Abstract: The present invention relates to the thickening of pulp suspensions. A low consistency pulp suspension is fed to a pre-thickener (10) through an inlet conduit (18). A layer of thickened pulp, formed on a filter surface (22), is pushed along the filter surface by a cleaning member to the discharge end of the pre-thickener and is discharged through the outlet (20). The cleaning member comprises a rotating shaft (30), on which shaft at least one screw thread (32) is fixed so as to leave a free space between the shaft and the screw thread. Essentially non-thickened pulp is allowed to flow through the apparatus via this space.

Abstract: An arrangement is disclosed for supplying an air jet form to the furnace of a recovery boiler, where the furnace has a front wall, a rear wall and side walls. Black liquor spraying devices are disposed on the furnace walls at one or several levels of the furnace. A plurality of air ports are located at several horizontal levels for introducing air into the furnace from an air supply. In the arrangement for the secondary air flows, two horizontal air levels at different elevations are arranged above the lower primary levels and below the black liquor sprayer. Secondary air is supplied from two opposite walls and the air ports from each of the two levels are located so that the air jets are introduced in an interlaced pattern having an even number of jets on one opposite wall and an uneven number of jets on the other opposite wall. The air jets of said at least two air levels are located substantially one above each other in substantially vertical rows.

Abstract: A sealing arrangement is provided between a rotary drum kiln and the stationary end thereof arranged in a material flow relation to each other, having enhanced effectiveness and requiring less maintenance. Pressurized gas, such as air, is fed to the connecting area of the drum and stationary end so that the angle &agr; between the feeding direction of the gas and a plane substantially perpendicular to the center axis of the rotary drum is 90° or less (preferably between about 10-30°). The air flow is directed to the seal in such a way that it prevents leaking of process gas and solid matter dust from the connecting point of the rotary drum and the feed chamber, and so that as little air as possible escapes to the surroundings. Due to the gas flow, the stationary surface and the moving surface substantially do not rub together.

Abstract: A method and system for handling foul condensate containing Hazardous Air Pollutants (HAPs) in a cellulose pulp mill has enhanced energy efficiency and lower cooling water usage, while complying with the Cluster Rules and other environmental regulations. The condensate is fed countercurrently to stripping vapor in the stripping column to produce a HAPs vapor and a clean condensate. Part of the clean condensate is fed from the stripping column reboiler, and the HAPs-rich vapor is directed to the reboiler to at least partially condense while vaporizing the clean condensate into the clean vapor (stripping vapor). The pressure of the stripping vapor is increased, such as utilizing a steam ejector, to about 0.1-30 psig and then is used as the stripping vapor in the stripping column. The non-condensed HAPs-rich vapor is fed to an external condenser, and the dirty condensate from the external condenser and the dirty condensate from the reboiler, are returned to the stripping column.

Abstract: In a method and apparatus for treating pulp, a peroxide treatment of chemical pulp, i.e., both sulphite pulp and kraft pulp, is used to quickly reduce the Kappa number of the pulp. The method involves treating a chemical pulp with at least hydrogen peroxide or its equivalent, the kappa number of which chemical pulp has been brought to a level below 20 by either at least cooking or cooking and delignifying. The pulp is treated in a fast alkaline or neutral peroxide stage (Pk) (e.g. a small reactor having a volume of, or proportional to, less than about 90 cubic meters for 1500 tons per day pulp treatment) to reduce the kappa number by 1-10 units, and preferably by 3-7 kappa units, in which treatment the reaction time is less than 10 minutes, and is preferably less than 5 minutes. The pulp is then transferred substantially without intermediate washing of any type to a bleaching tower, and then bleached further in an acidic bleaching step (e.g. a D or Z step) in the bleaching tower.

Abstract: A method and apparatus for bleaching medium consistency pulp with ozone using at least 2 fluidizing mixers to mix ozone and carrier gas into the pulp. The method is particularly applicable when the volume of the bleaching gas is larger than the volume used in conventional ozone bleaching, e.g. 2 m3/adt.

