Patent Grant
8801898
This application is a U.S. national phase application that is based on and claims priority from International Application No. PCT/SE2009/000383, filed 19 Aug. 2009.
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.
In old conventional Prior Art used 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 and water that is bound in the chips, 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 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 central pipe or annular distribution nozzles 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 fact that the diameter of the vessel increases and in combination with using prior art technology, the added treatment liquor may not be evenly distributed over the entire cross-sectional area of the vessel resulting in a chemical concentration gradient.
SE 523.850 discloses another solution to improve the distribution but it will then instead introduce a great risk for chip plug blockage.
Another disadvantage with a single central pipe for adding the treatment chemicals in larger treatment vessels is that the flow of chemicals is high and would be disruptive for a uniform plug flow movement in the lower part of the vessel.
Other disadvantages with only one central pipe for adding treatment chemicals are
(1) the diameter of the central pipe becomes big in systems with high design capacity, which means that a hole with same diameter as the pipe is formed below the end of the central pipe which may continue all the way down to the bottom of the vessel, which in turn give rise to (chip and) liquor channeling,
(2) that a huge quantity of the generated flash steam is introduced at one point, which could cause steam channeling around the central pipe due to the high velocity of the steam going counter-current the chip flow, which could result in steam blow-through of the chip pile.
A disadvantage with a distribution manifold outside of the vessel and supply nozzles penetrating the wall of the vessel for adding the treatment chemicals is, except additional requirement of control valves/instrumentation and pipes, thus increased cost, that it is difficult to completely distribute the chemicals from the shell side to the center of the vessel, thus there is an apparent risk for liquor channeling along the shell of the vessel. All these disadvantages may cause an uneven treatment of the chips, such that quite different pulp quality is produced from those plug flows being closest to wall or central pipe.
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;
The above mentioned disadvantages with prior art addition of treatment liquors are made more obvious as sizes of these steaming and impregnation vessels of the IMPBIN type becomes bigger. The diameter of a typical cylindrical IMPBIN vessel for a digester system with capacity over 5000 ADT per day is well over 9 meter.
The principle object of the invention is to obtain an improved arrangement for the addition of treatment liquors 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. This principal objective becomes more important in high capacity processes, with capacities of producing well over 4000 and as much as 6000 ADT/pulp per day, and where treatment vessels becomes huge and having diameters well over 9 meter.
A specific objective is to enable equal treatment of the wood material in the entire volume of the treatment vessel, minimizing variations in kappa number of the produced pulp and decreasing the amount of rejects (uncooked wood material) from the process. By an even initial distribution of alkaline black liquor, thus ensuring that the alkali concentration over the vessel's entire cross-section and volume will be sufficient, could also the chip volumes being exposed to extensive acidic pre hydrolysis be reduced, since acidic pre hydrolysis is negative for pulp strength properties and yield.
Another specific objective is to minimize channeling effects in the chip or wood material plug flow, which formations of channels or voids is almost impossible to avoid by using singular central pipes with large diameters according to conventional prior art. If such channels are formed inside of the treatment vessel, then most or a large part of the added treatment liquor may be by-passed the bulk flow of wood material intended to be treated in the treatment vessel.
Yet another specific objective is to decrease the steam velocity of the steam being flashed out from the hot treatment liquor, which per se reduces the risk for channeling and leakage of steam along the exterior surface of the supply pipes. By reducing the steam velocity will also the risk for blow-trough, i.e. steam being pushed up and through the entire chip volume, be reduced.
The invention can advantageously be used when cooking hard wood and softwood wood chips, bagasse and 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 liquor” be used, and by this is meant one kind of treatment liquor that is intended to be added evenly to the entire chip flow in the treatment vessel. This treatment liquor could comprise only of spent cooking liquor, i.e. black liquor, from a subsequent digester, but could also be a mixture of two or more of following liquids;
The term “treatment liquid” will also be used, and by this is meant the treatment liquid established in or withdrawn from the vessel, which besides partially used treatment liquor also contains chip moisture or any other organic or inorganic content dissolved from the chips.
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” 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.
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 (−50 kPa), or a slight excess pressure of magnitude up to 0.5 bar (50 kPa).
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 (not shown in the drawing), 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 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. Fresh steam is thus not necessarily added to the chips that lie on top of the fluid level established by the impregnation fluid during normal steady-state operation. The invention can also be applied even if softwood with lower density is used as raw material, giving a markedly reduced need for steaming, that is, a reduced addition of fresh steam.
