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(11) | EP 0 517 689 B1 |
| (12) | EUROPEAN PATENT SPECIFICATION |
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| (54) |
A method of producing kraft pulp Ein Verfahren zur Herstellung von Kraftpulpe Un procédé de fabrication de pâte kraft |
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| Note: Within nine months from the publication of the mention of the grant of the European patent, any person may give notice to the European Patent Office of opposition to the European patent granted. Notice of opposition shall be filed in a written reasoned statement. It shall not be deemed to have been filed until the opposition fee has been paid. (Art. 99(1) European Patent Convention). |
BACKGROUND AND SUMMARY OF THE INVENTION
[0001] The present invention relates to a method of producing kraft pulp by cooking comminuted cellulosic fibrous material with white liquor to produce kraft pulp and black liquor, whereby
(a) a slurry of cellulosic fibrous material is treated in a plurality of consecutive stages with white liquor, including at least first and second stages, using a first supply of white liquor to the first stage and a second supply to the second stage, the first supply of white liquor having a sulfur content greater than the sulfur content of the second supply of white liquor;
(b) the material treated with white liquor is subjected to cooking conditions in at least one of the stages to effect kraft cooking thereof, and black liquor is produced.
[0002] For many years it has been known that a higher sulfide concentration in white liquor for kraft pulping in the pulp and paper industry (i.e. higher white liquor sulfur content) could produce kraft pulp with higher viscosity and better physical properties. It has also been known that the beneficial effect of higher white liquor sulfur content is more profound in the early stages of the kraft cook than in the later stages (S. Nordén and A. Teder, Tappi, vol. 62, no. 7, July 1979, p. 49-51; B. Johannson et al, Svensk Papperstidning no. 10, 1984, p. 30-35). For improving the conditions in the initial phase S. Nordén and A. Teder describe to use two separate white liquors with different sulfidities. The higher-sulfidity liquor can be used in the impregnation and the lower-sulfidity liquor introduced later, e.g. in the transfer circulation or in the first pulping circuit. It is well-known, as dislosed in J.P. Casey "Pulp and Paper"; Chemistry and Chemical Technology 3rd ed., vol. I, 1980, John Wiley & Sons, New York, p. 470-476, that sulfur-containing gases are released during the digester relief and blow, from condensate stripping, and from other sources.
[0003] Several methods, including absorption in white liquor, has been proposed to treat said gases. However in the past there have been a number of technical and practical concerns and conditions which have precluded practical utilization of these concepts. Similarly maximum utilization has not been commercially made of the known ability of polysulfide to stabilize carbohydrates and wood against degradation during chemical pulping by oxidatively converting the reducing end groups in celluloses and hemi-cellulose to carboxylic groups (US-A-2,944,928).
[0004] According to the present invention, a method of producing kraft pulp from cellulosic comminuted fibrous material utilizing white liquor, as described above, is provided. The invention is thereby characterized by the following steps: (c) sulfur from the black liquor is recovered by heating the black liquor to produce sulfur-containing off gases; and (d) the recovered sulfur is added to a stream of white liquor made from the remaining black liquor to increase the sulfur content thereof thereby producing said first supply of white liquor deriving from said remaining black liquor.
[0005] In a preferred embodiment of the inventive method the off gases are treated to produce primarily methane and hydrogen sulfide. Preferably the hydrogen sulfide from the treated off gases is fed to a scrubber in which it is brought into contact with white liquor, thereby producing said first supply of white liquor so that an optimum viscosity/kappa ratio can be achieved.
[0006] According to the most specific aspects of the present invention, the concepts described above are utilized in a practical manner to provide kraft pulp that has an optimum viscosity/kappa ratio, and/or good strength properties, and with good yield. The invention is applicable to a wide variety of different kraft cooking processes, both batch and continuous. For example the invention can be utilized in continuous digesters having an impregnation zone, or in cooking systems utilizing a separate impregnation vessel from the continuous digester, or in batch digester. The invention can also be utilized in association with co-current movements of white liquor with the pulp, or countercurrent movements, such as are provided in the commercial digesting process marketed by Kamyr, Inc. of Glens Falls, New York under the trademark "MCC".
