CN110258160A - A kind of efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe and bleaching system - Google Patents
A kind of efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe and bleaching system Download PDFInfo
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- CN110258160A CN110258160A CN201910667844.4A CN201910667844A CN110258160A CN 110258160 A CN110258160 A CN 110258160A CN 201910667844 A CN201910667844 A CN 201910667844A CN 110258160 A CN110258160 A CN 110258160A
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- Prior art keywords
- bleaching
- temperature
- chlorine dioxide
- high temperature
- acidification
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- 238000004061 bleaching Methods 0.000 title claims abstract description 174
- OSVXSBDYLRYLIG-UHFFFAOYSA-N dioxidochlorine(.) Chemical compound O=Cl=O OSVXSBDYLRYLIG-UHFFFAOYSA-N 0.000 title claims abstract description 142
- 239000004155 Chlorine dioxide Substances 0.000 title claims abstract description 72
- 235000019398 chlorine dioxide Nutrition 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title claims abstract description 47
- QAOWNCQODCNURD-UHFFFAOYSA-N sulfuric acid Substances OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 53
- 230000020477 pH reduction Effects 0.000 claims abstract description 36
- 239000002002 slurry Substances 0.000 claims abstract description 36
- 229920001131 Pulp (paper) Polymers 0.000 claims abstract description 28
- 239000002253 acid Substances 0.000 claims abstract description 23
- 239000002535 acidifier Substances 0.000 claims abstract description 20
- 230000015556 catabolic process Effects 0.000 claims abstract description 12
- 238000006731 degradation reaction Methods 0.000 claims abstract description 12
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims abstract description 10
- 230000035484 reaction time Effects 0.000 claims abstract description 6
- 239000000706 filtrate Substances 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 18
- 239000011440 grout Substances 0.000 claims description 15
- 239000007844 bleaching agent Substances 0.000 claims description 8
- 238000005406 washing Methods 0.000 claims description 8
- 238000005260 corrosion Methods 0.000 claims description 7
- 230000007797 corrosion Effects 0.000 claims description 7
- 239000000463 material Substances 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 238000006386 neutralization reaction Methods 0.000 claims description 5
- 239000000919 ceramic Substances 0.000 claims description 4
- 229910000975 Carbon steel Inorganic materials 0.000 claims description 3
- 239000010962 carbon steel Substances 0.000 claims description 3
- 238000011017 operating method Methods 0.000 claims description 3
- 239000010935 stainless steel Substances 0.000 claims description 3
- 229910001220 stainless steel Inorganic materials 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 abstract description 14
- 239000003513 alkali Substances 0.000 abstract description 4
- XTEGARKTQYYJKE-UHFFFAOYSA-N chloric acid Chemical compound OCl(=O)=O XTEGARKTQYYJKE-UHFFFAOYSA-N 0.000 abstract description 2
- 229940005991 chloric acid Drugs 0.000 abstract description 2
- 238000007865 diluting Methods 0.000 abstract 1
- 230000003301 hydrolyzing effect Effects 0.000 abstract 1
- NHYCGSASNAIGLD-UHFFFAOYSA-N Chlorine monoxide Chemical compound Cl[O] NHYCGSASNAIGLD-UHFFFAOYSA-N 0.000 description 50
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 8
- 239000000460 chlorine Substances 0.000 description 8
- 229910052801 chlorine Inorganic materials 0.000 description 8
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 6
- 239000007788 liquid Substances 0.000 description 6
- 241000609240 Ambelania acida Species 0.000 description 4
- 244000166124 Eucalyptus globulus Species 0.000 description 4
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 4
- 239000010905 bagasse Substances 0.000 description 4
- 239000002585 base Substances 0.000 description 4
- 239000001301 oxygen Substances 0.000 description 4
- 229910052760 oxygen Inorganic materials 0.000 description 4
- 238000004076 pulp bleaching Methods 0.000 description 4
- 239000004408 titanium dioxide Substances 0.000 description 3
- 230000008901 benefit Effects 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- BZSXEZOLBIJVQK-UHFFFAOYSA-N 2-methylsulfonylbenzoic acid Chemical compound CS(=O)(=O)C1=CC=CC=C1C(O)=O BZSXEZOLBIJVQK-UHFFFAOYSA-N 0.000 description 1
- 229920002472 Starch Polymers 0.000 description 1
- DFGWJCZWKBGVOX-UHFFFAOYSA-N [Cl+].[O-2].[O-2].[Ti+4] Chemical compound [Cl+].[O-2].[O-2].[Ti+4] DFGWJCZWKBGVOX-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000012467 final product Substances 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000013011 mating Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000012946 outsourcing Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000013055 pulp slurry Substances 0.000 description 1
