The water-removal duty starts at the pulp feed
An evaporator receives prepared pulp, not whole mangoes. Define the pulp flow and soluble-solids measurement at that inlet, then state the target on the same basis. Fresh-fruit input cannot stand in for evaporator feed because destoning, screening and rejected fruit intervene.
For an initial accounting estimate, feed mass multiplied by feed-solids fraction equals concentrate mass multiplied by target-solids fraction. The difference between the two mass flows is the estimated removed water only when there are no additions, solids losses or inventory changes.
Estimate a mass balance from your own inputs
The calculator below uses your supplied mass flow and comparable solids percentages. It supplies an ideal balance for discussion, rather than a measured trial result, selected evaporator rating or utility estimate. Brix used as a proxy for solids must be suitable for the product and agreed measurement method. Blank inputs have no assumed value.
A mass balance cannot select the heating surface
Viscosity, fibre, temperature, boiling conditions, residence time and fouling affect equipment selection. The existing forced-circulation equipment image does not establish any evaporation rate, final Brix or steam consumption. Provide a representative product specification and utility conditions alongside the balance.
Define the feed buffer and transfer, heating and vacuum scope, condensate and cooling connections, concentrate discharge, cleaning circuit and downstream treatment or packaging. These interfaces remain project-specific.