[0007] White liqour is that treatment liquid in a kraft process which contains the active cooking chemicals, sodium hydroxide (NaOH) and sodium sulfide (Na2S); or white liquor in an extreme situation may contain substantially only NaOH as active ingredient. According to standard practice, the white liquor sulfur content in the cook is maintained in the range of 25-35 % (this overall sulfur content ratio is the amount of sodium sulfide to the sum of sodium sulfide and sodium hydroxide applied to the whole cooking process), and according to standard practice in the art, a sulfur content level below 15 % results in a deterioration in the cooking rate and pulp quality. During the production of kraft pulp, residual or "black liquor" containing the reaction products of lignin solublization is whithdrawn from the digester, concentrated, and burned in a recovery furnace to yield an inorganic smelt of sodium carbonate and sodium sulfide. The smelt is dissolved to form green liquor which is reacted with quick lime (CaO) to convert the sodium carbonate into sodium hydroxide and thereby regenerate the original white liquor.
[0008] According to the present invention, it has been found that by making two (or more) supplies or streams of white liquor, with different sulfur contents, and applying them to different portions in the kraft cycle, significantly improved results can be achieved. In fact it has been found that it is highly desirable to add the majority of the sulfide in the total white liquor (total cooking chemical) -- at least about 60-90 %, in fact even almost all the sulfide -- at the initial stages (e.g. impregnation) of the kraft cycle, while adding white liquor with primarily only sodium hydroxide at the later stages (e.g. co-current or countercurrent cooks). Practicing the invention, it is possible to optimize the viscosity/kappa ratio of the produced pulp for any given level of sulfur content, and/or to optimize pulp strength properties. The increase can be dramatic, easily on the order of 25 % for conventional cooks with multiple white liquor additions (co-current), about the same increase for modified continuous cooking (MMC™), and 15 % or more for extended modified continuous cooking (EMMC™). Comparable increases occur for batch treatment too.
[0009] When about 2 % polysulfide on wood, expressed as elemental sulfur, is provided in the white liquor, a yield equal to kappa 18-20 for a conventional kraft cook is produced with a kappa of about 12.5, and pulp with a viscosity comparable to conventional cook kraft pulp at a kappa of about 26 is produced. Elemental sulfur (in dry or slurry form) may be used instead of polysulfide; elemental sulfur is about 60-75 % as effective as polysulfide.
[0010] While the exact source of the sulfur for producing the high sulfur content stream or supply of white liquor according to the invention is not critical as long as the sulfur is recovered according to step (c) of claim 1, one exceptionally good source that allows a practical, industrial scale process to be practiced is that shown in US-A-4,929,307 wherein sulfate black liquor is heated to above the cooking temperature so as to split the macro-molecular lignin fraction, to produce sulfur-containing off gases. Those off gases are favourably reacted to produce primarily methane and hydrogen sulfide, and then brought into contact with sulfur depleted white liquor from the normal chemical manufacturing facility of the pulp mill, to produce an extremely high sulfur content white liquor, the hydrogen sulfide being selectively absorbed into the white liquor. That high sulfur content white liquor may then be acted upon to produce at least some significant portions of polysulfide, and then utilized in early stages of the kraft cook.
[0011] The cooking liquor utilized above is a kraft cooking liquor. It may contain anthraquinone or its derivatives or equivalents, or the like, and the first liquor may be targeted to an impregnation stage, co-current cook stage, or countercurrent cook stage.
[0012] It is the primary object of the present invention to provide a substantially improved cook cycle for the production of paper pulp. This and other objects of the invention will become clear from an inspection of the detailed description of the invention, and from the appended claims.
BRIEF DESCRIPTION OF THE DRAWING
[0013] FIGURE 1 is a schematic view of exemplary apparatus for practicing an exemplary method according to the present invention.
DETAILED DESCRIPTION OF THE DRAWING
[0015] In a typical kraft pulping process, as illustrated in FIGURE 1, a digester 12 -- which preferably is a continuous digester such as that sold by Kamyr, Inc. of Glens Falls, New York, but may be a batch digester -- has a stream of off gases 13, and black liquor (residual white liquor containing the reaction products of lignin solubilization) is withdrawn at an intermediate position as indicated at 14, while the kraft pulp produced is discharged at 15. When the black liquor in line 14 is discharged, it may be passed directly to black liquor evaporators, and preferably it is subjected, somewhere in the evaporator chain, to a heat treatment process at step 17 to produce off gases in line 18. The heat treatment of block 17 is preferably that described in US-A-4,929,307. After heat treatment at 17 the black liquor passes to evaporators 19 (evaporator 19' may concentrate the black liquor before heat treatment 17 too), which also produce off gases in line 20, then to a conventional recovery boiler 22, with conventional white liquor manufacture at block 23, to produce white liquor in line 24 having depleted sulfur content.