- 238000004537 pulping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 235000019698 starch Nutrition 0.000 description 1
- 239000008107 starch Substances 0.000 description 1
- 238000012360 testing method Methods 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
- D21C9/00—After-treatment of cellulose pulp, e.g. of wood pulp, or cotton linters ; Treatment of dilute or dewatered pulp or process improvement taking place after obtaining the raw cellulosic material and not provided for elsewhere
- D21C9/10—Bleaching ; Apparatus therefor
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/08—Pipe-line systems for liquids or viscous products
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
Abstract
The present invention discloses a kind of efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe and bleaching system, the bleaching system by brown stock washers, in dense standpipe, acidification steam heater, acidification mixer, N-shaped acidifier, bleaching steam heater, bleaching mixer, high-temperature bleaching tower, high-temperature bleaching section wash engine etc. form.The method for bleaching is first acidified paper pulp with high temperature acidified pretreating process in advance, in acidified degradation paper pulp while HexA, neutralizes the residual alkali of slurry carrying before drift, avoids residual alkali from hydrolyzing the chloric acid generated with chlorine dioxide and reacts；After high temperature acidified pretreated slurry is mixed with chlorine dioxide, then carry out high temperature ClO 2 bleaching.The present invention can shorten the reaction time of conventional high temperature ClO 2 bleaching, save the cost of manufacture of high-temperature bleaching tower, and can reduce the steam consumption of bleaching, and after the concentrated sulfuric acid and acid saltcake solution mixed diluting for being acidified, slurry pipe is added, corrosivity is not strong, and production operation safety coefficient is high.
Description
Technical field
The invention belongs to chlorine dioxide pulp bleaching technology field, specifically a kind of efficient high temperature titanium dioxide of energy-saving safe
Chlorine dioxde pulp bleaching process and bleaching system.
Background technique
The bleaching agent that chlorine dioxide is high as a kind of bleaching efficiency, selectivity is strong, bleaching effluent pollutional load is low, at present quilt
It is widely used in pulping and paper-making industry.But because its high production cost (in particular by the production method of the raw materials such as outsourcing sodium chlorate,
About 10,000 yuan of the production cost of chlorine dioxide per ton), considerably increase paper pulp bleaching production cost.
Traditional ClO 2 bleaching technique is to starch without oxygen delignification, using conventional D0-Ep-
D1Chlorine-free bleaching process, finished pulp are bleached to the whiteness of 85% (ISO), and bagasse pulp slurry per ton consumes total chlorine dioxide (D0+
D1) it is generally 15-20kg, the ClO 2 bleaching cost about 150-200 member of slurry per ton, the Chlorine that wood pulp needs is more
It is high.For this purpose, the ClO 2 bleaching mode that research and development are energy-efficient, reducing enterprise's production run cost becomes inevitable.
High temperature ClO 2 bleaching technique (Dht) it is exactly a kind of ClO 2 bleaching technique after optimization, which, which replaces, passes
The D of system0Bleach paragraph heats slurry in first segment ClO 2 bleaching process, enriching sulfuric acid and with steam, slurry is made to carry out two
While chlorine monoxid reacts, progress is high temperature acidified, and the HexA in paper pulp is made to degrade, and reduces the two of entire bleachery to reach
The purpose of chlorine monoxid dosage, but the technique has the disadvantage in that the concentrated sulfuric acid 1) for acidification adds in pulp-entering pipe, (contains with slurry
90% or so moisture) heat release can be diluted after mixing, slurry corrosive pipeline perforation is easily led to, security risk is high；2) high-temperature bleaching
Reaction temperature is up to 90 DEG C or so, needs to consume a large amount of steam, although Chlorine can be reduced, in steam unit cost
In the case where height, comprehensive production cost is without significant advantage；3) the high-temperature bleaching reaction time, (conventional bleaching was 1 small up to 2 hours
When), it is therefore desirable to ClO 2 bleaching tower volume it is big (inside lining anti-corrosive resin simultaneously pastes acid-proof ceramic tile), cost is high, project construction
Investment is big.
