CN107265454A - A kind of cotton pulp Bo liquid recycling system and method - Google Patents

A kind of cotton pulp Bo liquid recycling system and method Download PDF

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Publication number
CN107265454A
CN107265454A CN201710446576.4A CN201710446576A CN107265454A CN 107265454 A CN107265454 A CN 107265454A CN 201710446576 A CN201710446576 A CN 201710446576A CN 107265454 A CN107265454 A CN 107265454A
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liquid
unit
separative element
solid
isolation
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杨刚
王云山
孙勇
安学斌
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Institute of Process Engineering of CAS
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
    • B01D50/40—Combinations of devices covered by groups B01D45/00 and B01D47/00
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
    • C01D1/00—Oxides or hydroxides of sodium, potassium or alkali metals in general
    • C01D1/04—Hydroxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F11/00—Compounds of calcium, strontium, or barium
    • C01F11/18—Carbonates
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/04—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste liquors, e.g. sulfite liquors

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  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Inorganic Chemistry (AREA)
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  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)

Abstract

The present invention relates to a kind of cotton pulp Bo liquid recycling system and method, the system includes：Drying unit, isolation calcining unit, separative element, causticization unit and activation unit；The isolation calcining unit includes heater；The separative element is provided with water inlet, taphole and solid material outlet；The entrance of the solid material outlet connection separative element of the isolation calcining unit；The entrance of the solid material outlet connection activation unit of the separative element；The taphole of the separative element connects the entrance of the causticization unit.The present invention using completely cut off air calcination instead of traditional wood pulp Bo oxy combustion in liquor treating process, product includes activated carbon, it is up to state standards (goods of inferior quality), the yield of activated carbon is more than 60%, realize suitable cotton pulp Bo liquid recycling system and method there is prominent economic benefit and environment protection significance.

Description

A kind of cotton pulp Bo liquid recycling system and method
Technical field
The present invention relates to paper industry wastewater treating technology field, more particularly to a kind of cotton pulp Bo liquid recycling system and Method.
Background technology
China is Chan Mian big countries, there is abundant cotton linter resource, and timber resources is shorter, therefore unlike west It is national many using wood pulp production viscose rayon like that, but cotton pulp pool is made as the main production of viscose rayon using cotton linter Raw material.Cotton pulp production process also as wood pulp production process, will produce substantial amounts of pollutant effluents --- black liquor, but cotton pulp black liquor It is not quite alike with pulp black liquor composition.Because the purity of cotton linter is more much higher than timber, predominantly cellulose and hemicellulose Basic degradation products, such as resin, fat soap compound, wax emulsion, its solid content, particularly content of organics ratio It is relatively low, and inorganic content is higher, therefore, some effective black liquor treatment technologies used during wood pulp production but without Method is effectively applied in cotton pulp production.At present, 10 tons or so of black digestion liquid, solid content will be discharged by often producing 1 ton of cotton pulp pool 5% or so.Xinjiang is the big province of production cotton, and according to existing 480,000 tons/year of accounting of Xinjiang production capacity, annual discharge Treatment of cotton pulp black is 4800000 tons, solid content is 240,000 tons, wherein Na2O content is 36.2%, then annual 11.2 ten thousand tons of caustic soda do not enter into product, into Discharged for discarded object.The requirement more and more higher protected with Environmental, cotton pulp pool manufacturing enterprise continues to increase to moor to cotton pulp The research and development of black liquor treatment technology, put into the fund of tens million of members with black liquor treatment.
