SE464921B - SAVED TO RECOVER CHEMICALS FROM MASS DEVICES - Google Patents
SAVED TO RECOVER CHEMICALS FROM MASS DEVICESInfo
- Publication number
- SE464921B SE464921B SE8702627A SE8702627A SE464921B SE 464921 B SE464921 B SE 464921B SE 8702627 A SE8702627 A SE 8702627A SE 8702627 A SE8702627 A SE 8702627A SE 464921 B SE464921 B SE 464921B
- Authority
- SE
- Sweden
- Prior art keywords
- reactor
- sulfur
- gas
- supplied
- oxygen
- 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
- D21C11/00—Regeneration of pulp liquors or effluent waste waters
- D21C11/12—Combustion of pulp liquors
- D21C11/125—Decomposition of the pulp liquors in reducing atmosphere or in the absence of oxidants, i.e. gasification or pyrolysis
Landscapes
- Paper (AREA)
Abstract
Description
464 921 10 15 20 25 30 bränning. Detta medför att både alkali och svavel till viss del avgår i gasfas. En lösning till denna problematik anvisas i den svenska patentskriften 83 02 245-0, vilken bygger på att man delar upp hela återvinningsprocessen i tre steg. Processen inleds med ett högtemperatursteg där svavel reduceras och avdrages i form av en smälta samti- digt som både alkali och organiskt material förgasas. 464 921 10 15 20 25 30 burning. This means that both alkali and sulfur are to some extent released in the gas phase. A solution to this problem is indicated in the Swedish patent specification 83 02 245-0, which is based on dividing the entire recycling process into three steps. The process begins with a high-temperature step where sulfur is reduced and removed in the form of a melt at the same time as both alkali and organic material are gasified.
I ett andra steg kondenseras alkali och övergår samtidigt i önskad form samt slutligen ett tredje steg där gasen från den organiska delen förbränns under samtidig energi- generering. Målsättningen med ovannämnda uppfinning är således att eliminera en efterföljande upparbetning av alkali.In a second step, alkali is condensed and simultaneously transforms into the desired form and finally a third step where the gas from the organic part is burned during simultaneous energy generation. The object of the above invention is thus to eliminate a subsequent work-up of alkali.
Ytterligare en process för återvinning av kokkemikalier från massaavlutar finns beskriven i SE 72 04 304-5. Meto- den bygger på att separera smälta och gas i en förreaktor.Another process for recycling cooking chemicals from pulp effluents is described in SE 72 04 304-5. The method is based on separating melt and gas in a pre-reactor.
I denna process är man helt beroende av den vid den par- tiella förbränningen utvecklade energin för att erhålla till- räckligt hög temperatur. I praktiken medför detta stora svårigheter. Drivs den partiella förbränningen inte till- räckligt långt blir temperatufen för låg för att garante- ra flamhållningen, drivs förbränningen för långt avgår både svavel och alkali till stor del med utgående gas.In this process, one is completely dependent on the energy developed during the partial combustion in order to obtain a sufficiently high temperature. In practice, this causes great difficulties. If the partial combustion is not driven far enough, the temperature becomes too low to guarantee the flame retention, if the combustion is driven too far, both sulfur and alkali are largely emitted with outgoing gas.
Ovannämnda problem och svårigheter löses nu vid det inled- ningsvis beskrivna sättet därigenom att en temperatur av 9000 till l100°C upprätthålles i reaktorn och att syrepo- tentialen styres genom en reglerad tillförsel av den syre- innehållande gasen och/eller det kolhaltiga materialet, varigenom i massaavluten ingående svavel reduceras och väsentligen all alkali och svavel binds i en smältfas, vilken smältfas separeras från gasfasen.The above-mentioned problems and difficulties are now solved in the manner initially described in that a temperature of 9000 to 1100 ° C is maintained in the reactor and that the oxygen potential is controlled by a regulated supply of the oxygen-containing gas and / or the carbonaceous material, whereby sulfur contained in the pulp effluent is reduced and substantially all of the alkali and sulfur are bound in a melt phase, which melt phase is separated from the gas phase.
