CN203820466U - Equipment for preparing activated carbon - Google Patents
Equipment for preparing activated carbon Download PDFInfo
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- CN203820466U CN203820466U CN201320869620.XU CN201320869620U CN203820466U CN 203820466 U CN203820466 U CN 203820466U CN 201320869620 U CN201320869620 U CN 201320869620U CN 203820466 U CN203820466 U CN 203820466U
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- discharge port
- feed
- opening
- carbonization
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title abstract description 36
- 239000000463 material Substances 0.000 claims abstract description 73
- 239000003054 catalyst Substances 0.000 claims abstract description 53
- 238000002156 mixing Methods 0.000 claims abstract description 51
- 239000002699 waste material Substances 0.000 claims abstract description 47
- 238000011084 recovery Methods 0.000 claims description 41
- 238000001035 drying Methods 0.000 claims description 39
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 239000003610 charcoal Substances 0.000 claims description 32
- 238000009434 installation Methods 0.000 claims description 31
- 239000000203 mixture Substances 0.000 claims description 31
- 238000005406 washing Methods 0.000 claims description 27
- 238000004898 kneading Methods 0.000 claims description 14
- 238000000605 extraction Methods 0.000 claims description 9
- 238000001914 filtration Methods 0.000 claims description 9
- 238000002485 combustion reaction Methods 0.000 claims description 8
- 239000002994 raw material Substances 0.000 abstract description 19
- 230000008901 benefit Effects 0.000 abstract description 14
- 230000004913 activation Effects 0.000 abstract description 5
- 230000007613 environmental effect Effects 0.000 abstract description 5
- 239000002028 Biomass Substances 0.000 abstract description 4
- 229920002488 Hemicellulose Polymers 0.000 abstract description 4
- 238000004064 recycling Methods 0.000 abstract description 4
- 238000003763 carbonization Methods 0.000 abstract 2
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 90
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical group OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 46
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 23
- 239000002253 acid Substances 0.000 description 16
- 238000000034 method Methods 0.000 description 16
- 230000007062 hydrolysis Effects 0.000 description 14
- 238000006460 hydrolysis reaction Methods 0.000 description 14
- 240000008042 Zea mays Species 0.000 description 12
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 12
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 12
- 235000005822 corn Nutrition 0.000 description 12
- 125000000969 xylosyl group Chemical group C1([C@H](O)[C@@H](O)[C@H](O)CO1)* 0.000 description 12
- 229910052799 carbon Inorganic materials 0.000 description 11
- 239000000243 solution Substances 0.000 description 10
- 238000012360 testing method Methods 0.000 description 10
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 9
- 238000004519 manufacturing process Methods 0.000 description 9
- 239000007789 gas Substances 0.000 description 8
- 239000007788 liquid Substances 0.000 description 7
- 238000002360 preparation method Methods 0.000 description 7
- 239000003245 coal Substances 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- 238000011056 performance test Methods 0.000 description 6
- 239000007787 solid Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 5
- 241000196324 Embryophyta Species 0.000 description 4
- 150000001299 aldehydes Chemical class 0.000 description 4
- 238000007598 dipping method Methods 0.000 description 4
- 239000008187 granular material Substances 0.000 description 4
- 235000019580 granularity Nutrition 0.000 description 4
- 239000002893 slag Substances 0.000 description 4
- SRBFZHDQGSBBOR-LECHCGJUSA-N alpha-D-xylose Chemical compound O[C@@H]1CO[C@H](O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-LECHCGJUSA-N 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 238000002203 pretreatment Methods 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000010298 pulverizing process Methods 0.000 description 3
- 238000012216 screening Methods 0.000 description 3
- 239000007858 starting material Substances 0.000 description 3
- 239000002023 wood Substances 0.000 description 3
- 229960003487 xylose Drugs 0.000 description 3
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 2
- SRBFZHDQGSBBOR-QMKXCQHVSA-N alpha-L-arabinopyranose Chemical compound O[C@H]1CO[C@@H](O)[C@H](O)[C@H]1O SRBFZHDQGSBBOR-QMKXCQHVSA-N 0.000 description 2
- 239000003575 carbonaceous material Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 235000013305 food Nutrition 0.000 description 2
- 239000008103 glucose Substances 0.000 description 2
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 description 2
- 239000010931 gold Substances 0.000 description 2
- 229910052737 gold Inorganic materials 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000001788 irregular Effects 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000000725 suspension Substances 0.000 description 2
- 238000012546 transfer Methods 0.000 description 2
- 244000060011 Cocos nucifera Species 0.000 description 1