For these reasons, high temperature ClO 2 bleaching can not be promoted on a large scale.For this reason, it may be necessary to research and develop a kind of energy-saving safe
Efficient high temperature ClO 2 bleaching method and bleaching system.
Summary of the invention
Technical problem to be solved by the invention is to provide a kind of efficient high temperature chlorine dioxide pulp bleachings of energy-saving safe
Method and bleaching system can be reduced chlorine dioxide use using the device and operating method while guaranteeing system safety operation
Amount reduces bleaching steam consumption, reduces project construction cost of investment.
The present invention solves above-mentioned technical problem with following technical solution:
A kind of efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe of the present invention, including following operating procedure:
1) paper pulp is through high temperature acidified pretreatment: first will slurry is washed before drift is concentrated into 10-12%, and after through being steam heated to
Desired temperature is reacted, N-shaped acidifier is entered after mixing with dilute sulfuric acid and carries out acid-base neutralization reaction and acidified degradation HexA, N-shaped
Souring temperature in acidifier is 80-85 DEG C, and the acidification time is 60min；
2) the pre-heat treatment is carried out to ClO 2 solution: first pre- with bleaching filtrate before ClO 2 solution is mixed with paper pulp
Heat is to 40 DEG C；The additional amount of ClO 2 solution is determining according to high-temperature bleaching section grout absorption and come the wash degree of the hardness, slurry starched,
It is general to pass through under identical reaction conditions, it carries out testing determining ton slurry Chlorine A (kg/Adt), then according to per small
When slurry through amount B (Adt/h) calculate Chlorine (Kg/h)=A (kg/Adt) × B (Adt/h))；
3) it carries out the processing of high temperature ClO 2 bleaching: by the paper pulp after acidizing pretreatment, being heated to reaction through steam benefit and want
It is anti-to enter high-temperature bleaching tower progress high temperature ClO 2 bleaching after the temperature asked, after mixing with the ClO 2 solution after preheating
It answers, while continuing acidified degradation HexA, the reaction temperature in high-temperature bleaching tower is 85-95 DEG C, reaction time 60min；
4) it carries out high-temperature wash: high-temperature bleaching tower treated paper pulp is sent into after the washing of high-temperature bleaching section wash engine to obtain the final product
To bleached pulp.
In step 1) of the present invention, the mass concentration of the dilute sulfuric acid is 10%, by by the concentrated sulfuric acid and acid saltcake
Solution mixing system obtains；The additional amount of dilute sulfuric acid is determined according to come the wash degree of the amount of slurry and slurry, it is desirable that reaches control high temperature titanium dioxide
The pH value starched after chlorine bleaching reaction is 2-3.
In step 4) of the present invention, high-temperature bleaching section wash engine is 2-3% into concentration is starched.
The bleaching system that the efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe of the present invention uses, including washed before drift
Pulp grinder, in dense standpipe, acidification steam heater, acidification mixer, N-shaped acidifier, bleaching steam heater, bleaching mixer,
High-temperature bleaching tower, high-temperature bleaching section wash engine；Through grout outlet one, the dense standpipe in is connect the brown stock washers, in dense standpipe warp
Middle underflow pipe is sequentially connected middle underflow pump, acidification steam heater, acidification mixer, N-shaped acidifier, in acidification steam heater
There is underflow pipe in the outlet end access of dilute sulfuric acid pipe between acidification mixer；N-shaped acidifier is sequentially connected drift through grout outlet two
White steam heater, bleaching mixer, high-temperature bleaching tower, bleaching between steam heater and bleaching mixer has chlorine dioxide to go out
Grout outlet is accessed in the outlet end of liquid pipe, and the input end of chlorine dioxide outlet tube connects chlorine dioxide preheater；High-temperature bleaching tower warp
Grout outlet three connects high-temperature bleaching section wash engine.
