CN201678895U - Alkali recovery device for gasifying and directly causticizing pulping black liquor - Google Patents
Alkali recovery device for gasifying and directly causticizing pulping black liquor Download PDFInfo
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- CN201678895U CN201678895U CN2010201854459U CN201020185445U CN201678895U CN 201678895 U CN201678895 U CN 201678895U CN 2010201854459 U CN2010201854459 U CN 2010201854459U CN 201020185445 U CN201020185445 U CN 201020185445U CN 201678895 U CN201678895 U CN 201678895U
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Abstract
The utility model relates to a set of alkali recovery device of black liquor by a sulfate method or a caustic-soda method. The alkali recovery device comprises a black liquor distribution tank 9, wherein a black liquor inlet is arranged on the black liquor distribution tank 9 and is connected to an atomizing nozzle 2 on a black liquor pyrolyzing furnace 1 by a pipeline through a feed preheater 10, and an oxygen or air inlet is arranged on the atomizing nozzle 2; a slag hole of the black liquor pyrolyzing furnace 1 is communicated to a screw feeder 4 and is finally communicated with a gasification furnace 5 of a rotary kiln, and an exhaust port of the black liquor pyrolyzing furnace 1 is communicated to a heating burner 3 and is finally communicated with the gasification furnace 5 of the rotary kiln; and a gas outlet of the gasification furnace 5 of the rotary kiln is communicated with a hydrogen sulfide absorption tower 6, a solid outlet is communicated with a hydrolysis pool 7 and is further communicated with the black liquor distribution tank 9 by a filter 8, the filter 8 is provided with a filtrate outlet, and a branch pipeline is arranged on the filtrate outlet and is communicated to the hydrogen sulfide absorption tower 6. The device has high carbon conversion rate, can generate synthetic gas and can be used for recovering wood-pulp black liquor by a sulfate method and straw-pulp black liquor by a caustic-soda method, a liquid melt is not contained in a reaction system, and the workshop section of lime calcination does not need to be configured.
Description
Technical field
The utility model relates to the pulp industry technical field, relates in particular to a kind of gasifying pulping black liquor and direct causticization soda recovery unit.
Technical background
The traditional black liquor processing mode of pulp industry is a kind of chemical recovery technology that generally adopts, and the core of this technology is recovery boiler (Recovery boiler), the domestic alkali recovery boiler that often is called.Recovery boiler in the thirties in 20th century by the G.H.Tomlinson utility model, become the important milestone of sulfate pulp-making technological development subsequently.Although recovery boiler has been done many improvement for many years, core technology does not change all the time, thereby its inherent shortcoming exists all the time, for example thermodynamic efficiency lower, have fused mass to meet water hidden peril of explosion etc.The black liquor gasification The Application of Technology is expected to address these problems.
Chemical recovery often is known as alkali at home and reclaims, and is that large-scale pulp mill realizes the quantity-produced essential elements.Sprayed in the recovery furnace after the equipment evaporation and concentration such as black liquor process multi-effect evaporator, drop successively through super-dry, pyrolytic process, drop on the soft coke layer of furnace bottom in the way that falls at last, and this one deck is known as bed course.The air feed of bed course (wind) needs control to make carbon generation imperfect combustion, and carbon monoxide and carbon play the effect of reductant, for saltcake (Na
2SO
4) be reduced to sulfide.The heat that produces can make inorganic matter become molten condition, and then enters dissolving tank from furnace bottom by the outflow of water-cooling wall chute.Promptly become green liquor after fused mass is water-soluble, main component is sodium carbonate and vulcanized sodium (if soda processes black liquor then not Containing Sulfur sodium), and this liquid is sent to causticizer and utilizes lime (CaO) to change sodium carbonate into NaOH.So far the white liquid of slurrying forms, and main component is NaOH and vulcanized sodium.Accessory substance white clay (CaCO
3) be admitted in the limekiln calcining and regenerate CaO.In the stove except an air feed of bed course, also have on the top secondary and three air feeds complete to guarantee the combustible gas burning, flue gas stream is by being discharged into atmosphere behind superheater, boiler tube bundle and the economizer, and the steam of production is used to drive the personal vapour of steam turbine and slurry factory.