- 235000013162 Cocos nucifera Nutrition 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910019142 PO4 Inorganic materials 0.000 description 1
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 235000013361 beverage Nutrition 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 230000001877 deodorizing effect Effects 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- PXEDJBXQKAGXNJ-QTNFYWBSSA-L disodium L-glutamate Chemical compound [Na+].[Na+].[O-]C(=O)[C@@H](N)CCC([O-])=O PXEDJBXQKAGXNJ-QTNFYWBSSA-L 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 239000010903 husk Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000006210 lotion Substances 0.000 description 1
- 238000005259 measurement Methods 0.000 description 1
- 235000013923 monosodium glutamate Nutrition 0.000 description 1
- 229920000620 organic polymer Polymers 0.000 description 1
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 description 1
- 239000010452 phosphate Substances 0.000 description 1
- 229910052698 phosphorus Inorganic materials 0.000 description 1
- 239000011574 phosphorus Substances 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000007873 sieving Methods 0.000 description 1
- 238000004513 sizing Methods 0.000 description 1
- 229940073490 sodium glutamate Drugs 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 235000019587 texture Nutrition 0.000 description 1
- -1 timber Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Landscapes
- Processing Of Solid Wastes (AREA)
Abstract
The utility model provides equipment for preparing activated carbon. The equipment for preparing the activated carbon comprises a waste residue feeding device, a material mixing device, a catalyst feeding device and a carbonization and activation device, wherein a first feeding hole of the material mixing device is connected with a discharge hole of the waste residue feeding device; a discharge hole of the catalyst feeding device is connected with a second feeding hole of the material mixing device; a feeding hole of the carbonization and activation device is connected with a discharge hole of the material mixing device. Compared with the prior art, the equipment for preparing the activated carbon has the advantages that residue of biomass after hemicelluloses are extracted is taken as a raw material for preparing the activated carbon, and performance indicators of the prepared activated carbon are equivalent to those of an activated carbon market product in the prior art; by adopting the equipment for preparing the activated carbon, recycling of the residue is realized, and pollution of the residue to the environment is avoided, so that the equipment for preparing the activated carbon has high environmental value; besides, the equipment for preparing the activated carbon has great economic benefit when being adopted for preparing the activated carbon.
Description
Technical field
The utility model relates to carbon material technical field, relates in particular to a kind of equipment of preparing gac.
Background technology
Gac claims again active black, is black powder shape or granular decolorizing carbon.Gac principal constituent is gone back the elements such as aerobic, hydrogen except carbon.Gac is structurally irregular alignment due to microcrystalline carbon, has pore between cross connection, in activation, time can produce carbon tissue defects, so it is a kind of porous carbon, and tap density is low, and specific surface area is large.And in the carbon granule of gac, also has more tiny hole---kapillary.This kapillary has very strong adsorptive power, because the surface-area of carbon granule is very large, so can fully contact with gas (impurity).When these gases (impurity), encounter kapillary and be adsorbed, aseptic.Due to the good absorption system energy of gac, it is widely used in the prior art, as being mainly used in alkali-free sweetening, ethene de-salted water, support of the catalyst and water in petrochemical industry, purifies and sewage disposal; In power industry, be mainly used in power plant's water quality treatment agent protection; In chemical industry, be mainly used in the decolouring, standing of chemical catalyst and carrier, gas sweetening, solvent recuperation and grease etc.; Food service industry is mainly used in refining, decolouring, purification and the deodorizing of beverage, drinks, sodium glutamate mother liquid and food; At gold industry, mainly as gold, extract and tail washings recovery; At environmental protection industry (epi), be mainly used in improvement, the gas sweetening of sewage disposal, waste gas and obnoxious flavour.
According to manufacture method, gac can be divided into active carbon by chemical method, Physical gac, chemistry-Physical and physics-active carbon by chemical method.Main application is that chemical method is prepared gac at present, and the main raw material of gac can be almost all organic materialss that are rich in carbon, as coal, timber, shell, coconut husk, nut-shell etc.These carbonaceous materials, in activation furnace, are converted into gac by pyrolysis under high temperature and certain pressure.This method of preparing gac of prior art has higher Financial cost, and raw material as this in coal has non-renewablely, is unfavorable for the Sustainable development of technique.