The input end of dilute sulfuric acid pipe of the present invention connects dilute acid bath through thin acid pump, and dilute acid bath and concentrated sulfuric acid pipe and saltcake are molten
Liquid pipe is connected.
Chlorine dioxide preheater of the present invention is heat exchanger, before and after tube side respectively with chlorine dioxide inlet tube and two
Chlorine monoxid outlet tube is connected, and is connected respectively with filtrate outlet tube and filtrate inlet tube before and after shell side.
N-shaped acidifier of the present invention selects the two-phase stainless steel material of acid corrosion-resistant to be made, and high-temperature bleaching tower is selected resistance to
Acid and the carbon steel of chlorine dioxide corrosion lining acid-proof ceramics material are made.
Acidification steam heater of the present invention and bleaching steam heater are separately connected steam pipe.
Compared to traditional high temperature ClO 2 bleaching technology, the beneficial effects of the present invention are:
1) present invention is acidified paper pulp by high temperature acidified pretreating process in advance, and HexA's is same in acidified degradation paper pulp
When, the residual alkali of slurry carrying before drift is neutralized, residual alkali is can avoid and is reacted with the chloric acid that chlorine dioxide hydrolysis generates, while reducing titanium dioxide
The available chlorine content of chlorine, to reduce the chlorine dioxide consumption of entire bleachery.
2) after high temperature acidified pretreated paper pulp is mixed with chlorine dioxide, then high temperature ClO 2 bleaching is carried out, it can be with
Shorten the reaction time of conventional high temperature ClO 2 bleaching, saves the cost of manufacture of high-temperature bleaching tower.
3) it before bleaching tower is added in chlorine dioxide, is first preheated with this section of filtrate, steam consumption can be reduced, save production cost.
4) slurry pipe is entered back into after first mixing with acid saltcake solution for the concentrated sulfuric acid of acidification, both can avoid concentrated sulfuric acid heat release
Corrosion slurry pipe, improves production operation safety, can also efficiently use the byproduct acidity saltcake of chlorine dioxide preparation system generation
Contained acid reduces sulfuric acid dosage.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the efficient high temperature ClO 2 bleaching device of energy-saving safe of the present invention.
In figure: 1- brown stock washers, dense standpipe in 2-, 3- middle underflow pump, 4- are acidified mixer, 5-n type acidifier, 6- bis-
Chlorine monoxid preheater, 7- bleach mixer, 8- high-temperature bleaching tower, 9- high-temperature bleaching section wash engine, and 10- grout outlet one is dense in 11-
Slurry pipe, 12- steam pipe one, 13- dilute sulfuric acid pipe, 14- grout outlet two, 15- chlorine dioxide inlet tube, 16- filtrate outlet tube, 17-
Filtrate inlet tube, 18- chlorine dioxide outlet tube, 19- grout outlet three, 20- are acidified steam heater, and 21- bleaches steam heater,
22- steam pipe two, 23- dilute acid bath, 24- thin acid pump, 25- concentrated sulfuric acid pipe, 26- saltcake solution conduit.
Specific embodiment
The present invention is described in detail below with reference to the accompanying drawings and embodiments, and described embodiment is only the present invention
A part of the embodiment, instead of all the embodiments.Based on the embodiments of the present invention, those of ordinary skill in the art are not having
Every other embodiment obtained under the premise of creative work is made, shall fall within the protection scope of the present invention.
