Abstract: The strength properties of chemical cellulose pulp (particularly kraft pulp) are improved by substituting a cold impregnation soak for conventional impregnation procedures. After steaming, wood chips are soaked in an alkaline liquid at a temperature of about 80-110° C. (preferably 80-100° C., or 90-105° C.) for between one-half-72 hours (typically about 2-4 hours) at a pressure of about 0-15 bar (preferably about 1-5 bar), to dissolve at least about 8% of the wood (preferably about 10-20%) and at least about 15% of the lignin. The alkaline liquid used preferably contains sulfide (e.g. black liquor, green liquor, white liquor, or mixtures thereof), but almost any alkaline liquid having an alkali concentration of about 1.0 mole of NaOH/liter or less (typically about 0.75 m/l or less) is suitable. The wood chips are then raised to a cooking temperature of about 145-180° C. and cooked to produce the cellulose chemical pulp.

Abstract: The sulfide ion concentration and sulfidity of kraft cooking liquor during kraft cooking of cellulose pulp is selectively increased. After treatment in a first treatment zone in which impregnation or kraft cooking takes place using a kraft cooking liquor having a first sulfide ion concentration and sulfidity, black liquor is extracted from the material, liquid is withdrawn from the material and dilution liquid is added to the withdrawn liquid and the withdrawn liquid with dilution liquid is reintroduced. In a second treatment zone after the first zone a second kraft cooking liquor is introduced having a second sulfide ion concentration and sulfidity greater than the first sulfide ion concentration and sulfidity (typically by about 20-50%), including by manipulating controlling the flow rate of extraction and the flow rates of withdrawal of liquid and addition of dilution liquid.

Abstract: An ozone generator has one or both of the tube type electrodes coated with a dielectric that has high dielectric strength, high dielectric constant, and low piezoelectric activity, and can be applied with a small thickness (less than 0.5 mm). The dielectric has a mixed oxide composition having a dielectric strength of at least about 800 volts/mil, has a dielectric constant that is at least 200, and has low enough piezoelectric activity that it will not ablate, crack, or other otherwise suffer damage as a result of high voltage application over months of use. A metal electrode for use in an ozone generator has a dielectric coating on a surface thereof having a composition comprising: about 30-70% lead oxide, about 2-8% barium oxide, about 2-12% lanthanum oxide, about 3-18% titanium dioxide, about 12-40% zirconium dioxide, and trace materials.

Abstract: Kraft pulp of increased strength and bleachability may be produced with decreased consumption of effective alkali, and at a lower H factor, by keeping the dissolved organic material (DOM) concentration low substantially through the entire kraft cook, including by extracting high DOM liquid from at least one part of a continuous digester and replacing it with much lower level DOM liquid. Existing pulp mills having two-vessel hydraulic, one-vessel hydraulic, or other systems may be retrofit to provide for extractions and additions of low DOM dilution liquor (including substantially DOM-free white liquor). Also, commercial size batch digesters (8 tons per day of pulp or more) can be operated with low DOM liquor to produce increased strength pulp. Using dilution with low DOM liquor also results in reduced H factor and effective alkali consumption, and increased bleachability.

Abstract: Ozone is generated from an oxygen-containing gas utilizing a tube-type ozone generator at significantly greater power efficiency. The oxygen is introduced into the annular passageway between the electrodes of the tube-type ozone generator at an angle (e.g. about 45.degree.-90.degree.) so that it swirls in a cyclonic flow path as it travels from one end of the annular passageway to the other. The amount of power consumed to produce a gas having about 8% ozone is roughly half of the power needed if the same conditions are applied but the oxygen gas is introduced conventionally (without swirling action, so that it travels along the dimension of elongation of the passageway). The swirling action also allows a higher concentration of ozone (e.g. 10% or more) to be achieved in the product gas compared to the same conditions when no swirling is employed.

Abstract: The removal of bleaching chemical-consuming metals from treatment fluids in a cellulose pulp mill is facilitated by treating the pulp in an acidic or neutral stage to dissolve metals, washing or thickening the pulp to produce a filtrate containing dissolved metals, and then using an alkali liquid to adjust the pH of the filtrate to cause dissolved metals to precipitate. The alkali liquid is pretreated with carbon dioxide to reduce the sulfide content and increase the carbonate content thereof, preferred alkali liquids being green liquor and white liquor. The reduced-metal content filtrate is used in the bleach plant of the pulp mill, to make bleaching chemicals, as a wash liquid, etc. Treatment of the alkali liquid with carbon dioxide is typically practiced by scrubbing the liquor with carbon dioxide gas, for example, using a plate column scrubber or a stationary packing scrubber.