Utility model content
The purpose of this utility model is to provide a kind of equipment of preparing gac, and the equipment that adopts the utility model to provide is prepared gac, can produce huge economic benefit.
The utility model provides a kind of equipment of preparing gac, comprises waste residue feeding unit;
The material mixing device that the first opening for feed is connected with described waste residue feeding unit discharge port;
The catalyst charge device that discharge port is connected with the second opening for feed of described material mixing device;
The carbonization-activation device that opening for feed is connected with the discharge port of described material mixing device.
Preferably, described waste residue feeding unit comprises waste residue storing unit;
The first drying installation that opening for feed is connected with the discharge port of described waste residue storing unit;
The filtration unit that opening for feed is connected with described the first drying installation discharge port.
Preferably, described filtration unit comprises shredding unit and filter sieve;
Described filter sieve is that aperture is 6 order～16 object double deck screens.
Preferably, also comprise the catalyst recovery devices that opening for feed is connected with the discharge port of described carbonization-activation device, the first discharge port of described catalyst recovery devices is connected with the 3rd opening for feed of described material mixing device;
The water washing device that opening for feed is connected with the second discharge port of described catalyst recovery devices;
The second drying installation that opening for feed is connected with described water washing device discharge port;
The shredding unit that opening for feed is connected with described the second drying installation discharge port.
Preferably, described catalyst recovery devices is pulsed extraction tower, filter or whizzer.
Preferably, described shredding unit comprises the pulverizer that opening for feed is connected with described the second drying installation discharge port;
The separator that opening for feed is connected with described pulverizer discharge port;
The collector that opening for feed is connected with described separator discharge port.
Preferably, described mixtures of materials device comprises measuring apparatus and material kneading unit;
The first opening for feed of described measuring apparatus is connected with the discharge port of described waste residue feeding unit;
The second opening for feed of described measuring apparatus is connected with the discharge port of described catalyst charge device;
The discharge port of described measuring apparatus is connected with the opening for feed of described material kneading unit;
The discharge port of described material kneading unit is connected with the opening for feed of described carbonization-activation device.
Preferably, described carbonization-activation device is obliquely installed horizontal by angle, and the discharge port of described carbonization-activation device is positioned at the bottom of described carbonization-activation device opening for feed, and the discharge port place of described carbonization-activation device is provided with combustion chamber;
The mixture being transported by described material mixing device is delivered to the opening for feed place of described carbonization-activation device, and described mixture is moved to described discharge port by described opening for feed along the angle of described inclination;
Heat-carrying gas and described mixture counter current contact that described combustion chamber produces.
Preferably, between described material mixing device and described carbonization-activation device, be provided with mixture e Foerderanlage;
Described mixture e Foerderanlage comprises feeder and feeder;
The opening for feed of described feeder is connected with the discharge port of described mixture e Foerderanlage;
The discharge port of described feeding machine is connected with the opening for feed of described feeder;
The discharge port of described feeder is connected with the opening for feed of described carbonization-activation device.
Preferably, described water washing device comprises charcoal pond;
The opening for feed in described charcoal pond is connected with the second discharge port of described catalyst recovery devices;
The discharge port in described charcoal pond is connected with described the second drying installation.
The utility model provides a kind of equipment of preparing gac, comprises waste residue feeding unit; The material mixing device that the first opening for feed is connected with described waste residue feeding unit discharge port; The catalyst charge device that discharge port is connected with the second opening for feed of described material mixing device; The carbonization-activation device that opening for feed is connected with the discharge port of described material mixing device.Compared with prior art, the equipment that the utility model provides can be take biomass, and to have extracted the residue after hemicellulose be raw material, prepare gac, and the performance index of the performance index of the gac obtaining and prior art gac commercial goods are suitable, the equipment that adopts the utility model to provide is prepared gac and has been realized the recycling to these residues, avoid the pollution of these residues to environment, there is the higher value of environmental protection.And, the equipment that adopts the utility model to provide carries out the preparation of gac, there is huge economic benefit, take that to prepare 1 ton of furfural be example, prior art is prepared after 1 ton of furfural, remaining furfural dregs, without any economic benefit, adopts the equipment coproduction simultaneously that the utility model provides to obtain 3 tons of gacs, produces the benefit of 3 tons of extra gacs; And prior art is prepared the producer of gac and be take wood chip, coal or shell as raw material, cost is at 2000 yuan/ton of gacs, and the utility model is that to adopt discarded furfural dregs or xylose residue be raw material, there is no raw materials cost, has also brought the benefit of gac.