[0016] The off gases in 18 -- which may include only those from the heat treatment 17, or also those from the digester line 13, only and from the black liquor evaporators in line 20, or a combination of any two of them -- are preferably first subjected to a drying or absorption stage (as indicated schematically at 27 in FIGURE 1) in order ro remove a majority of the water vapor. The removal of the water vapor increases the concentration of organic sulfur gases. Step 27 is accomplished by drying the gas stream by any conventional means and/or by absorbing or adsorbing the organic portion of the gas onto a solid, or additionally by absorbing the off gas into one of any non-polar liquids (e.g.kerosene or mineral oil). Treatment may be provided of a liquid mixture, but preferably according to the invention further treatment is of the concentrated gas.
[0017] The next steps in the treatment of the off gases as illustrated in FIGURE 1 are to add hydrogen, and the pass the gas in the presence of the added hydrogen past a hydrogen desulfurization catalyst. This may be accomplished, for example, in the hydrogen desulfurization (HDS) unit 28, with the hydrogen gas from line 29 added to the unit 28 along with the gas in line 18. The hydrogen gas in line 29 can come from any source (e.g. be purchased, from water electrolysis, etc.). It is preferred that the hydrogen desulfurization catalyst consist essentially of a transition metal-molybdenum alloy, particularly a nickel molybdenum or cobalt molybdenum alloy.
[0018] Typically, in gaseous processing, the product gas stream in line 30 is further acted upon. The gas stream in line 30 contains primarily methane, and hydrogen sulfide, with hydrogen also present. Preferably the hydrogen sulfide is then separated out from the gas in stream 30. While the hydrogen sulfide may be separated as a gas and then used in its gaseous form in conventional pulping techniques, it may be fed to a scrubber 32 in which it is brought into contact with a caustic solution, preferably kraft white liquor, which contains sodium hydroxide and most likely at least some sodium sulfide. While in the preferred embodiment illustrated in the drawings white liquor is utilized, under some circumstances green liquor may be advantageously utilized, with white liquor subsequently made from the green liquor.
[0019] White liquor from line 24 is passed into inlet 33 of scrubber 32, the hydrogen sulfide being absorbed in the white liquor and thereby significantly enhancing its sulfur content. The significantly enhanced sulfur content white liquor then passes through the outlet 34 of the scrubber into line 35, to be used in the pulping process. Desirably, the white liquor in line 35 passes through a polysulfide treatment stage, as illustrated at 36, and then to the impregnation vessel 37 (if a separate impregnation vessel is used) or the like, to be utilized in the pulping cycle. Elemental sulfur may be added at 36 instead of polysulfide.
[0020] The gas stream that remains, in line 38, contains primarily methane, but also some hydrogen. Ultimately, the gas in line 38 may become the source of the hydrogen for line 29.
[0021] According to the invention, the high sulfur content white liquor in line 35 is provided at an early stage of the cook, e.g. at the beginning of the impregnation vessel 37, or impregnation stage if impregnation takes place in the digester 12 itself, or at multiple places in the impregnation zone and/or vessel 37. A countercurrent impregnation flow may be provided, in which case the higher sulfur content liquor is added near the end of the impregnation stage. Part of the sulfide depleted white liquor in line 24 is passed into line 41, and it is then introduced into the cook, preferably at multiple locations, as indicated at 42 and 43 in FIGURE 1.
[0022] According to the invention, where the low sulfur content white liquor in line 41 is introduced into the kraft cook may vary widely. For example, it may be added to the middle of the impregnation vessel 37, at one, two, or more co-current stages in the digester 12, or at one, two, or more countercurrent stages in the digester 12 (e.g. for modified continuous cooking, or extended modified continuous cooking). Of course, the liquor in line 41 may also be utilized in a batch process.