As shown in Figure 1, the bleaching system that the efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe of the present invention uses,
Including brown stock washers 1, in dense standpipe 2, acidification steam heater 20, acidification mixer 4, N-shaped acidifier 5, bleaching steam add
Hot device 21, bleaching mixer 7, high-temperature bleaching tower 8, high-temperature bleaching section wash engine 9；Brown stock washers 1 are through grout outlet 1 in
Dense standpipe 2 connects, in the dense warp of standpipe 2 underflow pipe 11 be sequentially connected middle underflow pump 3, acidification steam heater 20, acidification mixing
Device 4, N-shaped acidifier 5 in acidification steam heater 20 and are acidified between mixer 4 in the outlet end access for having dilute sulfuric acid pipe 13
The input end of underflow pipe 11, dilute sulfuric acid pipe 13 connects dilute acid bath 23, dilute acid bath 23 and concentrated sulfuric acid pipe 25 and saltcake through thin acid pump 24
Solution conduit 26 is connected, and mixes the concentrated sulfuric acid of introducing and saltcake solution by concentrated sulfuric acid pipe 25 and saltcake solution conduit 26, makes dense
Sulfuric acid is diluted to the dilute sulfuric acid that mass concentration is 10%；N-shaped acidifier 5 is sequentially connected bleaching steam heater through grout outlet 2 14
21, mixer 7, high-temperature bleaching tower 8 are bleached, bleaching between steam heater 21 and bleaching mixer 7 has chlorine dioxide outlet tube
Grout outlet 14 is accessed in 18 outlet end, and the input end of chlorine dioxide outlet tube 18 connects chlorine dioxide preheater 6；High-temperature bleaching tower
8 connect high-temperature bleaching section wash engine 9 through grout outlet 3 19.
Acidification steam heater 20 of the present invention and bleaching steam heater 21 respectively with steam pipe 1 and steam pipe
2 22 are connected, and are used to heat slurry by the steam that steam pipe 1 and steam pipe 2 22 generate this segment process.
In order to reduce the steam consumption of ClO 2 bleaching, the mating chlorine dioxide preheater 6 of apparatus of the present invention, chlorine dioxide
Preheater 6 is heat exchanger, and connection chlorine dioxide inlet tube 15, chlorine dioxide outlet tube 18, filtrate inlet tube 17, filtrate go out
Liquid pipe 16；Filtrate inlet tube 17, filtrate outlet tube 16 are separately connected the shell side rear and front end of chlorine dioxide preheater 6, titanium dioxide
Chlorine inlet tube 15, chlorine dioxide outlet tube 18 are separately connected the tube side rear and front end of chlorine dioxide preheater 6.
While ensuring equipment safety even running, to save apparatus cost, the N-shaped acidifier 5 select cost compared with
The two-phase stainless steel material of low acid corrosion-resistant is made, and high-temperature bleaching tower 8 selects cost higher acidproof and chlorine dioxide corrosion
Carbon steel lining acid-proof ceramics material be made.
It is the embodiment for implementing high temperature ClO 2 bleaching method using apparatus of the present invention below:
Embodiment 1, using Dht-Ep-D1 technique, bleaching does not carry out the bagasse pulp of the de- processing of oxygen, and concrete operation step is such as
Under:
Step 1, the high temperature acidified pretreatment of paper pulp: slurry is laggard to 10% concentration through 1 washing concentrating of brown stock washers before drift
Dense standpipe 2 in entering, is sent to acidification steam heater 20 by middle underflow pump 3 and is heated, and is then entered acidification mixer 4 and is come from diluted acid
The dilute sulfuric acid that the mass concentration of slot 23 is 10% mixes, and controlling the pH value after high-temperature bleaching reaction is 2.2, then enters back into n
Type acidifier 5 carries out acid-base neutralization reaction and acidified degradation HexA.Acidification reaction temperature be 80 DEG C, pre-acidified processing the time be
60min。
Step 2, chlorine dioxide preheats: before chlorine dioxide is mixed with paper pulp, first with bleaching filter in chlorine dioxide preheater 6
Liquid is preheated to 40 DEG C.
Step 3, high temperature ClO 2 bleaching: the paper pulp after acidizing pretreatment, through bleaching 21 supplementary heating of steam heater
Afterwards, it is mixed with the ClO 2 solution after preheating, chlorine dioxide additional amount is 10.7kg/Adt, is carried out into high-temperature bleaching tower 8
While high temperature ClO 2 bleaching reacts, continue acidified degradation HexA, and keeping 8 interior reaction temperature of high-temperature bleaching tower is 85
DEG C, reaction time 60min.
