| acid pretreatment |
temperature (°C) |
190 |
(35) |
| |
pressure (atm) |
13 |
(17) |
| |
% solids |
0.42 |
(35) |
| |
acid concentration (% w/w) |
0.0011 |
(35) |
| |
water mass flow (kg/h) |
8480.36 |
estimated |
| |
acid mass flow (kg/h) |
100.6 |
estimated |
| |
NH3 concentration (% w/w) |
1.1 |
(17) |
| |
NH3 mass flow rate (kg/h) |
3.8 |
estimated |
| |
reactions |
(xylan)n + nH2O → nxylose |
(35) |
| |
|
(xylan)n → nfurfural + 2H2O |
|
| |
|
(glucan)m + mH2O → mglucose |
|
| |
|
|
|
| |
|
acetate → acetic acid |
|
| |
|
lignin → soluble lignin |
|
| |
|
H2SO4 + Ca(OH)2 → CaSO4·2H2O |
|
| enzymatic hydrolysis |
reactor temperature (°C) |
45 |
(33) |
| |
reactor pressure (atm) |
1.66 |
(17) |
| |
water supply in the reactor |
22.90 |
estimated |
| |
reactions |
(glucan)m + mH2O → mglucose |
(32) |
| acid-catalyzed dehydration |
temperature reactor 1 (°C) |
210 |
(14) |
| |
temperature reactor 2 (°C) |
180 |
|
| |
pressure reactor 1 (atm) |
24.67 |
|
| |
pressure reactor 2 (atm) |
14.10 |
|
| |
% moisture in the final reactor |
28.76% |
estimated |
| |
reactions |
glucose → 3H2O + HMF |
(5) |
| |
|
xylose → furfural + 3H2O |
|
| |
|
2H2O + HMF → LA + FA |
|
| purification |
equilibrium stages tower 1 |
10 |
estimated |
| |
reflux ratio tower 1 (mass) |
1.5 |
|
| |
distillate rate tower 2 (kg/h) |
5180 |
|
| |
equilibrium stages tower 2 |
10 |
|
| |
reflux ratio tower 2 |
2.5 |
|
| |
distillate rate tower 2 (kg/h) |
170 |
|
