CA1212505A - Method, process and apparatus for converting wood, wood residue and or biomass into pulp - Google Patents
Method, process and apparatus for converting wood, wood residue and or biomass into pulpInfo
- Publication number
- CA1212505A CA1212505A CA000459020A CA459020A CA1212505A CA 1212505 A CA1212505 A CA 1212505A CA 000459020 A CA000459020 A CA 000459020A CA 459020 A CA459020 A CA 459020A CA 1212505 A CA1212505 A CA 1212505A
- Authority
- CA
- Canada
- Prior art keywords
- range
- concentration range
- wood
- followed
- fibres
- 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.)
- Expired
Links
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000002023 wood Substances 0.000 title claims abstract description 32
- 239000002028 Biomass Substances 0.000 title 1
- 239000000126 substance Substances 0.000 claims abstract description 29
- 239000000835 fiber Substances 0.000 claims abstract description 17
- 238000011282 treatment Methods 0.000 claims abstract description 11
- 238000007599 discharging Methods 0.000 claims abstract description 3
- 235000013311 vegetables Nutrition 0.000 claims description 29
- 238000007670 refining Methods 0.000 claims description 15
- 230000006835 compression Effects 0.000 claims description 13
- 238000007906 compression Methods 0.000 claims description 13
- CSNNHWWHGAXBCP-UHFFFAOYSA-L Magnesium sulfate Chemical compound [Mg+2].[O-][S+2]([O-])([O-])[O-] CSNNHWWHGAXBCP-UHFFFAOYSA-L 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 12
- 230000006837 decompression Effects 0.000 claims description 12
- GEHJYWRUCIMESM-UHFFFAOYSA-L sodium sulfite Chemical compound [Na+].[Na+].[O-]S([O-])=O GEHJYWRUCIMESM-UHFFFAOYSA-L 0.000 claims description 11
- 239000003795 chemical substances by application Substances 0.000 claims description 10
- 238000004061 bleaching Methods 0.000 claims description 9
- 238000005406 washing Methods 0.000 claims description 9
- 230000014759 maintenance of location Effects 0.000 claims description 8
- 238000007254 oxidation reaction Methods 0.000 claims description 8
- 235000010265 sodium sulphite Nutrition 0.000 claims description 7
- QPCDCPDFJACHGM-UHFFFAOYSA-N N,N-bis{2-[bis(carboxymethyl)amino]ethyl}glycine Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(=O)O)CCN(CC(O)=O)CC(O)=O QPCDCPDFJACHGM-UHFFFAOYSA-N 0.000 claims description 6
- 238000009792 diffusion process Methods 0.000 claims description 6
- 230000003647 oxidation Effects 0.000 claims description 6
- 238000006277 sulfonation reaction Methods 0.000 claims description 6
- 229910052911 sodium silicate Inorganic materials 0.000 claims description 5
- KFSLWBXXFJQRDL-UHFFFAOYSA-N Peracetic acid Chemical compound CC(=O)OO KFSLWBXXFJQRDL-UHFFFAOYSA-N 0.000 claims description 4
- 239000004115 Sodium Silicate Substances 0.000 claims description 4
- 230000003213 activating effect Effects 0.000 claims description 4
- 238000004140 cleaning Methods 0.000 claims description 4
- PFUVRDFDKPNGAV-UHFFFAOYSA-N sodium peroxide Chemical compound [Na+].[Na+].[O-][O-] PFUVRDFDKPNGAV-UHFFFAOYSA-N 0.000 claims description 4
- NTHWMYGWWRZVTN-UHFFFAOYSA-N sodium silicate Chemical compound [Na+].[Na+].[O-][Si]([O-])=O NTHWMYGWWRZVTN-UHFFFAOYSA-N 0.000 claims description 4
- -1 carboxylic groups Chemical group 0.000 claims description 3
- KCXVZYZYPLLWCC-UHFFFAOYSA-N EDTA Chemical compound OC(=O)CN(CC(O)=O)CCN(CC(O)=O)CC(O)=O KCXVZYZYPLLWCC-UHFFFAOYSA-N 0.000 claims description 3
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims description 3
- 239000008139 complexing agent Substances 0.000 claims description 3
- 229910052751 metal Inorganic materials 0.000 claims description 3
- 239000002184 metal Substances 0.000 claims description 3
- 235000019832 sodium triphosphate Nutrition 0.000 claims description 3
- 229920001131 Pulp (paper) Polymers 0.000 claims description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 2
- 238000005282 brightening Methods 0.000 claims description 2
- 230000015556 catabolic process Effects 0.000 claims description 2
- 150000001768 cations Chemical class 0.000 claims description 2
- 235000019398 chlorine dioxide Nutrition 0.000 claims description 2
- OSVXSBDYLRYLIG-UHFFFAOYSA-N chlorine dioxide Inorganic materials O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 claims description 2
- QBWCMBCROVPCKQ-UHFFFAOYSA-N chlorous acid Chemical compound OCl=O QBWCMBCROVPCKQ-UHFFFAOYSA-N 0.000 claims description 2
- 230000000536 complexating effect Effects 0.000 claims description 2
- 238000006731 degradation reaction Methods 0.000 claims description 2
- 230000000694 effects Effects 0.000 claims description 2
- 230000003301 hydrolyzing effect Effects 0.000 claims description 2
- 238000005470 impregnation Methods 0.000 claims description 2
- 239000007788 liquid Substances 0.000 claims description 2
- 238000012216 screening Methods 0.000 claims description 2
- UKLNMMHNWFDKNT-UHFFFAOYSA-M sodium chlorite Chemical compound [Na+].[O-]Cl=O UKLNMMHNWFDKNT-UHFFFAOYSA-M 0.000 claims description 2
- 229910052717 sulfur Inorganic materials 0.000 claims description 2
- 239000011593 sulfur Substances 0.000 claims description 2
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims 20
- 235000011121 sodium hydroxide Nutrition 0.000 claims 7
- 229910052943 magnesium sulfate Inorganic materials 0.000 claims 5
- 235000019341 magnesium sulphate Nutrition 0.000 claims 5
- KRKNYBCHXYNGOX-UHFFFAOYSA-N citric acid Chemical compound OC(=O)CC(O)(C(O)=O)CC(O)=O KRKNYBCHXYNGOX-UHFFFAOYSA-N 0.000 claims 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims 2
- 239000007844 bleaching agent Substances 0.000 claims 2
- 230000000295 complement effect Effects 0.000 claims 2
- 239000000203 mixture Substances 0.000 claims 2
- 229910052760 oxygen Inorganic materials 0.000 claims 2
- 239000001301 oxygen Substances 0.000 claims 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical group O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims 2
- XMNIXWIUMCBBBL-UHFFFAOYSA-N 2-(2-phenylpropan-2-ylperoxy)propan-2-ylbenzene Chemical compound C=1C=CC=CC=1C(C)(C)OOC(C)(C)C1=CC=CC=C1 XMNIXWIUMCBBBL-UHFFFAOYSA-N 0.000 claims 1