At present, paper industry conventional art is alkali collection, and it applies the general principle of Lv Bulan alkaline methods, by sodium in black liquor Organic compound burn till sodium carbonate, then by lime causticization, sodium hydroxide solution is made.Technical process includes：From washed In the black liquor that journey is extracted, through pervaporation moisture, improve black liquid consistency to burn.Black liquor vaporizing uses quintuple effect evaporator system System.It will be burnt in the black liquor feeding recovery furnace of inspissation.Alkali recovery furnace is the reactor for completing alkali collection chemical reaction, is to produce again The power boiler of steam, 1000 DEG C~1200 DEG C of burner hearth Nei Wenduda, makes black liquor vaporizing, drying, falls as grey black on furnace bottom, Bed course is paved into, ignition flows into dissolving tank into sodium carbonate fusion thing from furnace bottom exit.Burn the flue gas produced, in stove Rise, heat is absorbed by boiler part, produce steam.Last flue gas further utilizes waste heat through evaporator, or again through electrostatic The devices such as deduster are reclaimed and discharged after alkali dirt.Lime slurry is added in green liquor, sodium carbonate is transformed into sodium hydroxide, to be made Cooking liquor --- white liquor.Subsequently into causticization, continuous causticizing is that, by green liquor clarification or filter type, continuous remove wherein is hanged Floating solid impurity, obtains clear green liquor, is re-fed into causticizer, fully reacts, is contained with the lime slurry by digestion The causticization emulsion of sodium hydroxide and sodium carbonate particle, continuously separates white clay, obtains pure liquid, is used for boiling.Due to raw material Difference, black digestion liquid and the Treatment of cotton pulp black of paper industry are very different, and Treatment of cotton pulp black concentration is low, boiling high energy consumption, The combustibility of solid content is poorer than black liquid simultaneously, and the structure of existing alkali recovery furnace can not realize that the alkali of Treatment of cotton pulp black is returned Receive, face very big engineering difficulty.There are indivedual enterprises to start to build Treatment of cotton pulp black soda recovery unit, but it is first without success so far Example, industry is held the suspicious attitude mostly.
CN101585617A discloses a kind of process for treating chemical fiber cotton pulp black liquor, is by chemical fiber cotton pulp black liquor and pulp black liquor Mixed in proportion after being filtered by black liquor filter, carry out oxy combustion after evaporation in alkali recovery furnace, the melting produced of burning Thing dissolving, causticization generation sodium hydroxide.Although this technique eliminate heavy oil combustion supporting, but its basic line still can not depart from wood pulp The traditional handicraft of black liquor, faces very big engineering difficulty, at present the country pulp black liquor output far fewer than cotton pulp black liquor, so this Technique is upper very limited in application.
In view of the foregoing, most enterprises are expected Treatment of cotton pulp black alkali collection to have more the technology of advantage.
The content of the invention
In view of problems of the prior art, an object of the present invention be to provide a kind of cotton pulp Bo liquid recycling System, the system includes：Drying unit, isolation calcining unit, separative element, causticization unit and activation unit.
The isolation calcining unit includes heater；The separative element is provided with water inlet, taphole and expects admittedly Mouthful.
The entrance of the solid material outlet connection separative element of the isolation calcining unit；The solid of the separative element expects The entrance of the mouth connection activation unit；The taphole of the separative element connects the entrance of the causticization unit.
Using system of the present invention carry out cotton pulp Bo liquid recycling when, it is concentrated after cotton pulp Bo liquid dry it is single Solidfied material is formed after being dried in member, heater is opened, high-temperature flue gas is produced, pre- thermal isolation calcining furnace, solidfied material enters isolation It is pyrolyzed in calcining unit by heater indirectly heat, the solid material outlet output of the solid after pyrolysis from isolation calcining unit enters Separative element, adds water from the water inlet of separative element, is washed, separation of solid and liquid, and the solution containing sodium carbonate is from separative element Taphole export and enter causticization unit and carry out causticization, obtain qualified soda bath and desulfurization calcium carbonate；Separate The solid phase arrived, which exports from the solid material outlet of separative element and enters activation unit separative element, carries out activated carbon modified, acquisition activity Charcoal product.
In the present invention heater to isolation calcining unit in concentration cotton pulp Bo liquid be indirectly heat, isolation air Calcining cause concentration cotton pulp Bo liquid decompose rather than aoxidize, oxidation is happens is that in alkali recovery furnace of the prior art, Fuel, air with and concentration cotton pulp Bo liquid directly contact, the corrosive gas such as generation oxysulfide, nitrogen oxides, under high temperature To the seriously corroded of equipment, the present invention utilizes indirectly heat, accurate temperature controlling, the process such as low temperature pyrogenation, effectively prevents that cotton pulp pool is solid The problems such as oxidizing process of shape thing, melting alkali liquid corrosion.
Drying unit of the present invention preferably includes spray dryer.
Preferably, dust removing units are provided between the drying unit and isolation calcining unit.