Accompanying drawing explanation
The structural representation of preparing activated-carbon device that Fig. 1 provides for the utility model embodiment.
Embodiment
The utility model provides a kind of equipment of preparing gac, comprises waste residue feeding unit;
The material mixing device that the first opening for feed is connected with described waste residue feeding unit discharge port;
The catalyst charge device that discharge port is connected with the second opening for feed of described material mixing device;
The carbonization-activation device that opening for feed is connected with the discharge port of described material mixing device.
The residue that the equipment of preparing gac that the utility model provides be take after biomass material extraction hemicellulose is raw material, prepares gac.The equipment that adopts the utility model to provide is prepared gac, has realized comprising the recycling of xylogen and cellulosic waste residue, as furfural dregs and/or xylose residue, and greatly reduces the cost of producing gac, has huge economic benefit.
The equipment of preparing gac that the utility model provides comprises waste residue feeding unit, and described waste residue feeding unit, for the waste residue described in technique scheme is delivered to material mixing device, mixes with catalyzer.In embodiment of the present utility model, for described waste residue is dried and is pulverized, described waste residue feeding unit can comprise waste residue storing unit; The first drying installation that opening for feed is connected with the discharge port of described waste residue storing unit; The filtration unit that opening for feed is connected with described the first drying installation discharge port.In embodiment of the present utility model, described waste residue storing unit is stored for the production of the furfural dregs obtaining and/or xylose residue; The outlet of described waste residue storing unit is connected with the opening for feed of described the first drying installation, by the drying materials transporting from described waste residue storing unit; The discharge port of described the first drying installation is connected with the opening for feed of described filtration unit, in embodiment of the present utility model, described filtration unit preferably includes shredding unit and filter sieve, the material transporting from described the first drying installation is pulverized described shredding unit, then be transported to filter sieve place and screen, obtain the waste particle of release mesh described in technique scheme.In embodiment of the present utility model, described filter sieve can be 6 order～16 order double deck screens for aperture, and in other embodiment of the utility model, described filter sieve can also be 10 order～15 object double deck screens for aperture.
The equipment of preparing gac that the utility model provides comprises catalyst charge device, the discharge port of described catalyst charge device is connected with the second opening for feed of described mixing of materials, in order to by catalyst transport to material mixing device, mix with waste particle.
The preparation that the utility model provides or the device of gac comprise material mixing device, the first opening for feed of described material mixing device is connected with the discharge port of described waste residue feeding unit, and the second opening for feed of described material mixing device is connected with the discharge port of described catalyst charge device.The do not have special restriction of the utility model to described material mixing device, as adopted material kneading unit well known to those skilled in the art, kneads described waste residue and catalyzer.
Concrete, in embodiment of the present utility model, amount for material and catalyzer in strict measurement input material kneading unit, described material mixing device can also comprise measuring apparatus, the first opening for feed of described measuring apparatus is connected with the discharge port of described waste residue feeding unit, concrete, be connected with the discharge port of described filtration unit; The second opening for feed of described measuring apparatus is connected with the discharge port of described catalyst charge device, and the discharge port of described measuring apparatus is connected with the opening for feed of described material kneading unit.In embodiment of the present utility model, preferably first waste residue is delivered in described measuring apparatus, then adds catalyzer in described measuring apparatus, after mixing, be delivered in material kneading unit and knead, obtain mixture.
The equipment of preparing gac that the utility model provides comprises carbonization-activation device, and the opening for feed of described carbonization-activation device is connected with the discharge port of described material mixing device, and the concrete discharge port with material kneading unit described in technique scheme is connected.In embodiment of the present utility model, between described material mixing device and described carbonization-activation device, be provided with mixture e Foerderanlage, described mixture e Foerderanlage specifically comprises feeder and feeder, the opening for feed of described feeder is connected with the discharge port of described mixture device, the discharge port of described feeder is connected with the opening for feed of described feeder, and the discharge port of described feeder is connected with the opening for feed of described carbonization-activation device.The utility model does not have special restriction to the type of described feeder and feeder, in an embodiment, can specifically adopt dise feeder and feed screw, and the utility model is not done special restriction.
