Patent Grant
8262851
The disclosure below relates generally to the pulping of cellulosic materials. More specifically, the present invention relates to the conversion of lignocellulosic materials into pulp by means of chemical mechanical pulping process.
In the pulp and paper industry, there are basically two fundamentally different processing methods for converting lignocellulosic material, being wood or nonwood, into pulp used in papermaking. One processing method is chemical pulping, which uses chemicals such sodium hydroxide, sodium sulfide, sodium sulfite or different solvents, to break down bonding between each individual fiber. The other processing method is mechanical pulping, which uses mainly mechanical means such as a pair of rotating discs commonly referred to as a refiner, or a rotating grinding stone, to separate the lignocellulosic fibers from one another. The process of using mainly mechanical means for separating lignocellulosic fibers from one another is commonly called defiberization. In some mechanical pulping processes chemicals are used before, during, and/or after the mechanical defiberization in order to modify the pulp properties and/or reduce energy consumption. Applying chemicals before and/or during refiner mechanical defiberization, is commonly referred to as Chemical Mechanical Pulping (CMP) process.
In CMP, there are three fundamentally different concepts used to produce pulp. The first of these CMP concepts is to treat the material, normally in the form of chips, with chemicals and complete the treatment, or most of it, before the refiner defiberization step. The treatment may be a high temperature cooking for an extended period of time, as in a conventional CMP process, or high temperature for a relatively short period of time, as in Chemi-Thermal Mechanical Pulping (CTMP), or relatively low temperature and long period of time as in Cold Caustic Soda (CCS), Alkali-Peroxide Mechanical Pulping (APMP), Alkali-Peroxide Pulping (APP) processes. Exemplary APMP processes are disclosed in U.S. Patent Application Publication 2004/0200586 and WO 05/042830 (the entire content of each being expressly incorporated hereinto by reference). Some of these CMP processes also use a compression device to squeeze the lignocellulosic material before the chemical application to improve the desired chemical treatment effect.
The second CMP concept is to add chemical to the chips during refiner defiberization, as proposed in U.S. Pat. Nos. 3,023,140; 3,069,309; 4,187,141; 4,311,553; 4,270,976; 5,129,987 (the entire content of each such patent being incorporated expressly hereinto by reference). This type of treatment uses the refiner not only to provide defiberization but also as a mixer for chemical distribution and reaction, although in some cases, a chip pretreatment is mentioned. The pretreatment step is only for stabilizing hydrogen peroxide (H2O2), as described in U.S. Pat. No. 4,311,553,or softening the chips as described in U.S. Pat. No. 3,069,309. In such a pretreatment step the principal chemicals, in most cases peroxide, have an effect on the development of pulp properties, such as brightness, are applied at the refiner.
The third CMP concept is to combine the chemical pretreatment (in this case referred as Preconditioning) before refiner defiberization, and chemical treatment during the refiner defiberization and fibrillization process and before the final refining step (referred to as Refiner Chemical treatment) and is referred to as P-RC, (Preconditioning, followed by Refiner Chemical treatment). In P-RC APMP pulping, two different chemical strategies had been introduced. The first is to add a significant amount of alkali peroxide chemicals immediately prior to the primary refining step, which is most suitable for atmospheric refining (e.g., as described in China Patent Number: CN ZL02814472.4,the entire content of which is incorporated fully hereinto by reference); and the second is to apply the main alkali peroxide chemicals immediately after the primary refiner, which is most suitable for pressurized refining (e.g., as described in United States Patent Application Publication US 2004/0069427 A1,the entire content of which is incorporated fully hereinto by reference).
One embodiment of the present invention comprises a process which uses a non-compression vessel, such as a digester, for chemical preconditioning of the chips followed by a fiberizing device to break the preconditioned chips down to fiber bundles, which are then washed before a high consistency chemical treatment. For the preconditioning, rather than using compression device, such as chip presses, the present invention employs a digester to distribute the chemicals inside of the chips. The digester could be one such as used in conventional chemical pulping of wood with or without screens for the extraction of chemical. If extracted this chemical could be recirculated to the digester with treatment in the circulation loop such as heating or the addition of dilution or other chemicals. This digester could be hydraulic or vapor phase (that is contain a vapor space within the digester), and operate in either a continuous or batch fashion. This digester allows for the discharge of material without the use of a screw mechanism. The digester treated material is then defiberized to convert the chips into course fiber bundles, which then is washed and dewatered. The washed and dewatered pulp is then treated with alkali peroxide chemicals to develop brightness and other pulp properties.
According to other embodiments, an alkaline peroxide mechanical pulping process is provided which comprises (a) preconditioning a lignocellulosic chip material with chemical stabilizers in a non-compression vessel; (b) discharging the preconditioned lignocellulosic chip material to a fiberizer so as to mechanically break apart the preconditioned lignocellulosic material and obtain a fiberized lignocellulosic material; (c) washing the fiberized lignocellulosic material, and thereafter (c) treating the washed and fiberized lignocellulosic material with alkali peroxide chemicals for a time and under conditions sufficient to obtain a pulp of desired consistency therefrom. Preferably, step (c) is practiced with a high consistency refiner.