Preferably, the dust removing units include cyclone separator and sack cleaner；Wherein, the spray dryer is consolidated The solid material entrance of the material outlet connection cyclone separator, the powder outlet connection sack cleaner of the cyclone separator Powder entrance, the sack cleaner powder outlet connection it is described isolation calcining unit solid material entrance.Dried gas Body qualified discharge after follow-up cyclone separator and sack cleaner are by the Powder Recovery in gas.
In real work, using Geldart-D particle by spray dryer, cyclone separator and sack cleaner Shou Ji Liquid powder delivers to intermediate bin, then granular material is imported into isolation calcining unit.
Heater of the present invention preferably includes combustion furnace.
Preferably, the gas vent of the isolation fuel element connects the fuel inlet of the heater.The gas of pyrolysis Body enters further to burn in combustion furnace, is used as calcining thermal source.
The outlet of heater of the present invention preferably connects the gas access of the spray dryer.Heater is produced Flue gas enter in spray dryer, with the cotton pulp Bo that sprays at the top of the drier liquid contacted, substantially reduce energy consumption.
Separative element of the present invention preferably includes slurrying groove and filter, and the outlet of the slurrying groove connects the filtering The mixed phase entrance of machine.Solid after pyrolysis enters slurrying groove, by the alkali lye dissolving in solid in the solution.
Preferably, the filter includes belt vacuum filter.
Preferably, the entrance of the separative element is the solid material entrance of the slurrying groove, and the solution of the separative element goes out Mouth is the one-level filtrate (liquid of the filter.
Preferably, the delivery port of the separative element connects the water inlet of the separative element.
Belt vacuum filter has the concentration of alkali lye in multi-stage countercurrent washing function, first order filtrate higher, more returns Value is received, the filtrate after multistage washing, filtering can be then back in slurrying groove, equivalent to saving slurry and reduce The loss of alkali.
The second object of the present invention be to provide a kind of cotton pulp Bo liquid method of resource, comprise the following steps：
(1) by cotton pulp Bo liquid concentrated, obtain concentrate, the concentrate is through being dried to obtain solid content；
(2) solid content obtained by step (1) is subjected to isolation air calcination, obtains carbide and gaseous product；
(3) carbide obtained by step (2) is washed, separation of solid and liquid, respectively collection solid phase and liquid phase；The solid phase warp Activation obtains activated carbon, meanwhile, the liquid phase obtains soda bath and calcium carbonate through causticization.It is used as the calcium carbonate of causticization accessory substance For desulfurization calcium carbonate, available for power plant desulfurization.
The method of the invention is preferably realized by the system as described in the first purpose.
Preferably, the solid content of step (1) described concentrate be more than or equal to 45wt%, such as 45wt%, 46wt%, 47wt%, 50wt%, 55wt%, 60wt%, 70wt% or 80wt% etc., preferably 45~60wt%.
Preferably, step (1) described drying is carried out in the drying unit.
Preferably, the temperature of step (1) described drying be 120~160 DEG C, such as 120 DEG C, 125 DEG C, 130 DEG C, 140 DEG C, 150 DEG C or 160 DEG C etc., preferably 130~150 DEG C.
Preferably, in step (1), the mode of the drying includes spray drying.
Preferably, the flue-gas temperature of the spray drying be 250~330 DEG C, such as 250 DEG C, 265 DEG C, 270 DEG C, 280 DEG C, 290 DEG C, 300 DEG C, 310 DEG C, 320 DEG C or 330 DEG C etc., preferably 300~330 DEG C.
Preferably, after step (1) described drying, in addition to：Dedusting.
Preferably, the dedusting includes cyclone dust removal and/or bag-type dust, preferably first carries out cyclone dust removal and carries out whirlwind again Dedusting.
Preferably, the water content in step (1) described solid content be less than or equal to 5wt%, such as 5wt%, 4.5wt%, 4wt%, 3.5wt%, 3wt%, 2.5wt%, 2wt%, 1wt%, 0.5wt% or 0.1wt% etc., preferably 2~5wt%.
Step (2) the isolation air calcination of the present invention is preferably carried out in the isolation calcining unit.
Preferably, step (2) it is described isolation air calcination temperature be 500~650 DEG C, such as 500 DEG C, 520 DEG C, 550 DEG C, 580 DEG C, 600 DEG C, 620 DEG C, 630 DEG C, 640 DEG C or 650 DEG C etc., preferably 600~650 DEG C.
Preferably, the time of step (2) the isolation air calcination is 40~90min, preferably 50~80min.
