CN105696397B - Extract the device of hemicellulose, cellulose and lignin simultaneously from biomass material - Google Patents
Extract the device of hemicellulose, cellulose and lignin simultaneously from biomass material Download PDFInfo
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- CN105696397B CN105696397B CN201610058558.4A CN201610058558A CN105696397B CN 105696397 B CN105696397 B CN 105696397B CN 201610058558 A CN201610058558 A CN 201610058558A CN 105696397 B CN105696397 B CN 105696397B
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- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C5/00—Other processes for obtaining cellulose, e.g. cooking cotton linters ; Processes characterised by the choice of cellulose-containing starting materials
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07G—COMPOUNDS OF UNKNOWN CONSTITUTION
- C07G1/00—Lignin; Lignin derivatives
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- C—CHEMISTRY; METALLURGY
- C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
- C08B—POLYSACCHARIDES; DERIVATIVES THEREOF
- C08B37/00—Preparation of polysaccharides not provided for in groups C08B1/00 - C08B35/00; Derivatives thereof
- C08B37/14—Hemicellulose; Derivatives thereof
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Abstract
The present invention provides the device for extracting hemicellulose, cellulose and lignin simultaneously from biomass material, and it includes one-level separator, secondary separation device, three-level separator, membrane treatment appts, pH real-time monitoring devices, liquid phase mixing arrangement and volume control device；Combination by these devices can be 10 with up to less than 13 lignin membrane processing supernatant replacement or partly substitute alkali lye to adjust the pH of IC anaerobic towers to required scope with pH value.The method of the present invention can reduce the independent processing cost of supernatant, and effectively solve the liquid to the potential contamination hazard of environment, reduce cumbersome procurement process, eliminate handling liquid caustic soda and danger be present.
Description
Technical field
The present invention relates to biomass as resources high-efficiency comprehensive utilization field, carried simultaneously more particularly to from biomass material
Take the device of hemicellulose, cellulose and lignin.
Background technology
Contain a large amount of fibre fractionations in for example various straws of agricultural biomass resource.Biomass as resources synthesis profit
One of important research direction is that biomass resource is obtained into cellulose, hemicellulose and lignin by isolation technics,
Three is referred to as " three elements ".Needed to use in three plain separation processes and largely use water, while also supervened considerable various
Liquid, including hemicellulose liquid phase caused by being separated in one-level and the biochemical lignin stoste obtained when three-level separates
And the supernatant obtained by stoste after film device is handled.
In traditional biomass resource comprehensive utilization technique, the supernatant that is obtained for biochemical lignin stoste after film process
Liquid is then expelled directly out generally as waste water.It is well known that lignin membrane processing supernatant be a kind of alkalescence it is higher, containing a large amount of solid
Body composition and the high liquid of COD.It is expelled directly out that Heavy environmental pollution can be caused.This is also three element separation works
Maximum pollution source in skill.Therefore traditional treatment method is both unfavorable for environmental protection, also result in the wasting of resources, is unfavorable for giving birth to
The comprehensive utilization of physical resources.As China's economic increasingly makes the transition to efficient, low-carbon, high processing cost and cost of material are to restrict
The commercialization of traditional handicraft is important obstacle, and the research of the reutilization technology of lignin membrane processing supernatant has great meaning
Justice.
At present, the correlative study for lignin membrane processing supernatant recycling is less.Such as in CN103373784A
Disclose for returning to the sode ash after recycling or sending to dissolving boiler combustion.Concentration charcoal is disclosed in CN101045535A
Change to produce the technology of carbon black.However, these reutilization technologies are in itself and imperfect, and can not meet current diversified
Need.Therefore, it is necessary to develop new reutilization technology for lignin membrane processing supernatant.
The content of the invention
In order to further develop waste water caused by three element separation, particularly lignin membrane processing supernatant, improve
Biomass resource comprehensive utilization ratio, various materials and chemistry of the present inventor for waste water caused by three element separation
Property is analyzed, and on this basis, inventor has found IC anaerobic tower inflow requirement pH 6.8~7.5, for anaerobism hair
The pH of hemicellulose liquid phase is usually less than 6.8 caused by the one-level separation of ferment, in order to meet IC anaerobic tower inflow requirements, generally
Liquid caustic soda regulation pH need to be used.On the other hand, inventor also found lignin membrane processing supernatant pH value for 10 with up to 13 with
Under, and by handling supernatant simple process to lignin membrane, you can alkali lye is substituted to adjust IC using its replacement or part
The pH of anaerobic tower is to required scope.The present invention is completed based on this.