[0023] While the drawing illustrates only two streams or supplies of white liquor, 35, 41, having different sulfur content, as many different sulfur content streams as desired may be produced. For example two series connected units 32 may be utilized, the first producing the highest sulfur content level white liquor, while the second produces an intermediate (between lines 35 and 41) sulfur content level white liquor. The intermediate sufidity white liquor is added earlier in the cook than the white liquor in line 41.
[0024] The relative amount of sulfur content of the white liquor added at various stages within the kraft cycle may also be varied widely according to the invention. For example, if the kraft pulping process is to be a multi-level conventional cook, that is white liquor is added at two or more points in the cook and flows co-currently with the pulp, then about 60% of the total cooking chemical is added to the impregnation vessel (e.g. in line 35), while about 25% is added to the first co-current stage (e.g. at 42) and about 15% to the second co-current stage (e.g. at 43). In this procedure, preferably the amount of sulfide provided in line 35 is about 60-90%, and if practical may be almost 100% of the total sulfide in all of the white liquor streams, that is the white liquor in stream 41 is substantially fully sulfide depleted. The stream in line 35 in this embodiment may be generated by passing 35-65% of the total volume of white liquor through the unit 32, the remaining 65-35% of the white liquor being added through line 41. According to another embodiment, about 35% of the total volume of white liquor is passed through unit 32, and this high sulfur content white liquor is then added to the top circulation in the conventional impregnation vessel 37. The sulfide-depleted white liquor in line 41 is added to middle circulation in the vessel 37 in the amount of about 25-35% of the total cooking chemical from white liquor, while about 20-25% of the total cooking chemical, in the sulfide depleted white liquor in line 41, is added to the continuous digester 12 first cooking circulation.
[0025] The low sodium sulfide content liquor in line 41 may also be added at 44 to an oxygen delignification or bleaching stage 45 as a source of sodium hydroxide.
[0026] When utilizing the multiple level sulphidity white liquors according to the invention in modified continuous cooking and extended modified continuous cooking sequences, the viscosity to kappa ratio may be increased by about 0.2-0.3 units if almost all sulfide is added to the impregnation stage (e.g. in line 35 to vessel 37). Preferably at least about 60% (e.g. 60-90%) of the total sulfur content is added in the impregnation stage (line 35), the total volume of white liquor added in line 35 being about 40-65% of the total volume of white liquor used in the pulping process.
[0027] In stage 36, polysulfide is added to the white liquor. For example, this can be done by the MOXY (TM) process in which some of the sodium sulfide in the white liquor is partially oxidized to produce polysulfide, or by other known polysulfide processes. Alternatively, in stage 36 polysulfide from an external source may merely be introduced into the white liquor, e.g. polysulfide produced by reacting elemental sulfur with sulfide ions in an aqueous solution under proper conditions; or elemental sulfur may be added to the white liquor instead of polysulfide.
[0028] The amount of polysulfide produced, or added, in stage 36 is about 0.5%-8% on wood, expressed as elemental sulfur. Typically, about 2% polysulfide is desirable. If 2% polysulfide is used in conjunction with extended modified continuous cooking, a kraft pulp with a kappa of about 12.5, a viscosity of about 33.7 cp, and a yield of about 44.6% can be made. This yield is equal to that of a conventional cook or extended modified continuous cook pulp at a kappa of about 18-20 without polysulfide, and the viscosity is equivalent to that of a conventional cook pulp at kappa 26, or an extended modified continuous cook pulp at kappa 17.
[0029] If an amount of elemental sulfur equivalent to about 0.5-8% polysulfide is used, the results are about 60-75% as good as when polysulfide is used.
[0030] Utilizing the apparatus schematically illustrated in the drawings, various methods may be practiced according to the invention. According to one method:
(a) Two (or more) streams of white liquor, 35, 41, are made up, the first stream (35) having relatively high sulfur content, and the second (41) relatively low sulfur content (even approaching zero).
(b) Cellulosic comminuted fibrous material (e.g. wood chips) are impregnated with the first stream 35 (e.g. in vessel 37).
(c) The material is cooked under kraft cooking conditions, in a cooking zone (in vessel 12) with cooking chemicals (the sodium hydroxide and sodium sulfide in the white liquor) to produce kraft pulp.
