Paper making and fiber liberation – Processes of chemical liberation – recovery or purification... – Continuous chemical treatment or continuous charging or...
Reexamination Certificate
2001-07-09
2002-08-13
Nguyen, Dean T. (Department: 1731)
Paper making and fiber liberation
Processes of chemical liberation, recovery or purification...
Continuous chemical treatment or continuous charging or...
C162S018000, C162S052000, C162S246000, C222S216000, C222S564000
Reexamination Certificate
active
06432264
ABSTRACT:
BACKGROUND AND SUMMARY OF THE INVENTION
In the processing of comminuted cellulosic fibrous material in the production of cellulose pulp, the material is typically stored or treated in several cylindrical vessels. The material is typically discharged from these vessels through restrictions that communicate with conduits, that is, piping, through which the material is transferred to the subsequent treatment. In order to promote the movement of the cellulose material, typically in the form of a chip slurry or fiber slurry in liquid, from the vessel to the restriction of the discharge, some form of agitation is provided in the vicinity of the discharge. This agitation typically takes the form of a rotating agitator or discharge device that agitates the material and promotes its movement toward and through the discharge of the vessel.
However, the geometry of the bottom heads of conventional treatment vessels, in particular, the bottom heads of continuous digesters, typically require the material being processed to make a dramatic change in flow path. That is, the flow of material in conventional vessels is required to change from a essentially downward vertical direction to an essentially horizontal direction toward a centrally-located outlet. This change in flow direction is typically associated with the “knuckle” of typical dished heads used in treatment vessels. The change in direction, and the compression of the material that is accompanied by such changes of direction, can produce dramatic variations in the liquid content, that is, the consistency, of the material in the vicinity of the change in flow path. For example, the consistency may change from 10-15% in the middle of the vessel to 30 to 40% adjacent the wall of the vessel. These local changes in consistency can effect the flow of material at or above such regions and can also affect the flow and distribution of treatment liquids introduced in these areas.
Also, in the processing of cellulose material to make cellulose pulp for paper, it is undesirable to treat the material with a mechanical agitator, especially when the material is in a hot, alkaline state, as is typical in the bottom of chemical digesters. Agitation or the application of “mechanical action” to the material has been associated with physical damage to the material; damage that can result in reduced strength of the paper subsequently produced. For example, in some cases the discharge from vessels can be effected without the aid of mechanical action as disclosed in U.S. Pat. Nos. 5,700,355; 5,617,975; 5,628,873; 5,500,083; and 4,958,741 or Statutory Invention Registration H1681; this technology is marketed under the trademark Diamondback by Ahlstrom Machinery of Glens Falls, N.Y.
Also, the rotating agitators require energy to rotate the device in the slurry of material. Rotating discharge devices are typically powered by electric motors coupled to the device by means of a mechanical transmission, for example, a gear box, belt drive or chain drive. The amount of energy required to drive these devices is dependent upon the geometry of the agitating device, the diameter and height of the vessel, and the state of the material being agitated, for example, its liquid content, among other things.
As the production rate of material passing through the vessels increases, the height and diameter of the vessel must be enlarged to accommodate these larger production rates. This directly affects the loading on the agitating device and the amount of energy or power that must be used to rotate the agitating device. For instance, as the vessel diameter becomes larger, the diameter of the rotating device must also increase so that as much of the diameter of the vessel is “swept” by the rotating device. The rotating device typically has paddled “arms” which extend from a centrally-located hub. As the vessel diameter increases, the length of the arms must increase. However, as the length of the arm increases, the moment arm of the torque which must be supplied to agitate the material also increases. The increased torque required by the increased diameter of the vessel translates directly into an increase in power consumption required to agitate the material. Thus, it is preferred to have the smallest moment arm as possible for the rotating device in order to minimize the power required.
In addition to the diameter of the vessel, the height of the vessel also effects how much power must be provided to rotate the agitator. As the production rate of material passing through a treatment vessel increases, for a desired retention time in the vessel, again, either the diameter or the height of the vessel must increase. Typically, treatment vessels are designed to have a limited length-to-diameter ratio, that is, L/O or “L over D ratio”. For example, for continuous digesters the L/O ratio is typically limited to a value less than 10. Typical production rates of vessels designed today exceed 500 tons of pulp per day[T/D], typically exceed 1000 T/D and approach 3000 T/D or more. Since the diameter of a vessel directly effects how much area the vessel will require, that is, how large a “foot print” the vessel will have, larger production rates are typically accommodated by increasing the vessel height, which typically comes at less cost to a mill, while limiting the L/D ratio as discussed above. (Of course, the diameter of such vessels may also be increased to provide the desired L/D ratio.) However, as the height of a vessel increases, the static head pressure on the material on the bottom of the vessel increases. As discussed above, this compression of the material in the bottom of the vessel is typically greatest in the vicinity of the lower head transition from vertical to horizontal and can affect the consistency and flow of the material and the flow of liquids in this area. In addition, localized regions of higher material consistency in the vicinity of the outlet and outlet agitator can increase the resistance of material to agitation and thus increase the power required to agitate the material.
The present invention addresses these limitations of the prior art and provides a vessel discharge with reduced compression of the material and reduced power requirements compared to vessels designed according to the existing art. In a broad embodiment of the invention there is provided a cylindrical vessel for storing or treating comminuted cellulosic fibrous material having a first cross section having a first diameter and a second cross section, below the first cross section, having a second diameter at least 20% less than the first diameter, wherein between the first cross section and the second cross section there is a transition from the first diameter to the second diameter. The second cross section is preferably a material outlet.
The treatment performed in the vessel may be chemical (e.g. kraft) pulping, delignification, washing, bleaching, or simply storage. The vessel is preferably a continuous digester or a continuous pretreatment vessel such as an impregnation vessel, but the present invention may also be used for non-continuous or batch-type treatments, for example, a batch digester.
The outlet of the digester preferably includes a means for agitating the material in the vicinity of the outlet in order to promote movement of the material, but based upon the geometry of the transition and the effectiveness with which the material can be transferred by the transition, an agitating device may not be necessary. If an agitator is required, due to the geometry of the transition, the power required to rotate the agitator may be at least 10% less than (e.g. at least 20% less than) a comparable conventional outlet and agitator.
The first diameter is typically at least 10 feet, preferably at least about 20 feet, and most preferably at least about 30 feet. The second diameter is typically at least 1 foot, preferably at least about 3 feet, most preferably at least about 5 feet.
The most preferred transition is a simple frusto-conical transition; however, other transitions
Johanson Jerry R.
Prough J. Robert
Andritz Inc.
Nguyen Dean T.
Nixon & Vanderhye P.C.
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