Therefore, the present invention provides a kind of dress for extracting hemicellulose, cellulose and lignin simultaneously from biomass material
Put, it includes one-level separator, secondary separation device, three-level separator, membrane treatment appts, pH real-time monitoring devices, liquid
Mix device and volume control device；
Wherein：
One-level separator is used to pretreated biomass material carrying out vapour cooking processing, is then cleaned through multistage
After carry out the first separation of solid and liquid and obtain the first liquid phase and the first solid phase, wherein, the vapour cooking processing be with 0.6MPa~
3.0MPa vapour cooking 1min~5min, first liquid phase are the hemicellulose liquid phase that pH is less than 6.8；
Secondary separation device be used for will the first solid phase carry out base extraction after carry out the second separation of solid and liquid and obtain second liquid phase
And second solid phase, wherein, the alkali process is in terms of the gross mass of the first solid phase, and it is 4% to add concentration to first solid phase
~10% aqueous slkali, boiling 0.5h~3h under conditions of 60 DEG C~130 DEG C；
Three-level separator be used for second liquid phase is precipitated, filtered, is activated, selected processing, obtain the 3rd liquid phase and
3rd solid phase, wherein the 3rd liquid phase is biochemical lignin stoste；
Membrane treatment appts are used to handle the biochemical lignin stoste, supernatant and biochemical lignin product are obtained, wherein described
The temperature of supernatant is for 0 DEG C with up to less than 45 DEG C, and for pH value for 10 with up to less than 13, COD content is 15000mg/
Below L, suspension content are below 300mg/L；
Liquid phase mixing arrangement is used to mix the supernatant with the hemicellulose liquid, so as to obtain mixed phase；
PH real-time monitoring devices include pH value measuring appliance, and the pH real-time monitoring devices are used to mix described in real time on-line monitoring
The pH value of phase is closed, and Monitoring Data is transferred to volume control device；
Volume control device is used for the mixing that supernatant and the hemicellulose liquid are adjusted according to the pH value monitored
Than so as to control the pH value of mixed phase for 6.8 with up to less than 7.5 scope.
Preferably, liquid phase mixing arrangement is circulatory pool.Further preferably it is provided with agitator.
Volume control device is control valve in certain embodiments, and it is configured to big according to the pH value monitored
The size of small next automatic control valve opening.
In certain embodiments, the device of hemicellulose, cellulose and lignin is extracted simultaneously from biomass material
Further comprise anaerobic tower, and the mixed phase passes through pipeline and anaerobic tower UNICOM.
In certain embodiments, one-level separator, secondary separation device, three-level separator, membrane treatment appts and
Pass through pipeline UNICOM between liquid phase mixing arrangement.
In certain embodiments, pH real-time monitoring devices are arranged in liquid phase mixing arrangement.
And first flow control in certain embodiments, including first flow control device and second flow control device,
Device processed is arranged between liquid phase mixing arrangement and membrane treatment appts, second flow control device be arranged on hemicellulose liquid phase with
Between liquid phase mixing arrangement.Preferably, also further 3rd volume control device, and the 3rd volume control device is arranged on alkali lye
Between storage device and liquid phase mixing arrangement.
In some embodiments, it is preferred that ground further comprises alkali storage device, alkali storage device and the liquid phase
Mixing arrangement is connected by pipeline.
In certain embodiments, pH real-time monitoring devices are provided with calculator.Calculator is electrically connected with volume control device
Connect.Such as electrically connected with second flow control device.Alternatively, electrically connected with the 3rd volume control device.
In conventional apparatus, anaerobic fermented liquid pH regulation needs to use alkali lye to be carried out in circulatory pool, it is necessary to using big
Alkali lye is measured, each cost consumption is big, and liquid caustic soda consumption is finished the procurement process, it is necessary to cumbersome, and loads and unloads liquid caustic soda and peace be present
It is complete dangerous.In the apparatus of the present, lignin membrane will be added in the hemicellulose liquid phase for being used as zymotic fluid by said apparatus
Supernatant after processing can keep the pH value of IC anaerobic towers to require, and from the point of view of sewage disposal system Monitoring Data, supernatant
Liquid substitutes liquid caustic soda and run without influence on biochemical system operation and advanced treating, and every monitoring index meets technic index.Therefore,
The device of the present invention can reduce the independent processing cost of supernatant, and effectively reduce cumbersome procurement process, eliminate handling
Danger be present in liquid caustic soda.