Abstract: A method and an apparatus for heating or cooling material having poor thermal conductivity, especially medium-consistency fiber suspensions. The material is directed, substantially as a plug flow, at a velocity below 5 m/s (e.g. 0.1-1 m/s) through an apparatus formed by a flow channel provided with heat exchange surfaces. The flow of the material is throttled at a throttling point by a more than 30% reduction in the cross-sectional area of the channel. After throttling, the material is discharged from the throttling point in such a manner that another portion of the material contacts the heat exchange surfaces.

Abstract: A method of cooking pulp in an alkaline batch process (using one or more batch digesters) improves pulp bleachability. The wood material is supplied to the digester; the cellulosic material is pre-treated in the digester with a first liquor, the first liquor is displaced by a second liquor, the displaced first liquor is led to a further treatment, the cellulose material is treated with the second liquor, and the cooked pulp is removed from the digester. The second liquor is displaced as two consecutive parts, i.e. as strong black liquor and weak black liquor, and after cooling in a heat exchanger the strong black liquor thus obtained is fed into the digester as the first liquor in a subsequent batch (in the same, or a different, batch digester).

Abstract: The present invention relates to a method of manufacturing a wire screen product which is especially suitable for screening fiber suspensions of the wood processing industry. It is a characteristic feature of the method according to the invention of manufacturing a wire screen product including screen wires disposed crosswire in relation to a support arranagement that includes at least one support wire, the screen wires and support wire being secured to each other such that, at the first stage, the screen wire is welded by a button spot weld to the support arrangement and, at the second stage, the screen wire is welded at another point to the same support structure.

Abstract: The present invention relates to a cooler (2) for a rotary drum kiln (1). The cooler comprises two cylindrical housings disposed one inside the other (6, 7), surrounding the kiln and rotating with it, which housings are mounted at the discharge end of the kiln concentrically with the kiln and between which housings an annular space (8) is formed. The housings are attached to each other by means of longitudinal radial partition walls (16), and the inner cylindrical housing (6) is attached at its ends to the kiln. The annular space (8) has a feeding inlet (11) communicating with the kiln for leading the hot material from the kiln into the cooler and a discharge outlet for discharging the cooled material. The material to be cooled flows counter-currently in relation to the cooling gas flow.

Abstract: In the treatment of cellulose pulp in connection with bleaching, the pulp is first cooked and, if necessary, oxygen delignified in order to reduce the Kappa number below 24, preferably below 14, and after that the pulp is treated in an acid stage at a pH of 2-5 and at a temperature range of 75-130° C. in order to reduce the Kappa number by 2-9 units. To prevent essential weakening of the strength properties of the pulp in the acid stage treatment tower, the retention time, t min, is 30 to 300 minutes and the treatment temperature, T° C. is Tmin<T<Tmax, in which T min = 10517 24 + ln ⁡ ( 2 ⁢ t ) - 273 and Tmax=Tmin+23° C.

Abstract: Calcium carbonate scaling is inhibited in a multi-stage alkaline waste liquor evaporation plant in a chemical cellulose pulp mill having a bleaching plant. Calcium-containing effluent from the bleaching plant is treated together with alkaline waste liquor in the evaporation plant. A portion of the alkaline waste liquor of the evaporation plant is supplied to the bleaching effluent to increase the carbonate content of the effluent. Then the bleaching effluent is heated to 110-160° C. by direct contact with a heating medium (e.g. steam, or secondary vapor) and maintained in a retention tank for a period of about 1-20 minutes to reduce the amount of dissolved calcium in the effluent. Finally the heat-treated bleaching effluent is evaporated with the alkaline waste liquor in the evaporation plant, with minimized scaling.

Abstract: A method of treating cellulose pulp mill condensates having an MeOH content using an evaporator and a steam stripper having a reboiler, comprising: (a) Collecting a feed liquor stream having at least 50% of the pulp mill MeOH. (b) Feeding the feed liquor stream to the evaporator having at least two heating element sections separated on a motive steam side. (c) Evaporating the liquor in the evaporator to produce a vapor containing at least 40% of the at least 50% of the pulp mill MeOH. (d) Compressing the vapor from (c) to increase the vapor pressure. (e) Using the vapor from (d) as condensing heating media in (c) for the evaporation in a first heating element section of the evaporator and venting a portion of the vapor through the first heating element section. (f) Compressing the vented vapor from the heating elements of the evaporator from (e) to increase the vapor pressure to be used as heating media in the reboiler.