In embodiment in the utility model, described carbonization-activation device is obliquely installed horizontal by angle, the discharge port of described carbonization-activation device is positioned at the bottom of described carbonization-activation device opening for feed, and the discharge port place of described carbonization-activation device is provided with combustion chamber; The mixture being transported by described material mixing device is delivered to the opening for feed place of described carbonization-activation device, and described mixture is moved to described discharge port by described opening for feed along the angle of described inclination; Heat-carrying gas and described mixture counter current contact that described combustion chamber produces.In embodiment of the present utility model, the angle of described carbonization-activation device and horizontal plane can be 3 ° of left and right, those skilled in the art can install the angle of inclination of described carbonization-activation device according to actual production process, and the utility model does not have special restriction to this.The utility model does not have special restriction to the kind of described carbonization-activation device, adopts the carbonization-activation stove adopting in gac scheme of preparing well known to those skilled in the art, as adopted internal-heated rotary furnace.In embodiment of the present utility model, described mixture e Foerderanlage is delivered to mixture on the stove tail of internal-heated rotary furnace, mixture slowly moves to burner by rotation and the obliquity of body of heater, described burner goes out to be provided with combustion chamber, coal-fired burning in described combustion chamber produces heat-carrying gas, described heat-carrying gas enters in stove, directly and mixture counter current contact, make mixture move to burner experience from stove tail dry, fibrous texture dehydration, material charing, a plurality of stages such as organic polymer decomposition and vesicular structure sizing, finally enter the discharge chamber of burner.
In embodiment of the present utility model, the described equipment of preparing gac also comprises the catalyst recovery devices that opening for feed is connected with the discharge port of described carbonization-activation device, and the first discharge port of described catalyst recovery devices is connected with the 3rd opening for feed of described material mixing device;
The water washing device that opening for feed is connected with the second discharge port of described catalyst recovery devices;
The second drying installation that opening for feed is connected with described water washing device discharge port;
The shredding unit that opening for feed is connected with described the second drying installation discharge port.
The equipment of preparing gac that the utility model provides also comprises catalyst recovery devices, when described catalyzer is phosphoric acid, this catalyst recovery devices is carried out catalyst recovery by the discharging of described carbonization-activation device, the catalyzer that recovery obtains can be transported to described material mixing device, continues on for the preparation of gac.In the utility model, described catalyst recovery devices is preferably acid-restoring plant.In the utility model, the opening for feed of described catalyst recovery devices is connected with the discharge port of described carbonization-activation device, the first discharge port of described catalyst recovery devices is connected with the 3rd opening for feed of described material mixing device, the second discharge port of described catalyst recovery devices is connected with the opening for feed of described water washing device, and the second discharge port of described catalyst recovery devices is washed in order to the charcoal after recovered acid is delivered to water washing device.The utility model does not have special restriction to the kind of described catalyst recovery devices, adopts catalyst recovery devices well known to those skilled in the art, as can pulsed extraction tower well known to those skilled in the art, filter or whizzer.
In embodiment of the present utility model, when described catalyst recovery devices is pulsed extraction tower, when described catalyzer is phosphoric acid, described catalyst recovery is acid recovery, and the detailed process of described acid recovery is as follows:
First in described pulsed extraction tower, inject the phosphoric acid liquid of low concentration, then with electric block, described activated material is promoted in impouring tower; Complete reinforced after, starting impulse producer, makes solid-liquid two-phase do turbulent motion, improves organic efficiency.In the utility model, the mass concentration of the phosphoric acid liquid of described low concentration is preferably 20Be～30Be.The phosphoric acid reclaiming for the first time, can be sent to burden process standby; Then successively the phosphoric acid of lower concentration is squeezed into extraction tower with pump, repeat above operation.The phosphoric acid from high density to lower concentration tool concentration gradient being recovered to stores respectively sour pond, for reclaiming next time.When the phosphoric acid concentration of extraction tower discharge reaches 0 ° of Be, then extract respectively secondary with the hot clear water that temperature is 60 ℃～80 ℃, extraction liquid returns to sour pond.