Brief description of the drawings
Fig. 1 schematically illustrates figure for traditional three-level separator.
Fig. 2 schematically illustrates figure for the device as one of the application preferred embodiment.Wherein pH value monitors in real time
Device is arranged on the mixing arrangement with agitator.
Fig. 3 schematically illustrates figure for the device as one of the application preferred embodiment.Wherein pH value monitors in real time
Device is arranged on the mixing arrangement with agitator, and pH value real-time monitoring device is further provided with calculator.
Fig. 4 schematically illustrates figure for the device as one of the application preferred embodiment.Wherein pH value monitors in real time
Device is arranged on the mixing arrangement with agitator, and pH value real-time monitoring device is further provided with calculator；And pH value
Real-time monitoring device with as second and the 3rd the valve of volume control device electrically connect.
Embodiment
Now each exemplary of the present invention is described in detail, embodiment therein is illustrated with accompanying drawing.
It is understood that following detailed description is not limitation of the invention, it is conversely to be provided for reader to some of the present invention
The details of aspect and feature is better understood from.
In the present invention, various scientific and technical terminologies, noun are respectively provided with common implication in the art, unless otherwise mentioned.Separately
Outside, the unit described herein for representing weight is kilogram (Kg), unless otherwise mentioned.
In the present invention, biomass material can produce cellulose, hemicellulose and lignin by three fractionation techniques.
These three materials are collectively referred to as " three elements " herein, by referred to as " three elements separate by the technology of the element of three fractionation techniques production three
Technology ".Different product is respectively obtained including by separation means three times, and different product is developed for producing three elements.
As the term " biomass " used in the present invention, refer to for various fibrous materials, as hardwood, cork,
Recycled writing paper, waste paper, forest trimmings, paper pulp and papermaking wastewater, agricultural crop straw, bagasse and switchgrass, and more than one classes
The mixture of the cellulose biomass of type.Those skilled in the art will recognize that other cellulose containing raw materials be present, and can be with
Separation is classified by the method for implementing the present invention.For example, include, but are not limited to as hardwood biolobic material, all kinds of trees
Branch such as shrub branch, dead leaves, and/or the material as caused by its processing, including sawdust, wood chip, wood shavings etc..As crop straw
Stalk, including cornstalk, wheat-straw, barley-straw, rice straw etc..Also include other plant fiber, for example, reed, flax class, weeds,
Waste material of edible mushroom, cereal shell, wheat bran, beans stalk, Cotton Stalk, potato class seedling etc..From the angle for reducing sugar content, preferably wheat
The other plant fiber such as the crop materials such as stalk, barley-straw, rice straw and reed, flax class, from cost economy, wide material sources
And angle easy to process, particularly preferred wheat-straw.
Term " classification separation " of the present invention, refers to removing at least part material from biomass material, such as remove
At least part cellulose.Including but not limited to it is separated by filtration, precipitates separation etc..
" pretreatment " refers to the physical property for changing biomass in some way, for example, the length of change biomass, size
Cutting and grinding are handled；Also include the chemical property for changing biomass, for example, crystallinity, the degree of polymerization, surface area, to hemicellulose
Change in terms of element and/or the combination of lignin and the solubility in specific solvent.
" aqueous slkali " (also referred to as " alkali lye ", " liquid caustic soda ") used in three-level separation is in the art usually used
The aqueous solution of akaline liquid, the usually hydroxide of alkali metal, for example, NaOH, KOH, Ca (OH)2Deng the aqueous solution, can also wrap
Include ammoniacal liquor, NaHCO3Deng the solution of common alkaline matter in the art.As alkali lye concentration based on weight be preferably 4%~
10%, preferably 6%~8%, further preferably 6.5%~7.5%, most preferably 7%.
In the present invention, " hemicellulose liquid " (herein sometimes referred to as " anaerobic fermented liquid ") preferably refer to by using
0.6MPa~3.0MPa vapour cooking 1min~5min, carries out multistage cleaning again after boiling and separation of solid and liquid obtains rich in half
The organic liquid phase of cellulose.The pH value of thus obtained hemicellulose liquid phase is usually less than 6.8.It is for example, low in some cases
It is less than 6.0 under 6.5, particular case.It is anaerobism therefore because hemicellulose liquid phase is the liquid containing large amount of organic matter
Fermentation produces the very good material of biogas.
