CN204570365U - A kind of bagasse pulp ClO 2 bleaching system - Google Patents
A kind of bagasse pulp ClO 2 bleaching system Download PDFInfo
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- CN204570365U CN204570365U CN201420813044.1U CN201420813044U CN204570365U CN 204570365 U CN204570365 U CN 204570365U CN 201420813044 U CN201420813044 U CN 201420813044U CN 204570365 U CN204570365 U CN 204570365U
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Abstract
The utility model discloses a kind of bagasse pulp ClO 2 bleaching system, comprise the pipeline circulated for the bleaching tower of bleaching bagasse pulp, the wash mill performing bagasse pulp matting and guiding bagasse pulp, bleaching tower comprises tri-stage bleaching structure---the alkalization of D0 section bleaching tower, Ep section tower, D1 section bleaching tower, the downstream line of every section of bleaching tower connects wash mill, the upstream line of Ep section alkalization tower is disposed with alkali liquor inlet and hydrogen peroxide entrance, the upstream line of D1 section bleaching tower is also provided with bleaching agent inlet, and bleaching system pipe end is screenings outlet.The utility model alleviates the problem of the serious and discharge extremely toxic substance of legacy equipment water consumption, and after using rear drift, pulp brightness improves, viscosity improves, and brightness reversion reduces, the quality of bagasse pulp is obviously improved, water-saving result is obvious, reduces middle-stage wastewater COD discharge capacity, meets energy-saving and emission-reduction and cleanly production requirement.
Description
Technical field
The utility model relates to a kind of element chlorine free bleaching equipment in bagasse pulp production process.
Background technology
Bagasse is the distinctive fibrous raw material in Guangxi, utilizes bagasse to carry out pulping and paper-making, has very ripe experience in Guangxi.At present, the slurrying of China's non-wood fiber still generally uses traditional chlorine bleach technique.Traditional chlorine bleach, particularly CEH tri-stage bleaching waste water, except containing higher COD, BOD, also containing a large amount of organic chlorides (AOX), the general toxicity of these organic chlorides is stronger, part organic chloride belongs to carcinogenic, teratogenesis and mutagenic " three cause " material (be as bioxin), and be difficult to biochemical degradation; The Non-toxic process of these organic chlorides is more difficult, is discharged in rivers water body and can causes more serious environmental pollution; Secondly because traditional chlorine bleach technique contains chlorine, waste water not easily reuses, and causes water consumption large; More troublesome, in chlorination C section, because chlorine does not have selective to the lignin in slurry, in reduction slurry, also use cellulose to be reduced while lignin, the intensity of slurry is declined.Therefore, traditional chlorine bleach process not only makes Pulping Middle-stage Wastewater Pollution serious, also makes the development of non-wood fiber slurrying receive serious restriction simultaneously.
Domestic patent data discloses many about traditional chlorine bleach technique (or system) patented technology:
The free pulping method of such as [title] a kind of low polymerization degree bamboo pulp; [application number] CN201410024665.6, [applicant] Sichuan University of Science & Engineering; [summary] the invention belongs to the cleaning pulping field of bamboo pulp, particularly relate to a kind of free pulping method of low polymerization degree bamboo pulp, utilize true qualities sulfate bamboo pulp (hereinafter referred to as KP bamboo pulp) for raw material production bamboo pulp for cellulose viscose, also can be used for production of cellulose derivative product.Comprise the following steps: raw material preparation, alkaline cooking, concentrated, oxygen bleaching, bleaching and cellulase treatment-chlorine dioxide are once bleached-EOP bleaching-chlorine dioxide secondary and bleached and ferment treatment step.This invented technology flow process is simple, production efficiency is high, production capacity is large, pulping yield rate is high, the bamboo pulp produced can meet the requirement that viscose is produced completely, also can be used for production of cellulose derivative product, but containing higher COD, BOD and organic chloride (AOX) in bleaching effluent, environment structure is endangered.
Such as [title] CEH bleaching waste liquor wet method improves the method for bagasse alkaline cooking effect, [patent No.] CN200910094429.0, [patentee] Kunming University of Science and Technology, [summary] the invention discloses a kind of bagasse wet method stacked arrangement of bagasse alkaline cooking pre-treatment, using Bagasse Pulp CEH substituting as clear water, the wet method being back to use bagasse respectively stores up process, then carry out the alkaline cooking of bagasse, its processing step is: get C, E, the washes of H tri-stage bleaching sprays the bagasse stored up in stock ground and piles, leakage water is had to flow out to bottom, bagasse after spray 10 ~ 20 is through discharging, feeding, washing, boiling vessel is conveyed into after dehydration, at NaOH consumption 14 ~ 16%, anthraquinone consumption 0.01 ~ 0.3%, weight liquor ratio 1: 3 ~ 6, boiling temperature 155 ~ 160 DEG C, heat up 70 ~ 110min, boiling is carried out under the condition of insulation 60 ~ 90min.Bagasse pulp yield 2 ~ 5 percentage points can be improved, reduce organic chloride 22 ~ 31%, ton slurry water consumption decline 8 ~ 15m3.This invention is bleached bleaching process to CEH and is improved, but still containing certain COD, BOD and organic chloride (AOX) in bleaching effluent.