In embodiment of the present utility model, when described catalyst recovery devices is filter, the utility model is preferably placed in described filter by described activated material and filters, and catalyst solution wherein is separated with activated material solid, realizes the recovery to catalyzer.The utility model does not have special restriction to the kind of described filter, adopts filter well known to those skilled in the art, as adopted flame filter press conventional in gac industrial production.
In embodiment of the present utility model, when described catalyst recovery devices is whizzer, the utility model is preferably placed in described activated material described whizzer and carries out centrifugally, makes catalyst solution wherein separated with activated material solid, realizes the recovery to catalyzer.The utility model does not have special restriction to the working conditions of the kind of described whizzer and whizzer, adopts whizzer well known to those skilled in the art.
In embodiment of the present utility model, the described equipment of preparing gac can also comprise water washing device, and the opening for feed of described water washing device is connected with the second discharge port of described catalyst recovery devices.In embodiment of the present utility model, described water washing device can comprise charcoal pond, in described charcoal pond, the activated material reclaiming after catalyzer is carried out to rinsing, concrete, described activated material is after flame filter press filters, and charcoal is stayed in sheet frame, to injected water in described sheet frame, charcoal is wherein washed; In the other embodiment of the utility model, described water washing device can also comprise rinsing narrow-necked earthen jar, and the opening for feed in described charcoal pond is connected with the second discharge port of described catalyst recovery devices, and the discharge port in described charcoal pond is connected with the opening for feed of described rinsing narrow-necked earthen jar.In embodiment of the present utility model, the charcoal of described catalyst recovery devices the second discharge port output is poured in water in charcoal pond, and the charcoal in described charcoal pond is delivered in rinsing narrow-necked earthen jar by slush pump, water by the charcoal stream in described rinsing narrow-necked earthen jar float to pH value be 4～5.
In embodiment of the present utility model, the described equipment of preparing gac can also comprise the second drying installation, and described the second drying installation is in order to be dried the charcoal after washing, and the opening for feed of described the second drying installation is connected with the discharge port of described water washing device.In embodiment of the present utility model, described the second drying installation can comprise dewatering unit and fluidised bed drying stove, the opening for feed of described dewatering unit is connected with the discharge port of described water washing device, the discharge port of described dewatering unit is connected with the opening for feed of described fluidised bed drying stove, between described dewatering unit and described fluidised bed drying stove, be provided with spiral conveyer, described spiral conveyer is sent into the wet charcoal obtaining through dewatering unit in fluidised bed drying stove.The utility model passes into high-temperature hot-air in described fluidised bed drying stove, makes charcoal in fluidized state, dry rapidly, obtains dry charcoal.In embodiment of the present utility model, the temperature of described high-temperature hot-air can be 80 ℃～200 ℃, and in the other embodiment of the utility model, the temperature of described high-temperature hot-air can also be 100 ℃～180 ℃.
In embodiment of the present utility model, described the second drying installation can also comprise tripping device and collection device, the opening for feed of described tripping device is connected with the discharge port of described fluidised bed drying stove, and the discharge port of described tripping device is connected with the opening for feed of described collection device.Concrete, described tripping device can be cyclonic separator, and described collection device can be bag filter, and described dry charcoal is collected by cyclonic separator and bag filter.
In embodiment of the present utility model, the described equipment of preparing gac can also comprise shredding unit, and described shredding unit, in order to the dry charcoal obtaining is pulverized, obtains the commercial goods of gac.Concrete, the opening for feed of described shredding unit is connected with the discharge port of described the second drying installation.In embodiment of the present utility model, described shredding unit can comprise the pulverizer that opening for feed is connected with described the second drying installation discharge port;
The separator that opening for feed is connected with described pulverizer discharge port;
The collector that opening for feed is connected with described separator discharge port.
The utility model does not have special restriction to the kind of described pulverizer, adopts pulverizer well known to those skilled in the art, and as adopted Raymond mill, the dry charcoal by described pulverizer is crushed to and is less than 200 object granularities.In embodiment of the present utility model, described separator can be cyclonic separator, and described collector can be bag filter, and the dry charcoal after described pulverizing is collected through cyclonic separator and bag filter.
