Patent Application
20140069598
The present invention concerns a method and an arrangement for adding treatment liquors to comminuted cellulose material, preferably wood chips, during the manufacture of chemical pulp in a continuous process using a down flow vessel where chips are descending down the vessel in a plug flow, according to the preamble of claim 1 and claim 6.
In old conventional Prior Art for cooking of chemical cellulose pulp with continuous digesters it was common to use a pre-treatment arrangement with a chip bin, steaming vessel and an impregnating chip chute, before the cooking process is established in the digester. Steaming has been carried out in one or several steps in the chip bin, prior to the subsequent formation of a slurry of the chips in an impregnation fluid or a transport fluid. The steaming has been considered to be absolutely necessary in order to be certain of expelling the air, such that the impregnation fluid can fully penetrate the chips, and such that air is not drawn into the system.
Attempts have been made to integrate the chip bin with the impregnation vessel in order to obtain in this manner a simpler system.
Already in U.S. Pat. No. 2,803,540, a system was revealed in which the chips from a chip bin were fed to a vessel in which a combined steaming and impregnation was achieved. In this vessel, the chips were steamed at the upper part of the vessel and impregnation fluid at the same temperature was added at various levels in the vessel using distributing annular manifolds/headers located outside of the vessel wall, and having nozzles penetrating the wall. These principles were also applied in a process known as “Mumin cooking”, which is described in “Continuous Pulping Processes”, Technical Association of the Pulp and Paper Industry, 1970, Sven Rydholm, page 144. In this process, unsteamed chips were passed to a combined impregnation vessel, where steaming was obtained in the upper part, and to which impregnation fluid was added at a point in the upper part of the vessel during forced circulation. The impregnation fluid was in this case carried exclusively in the same direction of flow as the chips.
A similar system with a low pressure first common steaming and impregnation vessel is shown in U.S. Pat. No. 3,532,594, which also was put into operation for example at the Skoghall mill in Sweden. Here was heated impregnation liquid added via a central pipe to the chip volume, but also showing an additional central pipe for steam supply. This system was later abandoned due to various reasons such as run ability problems, capacity problems in subsequent feeding system and far too high reject and shive content in the blown pulp.
A system is shown in U.S. Pat. No. 5,635,025 in which the chips are fed without prior steaming to a vessel in the form of a combined chip bin, impregnation vessel and chip chute. Steaming of the chips takes place here, the chips lying above the fluid level, and a simple addition of impregnation fluid takes place trough the vessel wall below the liquid level.
A further such system is revealed in U.S. Pat. No. 6,280,567, in which the chips are fed without prior steaming to an atmospheric impregnation vessel in which the chips are heated by the addition of warm black liquor that maintains a temperature around 130-140 C. The added impregnation liquid is added via nozzles in a manner similar to what is shown in U.S. Pat. No. 2,803,540, i.e. using supply nozzles penetrating the wall of the vessel.
An alternative system is revealed by SE 523,850 in which pressurized black liquor is added to the upper part of the steaming vessel, whereby the black liquor after being subjected to a pressure reduction releases steam for the steaming process. The addition of the hot black liquor is made by a stationary horizontal supply pipe penetrating the chip bed, and having a multitude of holes over the length of the pipe. Even if the distribution of hot black liquor is made over a larger (but not over the complete cross-sectional) area this solution is not advisable since the horizontal pipe may hinder the chip plug movement. The prior art has mostly used either a stationary central pipe or stationary annular distribution nozzles located in the wall of the vessel for the added impregnation liquid to the combined steaming and impregnation vessel.
During the last few years the design capacity of new digester systems has been significantly increased, from typically 500-2000 ADt/24 h to production rates over 5000 ADt/24 h. As the design production rate increases the combined chip steaming and impregnation vessel diameter increases as well.
The technique with a common treatment vessel for steaming and impregnation at substantially atmospheric conditions is marketed by Metso Paper under the name of IMPBIN™. Several improvements of the concept have been patented in;
Another disadvantage with known solutions is that this common steaming and impregnation vessel should optimize both functions, and it is a conflicting interest, as both steaming effect and impregnation time needs may vary depend on differing operating conditions and type of cellulose material fed to system. If there is a need to extend the impregnation time in the impregnation liquid it may not be possible to increase the liquid level, as such an increase may reduce the time in the steaming zone, or may reduce the amount of steam generated by flashing hot liquors. Flashing off steam beneath the liquid level creates a boiling effect that disrupts the formation of a well packed chip pile in the center of the vessel, which may cause a channeling effect inside the vessel hampering a uniform treatment of the cellulose material inside the vessel.