- PMAAOHONJPSASX-UHFFFAOYSA-N 2-butylperoxypropan-2-ylbenzene Chemical compound CCCCOOC(C)(C)C1=CC=CC=C1 PMAAOHONJPSASX-UHFFFAOYSA-N 0.000 claims 1
- ZPMCCZKDFLIVHD-UHFFFAOYSA-N 2-tert-butylperoxy-2-methylpropane;1,2-di(propan-2-yl)benzene Chemical compound CC(C)(C)OOC(C)(C)C.CC(C)C1=CC=CC=C1C(C)C ZPMCCZKDFLIVHD-UHFFFAOYSA-N 0.000 claims 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 1
- DWAQJAXMDSEUJJ-UHFFFAOYSA-M Sodium bisulfite Chemical compound [Na+].OS([O-])=O DWAQJAXMDSEUJJ-UHFFFAOYSA-M 0.000 claims 1
- ZMANZCXQSJIPKH-UHFFFAOYSA-N Triethylamine Chemical compound CCN(CC)CC ZMANZCXQSJIPKH-UHFFFAOYSA-N 0.000 claims 1
- 125000003172 aldehyde group Chemical group 0.000 claims 1
- 230000000712 assembly Effects 0.000 claims 1
- 238000000429 assembly Methods 0.000 claims 1
- HJMZMZRCABDKKV-UHFFFAOYSA-N carbonocyanidic acid Chemical compound OC(=O)C#N HJMZMZRCABDKKV-UHFFFAOYSA-N 0.000 claims 1
- LSXWFXONGKSEMY-UHFFFAOYSA-N di-tert-butyl peroxide Chemical compound CC(C)(C)OOC(C)(C)C LSXWFXONGKSEMY-UHFFFAOYSA-N 0.000 claims 1
- 238000006073 displacement reaction Methods 0.000 claims 1
- MHAJPDPJQMAIIY-UHFFFAOYSA-M hydroperoxide group Chemical group [O-]O MHAJPDPJQMAIIY-UHFFFAOYSA-M 0.000 claims 1
- 229920005610 lignin Polymers 0.000 claims 1
- 238000005259 measurement Methods 0.000 claims 1
- 238000012986 modification Methods 0.000 claims 1
- 230000004048 modification Effects 0.000 claims 1
- 230000035515 penetration Effects 0.000 claims 1
- 150000002978 peroxides Chemical class 0.000 claims 1
- 238000004537 pulping Methods 0.000 claims 1
- 229920006395 saturated elastomer Polymers 0.000 claims 1
- 235000010267 sodium hydrogen sulphite Nutrition 0.000 claims 1
- 235000019795 sodium metasilicate Nutrition 0.000 claims 1
- WGRULTCAYDOGQK-UHFFFAOYSA-M sodium;sodium;hydroxide Chemical compound [OH-].[Na].[Na+] WGRULTCAYDOGQK-UHFFFAOYSA-M 0.000 claims 1
- 238000010025 steaming Methods 0.000 abstract description 5
- 230000015572 biosynthetic process Effects 0.000 description 3
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000011734 sodium Substances 0.000 description 2
- 229910052708 sodium Inorganic materials 0.000 description 2
- LSNNMFCWUKXFEE-UHFFFAOYSA-L sulfite Chemical compound [O-]S([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-L 0.000 description 2
- HHBOUFYYHJJTNU-UHFFFAOYSA-N 1,3,6-thiadiazepane-2,7-dithione Chemical compound S=C1NCCNC(=S)S1 HHBOUFYYHJJTNU-UHFFFAOYSA-N 0.000 description 1
- 102100031260 Acyl-coenzyme A thioesterase THEM4 Human genes 0.000 description 1
- 244000118350 Andrographis paniculata Species 0.000 description 1
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 101000638510 Homo sapiens Acyl-coenzyme A thioesterase THEM4 Proteins 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- 208000036366 Sensation of pressure Diseases 0.000 description 1
- 239000013043 chemical agent Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 150000002739 metals Chemical class 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
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
- D21C3/00—Pulping cellulose-containing materials
- D21C3/22—Other features of pulping processes
- D21C3/228—Automation of the pulping processes
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21B—FIBROUS RAW MATERIALS OR THEIR MECHANICAL TREATMENT
- D21B1/00—Fibrous raw materials or their mechanical treatment
- D21B1/02—Pretreatment of the raw materials by chemical or physical means
- D21B1/021—Pretreatment of the raw materials by chemical or physical means by chemical means
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Mechanical Engineering (AREA)
- Paper (AREA)
Abstract
ABSTRACT
A method, process, and apparatus are described wherein includes conveying means for feeding chips and wood residue in a continuous fashion for chemical pretreating, compressing, deairing, dewatering, pressure steaming, pressure releasing, all in accordace with predetermined time intervals, concentration of chemicals in relation to fibre dry weight and retension time in pressure steaming vessel, defibrating chips and wood residue, means to interpret rate of feed to control residue movement throughout the process, according to a predetermined schedule, stored in the memory to further advance the defibrated residue into refiner and further discharging the refined pulp for other treatment.
A method, process, and apparatus are described wherein includes conveying means for feeding chips and wood residue in a continuous fashion for chemical pretreating, compressing, deairing, dewatering, pressure steaming, pressure releasing, all in accordace with predetermined time intervals, concentration of chemicals in relation to fibre dry weight and retension time in pressure steaming vessel, defibrating chips and wood residue, means to interpret rate of feed to control residue movement throughout the process, according to a predetermined schedule, stored in the memory to further advance the defibrated residue into refiner and further discharging the refined pulp for other treatment.
Description
~2~ 5~
l;he present invention relates to an apparatus for converting tree chips, wood or vegetable fibres into pulp and more particularly, to a process of producing pulp from ve~e-table fibres compri~sinc~ the combinatior1 in sequence of the steps of handling, conveying, chemical pretreating, COrnpreSSinCJ, deairinc~, dewatering, pressure steaming, pressure releasinq, refinincJ and bleaching.
It is well known the conventional production oE pulp by ~raft, Sulphite, Trqpr CTMP, SGlJ, R~1P, SC~P, BSK, HY~S, ~JSSC, ~d PBI-IK processes, is expensive, highly capital intensive, high enercJy consumin(~ and enviro~entaly restrictive.
It is an alm of this present invention to providc a simple, relatively low capital cost ec~uipment, in such an orcler as to handle the residues in an economic manner, with relati~
vely low energy requirement while minimizin~ the creation of rejects and minimizing the manual input.