It is the important difference of itself and general industry boiler that there is one deck fused mass in recovery boiler bottom, and this is the root place of hidden peril of explosion just.Severe corrosive environment in the alkali stove has also limited the raising of steam heat force parameter.In addition, traditional recovery boiler investment is huge, unable the bearing in general medium and small pulp mill, and relatively poor to the straw pulp black liquor operational effect.
The development of black liquor gasification technology is expected to solve the weak point that recovery boiler exists.The black liquor gasification technology just is divided into 2 technology paths at the beginning of its development, and the one, low temperature gasification, the gasifier operation temperature is 600～700 ℃, under the inorganic salts fusing point, so the chemical recovery form is solid-state; The 2nd, high-temperature gasification, the gasifier operation temperature generally is higher than 900 ℃, similar traditional alkali recovery boiler, chemicals is recovered with molten state.
In September, 2004, laid-open U.S. Patents 20040182000 provided the technology of a cover black liquor low temperature steam gasification.The core of this technology is a bubbling fluidized bed, with superheated steam as fluidizing agent and gasifying agent.The black liquor that concentrates is sprayed at a material equably and is gone up generation rapid draing and pyrolysis, and remaining coke is reacted by steam fluidization and generating gasification as the bed material.The bed material time of staying reaches tens of hours, and (general about 24 hours) back draws from furnace bottom dissolves in the water, unconverted carbon is filtered and obtains sodium carbonate liquor, and as traditional alkali recovery process, this solution will be sent to causticization.Different with traditional handicraft is, sulphur will be reclaimed in gas phase, crude synthesis gas through after the hydrogen sulfide absorption for the downstream use, the liquid that has absorbed hydrogen sulfide then becomes the white liquid of rich sulphur and is used for slurrying.The remarkable advantage of this technology is the hidden peril of explosion that does not have the existence of fused mass thereby eliminated conventional recovery boiler.In order to guarantee the fluid bed trouble-free operation, gasifier temperature must keep lower (about 610 ℃) so that the unlikely fusion of black liquor inorganic matter.The required heat that gasifies is provided by a kind of indirect heating apparatus of particular design, and the synthesis gas that is obtained is rich in hydrogen, does not contain or seldom contains nitrogen, and calorific value is higher.Sulphur almost all is released to gas phase, and vulcanized sodium every release 1mol hydrogen sulfide under steam and carbon dioxide effect just will produce 1mol sodium carbonate, and this has increased the causticization load undoubtedly.Lower running temperature causes coke gasification speed slow, goes out still to contain a certain amount of unconverted carbon in the siege material.
6790246 of the U.S. Pat of authorizing in September, 2004 are typical case's representatives of high-temperature gasification technique.Black liquor is sprayed into burner hearth together with air in certain amount or oxygen from top of gasification furnace, and the heat of generation is enough to keep the high temperature more than 900 ℃, and the then separated back of the particle of generation or fused mass is dissolved in the bottom of reactor and formed green liquor in the water.Gas is drawn from reactor and is also contained a certain amount of hydrogen sulfide, and different with aforementioned low temperature process be that the green liquor of Xing Chenging also contains a certain amount of sulfide here.High-temperature molten is a major challenge that this technology faces to the corrosion of reactor linings.
A common feature of black liquor gasification technology is that total some or whole sulfide can be discharged into gas phase, be that vulcanized sodium is transformed into hydrogen sulfide and sodium carbonate under steam and carbon dioxide effect, compare traditional alkali recovery process, this will cause caustic room causticization load to increase.Greatly improve although high-temperature technology is compared low temperature process on the carbon conversion rate, have in the face of the fused mass etching problem.Industry wishes to seek a kind of can at high temperature the operation, can keep inorganic matter again is solid-state black liquor gasification technology, so-called directly causticization (Direct causticization) technology can satisfy this requirement just, and directly the causticization technology will make traditional lime causticization circulation no longer necessary, so the lime calcining kiln of highly energy-consuming also will no longer need.