(d) The second stream, 41, of white liquor is supplied to the cooking zone (e.g. digester 12) as cooking chemicals; and
(e) the kraft pulp is washed (e.g. in a wash zone in digester 12, and/or in a separate wash vessel).
[0031] According to another aspect of the invention, a slurry of wood chips is treated in a plurality of consecutive stages (e.g. impregnation stage, first and second co-current or countercurrent cooking stages) with white liquor using first and second supplies, differing in the sulfur content thereof. The chips are treated with white liquor under cooking conditions (e.g. in digester 12) in at least one stage, to effect kraft cooking thereof. Black liquor is withdrawn (at 14) and sulfur is recovered from the black liquor, as by heating treating it (at 17) according to the process of US-A-4,929,307, evaporating it (in 19), etc. (see 22 and 23 in FIGURE 1). The recovered sulfur is added to the first supply of white liquor, as in unit 32, to significantly increase the sulfur content thereof, so that the sulfur content of the liquor in line 35 is substantially greater than that in line 24 (which is sulfur depleted, and may be near zero). The relative sulfur contents of the white liquors in lines 35 and 24 are controlled so as to optimize the viscosity/kappa ratio and/or physical strength properties.
[0032] The invention allows advantageous production of kraft pulp to be practiced on an industrial scale -- that is, larger production than reasonably possible in a laboratory, with complete chemical recovery.
[0034] Tables IA-IE provide the results of laboratory batch cooks using split white liquor streams with variable sulfur content, according to the invention, and conventional cooks for comparison purposes. In these tables, "CK" means conventional kraft cooking, "MCK" means kraft cooking with multiple introductions of white liquor, with more than one co-current cooking stage, "MCC" refers to Kamyr, Inc.'s trademarked modified continuous cooking process in which multiple introductions of white liquor are provided, and a countercurrent cook stage, and "EMCC" refers to Kamyr, Inc.'s trademarked extended modified continuous cooking process in which a second countercurrent cook is provided.
[0035] Table II illustrates the advantages achieved when polysulfide is used. The liquid to wood ratio for all cooks in Table II is 4/1. "Sulfidity" refers to sodium sulfide content.
[0036] The wood utilized in all of TABLES IA-E and II is southern pine from the Mississippi area. However, the results are applicable to a wide variety of wood species.
TABLE II
| Cook number | A2961 | A2958 | A2962 | A2959 | A2960 | A2963 |
| Type | EMCC | EMCC | EMCC | MCK | MCK | EMCC |
| Polysulfide, % | 2 | 2 | 3 | 2 | 3 | nil |
| PRESTEAMING: | ||||||
| Time, min | 5 | 5 | 5 | 5 | 5 | 5 |
| Temperature, °C | 110 | 110 | 110 | 110 | 110 | 110 |
| IMPREGNATION: | ||||||
| Time, min | 30 | 30 | 30 | 30 | 30 | 30 |
| Temperature, °C | 110 | 110 | 110 | 110 | 110 | 110 |
| Pressure, kPa (psig) | 1034 (150) | 1034 (150) | 1034 (150) | 1034 (150) | 1034 (150) | 1034 (150) |
| Initial EA, % NaOH | 12 | 16 | 13 | - | - | 12 |
| Initial EA, % Na2O | - | - | - | 11.4 | 12.6 | - |
| Sulfidity, % on AA | 62.5 | 73.6 | 62.5 | 62.5 | 62.5 | 62.8 |
| 2nd EA @ 5 min, % NaOH | 2 | 2 | 2 | - | - | 2 |
| Residual EA, g/L Na2O | 13.6 | 22.0 | 14.4 | 15.9 | 15.7 | |
| Resid. polysulfide, g/L S° | 1.6 | 1.6 | 1.9 | 2.6 | - | |
| COCURRENT STAGE: | ||||||
| Total time, min | 61 | 60 | 60 | 73 | 75 | 60 |
| Max temperature, °C | 164 | 165 | 164 | 170 | 170 | 165 |