Heretofore described term " the film process supernatant of lignin " is (sometimes referred to as " supernatant " herein, " clear
Liquid ", " industrial wastewater ", " film process supernatant " or " pH adjusts liquid ") refer to obtain lignin liquid phase by three fractionation techniques
Afterwards, then by seperation film the supernatant obtained after the removal of impurity is filtered off.Under normal circumstances, the temperature of supernatant is 0 DEG C with up to
Less than 45 DEG C, pH value is for 12 with up to less than 12.5, and COD content is below 15000mg/L, and suspension content is
Below 300mg/L.From the viewpoint for being easy to subsequent fermentation, preferably the temperature of supernatant be 30 DEG C with up to less than 40 DEG C, it is especially excellent
Select 37 DEG C.PH value on supernatant is different because of the usage amount of alkali lye, but usually 12 with up to less than 12.5.From as detesting
The viewpoint of the pH regulation liquid of aerobe fermentation liquid, preferably higher pH value, such as preferable ph is 12.5,12.4,12.3,12.2 etc..
Content on suspension is different because of the film difference used, generally, as long as can be that arbitrary content not influence this hair
Bright described purpose.Although being not particularly limited, the content of suspension is after film process under normal conditions
Below 300mg/L, although can also exceed more than 300mg/L.In the case of using having tiny aperture film, the content of suspension
It is smaller, such as can be below 250mg/L, below 230mg/L, below 200mg/L, or even 150 or below 100mg/L.Using
In the case of larger aperture film, the content of suspension can become big, such as can be below 350mg/L, below 400mg/L, even
Below 450mg/L.
In addition, " film " as described herein is usually used film in the art, including it is microfiltration membranes, milipore filter, NF membrane, anti-
Permeable membrane and combinations thereof.
It should be noted that the mixing arrangement of the present invention is used to adjust liquid using supernatant as pH to adjust anaerobic fermented liquid
PH value.In certain embodiments, mixing arrangement of the invention is only used for the pH value of supernatant regulation anaerobic fermented liquid.
In other some embodiments, the present invention adjusts anaerobic fermented liquid using a part of alkali lye simultaneously using a part of supernatant
PH value.As long as can realize that the pH value of regulation anaerobic fermented liquid is arrived in required scope, the present invention can be combined use supernatant and
Alkali lye.On both use levels, it is not particularly limited, as long as the purpose of the present invention can be realized.For example, in some implementations
In scheme, 80 volume % supernatant and 20 volume % alkali lye (the 5%NaOH aqueous solution) can be used to adjust pH value.
Heretofore described " regulation " is well known in the art including supernatant and/or alkali lye are passed through with anaerobic fermented liquid
Means, such as stirring etc. mixed, so as to which high pH value supernatant and/or alkali lye and low pH anaerobic fermented liquid be occurred
Neutralization reaction, make pH value control in required scope, for example, in the range of 6.8~7.5, or in the range of 6.9~7.4, preferably control
It is formed on 7.0.When " regulation " can betide fermentation progress, such as the fermentation tank (such as IC anaerobic towers) to be fermented
It is interior, it can also betide before being fermented.From pH stability, be advantageous to the viewpoint of uniform fermentation, preferably enter in anaerobic fermented liquid
The regulation or mixing are carried out in circulatory pool before entering fermentation tank.
In invention preferred embodiment, the regulation includes monitoring the pH of the anaerobic fermented liquid in real time, and according to
The pH monitored adjusts the combined amount of anaerobic fermented liquid and supernatant and/or alkali lye by automatic control means.Preferably, lead to
The pH of pH measure device measure anaerobic fermented liquids is crossed, and pH data are sent to by computer by data wire in real time, and by calculating
Machine operation program analyze data is simultaneously calculated the pH of mixed liquor and is maintained at 6.8 with required in up to less than 7.5 scope
Supernatant and/or alkali lye, instruction control supernatant is then sent according to result of calculation and/or alkali lye enters anaerobic fermented liquid
Amount.
