SE453673B - SEE CONTINUOUS COOKING TO HEAT THE FIBER MATERIAL AT THE COOKER'S TOP - Google Patents
SEE CONTINUOUS COOKING TO HEAT THE FIBER MATERIAL AT THE COOKER'S TOPInfo
- Publication number
- SE453673B SE453673B SE8503282A SE8503282A SE453673B SE 453673 B SE453673 B SE 453673B SE 8503282 A SE8503282 A SE 8503282A SE 8503282 A SE8503282 A SE 8503282A SE 453673 B SE453673 B SE 453673B
- Authority
- SE
- Sweden
- Prior art keywords
- digester
- steam
- liquid
- temperature
- fibrous material
- Prior art date
Links
Classifications
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C7/00—Digesters
- D21C7/10—Heating devices
Landscapes
- Paper (AREA)
- Polysaccharides And Polysaccharide Derivatives (AREA)
- Treatments For Attaching Organic Compounds To Fibrous Goods (AREA)
Description
453 673 av koklut, passerar fibermaterialet en avdragszon för kok- vätska, där en del av kokluten sugs ut ur kokaren och leds genom en värmeväxlare för indirekt temperaturjustering till exakt det för kokningen önskvärda temperaturläget, varefter kokluten cirkulerar tillbaks in i kokaren genom en ledning, som mynnar något över det ställe i kokaren där kokluten drogs ut. Genom att uppvärmningen av fibermaterialet i kokartoppen huvudsakligen sker medelst direkt tillsatt högtrycksànga, uppstår nackdelen att kokluten i kokaren späds ut med kondensat, vilket senare under processen leder till ett ökat energibehov, när kokluten skall indunstas och senare brännas för återvinning av kemikalier. Vidare förlo- rar man motsvarande mängd färskángkondensat, vilket leder till ökad belastning på matarvattenberedningen. 453 673 of cooking liquor, the fibrous material passes through a boiling zone extraction zone, where a part of the cooking liquor is sucked out of the digester and passed through a heat exchanger for indirect temperature adjustment to exactly the desired temperature for cooking, after which the cooking liquor circulates back into the digester which opens slightly over the place in the boiler where the cooking liquor was drawn out. Because the fibrous material in the top of the cooker is heated mainly by means of directly added high-pressure steam, the disadvantage arises that the cooking liquor in the boiler is diluted with condensate, which later in the process leads to an increased energy requirement. Furthermore, the corresponding amount of fresh steam condensate is lost, which leads to an increased load on the feed water preparation.
Uppfinningen syftar därför till att avskaffa ovanstå- ende nackdelar genom att generera ånga från den nyss nämnda temperaturjusteringscirkulationen eller från en speciellt anordnad mindre cirkulation enbart för ånggenerering, och att använda denna ånga till uppvärmning i kokartoppen.The invention therefore aims to eliminate the above-mentioned disadvantages by generating steam from the temperature adjustment circulation just mentioned or from a specially arranged smaller circulation only for steam generation, and to use this steam for heating in the boiler top.
Färskångtillsättningen sker då i stället till en ånggenera- tor, där kondensatet tas tillvara. Uppfinningen skall nedan beskrivas i detalj under hänvisning till bifogade figur.The addition of fresh steam then takes place instead to a steam generator, where the condensate is utilized. The invention will be described in detail below with reference to the accompanying figure.