Enligt föreliggande uppfinning delas àtervinningsprocessen 10 15 20 25 464 921 upp i tre separata steg. I första steget reduceras svavlet och avdrages tillsammans med massaavlutens oorganiska del i en smältfas under samtidig förgasning av den organiska delen. Detta steg optimeras för att erhålla en i det när- maste total separation av svavel- och alkali. I andra ste- get förbränns gasen under samtidig energigenerering. Det- ta kan ske på många sätt och för många ändamål men då det är helt skiljt från âtervinningen kan det enkelt sub- optimeras. I det tredje steget sker en konventionell upp- arbetning av alkali till önskvärd form.According to the present invention, the recycling process 10 464 464 is divided into three separate steps. In the first step, the sulfur is reduced and withdrawn together with the inorganic part of the pulp liquor in a melting phase while simultaneously gasifying the organic part. This step is optimized to obtain an almost total separation of sulfur and alkali. In the second stage, the gas is burned during simultaneous energy generation. This can happen in many ways and for many purposes, but since it is completely separate from recycling, it can easily be sub-optimized. In the third step, a conventional reprocessing of alkali takes place to the desired shape.
Lämpligen utgöres den tillförda gasen av luft och utgör bärare av till reaktorn tillförd extra värmeenergi.Suitably the supplied gas consists of air and constitutes a carrier of extra heat energy supplied to the reactor.
Alternativt kan den externa energin tillföras i form av en i en plasmagenerator upphettad energirik gas.Alternatively, the external energy can be supplied in the form of an energy-rich gas heated in a plasma generator.
Lämpligen binds härvid 95% till 100% av all alkali och svavel i en smältfas.Preferably, 95% to 100% of all alkali and sulfur are bound in a melt phase.
Genom att man vid det uppfinningsenliga sättet, i likhet med det koncept som anvisas genom SE 83 02 245-9, anvisar utnyttjandet av en från förbränning oberoende energitill- sats, har man helt kunnat eliminera de tidigare nämnda prob- lem som uppträder vid ett förfarande enligt SE 72 04 304-5.By the method according to the invention, similar to the concept instructed by SE 83 02 245-9, by directing the use of an energy additive independent of combustion, it has been possible to completely eliminate the previously mentioned problems which occur in a process. according to SE 72 04 304-5.
I det specifika utförandet med plasmagenerator har det ovän- tat visat sig att reaktionshastigheten för förgasningen av tjockluten är mycket hög, varför reaktorn kan utformas specifikt för att ge maximal separation av smältfasen från gasen. 10 15 20 25 464 921 Möjligheten att på det uppfinningsenliga sättet noggrant reglera temperaturen, medför vidare att kokkemikaliernas sammansättning kan optimeras med avseende på kokprocessen utan att smältfasens smältpunkt samt flytbarhet behöver ge upphov till problem i återvinningssteget.In the specific embodiment with plasma generator, it has unexpectedly been found that the reaction rate for the gasification of the thick liquor is very high, so that the reactor can be designed specifically to give maximum separation of the melt phase from the gas. The possibility of accurately regulating the temperature in the manner according to the invention further means that the composition of the cooking chemicals can be optimized with respect to the cooking process without the melting point melting point and flowability having to give rise to problems in the recovery step.
Exempel I en försöksutrustning tillför en cylinderformad reaktor 9 kg tjocklut framför en på cylindern tangentiellt place- rad plasmagenerator. Genom plasmageneratorn leds 270 m3N luft per timme. Genom ännu ett tangentiellt inlopp sätts ytterligare 120 m3N luft till processen.Example In an experimental equipment, a cylindrical reactor supplies 9 kg of thick liquor in front of a plasma generator placed tangentially on the cylinder. The plasma generator conducts 270 m3N of air per hour. An additional 120 m3N of air is added to the process through another tangential inlet.
Tjockluten har följande analys: Na 20,5% av torrt material s 4,52; - " -* H2 3,7% - “ - 02 37 % - " - C 34 % - " - Cl 0,3% - " - 65% torrsubstans och kalorimetriskt värmevärde 13,89 MJ/kg TS.The thick liquor has the following analysis: Na 20.5% of dry material s 4.52; - "- * H2 3,7% -" - 02 37% - "- C 34% -" - Cl 0,3% - "- 65% dry matter and calorimetric calorific value 13,89 MJ / kg TS.