The above mentioned disadvantages with possibilities of extending the impregnation zone for wood material that is difficult to impregnate, or if other process conditions call for an increased liquid level in the impregnation zone, while still maintaining an efficient steaming effect, has become apparent after a large number of implementations of IMPBIN, especially those being fed with cellulose material of differing qualities during operation.
The principle object of the invention is to obtain an improved and more flexible arrangement for the addition of treatment liquids to chips during the manufacture of chemical pulp in a continuous process using a down flow vessel where chips are descending down the vessel in a plug flow, which arrangement does not demonstrate the disadvantages that are associated with other known solutions as described above.
A specific objective is to enable changes of the liquid level while adding steam, from a supply of steam and/or from flashing hot liquor, which addition of steam is controlled to take place very closely above the liquid level such that an optimum steaming effect is at hand independently of the established liquid level.
Another specific objective is to be able to change the retention time in the impregnation zone when changes in wood quality occur. These changes in wood quality could depend upon
Yet another specific objective is to be able to reduce the torque demand on mechanical feed means in bottom of the down flow vessel, typically a bottom scraper. When the chip quality occasionally is outside of specifications, for example a high content of fine wood particles (sawdust or pin chips fractions are high), then the compaction of the chip column in the vessel might increase to such extent that the working load on the bottom scraper becomes excessively high. This may cause operational disturbances and production losses. To counter-act too high chip column compaction it is common practice to reduce the difference between the chip and liquor level in the vessel by increasing the liquor level so that the downward thrust from the chips being located above the liquid level is reduced. It is important that during such control should not the point of introduction of steam and/or hot liquor be drenched by the rising liquid level, which would reduce an effective generation of steam.
The invention can advantageously be used when cooking hard wood or softwood chips, bagasse, bamboo or other annual plants.
The characteristics of the invention are defined by the independent claims, and optional embodiments are defined in dependent claims in order of dependency of preceding claims. The invention is also disclosed in a preferred embodiment, but any specific feature of this embodiment could as such be included in the invention optionally, if not specifically defined as a necessary feature for the argued effect.
During following description will the term “treatment liquid” be used, and by this is meant one kind of treatment liquid that is intended to be added evenly to the entire chip flow in the treatment vessel. This treatment liquid could comprise only of steam, but also hot spent cooking liquor, i.e. black liquor, from a subsequent digester, as well as a mixture of two or more of following hot liquids;
The term “treatment vessel” will also be used, and by this is meant any kind of treatment vessel used for treating chips in either form of delignification or impregnation state, i.e. the vessel could be an atmospheric combined steaming and treatment vessel like IMPBIN, or a pressurized digester.
The term “comminuted cellulose material” will be used, which preferably could be in form of wood chips, but also more fragmented wood material such as sawdust or pin chips, all obtained from either hardwood or softwood or annual plants.
A prior art arrangement for the impregnation of chips during the manufacture of chemical pulp is shown in
The pressure in the vessel can be adjusted as necessary through a control valve 31 arranged in a valve line 4 at the top of the impregnation vessel, possibly also in combination with control of the steam ST via input lines 5.
When atmospheric pressure is to be established, this valve line can open out directly to the atmosphere. It is preferable that a pressure is established at the level of atmospheric pressure, or a slight deficit pressure by the outlet 4 of magnitude −0.5 bar (g) (−50 kPa), or a slight excess pressure of magnitude up to 0. 5 bar (g) (50kPa).
Input of a ventilating flow, SW_AIR (sweep air), can be applied at the top as necessary, which ensures the removal of any gases present or brought into the vessel by the in feed of comminuted cellulosic material.
The impregnated chips are continuously fed out via output means, here in the form of an outlet 10, possibly also in combination with bottom scrapers (BS), at the bottom of the impregnation vessel 30.
The level of the chips, CH_LEV, above the level of the liquid, LIQ_LEV, should preferably be at least 2 meters and preferably at least 5 meters when impregnating wood chips. In the case of pulping raw material of low bulk density, a corresponding increase in the height of the column of chips over the surface of the fluid is preferably established. This height is important in order to provide an optimal passage of the chips in an even plug flow through the vessel.
When impregnating primarily easily cooked types of wood, such as eucalyptus and other annual plants, steaming with fresh steam can be essentially avoided, especially in a warm climate where chip temperature normally is high. Fresh steam is thus not necessarily added to the chips that lie above the fluid level established by the impregnation fluid during normal steady-state operation. The invention can also be applied also if softwood with lower bulk density is used as raw material.