Preferably, step (2) gaseous product provides heat through burning to the isolation air calcination.
Preferably, carried out in the heater again that burns.
Preferably, step (2) gaseous product produces the high-temperature flue gas that temperature is 800~1000 DEG C through burning.For example The temperature of the high-temperature flue gas be 800 DEG C, 810 DEG C, 820 DEG C, 830 DEG C, 850 DEG C, 880 DEG C, 900 DEG C, 920 DEG C, 950 DEG C, 980 DEG C or 1000 DEG C etc..
Preferably, the high-temperature flue gas is used for step (1) spray drying.
Step (3) washing of the present invention preferably includes countercurrent washing.
Preferably, the cycle-index of the countercurrent washing is more than or equal to 4 times, and such as 4 times, 5 times or 8 are inferior, and preferably 4~6 It is secondary.
Preferably, the detergent of step (3) described washing includes desalted water.
Preferably, the quality of step (3) desalted water is 4~6 times of the carbide quality, preferably 4.5~ 5.5 again.
Preferably, step (3) washing is carried out in the separative element.
Preferably, step (3) described separation of solid and liquid is carried out in the separative element.
Preferably, the mode of step (3) described separation of solid and liquid includes filtering.
Preferably, step (3) activation is specifically included：The solid phase at 700~900 DEG C is contacted 1 with vapor ~2h, obtains activated carbon.
Preferably, in step (3) described liquid phase sodium carbonate concentration be 110~160g/L, such as 110g/L, 120g/L, 130g/L, 140g/L, 150g/L or 160g/L etc., preferably 120~150g/L.
Preferably, the concentration of step (3) described soda bath is 110~130g/L, such as 110g/L, 112g/L, 115g/ L, 118g/L, 120g/L, 125g/L or 130g/L etc., preferably 110~120g/L.
As currently preferred technical scheme, cotton pulp Bo liquid method of resource comprise the following steps：
(1) by cotton pulp Bo liquid concentrated, obtain the concentrate that solid content is more than or equal to 45wt%, the concentrate exists In the drying unit solid content that water content is less than or equal to 5wt% is dried to obtain through 120~160 DEG C；
(2) solid content obtained by step (1) is completely cut off in calcining unit in progress isolation air at 500~650 DEG C described 40~90min is calcined, carbide and gaseous product is obtained；The gaseous product is burnt in the heater to the isolation Air calcination provides heat；
(3) carbide obtained by step (2) is washed in the separative element, separation of solid and liquid, solid phase is collected respectively With 110~160g/L of containing sodium carbonate liquid phase；The solid phase in the activation unit activate obtaining activated carbon, meanwhile, The liquid phase carries out causticization in the causticization unit and obtains soda bath and calcium carbonate.
Compared with prior art, the present invention at least has the advantages that：
(1) present invention using completely cut off air calcination instead of traditional wood pulp Bo oxy combustion in liquor treating process there is provided A kind of suitable cotton pulp Bo liquid recycling system and method, product includes activated carbon, and be up to state standards (goods of inferior quality), living Property charcoal yield be more than 60%, with prominent economic benefit, and in the prior art cotton pulp Bo liquid oxy combustion generation two Carbonoxide, carbon is not efficiently used；
(2) contain imflammable gas in the gaseous product calcined in the present invention, can be generated as fuel after fuel combustion High-temperature gas can be spray-dried, the water of washing can recycle the loss of less alkali lye；Finally realize system The Two-way Cycle of internal heat and material, the treatment of wastes with processes of wastes against one another, energy-saving and emission-reduction.
Brief description of the drawings
Fig. 1 is the exemplary process route chart of the present invention；
Fig. 2 is the system schematic of the embodiment of the present invention 1；
Mark is illustrated as in figure：1- spray dryers；2- cyclone separators；3- sack cleaners；4- air-introduced machines；5- band cloth Bag dedusting intermediate bin；6- Geldart-D particle blower fans；7- combustion furnaces；8- completely cuts off calcining furnace；9- slurrying grooves；10-ization oar pump；11- belts Vacuum filter；12- causticization systems；13- activated carbon activation systems
Embodiment
Further illustrate technical scheme below in conjunction with the accompanying drawings and by embodiment.But following realities The simple example that example is only the present invention is applied, the scope of the present invention, protection model of the invention is not represented or limit Enclose and be defined by claims.