I figuren är visat övre delen av en kokare 10, en värmeväxlare 20 och en ångomformare 30. Till kokarens topp anländer fibermaterialet suspenderat i vätska, såsom antytt med pilen 14, från föregående utrustning, som kan vara ett ej visat förimpregneringskärl eller en högtryckskik för matning. I kokarens topp är anordnat en separationsanord- ning 11, där fibermaterialet skiljs från vätskan och faller ned i kokaren till en nivå 18. Vätskan returneras till den föregående utrustningen, som antytt med pilen 15. I kokaren upprätthålls en vätskenivå 13 över vilken det från separationsanordningen 11 nedfallande fibermaterialet befinner sig i ängatmosfär. Ångan tillsättes kokartoppen så 4. 453 673 som antytt med pilen 16. Ett stycke under vätskenivàn 13 är i kokarens vägg anordnat ett silparti 12, där vätska kan avdragas kokaren genom ledningen 17. Den avdragna vätskan fördelar sig i lämpliga förhållanden dels till värmeväxlaren 20, som antytt med pilen 21, och dels till àngomformaren 30, som antytt med pilen 22. Till värmeväxlaren 20 och àngomformaren 30 tillsätts högtrycksánga, som antytt med pilen 31, som fördelar sig genom ledningarna 32 och 33 till nämnda anordningar, som antytt med pilarna 34 respektive 35.The figure shows the upper part of a digester 10, a heat exchanger 20 and a steam converter 30. The fibrous material suspended in liquid, as indicated by the arrow 14, from the previous equipment arrives at the top of the digester, which may be a pre-impregnation vessel (not shown) or a high pressure feed. . A separation device 11 is arranged in the top of the digester, where the fibrous material is separated from the liquid and falls into the digester to a level 18. The liquid is returned to the previous equipment, as indicated by the arrow 15. In the digester a liquid level 13 is maintained above which from the separation device The precipitating fibrous material is in a meadow atmosphere. The steam is added to the boiler top as 4. 453 673 as indicated by the arrow 16. A piece below the liquid level 13 is arranged in the boiler wall a sieve portion 12, where liquid can be drawn off the boiler through the line 17. The drawn liquid is distributed in suitable conditions partly to the heat exchanger 20, as indicated by the arrow 21, and partly to the steam converter 30, as indicated by the arrow 22. High pressure steam is added to the heat exchanger 20 and the steam converter 30, as indicated by the arrow 31, which is distributed through the lines 32 and 33 to said devices, as indicated by the arrows 34 respectively 35.
Kondensatet från anordningarna 20 och 30 samlar sig, som antytt med pilarna 36 och 37, till en gemensam utgående mängd 38. Den i ångomformaren 30 bildade ångan lämnar denna genom ledningen 39 och tillsätts kokartoppen, som antytt med pilen 16. Den del av vätskan 22, som inte ombildas till ånga i ångomformaren 30, lämnar denna genom ledningen 40 och sammanförs med i värmeväxlaren 20 uppvärmd vätska i led- ningen 23 till ledningen 41, som fortsätter in i kokaren och mynnar, som antytt med pilen 42, i centrum av denna något över silpartiet 12, där vätskan ursprungligen drogs av kokaren. Som ett alternativ kan den överblivna vätskan i ledningen 40 värmeväxlas till lämplig temperatur för införande i kokaren genom ledningen 41 i stället för att ta en del 21 av den avdragna vätskan i ledningen 17 till värmeväxlaren 20.The condensate from the devices 20 and 30 collects, as indicated by the arrows 36 and 37, to a common output quantity 38. The steam formed in the steam converter 30 leaves it through the line 39 and is added to the boiler top, as indicated by the arrow 16. The part of the liquid 22 , which is not converted to steam in the steam converter 30, leaves it through the line 40 and is combined with liquid heated in the heat exchanger 20 in the line 23 to the line 41, which continues into the digester and opens, as indicated by the arrow 42, in the center thereof. slightly above the screen portion 12, where the liquid was originally drawn by the digester. Alternatively, the remaining liquid in line 40 may be heat exchanged to a suitable temperature for introduction into the digester through line 41 instead of taking a portion 21 of the withdrawn liquid in line 17 to the heat exchanger 20.