For the gac obtaining being sold as commercial goods, the utility model is packed the gac obtaining after pulverizing, in embodiment of the present utility model, the described equipment of preparing gac can also comprise hybrid packed device, the opening for feed of described hybrid packed device is connected with the discharge port of described shredding unit, concrete described hybrid packed device can comprise mixing tank and packing plant, the opening for feed of described mixing tank is connected with the discharge port of described shredding unit, the discharge port of described mixing tank is connected with the opening for feed of described packing plant, described mixing tank has the performance of irregular rotation, its capacity can meet the quantity of a batch products.
Referring to Fig. 1, the structural representation of the equipment of preparing gac that Fig. 1 provides for the utility model embodiment.
Below in conjunction with the device shown in Fig. 1, the workflow of the equipment of preparing gac that the utility model is provided is set forth:
The utility model stores in waste residue storing unit preparing furfural dregs and/or the xylose residue that furfural or wood sugar obtain, and the waste residue in waste residue storing unit is delivered in the first drying installation and is dried, and obtains the waste residue of weight water content below 20wt%; By described weight water content, the waste residue below 20wt% is delivered in filtration unit and pulverizes and screen again, must be 6 order～16 object waste particle; By described waste particle, the first opening for feed by material mixing device is delivered in material mixing device again, by catalyzer, from described catalyst charge device, the second opening for feed by material mixing device is delivered to material mixing device again, waste particle is mixed with catalyzer, obtain mixture; Again the mixture obtaining is delivered to carbonization-activation device and carries out carbonization-activation, obtain activating charcoal; Then described activation charcoal is delivered in catalyst recovery devices and carries out catalyst recovery, be specially acid solution and reclaim, the catalyzer being recovered to is delivered in material mixing device by the 3rd opening for feed of material mixing device, continues on for the preparation of gac; Charcoal after recovery catalyzer is delivered to water washing device by catalyst recovery devices and washes, and making its pH value is 4～5; Then by the pH obtaining most 4～5 charcoal be delivered to the second drying installation and be dried, obtain weight water content at the charcoal below 10%; Again described weight water content is delivered to shredding unit at the charcoal below 10% and pulverizes, obtain granularity and be less than 200 object charcoals.In order to obtain the commercial goods of gac, the granularity that the utility model obtains described shredding unit is less than 200 object charcoals and is delivered to that hybrid packed device mixes and packing is dispatched from the factory.
The utility model provides a kind of equipment of preparing gac, comprises waste residue feeding unit; The material mixing device that the first opening for feed is connected with described waste residue feeding unit discharge port; The catalyst charge device that discharge port is connected with the second opening for feed of described material mixing device; The carbonization-activation device that opening for feed is connected with the discharge port of described material mixing device.Compared with prior art, the equipment that the utility model provides can be take biomass, and to have extracted the residue after hemicellulose be raw material, prepare gac, and the performance index of the performance index of the gac obtaining and prior art gac commercial goods are suitable, the equipment that adopts the utility model to provide is prepared gac and has been realized the recycling to these residues, avoid the pollution of these residues to environment, there is the higher value of environmental protection.And, the equipment that adopts the utility model to provide carries out the preparation of gac, there is huge economic benefit, take that to prepare 1 ton of furfural be example, prior art is prepared after 1 ton of furfural, remaining furfural dregs, without any economic benefit, adopts the equipment coproduction simultaneously that the utility model provides to obtain 3 tons of gacs, produces the benefit of 3 tons of extra gacs; And prior art is prepared the producer of gac and be take wood chip, coal or shell as raw material, cost is at 2000 yuan/ton of gacs, and the utility model is that to adopt discarded furfural dregs or xylose residue be raw material, there is no raw materials cost, has also brought the benefit of gac.
In order to further illustrate the utility model, the workflow of the equipment of preparing gac the utility model being provided below in conjunction with embodiment is described in detail, but they can not be interpreted as to the restriction to the utility model protection domain.
In following embodiment 5～8, adopt the equipment of structure shown in Fig. 1 to carry out the preparation of gac.
