**7. Final remarks**

584 Heat Exchangers – Basics Design Applications

For more information about the performance and the potential of HPAL plants equipped

Inlet- / Outlet- / Steam temperature °C 185 / 235 / 275 185 / 235 275 

Density slurry kg/m³ 1 340 1 340

 [kJ/(kg K)] kJ/(kg K) 3.6 3.6 Dynamic viscosity cP 50 - 70 10 - 15

Tube velocity slurry m/s 2.0 0.35 Diameter tube mm 38 × 3.0 38 × 3.0 Diameter- / Material particles mm n.a. 4.0 / Titanium Clean- / Design k-value W/(m²·K) ~ 600 / 300 1 500 / 1 500 

values and Eq. (5) m 166.8 5.84

Table 4. Comparison significant parameters for indirect heating of high temperature stage of

Pressure drop bar ~ 6 - 10 < 1.0

Specific heat slurry

Tube length based on design k-

shell equal to 8 m

shell equal to 8 m

HPAL plant of Fig. 25.

Total number of shells in series for 1 pass tube-side and tube length per

Total number of shells in series for 2 pass tube-side and tube length per

**Unit Conventional** 

**shell and tube** 



**Self-cleaning fluidised bed** 

with self-cleaning fluidised bed heat exchangers, one is referred to Ref. [6].

We have given an indication about the cost of fouling of heat exchangers on a global scale and we have shown that the self-cleaning fluidised bed heat exchange technology can play a significant role in battling these fouling cost, and does have even more potential that solving fouling problems only.

Particularly, the latter aspect has caught the attention of an increasing number of very large companies which are very much interested to implement the self-cleaning fluidised heat exchange technology for the upgrading of their existing proprietary processes, or even for the development of completely new processes.