Uppfinningen fungerar på följande sätt. Konventio- nellt har man i kokare, där man önskar efterjustera tempera- turen medelst avdrag av vätska genom silpartiet 12 endast värmeväxlaren 20 inkopplad, där upphettning av en lämplig mängd med kokvätska uppvärms och cirkulerar tillbaka till kokarens mitt vid pilen 42, där den sprider sig utåt mot kokarens periferi samtidigt som hela kokarinnehàllet av fibermaterial rör sig kontinuerligt i en långsam rörelse ned mot kokarens botten, där det matas ut ur denna. Uppvärm- ningen av det till kokaren vid pilen 14 ankommande fiber- materialet sker då medelst tillsättning av högtrycksànga vid 453 673 pilen 16. Härvid kommer kokarvätskan att spädas ut med kondensat, så som kommer att visas nedan med angivna exem- pel.The invention works in the following way. Conventionally, in boilers where it is desired to readjust the temperature by subtracting liquid through the sieve portion 12, only the heat exchanger 20 is connected, where heating of a suitable amount of cooking liquid is heated and circulated back to the center of the digester at arrow 42, where it spreads. outwards towards the periphery of the digester at the same time as the entire digester content of fibrous material moves continuously in a slow movement down towards the bottom of the digester, where it is discharged from it. The heating material arriving at the digester at arrow 14 is then heated by adding high-pressure steam at 453 673 arrow 16. The digester liquid will then be diluted with condensate, as will be shown below with the examples given.
Enligt uppfinningen tar man en del av den kokvätska, som lämnar kokaren genom ledning 17, till àngomformaren 30 och bildar där tillräcklig ånga genom ledningen 39 och till pilen 16 för att åstadkomma den nödvändiga uppvärmningen av det inkommande fibermaterialet i stället för att som ovan här använda färsk ånga från fabrikens ángnät. På detta sätt kommer kondensatet 37 att tas till vara pá lämpligaste sätt i matarvattenberedningen i stället för att det som i konven- tionella system kommer att späda ut kokvätskan i själva kokaren.According to the invention, a portion of the cooking liquid leaving the digester through line 17 is taken to the steam converter 30 and there is formed sufficient steam through line 39 and to the arrow 16 to provide the necessary heating of the incoming fibrous material instead of using as above fresh steam from the factory's steam network. In this way, the condensate 37 will be used in the most suitable way in the feed water preparation instead of what in conventional systems will dilute the cooking liquid in the boiler itself.
Exempel 1 För att uppnå en normal temperatur i kokartoppen på ca 165°C måste i vanliga fall beroende på systemutformning 0.2 - 0.45 ton ånga per lufttorrt ton producerad massa till- sättas som direktánga, d.v.s. för en normalstor anläggning på 800 ton/24h blir àngförbrukningen upp till 350 ton/24h.Example 1 In order to achieve a normal temperature in the boiler top of approx. 165 ° C, depending on the system design, 0.2 - 0.45 tonnes of steam per air-dry tonne of mass produced must be added as direct steam, i.e. for a normal-sized plant of 800 tonnes / 24h, the steam consumption will be up to 350 tonnes / 24h.
Trycket i kokartoppen kan härvid vara 600-800 kPa. För att något lägre i kokartoppen, under vätskenivån, justera tempe- raturen till en normal koktemperatur på ca 167°C dras i förekommande fall av en vätskemängd på ca 4800 l/min, som uppvärms i en indirekt värmeväxlare och återförs tillbaka till kokaren något högre än avdraget, så att temperaturen justeras uppåt till den önskvärda ca 167°C.The pressure in the cooker top can be 600-800 kPa. In order to adjust the temperature slightly below the liquid level, below the liquid level, to a normal boiling temperature of approx. 167 ° C, a liquid volume of approx. 4800 l / min is drawn, which is heated in an indirect heat exchanger and returned to the digester slightly higher. than the deduction, so that the temperature is adjusted upwards to the desired approx. 167 ° C.