Substantially all the alkali peroxide chemicals are added immediately before the fiberized lignocellulosic material is transferred to the refiner. The fiberized lignocellulosic material may advantageously be washed with a press.
According to some embodiments, the preconditioning step (a) is practiced in a digester as a non-compression vessel. Conditions within the digester may include a pressure of between 0 to 10 bar (e.g., between 0 to 6 bar), a temperature of between 10 to 170° C. (e.g., between 30 to 120° C.), and a retention time of from between 0.1 to 7 hours (e.g., between 0.1 to 4 hours). Liquor may be added lignocellulosic chip material in the digester so as to achieve a liquor to wood ratio of between about 0.5:1 to about 5:1 (e.g., between about 1.25:1 or 1.5:1 to about 1:1).
The chemical stabilizers may comprise organic chelating reagents or inorganic compounds. Preferred organic chelating reagents include diethylene triamine pentaacetic acid, ethylene diamine tetraacetic acid, and nitriletriactic acid. Preferred inorganic chemicals may comprise silicate and MgSO4.
Advantageously, the process may comprise discharging the pulp to a high consistency tower and retaining the pulp in the high consistency tower for a time and under temperature conditions sufficient to achieve a desired pulp consistency. The time and temperature conditions may be sufficient to achieve a pulp consistency of between about 15 to about 45%, more preferably, more preferably between about 12 to about 60% (e.g., between about 25 to about 30%). The temperature condition within the high consistency tower may be between about 20 to about 100° C. (e.g., between about 40 to about 100° C.). The pulp is advantageously retained within the high consistency tower for up to about 7 hours (e.g., between about 15 minutes to about 4 hours).
These and other aspects and advantages of the present invention will become more clear after careful consideration is given to the following detailed description of the preferred exemplary embodiments thereof.
Accompanying
As shown in accompanying
Pressure: 0-6 bar (preferably 3.5 bar)
Temperature: 30-120° C. (preferably 40-90° C.)
Time: 0.1-4 hours (preferably 1 hour)
Liquor to Wood ratio: 1.5:1 (preferably 2.5:1)
Liquor may be added to the digester to obtain the desired liquor to wood ratio. This liquor may be stabilizer dissolved in water with or without alkali and with or without peroxide. The fiberizer after the digester is designed to gently break the impregnated chips into fiber bundles so that the material can be easily washed with conventional washing equipment and be easily fed to a conventional high consistency refiner. Most or all the alkali peroxide chemicals are added either immediately before the refiner and/or a blow line immediately after the refiner. The chemical-mixed material (pulp) is then retained in a high consistency tower to allow the chemical reactions to complete. The treated pulp is then, with or without washing, refined using either a high, medium, or low consistency refiner, with at least one stage of refining, which may be one or more refiners run at the same consistency or a combination of refiners run at different consistencies. The refined pulp undergoes treatments as is conventional in mechanical pulping processes, such as latency removal, screening, cleaning, screen reject treatment, washing/dewatering, and the like.
The high consistency refiner performs both further defiberization and fibrillation as a conventional primary mechanical pulp system (e.g. either thermal mechanical pulping (TMP) or refiner mechanical pulping (RMP)), and mixing alkali peroxide chemicals either at the refiner or in the blow line after the refiner. The alkali chemicals include alkali and peroxide in various forms, and with or without peroxide stabilizers. Quantities of the chemicals used vary, and depend on the nature of the raw material and the product.
The high consistency tower is mainly to give the added chemicals enough reaction time to complete their reactions. The pulp consistency can be between about 12 to about 60% (e.g., between about 15 to about 45%, preferably between about 25 to about 30%), and the temperature can be between about 20 to about 100° C (e.g., between about 40 to about 100° C., preferably between about 70 to about 95° C.). The retention time may varies a few minutes to several hours (e.g., up to 7 hours), for example from about 15 minutes to about 4 hours, depending on the raw materials and the products.
After the high consistency tower, the pulp can either be washed with a pulp press first, or is refined using at least one of a high, medium, or low consistency refiner, with at least one stage of refining, which may be one or more refiners run at the same consistency or a combination of refiners run at different consistencies with or without a latency chest in between. The washed and dewatered (pressed) pulp can be refined using either high or low or medium consistency refiner.
After the main line refining, the pulp goes through normal pulping process stages, e.g. screening, cleaning (if necessary), thickening and washing, and final storage.
Another embodiment of the process system according to the present invention is depicted in
The process system depicted in
While the invention has been described in connection with what is presently considered to be the most practical and preferred embodiment, it is to be understood that the invention is not to be limited to the disclosed embodiment, but on the contrary, is intended to cover various modifications and equivalent arrangements included within the spirit and scope of the appended claims.
This application is based on and claims domestic priority benefits under 35 USC §119(e) from U.S. Provisional Application Ser. No. 60/836,678 filed on Aug. 10, 2006,the entire content of which is expressly incorporated hereinto by reference.
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| 60836678 | Aug 2006 | US |