Temperaturen i reaktorn regleras till l000°C. För att er- hålla denna temperatur krävs en energitillsats pà 1260 kW el, delvis för att täcka förluster i reaktionskärlet. Ge- nom att hålla swirtalet högre än 0,6, ett Reynoldstal högre än 18000 samt välja lämpliga dimensioner på reak- torn fås en nära nog 100%-ig avskiljning av bildad smälta. 10 15 464 921 Mängd smälta är 147,5 kg i timmen, vilken tappas av kon- tinuerligt under försökens gång. Smältan analyseras till följande: Na0H Na2CO3 NaCl Na2S Dessutom sättning: CO 2,l% 64,7% 0,7% 31,5% erhölls l6,8% l3,0% 23,5% 46,6% en gas med följande torra gassamman- Na 0,03% NaOH 0,04% NaCl 0,02% Skulle man för att minska energitillsatsen öka mängden luft skulle Na2S i stor utsträckning oxideras, vilket man till varje pris vill undvika.The temperature in the reactor is regulated to 1000 ° C. To obtain this temperature, an energy addition of 1260 kW of electricity is required, partly to cover losses in the reaction vessel. By keeping the swirt number higher than 0.6, a Reynolds number higher than 18000 and choosing suitable dimensions on the reactor, a nearly 100% separation of the formed melt is obtained. 10 15 464 921 The amount of melt is 147.5 kg per hour, which is continuously lost during the experiments. The melt is analyzed to the following: NaOH Na2CO3 NaCl Na2S In addition saturation: CO 2, 1% 64.7% 0.7% 31.5%, 16.8% l3.0% 23.5% 46.6% a gas was obtained with the following dry gas aggregate Na 0.03% NaOH 0.04% NaCl 0.02% If the amount of air were to be increased in order to reduce the energy addition, Na2S would be largely oxidized, which is to be avoided at all costs.
Claims (4)
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
SE8702627A SE464921B (en) | 1987-06-25 | 1987-06-25 | SAVED TO RECOVER CHEMICALS FROM MASS DEVICES |
FI881088A FI85994B (en) | 1987-06-25 | 1988-03-09 | SAETT ATT AOTERVINNA KEMIKALIER UR MASSAAVLUTAR. |
JP63058546A JPS646191A (en) | 1987-06-25 | 1988-03-14 | Recovery of chemical substance from pulp waste liquid |
CN88101785A CN1030107A (en) | 1987-06-25 | 1988-03-29 | Method for recovering chemicals from pulping waste liquor |
CA000567585A CA1324865C (en) | 1987-06-25 | 1988-05-25 | Method for recovering chemicals from spent pulp liquors |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
SE8702627A SE464921B (en) | 1987-06-25 | 1987-06-25 | SAVED TO RECOVER CHEMICALS FROM MASS DEVICES |
Publications (3)
Publication Number | Publication Date |
---|---|
SE8702627D0 SE8702627D0 (en) | 1987-06-25 |
SE8702627L SE8702627L (en) | 1988-12-26 |
SE464921B true SE464921B (en) | 1991-07-01 |
Family
ID=20368972
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
SE8702627A SE464921B (en) | 1987-06-25 | 1987-06-25 | SAVED TO RECOVER CHEMICALS FROM MASS DEVICES |
Country Status (5)
Country | Link |
---|---|
JP (1) | JPS646191A (en) |
CN (1) | CN1030107A (en) |
CA (1) | CA1324865C (en) |
FI (1) | FI85994B (en) |
SE (1) | SE464921B (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5746886A (en) * | 1993-01-25 | 1998-05-05 | Kvaerner Pulping Ab | Method for the recovery of energy and chemicals from cellulose spent liquor containing potassium using a gasifier |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US7494637B2 (en) | 2000-05-16 | 2009-02-24 | Massachusetts Institute Of Technology | Thermal conversion of biomass to valuable fuels, chemical feedstocks and chemicals |
Family Cites Families (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
SE454188B (en) * | 1984-10-19 | 1988-04-11 | Skf Steel Eng Ab | MAKE RECYCLING CHEMICALS FROM MASS DISPENSER |
-
1987
- 1987-06-25 SE SE8702627A patent/SE464921B/en not_active IP Right Cessation
-
1988
- 1988-03-09 FI FI881088A patent/FI85994B/en not_active Application Discontinuation
- 1988-03-14 JP JP63058546A patent/JPS646191A/en active Pending
- 1988-03-29 CN CN88101785A patent/CN1030107A/en active Pending
- 1988-05-25 CA CA000567585A patent/CA1324865C/en not_active Expired - Lifetime
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US5746886A (en) * | 1993-01-25 | 1998-05-05 | Kvaerner Pulping Ab | Method for the recovery of energy and chemicals from cellulose spent liquor containing potassium using a gasifier |
Also Published As
Publication number | Publication date |
---|---|
FI881088A0 (en) | 1988-03-09 |
CN1030107A (en) | 1989-01-04 |
FI85994B (en) | 1992-03-13 |
SE8702627L (en) | 1988-12-26 |
FI881088A (en) | 1988-12-26 |
CA1324865C (en) | 1993-12-07 |
SE8702627D0 (en) | 1987-06-25 |
JPS646191A (en) | 1989-01-10 |
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