Canadian Patent CA1193406 has provided a kind of direct causticizing process black liquor treatment technology.As direct caustic, carry out the carbon dioxide removal reaction with iron oxide or titanium oxide, generate sodium ferrite or the sodium titanate and the saltcake of solid state with black-liquor combustion product sodium carbonate.Fully the saltcake reduction can not be finished simultaneously under the burning condition, needs to introduce second reactor and reduces under the effect of hydrogen or carbon monoxide.Can produce the white liquid of slurrying after the solid product hydrolysis after the reduction, comprise sulfide and hydroxide, can't continue the then recycle of solid product of hydrolysis.
The technology of handling black liquor as caustic with iron oxide promptly so-called " directly chemical recovery system " is called for short DARS, and this technology once obtained commercial the application in Australia.But the DARS technology it is generally acknowledged and cannot be used for sulfate liquor that this is that iron oxide can be converted into the sulfide of iron because in the presence of sulfur-containing compound.
Titanium dioxide and titanate are considered to be suitable for the direct preferably caustic of sulfate liquor and obtained more research.Because directly the high-melting-point of higher temperature requirements of causticizing reaction and titanate makes direct causticization technology be applied to existing low temperature fluidized gasification and high-temperature liquid state deslagging entrained flow gasification all has difficulties.
Summary of the invention
The purpose of this utility model provides a kind of carbon conversion rate height, can produce the gasifying pulping black liquor and direct causticization soda recovery unit that do not contain fused mass in synthesis gas, the reaction system, do not need to dispose lime calcining workshop section.The utility model device can be used for reclaim sulfuric acid salt method pulp black liquor and soda processes straw pulp black liquor.
For achieving the above object, the utility model provides following technical scheme:
The utility model device comprises black liquor material-compound tank 9, and black liquor material-compound tank 9 has the black liquor inlet, and black liquor material-compound tank 9 through feed preheater 10, is connected to the atomizer 2 on the black liquor pyrolysis oven 1 by pipeline, and atomizer 2 is provided with oxygen or air intake; The slag notch of black liquor pyrolysis oven 1 is communicated to kiln gas gasifier feeding screw 4 and the final kiln gas gasifier 5 that is communicated with by pipeline, and the exhaust outlet of black liquor pyrolysis oven 1 is communicated to kiln gas gasifier burner for heating 3 and the final kiln gas gasifier 5 that is communicated with by pipeline; The gas vent of kiln gas gasifier 5 is communicated with hydrogen sulfide absorption tower 6 by pipeline, solid outlet is communicated with hydrolytic tank 7 and further is communicated with black liquor material-compound tank 9 through filter 8 by pipeline, filter 8 is provided with filtrate (liquid, and filtrate (liquid is provided with shunt tubes and is communicated to hydrogen sulfide absorption tower 6.
Described black liquor pyrolysis oven 1 and kiln gas gasifier 5 all can adopt prior art equipment.
Water evaporates and the devolatilization of being characterised in that of the present utility model carries out in pyrolysis oven, and be gasified totally and the direct causticizing reaction of organic carbon carry out in kiln gas gasifier.The black liquor that contains direct caustic generates dry, loose semicoke after super-dry, devolatilization, anoxycausis in pyrolysis oven; This kind semicoke is transported to kiln gas gasifier again, finally finishes reactions such as organic carbon gasification, sodium carbonate carbon dioxide removal, saltcake reduction, hydrogen sulfide release at this, exports solid-state sodium salt and hydrogen-rich synthetic gas; Solid-state sodium salt just generates the white liquid of poor sulphur after hydrolysis be sodium hydrate aqueous solution, can not continue the then recycle of sodium salt of hydrolysis; Crude synthesis gas becomes refining synthesis gas behind the hydrogen sulfide and can be used for boiler, internal combustion engine, gas turbine through removing, and also can be used for chemicals such as synthetic liquid fuel, and the liquid behind the absorbing hydrogen sulphide becomes the white liquid of rich sulphur, is sent to slurrying workshop section jointly with the white liquid of above-mentioned poor sulphur.