Embodiment 1
A kind of cotton pulp Bo liquid recycling system, as shown in Fig. 2 including spray dryer 1；Cyclone separator 2；Cloth bag is removed Dirt device 3；Air-introduced machine 4；Band bag-type dust intermediate bin 5；Geldart-D particle blower fan 6；Combustion furnace 7；Completely cut off calcining furnace 8；Slurrying groove 9；Change Oar pump 10；Belt vacuum filter 11；Causticization system 12；Activated carbon activation system 13.Also, described spray dryer 1 connects The entrance of cyclone separator 2 is connected to, the outlet of cyclone separator 2 is connected to the entrance of sack cleaner 3, sack cleaner 3 Outlet is connected to the entrance of air-introduced machine 4, the emptying of the gas vent of air-introduced machine 4, spray dryer 1, cyclone separator 2 and bag-type dust The dust outlet of the bottom of device 3 is connected to the entrance with sack cleaner intermediate bin 5, and the gas with sack cleaner intermediate bin 5 goes out Mouth is connected to the entrance of Geldart-D particle blower fan 6, the outlet emptying of Geldart-D particle blower fan 6, the bottom with sack cleaner intermediate bin 5 Powder outlet is connected to the isolation powder entrance of calcining furnace 8, and clean fuel is connected to the entrance of combustion furnace 7, and the outlet of Fuel Furnace 7 is connected to Completely cut off the high-temperature flue gas entry of calcining furnace 8, the isolation gas vent of calcining furnace 8 is connected to the entrance of combustion furnace 7, completely cuts off the powder of calcining furnace 8 Outlet is connected to the entrance of slurrying groove 9, and the outlet of slurrying groove 9 is connected to the entrance of slurrying pump 10, and it is true that the outlet of slurrying pump 10 is connected to belt The empty entrance of filter slurry 11, extraneous desalted water is connected to the wash water entrance of belt vacuum filter 11, belt vacuum filter 11 Least significant end washing water outlet is connected to the entrance of slurrying groove 9, and the filtering of belt vacuum filter 11 lye export is connected to causticization system 12 entrances, the outlet of causticization system 12 obtains qualified soda bath and desulfurization calcium carbonate, and the filtered solid outlet of belt vacuum filter 11 connects The entrance of activated carbon activation system 13 is connected to, the outlet of activated carbon activation system 13 obtains qualified activated carbon product.
Using system as shown in Figure 2 carry out cotton pulp Bo liquid recycling method：
1) 1000kg solid contents 45wt% cotton pulp is moored into liquid to spray into spray dryer 1 using pressure type shower nozzle, its The heat source temperature of middle spray dryer 1 is 300 DEG C, and exhaust temperature is 130~135 DEG C after spraying, is taken in the bottom of spray dryer 1 Sample Fen Xi liquid powder moisture be 4.8wt%.The furnace body temperature of calcining furnace 8 to be completely cut off reaches 500 DEG C, will enter intermediate bin 5 Solid powder is quantitatively adding in isolation calcining furnace 8 and carries out isolation calcining, wherein it is 420kg to add weight of material, material is from addition It is 268.8kg to last solid powder weight after 60min, calcining to discharging, and burning decrement is 36wt%.
2) the 268.8kg solid materials of acquisition are added in the slurrying groove 9 being currently running, wherein belt vacuum filter 11 The amount of desalted water used is 1344kg, i.e., be 5 times of amount of solid in mass ratio, the stirring of running pipeline stock tank 9 is filtered with belt vacuum Machine 11 carries out filtration washing, and the filter cake and filtrate composition of acquisition are as shown in table 1, wherein c0Represent slurrying filtrate Na contents, c1Represent One-level washing lotion Na contents, c2Represent two grades of washing lotion Na contents, c3Represent three-level washing lotion Na contents, c4Level Four washing lotion Na contents are represented, wWaterRepresent cake moisture, wNA represents the Na contents in dry slag, and X% represents Na leaching rates.
Table 1
c0(g/L) c1(g/L) c2(g/L) c3(g/L) c4(g/L) wWater(wt%) wNa(wt%) X%
53.54 0.4652 0.2847 0.1447 0.0847 65 0.7 97.00%
Na in filtrate2CO3Concentration is 123.4g/L.