A process in accordance with the present invention includes the steps of conveying the vegetable fibres for a pretreatment, impregnation with chemicals, then the compression of the vegetable fibres in order to extract air between the fibres and to extract some of the liquid from the fibres. The compressed residues are then loaded throuqh a pocket valve, loading screw or vegetable fibre plug created by mechanical or hydraulical means into a pressurized steam vessel where additional chemicals may be introduced with the ste~m. In the pressurized steam vessel, the hydrolytic reaction occurs at a preselected pressure, temperature and retention time of said vegetable fibres. The vegetabLe fibres are freely moved by means of a worm or ribon conveyo-r.
The speèd of the movement ot the ve(~etable fibres in the pressure steamin~ vessel is variable. It is directly related to the rate ot ~e~, volume of the fibre ancl the desired steam treatrnent. At the encl of the pressure vessel, ~h~
~ .
l;he present invention relates to an apparatus for converting tree chips, wood or vegetable fibres into pulp and more particularly, to a process of producing pulp from ve~e-table fibres compri~sinc~ the combinatior1 in sequence of the steps of handling, conveying, chemical pretreating, COrnpreSSinCJ, deairinc~, dewatering, pressure steaming, pressure releasinq, refinincJ and bleaching.
It is well known the conventional production oE pulp by ~raft, Sulphite, Trqpr CTMP, SGlJ, R~1P, SC~P, BSK, HY~S, ~JSSC, ~d PBI-IK processes, is expensive, highly capital intensive, high enercJy consumin(~ and enviro~entaly restrictive.
It is an alm of this present invention to providc a simple, relatively low capital cost ec~uipment, in such an orcler as to handle the residues in an economic manner, with relati~
vely low energy requirement while minimizin~ the creation of rejects and minimizing the manual input.
A process in accordance with the present invention includes the steps of conveying the vegetable fibres for a pretreatment, impregnation with chemicals, then the compression of the vegetable fibres in order to extract air between the fibres and to extract some of the liquid from the fibres. The compressed residues are then loaded throuqh a pocket valve, loading screw or vegetable fibre plug created by mechanical or hydraulical means into a pressurized steam vessel where additional chemicals may be introduced with the ste~m. In the pressurized steam vessel, the hydrolytic reaction occurs at a preselected pressure, temperature and retention time of said vegetable fibres. The vegetabLe fibres are freely moved by means of a worm or ribon conveyo-r.
The speèd of the movement ot the ve(~etable fibres in the pressure steamin~ vessel is variable. It is directly related to the rate ot ~e~, volume of the fibre ancl the desired steam treatrnent. At the encl of the pressure vessel, ~h~
~ .
2~
O chemically pretreated and pressure steamed residues are relea-sed by means of a decompression chambre into a dozing bin. From the dozing bin the residue fibres are transported and conveyed into a refiner. A refining is executed by a disc refiner under pressurized and or atmospheric discharge operation.
An apparatus in accordance with the present invention includes an intergrated system having a chemical pretreatment metering means in to the wood residue flow, metering means of residues into a residue compression chambre, residue compressing means, air a~d moisture relieve means from a residue compression means, means to activate pocket valve of a compression means, means to discharge a pocket valve into the pressurized steam vessel, means to move the fibre residues inside the steam press-ure vessel, means for activating the worm conveyor according to predetermined infor~lations received from the residue metering means, means of unloading fibre residues from a steam pressurized vessel into a decompression means, means to release the fibre residues from decompressed means to a dozing means, means trans-porting and conveying the decompressed fibre residues into the refining means.
A further feature of the present invention includes a control system which includes a first scanning means at the infeed of wood residues, input data receiving means for interp-reting the data received from the first scanning means and for measuring the moisture content of the residue and weight-volume input according to the predetermined parameters, means associat-ed with said control system for activating a speed control of the residue infeed, measuring means controled by the control system means of the residue flow control system based on said data to introduce chemicals in solution and or in a dry form into the residue flow, means for controling the pocket valve or fibre plug activity, means to activate the discharging of vegetable fibres into a pressure vessel, means related to flow of ,.
~2~L~25~5 vegetable fibres into a vegeta~le fibres compression means, means to interpret rate of feed to control the residue movement in a steam pressure vessel according to the predetermined schedule stored in a memory, sensing means associated with discharge of residues from pressure steam vessel~ input data receiving means for interpreting and controling the refining mechanism and refining accordin~ to a predetermined refining patterns stored in the memory.
Ha~ing thus generally described the nature of the inv-ention, reference will now be made to the accompanying drawings, showing by way of illustration, a preferred embodiment thereof and in which:
Figure 1 is a diagram illustrating the various steps af a continuous process;
Figure 2 is a diagram illustrating the various reactions and changes of properties of residues from wood type form to pulp type form;
Figure 3 is illustrating step-by-step the process sequence of converting wood residues into a marketable pulp;
Figure 4 depicts the process of brightening or bleaching.
Referring now to the drawings and particulary to figure 1, there is shown an integrated processing mill for con-version of wood chips and or wood residues into wood pulp. An embodiment of the integrated processing mill includes a chip or residue conveyor 1 for conveying chips or wood residues, a pretreatment station 2 for application of chemicals, chips and residue level detector 17 for controling the flow of chips and residues through the pretreatment station and for controling the level of chemicals 4 in the first pretreatment station 2 a further a worm conveyor 3 for conveying residues from first pretreatment station 2 on to a residue conveyor 5 leadi.ng into second pretreatment station 6. A further scanner 18 may be ~2~;~50~;
provided for again measuring the residue volume from the second pretreatment station 6 into the compression chamber 8 operating under a predetermined pressure, compressed residues are then advanced through a pocket valve or fibre plug 9 through a steam pressure vessel 10, through a decompression chamber 11 and 12 into a dozing bin 13 and from the dozing bin through a washing station 14 or directly on to worm conveyor 15, bypassing the washing station,leading into the refiner 16. Refi.ned pulp is discharged into latency chest 19 and further the refined pulp may be introduced in to the bleaching station 20. Figure 2 shows reactions of chemical pretreatment of vegetable fibres 20 by complexing agents 21 and formation of hydrophylic group 22,23,24, 25, 26, 27, on wood surface, creat:inc3 a bond 28 it also demonstrates formation of hydrophilic group 22, 23, 24 on surface of residues 20 by oxidating agents 21.
Figure 3 is the step by step process sequence of che-mical reactions by various pretreatment of residues:
~tep 1- rrrys to eliminate free metalic cations which may cata-lize oxidation of SO2 to SO3,elimination is done by complexing with complexing agent DTPA or others.
Free metal ~ DTPA-~-------- Metal-DTPA
(non-reactive complex) Example: Ee, Mn, Cu, Al, etcO Metals may be pressnt in different valences.
