Translation of "Nachaktivierung" in English

Without any need for reactivation, coconut oil was hydrogenated under the following conditions:

36 g of di-t-butyl peroxide in 387 g of xylene are added for reactivation.

Example 2 is repeated, except that 0.6 g of hydrogen peroxide is used for the subsequent activation.

In the continuous process for post-activation of coconut shell active carbon active carbon and reaction gas are passed in co-flow relationship.

It may be necessary to reactivate the reaction by subsequent addition of small quantities of initiator in order to achieve the required monomer conversion.

In order to increase the abrasion resistance, the activated charcoal can also be impregnated at its surface in a plastic dispersion or a coal tar pitch solution or bitumen solution, and subjected to slight post-activation.

The sensitivity with regard to steam can be significantly reduced by adding ammonia gas during post-activation and cooling to 100° C. with exclusion of air.

It may be necessary to carry out a subsequent activation by subsequent addition of small amounts of initiator in order to achieve the monomer conversion desired.

It may be necessary to carry out a reactivation by subsequent addition of small quantities of initiator in order to achieve the desired monomer conversion.

At a solids concentration of 33%, the reaction mixture is reactivated with a solution of 20 g of ammonium peroxodisulphate in 100 g of water and 20 g of sodium disulphite in 100 g of water.

In conventional polymerization techniques without subsequent activation the residual monomer content is so high that subsequent demonomerization, for example, by steam distillation, is necessary in order to keep the residual monomer content below required limit values and to avoid undesirable odor in use.

It was surprisingly found that the polymerization can be continued to very high conversion and to very low residual monomer content if an oil-soluble, sparingly water-soluble free radical initiator is added for subsequent activation after the polymerization with the water-soluble redox system, and the polymerization is completed therewith.

In polymerization processes without subsequent activation, the residual monomer content is so high that subsequent monomer removal, for example by steam distillation or by passing in a gas stream, is required in order to keep the residual monomer content below required limits and to avoid odour annoyance during use.

The grafting reaction with a water-soluble redox system, such as, for example, hydrogen peroxide and iron(II) sulphate, and the subsequent activation with a sparingly water-soluble organic peroxide, such as tert-butyl hydroperoxide, is therefore particularly preferred.

After the end of the metering, stirring is carried out for a further 15 min at 86° C. and 2 g of tert-butyl hydroperoxide are then added for subsequent activation.

The reaction may have to be reactivated by the subsequent addition of small quantities of initiator to achieve complete conversion of the monomers.

If, in exceptional cases, an inadequate conversion is determined after termination of the reaction and even larger quantities of starting compounds a) and b) are present in the reaction mixture, they may either be removed by distillation or may be reacted by reactivation with the initiator or catalyst and heating to the reaction temperature.

The hydrogenation reaction can be continued without reactivation of the catalyst material and the shaped catalyst elements show uniform activity and selectivity throughout the entire hydrogenation process.

Said layer absorbs in particular the scattered radiation 25 resulting at the striking point 26 and so prevents said scattered radiation from leading to pre- and/or post-activation of the coating material 2 .

If the subsequent capitalization is considered a late partial invoice, this can be mapped using the manual depreciation date.

Note: This setting follows the principle of a subsequent capitalization being considered an actual subsequent acquisition that is placed in operation.

After the end of the metering, stirring was effected for a further 15 min at 86° C. and 2 g of tert-butyl hydroperoxide were then added for reactivation.

After the end of the metering operations, stirring is continued for 45 min at 85° C., after which 15.0 g of a 2% strength aqueous solution of ammonium peroxodisulphate are added for subsequent activation.

If you enter a subsequent capitalization for a fixed asset in the last year of the useful life or after the useful life expired, a system message informs you about the remaining useful life.

The disadvantage is that even the subsequent activation in the reactor necessitates high temperatures in the range from 200 to 400° C. This leads to appreciable extra costs on account of the increased equipment needs (preheater, cycle gas compressor, reactor material, etc.).

Monomer mixture M2 and the aqueous solution W2 were then metered in the course of 240 minutes Immediately after completion of the metered additions of M2 and W2, the aqueous solution W3 for post-activation was metered in the course of 60 minutes, and the dispersion was stirred further for a period of 60 minutes and then cooled.