3) above-mentioned filtrate respectively enters causticization system 12 and activated carbon activation system 13 with filter cake, and wherein filtrate enters causticization System 12, obtains soda bath, wherein NaOH concentration is 110g/L after causticization.Filter cake enters activated carbon activation system 13, Activated using vapor, 800 DEG C of activation temperature, obtain 33.3kg activated carbons, yield (activity following activation carbonaceous amount and activation The ratio of preceding material mass, similarly hereinafter) it is 62wt%, the standard of goods of inferior quality in standard GB/T/T 13803.2-1999 is met, such as Shown in table 2.
Table 2
Embodiment 2
1) sprayed into so that 1000kg solid contents 45wt% cotton pulp is moored into liquid using pressure type shower nozzle in spray dryer, its 250 DEG C of the heat source temperature of middle spray dryer, 120~125 DEG C of exhaust temperature after spraying, in spray dryer bottom sampling analysis liquid powder moisture be 4.7wt%.Calcining furnace body temperature to be completely cut off reaches 600 DEG C, will enter the solid powder of intermediate bin Progress isolation calcining in calcining furnace is quantitatively adding, wherein it is 410kg to add weight of material, material lasts from adding to discharging 60min, solid powder weight is 258kg, and burning decrement is 37wt%.
2) the 258kg solid materials of acquisition are added in the slurrying groove being currently running, wherein used in belt vacuum filter The amount of desalted water is 1161kg, i.e., be 4.5 times of amount of solid in mass ratio, the stirring of running pipeline stock tank is entered with belt vacuum filter Row filtration washing, the filter cake and filtrate composition of acquisition is as shown in table 3.
Table 3
c0(g/L) c1(g/L) c2(g/L) c3(g/L) c4(g/L) wWater(wt%) wNa(wt%) X%
59.10 0.5652 0.3247 0.1847 0.0947 65 0.9 95.00%
Na in filtrate2CO3Concentration is 136.2g/L.
3) above-mentioned filtrate respectively enters causticization system and activated carbon activation system with filter cake, and wherein filtrate enters causticization system System, obtains soda bath, wherein NaOH concentration is 115g/L after causticization；The filter cake of acquisition enters activated carbon activation system, Activated using vapor, 800 DEG C of activation temperature, obtain 36.9kg activated carbon, yield 65wt%.Meet national standard The standard of goods of inferior quality product in GB/T 13803.2-1999, as shown in table 4.
Table 4
Embodiment 3
1) 1000kg solid contents 45wt% cotton pulp is moored into liquid to spray into spray dryer using pressure type shower nozzle, wherein 300 DEG C of the heat source temperature of spray dryer, 135~140 DEG C of exhaust temperature after spraying, in spray dryer bottom Qu sample Fen Xi Liquid powder moisture is 3.5wt%.Calcining furnace body temperature to be completely cut off reaches 650 DEG C, and the solid powder for entering intermediate bin is determined Amount, which is added, carries out isolation calcining in calcining furnace, wherein it is 400kg to add weight of material, material lasts 60min from adding to discharging, Solid powder weight is 240kg, and burning decrement is 40wt%.
2) the 240kg solid materials of acquisition are added in the slurrying groove being currently running, wherein used in belt vacuum filter The amount of desalted water is 1200kg, i.e., be 5 times of amount of solid in mass ratio, the stirring of running pipeline stock tank is carried out with belt vacuum filter Filtration washing, the filter cake and filtrate composition of acquisition is as shown in table 5.
Table 5
c0(g/L) c1(g/L) c2(g/L) c3(g/L) c4(g/L) wWater(wt%) wNa(wt%) X%
54.01 0.4652 0.2214 0.1321 0.0765 65 0.6 96.00%
Na in filtrate2CO3Concentration is 124.5g/L.
3) above-mentioned filtrate respectively enters causticization system and activated carbon activation system with filter cake, and wherein filtrate enters causticization system System, obtains soda bath, NaOH concentration is 110g/L after causticization；The filter cake of acquisition enters activated carbon activation system, utilizes Vapor is activated, 700 DEG C of activation temperature, obtains 28.8kg activated carbon, and yield 60wt% meets standard GB/T/T 13803.2-1999 the standard of middle goods of inferior quality product, as shown in table 6.