To protect against oxydation, residues are pretreated with DTPA -Sodium Diethylenetriaminopentaactate (.5-3% ) or TPT - Sodium Tripolyphosphate EDTA - Ethylen Diamietetraacetic Acid -Nitriloacetic Acid Further treatment is done by the following agen-ts:
Sodium Sulphite Na2SO3 (Equilibrium pH 9.3) or Ozone- O3 or 25~i !~ Oxygene or Peracetic Acid or ClO2 Bioxide of chlore or NaClO2 or NaHS~3 or H2O2- Hydrogene Peroxide or Na2O2 Sodium peroxide or Steps 2-5 are designed to form Hydrophylic group by:
-sulfonation and/or -oxydation The formation of Hydrophylic groups either by oxidation and/or sulfonation is proportional to the concentration of chemicalproducts, wood residue, time and temperature.
At constant concentration of residue and chemicals used, the process is controlled by time and retention temperature.
In Step no. 2 and 3 determining factor for chemical reaction is time, since the temperature is very low.
In the step number 4, it is the temperature which con-trols the extent of sulfonation or oxidation. The speed of the sulfonation or oxidation may be also varied by concentration of the chemical product.
Further figure 3 depicts step by step the se~uence of the process of pretreatment of residues, its defibration and its refining as fo]lows:
Step 1- To prevent degradation by burning of residues which may take place in residue pressure steaming vessel, residues are mixed in solution of O5-3~0~ solution related to dry weight of residues at ambiant temperature and under atmospheric pressure.
Step 2- In order to form hydrophilic group on the surface of residues the following treatment is made:
-with sulphonating agents; DTPA
Sodiumdiethylenetriaminopentaacetate and others ` ~Zl~S~S
-with oxidative agents; TPF as sodium tripolyphosphate, ethylen diamietetraacetic acid.
This begins a topochemical reaction which consist in diffusion of chemical agents inside of the wood resi-dues and subsequently chemical reaction with the wood substrate.
Step 3- In order to increase the efficiency of the reaction and or the rate of diffusion the residues are introdu-ced into a compression-decompression cha~ber.
0 Step 4- After the compression-decompression of residues, the residues are trar~sferred into pressure steaming vessel, to complete the saturation process of residues,a final part of chemicals is introduced by steam at the beginning of a steam pressure vessel, major parts of hydrophylic groups are formed in the vessel due to high temperature and time of retention.
Step 5- Treated residues leave the pressurized vessel into a decompression chamber where de~ibration of residues occures. Further, residues are conveyed to a dozing ~0 bin under atmospheric pressure.
Step 6- Defibrated residues are conveyed through a washing station and/or they are conveyed without washing into a refiner.
Step 7- Depending on the pre-determined quality of pulp, refining of defibrated residues is directed to achie-ve ~anadians Standard Freenes varying from 600 to 50 CSF.
This is achieved by using commercial atmosphe-ric refinèrs and/or pressurized refiners.
According to the final product requirement,the pulp could be used as it is and/or could be transferred to other treatments as follows;bleaching treatment, curl setting, latency, screening, or cleaning.
Z~
"SUPPL~MENTARY DISCLOSURE" r Prior to noncompulsory bleaching the refined pulp is washed, noncompulsury screened, cleaned, thickened and preferably bleached in a single stage process. The brightness increase of up to 32 points have been experienced during laboratory and pilot bleaching trials with Hydrogene Peroxide H202, Sodium Peroxide Na202, Oxygene 2 and Ozone 03 Magnesium Sulfat, Sodium Silicate, DTPA, Sodium ~ydroxyde at pulp consistency range of 12% to 40~. Brightness reversion protection have been succesfully achieved by non compulsory diffusion washing and post treatment with Sulfur Bioxyde S02.
O chemically pretreated and pressure steamed residues are relea-sed by means of a decompression chambre into a dozing bin. From the dozing bin the residue fibres are transported and conveyed into a refiner. A refining is executed by a disc refiner under pressurized and or atmospheric discharge operation.
An apparatus in accordance with the present invention includes an intergrated system having a chemical pretreatment metering means in to the wood residue flow, metering means of residues into a residue compression chambre, residue compressing means, air a~d moisture relieve means from a residue compression means, means to activate pocket valve of a compression means, means to discharge a pocket valve into the pressurized steam vessel, means to move the fibre residues inside the steam press-ure vessel, means for activating the worm conveyor according to predetermined infor~lations received from the residue metering means, means of unloading fibre residues from a steam pressurized vessel into a decompression means, means to release the fibre residues from decompressed means to a dozing means, means trans-porting and conveying the decompressed fibre residues into the refining means.
A further feature of the present invention includes a control system which includes a first scanning means at the infeed of wood residues, input data receiving means for interp-reting the data received from the first scanning means and for measuring the moisture content of the residue and weight-volume input according to the predetermined parameters, means associat-ed with said control system for activating a speed control of the residue infeed, measuring means controled by the control system means of the residue flow control system based on said data to introduce chemicals in solution and or in a dry form into the residue flow, means for controling the pocket valve or fibre plug activity, means to activate the discharging of vegetable fibres into a pressure vessel, means related to flow of ,.
~2~L~25~5 vegetable fibres into a vegeta~le fibres compression means, means to interpret rate of feed to control the residue movement in a steam pressure vessel according to the predetermined schedule stored in a memory, sensing means associated with discharge of residues from pressure steam vessel~ input data receiving means for interpreting and controling the refining mechanism and refining accordin~ to a predetermined refining patterns stored in the memory.
Ha~ing thus generally described the nature of the inv-ention, reference will now be made to the accompanying drawings, showing by way of illustration, a preferred embodiment thereof and in which:
Figure 1 is a diagram illustrating the various steps af a continuous process;
Figure 2 is a diagram illustrating the various reactions and changes of properties of residues from wood type form to pulp type form;
Figure 3 is illustrating step-by-step the process sequence of converting wood residues into a marketable pulp;
Figure 4 depicts the process of brightening or bleaching.
Referring now to the drawings and particulary to figure 1, there is shown an integrated processing mill for con-version of wood chips and or wood residues into wood pulp. An embodiment of the integrated processing mill includes a chip or residue conveyor 1 for conveying chips or wood residues, a pretreatment station 2 for application of chemicals, chips and residue level detector 17 for controling the flow of chips and residues through the pretreatment station and for controling the level of chemicals 4 in the first pretreatment station 2 a further a worm conveyor 3 for conveying residues from first pretreatment station 2 on to a residue conveyor 5 leadi.ng into second pretreatment station 6. A further scanner 18 may be ~2~;~50~;
provided for again measuring the residue volume from the second pretreatment station 6 into the compression chamber 8 operating under a predetermined pressure, compressed residues are then advanced through a pocket valve or fibre plug 9 through a steam pressure vessel 10, through a decompression chamber 11 and 12 into a dozing bin 13 and from the dozing bin through a washing station 14 or directly on to worm conveyor 15, bypassing the washing station,leading into the refiner 16. Refi.ned pulp is discharged into latency chest 19 and further the refined pulp may be introduced in to the bleaching station 20. Figure 2 shows reactions of chemical pretreatment of vegetable fibres 20 by complexing agents 21 and formation of hydrophylic group 22,23,24, 25, 26, 27, on wood surface, creat:inc3 a bond 28 it also demonstrates formation of hydrophilic group 22, 23, 24 on surface of residues 20 by oxidating agents 21.