Exempel 2 I ett motsvarande fall som i exempel 1 produceras enligt uppfinningen ånga av en del av den avdragna vätske- mängden pà ca 4800 l/min i en ànggenerator tillräckligt för att öka temperaturen pá den inkommande vätskan från ca 147°C m 453 675 till i första hand ca 16500. Med en ångförbrukning som nämnt i exempel'1 på 0.2 - 0.45 ton/ADMT ökar kondensatåter- vinningen med upp till 350 t/24h. Det blir således en betydande mängd kondensat som inte hamnar i kokaren utan används på lämpligt sätt inom fabriken ifråga, vilket inne- bär en betydande ekonomisk vinst i indunstningsavdelning och i matarvattenhantering.Example 2 In a similar case as in Example 1, steam is produced from a portion of the withdrawn liquid amount of about 4800 l / min in a steam generator sufficient to increase the temperature of the incoming liquid from about 147 ° C m to 453 675 to primarily approx. 16500. With a steam consumption as mentioned in example '1 of 0.2 - 0.45 tonnes / ADMT, condensate recovery increases by up to 350 t / 24h. There will thus be a significant amount of condensate that does not end up in the boiler but is used in a suitable way within the factory in question, which means a significant financial gain in the evaporation department and in feed water management.
Claims (5)
Priority Applications (8)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
SE8503282A SE453673B (en) | 1985-07-02 | 1985-07-02 | SEE CONTINUOUS COOKING TO HEAT THE FIBER MATERIAL AT THE COOKER'S TOP |
FI862564A FI80084C (en) | 1985-07-02 | 1986-06-17 | Put on steam / liquid phase boiler for cellulose pulp |
NO862425A NO166417C (en) | 1985-07-02 | 1986-06-18 | PROCEDURE FOR OPERATING A CELLULOSE PLANT. |
DE19863621120 DE3621120A1 (en) | 1985-07-02 | 1986-06-24 | METHOD FOR TREATING CELLULOSE MATERIAL IN A STEAM LIQUID PHASE STOVE |
AT174886A AT392496B (en) | 1985-07-02 | 1986-06-27 | METHOD FOR TREATING CELLULOSE MATERIAL IN A CELLULOSE Digestion Plant |
FR8609542A FR2584433A1 (en) | 1985-07-02 | 1986-07-01 | Process employed in a plant for cooking cellulose |
BR8603064A BR8603064A (en) | 1985-07-02 | 1986-07-01 | PROCESS TO DIGIT CELLULOSE PULP IN A STEAM / LIQUID PHASE DIGESTOR |
JP15430186A JPS626991A (en) | 1985-07-02 | 1986-07-02 | Digestion of cellulose pulp by steam/liquid phase |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
SE8503282A SE453673B (en) | 1985-07-02 | 1985-07-02 | SEE CONTINUOUS COOKING TO HEAT THE FIBER MATERIAL AT THE COOKER'S TOP |
Publications (3)
Publication Number | Publication Date |
---|---|
SE8503282D0 SE8503282D0 (en) | 1985-07-02 |
SE8503282L SE8503282L (en) | 1987-01-03 |
SE453673B true SE453673B (en) | 1988-02-22 |
Family
ID=20360776
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
SE8503282A SE453673B (en) | 1985-07-02 | 1985-07-02 | SEE CONTINUOUS COOKING TO HEAT THE FIBER MATERIAL AT THE COOKER'S TOP |
Country Status (8)
Country | Link |
---|---|
JP (1) | JPS626991A (en) |
AT (1) | AT392496B (en) |
BR (1) | BR8603064A (en) |
DE (1) | DE3621120A1 (en) |
FI (1) | FI80084C (en) |
FR (1) | FR2584433A1 (en) |
NO (1) | NO166417C (en) |
SE (1) | SE453673B (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4944840A (en) * | 1988-01-14 | 1990-07-31 | Ahlstromforetagen Svenska Ab | Method and apparatus for evaporating waste liquor produced when cooking fibrous material containing cellulose |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FI82079C (en) * | 1989-04-27 | 1993-05-11 | Poeyry Jaakko & Co Oy | Foerfarande och anordning Foer kontinuerlig kokning av Cellulosa |