Following reaction equation 1～11st, some important chemical reactions that the utility model is related:
6TiO
2+ Na
2CO
3→ Na
2O6TiO
2+ CO
2(formula 1)
Na
2O6TiO
2+ Na
2CO
3→ 2 (Na
2O3TiO
2)+CO
2(formula 2)
7Na
2CO
3+ 5 (Na
2O3TiO
2) → 3 (4Na
2O5TiO
2)+7CO
2(formula 3)
5TiO
2+ 4Na
2CO
3→ 4Na
2O5TiO
2+ 4CO
2(formula 4)
3 (4Na
2O5TiO
2)+7H
2O → 14NaOH+5 (Na
2O3TiO
2) (formula 5)
Na
2SO
4+ 2C → 2CO
2+ Na
2S (formula 6)
Na
2SO
4+ 4C → 4CO+Na
2S (formula 7)
Na
2SO
4+ 4CO → 4CO
2+ Na
2S (formula 8)
Na
2S+CO
2+ H
2O → Na
2CO
3+ H
2S (formula 9)
H
2S+2NaOH → Na
2S+2H
2O (formula 10)
Na
2S+H
2S → 2NaHS (formula 11)
The course of work of the utility model device comprises the steps:
1, is delivered to the nozzle of pyrolysis oven continuously through (preheat temperature is no more than 100 ℃) after the preheating together with saltcake of adding and water-fast direct caustic (titanium dioxide or sodium trititanate) from the black liquor of material-compound tank, spray into pyrolysis oven at this by preheated air or oxygen (temperature is generally more than 300 ℃) atomizing, form flame at the spout place.The moisture that contains in the black liquor evaporates rapidly, the organic matter pyrolysis goes out fuel gas and burns, oxygen feeding amount is lower than theoretical oxygen demand, therefore organic carbon does not transform fully, final formation is dry, loose semicoke drops on furnace bottom, wherein contains components such as sodium carbonate, sodium titanate, sodium sulphate and organic carbon.Described pyrolysis oven running temperature is at 800～900 ℃.
2, to be delivered to the next stage reactor continuously be kiln gas gasifier to the semicoke that forms in the above-mentioned pyrolysis oven, formed steam, tar, total reduced form sulphur compound and a small amount of combustible gas etc. also are transported to kiln gas gasifier by burner in the pyrolysis oven, the required heat that gasifies comes from the burning of auxiliary fuel (as diesel oil, heavy oil etc.), is used for the gasification of organic carbon as main gasifying agent from the steam of pyrolysis oven.Sodium carbonate is then finally sloughed carbon dioxide with direct caustic reaction and is formed sodium titanate (reaction equation 1～3, overall reaction 4) in rotary kiln.Saltcake is reduced to vulcanized sodium (reaction equation 6～8) under the effect of carbon, carbon monoxide etc., and vulcanized sodium discharges hydrogen sulfide generation sodium carbonate (reaction equation 9) under the effect of carbon dioxide and steam, and this part sodium carbonate also direct causticizing reaction will take place.The kiln gas gasifier running temperature is at 800～900 ℃, and after the time of staying through 5～10min, will export the end-product sodium titanate (mainly is 4Na
2O5TiO
2) solid and be rich in synthesis gas hydrogen, that contain hydrogen sulfide.
3, the sodium titanate solid from above-mentioned kiln gas gasifier will be introduced into a hydrolytic tank, and airtight hydrolysis 10～30min under boiling or normal temperature state generates sodium hydroxide solution and the another kind of solid sodium titanate (reaction equation 5) that is not easy to continue hydrolysis.Sodium hydroxide solution be the white liquid of poor sulphur some be drawn out of and be sent to the hydrogen sulfide absorption tower as absorption liquid, the overwhelming majority then is sent to slurrying workshop section.
4, being introduced into the hydrogen sulfide absorption tower from the crude synthesis gas of kiln gas gasifier removes hydrogen sulfide (reaction equation 10,11) and forms white liquid of rich sulphur and refining synthesis gas.
5, the sodium titanate that can not continue hydrolysis in the hydrolytic tank is recovered and is sent to the black liquor material-compound tank and continues to be used as direct caustic.
The utility model is compared with traditional alkali recovery technology, air flow bed high temperature air/oxygen-rich gasification technology and fluid bed water at low temperature steam gasification technology, has the following advantages:
1, causticizing reaction is finished in gasification furnace, has saved lime causticization and calcination cycle.