Figure 3 is the step by step process sequence of che-mical reactions by various pretreatment of residues:
~tep 1- rrrys to eliminate free metalic cations which may cata-lize oxidation of SO2 to SO3,elimination is done by complexing with complexing agent DTPA or others.
Free metal ~ DTPA-~-------- Metal-DTPA
(non-reactive complex) Example: Ee, Mn, Cu, Al, etcO Metals may be pressnt in different valences.
To protect against oxydation, residues are pretreated with DTPA -Sodium Diethylenetriaminopentaactate (.5-3% ) or TPT - Sodium Tripolyphosphate EDTA - Ethylen Diamietetraacetic Acid -Nitriloacetic Acid Further treatment is done by the following agen-ts:
Sodium Sulphite Na2SO3 (Equilibrium pH 9.3) or Ozone- O3 or 25~i !~ Oxygene or Peracetic Acid or ClO2 Bioxide of chlore or NaClO2 or NaHS~3 or H2O2- Hydrogene Peroxide or Na2O2 Sodium peroxide or Steps 2-5 are designed to form Hydrophylic group by:
-sulfonation and/or -oxydation The formation of Hydrophylic groups either by oxidation and/or sulfonation is proportional to the concentration of chemicalproducts, wood residue, time and temperature.
At constant concentration of residue and chemicals used, the process is controlled by time and retention temperature.
In Step no. 2 and 3 determining factor for chemical reaction is time, since the temperature is very low.
In the step number 4, it is the temperature which con-trols the extent of sulfonation or oxidation. The speed of the sulfonation or oxidation may be also varied by concentration of the chemical product.
Further figure 3 depicts step by step the se~uence of the process of pretreatment of residues, its defibration and its refining as fo]lows:
Step 1- To prevent degradation by burning of residues which may take place in residue pressure steaming vessel, residues are mixed in solution of O5-3~0~ solution related to dry weight of residues at ambiant temperature and under atmospheric pressure.
Step 2- In order to form hydrophilic group on the surface of residues the following treatment is made:
-with sulphonating agents; DTPA
Sodiumdiethylenetriaminopentaacetate and others ` ~Zl~S~S
-with oxidative agents; TPF as sodium tripolyphosphate, ethylen diamietetraacetic acid.
This begins a topochemical reaction which consist in diffusion of chemical agents inside of the wood resi-dues and subsequently chemical reaction with the wood substrate.
Step 3- In order to increase the efficiency of the reaction and or the rate of diffusion the residues are introdu-ced into a compression-decompression cha~ber.
0 Step 4- After the compression-decompression of residues, the residues are trar~sferred into pressure steaming vessel, to complete the saturation process of residues,a final part of chemicals is introduced by steam at the beginning of a steam pressure vessel, major parts of hydrophylic groups are formed in the vessel due to high temperature and time of retention.
Step 5- Treated residues leave the pressurized vessel into a decompression chamber where de~ibration of residues occures. Further, residues are conveyed to a dozing ~0 bin under atmospheric pressure.
Step 6- Defibrated residues are conveyed through a washing station and/or they are conveyed without washing into a refiner.
Step 7- Depending on the pre-determined quality of pulp, refining of defibrated residues is directed to achie-ve ~anadians Standard Freenes varying from 600 to 50 CSF.
This is achieved by using commercial atmosphe-ric refinèrs and/or pressurized refiners.
According to the final product requirement,the pulp could be used as it is and/or could be transferred to other treatments as follows;bleaching treatment, curl setting, latency, screening, or cleaning.
Z~
"SUPPL~MENTARY DISCLOSURE" r Prior to noncompulsory bleaching the refined pulp is washed, noncompulsury screened, cleaned, thickened and preferably bleached in a single stage process. The brightness increase of up to 32 points have been experienced during laboratory and pilot bleaching trials with Hydrogene Peroxide H202, Sodium Peroxide Na202, Oxygene 2 and Ozone 03 Magnesium Sulfat, Sodium Silicate, DTPA, Sodium ~ydroxyde at pulp consistency range of 12% to 40~. Brightness reversion protection have been succesfully achieved by non compulsory diffusion washing and post treatment with Sulfur Bioxyde S02.
Claims (6)
1. A process of producing pulp from tree chips, sawmill residues, wood or vegetable fibres comprising the combination in sequence of the steps of:
conveying of vegetable fibres for a pretreatment, impregnation with chemicals, compression of vegetable fibres to extract air between the fibres and to extract some of the liquid from the fibres, followed by loading sequence step carried out by one of the following: pocket valve, loading screw, or vegetable fibre plug created by mechanical or hydraulical means into pressurized steam vessel, followed by hydrolytic reaction at preselected steam pressure, temperature and retention of said vegetable fibre in the said pressurized steam vessel, followed by releasing the vegetable fibres into decompression chamber for de-fibration, followed by pulping, using either atmo-spheric or pressurized refiners, followed by screaning, cleaning of the produced pulp, all parameters for each individual step are predetermined in advance and are programed in an integrated control system.
conveying of vegetable fibres for a pretreatment, impregnation with chemicals, compression of vegetable fibres to extract air between the fibres and to extract some of the liquid from the fibres, followed by loading sequence step carried out by one of the following: pocket valve, loading screw, or vegetable fibre plug created by mechanical or hydraulical means into pressurized steam vessel, followed by hydrolytic reaction at preselected steam pressure, temperature and retention of said vegetable fibre in the said pressurized steam vessel, followed by releasing the vegetable fibres into decompression chamber for de-fibration, followed by pulping, using either atmo-spheric or pressurized refiners, followed by screaning, cleaning of the produced pulp, all parameters for each individual step are predetermined in advance and are programed in an integrated control system.
2. Apparatus including an integrated system for producing wood or vegetable pulp from wood or vegetable fibres consisting of the combination in sequence of the following apparatus parts, assemblies and units having a chemical pretreatment metering means of the wood or vegetable fibre, followed by metering means of said fibres into compression chamber, followed by compressing means, followed by means to activate one of the following: pocket valve, loading screw or residue plug created either by mechanical or hydraulical means to discharge said wood or vegetable fibres into the pressurized steam vessel, followed by means to complete the chemical pretreatment by mixture of chemicals and steam, followed by means to inject the chemicals and steam mixture into the steam pressure vessel, followed by means to move the wood or vegetable fibres inside the steam pressure vessel, followed by means for activating the said wood or vegetable fibres moving means according to predetermined information received from the residue metering means, followed by means to unload wood or vegetable fibres from steam pressurized vessel into decompression means, followed by means to release the fibres from decompression means to dozing means, followed by transportation and conveying means of the decompressed said fibres to diffusion washers or applicators of chemicals followed by transportation and conveying means of washed and chemicaly treated said fibres into the refining means.