The such as preparation method of [title] a kind of bleaching straw pulp; [application number] CN201310177495.0, [applicant] Kunming University of Science and Technology, Longjiang, Jiamusi Fu Jiangzhi Co., Ltd; [summary] the invention discloses a kind of preparation method of bleaching straw pulp, the method comprises following operation: 1) grass as raw material and cooking liquor to be added in digesting apparatus with the weight ratio of 1:3-1:6 and to mix, then digesting apparatus is airtight, wherein, containing alkali in described cooking liquor; 2) in described airtight digesting apparatus, passing into oxygen makes oxygen pressure in digesting apparatus remain 0.3-1.0MPa, by described grass as raw material described cooking liquor boiling 30-240 minute at 90-130 DEG C; (3) slurry obtained after completing digestion process is carried out washing and screening, obtain screened stock; 4) the screened stock chlorine dioxide in described operation (3) is bleached.This invention is same as the further improvement to CEH bleaching process, two sections of driftages that the CEH bleaching process usually adopted than common alkaline straw-pulp is few, but still on Wastewater Pollutant content, does not have remarkable breakthrough.
Therefore the production water consumption that traditional traditional chlorine bleach system exists is serious, and the problem, particularly CEH tri-stage bleaching waste water of discharge extremely toxic substance, except containing except higher COD, BOD, the more important thing is containing a large amount of organic chlorides (AOX).Therefore need to improve further traditional bagasse pulp bleaching system.
Summary of the invention
The purpose of this utility model is that to solve the production water consumption that traditional bagasse pulp chlorine bleach system exists serious, and the problem of discharge extremely toxic substance, provides the bagasse pulp ClO 2 bleaching system that a set of water consumption is low, toxic emission is few.
The utility model comprises the pipeline circulated for the bleaching tower of bleaching bagasse pulp, the wash mill performing bagasse pulp matting and guiding bagasse pulp.Described bleaching tower comprises tri-stage bleaching structure---and the alkalization of D0 section bleaching tower, Ep section tower, D1 section bleaching tower, the downstream line of every section of bleaching tower connects wash mill.D0 section bleaching tower upstream line connects screenings entrance, and this place's pipeline is also provided with bleaching agent inlet.The upstream line of Ep section alkalization tower is disposed with alkali liquor inlet and hydrogen peroxide entrance, and the upstream line of D1 section bleaching tower is also provided with bleaching agent inlet, and bleaching system pipe end is screenings outlet.
Described wash mill is divided into two sections of cleaning structures---slag slurry cleaning machine and slag slurry screening machine, and be that slag starches cleaning machine front by the sequence in operation, slag slurry screening machine is rear.The bagasse pulp injection end of described D0 section bleaching tower, Ep section alkalization tower, D1 section bleaching tower is also provided with blender, has the effect of fully mixing bagasse pulp and medicament.Described D0 section bleaching tower is dense reaction tower in up-flow, and Ep section alkalization tower is for rise-falling streaming alkalization tower, and D1 section bleaching tower is up-flow bleaching tower.
Illustrate as further improvement of the utility model, described system unit is provided with remote interface units, and the Programmable Logic Controller outside remote interface units and system, industrial control computer form network monitoring system by respective communication process plate bus.
Bagasse pulp ClO 2 bleaching system of the present utility model is suitable for new bagasse pulp ClO 2 bleaching technique, replace original chlorine bleach system, namely replace chlorine and calcium hypochlorite in former bagasse pulp bleaching production procedure with chlorine dioxide, add hydrogen peroxide in alkali treatment section, the technique effect brought thus:
(1) compare traditional traditional chlorine bleach system, after drift, pulp brightness raising, viscosity improve, and brightness reversion reduces, and the quality of bagasse pulp is obviously improved.
(2) the paper pulp more environmental protection of bagasse pulp ClO 2 bleaching system production of the present utility model, as multiple paper for daily use raw materials such as toilet paper, cup paper, paper dishware.