Step 4, washed: high-temperature bleaching tower treated paper pulp after this section of filtrate is diluted to 2.5% concentration, into
Enter high-temperature bleaching section wash engine to be washed with Ep, D1 sections of back segment of filtrate.
Step 5, the slurry after washing is carried out subsequent conventional Ep, D1 to bleach, the pulp brightness after drift is >=85%.
First segment ClO 2 bleaching carries out the bleaching agent dosage of high temperature ClO 2 bleaching, steam using the method for the present invention
Consumption, overall cost of ownership, as follows with conventional high-temperature ClO 2 bleaching, the data of conventional ClO 2 bleaching relatively:
As seen from the above table, first segment ClO 2 bleaching uses the method for the present invention, compared to conventional high-temperature bleaching method, often
ClO 2 bleaching mode is advised, can all reduce by 16.7% total chlorine dioxide consumption, and using total steam of the method for the present invention
Amount ratio conventional high-temperature bleaching method is few, and overall cost of ownership is relatively low, in the case that slurry production capacity is 300Adt, in 1 year
Increased cost of investment can be recycled.
Embodiment 2, using Dht-Ep-D1 technique, bleaching does not carry out the de- Eucalyptus handled of oxygen, and (Eucalyptus is accounted for bagasse mixing slurry
25%), the specific steps are as follows:
Step 1, the high temperature acidified pretreatment of paper pulp: slurry is after brown stock washers 1 washing concentrating to 10.8% concentration before drift
The dense standpipe 2 in, by middle underflow pump 3 send to acidification steam heater 20 heat, then enter acidification mixer 4 with come from it is dilute
The dilute sulfuric acid that the mass concentration of acid tank 23 is 10% mixes, and controlling the pH value after high-temperature bleaching reaction is 2.5, is then entered back into
N-shaped acidifier 5 carries out acid-base neutralization reaction and acidified degradation HexA, and acidification reaction temperature is 82 DEG C, and the pre-acidified processing time is
60min。
Step 2, chlorine dioxide preheats: before chlorine dioxide is mixed with paper pulp, first with bleaching filter in chlorine dioxide preheater 6
Liquid is preheated to 40 DEG C.
Step 3, high temperature ClO 2 bleaching: the paper pulp after acidizing pretreatment, through bleaching 21 supplementary heating of steam heater
Afterwards, it is mixed with the chlorine dioxide after preheating, chlorine dioxide additional amount is 17.5kg/Adt, carries out high temperature into high-temperature bleaching tower 8
While ClO 2 bleaching reacts, continue acidified degradation HexA, and keeping 8 interior reaction temperature of high-temperature bleaching tower is 90 DEG C, instead
It is 60min between seasonable.
Step 4, carry out high-temperature wash: high-temperature bleaching tower treated paper pulp is diluted to through this section of filtrate 2.5% concentration
Afterwards, it is washed into high-temperature bleaching section wash engine with Ep, D1 sections of back segment of filtrate.
Step 5, the slurry after washing carries out subsequent conventional Ep, D1 bleaching, and the pulp brightness after drift is >=85%.
First segment ClO 2 bleaching carries out the bleaching agent dosage of high temperature ClO 2 bleaching, steam using the method for the present invention
Consumption, overall cost of ownership, the data compared with conventional high-temperature ClO 2 bleaching, conventional ClO 2 bleaching are as follows:
As seen from the above table, first segment ClO 2 bleaching uses the method for the present invention, compared to conventional high-temperature bleaching method, often
ClO 2 bleaching mode is advised, can all reduce by 21.9% total chlorine dioxide consumption, and using total steam of the method for the present invention
Amount ratio conventional high-temperature bleaching method is few, and overall cost of ownership is relatively low, in the case that slurry production capacity is 300Adt, in half a year
Increased cost of investment can be recycled.