3. An integrated control system as claimed in claim 2 which further includes a first scanning means at the infeed of wood and vegetable fibres in form of chips or residues, input data receiving means for interpreting the data received from the first scanning means and for measuring the moisture content of the residue and weight-volume input according to the predetermined parameters, means associated with said control system for activating a speed control of the residue infeed, measuring means controlled by the control system means of the residue flow control system based on said data to introduce chemicals in solution or in dry form into the residue flow, means for controlling one of the following: pocket valve, or loading screw or residue plug activity, further includs means to activate the discharging of residues into a pressure vessel, means related to flow of residues into a residue compression means, means to interpret rate of feed to control the residue movement in a steam pressure vessel according to the predetermined schedule stored in a memory, sensing means associated with discharge of residues from steam pressure vessel, input data receiving means for interpreting and controlling the refining mechanism and refining according to a predetermined refining patterns stored in the memory, the measurement is done by sensing means located in strategic areas of each step.
4. A process according to claim number 1 of converting wood chips, wood residues and vegetable fibres into wood pulp including process step of protection the said fibre against subsequent degradation, by binding of metal cations present, with completing agents, process step of chemical treatment with sulfonating agents in order to introduce hydrophilic sulfonated group in wood or vegetable fibres, process step of chemical treatment with oxidating agents in order to form hydrophilic groups, hydroxide groups, carboxylic groups, hydroperoxide groups, aldehyde groups on wood or vegetable fibres or residue surface, process step of chemical treatment with antraqinon in combination either with sodium hydroxide and sodium sulfite or sodium bisulfite in order to form hydrophylic groups on residues and to facilitate lignin modification, process step of residue compression, decompression and process step of alternating compression, decompression, compression in order to assure air removal and subsequent chemical penetration of chemicals into wood, vegetable fibre or residue, process step of complementary chemical treatment of said fibre when introducing it into a pressurized steam vessel, process step of physico-chemical reaction inside of pressurized steam vessel, process step of defibration in a decompression chamber, process step of washing and displacement of chemicals from defibrated products in diffusion washers, process step of atmospheric refining or process step of pressurized refining, process step of screaning and cleaning of the produced pulp.
5. Process according to claim 1 includes the step wherein complexing of the said wood and vegetable fibre is carried out employing one or more of the following complexing agents:
DTPA Sodiumdiethylenetriaminpentaacetate in a concentration range of 0.1% to 5.0%, TPF sodiumtripolyphosphate in a concentration range of 0.1% to 5%
ethylene diamintetraacetic acid EDTA in a concentration range of 0.1% to 5%, nitriloacetic acid in a concentration range of 0.1% to 6.0%, triethylamin in a concentration range of 0.1% to 7%, citric acid in a concentration range of 0.1% to 7%, the step wherein sulfonation is carried out employing one or more of the following sulfonation agents:
Na2SO3 sodium sulfite in a concentration range of 0.5%
to 15.0%, Na2SO3 sodium sulphite in a concentration range of 0.5% to 15% plus NaOH sodium hydroxide in a concentration range from .1% to 7.5% in case of broad leaf species, the step wherein oxidation is carried out employing one or more of the oxidation agents:
hydrogene peroxide in a concentration range of 1% to 20%, sodium silicate in a concentration range of 0.1% to 5.0%, magnesium sulphate in a concentration range of 0.1% to 3.0%, pH is adjusted if necessary by sodium hydroxide in a concentration range of 0.1% to 10.0%, sodium peroxide Na2O2 in a concentration range of 1% to 20%, sodium silicate in a concentration range of 0.1% to 5%, magnesium sulphate in a concentration range of 0.1% to 5%, ClO2 in a concentration range of 0.1% to 20.0% and pH in a range of 4-6.5, temperature in a range of 40°-60°C, NaClO2 in a concentration range of 0.1% to 20% pH in a range of 4-12, temperature in a range of 40°-60°C, peracetic acid in a concentration range of 0.1% to 20%, ozone O3 in a concentration range of 0.1% to 8%, MgSO4 in a concentration range of 0.1% to 4.0%, NaOH in a concentration range of 0.1% to 4%, oxygen °2 in a concentration range of 1% to 10%, MgSO4 in a concentration range of 0.1% to 4%, NaOH in a concentration range of 1% to 4%, BIS t-butylperoxide diisopropylbenzene in a concentration range of 1% to 10%, Di-t-butyl peroxide in a concentration range of 0.1% to 10%, Di-cumylperoxide in a concentration range of 0.1%to 10%, t. butyl cumyl peroxide in a concentration range of0.1% to 10%, all percentages are calculated by weight related to dry weight of fibres, the step wherein compression and decompression is carried out in an range of 5-2-5-2-5 atms., in a range of time of 1 to 15 minutes, temperature in a range of 20°-120°C, said wood or vegetable fibres in a concentration range of 1% - 30%, the step wherein complementary chemical addition is carried out in a concentration of 1% -5% of sulfonating or oxidating agents at the entry in to steam pressurized vessel, temperature in a range of 130° C to 220° C, saturated steam pressure in a range of 0.5 MPa to 2.5 MPa, time in a range of 10 seconds to 30 minutes, wherein the step of defibration is carried out in decompression chamber to atmospheric pressure, the step wherein diffusion washing or chemical addition of sulfonating, bleaching or completing agents are followed by the step wherein atmospheric refining is carried out in a concentration range of 5% to 25%, freeness in a range from 700 to 50 CSF(Canadian Standard Freeness), or the step wherein pressurized refining is carried out in a pressure range of 1.5 - 15 atms., in a consistency range of 5% - 40%, freeness in a range from 700 to 50 CSF followed by the step of non co.mpulsory washing, screening and cleaning of the produced pulp.