It should be strongly noted that the key of the present invention is supernatant is substituted into liquid caustic soda using acid-base neutralization reaction principle
The pH of mixed liquor in circulatory pool is adjusted, on the premise of rationally hemicellulose liquid pH value is improved, individually processing supernatant is reduced and takes
With, and save the use of liquid caustic soda.IC anaerobic tower inlet flow-patterms claimed range 6.8~7.5, the hemicellulose liquid pH in circulatory pool are past
Toward being less than 6.8, film process supernatant is added at circulatory pool water inlet, uninterrupted control can keep circulatory pool pH 6.8
In the range of~7.5, IC anaerobic towers normal operation in the range of technic index can be ensured.Dosing flow：Workshop film process supernatant
Liquid is to enter holding vessel by pipeline, clear liquid is entered circulatory pool by the drug feeding pipeline valve regulated flow on holding vessel, follows
The operation of cisterna ambiens submersible agitator promotes clear liquid and hemicellulose liquid uniformly to mix.
The present invention is described in detail below by the accompanying drawing of the application.
Fig. 1 schematically illustrates figure for traditional three-level separator.Wherein one-level separator be used for will be pretreated
Biomass material carries out vapour cooking processing, and then carrying out the first separation of solid and liquid after multistage is cleaned obtains the first liquid phase and first
Solid phase, wherein, vapour cooking processing is vapour cooking 1min~5min with 0.6MPa~3.0MPa, first liquid phase
It is less than 6.8 hemicellulose liquid phase for pH；
Secondary separation device be used for will the first solid phase carry out base extraction after carry out the second separation of solid and liquid and obtain second liquid phase
And second solid phase, wherein, the alkali process is in terms of the gross mass of the first solid phase, and 4%~10% is added to first solid phase
Aqueous slkali, boiling 0.5h~3h under conditions of 60 DEG C~130 DEG C；
Three-level separator be used for second liquid phase is precipitated, filtered, is activated, selected processing, obtain the 3rd liquid phase and
3rd solid phase, wherein the 3rd liquid phase is biochemical lignin stoste；
Membrane treatment appts are used to handle the biochemical lignin stoste, supernatant and biochemical lignin product are obtained, wherein described
The temperature of supernatant be 0 DEG C with up to less than 45 DEG C, for 12 with up to less than 12.5, COD content is pH value
Below 15000mg/L, suspension content are below 300mg/L.Supernatant is discharged as waste liquid by outlet.
In the device of one of the preferred embodiments of the invention, on the basis of traditional three-level separator, further
Liquid phase mixing arrangement is provided with, it is used to mix aqueous slkali or aqueous slkali with supernatant with the hemicellulose liquid, so as to
To mixed phase.Preferably, mixing arrangement can be circulatory pool.Further optionally, mixing arrangement is the container being separately provided in addition.
As long as mixing arrangement can be used to mix two kinds of different even in liquid phase, then the shape for mixing arrangement or outward appearance do not limit especially
It is fixed.Even so, from the viewpoint for avoiding external environment to influence as far as possible, preferably mixing arrangement is locking device.Alternatively, mixing dress
At least two liquid phase inlet ports are installed, one of them is used to introduce the hemicellulose liquid phase that pH is less than 6.8, and another inlet port is used
In introducing pH value for 12 with up to less than 12.5 supernatant.Alternatively, mixing arrangement may also include at least one outlet, and it is used
In well mixed rear pH value is introduced into other devices with up to less than 7.5 mixed phase for 6.8, for example, introducing anaerobic fermentation dress
Put.
Preferably, mixing arrangement is further provided with pH value monitoring device.For example, pH value measure commonly used in the art
Instrument, it is generally BPH-200A, BPH-200B, BPH-200D, BPH-220 etc..Mainly it is made up of sensor and secondary meter,
Sensor (namely electrode part) can according to different application scenarios, match different electrodes (such as：It is high temperature, strong acid, strong
Alkali, hygiene-type).For example, triplex or two combination electrodes can be matched somebody with somebody, to meet various fields of employment.Further preferred pH value monitoring
Device is real time on-line monitoring device.
In certain preferred embodiments, volume control device is further provided with.Preferably, itself and pH value monitoring device
Connection, such as electrically connect.Alternatively, volume control device is the valve of control fluid flow.Alternatively, valve can have and cut
Only, regulation, water conservancy diversion, prevent any function such as adverse current, voltage stabilizing, shunting or overflow pressure relief.It is not particularly limited type, the material of valve
Material.For example, it may be selected from the simplest stop valve various valves used into extremely complex robot control system(RCS), its kind and rule
Lattice are quite various.Valve can be used for the flowing of control all kinds fluid.Valve is also divided into cast iron valve, cast-steel valve according to material
Door, stainless valve (201,304,316 etc.), chrome-molybdenum steel valve, Chrominm-molybdenum-vanadium steel valve, dual phase steel valve, Plastic valve are nonstandard
It is customized to wait valve material.