Embodiment 3, using Dht-Ep-D1 technique, bleaching does not carry out the de- Eucalyptus handled of oxygen, and (Eucalyptus is accounted for bagasse mixing slurry
50%), the specific steps are as follows:
Step 1, the high temperature acidified pretreatment of paper pulp: slurry is after brown stock washers 1 washing concentrating to 11.9% concentration before drift
The dense standpipe 2 in, by middle underflow pump 3 send to acidification steam heater 20 heat, then enter acidification mixer 4 with come from it is dilute
The dilute sulfuric acid that the mass concentration of acid tank 23 is 10% mixes, and controlling the pH value after high-temperature bleaching reaction is 2.6, is then entered back into
N-shaped acidifier 5 carries out acid-base neutralization reaction and acidified degradation HexA, and acidification reaction temperature is 85 DEG C, and the pre-acidified processing time is
60min。
Step 2, chlorine dioxide preheats: before chlorine dioxide is mixed with paper pulp, first with bleaching filter in chlorine dioxide preheater 6
Liquid is preheated to 40 DEG C.
Step 3, high temperature ClO 2 bleaching: the paper pulp after acidizing pretreatment, through bleaching 21 supplementary heating of steam heater
Afterwards, it is mixed with the chlorine dioxide after preheating, chlorine dioxide additional amount is 22.8kg/Adt, carries out high temperature into high-temperature bleaching tower 8
While ClO 2 bleaching reacts, continue acidified degradation HexA, and keeping 8 interior reaction temperature of high-temperature bleaching tower is 95 DEG C, instead
It is 60min between seasonable.
Step 4, carry out high-temperature wash: high-temperature bleaching tower treated paper pulp is diluted to through this section of filtrate 2.5% concentration
Afterwards, it is washed into high-temperature bleaching section wash engine with Ep, D1 sections of back segment of filtrate.
Step 5, the slurry after washing carries out subsequent conventional Ep, D1 bleaching, and the pulp brightness after drift is >=85%.
First segment ClO 2 bleaching uses the bleaching agent dosage, steam consumption, overall cost of ownership of the method for the present invention, with biography
The data that system high temperature ClO 2 bleaching, conventional ClO 2 bleaching compare are as follows:
As seen from the above table, first segment ClO 2 bleaching uses the method for the present invention, compared to conventional high-temperature bleaching method, often
ClO 2 bleaching mode is advised, can all reduce by 25.9% total chlorine dioxide consumption, and using total steam of the method for the present invention
Amount ratio conventional high-temperature bleaching method is few, and overall cost of ownership is relatively low, in the case that slurry production capacity is 300Adt, a season
Increased cost of investment can be recycled in degree.
Above-described embodiment while reaching conventional high-temperature ClO 2 bleaching effect (relative to conventional chlorine dioxide float,
The chlorine dioxide consumption of 15-30% can be reduced), ton slurry consumption quantity of steam can reduce 12%, first segment ClO 2 bleaching section
Overall cost of ownership can reduce 10%, and simultaneity factor operational safety is stronger.
Although above having used specific embodiment, the present invention is described in detail, on basis of the invention
On, it can be made some modifications or improvements, this will be apparent to those skilled in the art.Therefore, without departing from
These modifications or improvements on the basis of spirit of that invention, fall within the scope of the claimed invention.
Claims (8)
1. a kind of efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe, which is characterized in that including following operating procedure:
1) paper pulp is through high temperature acidified pretreatment: first will slurry is washed before drift is concentrated into 10-12%, and after be steam heated to reaction
It is required that temperature, N-shaped acidifier is entered after mixing with dilute sulfuric acid and carries out acid-base neutralization reaction and acidified degradation HexA, N-shaped acidification
Souring temperature in device is 80-85 DEG C, and the acidification time is 60min；
2) the pre-heat treatment is carried out to ClO 2 solution: before ClO 2 solution is mixed with paper pulp, is first preheated to bleaching filtrate
40℃；
3) it carries out the processing of high temperature ClO 2 bleaching: by the paper pulp after acidizing pretreatment, being mended through steam and be heated to what reaction required
After temperature, reacted with high-temperature bleaching tower progress high temperature ClO 2 bleaching is entered after the ClO 2 solution mixing after preheating, together
Shi Chixu acidified degradation HexA, the reaction temperature in high-temperature bleaching tower are 85-95 DEG C, reaction time 60min；
4) it carries out high-temperature wash: high-temperature bleaching tower treated paper pulp being sent into after the washing of high-temperature bleaching section wash engine and is floated
Blank sheet of paper slurry.
