Abstract:
A process control method for adjusting chemical application in response to the pulp brightness and/or lignin content is realized by utilizing a coupled control feedforward, feedback or combination feedforward/feedback control system, wherein brightness measurements are made between successive lignin content measurements and adjustments made to the chemical application in response to a comparison value.
Abstract:
The present invention relates to a method of and an apparatus for bleaching pulp. The method and apparatus in accordance with the invention are especially suitable for bleaching pulp with ozone at medium consistency, in other words when the consistency is 5 - 25 %, preferably 10 - 15 %. It is characteristic of the invention that ozone is mixed into the pulp to be bleached by means of two fluidizing mixers (14 and 16) and that the foamy suspension of gas and pulp thus obtained is discharged to a reaction vessel (30), in which the suspension is mixed, for example, by a paddle mixer.
Abstract:
A method for reprocessing an ozone-containing gas present in a pulp bleaching plant comprising the steps of supplying the ozone-containing gas to a scrubber and reducing the ozone concentration of the gas as the gas flows through the scrubber. The step of reducing comprises the steps of supplying an alkaline medium to the scrubber and flowing the ozone-containing gas in countercurrent relationship with the alkaline medium within the scrubber so as to provide intimate contact between the ozone-containing gas and the alkaline medium, thereby converting the ozone-containing gas into a substantially ozone-free gas. The alkaline medium may comprise one of the following: a sodium hydroxide solution; white liquor; post oxygen stage filtrate; weak black liquor; or filtrate from an Eo stage of the pulp bleaching plant. The method further comprises the step of separately discharging the ozone-containing gas and the alkaline medium from the scrubber. The ozone-containing gas may comprise an off-gas, which has been partially reacted with a pulp within a pulp bleaching stage or alternatively may comprise fresh bleaching gas, having an ozone concentration ranging from about 6 % to about 14 % by weight within a carrier gas, with the fresh bleaching gas being supplied directly from an ozone generator to the scrubber.
Abstract:
A process for bleaching pulp by impregnating the pulp with an aqueous organic solvent medium and then bleaching in an ozone stage (Z stage) to form a bleached pulp characterized in that organic solvent in the organic solvent medium accompanying the pulp through the ozone stage is stripped from the bleached pulp leaving the ozone stage and the separated organic solvent is recovered for reuse.
Abstract:
A process for delignifying and bleaching a lignocellulosic material (2) without the use of elemental chlorine or chlorine-containing compounds by forming (4) a pulp, oxygen delignifying (40) the pulp and thereafter further delignifying the oxygen delignified pulp by lifting, displacing and tossing the pulp in a radial direction while advancing it in an axial direction in a plug fow-like manner with an effective amount of ozone (88) for a sufficient time to obtain a substantially delignified pulp having a GE brightness of at least about 35 %. The substantially delignified pulp may then be brightened to a final product by treating the pulp with a brightening stage peroxide compound, followed by subsequently treating the pulp at low to medium consistency with ozone.
Abstract:
A method for controlling the gas recycle loop of an ozone bleaching process wherein an ozone generator (18) produces an ozone containing gas from an oxygen containing feed gas (74) and delivers the ozone containing feed gas to an ozone reactor (22) at a variable flow rate responsive to reactor demand. Pulp (20) is bleached with the ozone containing gas, thereby producing an exhaust gas (38) having a flow rate that varies in response to the flow rate of the ozone gas delivered to the ozone reactor. The exhaust gas (38) is then recovered and its flow rate is modified within the recycle loop so that an amount equivalent to reactor ozone demand is returned to the ozone generator. The oxygen content of the oxygen containing feed gas is monitored at or near the inlet of the ozone generator and an amount of fresh oxygen is supplied to the oxygen containing feed gas (74) to obtain a predetermined level of oxygen therein.
Abstract:
A process for delignifying and bleaching a lignocellulosic pulp without the use of elemental chlorine or chlorine-containing compounds by oxygen delignifying (40) the pulp to a K No. of about 10 or less, a viscosity of greater than about 12 cps and a GEB of about 33-43; and thereafter further delignifying (78) the partially delignified pulp by lifting, displacing and tossing the pulp in a radial direction while advancing it in an axial direction in a plug flow-like manner with an effective amount of ozone (88) for a sufficient time to obtain a substantially delignified pulp having a K No. of about 5 or less, a viscosity of at least about 9-10 cps and a GE brightness of at least about 59. The substantially delignified pulp (102) may then be brightened to a final product having a GE brightness of at least about 75, or alternately up to about 83+ by contacting the ozonated pulp with a sufficient amount of a peroxide compound for a time of up to about three hours, with optional mixing of the pulp/peroxide mixture.
Abstract:
The present invention relates to a method of bleaching lignocellulosic fiber material in a combination step with ozone and peracid, such as peracetic acid, ZHCPaaMC. The invention preferably relates to the bleaching of sulphate pulp. The pulp is ozone treated in a HC step in an ozone reactor, whereafter the pulp is diluted with water or white water, and peracid is added prior to an MC bleaching tower with subsequent washing.
Abstract:
A method for ozone bleaching unbleached chemical paper pulp in a single ozone stage and in the presence of a tertiary alcohol including four to eight carbon atoms which is fed into the reaction medium at a temperature of - 5 DEG C to 80 DEG C prior to the actual ozone treatment stage, whereby the gas-liquid transfer, the exchange potentiality, the lignin oxidation selectivity and the ozone efficiency are improved, and the consitency of the treated pulp undergoing ozone treatment is between 6 and 60 %.
Abstract:
Kraft pulp is bleached to an acceptable brightness (e.g. 86 ISO or more) without using chlorinated organic compounds, yet the strength of the produced pulp remains commercially acceptable. In the manufacture of pulp, the pulp which is cooked and oxygen delignified to a kappa number of 14 or less, and then is bleached with ozone at a medium consistency. After the ozone treatment, heavy metals are removed from the pulp, and then the pulp is led to oxygen and/or peroxide treatment, which is followed by a second ozone bleaching stage. The sequence (ZT) (EOP) (ZP) is preferred.