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 winter), 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 treatment liquor 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 liquor added can also be a mixture of black liquor and an additive amount of fresh cooking chemicals, i.e. white liquor, 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 to allow liquid extraction (REC) early in the process.
In
As shown here is the alkali profiling in the chip column indicated by pH boundaries, where pH1 and pH2 indicate different pH's established at each respective boundary line, and where the pH at pH1>pH2.
Another effect of using a large central pipe for the supply of the treatment liquor is the formation of a larger hole or a less compacted central part of the chip plug descending down the vessel, and this area is marked by CF. This central part CF with less well packed chips could form a channel for the added treatment liquor that instead of being distributed to the entire chip volume is led quicker to the outlet end of the treatment vessel with less effective treatment time on the chips.
In
As shown in
The vertical pipes 7b are connected to the common header 7c at even angular positions in the circumferential direction of the circular common header 7c.
Meaning that at least three vertical pipes 7b could be connected to the common header 7c at angular positions 120 degrees apart in the circumferential direction of circular header, or that at least four vertical pipes 7b could be connected to the common header 7c at angular positions 90 degrees apart in the circumferential direction of circular header, this latter version shown in
As shown in
The common supply header could in an alternative embodiment (not shown) also be located outside of the vessel, and each individual vertical pipe 7b could be controlled by its own individual control valve.
As shown in the
The arrangement as shown thus provides a method for adding a treatment liquor 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 and where treated chips are continuously fed out at the bottom of the vessel and where the addition of the treatment liquor is made via 2 or more pipes being arranged parallel to plug flow direction, thus distributing the treatment liquor in parallel flows at multiple points over the plug flow area and reducing interference of the plug flow to a minimum.
According the inventive method it is preferred during steady state operations (i.e. excluding start and stop or occasional disturbances) that the fluid level in the vessel is established such that it lies under the level of the chips in the treatment vessel and that the outlets of the pipes are located above the fluid level but below the level of the chips in the treatment vessel. The inventive method utilize the wet steaming process where the temperature of the treatment liquor added via the 2 or more pipes at the position of the outlets exceeds the boiling temperature at the prevailing pressure close to the outlets, such that a flashing effect is obtained in the chip volume being located above the fluid level in the vessel. There is thus no need to use any flash tanks for flashing of steam and pressure from the black liquor withdrawn from the digester and the black liquor is instead flashed inside of the chip pile where the heating is required, and at no energy losses.
In a preferred but not necessary mode could according to the invention a withdrawal of treatment fluid take place at a position in the wall of the treatment vessel, inducing a radial displacement flow of treatment liquor from the outlets of the pipes and further trough the chips in the liquid volume.
Besides the shown embodiment with the addition of the treatment liquor made via 2 or more pipes being arranged parallel to plug flow direction, could also additional treatment liquor be added simultaneously via distribution nozzles arranged in the vessel shell,
Tests
In tests with a large diameter IMPBIN, similar to
When testing with a withdrawal volume of 1.5 m3/BDT chips was instead a residual alkali level of about 2-5 g/l obtained in the withdrawn treatment liquid. However, still not as high as indicated by the residual alkali level in the chips being fed out from the treatment vessel.
These tests indicated the general alkali profiling throughout the vessel as shown in
While the present invention has been described in accordance with preferred compositions and embodiments, it is to be understood that certain substitutions and alterations may be made thereto without departing from the spirit and scope of the following claims.
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/SE2009/000383 | 8/19/2009 | WO | 00 | 4/26/2012 |
| Publishing Document | Publishing Date | Country | Kind |
|---|---|---|---|
| WO2011/021968 | 2/24/2011 | WO | A |
| Number | Name | Date | Kind |
|---|---|---|---|
| 3434920 | Green | Mar 1969 | A |
| 3881986 | Backlund | May 1975 | A |
| 4120748 | Zucker | Oct 1978 | A |
| Number | Date | Country |
|---|---|---|
| 523850 | May 2004 | SE |
| WO2006006934 | Jan 2006 | SE |
| EP2065513 | Jun 2009 | SE |
| Number | Date | Country | |
|---|---|---|---|
| 20120216971 A1 | Aug 2012 | US |