SE518993E (en) * | 2002-01-24 | 2013-04-23 | Metso Paper Sweden Ab | Preparation of cellulose pulp by boiling with a boiling liquid containing evaporated black liquor |
SG136850A1 (en) * | 2006-04-25 | 2007-11-29 | Itef Singapore Pte Ltd | Method of manufacturing cellulose acetate, high temperature steam reactor vessel used in the same method, and superheated steam generator used in the same method |
FI122983B (en) * | 2009-02-09 | 2012-09-28 | Andritz Inc | A process for steam generation at a pulp mill digester |
CN103451987B (en) * | 2013-08-23 | 2015-10-28 | 湖南骏泰浆纸有限责任公司 | A kind of dissolving pulp pre-hydrolyzed solution extracting method and device |
SE539449C2 (en) * | 2015-11-16 | 2017-09-26 | Valmet Oy | Method for heating cellulosic material to full cooking temperature in digesters |
FI20165470A (en) | 2016-06-06 | 2017-12-07 | Andritz Oy | A process for producing chemical pulp at a pulp mill digester |
Family Cites Families (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE1080848B (en) * | 1958-02-06 | 1960-04-28 | Escher Wyss Gmbh | Device for the continuous digestion of fibrous vegetable substances in the pulp industry |
DE1096181B (en) * | 1958-07-02 | 1960-12-29 | Kamyr Ab | Process and device for utilizing the heat of the waste liquor in the continuous digestion of pulp-containing raw materials under pressure |
AT262046B (en) * | 1962-10-20 | 1968-05-27 | Dominion Tar & Chemical Co | Process for maintaining the water balance in an impregnation system |
JPS519401A (en) * | 1974-07-15 | 1976-01-26 | Oodeio Enjiniaringu Kk | DENCHIKUYOTOONAAMUNO JOGEHOKOKAITENJUKUSHIJISOCHI |
NZ191061A (en) * | 1978-07-27 | 1982-03-16 | Obbola Linerboard Ab | Chemical pulp manufacture cellulosic material preheated by steam in a storage container |
PT71072A (en) * | 1979-04-11 | 1980-05-01 | Rosenblads Patenter Ab | Method for secondary heat recovery in batchwise cellulose digesting |
-
1985
- 1985-07-02 SE SE8503282A patent/SE453673B/en not_active IP Right Cessation
-
1986
- 1986-06-17 FI FI862564A patent/FI80084C/en not_active IP Right Cessation
- 1986-06-18 NO NO862425A patent/NO166417C/en unknown
- 1986-06-24 DE DE19863621120 patent/DE3621120A1/en active Granted
- 1986-06-27 AT AT174886A patent/AT392496B/en not_active IP Right Cessation
- 1986-07-01 BR BR8603064A patent/BR8603064A/en not_active IP Right Cessation
- 1986-07-01 FR FR8609542A patent/FR2584433A1/en active Granted
- 1986-07-02 JP JP15430186A patent/JPS626991A/en active Pending
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4944840A (en) * | 1988-01-14 | 1990-07-31 | Ahlstromforetagen Svenska Ab | Method and apparatus for evaporating waste liquor produced when cooking fibrous material containing cellulose |
Also Published As
Publication number | Publication date |
---|---|
DE3621120A1 (en) | 1987-01-15 |
FI80084C (en) | 1990-04-10 |
ATA174886A (en) | 1990-09-15 |
NO166417B (en) | 1991-04-08 |
FR2584433B1 (en) | 1994-04-22 |
NO862425D0 (en) | 1986-06-18 |
SE8503282D0 (en) | 1985-07-02 |
AT392496B (en) | 1991-04-10 |
NO862425L (en) | 1987-01-05 |
FI862564A0 (en) | 1986-06-17 |
JPS626991A (en) | 1987-01-13 |
SE8503282L (en) | 1987-01-03 |
NO166417C (en) | 1991-07-17 |
FI862564A (en) | 1987-01-03 |
FI80084B (en) | 1989-12-29 |
FR2584433A1 (en) | 1987-01-09 |
DE3621120C2 (en) | 1987-05-27 |
BR8603064A (en) | 1987-02-17 |
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