"CLAIMS SUPPORTED BY SUPPLEMENlARY DISCLOSURE"
DTPA Sodiumdiethylenetriaminpentaacetate in a concentration range of 0.1% to 5.0%, TPF sodiumtripolyphosphate in a concentration range of 0.1% to 5%
ethylene diamintetraacetic acid EDTA in a concentration range of 0.1% to 5%, nitriloacetic acid in a concentration range of 0.1% to 6.0%, triethylamin in a concentration range of 0.1% to 7%, citric acid in a concentration range of 0.1% to 7%, the step wherein sulfonation is carried out employing one or more of the following sulfonation agents:
Na2SO3 sodium sulfite in a concentration range of 0.5%
to 15.0%, Na2SO3 sodium sulphite in a concentration range of 0.5% to 15% plus NaOH sodium hydroxide in a concentration range from .1% to 7.5% in case of broad leaf species, the step wherein oxidation is carried out employing one or more of the oxidation agents:
hydrogene peroxide in a concentration range of 1% to 20%, sodium silicate in a concentration range of 0.1% to 5.0%, magnesium sulphate in a concentration range of 0.1% to 3.0%, pH is adjusted if necessary by sodium hydroxide in a concentration range of 0.1% to 10.0%, sodium peroxide Na2O2 in a concentration range of 1% to 20%, sodium silicate in a concentration range of 0.1% to 5%, magnesium sulphate in a concentration range of 0.1% to 5%, ClO2 in a concentration range of 0.1% to 20.0% and pH in a range of 4-6.5, temperature in a range of 40°-60°C, NaClO2 in a concentration range of 0.1% to 20% pH in a range of 4-12, temperature in a range of 40°-60°C, peracetic acid in a concentration range of 0.1% to 20%, ozone O3 in a concentration range of 0.1% to 8%, MgSO4 in a concentration range of 0.1% to 4.0%, NaOH in a concentration range of 0.1% to 4%, oxygen °2 in a concentration range of 1% to 10%, MgSO4 in a concentration range of 0.1% to 4%, NaOH in a concentration range of 1% to 4%, BIS t-butylperoxide diisopropylbenzene in a concentration range of 1% to 10%, Di-t-butyl peroxide in a concentration range of 0.1% to 10%, Di-cumylperoxide in a concentration range of 0.1%to 10%, t. butyl cumyl peroxide in a concentration range of0.1% to 10%, all percentages are calculated by weight related to dry weight of fibres, the step wherein compression and decompression is carried out in an range of 5-2-5-2-5 atms., in a range of time of 1 to 15 minutes, temperature in a range of 20°-120°C, said wood or vegetable fibres in a concentration range of 1% - 30%, the step wherein complementary chemical addition is carried out in a concentration of 1% -5% of sulfonating or oxidating agents at the entry in to steam pressurized vessel, temperature in a range of 130° C to 220° C, saturated steam pressure in a range of 0.5 MPa to 2.5 MPa, time in a range of 10 seconds to 30 minutes, wherein the step of defibration is carried out in decompression chamber to atmospheric pressure, the step wherein diffusion washing or chemical addition of sulfonating, bleaching or completing agents are followed by the step wherein atmospheric refining is carried out in a concentration range of 5% to 25%, freeness in a range from 700 to 50 CSF(Canadian Standard Freeness), or the step wherein pressurized refining is carried out in a pressure range of 1.5 - 15 atms., in a consistency range of 5% - 40%, freeness in a range from 700 to 50 CSF followed by the step of non co.mpulsory washing, screening and cleaning of the produced pulp.
"CLAIMS SUPPORTED BY SUPPLEMENlARY DISCLOSURE"
6. Process of brightening the refined pulp obtained by the process of claims 1, 4 or 5, comprising the step wherein bleaching of refined pulp is carried out employing one or more of the bleaching agents:
Hydrogene Peroxide H2O2 in a concentration range of 0.5% to 10 Sodium Peroxide Na2O2 in a concentration range of0.5% to 10%, Magnesium Sulfat MgSO4 in a concentration range of 0.1% to 2%, Sodium silicate Na2SiO3 in a concentration range of 1.0%
to 4% as a buffer, DTPA in a concentration range of 0.1% to 0.5%, Sodium hydroxide NaOH in a concentration range of 1.0% to 5%
in a range of pH 9-11 adjustement, at temperature range of 40°C to 70°C, at retention time of 60 to 120 minutes, at consitency range of pulp 12% to 40% of dry fibre weight base, Oxygen O2, at pressure range of 2 to 6 atmospheres, at temperature range of 80°C to 140°C, at retention time range of 45 minutes to 120 minutes, Ozone O3, at pressure range of 1 to 3 atmospheres at temperature range of 70°C to 150°C, at retention time range of 40 minutes to 120 minutes, at pulp consistency range of 12% to 40%, resulting in brightness increase of up to 32%
in the single stage bleaching sequence, includes the step wherein brightness reversion protection is achieved by sulfur bioxyde SO2 treatment in a concentration range of 0.1% to 1.0% and retention time range of 5 minutes to 60 minutes, includes the step, wherein noncompulsory water washing is carried out after each bleaching agent reaction, all percentages being based upon the dry weight of said veyetable fibres.
Hydrogene Peroxide H2O2 in a concentration range of 0.5% to 10 Sodium Peroxide Na2O2 in a concentration range of0.5% to 10%, Magnesium Sulfat MgSO4 in a concentration range of 0.1% to 2%, Sodium silicate Na2SiO3 in a concentration range of 1.0%
to 4% as a buffer, DTPA in a concentration range of 0.1% to 0.5%, Sodium hydroxide NaOH in a concentration range of 1.0% to 5%
in a range of pH 9-11 adjustement, at temperature range of 40°C to 70°C, at retention time of 60 to 120 minutes, at consitency range of pulp 12% to 40% of dry fibre weight base, Oxygen O2, at pressure range of 2 to 6 atmospheres, at temperature range of 80°C to 140°C, at retention time range of 45 minutes to 120 minutes, Ozone O3, at pressure range of 1 to 3 atmospheres at temperature range of 70°C to 150°C, at retention time range of 40 minutes to 120 minutes, at pulp consistency range of 12% to 40%, resulting in brightness increase of up to 32%
in the single stage bleaching sequence, includes the step wherein brightness reversion protection is achieved by sulfur bioxyde SO2 treatment in a concentration range of 0.1% to 1.0% and retention time range of 5 minutes to 60 minutes, includes the step, wherein noncompulsory water washing is carried out after each bleaching agent reaction, all percentages being based upon the dry weight of said veyetable fibres.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000459020A CA1212505A (en) | 1984-07-17 | 1984-07-17 | Method, process and apparatus for converting wood, wood residue and or biomass into pulp |