2, behind the direct caustic of introducing, can adopt higher running temperature to improve the carbon conversion rate, simultaneously, owing to do not generate fused mass in the higher thereby reaction system of titanate fusing point, this has eliminated fused mass on the one hand and has met the water explosion danger, has greatly avoided the corrosion of fused mass to refractory brick and steel on the other hand.
3, the synthesis gas of high-temperature vapor gasification generation is rich in hydrogen, if pyrolysis oven adopts oxygen enrichment (for example the carrier of oxygen volume concentrations is greater than 90%), the synthesis gas of then producing at last will have higher quality, and Lower heat value is at 10MJ/Nm
3More than.
4, the staged operation of evaporation and pyrolysis and gasification makes the control of reaction time become simple, and the time of staying that the rotating speed of adjusting kiln gas gasifier can obtain to expect, tar, total reduced form sulphur compound have more time to be able to cracking
5, compare with fluidized-bed gasification furnace, dust content will greatly reduce from the gas that kiln gas gasifier is drawn, and therefore the dedusting cost will reduce.
6, the separately recovery of sulphur and sodium helps making the white liquid of slurrying of different sulphidities, and this has certain effect to optimizing existing sulfate pulp-making technology.
Description of drawings
Fig. 1 is the utility model device technique flow chart.
Description of reference numerals: black liquor pyrolysis oven 1, atomizer 2, kiln gas gasifier feeding screw 3, kiln gas gasifier burner for heating 4, kiln gas gasifier 5, hydrogen sulfide absorption tower 6,4Na
2O5TiO
2Hydrolytic tank 7, Na
2O3TiO
2Filter 8, black liquor material-compound tank 9, feed preheater 10.
The specific embodiment
Below in conjunction with accompanying drawing the utility model is elaborated.
Embodiment one
As shown in Figure 1.Enter black liquor material-compound tank 9 from evaporation section, solid content at the concentrated black liquid more than 50% 21, mix with a kind of direct caustic at this black liquor, directly caustic can be TiO
2If the Na and the K that contain in the black liquor are Na by the whole conversions of its amount of substance
2O, then TiO
2With Na
2O amount of substance ratio should control 1～3, is generally 1.25～1.3.TiO
2Be a kind of water insoluble oxide that also is insoluble to alkali lye, therefore also be insoluble to black liquor, material-compound tank 9 must install agitating device additional to keep the stable homogeneous of material, and speed of agitator generally should not be lower than 50r/min.
In order to increase pyrolysis oven 1 reliability of operation, black liquor and TiO
2Mixture should be preheated to uniform temperature going into the stokehold, be generally 100 ℃, this can realize by feed preheater 10, also material-compound tank 9 can be designed to jacketed type exchanger, perhaps both have both at the same time.The black liquor of preheating and TiO
2Mixture by pipeline 11 by uninterrupted pumping to pyrolysis oven atomizing feed nozzle 2, oxygen or air also are delivered to atomizer 2 by air pump or compressor continuously by pipeline 12.Similarly, in order to improve pyrolysis oven 1 reliability of operation, air or oxygen also should be preheated, for example 300 ℃.Two fluid streams will obtain in the premixer of atomizer 2 mixing, and then spray in pyrolysis oven 1 burner hearth at a high speed.Oxygen that is fed or air capacity should be theoretical oxygen demand or theoretical 40～60% of the air capacity that needs.
Under the about 850 ℃ high temperature action, a series of physicochemical change such as drying, pyrolysis, gas-phase combustion, gasification take place rapidly in the black liquor fine droplet that sprays in burner hearth.If adopt chain grate-type pyrolysis oven, then Can Yu grey black is that black liquid semi-coke drops on the chain type fire grate, moves to pyrolysis oven 1 terminal discharging with fire grate, during can on fire grate, continue variations such as generation drying, pyrolysis, gasification.Above-mentioned pyrolytic process also can adopt other type of furnaces of prior art to realize.Because TiO
2Existence, all do not have fused mass in the reaction system of whole pyrolysis oven 1, even there is the carbonate fusion thing to occur in other words, under high temperature action also rapidly and TiO
2Reaction generates the titanate of high-melting-point (being higher than 950 ℃).Comprise organic carbon, carbonate, titanate, sulfide, sulfate and unreacted TiO in the black liquid semi-coke on the fire grate
2Etc. multiple material, have loose frangible characteristic, be convenient to adopt the various equipment of slagging tap to carry.