(3) bagasse pulp ClO 2 bleaching system of the present utility model, dense during technological reaction condition is, and water-saving result is obvious, meets energy-saving and emission-reduction and cleanly production requirement.
(4) bagasse pulp ClO 2 bleaching system of the present utility model, decrease chlorine bleach and produce organic chloride (AOX), make bleaching have more selective, washings can recycle simultaneously, reduce middle-stage wastewater COD discharge capacity.
Accompanying drawing explanation
Fig. 1 is system connection diagram of the present utility model.
In figure: 1-screenings entrance; 2-D0 section bleaching tower; 3-wash mill; 4-Ep section alkalization tower; 5-hydrogen peroxide entrance; 6-D1 section bleaching tower; 7-alkali liquor inlet; 8-screenings exports; 9-bleaching agent inlet.
Detailed description of the invention
As shown in Figure 1, the utility model comprises the pipeline circulated for the bleaching tower of bleaching bagasse pulp, the wash mill 3 performing bagasse pulp matting and guiding bagasse pulp, bleaching tower comprises tri-stage bleaching structure---the alkalization of D0 section bleaching tower 2, Ep section tower 4, D1 section bleaching tower 6, the downstream line of every section of bleaching tower connects wash mill, D0 section bleaching tower upstream line connects screenings entrance 1, and this place's pipeline is also provided with bleaching agent inlet 9.The upstream line that the upstream line of Ep section alkalization tower is disposed with alkali liquor inlet 7 and hydrogen peroxide entrance 5, D1 section bleaching tower is also provided with bleaching agent inlet, and bleaching system pipe end is screenings outlet 8.
Wash mill 3 is divided into two sections of cleaning structures---slag slurry cleaning machine and slag slurry screening machine, and be that slag starches cleaning machine front by the sequence in operation, slag slurry screening machine is rear.The bagasse pulp injection end of D0 section bleaching tower 2, Ep section alkalization tower 4, D1 section bleaching tower 6 is also provided with blender, has the effect of fully mixing bagasse pulp and medicament.D0 section bleaching tower 2 is dense reaction tower in up-flow, and Ep section alkalization tower 4 is for rise-falling streaming alkalization tower, and D1 section bleaching tower 6 is up-flow bleaching tower.
Using method corresponding to bagasse pulp ClO 2 bleaching system of the present utility model is as follows:
(1) D0 section bleaching, add chlorine dioxide oven dry stock to not floating in bagasse pulp, the chlorine dioxide oven dry stock addition of bagasse pulp per ton is 33 ~ 40 kg, and wherein chlorine dioxide oven dry stock is containing effective chlorine with being 78 ~ 80%, adds middle pressure steam simultaneously; Medicament and bagasse pulp enter D0 section bleaching tower and react after blender mixes, and add antichlor and remove residual chlorine in slurry and wash after having reacted.
(2) Ep section alkalization, NaOH and hydrogen peroxide oven dry stock is added successively to the D0 section bagasse pulp after washing, the NaOH oven dry stock addition of bagasse pulp per ton is 11 ~ 14 kg, hydrogen peroxide oven dry stock addition is 20 ~ 30 kg, wherein NaOH oven dry stock concentration is 100%, and hydrogen peroxide oven dry stock concentration is 27.5%; Add middle pressure steam, medicament and bagasse pulp enter the Ep section tower that alkalizes and react after blender mixes, and have reacted rear washing simultaneously.
(3) D1 section bleaching, in after washing, dense bagasse pulp adds chlorine dioxide oven dry stock, and the chlorine dioxide oven dry stock addition of bagasse pulp per ton is 8 ~ 11 kg/t oven dry stocks, wherein chlorine dioxide oven dry stock containing effective chlorine with being 20 ~ 22%, add middle pressure steam simultaneously, add middle pressure steam simultaneously; Medicament and bagasse pulp enter D1 section bleaching tower and react after blender mixes, and add antichlor and remove residual chlorine in slurry and wash after having reacted;
Described D0 section bleaching process, reaction temperature controls at 45 ~ 55 DEG C, reaction time 40min, and going out D0 tower pulp brightness is 50 ~ 55%ISO;
Described Ep section alkalinization, reaction temperature controls at 65 ~ 75 DEG C, and bagasse pulp first reacts 25min with NaOH, then reacts 95min with hydrogen peroxide, and going out Ep tower pulp brightness is 70 ~ 75%ISO;
Described D1 section bleaching process, reaction temperature controls at 60 ~ 65 DEG C, and the reaction time is about 180min, and going out D1 tower pulp brightness is more than 82%ISO.
