EP3828336A1 - Verfahren zur reinigung von terpentinkondensat aus trs - Google Patents

Verfahren zur reinigung von terpentinkondensat aus trs Download PDF

Info

Publication number
EP3828336A1
EP3828336A1 EP19211806.5A EP19211806A EP3828336A1 EP 3828336 A1 EP3828336 A1 EP 3828336A1 EP 19211806 A EP19211806 A EP 19211806A EP 3828336 A1 EP3828336 A1 EP 3828336A1
Authority
EP
European Patent Office
Prior art keywords
condensate
turpentine
column
resultant
trs
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP19211806.5A
Other languages
English (en)
French (fr)
Inventor
Anders Norberg
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Mistab Innovation AB
Original Assignee
Mistab Innovation AB
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Mistab Innovation AB filed Critical Mistab Innovation AB
Priority to EP19211806.5A priority Critical patent/EP3828336A1/de
Publication of EP3828336A1 publication Critical patent/EP3828336A1/de
Withdrawn legal-status Critical Current

Links

Images

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
    • D21C11/06—Treatment of pulp gases; Recovery of the heat content of the gases; Treatment of gases arising from various sources in pulp and paper mills; Regeneration of gaseous SO2, e.g. arising from liquors containing sulfur compounds
    • 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
    • D21C11/0007—Recovery of by-products, i.e. compounds other than those necessary for pulping, for multiple uses or not otherwise provided for
    • 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
    • D21C11/0042—Fractionating or concentration of spent liquors by special methods

