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Forced Circulation Evaporators

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8.0 Experimental Results
Basis: 1kg= 1L
8.1 DRY RUN Steam pressure(psig) | 42 | Steam condensate(kg/s) | 0.00083 |
Table (8.1):Experimental data obtained from dry run
Table(): shows the mass of steam condensed per second at 42 psig obtained during the dry run (no recirculating liquor) these data along with the latent heat of vaporisation were used to calculate the rate of heat loss from the calandria.
Heat loss calculation
Time taken to fill 250ml for 5minutes=300seconds
Sd=0.25/300=0.00083L/s = 0.00083Kg/s
42psig=3.89bar
Calculation
42psig=(42/14.5)+1=3.89bar
Latent heat of vaporisation at 3.89bar =2141.79kj/kg
Qlost=0.00083*2141.79= 1.785KJ/s

Subsequent runs with recirculating liquor Parameter measured | Run 1 | Run 2 | Run 3 | Run 4 | W(L/s) | 0.89 | 0.89 | 1.25 | 0.89 | S (L/s) | 0.014 | 0.014 | 0.013 | 0.0097 | R(L/min) | 100.5 | 65.5 | 55.5 | 55.5 | V(L/s) | 0.01 | 0.01 | 0.00894 | 0.0076 | Pressure (psig) | 42 | 42 | 42 | 30 | T1 0C | 11.4 | 11.3 | 11.1 | 11.2 | T2 0C | 19.4 | 18.7 | 15.2 | 15.5 | T3 0C | 100.2 | 100.3 | 90.7 | 99.4 | T5 0C | 100.1 | 98.3 | 90.3 | 96.9 | T6 0C | 101.7 | 101.6 | 93.7 | 100.5 | T7 0C | 19 | 19.3 | 17.2 | 17.9 |
Table (8.2):Experimental data obtained from runs with recirculating liquor.

Symbol | Parameters represented | T1 | Cooling water inlet | T2 | Cooling water outlet | T3 | Vapour | T5 | Weak liquor inlet | T6 | Liquor Calandria inlet | T7 | Liquor Calandria outlet | W | Cooling water | S | Steam condensate | R | Recirculating liquor | V | Vapour condensate | | |
Table: Table (8.3)showing symbols and their meanings

Heat balance:
Two heat balances were conducted, one on the condenser and the other on the calandria.
Heat balance on the calandria: The heat balance on the calandria carried out is an indirect method of validation to assess instrument reliability. The table below shows the heat supplied to the system taking into account heat loss (Q1) and the heat supplied to the recirculating liquor (Q2). The two quantities were calculated independently and compared. Heat balance parameters | | Run | | | | | Dry | 1 | 2 | 3 | 4 | Q1=S x λs-Qloss | 1.785 | 28.1148 | 28.1148 | 25.9791 | 19.18 | Q2=R x Cp(T6-T5) | - | 33.7814 | 37.65 | 34.49 | 31.0794 | Discrepancy | - | 5.6666 | 9.5352 | 8.5109 | 11.8994 | % Discrepancy | - | 16.77 | 25 | 24.6 | 38 |
Table (8.4)
Heat balance on the condenser: The table below shows the balance between the heat given by the vapour being condensed (Q3) and the rate of heat removal by the cooling water (Q4). Heat balance parameters | | Run | | | | 1 | 2 | 3 | 4 | Q3=VλT3 | 22.5638 | 22.5387 | 20.395 | 17.1646 | Q4=WCp(T2-T1) | 29.7616 | 27.52948 | 21.4225 | 15.996 | Discrepancy | 7.1978 | 4.9908 | 1.0275 | 1.1686 | % Discrepancy | 24.18 | 18.13 | 4.79 | 6.8 |
Table 8.5
All heat balance calculations are sown in the appendix.

Overall Heat transfer co-efficient Calculation Heat balance | Unit | | Run | | | Tsteam=142.618 | 0C | 1 | 2 | 3 | 4 | Θ1 (Ts-T5) | 0C | 42.518 | 41.018 | 52.318 | 37.3 | Θ2 (TS-T6) | 0C | 40.918 | 44.318 | 48.918 | 33.7 | ΘLM | 0C | 41.712 | 42.646 | 50.5 | 35.47 | Area of HE | M2 | 0.3922 | 0.3922 | 0.3922 | 0.3922 | U | KW/m20C | 1.727 | 1.689 | 1.426 | 1.39 |
Table 8.6: shows the parameters used in calculation of the overall heat transfer coeffiecients and the calculated values. The temperature of steam was constant and the curve surface area of the calandria was used. An example of the calculation is involved in the appendix.

Graph(8.1) showing the relationship between Overall heat transfer coefficient and Recirculating liquor

Graph(8.2) showing the effect of varying recirculating liquor rate on rate of evaporation

Discussion
Heat balance (Calandra)
Referring to table 8.4 , showing the results of the heat balance conducted on four different runs, varying the pressure of the last run and varying the recirculation liquor flowrate of the first three runs. A trend along the discrepancies can be observed ,as the recirculation rate was decreased there was a negative correlation in the discrepancies. Large discrepancies as in run 4 are due to a higher number of factors such as human errors, during time measurement , also the water pressure from the pipe overfilled the cylinders which served as a source of error in taking an accurate time measurement.

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