Table 6
The present invention by existing Zao Zhi liquid high temperature incineration reclaim alkali lye technology in oxygen-enriched combusting replace with indirectly heat Anaerobic pyrolysis, add the species and yield of recycling product, recycling degree is greatly improved.Jiang of the present invention liquid solid content Spray drying, pyrolysis and belt type filter washing technology coupled, constitute a kind of cotton pulp Bo liquid recycling system.It is true On, those skilled in the art tends in the alkali recovery process using prior art reclaim hydroxide according to common knowledge Sodium is used for paper technology, improvement project is at most taken in terms of how improving alkali recovery, such as CN101585617A is disclosed One kind chemical fiber cotton pulp black liquor is filtered with pulp black liquor by black liquor filter after mix in proportion, evaporate after in alkali recovery furnace The method for carrying out oxy combustion, but its basic line still can not depart from the traditional handicraft of pulp black liquor, face very big engineering There is a wood pulp papermaking in difficulty, only seldom place domestic at present, the place especially more than the fast-growing woods such as Hainan, and Xinjiang is cotton pulp The main product of pool, wooden scarcity of resources, so this technique is upper very limited in application, without exploitativeness.
Applicant states that the present invention illustrates detailed process equipment and the technological process of the present invention by above-described embodiment, But the invention is not limited in above-mentioned detailed process equipment and technological process, that is, do not mean that the present invention has to rely on above-mentioned detailed Process equipment and technological process could be implemented.Person of ordinary skill in the field it will be clearly understood that any improvement in the present invention, Addition, selection of concrete mode of equivalence replacement and auxiliary element to each raw material of product of the present invention etc., all fall within the present invention's Within the scope of protection domain and disclosure.

Claims (10)

1. a kind of cotton pulp Bo liquid recycling system, it is characterised in that the system includes：Drying unit, isolation calcining unit, Separative element, causticization unit and activation unit；
The isolation calcining unit includes heater；The separative element is provided with water inlet, taphole and solid material outlet；
The entrance of the solid material outlet connection separative element of the isolation calcining unit；The solid material outlet of the separative element connects Connect the entrance of the activation unit；The taphole of the separative element connects the entrance of the causticization unit.
2. cotton pulp Bo as claimed in claim 1 liquid recycling system, it is characterised in that it is dry that the drying unit includes spraying Dry device；
Preferably, dust removing units are provided between the drying unit and isolation calcining unit；
Preferably, the dust removing units include cyclone separator and sack cleaner；Wherein, the solid of the spray dryer expects The solid material entrance of the mouth connection cyclone separator, the powder of the powder outlet connection sack cleaner of the cyclone separator Body entrance, the solid material entrance of the powder outlet connection isolation calcining unit of the sack cleaner.
3. cotton pulp Bo as described in any one of claim 1 or 2 liquid recycling system, it is characterised in that the heater Including combustion furnace；
Preferably, the gas vent of the isolation fuel element connects the fuel inlet of the heater.
4. cotton pulp Bo as described in any one of Claims 2 or 3 liquid recycling system, it is characterised in that the heater The outlet connection spray dryer gas access.
5. cotton pulp Bo as described in any one of Claims 1 to 4 liquid recycling system, it is characterised in that the separative element Including slurrying groove and filter, the mixed phase entrance of the outlet connection filter of the slurrying groove；
Preferably, the filter includes belt vacuum filter；
Preferably, the entrance of the separative element is the solid material entrance of the slurrying groove, and the taphole of the separative element is The one-level filtrate (liquid of the filter；
Preferably, the delivery port of the separative element connects the water inlet of the separative element.
6. a kind of cotton pulp Bo liquid method of resource, it is characterised in that comprise the following steps：
(1) by cotton pulp Bo liquid concentrated, obtain concentrate, the concentrate is through being dried to obtain solid content；
(2) solid content obtained by step (1) is subjected to isolation air calcination, obtains carbide and gaseous product；
(3) carbide obtained by step (2) is washed, separation of solid and liquid, respectively collection solid phase and liquid phase；The solid phase is activated Activated carbon is obtained, meanwhile, the liquid phase obtains soda bath and calcium carbonate through causticization.