Definitions

  • the present invention relates to a method for purifying turpentine condensate from reduced sulphur compounds, so called TRS (Total Reduced Sulphur).
  • the amount of turpentine recovered varies widely and is due to a number of more or less complex factors. Among the most important are wood species, the zone and origin of growth of the wood, the storage time of the wood and wood chips, the type of digester process, how the turpentine recovery equipment is designed and its operating conditions, etc.
  • the extraction liquors of the digester house are thickened from thin black liquor to heavy black liquor, while condensate with different purity grades are extracted.
  • the amount of turpentine extracted within the evaporation plant is in most cases substantially lower than the amount of turpentine extracted in the turpentine recovery system of the digester house.
  • the most common location for turpentine extraction is within the methanol recovery system but can be accomplished by other methods within the evaporation plant as well.
  • the inventive method for purifying turpentine from reduced sulphur can either be operated as a batch process or a continuous process depending on specific circumstances.
  • turpentine condensate streams originating from a soft wood pulp process can be purified from reduced sulphur compounds (TRS).
  • the inventive method for purification with respect to TRS relates to turpentine condensate streams found from the methanol recovery system of the chemical recovery plant, the evaporation plant, condensates derived from the handling of diluted and concentrated non-condensable gas or similar turpentine condensate streams found within the pulp mill.
  • the pulp mill is intended for processing soft wood pulp and refers to a process for exploit of sulphate pulp, sulphite pulp and processes for the extraction of so-called NSSC, CTMP and TMP pulp.
  • the inventive method is applicable to any turpentine condensate with high sulphur content within the pulp mill.
  • the inventive method for sulphur purification of turpentine condensates consists of a number of sub-processes where the customer requirement regarding the sulphur content of the purified turpentine determines whether subsequent sub-processes are necessary or not.
  • the quality requirement for a customer may be that only one of the sub-processes is required to obtain sufficiently pure turpentine, while the quality requirement of another customer requires that the system is designed with all the described sub-processes.
  • the object of the invention is to increase the amount of turpentine that can be extracted from TRS containing condensates within a pulp mill producing soft wood pulp.
  • this object is achieved by a method for cleaning turpentine condensates from total reduced sulphur (TRS) compounds which turpentine condensate is obtained by cooking soft wood pulp in a pulp mill, characterized by
  • a turpentine containing condensate, below called turpentine condensate 1, to be treated so as to reduce its TRS content is collected and passed by pumping or hydraulically drainage, for instance, to a tank 2.
  • the tank 2 can be vented to an external gas system or to any of the vessels described below (not shown).
  • said collected turpentine condensate 1 stored in the tank 2, if appropriate, is supplied through pumping or hydraulic drainage, for instance, via a pipe system 3 to a first column 4.
  • a first steam input 5 is supplied to the first column 4 in which said supplied turpentine condensate 3 and said supplied first steam input 5 are brought into contact with each other in such a way that TRS compounds in the supplied turpentine condensate is totally or partially removed by a first gas stream 6 stripped from said first column.
  • the first steam input 5 either pure steam or TRS containing steam can be used.
  • the first column 4 can be provided with a stripping section with or without a rectifying section depending on prevailing circumstances.
  • Said first gas stream 6 stripped from the first column 4 is passed to a first condenser 7 where said first gas stream 6 is partially condensed out by supplying a first cooling media 8 thereby obtaining a first resultant turpentine condensate 9, the condensing heat being extracted through a first outgoing cooling media 10.
  • the first resultant turpentine condensate 9 is returned to the first column 4 in such a way that a reflux is obtained.
  • the returned first resultant turpentine condensate 9 can be returned to the first column 4 by pumping or by hydraulic drainage, for instance.
  • the returned first resultant turpentine condensate 9 can be returned to the first column 4 at one or several different levels of the first column 4.
  • a second resultant gas stream 11 from the first condenser 7 is further passed to a second condenser 12 where the second resultant gas stream 11 is totally or partially condensed out depending on inert gas content.
  • a second cooling media 13 is supplied to the second condenser 12 and the condensing heat being extracted through a second outgoing cooling media 14.
  • a first resultant condensate 15 from the second condenser 12 consists of an impure TRS-containing condensate which is advantageously passed towards the pulp mill handling system for foul condensates.
  • a first resultant inert gas stream 16 is advantageously passed towards the pulp mill system for handling of concentrated non-condensable gas.
  • a first purified turpentine condensate 17 is obtained and removed.
  • This first purified turpentine condensate is preferably passed to a decanter 18 for gravimetric separation of purified turpentine 19 from the aqueous phase condensate 20.
  • the first purified turpentine condensate 19 can be passed to the same tank as used for storage of turpentine obtained in the turpentine recovery system of the digester house as mentioned above or to a different tank.
  • first purified turpentine condensate 17 in case the first purified turpentine condensate 17 also contains amounts of heavier TRS compounds such as polymeric sulphur compounds, S8 compounds and similar sulphur compounds, said first purified turpentine condensate 17 is passed without passing a decanter, such as decanter 18, to an oxidizing reactor 30 for total or partial oxidation of residual sulphur compounds.
  • An oxidizing agent 31 is added to the oxidizing reactor 30.
  • the oxidizing agent 31 is preferably selected from the group consisting of peroxides such as hydrogen peroxide, oxygen, air, and the like, and commonly used oxidizing agents in the pulping process of a pulp mill.
  • the oxidizing reactor 30 is designed as a vessel so as to obtain a good contact between the first purified turpentine condensate 17 and the oxidizing agent 31 supplied.
  • the reactor 30 may have means which improves contact between said treated first purified turpentine condensate and the oxidizing agent supplied.
  • a resultant TRS-oxidized turpentine condensate 32 from the reactor 30 is pumped or hydraulically drained, for instance, to a second column 33.
  • a second steam input 34 is supplied to the second column 33 in which supplied TRS-oxidized turpentine condensate 32 and the second steam input 34 are brought into contact with each other in such a way that the components of the turpentine are totally or partially evaporated in the form of a second gas stream 35 stripped from the second column 33.
  • second steam input 34 pure steam is preferably used.
  • the second column 33 can be designed with a stripping section with or without a rectifying section.
  • the second gas stream 35 stripped from the second column 33 is passed to a third condenser 36 where the second gas stream 35 is partially condensed out by supplying a third cooling media 37 thereby obtaining a second resultant turpentine condensate 38 while the condensing heat is extracted by a third cooling media 39.
  • Said second resultant condensate 38 is returned to the second column 33 in such a way that a reflux is obtained.
  • Said second resultant turpentine condensate 38 can be returned to the second column 33 by either pumping or hydraulic drainage, for instance.
  • Said second resultant turpentine condensate 38 can be returned to the second column 33 at one or several different levels of the second column 33.
  • a second resultant gas stream 40 from the third condenser 36 is further passed to a fourth condenser 41 where said second resultant gas stream 40 is totally or partially condensed out depending on the inert gas content.
  • the fourth condenser 41 is supplied with a fourth cooling media 42 while the condensing heat is extracted through a fourth outgoing cooling media 43.
  • the resultant inert gas phase 44 is advantageously passed towards the pulp mill system for handling of concentrated non-condensable gas or similar position.
  • a second purified turpentine condensate 45 from the fourth condenser 41 is a pure TRS-free turpentine condensate which, by preferably pumping or hydraulic drainage, is passed to a second decanter 46 for gravimetric separation of a second purified turpentine 47 from a second aqueous phase condensate 48.
  • Said second purified turpentine 47 can be led to a handling system of the pulp mill for handling turpentine to be sold, while said second aqueous phase condensate 48 is preferably returned to the pulp mill handling system for foul condensates.
  • a foul sulphur-containing condensate 49 is removed.
  • the foul sulphur-containing condensate 49 may contain varying amounts of resulting oxidized sulphur compounds of polymeric sulphur compounds, S8 compounds and other heavy TRS compounds.
  • the foul sulphur-containing condensate 49 can preferably be recycled to any of the black liquor streams of the pulp mill chemical recovery process, the pulp mill handling system for foul condensates or similar suitable liquid partial stream of the pulp mill.