Above-mentioned black liquid semi-coke will be delivered to the feeding screw 3 of kiln gas gasifier 5 continuously by pipeline 14, and feeding screw 3 is delivered to kiln gas gasifier 5 continuously with black liquid semi-coke.Gaseous substances such as steam, tar, total reduced form sulphur compound and a small amount of combustible gas from pyrolysis oven 1 spray into kiln gas gasifier 5 via pipeline 13 by burner 4, also can not enter by other approach by burner 4.Steam from pyrolysis oven 1 will be as the organic carbon gasification reaction in the topmost gasifying medium participation kiln gas gasifier 5.For example burning takes place to provide gasification, carbonate to take off CO by burner 4 in heavy oil, natural gas etc. in kiln gas gasifier 5 cylindrical shells from the fuel of pipeline 15
2, the necessary heat of reaction such as saltcake reduction.
The time of staying of solid material in kiln gas gasifier 5 depends primarily on parameters such as kiln bore, kiln length of tube, kiln body rotating speed, material angle of repose, and the kiln pipe has or not inner member.By these parameters of appropriate design, make solid material remain on 5～10min in the time of staying of kiln gas gasifier 5 constant temperature zones, the temperature of constant temperature zone should not be lower than 800 ℃, generally is controlled at 850～900 ℃.Organic carbon gasification, carbonate carbon dioxide removal (reaction equation 4), saltcake reduction (reaction equation 6～8), hydrogen sulfide release a series of chemical changes such as (reaction equations 9) will take place in the kiln gas gasifier 5, finally generate based on the solid matter of titanate with H
2, CO, CO
2, CH
4Be main gas, also contain certain amount of H in the gas
2S, cracking will take place and generate micro-molecular gas in the tar overwhelming majority, and dust content is few in the gas.
Above-mentioned solid product is delivered to hydrolytic tank 7 continuously by pipeline 17, and in order to improve hydrolysis rate, the feedwater 18 of hydrolytic tank 7 can be adopted higher temperature, and hydrolytic tank 7 itself be should give insulation, also can heat.In hydrolytic tank 7, material will stop 10～30min so that hydrolysis (reaction equation 5) is complete substantially, the concrete time according to hydrolysis temperature and water consumption what and different.The hydrolyzate and the solid product that can not continue hydrolysis will be transported to filter 8 afterwards, finish the separation of solid-liquid two-phase at this.Na
2O3TiO
2Generally be considered as not facile hydrolysis, but this hydrolysate can recycle (reaction equation 3), thereby will be recovered and send into black liquor material-compound tank 9, replace fresh TiO
2Continue on for next circulation and carry out same effect.Filtrate just hydrolyzate is the liquid that is rich in NaOH, and the wherein less sulfide that contains, through pipeline 20 outputs, this liquid 24 will be transported to slurrying workshop section and use for boiling, and a small part will be drawn out of by pipeline and be transported to hydrogen sulfide absorption tower 6 and be used to gasify the washing of crude synthesis gas to absorb H
2S.
As previously mentioned, contain certain amount of H in the crude synthesis gas from kiln gas gasifier 5
2S, crude synthesis gas will be admitted to hydrogen sulfide absorption tower 6 by pipeline 16, with the liquid generation counter-current absorption effect from pipeline 20.If aforesaid liquid 24 is referred to as the white liquid of poor sulphur, then control the white liquid 23 of rich sulphur that The reasonable operating conditions can obtain containing sulfide, the white liquid 23 of rich sulphur promptly becomes the kraft cooking soup with the white liquid 24 of poor sulphur by allotment.The gas that the absorption cat head obtains becomes refining synthesis gas 22.
