amount
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!Unit price
 +
!Cost
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|-
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|Steam
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|200 kg/h
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|&pound;7/t
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|&pound;9811.2
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|-
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|Cooling water
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|3,000 kg/h
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|1.5p/t
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|&pound;315.36
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|-
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|Power
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|100 kwh/d
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|1.2p/mj
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|&pound;43,200
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|}
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{| class="wikitable centredtext"
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|-
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!Equipment number
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!Equipment name
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!Comment
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|-
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|Tank 100,101,102
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|Feed storage tanks
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|Capacity: 3.3 m<sup>3</sup>
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|-
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|Tank 103
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|Product storage tank
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|Capacity: 93.2 m<sup>3</sup>
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|-
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|Tank 104
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|Product storage tank
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|Capacity: 40 m<sup>3</sup>
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|-
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|Tank 105
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|Product storage tank
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|Capacity: 147 m<sup>3</sup>
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|-
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|Tank 106
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|Product storage tank
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|Capacity: 17 m<sup>3</sup>
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|-
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|colspan="3"|&nbsp;
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|-
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|R-1
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|Pre-treatment reactor
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|Capacity:8 m<sup>3, 140 C, 20 bar
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|-
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|R-2
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|Thermal depolymerisation of hemicellulose
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|Capacity: 4 m<sup>3</sup>
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|-
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|R-3
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|Hydrous pyrolysis of lignin
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|Capacity: 4 m<sup>3</sup>
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|-
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|R-4
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|Degradation of cellulose
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|Capacity: 4 m<sup>3</sup>
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|-
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|R-5
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|Conversion of glucose to sorbitol
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|Capacity: 4 m<sup>3</sup>
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|-
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|R-6
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|Conversion of glucose to fructose syrup
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|Capacity 4 m<sup>3</sup>
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|-
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|P-1, P-2
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|Pumps
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|
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|-
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|D-1
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|Recovery column
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|1 bar
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|-
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|HE-1, 2, 3, 4
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|Heat exchangers
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|
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|-
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|LI-1, 2, 3, 4, 5, 6, 7, 8, 9
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|Level indicators
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|PID control
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|-
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|TI-1, 2, 3, 4, 5, 6
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|Temperature indicators
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|PID control
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|-
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|FI-1 to FI-15
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|Flow indicators
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|PID control
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|-
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|V-1, 2, 3, 6, 7, 8
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|Mixing valve
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|
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|-
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|V-4, 5
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|Angle valve
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|
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|-
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|V-9 to V-42
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|Gate valve
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|
 +
|}

Revision as of 17:03, 12 September 2011

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 for Yassen

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
Retrieved from "http://2011.igem.org/User_talk:Yazbo91"