As preferred embodiment, volume control device electrically connects with pH value monitoring device, and can be according to being supervised
The pH value size of survey and adjust the flow of fluid.As long as the pH value that can control mixed phase is 6.8 with up to less than 7.5 scope
It is interior, then it is not particularly limited specifically connected mode.Preferably, pH value size is easily achieved by the accurate calculating of calculator
Associating between fluid flow size.Preferably, the electrical connection includes pH value Monitoring Data is transferred into calculator and led to
The uninterrupted data transfer crossed after calculator conversion controls volume control device to controller.
Embodiment 1
Figure below illustrates the device of the present invention according to schematic Fig. 2-4.One-level separator includes one-level separation steaming in Fig. 2-4
Boil device and one-level separation cleaning device.Biomass carries out 0.6MPa~3.0MPa steamed in one-level separates steaming plant
Boil 1min~5min.Enter one-level separation cleaning device after steam treatment.Obtained solid fabric element enters secondary separation device,
Liquid hemicellulose then enters the circulatory pool with stirring slurry.In secondary separation device, in terms of the gross mass of the first solid phase, add
Enter the aqueous slkali that concentration is 4%~10%, boiling 0.5h~3h under conditions of 60 DEG C~130 DEG C.Obtain liquid.In three fractions
From in device, aforesaid liquid being precipitated, filtering, activating, selected processing, biochemical lignin stoste is obtained.Filled into film process
Put to obtain supernatant and biochemical lignin product.Supernatant is mixed so as to obtain mixed phase with hemicellulose liquid in circulatory pool.
PH real-time monitoring devices are arranged in circulatory pool side wall in fig. 2.PH real-time monitoring devices, which are arranged at, in figure 3 follows
In cisterna ambiens side wall, and further pH real-time monitoring devices are provided with calculator.PH real-time monitoring devices, which are arranged at, in Fig. 4 follows
In cisterna ambiens side wall, pH real-time monitoring devices are provided with calculator, and further pH real-time monitoring devices lead to the pH value monitored
Data line transfer is crossed to the valve of alkali lye and the valve of liquid hemicellulose, and the big I of valve openings according to pH value and
Regulation, so as to control the pH value of mixed phase for 6.8 with up to less than 7.5 scope.
Embodiment 2
In order to verify the feasibility of the present invention, following experiment has been carried out by Fig. 3 described devices of the present invention：
1st, clear liquid storage tank：Storage tank is that cuboid stainless steel is box, volume 12m3。
2nd, clear liquid comes water process and is introduced into storage tank, and then by adjusting outlet valve, uninterrupted is controlled in energy
Circulatory pool pH is enough kept in the range of 6.8~7.5.
3rd, clear liquid indices：Temperature≤45 DEG C, pH value 12~12.5, COD (COD) content≤15000mg/
L, SS (suspension) content≤300mg/L.
4th, into hemicellulose liquid indices in circulatory pool：30 DEG C~37 DEG C of temperature, pH value 5.0~7.5, COD (chemistry
Oxygen demand) content≤8000mg/L, SS (suspension) content≤500mg/L.
5th, hemicellulose liquid indices in circulatory pool：30 DEG C~37 DEG C of temperature, pH value 6.8~7.5, COD (chemical oxygen demands
Amount) content≤8000mg/L, SS (suspension) content≤500mg/L.
6th, IC anaerobic towers Inlet and outlet water, oxidation ditch Inlet and outlet water COD (COD) are detected, calculates COD (COD)
Clearance, the outer draining indices of detection advanced treating, record observation 15 days.
The liquid caustic soda of table 1. adjusts circulatory pool pH operational monitoring data
The clear liquid of table 2. substitutes the day data of liquid caustic soda regulation circulatory pool pH operational monitorings 15
From the point of view of data comparison before and after Tables 1 and 2, supernatant can be substituted by liquid caustic soda addition by the device of the present invention and followed
Cisterna ambiens adjusts IC reaction tower inlet flow-patterms, does not have because of influenceing the normal operation of sewage disposal system using clear liquid and technique refers to
Mark.That is, device of the invention is feasible.
Although the present invention has been described on exemplary, the invention is not limited in described disclosed exemplary
Embodiment.The scope of claim is consistent with most wide explanation so as to including all such improvement and equivalent structure and effect.