Landscapes

  • Paper (AREA)
EP19211806.5A 2019-11-27 2019-11-27 Verfahren zur reinigung von terpentinkondensat aus trs Withdrawn EP3828336A1 (de)

Priority Applications (1)

Application Number Priority Date Filing Date Title
EP19211806.5A EP3828336A1 (de) 2019-11-27 2019-11-27 Verfahren zur reinigung von terpentinkondensat aus trs

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP19211806.5A EP3828336A1 (de) 2019-11-27 2019-11-27 Verfahren zur reinigung von terpentinkondensat aus trs

Publications (1)

Publication Number Publication Date
EP3828336A1 true EP3828336A1 (de) 2021-06-02

Family

ID=68699328

Family Applications (1)

Application Number Title Priority Date Filing Date
EP19211806.5A Withdrawn EP3828336A1 (de) 2019-11-27 2019-11-27 Verfahren zur reinigung von terpentinkondensat aus trs

Country Status (1)

Country Link
EP (1) EP3828336A1 (de)

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3745063A (en) * 1971-11-01 1973-07-10 British Columbia Forest Prod L Process for simultaneous turpentine recovery and odor control
US4915784A (en) * 1989-05-03 1990-04-10 Reynolds Ellis W Process and apparatus for removing contaminants from pulp digester vent gas
US4925527A (en) * 1989-02-22 1990-05-15 Ahlstromforetagen Svenska Ab Method for the recovery of turpentine and heat in a refiner pulping process
WO1999037853A1 (en) * 1998-01-23 1999-07-29 Mo Och Domsjö Aktiebolag Method for processing of alkaline condensate emanating from the manufacture of cellulose pulp
WO2000001879A1 (en) * 1998-07-07 2000-01-13 Papsea Ab Method an arrangement for cleaning contaminated condensate including a combined stripper/condenser
WO2001049928A1 (en) * 1999-12-29 2001-07-12 Metso Chemical Pulping Oy Method for improved turpentine recovery from modern cooking plants
WO2014201555A1 (en) * 2013-06-19 2014-12-24 Fpinnovations Method for producing bio-methanol at pulp mills
WO2017053342A1 (en) * 2015-09-24 2017-03-30 Veolia Water Technologies, Inc. System and process for stripping volatile organic compounds from foul condensate

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3745063A (en) * 1971-11-01 1973-07-10 British Columbia Forest Prod L Process for simultaneous turpentine recovery and odor control
US4925527A (en) * 1989-02-22 1990-05-15 Ahlstromforetagen Svenska Ab Method for the recovery of turpentine and heat in a refiner pulping process
US4915784A (en) * 1989-05-03 1990-04-10 Reynolds Ellis W Process and apparatus for removing contaminants from pulp digester vent gas
WO1999037853A1 (en) * 1998-01-23 1999-07-29 Mo Och Domsjö Aktiebolag Method for processing of alkaline condensate emanating from the manufacture of cellulose pulp
WO2000001879A1 (en) * 1998-07-07 2000-01-13 Papsea Ab Method an arrangement for cleaning contaminated condensate including a combined stripper/condenser
WO2001049928A1 (en) * 1999-12-29 2001-07-12 Metso Chemical Pulping Oy Method for improved turpentine recovery from modern cooking plants
WO2014201555A1 (en) * 2013-06-19 2014-12-24 Fpinnovations Method for producing bio-methanol at pulp mills
WO2017053342A1 (en) * 2015-09-24 2017-03-30 Veolia Water Technologies, Inc. System and process for stripping volatile organic compounds from foul condensate

Similar Documents

Publication Publication Date Title
US9938216B2 (en) Methanol purification method and apparatus
US20110198049A1 (en) Fiberline systems, processes and methods
EP3010877B1 (de) Verfahren zur herstellung von biomethanol in zellstoffwerken
FI63611C (fi) Foerfarande foer avlaegsning och aotervinning av flyktiga organiska komponenter fraon sulfitavlut
US5830314A (en) Cleaning condensates from multi-effect evaporator of cellulose pulp waste liquors
US20100316553A1 (en) Method for extracting ammonium salt and methanol from a liquid obtained from foul condensates in a cellulose pulp mill
US11898309B2 (en) Method and a system for obtaining methanol from foul condensate of a pulping process
EP3828336A1 (de) Verfahren zur reinigung von terpentinkondensat aus trs
SE502172C2 (sv) Förfarande för framställning av blekt cellulosamassa med en klorfri bleksekvens i närvaro av karbonat
US5989394A (en) Process for treatment of a contaminated liquid
US6217711B1 (en) Method of treating condensates
US20220185700A1 (en) Kraft pulping foul condensate treatment process and apparatus
US4915784A (en) Process and apparatus for removing contaminants from pulp digester vent gas
FI20216182A1 (en) Method and device for the production of methanol
EP0040093A1 (de) System und Verfahren zur Herabsetzung des Sauerstoffverbrauchs in der Oxydation von Schwarzlauge
NO126049B (de)
US5507913A (en) Solvent recovery in pulp bleaching with ozone
AU2022389653A1 (en) A modified air stripping process and apparatus
JP2024540434A (ja) 修正エアストリッピングプロセスおよび装置
FI20216183A1 (en) Process and apparatus for producing methanol from black liquor
FI20245265A1 (en) Method and device for producing methanol from black liquor
Lin et al. The basics of foul condensate stripping

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN PUBLISHED

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20210610

RBV Designated contracting states (corrected)

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20240601