| Time at max, min | 45 | 45 | 45 | 45 | 45 | 45 |
| EA, % NaOH | 5 | 5 | 6 | - | - | 5 |
| EA, % Na2O | - | - | - | 4.75 | 5.25 | - |
| Sulfidity, % | 0 | 0 | 0 | 0 | 0 | 0 |
| Residual EA, g/L Na2O | 8.5 | 14.0 | 8.0 | 10.2 | 9.6 | |
| COCURRENT STAGE II: | ||||||
| Time, min. | - | - | 135 | 72 | - | |
| Temperature, °C | - | - | 170 | 170 | - | |
| EA, % Na2O | - | - | 2.85 | 3.15 | - | |
| Sulfidity, % | - | - | 0 | 0 | - | |
| COUNTERCURRENT STAGE: | ||||||
| Time, min | 240 | 240 | 240 | - | - | 240 |
| Temperature, °C | 164 | 160 | 164 | - | - | 165 |
| EA, % NaOH on wood | 15.3 | 15.4 | 15.4 | - | - | 15.4 |
| Sulfidity, % | 0 | 0 | 0 | - | - | 0 |
| EA, g/L as NaOH | 11.9 | 12.0 | 12.0 | - | - | 12.0 |
| Displacement, L/min. | 0.16 | 0.16 | 0.16 | - | - | 0.16 |
| Displaced volume, L | 38.4 | 38.4 | 38.4 | - | - | 38.4 |
| Displacement Residual : | ||||||
| @ 60 minutes, EA g/L Na2O | 6.9 | 10.4 | - | - | ||
| @ 120 minutes, EA g/L Na2O | 7.6 | 9.1 | - | - | ||
| Total Composite, EA g/L Na2O | 7.3 | 9.6 | - | - | ||
| END OF COOKING: | ||||||
| Residual EA, g/L NaOH | 10.0 | 10.0 | 12.4 | 13.4 | ||
| g/L Na2O | 7.7 | 7.8 | 9.6 | 10.4 | ||
| H factor | 2733 | 2239 | 2695 | 2947 | 1935 | |
| UNBLEACHED PULP: | ||||||
| Total yield, % | 45.5 | 44.6 | 43.5 | 45.6 | ||
| Rejects, % | 0.02 | <0.01 | <0.01 | <0.02 | ||
| Screened yield, % | 45.5 | 44.6 | 43.5 | 45.6 | ||
| Kappa, unscreened | 17.1 | 12.4 | 15.1 | 11.7 | 15.6 | |
| Kappa, screened | 16.9 | 12.6 | 11.7 | 14.6 | ||
| Kappa, screened (test 2) | 16.8 | 12.4 | 11.7 | 14.4 | ||
| Viscosity, 0.5% CED, cp | 42.4 | 33.7 | 23.6 | 32.3 | ||
| Viscosity, (test 2) | 43.7 | 34.5 | 22.0 | 32.4 | ||
| V/K, (test 1) | 2.51 | 2.67 | 2.02 | 2.21 |
[0037] As can be seen from the above examples, the method according to the invention optimizes the viscosity/kappa ratio and/or strength properties of kraft pulp produced, and achieves other advantageous results. The utilization of polysulfide or elemental sulfur as part of the sulfide content of the white liquor also significantly increases yield.
[0038] When using other lignin reaction enhancing or carbohydrate degradation slowing chemicals, such as anthraquinone or its derivatives or equivalents, or the like, significant increases in viscosity/kappa ratio or pulp strength properties can be obtained by targeting one cooking liquor to a specific stage (or stages) of the cook, while another cooking liquor is used in other portions.
1. A method of producing kraft pulp by cooking comminuted cellulosic fibrous material
with white liquor to produce kraft pulp (15) and black liquor (14), whereby
(a) a slurry of cellulosic fibrous material is treated in a plurality of consecutive stages with white liquor, including at least first and second stages (37,12), using a first supply (35) of white liquor to the first stage and a second supply (41) to the second stage, the first supply of white liquor having a sulfur content greater than the sulfur content of the second supply (41) of white liquor;
(b) the material treated with white liquor is subjected to cooking conditions in at least one of the stages (12) to effect kraft cooking thereof, and black liquor is produced; characterized in that
(c) sulfur from the black liquor (14) is recovered by heating (17) the black liquor to produce sulfur-containing off gases (18); and
(d) the recovered sulfur is added to a stream (24) of white liquor made from the remaining black liquor to increase the sulfur content thereof thereby producing said first supply (35) of white liquor deriving from said remaining black liquor.