Abstract: The present invention relates to a method and an apparatus for mixing a pulp suspension with a fluid medium. The method and the apparatus according to the invention are particularly advantageous when used for mixing different chemicals, both liquid and gaseous, or steam into pulp suspension in the wood processing industry. In the method and the apparatus according to the invention, the pulp suspension and the fluid medium are fed into a mixer casing, mixed therein and removed from the casing, and a freely rotatable mixing rotor with mixing blades, is placed within the casing and turned by means of incoming flow of pulp suspension being in contact with the mixing blades of the rotor.

Abstract: An alkaline cellulose pulp pulping process treats soap and fiber-containing liquids to separate fibers from the liquids prior to further treatment of the liquids (e.g. by evaporation and combustion, or by cooking to produce tall oil). Black liquor containing soap, and/or washer filtrate containing soap, are fed to one or more soap separating tanks, and then the soap fraction from the top of the tanks is fed to a pressure screen where fiber separation takes place (preferably at a temperature of at least 70.degree. C.). Black liquor may be added to the soap fraction to dilute it, and preferably simultaneously raise its temperature. The pressure screen has a screen surface with holes of 0.4 mm diameter or less, or slots with a width of 0.2 mm or less.

Abstract: A method of displacement washing of cellulose pulp achieves substantially optimal results without the consumption of excessive clean wash liquid. In the practice of the method there is at least one washing stage, and a second stage, including a suction, press, and/or thickening stage, following the washing stage. Cellulose pulp is fed to the washing stage, and then the washed pulp is fed to the second stage. A first filtrate is withdrawn from the second stage and a second filtrate is withdrawn from a washing stage of the at least one washing stage, or the second stage. The first filtrate is directed to the washing stage and the first filtrate is used as washing liquid in the washing stage. For example the washing stage may include a last washing stage in a multi-stage fractionating washer, and the second stage may be in the fractionating washer; and the first filtrate may be directed to the last washing stage of the multi-stage fractionating washer.

Abstract: A method of manufacturing a core, especially a spiral core, from superimposed plies of board produced by winding, gluing, and drying them, is provided. The method is practiced so that the moisture content of at least some of the board plies entering the winding stage differ from each other in order to provide a stepwise moisture structure within the core wall. This decreases unfavorable stresses which are produced in the drying stage if a core is manufactured from plies having equal moisture content.

Abstract: A method of removing nitrogen oxides from flue gases of a cellulose pulp mill recovery boiler does so in a cost effective and environmentally friendly manner. In the heat recovery section of the recovery boiler, a peroxide solution (e.g. a water solution containing about 1-35% hydrogen peroxide) is brought into contact with (e.g. sprayed into) the flue gases in the heat recovery section, so that the flue gases and the peroxide remain in contact between about 0.5-5 (preferably between about 1-2) seconds. The majority (e.g. about 60-90%) of the nitrogen oxides are converted to nitrogen dioxide. The temperature of the flue gases at the time of contact with the peroxide solution is between about 300-800.degree. (preferably 400-600.degree.) C. The nitrogen dioxide is removed by scrubbing the flue gases, downstream of the recovery boiler, with an alkaline liquid (e.g. a liquid otherwise used in the pulp mill having a pH of greater than 9) to convert the majority of the nitrogen dioxides into nitrate.

Abstract: A method of treating pulp and an apparatus for practicing the method are particularly suitable for the bleaching of medium consistency pulp when bleaching stages of varying temperature are used. Chemical pulp is treated in such a way that the pulp is allowed to flow prior to a bleaching reactor, in the reactor itself, and/or after the reactor, at a velocity of less than 5 m/s through an indirect heat exchanger in order to change the pulp temperature more than 5.degree. C., preferably more than 10.degree. C.

Abstract: The present invention is related to a method of determining the amount of gas in a liquid. The method is particularly well suited for determining the amount of both the gas in the form of bubbles and the gas dissolved in pulp, i.e. in various fiber suspensions of paper and pulp industry. The invention is advantageously applied to the control and regulation applications of removal of air in the short circulation of a paper machine.