2. the efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe according to claim 1, which is characterized in that step
1) in, the mass concentration of the dilute sulfuric acid is 10%, by obtaining the concentrated sulfuric acid and acid saltcake solution mixing system；Dilute sulfuric acid adds
Enter amount to determine according to come the wash degree of the amount of slurry and slurry, it is desirable that reaching the pH value starched after control high temperature ClO 2 bleaching reaction is 2-
3。
3. the efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe according to claim 1, which is characterized in that step
4) in, the high-temperature bleaching section wash engine is 2-3% into concentration is starched.
4. according to claim 1 to the bleaching dress that the 3 efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe use
Set, which is characterized in that the device include brown stock washers (1), in dense standpipe (2), acidification steam heater (20), acidification mixing
Device (4), N-shaped acidifier (5), bleaching steam heater (21), bleaching mixer (7), high-temperature bleaching tower (8), high-temperature bleaching section
Wash engine (9)；Through grout outlet one (10), the dense standpipe (2) in connect the brown stock washers (1), in dense standpipe (2) Jing Zhongnong
Slurry pipe (11) is sequentially connected middle underflow pump (3), acidification steam heater (20), acidification mixer (4), N-shaped acidifier (5),
There is underflow pipe (11) in the outlet end access of dilute sulfuric acid pipe (13) between acidification steam heater (20) and acidification mixer (4)；n
Type acidifier (5) is sequentially connected bleaching steam heater (21), bleaching mixer (7), high-temperature bleaching tower through grout outlet two (14)
(8), steam heater (21) are bleached and bleach the outlet end access pulp for having chlorine dioxide outlet tube (18) between mixer (7)
It manages (14), the input end of chlorine dioxide outlet tube (18) connects chlorine dioxide preheater (6)；High-temperature bleaching tower (8) is through grout outlet
Three (19) connect high-temperature bleaching section wash engine (9).
5. the bleaching system that the efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe uses according to claim 4,
It is characterized in that, the input end of the dilute sulfuric acid pipe (13) through thin acid pump (24) connect dilute acid bath (23), dilute acid bath (23) with it is dense
Sulfuric acid pipe (25) is connected with saltcake solution conduit (26).
6. the bleaching system that the efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe uses according to claim 4,
It is characterized in that, the chlorine dioxide preheater (6) is heat exchanger, before and after tube side respectively with chlorine dioxide inlet tube (15)
It is connected with chlorine dioxide outlet tube (18), is connected respectively with filtrate outlet tube (16) and filtrate inlet tube (17) before and after shell side
It connects.
7. the bleaching system that the efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe uses according to claim 4,
It is characterized in that, the N-shaped acidifier (5) selects the two-phase stainless steel material of acid corrosion-resistant to be made, high-temperature bleaching tower (8) is selected
Acidproof and chlorine dioxide corrosion carbon steel lining acid-proof ceramics material is made.
8. the bleaching system that the efficient high temperature chlorine dioxide pulp method for bleaching of energy-saving safe uses according to claim 4,
It is characterized in that, the acidification steam heater (20) and bleaching steam heater (21) are separately connected steam pipe.
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| CN1168706A (en) * | 1994-10-13 | 1997-12-24 | 阿尔斯特罗姆机器有限公司 | Method for removal of hexenuronic acid groups in cellulose pulp by heat treatment |
| US6736934B1 (en) * | 1995-02-17 | 2004-05-18 | Andritz Oy | Method of pretreating pulp in an acid tower prior to bleaching with peroxide |
| SE9602203D0 (en) * | 1996-06-03 | 1996-06-03 | Ahlstroem Oy | Method of and apparatus for treating pulp in connection with digestion |
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Application publication date: 20190920 |