| EP85810326A EP0172135A1 (en) | 1984-07-17 | 1985-07-17 | Method, process and apparatus for converting wood, wood residue, vegetable fibre and biomass into pulp |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CA000459020A CA1212505A (en) | 1984-07-17 | 1984-07-17 | Method, process and apparatus for converting wood, wood residue and or biomass into pulp |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1212505A true CA1212505A (en) | 1986-10-14 |
Family
ID=4128326
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000459020A Expired CA1212505A (en) | 1984-07-17 | 1984-07-17 | Method, process and apparatus for converting wood, wood residue and or biomass into pulp |
Country Status (2)
| Country | Link |
|---|---|
| EP (1) | EP0172135A1 (en) |
| CA (1) | CA1212505A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU616541B2 (en) * | 1988-07-12 | 1991-10-31 | Atochem | Process for the manufacture of bleached chemithermomechanical pulps |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CA1230208A (en) * | 1987-03-24 | 1987-12-15 | Bohuslav V. Kokta | Process for preparing pulp for paper making |
| FR2615874B1 (en) * | 1987-05-25 | 1992-02-21 | Atochem | PROCESS FOR THE PREPARATION OF CHEMICOTHERMOMECHANICAL PASTES |
| US5338402A (en) * | 1987-05-25 | 1994-08-16 | Societe Atochem | Process for preparing a bleached chemithermomechanical pulp |
| CA2037275A1 (en) * | 1991-02-28 | 1992-08-29 | Bohuslav V. Kokta | Steam explosion pulping process for papermaking |
| NZ248884A (en) * | 1993-10-07 | 1995-10-26 | Convertech Group Ltd | Hydrolysis and/or drying of biological material with steam |
| NZ248895A (en) * | 1993-10-08 | 1995-07-26 | Convertech Group Ltd | Transfer device having intermittently rotated carousel having through passageways with assembly sealing pressure maximised during rotor dwell periods |
| US5522967A (en) * | 1994-05-27 | 1996-06-04 | Kimberly-Clark Corporation | Sulfonated cellulose and method of preparation |
| US5703225A (en) * | 1995-12-13 | 1997-12-30 | Kimberly-Clark Worldwide, Inc. | Sulfonated cellulose having improved absorbent properties |
| FR2751671B1 (en) * | 1996-07-26 | 1998-09-25 | E Mc2 Dev | PROCESS FOR THE MANUFACTURE OF BLEACHED PAPER PULP |
| WO2000019004A1 (en) * | 1998-09-25 | 2000-04-06 | Stake Technology Ltd. | Semi alkaline steam explosion treatment of fibrous material for the production of cellulose pulp |
| KR20010100017A (en) | 1998-12-30 | 2001-11-09 | 로날드 디. 맥크레이 | Steam Explosion Treatment with Addition of Chemicals |
| US6413362B1 (en) | 1999-11-24 | 2002-07-02 | Kimberly-Clark Worldwide, Inc. | Method of steam treating low yield papermaking fibers to produce a permanent curl |
| US7300541B2 (en) * | 2002-07-19 | 2007-11-27 | Andritz Inc. | High defiberization chip pretreatment |
| CA2507321C (en) | 2004-07-08 | 2012-06-26 | Andritz Inc. | High intensity refiner plate with inner fiberizing zone |
| US7300540B2 (en) | 2004-07-08 | 2007-11-27 | Andritz Inc. | Energy efficient TMP refining of destructured chips |
| BRPI0916139A8 (en) | 2008-11-21 | 2018-02-06 | Inbicon As | method for the transfer of particulate and / or fibrous raw material. and apparatus for the transfer of particulate and / or fibrous raw material |
| US9512237B2 (en) | 2009-05-28 | 2016-12-06 | Gp Cellulose Gmbh | Method for inhibiting the growth of microbes with a modified cellulose fiber |
| US9512563B2 (en) | 2009-05-28 | 2016-12-06 | Gp Cellulose Gmbh | Surface treated modified cellulose from chemical kraft fiber and methods of making and using same |
| KR101797943B1 (en) | 2009-05-28 | 2017-11-15 | 게페 첼루로제 게엠베하 | Modified cellulose from chemical kraft fiber and methods of making and using the same |
| US9511167B2 (en) | 2009-05-28 | 2016-12-06 | Gp Cellulose Gmbh | Modified cellulose from chemical kraft fiber and methods of making and using the same |
| BR112013030060A2 (en) | 2011-05-23 | 2018-01-16 | Gp Cellulose Gmbh | kraft resin wood fibers and board and their method for making kraft fiber |
| MX366988B (en) | 2012-01-12 | 2019-08-01 | Gp Cellulose Gmbh | A low viscosity kraft fiber having reduced yellowing properties and methods of making and using the same. |
| WO2013158384A1 (en) | 2012-04-18 | 2013-10-24 | Georgia-Pacific Consumer Products Lp | The use of surfactant to treat pulp and improve the incorporation of kraft pulp into fiber for the production of viscose and other secondary fiber products |
| EP2954115B1 (en) | 2013-02-08 | 2022-01-12 | GP Cellulose GmbH | Softwood kraft fiber having an improved a-cellulose content and its use in the production of chemical cellulose products |
| BR112015019882A2 (en) | 2013-03-14 | 2017-07-18 | Gp Cellulose Gmbh | oxidized bleached kraft fiber and methods for making kraft pulp and softwood kraft fiber and for bleaching multi-stage bleaching cellulose kraft pulp |
| CA2901915A1 (en) | 2013-03-15 | 2014-09-18 | Gp Cellulose Gmbh | A low viscosity kraft fiber having an enhanced carboxyl content and methods of making and using the same |
| US10865519B2 (en) | 2016-11-16 | 2020-12-15 | Gp Cellulose Gmbh | Modified cellulose from chemical fiber and methods of making and using the same |
| FI129928B (en) * | 2019-01-29 | 2022-11-15 | Upm Kymmene Corp | Method and arrangement for feedback based control in chemical refining of wood |
| CN109706772B (en) * | 2019-02-01 | 2020-06-30 | 丰禾新材（北京）技术有限公司 | Normal pressure paper pulp making process |
| CN113718545A (en) * | 2020-05-25 | 2021-11-30 | 海安县金鑫纸业有限公司 | Papermaking control system for maintaining quantification, thickness and moisture stability |
| CN114351497B (en) * | 2021-12-27 | 2023-05-02 | 湛江晨鸣浆纸有限公司 | Preparation process of broad-leaved wood bleached mechanical pulp |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3012927A (en) * | 1957-09-11 | 1961-12-12 | Process Evaluation Devel | Continuous process of converting vegetable stock to paper pulp |
| SE352120B (en) * | 1969-02-17 | 1972-12-18 | Reinhall Rolf | |
| US3822179A (en) * | 1969-02-27 | 1974-07-02 | N Chari | Method and apparatus for optimizing steam consumption of continuous digester |
| CA1075857A (en) * | 1976-02-20 | 1980-04-22 | Price Company Limited (The) | Chemical pretreatment of wood prior to making refiner groundwood |
| SE416481B (en) * | 1977-05-02 | 1981-01-05 | Mo Och Domsjoe Ab | METHOD AND DEVICE FOR TREATMENT OF WOOD TIP FOR REMOVAL OF HEAVY METALS AND RESIN |
-
1984
- 1984-07-17 CA CA000459020A patent/CA1212505A/en not_active Expired
-
1985
- 1985-07-17 EP EP85810326A patent/EP0172135A1/en not_active Withdrawn
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| AU616541B2 (en) * | 1988-07-12 | 1991-10-31 | Atochem | Process for the manufacture of bleached chemithermomechanical pulps |
Also Published As
| Publication number | Publication date |
|---|---|
| EP0172135A1 (en) | 1986-02-19 |
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