2. A method in accordance with claim 1, characterized in that the off gases (18) are
treated to produce primarily methane and hydrogen sulfide.
3. A method in accordance with claim 2, characterized in that the hydrogen sulfide from
the treated off gases (30) is fed to a scrubber (32) in which it is brought into contact
with white liquor (24), thereby producing said first supply of white liquor (35).
1. Verfahren zur Herstellung von Kraftzellstofff durch Aufschluß von zerkleinertem zellulosehaltigem
Fasermaterial mit Weißlauge, um Kraftzellstoff (15) und Schwarzlauge (14) zu produzieren,
wobei
(a) eine Aufschlämmung zellulosehaltigen Fasermaterials in einer Vielzahl aufeinanderfolgender Stufen, einschließlich zumindest erster und zweiter Stufen (37, 12), unter Nutzung einer ersten Zufuhr (35) von Weißlauge zur ersten Stufe und einer zweiten Zufuhr (41) zur zweiten Stufe behandelt wird, welche erste Zufuhr von Weißlauge einen Schwefelgehalt hat, der größer als der Schwefelgehalt der zweiten Zufuhr (41) von Weißlauge ist;
(b) das mit Weißlauge behandelte Material Aufschlußverhältnissen in zumindest einer der Stufen (12) ausgesetzt wird, um Sulfataufschluß desselben zu bewirken, und Schwarzlauge produziert wird, dadurch gekennzeichnet, daß
(c) aus der Schwarzlauge (14) Schwefel durch Aufheizung (17) der Schwarzlauge zurückgewonnen wird, um schwefelhaltige Abgase (18) zu produzieren; und
(d) der zurückgewonnene Schwefel einem Strom (24) von Weißlauge zugesetzt wird, der aus der zurückbleibenden Schwarzlauge erzeugt ist, um den Schwefelgehalt desselben zu erhöhen, wodurch die erste von der zurückbleibenden Schwarzlauge abgeleitete Zufuhr (35) von Weißlauge entsteht.
2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Abgase (18) behandelt werden,
um hauptsächlich Methan und Schwefelwasserstoff zu produzieren.
3. Verfahren nach Anspruch 2, dadurch gekennzeichnet, daß der Schwefelwasserstoff aus
den behandelten Abgasen (30) einem Wäscher (32) zugeführt wird, wo es mit Weißlauge
(24) kontaktiert wird, wodurch die erste Zufuhr von Weißlauge (35) entsteht.
1. Procédé de fabrication de la pâte kraft par cuisson de la matière fibreuse cellulosique
désintégrée avec de la lessive blanche afin de produire de la pâte kraft (15) et de
la lessive noire (14), par lequel
(a) une suspension dense de la matière fibreuse cellulosique est traitée dans plusieurs stades consécutifs avec de la lessive blanche, y compris au moins les premier et seconde stades (37,12), utilisant un premier apport (35) de la lessive blanche au premier stade et un second apport (41) au second stade, le premier apport de la lessive blanche présentant une teneur en soufre supérieure à celle du second apport (41) de la lessive blanche;
(b) la matière traitée avec de la lessive blanche est soumise à des conditions de cuisson dans au moins un des stades (12) afin d'effectuer sa cuisson kraft, et on produit de la lessive noire;
caractérisé en ce que(c) du soufre issu de la lessive noire (14) est récupéré en chauffant (17) la lessive noire afin de produire des effluants gazeux contenant du soufre (18); et en ce que
(d) le soufre récupéré est versé dans un écoulement (24) de la lessive blanche réalisé à partir de la lessive blanche résiduaire afin d'augmenter sa teneur en soufre, produisant de ce fait ledit premier apport (35) de la lessive blanche dérivée de ladite lessive noire résiduaire.
2. Procédé selon la revendication 1, caractérisé en ce que les effluants gazeux (18)
sont traités de façon à produire principalement du méthane et du sulfure d'hydrogène.
3. Procédé selon la revendication 2, caractérisé en ce que le sulfure d'hydrogène issu
des effluants gazeux traités (30) est délivré dans un épurateur (32) à l'intérieur
duquel il est amené en contact avec de la lessive blanche (24), produisant de ce fait
ledit premier apport de la lessive blanche (35).