Abstract: A chip bin construction, ideally suited for bins having a maximum diameter of twelve feet or more, uniformly discharges chips, after steaming, without the necessity of a vibratory discharge. A hollow transition portion is provided between a hollow substantially right circular cylindrical main body and a rectangular discharge. The hollow transition may have a substantially circular cross-section open top and a substantially rectangular cross-section open bottom and opposite non-vertical gradually tapering side walls. At least one feed screw may be mounted at the open bottom of the transition for cooperation with the discharge, and the feed screw(s)--or the equivalent--may provide for metering of the chips. Alternatively, the hollow transition portion may provide one dimensional convergence and side relief, and no screw feeders need be provided, in which case a conventional chip meter is used.

Abstract: Kraft pulp of increased strength (e.g. at least about 15% greater tear strength at a specified tensile for fully refined pulp, and as much as about 27%) is produced by keeping the dissolved organic material (DOM) concentration below about 100 g/l (e.g. <50 g/l) throughout substantially the entire kraft cook. This may be done by extracting liquor containing a level of DOM substantial enough to adversely affect pulp strength, and replacing some or all of the extracted liquor with liquor containing a substantially lower effective DOM level than the extracted liquor, so as to positively affect pulp strength. The replacement liquor may be water, white liquor, pressure heat treated black liquor, washer filtrate, cold blow filtrate, or combinations, or the extracted liquor can be treated to remove or passivate the DOM (e.g. by precipitation, ultrafiltration, or absorption).

Abstract: A chip feeding system for a continuous digester provides for a greater rate of delivery of chip slurry to the digester, and is much less expensive than conventional chip feeding systems, typically being only 40-50% of the height of the conventional system. An atmospheric vessel may be connected at the bottom thereof to a slurry pump which pumps the chip slurry to a conventional high pressure feeder. A recirculation loop for returning liquid from the feeder to the vessel may include an atmospheric level tank, and a liquid cooler. The vessel may have one dimensional convergence and side relief, and instead of a conventional cylindrical chip bin, the chip bin may have a hopper having two transitions with one dimensional convergence and side relief. The chip bin also may be at atmospheric pressure so that no low pressure feeder between the bin and vessel is necessary.

Abstract: A number of different, efficient treatments of slurries and liquid with gas can be provided. A slurry or liquid is introduced into a first end of a vortex. A gas--such as a chemically reactive gas--is introduced from exteriorly of the vortex into contact with the slurry or liquid in the vortex, so that a desired reaction between the slurry or liquid and the gas takes place. The treated slurry or liquid is removed from the second end of the vortex while any residual or carrier gas is removed from the first end of the vortex. Gas introduction is preferably accomplished through a porous surface of revolution (e.g. cylindrical or conical) wall surrounding the vortex, the gas being in minute bubble form when it enters the slurry or liquid.

Abstract: Liquid process streams--such as white water, pressate, or washer filtrate from a pulp and paper mill--are clarified in an efficient manner using a gas sparged hydrocyclone, which takes up a minimum of floor space. A liquid stream having a consistency of less than about 0.5% solids is introduced into a first end of a vortex. Gas is sparged into the liquid in the vortex to cause particles to attach to gas bubbles and move through a rejects outlet at the first end of the vortex, while clarified liquid is removed from a second end of the vortex. A pedestal is typically provided at the accepts outlet, having a radial clearance with the inside of a porous tube through which the gas is sparged that is about 8-12% the radius of the porous tube.

Abstract: In a chip bin or similar cylindrical upright vessel for storing particulate material the interior generally vertical wall of the vessel has a surface configuration which reduces compression of particulates within the vessel so as to substantially prevent pluggage or particulate bridging. Three or more right circular cone frustrums having a larger diameter at higher portions than at lower portions are provided along the interior generally vertical, either one immediately adjacent the other without significant spacing between them, or in a discontinuous manner being spaced from each other a significant distance. The frustrums insure that the vertical pressure level throughout the vessel is less than about 250 psf (e.g. less than about 200 psf). The vessel may be constructed of concrete using slip forms, with the concrete providing both the exterior and interior of the vessel, or a steel shell may comprise the exterior.

Abstract: A pressure diffuser is constructed so that the compression of pulp that normally occurs during rapid movement of the screen assembly does not significantly degrade the efficiency of the washing (or other treatment liquid) action in the diffuser. This is accomplished by providing at least two headers, including a first vertical header and flow control assembly for one or more sets of horizontal treatment liquid conduits adjacent the pulp inlet to the diffuser, and a second vertical header and flow control assembly for one or more horizontal treatment liquid conduits remote from the pulp inlet. The first and second vertical headers may comprise a common pipe with a flow preventer precluding flow between them, or distinct pipes supplied with treatment liquid by a common pump. The advantageous results are further achieved by providing at least one ring [mounted between the outer screen and the concentric inner support cylinder of the screen assembly] with a plurality of rapid-flow restricting openings.

