Cost Acid Dilutable Concentrate

Dai rv Mi 1kstone Remover Low Cost Acid Dilutable Concentrate 

Appearance Clear, water-white liquid Procedure  

To mixing vessel, charge the water and start agitation. 

Slowly charge the Phosphoric Acid to avoid splattering. Cool to room temperature and charge the Gluconic Acid and Avanel S-70. 

A lower cost substitute for PPG/Mazers CD-101 dairy cleaner formulation. It retains the general performance attributes of the original formulation. 

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The dilute sulfuric acid is drained from the chambers it contains 60 to 65% H2S04. This acid is normally used at this concentration. Although there are several inconvenient and somewhat costly processes for concentrating the lead-chamber acid, it is difficult to concentrate this product economically in view of the ease with which concentrated sulfuric acid may be produced directly by the contact process. 

Hydrolysis of cellulose have been carried out by two approaches, ie, acid hydrolysis and enzymatic hydrolysis. Concentrated acid was used to dissociate the biomass completely but is not widely used nowadays due to high operation costs, acid recovery, equipment corrosion, and decomposition of product sugars. Diluted acid is a strategy applied in pretreatment, but it also requires proper equipment and can produce growth-inhibiting components, such as furfural and hydroxymethylfurfural (HMF). 

The product is of lower purity than the phosphoric acid produced by the thermal process described below, but this costs about three times as much to produce. The gypsum (calcium sulfate), is a by-product that is widely used in the building industry as a low cost, fire-retardant wall board. After filtration, the dilute phosphoric acid is concentrated by evaporation to a rather dark impure brownish liquid, which is suitable for use in fertilizer manufacture. 

The reconcentration of dilute (50—60%) sulfuric acid is one of the more costly operations in the manufacture of ethanol by this process. An acid reboiler, followed by a two-stage vacuum evaporation system, raises acid concentration to about 90%. The 90% acid is then brought to 96—98% strength by fortification with 103% oleum (fuming sulfuric acid). 

Because of its high cost gold is rarely used as a material of construction. It is highly resistant to attack by dilute nitric acid and hot concentrated sulphuric acid, but is dissolved by aqua regia (a mixture of concentrated nitric and sulphuric acids). It is attacked by chlorine and bromine, and forms an amalgam with mercury. 

Recycling metal ions is part of the concentration process noted above. It can typically be achieved by treatment of the sorbed metals with dilute nitric acid. This is a strong acid, and the nitrate ion is not a strongly coordinating anion. In addition, recycling can be a useful means of paying for the removal process. Tkn example of this was a laboratory bench-scale experiment to treat water from the Berkley Pit, recycle the copper and sell the copper to help pay the processing costs. The Berkley Pit [11] was once an open pit copper mine that was opened in 1955 and closed in 1982. 

Despite the high reactivity and the low cost of the reagents, the use of sulfuric acid is however connected with some disadvantages. First of all, because it captures all the water liberated, it cannot be recycled directly without a high temperature dehydrating step (sulfuric concentration SC). If no SC is operated, the outcoming aqueous sulfuric acid has to be neutralized and produces highly salty effluents, non desirable for the environment. Furthermore, dilute sulfuric acid can produce severe corrosion problems of the reaction vessels. 

Anodes. There are two types of anodes soluble and insoluble. Most electroplating baths use one or the other specifically however, a few baths use either or both. Chromic acid plating baths use insoluble anodes alkaline zinc cyanide baths use both noncyanide alkaline zincs may use either. Soluble anodes are designed to dissolve efficiendy with current flow and preferably, not to dissolve when the system is idle. A plating solution having the anode efficiency close to the cathode efficiency provides a balanced process that has fewer control problems and is less cosdy. If the anode efficiency is much greater than the cathode efficiency and there are only small solution losses, the dissolved metal concentration rises until at some time the bath has to be diluted back or the excess metal has to be reduced by some other means. If the anode efficiency is less than the cathode efficiency, the dissolved metal decreases, pH decreases, and eventually metal salt additions and other solution corrections are required. Based on the cost of metal, it is usually considerably more economical to plate from the anode rather than add metal salt. Copper cyanide, for example, costs about twice as much to add than to dissolve a comparable amount of copper anode. Additionally, the anion added with the metal salt may build up in the plating solution. 

Experimental results for carbonic acid pretreatment have been generated at low solids concentration (6,8,9), but no data are available for pretreatment conversions at higher solids concentrations, as are available for dilute H2S04. The equipment costs for carbonic acid pretreatment were calculated for different solids concentrations (Fig. 2), and it canbe seen that equipment costs are highly sensitive to solids concentration. For comparison to the dilute-acid system, a high reactor solids concentration of 40% was chosen to enable direct comparison with the NREF model. 

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