Embodiment two
Na
2O3TiO
2With fresh TiO
2Has the CO that takes off much at one
2Ability can at high temperature be sloughed CO with carbonate
2And form for example 4Na of new titanate
2O5TiO
2, temperature is controlled at 850～900 ℃.Although 4Na
2O5TiO
2Can not hydrolysis complete, but its hydrolysis solid product Na
2O3TiO
2Can utilize again, satisfy the closed circulation that this point just can form caustic, therefore can the circulation of replace lime causticization.The TiO that in a last embodiment, describes
2The direct formed end-product Na of causticization process
2O3TiO
2Become the direct causticization intercycle product of present embodiment.
As shown in Figure 1, from the sulfate liquor 21 of evaporation section and Na from hydrolytic tank 7
2O3TiO
2Fully mix the back and is delivered to atomizer 2 continuously in black liquor material-compound tank 9, carry out the various processes identical with embodiment one, the solid-state end-product of output kiln gas gasifier 5 is similarly 4Na
2O5TiO
2(reaction equation 3).
Embodiment three
The soda processes straw pulp black liquor is because therefore sulfur-bearing not adopts the alkali recovery equipment of this technology simple relatively.Needn't install hydrogen sulfide absorption tower 6 additional in the processing of crude synthesis gas, the liquid of hydrolytic tank 7 outputs is NaOH solution, directly uses for boiling.Other aspects reclaim not different significantly with the gasification and the alkali of sulfate liquor.
Claims (2)
1. gasifying pulping black liquor and direct causticization soda recovery unit, comprise black liquor material-compound tank (9), black liquor material-compound tank (9) has the black liquor inlet, it is characterized in that black liquor material-compound tank (9) by pipeline through feed preheater (10), be communicated to the atomizer (2) on the black liquor pyrolysis oven (1), atomizer (2) is provided with oxygen or air intake; The slag notch of black liquor pyrolysis oven (1) is communicated to kiln gas gasifier feeding screw (4) and the final kiln gas gasifier (5) that is communicated with by pipeline, and the exhaust outlet of black liquor pyrolysis oven (1) is communicated to kiln gas gasifier burner for heating (3) and the final kiln gas gasifier (5) that is communicated with by pipeline; The gas vent of kiln gas gasifier (5) is communicated with hydrogen sulfide absorption tower (6) by pipeline, and solid outlet is communicated with hydrolytic tank (7) and further is communicated with black liquor material-compound tank (9) through filter (8) by pipeline, and filter (8) is provided with filtrate (liquid.
2. gasifying pulping black liquor as claimed in claim 1 and direct causticization soda recovery unit is characterized in that filter (8) filtrate (liquid is provided with shunt tubes and is communicated to hydrogen sulfide absorption tower (6).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010201854459U CN201678895U (en) | 2010-04-30 | 2010-04-30 | Alkali recovery device for gasifying and directly causticizing pulping black liquor |
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|---|---|---|---|
| CN2010201854459U CN201678895U (en) | 2010-04-30 | 2010-04-30 | Alkali recovery device for gasifying and directly causticizing pulping black liquor |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101845766A (en) * | 2010-04-30 | 2010-09-29 | 中国科学院广州能源研究所 | Method and device for gasifying pulping black liquor and reclaiming directly causticized alkali |
| CN105668892A (en) * | 2016-02-02 | 2016-06-15 | 南京林业大学 | Straw pulp black liquor processing device and method thereof |
| CN110938474A (en) * | 2019-12-17 | 2020-03-31 | 新奥科技发展有限公司 | Method for loading papermaking black liquor on coal sample, fluidized bed furnace and system |
-
2010
- 2010-04-30 CN CN2010201854459U patent/CN201678895U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101845766A (en) * | 2010-04-30 | 2010-09-29 | 中国科学院广州能源研究所 | Method and device for gasifying pulping black liquor and reclaiming directly causticized alkali |
| CN105668892A (en) * | 2016-02-02 | 2016-06-15 | 南京林业大学 | Straw pulp black liquor processing device and method thereof |
| CN105668892B (en) * | 2016-02-02 | 2018-02-02 | 南京林业大学 | Straw pulp black liquor processing unit and its method |
| CN110938474A (en) * | 2019-12-17 | 2020-03-31 | 新奥科技发展有限公司 | Method for loading papermaking black liquor on coal sample, fluidized bed furnace and system |
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