Abstract: Liquid effluent from a pulp mill bleach plant having at least one chlorine chemical bleach stage is evaporated and then used in chlorate manufacture. The bleach plant effluent produced by evaporation may be stored and then transported to an off-site chlorate production location, and/or may be subjected to a sodium chloride removal process (such as evaporative crystallization) and only sodium chloride transported to the off-site location. Chlorates produced off site can be returned to the mill (with acid and caustic that are optionally produced) for chlorine dioxide manufacture on site. The chloride-depleted stream from sodium chloride removal may be burned in the mill recovery boiler.

Abstract: Chemical pulp is produced from hardwood chips in a simplified manner utilizing a continuous digester. An inverted top separator is provided in the circulatory loop between the high pressure feeder and the top of the continuous digester for thermally isolating circulations on either side of the inverted top separator. Relatively cool liquor circulates between the inverted top separator and high pressure feeder, at a temperature such that it will not flash into steam in a high pressure feeder, while in the circulatory loop from the high pressure feeder to the digester the chips are in cooking liquor at cooking temperature. Since hardwood chips require less cooking than softwood chips, a single heating source for heating the liquor to cooking temperature is provided, external of the digester, and a conventional cooking circulation loop within the digester is not required.

Abstract: In a method of bleaching medium consistency pulp with ozone using a mixer, ozone containing gas and about 6-15% consistency pulp are fed to the mixer, and then discharged in a first, preferably vertical, path. The mixture of pulp and ozone moves in a first part of the vertical path a time period of about 1-5 seconds at a velocity of about 1-5 m/s so that the gas and pulp do not separate during movement in this first part, and the vast majority of the pulp brightening reaction between the ozone and pulp takes place. This is preferably accomplished by passing the mixture upwardly in a small diameter conduit having a height of about 3-20 meters. Then the velocity of the pulp is slowed while still moving in the first path, preferably by feeding it directly to a much larger diameter (e. g. 1.5-10 times) conduit, so the height of the unit may be kept under 100 feet. The pulp flows in the large diameter conduit for about 0.5-5 minutes so that residual reactions take place.

Abstract: Medium consistency (e.g. about 6-15%) paper pulp is effectively bleached with ozone in a carrier gas (typically oxygen) by effecting efficient separation of carrier gas from the pulp after reaction with the ozone, and introducing the ozone into the pulp at a pressure of about 10-13 bar. Ozone in oxygen and medium consistency paper pulp are fed to a fluidizing mixer; the intimate uniform mixture produced is then passed upwardly in a reaction vessel until about 99% of the ozone has been consumed, and then separation of gas from the pulp is initiated by moving the pulp mixture into a generally horizontal tube leading to a gas zone in a large diameter retention vessel. A pressurized gas pad is maintained at and above the introduction of the pulp into the retention vessel, while the level of pulp in the retention vessel is maintained below the point of introduction.

Abstract: A slurry or liquid is introduced into a first end of a vortex. A gas--such as a chemically reactive gas--is introduced from exteriorly of the vortex into contact with the slurry or liquid in the vortex, so that a desired reaction between the slurry or liquid and the gas takes place. The treated slurry or liquid is removed from the second end of the vortex while any residual or carrier gas is removed from the first end of the vortex. Gas introduction is preferably accomplished through a porous surface of revolution (e.g. cylindrical or conical) wall surrounding the vortex, the gas being in minute bubble form when it enters the slurry or liquid. This has particular applicability in the treatment of paper pulp using an ozone containing gas, or in reacting various liquids in the paper and pulp industry with gas (such as reaction of caustic solutions with chlorine or chlorine dioxide gas), the stripping of a strippable component from a liquid (e.g.

Abstract: A conventional continuous digester is modified so as to provide a countercurrent cook throughout the entire height of the digester. Instead of connecting an upper mid-point extraction screen to a flash tank, that screen is closed off and extraction is provided at the top of the digester, utilizing an in-line drainer to remove some of the liquor and feed it to a flash tank. The liquor not removed recirculates through a pressure screen to an impregnation vessel, and then back to the digester. A cooling circulation is provided just below the top extraction. Valves are provided in the liquor discharged from the drainer and a conduit from the upper mid-point extraction which may be manipulated to return the digester to conventional operation, including the addition of white liquor to the bottom recirculation.

Abstract: Transition metals are removed from cellulose pulp and treatment fluids in a pulp mill. Medium consistency digested pulp is treated in an acidic stage, and then washed to produce a filtrate. The pH of at least a substantial part of the filtrate is adjusted so that it is greater than 9 (preferably greater than 10.5), while a sufficient carbonate content is provided to keep the calcium content low. Adjusting the pH causes dissolved transition metals in the filtrate to precipitate as solids, and the solids can then be filtered out, e.g. by precoat filtering, or clarification followed by polishing filtering. The greatly reduced transition metal content filtrate is then used elsewhere in the pulp mill, as in a washer following an oxygen delignification stage. The acidic stage may be an EDTA stage, an ozone stage, an acid only stage, etc., and the pulp is preferably treated so that it is bleached in at least one Z stage and one P stage, and preferably also an E (e.g. E.sub.op) stage.