Embodiment 1: brown stock enters bagasse pulp ClO 2 bleaching system of the present utility model after washing concentrating, in dense condition issue biochemical reaction, D0 section chlorine dioxide addition is 34.7 kg/t oven dry stocks (effective chlorine meters), Ep section alkali lye addition is 11.9 kg/t oven dry stocks (with 100% densimeters), it is 23 kg/t oven dry stocks (with 27.5% densimeters) that hydrogen peroxide enters amount, D1 section chlorine dioxide addition is 9.5 kg/t oven dry stocks (effective chlorine meters), adds every section of steam and heats, reacts, washs.After drift, pulp brightness is 83.6%, and qualification rate is 99.5%.
Embodiment 2: brown stock enters bagasse pulp ClO 2 bleaching system of the present utility model after washing concentrating, in dense condition issue biochemical reaction, D0 section chlorine dioxide addition is 36.7 kg/t oven dry stocks (effective chlorine meters), Ep section alkali lye addition is 12.6 kg/t oven dry stocks (with 100% densimeters), it is 27kg/t oven dry stock (with 27.5% densimeter) that hydrogen peroxide enters amount, D1 section chlorine dioxide addition is 9.9kg/t oven dry stock (effective chlorine meter), adds every section of steam and heats, reacts, washs.After drift, pulp brightness is 84.8%, and qualification rate is 99.6%.
Embodiment 3: brown stock enters bagasse pulp ClO 2 bleaching system of the present utility model after washing concentrating, in dense condition issue biochemical reaction, D0 section chlorine dioxide addition is 38.9 kg/t oven dry stocks (effective chlorine meters), Ep section alkali lye addition is 12.8 kg/t oven dry stocks (with 100% densimeters), it is 30kg/t oven dry stock (with 27.5% densimeter) that hydrogen peroxide enters amount, D1 section chlorine dioxide addition is 10.5kg/t oven dry stock (effective chlorine meter), adds every section of steam and heats, reacts, washs.After drift, pulp brightness is 85.8%, and qualification rate is 99.8%.
Claims (5)
1. a bagasse pulp ClO 2 bleaching system, comprise the pipeline circulated for the bleaching tower of bleaching bagasse pulp, the wash mill (3) performing bagasse pulp matting and guiding bagasse pulp, it is characterized in that: described bleaching tower comprises tri-stage bleaching structure---D0 section bleaching tower (2), Ep section alkalization tower (4), D1 section bleaching tower (6), the downstream line of every section of bleaching tower connects wash mill, D0 section bleaching tower upstream line connects screenings entrance (1), and this place's pipeline is also provided with bleaching agent inlet (9); The upstream line of Ep section alkalization tower is disposed with alkali liquor inlet (7) and hydrogen peroxide entrance (5), and the upstream line of D1 section bleaching tower is also provided with bleaching agent inlet, and bleaching system pipe end is screenings outlet (8).
2. bagasse pulp ClO 2 bleaching system according to claim 1, it is characterized in that: described wash mill (3) is divided into two sections of cleaning structures---slag slurry cleaning machine and slag slurry screening machine, and by the sequence in operation be slag slurry cleaning machine front, slag slurry screening machine rear.
3. bagasse pulp ClO 2 bleaching system according to claim 1, it is characterized in that: the bagasse pulp injection end of described D0 section bleaching tower (2), Ep section alkalization tower (4), D1 section bleaching tower (6) is also provided with blender, there is the effect of fully mixing bagasse pulp and medicament.
4. according to the arbitrary described bagasse pulp ClO 2 bleaching system of claim 1-3, it is characterized in that: described D0 section bleaching tower (2) is reaction tower dense in up-flow, Ep section alkalization tower (4) is for rise-falling streaming alkalization tower, and D1 section bleaching tower (6) is up-flow bleaching tower.
5. bagasse pulp ClO 2 bleaching system according to claim 4, it is characterized in that: described bleaching system is provided with remote interface units, the Programmable Logic Controller outside remote interface units and system, industrial control computer form network monitoring system by respective communication process plate bus.
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| CN201420813044.1U CN204570365U (en) | 2014-12-22 | 2014-12-22 | A kind of bagasse pulp ClO 2 bleaching system |
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| CN201420813044.1U CN204570365U (en) | 2014-12-22 | 2014-12-22 | A kind of bagasse pulp ClO 2 bleaching system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104611971A (en) * | 2014-12-22 | 2015-05-13 | 南宁糖业股份有限公司 | A system and a method for bleaching bagasse pulp with chlorine dioxide |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104611971A (en) * | 2014-12-22 | 2015-05-13 | 南宁糖业股份有限公司 | A system and a method for bleaching bagasse pulp with chlorine dioxide |
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