Claims (16)
1. a kind of device for extracting hemicellulose, cellulose and lignin simultaneously from biomass material, it includes one-level separation
Device, secondary separation device, three-level separator, membrane treatment appts, pH real-time monitoring devices, liquid phase mixing arrangement and flow control
Device processed；
Wherein：
One-level separator is used to pretreated biomass material carrying out vapour cooking processing, then laggard through multistage cleaning
The separation of solid and liquid of row first obtains the first liquid phase and the first solid phase, wherein, the vapour cooking processing is with 0.6MPa~3.0MPa
Vapour cooking 1min~5min, first liquid phase be pH be less than 6.8 hemicellulose liquid phase；
Secondary separation device is used to carrying out the first solid phase carrying out the second separation of solid and liquid after base extraction obtaining second liquid phase and the
Two solid phases, wherein, the alkali process be in terms of the gross mass of the first solid phase, to first solid phase add concentration be 4%~
10% aqueous slkali, boiling 0.5h~3h under conditions of 60 DEG C~130 DEG C；
Three-level separator by second liquid phase for being precipitated, being filtered, being activated, selected processing, obtains the 3rd liquid phase and the 3rd
Solid phase, wherein the 3rd liquid phase is biochemical lignin stoste；
Membrane treatment appts are used to handle the biochemical lignin stoste, supernatant and biochemical lignin product are obtained, wherein the supernatant
The temperature of liquid is for 0 DEG C with up to less than 45 DEG C, and for pH value for 12 with up to less than 12.5, COD content is 15000mg/L
Hereinafter, suspension content is below 300mg/L；
Liquid phase mixing arrangement is used to mix the supernatant with the hemicellulose liquid, so as to obtain mixed phase, the mixing
Device sets at least two liquid phase inlet ports and at least one outlet, and at least two liquid phases inlet port is respectively used to introduce pH
Hemicellulose liquid phase and pH value less than 6.8 are used to incite somebody to action for 12 with up to less than 12.5 supernatant, at least one export
Mixed phase introduces other devices；
PH real-time monitoring devices include pH value measuring appliance, and the pH real-time monitoring devices are used for mixed phase described in real time on-line monitoring
PH value, and Monitoring Data is transferred to volume control device；
Volume control device is used for the mixing ratio that supernatant and the hemicellulose liquid are adjusted according to the pH value monitored, from
And control the pH value of mixed phase for 6.8 with up to less than 7.5 scope.
2. device according to claim 1, wherein the liquid phase mixing arrangement is circulatory pool.
3. device according to claim 1 or 2, wherein the liquid phase mixing arrangement is provided with agitator.
4. device according to claim 1 or 2, wherein the volume control device is control valve, it is configured to root
Carry out the size of automatic control valve opening according to the pH value size monitored.
5. device according to claim 1 or 2, it further comprises anaerobic tower, and the mixed phase by pipeline with detesting
Oxygen column UNICOM.
6. device according to claim 1 or 2, wherein the one-level separator, the secondary separation device, described three
Pass through pipeline UNICOM between level separator, the membrane treatment appts and the liquid phase mixing arrangement.
7. device according to claim 1 or 2, wherein the pH real-time monitoring devices are arranged on the liquid phase mixing arrangement
In.
8. device according to claim 1 or 2, including first flow control device and second flow control device,
And first flow control device is arranged between the liquid phase mixing arrangement and the membrane treatment appts, second flow control device
It is arranged between the hemicellulose liquid phase and the liquid phase mixing arrangement.
9. device according to claim 1 or 2, it further comprises alkali storage device, the alkali storage device with
The liquid phase mixing arrangement is connected by pipeline.
10. device according to claim 9, it further comprises the 3rd volume control device, and the 3rd flow control dress
Put and be arranged between the alkali storage device and the liquid phase mixing arrangement.
11. device according to claim 1 or 2, wherein the pH real-time monitoring devices are provided with calculator.
12. device according to claim 11, wherein the calculator electrically connects with the volume control device.
13. device according to claim 8, wherein the pH real-time monitoring devices are provided with calculator.
14. device according to claim 13, wherein the calculator electrically connects with second flow control device.
15. device according to claim 10, wherein the pH real-time monitoring devices are provided with calculator.
16. device according to claim 15, wherein the calculator electrically connects with the 3rd volume control device.
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