7. cotton pulp Bo as claimed in claim 6 liquid method of resource, it is characterised in that methods described passes through such as claim System described in 1~5 any one is realized；
Preferably, the solid content of step (1) concentrate is more than or equal to 45wt%, preferably 45~60wt%；
Preferably, step (1) described drying is carried out in the drying unit；
Preferably, the temperature of step (1) described drying is 120~160 DEG C, preferably 130~150 DEG C；
Preferably, in step (1), the mode of the drying includes spray drying；
Preferably, the flue-gas temperature of the spray drying is 250~330 DEG C, preferably 300~330 DEG C；
Preferably, after step (1) described drying, in addition to：Dedusting；
Preferably, the dedusting includes cyclone dust removal and/or bag-type dust, preferably first carries out cyclone dust removal and carries out whirlwind again and remove Dirt；
Preferably, the water content in step (1) described solid content is less than or equal to 5wt%, preferably 2~5wt%.
8. cotton pulp Bo as claimed in claims 6 or 7 liquid method of resource, it is characterised in that step (2) the isolation air Calcining is carried out in the isolation calcining unit；
Preferably, the temperature of step (2) the isolation air calcination is 500~650 DEG C, preferably 600~650 DEG C；
Preferably, the time of step (2) the isolation air calcination is 40~90min, preferably 50~80min；
Preferably, step (2) gaseous product provides heat through burning to the isolation air calcination；
Preferably, carried out in the heater again that burns；
Preferably, step (2) gaseous product produces the high-temperature flue gas that temperature is 800~1000 DEG C through burning；
Preferably, the high-temperature flue gas is used for step (1) spray drying.
9. cotton pulp Bo as described in any one of claim 6~8 liquid method of resource, it is characterised in that step (3) is described to wash Wash including countercurrent washing；
Preferably, the cycle-index of the countercurrent washing is more than or equal to 4 times, preferably 4~6 times；
Preferably, the detergent of step (3) described washing includes desalted water；
Preferably, the quality of step (3) described desalted water is 4~6 times, preferably 4.5~5.5 times of the carbide quality；
Preferably, step (3) washing is carried out in the separative element；
Preferably, step (3) described separation of solid and liquid is carried out in the separative element；
Preferably, the mode of step (3) described separation of solid and liquid includes filtering；
Preferably, step (3) activation is specifically included：The solid phase at 700~900 DEG C is contacted into 1~2h with vapor, Obtain activated carbon；
Preferably, the concentration of sodium carbonate is 110~160g/L, preferably 120~150g/L in step (3) described liquid phase；
Preferably, the concentration of step (3) described soda bath is 110~130g/L, preferably 110~120g/L.
10. cotton pulp Bo as described in any one of claim 6~9 liquid method of resource, it is characterised in that including following step Suddenly：
(1) by cotton pulp Bo liquid concentrated, obtain solid content be more than or equal to 45wt% concentrate, the concentrate is described In drying unit the solid content that water content is less than or equal to 5wt% is dried to obtain through 120~160 DEG C；
(2) solid content obtained by step (1) is completely cut off in calcining unit in progress isolation air calcination at 500~650 DEG C described 40~90min, obtains carbide and gaseous product；The gaseous product is burnt in the heater to the isolation air Calcining provides heat；
(3) carbide obtained by step (2) is washed in the separative element, separation of solid and liquid, collection solid phase and contain respectively 110~160g/L of sodium carbonate liquid phase；The solid phase in the activation unit activate obtaining activated carbon, meanwhile, it is described Liquid phase carries out causticization in the causticization unit and obtains soda bath and calcium carbonate.
CN201710446576.4A 2017-06-14 2017-06-14 A kind of cotton pulp Bo liquid recycling system and method Pending CN107265454A (en)

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Publication number Priority date Publication date Assignee Title
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CN102046877A (en) * 2008-05-06 2011-05-04 美卓动力有限公司 Method and equipment for treatment of black liquor at pulp mill
CN102086605A (en) * 2009-10-05 2011-06-08 美卓动力有限公司 Method and apparatus for processing black liquor of pulp mill

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN85109413A (en) * 1985-12-30 1987-07-08 天津市轻工业学院 Treating waste lye straw pulp-making with wet cracking reaction
CN102046877A (en) * 2008-05-06 2011-05-04 美卓动力有限公司 Method and equipment for treatment of black liquor at pulp mill
CN102086605A (en) * 2009-10-05 2011-06-08 美卓动力有限公司 Method and apparatus for processing black liquor of pulp mill

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Title
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Application publication date: 20171020