When treating primarily wood raw material that is difficult to cook, especially softwood having less density, and in operational cases with extremely low temperature of the chips, such as during the cold season, the chips that lie above the fluid level established by the impregnation fluid can be heated by the addition to the impregnation vessel of external steam ST such that a temperature of the chips approach 100° C. in the chip pile before the chips reach the fluid level that has been established by the treatment liquor
The hot treatment liquid added via a common central pipe 7a can also be established as a mixture from totally separate sources, that is, not from one common flow of black liquor.
For example, the treatment liquor may also contain a wash filtrate.
The treatment liquid added can also be a mixture of black liquor and an additive amount of fresh cooking chemicals, i.e. white liquor, as well as steam with the object of establishing alkali profiles that are necessary for the process. In particular if the residual alkali in the black liquor is low. A rapid initial consumption of alkali normally takes place, simply in order to neutralize the wood acidity, while it is desired to keep the final residual alkali after the impregnation stage at a certain level. The needed amount of additional alkali is mostly dependent on the level of wood acidity being released during steaming in the chip volume above the liquid level, and thus dependent on type of wood being treated (softwood or hardwood).
The vessel may be equipped without or with extraction screens 6 to allow liquid extraction (REC) early in the process.
In
In
Here is shown an arrangement for adding the hot treatment liquor BL to comminuted cellulose material, preferably wood chips, during the manufacture of chemical pulp in a continuous process. Said process using a down flow vessel 13 where comminuted cellulose material is descending down the vessel in a plug flow and where treated comminuted cellulose material is continuously fed out at the bottom of the vessel, similar to what is intended in
The treatment liquor BL is supplied from a common source BL via piping 7 to a common header 7c. More than 2 vertical pipes 7b1 and 7b2 are connected with their upper end to the common header 7c. The vertical pipes 7b1 and 7b2 preferably have an upper stationary pipe part and telescopically arranged with said stationary pipe part is a lower outlet part 701 and 702 respectively.
The lower outlet parts having their open lower ends inserted in the chip plug flow.
As shown in the left hand side of the center line CL is a lower liquid level LIQ_LEV1 established, and the height position of lower outlet part 701 is adjusted to a distance above this liquid level. As shown in the right hand side of the center line CL is a higher liquid level LIQ_LEV2 established, and the height position of lower outlet part 702 is adjusted to a distance above this liquid level. In each case the adjustment is made by sliding the lower outlet part telescopically on or in said stationary pipe part.
As shown in
As shown in the
A control system CPU could be used, having at least one process parameter as input parameter for controlling the height position of the lower outlet part 70, and the control unit could via a bi-directional connection control the motor and position obtained by the adjustment means. One such input parameter could be the detected liquid level LIQ_LEV, and another input parameter could be the detected torque requirement on the bottom scraper BS.
Control Modes
If the actual liquid level is used as a feed-back signal, the system could otherwise change net input flows of liquid and as soon as the liquid level starts to rise, the adjustment means starts lifting the lower outlet pipe striving to maintain a set distance between liquid level and outlet of the outlet part 70. to the vessel liquid level. If the intended liquid level is used as a feed-forward signal, the system could start lifting the lower outlet part 70 as soon as the intended control to increase the liquid level starts to act.
If the torque requirement on the bottom scraper BS exceed a set level could also the system start lifting the lower outlet part 70 with simultaneous increase of the liquid level.
The arrangement with a telescopic pipe thus provides a possibility to change the liquid level established in the vessel, while allowing addition of treatment liquid in form of steam, or preferably hot treatment liquor flashing off steam, to be made close to the liquid surface but still above the liquid level. The steaming effect will thus be able to steam the entire chip volume above the liquid level.
The possibility to alter the liquid level, while maintaining maximum steaming effect, is important in order to adapt the process to different process conditions.
Different process conditions could depend on the wood material fed to the vessel. For instance could the specific weight of chips change, due to changes in type of wood or wood mixture (softwood/hardwood), or if more juvenile wood is fed to vessel, or if the vessel is used in the winter or summer (amount of ice brought into vessel by chips may change steaming requirement).
Changing the liquid level is also an important control aspect when trying to reduce the torque requirements on any bottom scraper located in bottom of vessel. By lifting the liquid level could the downward force from the chip pile above the liquid level be reduced, and hence the total downward thrust from the chip plug onto the bottom scraper.
The invention could be altered in many ways under the inventive scope as defined in claims. The telescopic pipe could also be by other means than by using two tubes sliding concentrically on each other. For instance could the upper stationary pipe part be connected to the lower outlet part via some bellow mechanism. The lower outlet part could include at least 2 sliding tubes, i.e. also using an intermediate sliding tube between the upper stationary pipe part and the lowermost outlet part. In its simplest form could the adjustment mean simply include a hand cranked adjustment wheel.
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/SE2011/050339 | 3/25/2011 | WO | 00 | 11/27/2013 |