Embodiment 1
Corn cob after raw material use is air-dry, its water-content is 15%.Corn cob is ground into the corn cob granule of 1～1.5cm after vibratory screening apparatus dedusting with beater grinder, then by lift, be transported to mix in sour car and mix acid, acid is dense 5% ± 2%, the solid-to-liquid ratio of the suspension obtaining with the maintenance of acid amount is 1:0.3, through rotary conveyor, sends in hydrolysis kettle, and hydrolysis kettle volume is 10 cubic metres, adopt two still serial operations, after filling hydrolysis kettle, pass into the water vapor that pressure is 0.50MPa ± 0.05MPa, hydrolysis temperature is 145 ℃, is hydrolyzed 4 hours.The furfural stoste that hydrolysis is obtained is introduced subsequent handling, and through extracting hair aldehyde, hair aldehyde continuous fine makes commodity furfural.Furfural dregs in still enters slag field, standby.
Embodiment 2
Corn cob after raw material use is air-dry, its water-content is 10%.Corn cob is ground into the corn cob granule of 1～1.5cm after vibratory screening apparatus dedusting with beater grinder, then by lift, be transported to mix in sour car and mix acid, acid is dense 8% ± 2%, the solid-to-liquid ratio of the suspension obtaining with the maintenance of acid amount is 1:0.5, through rotary conveyor, sends in hydrolysis kettle, and hydrolysis kettle volume is 10 cubic metres, adopt two still serial operations, after filling hydrolysis kettle, pass into the water vapor that pressure is 0.70MPa ± 0.05MPa, hydrolysis temperature is 180 ℃, is hydrolyzed 2 hours.The furfural stoste that hydrolysis is obtained is introduced subsequent handling, and through extracting hair aldehyde, hair aldehyde continuous fine makes commodity furfural.Furfural dregs in still enters slag field, standby.
Embodiment 3
(1) material loading of raw material and pre-treatment:
Corn cob is sent in the receiving hopper of workshop charging belt, after by belt, deliver to after screening out a part of silt and chip on vibrosieve transfer roller and enter washing machine.Corn cob washing machine should regularly be removed the silt in its sand deposition hopper.After washing, corn cob enters chapelet or high spud angle band rib rotary conveyor after dewatering by vibrating-dewatering screen, then be raised on the horizontal belt transfer roller that is transported to hydrolyzer top, then send in the hydrolyzer that needs charging by distributing plate to control through chute.
(2) hydrolysis:
In being hydrolyzed, first, to the corn cob pre-treatment that is hydrolyzed, corn cob is immersed in the sulphuric acid soln that mass concentration is 0.1wt% ± 2wt%, at 110 ℃, process 3 hours;
Corn cob is after dilute acid pretreatment, and the acid solution of draining, is the aqueous sulfuric acid of 0.6wt% ± 1wt% to adding mass concentration in hydrolyzer again, and logical steam is warmed up to 128 ℃ wherein, and insulation 2.5h, completes hydrolysis.
Be hydrolyzed hydrolyzed solution is discharged and collected, washing waste residue, then opens residual cake valve residue is entered to slag field, standby.The hydrolyzed solution chief component of collecting is as follows: wood sugar: 3～5%wt, and pectinose: 0.4～0.65%wt, glucose: 0.4～0.65%wt, semi-lactosi: 0.1～0.2%wt, sugared concentration is generally at 5～8%wt.
Embodiment 4
Adopt the technical scheme of embodiment 3 to prepare hydrolyzed solution and xylose residue, different, the acid solution that the present embodiment hydrolysis pre-treatment adopts is that mass concentration is the phosphate aqueous solution of 0.15wt%, and pretreated temperature is 130 ℃, and the pretreated time is 1h; The acid solution that hydrolysis treatment adopts is that mass concentration is 1% sulfuric acid, and the temperature of steam is 132 ℃.
The chief component of the hydrolyzed solution of collecting is: wood sugar: 3～5%wt, and pectinose: 0.3～0.55%wt, glucose: 0.45～0.65%wt, semi-lactosi: 0.15～0.3%wt, sugared concentration is generally at 5～8%wt.
Embodiment 5
The furfural dregs that the embodiment 1 being stored in waste residue storing unit is obtained is delivered to the first drying installation and is dried, and obtains weight water content and be 15% furfural dregs; And then the first drying installation is obtained to mass transport to pulverizing and cross 6 orders in filter plant and 16 object double deck screens screen, the furfural dregs particle 100kg sieving is delivered in material mixing device, it is that 60% phosphoric acid 255kg mixes that the ratio that is 1:1.8 according to over dry acidolysis slag ratio pure phosphoric acid mass ratio again adds mass concentration wherein, under normal temperature state, mediate dipping 20min, then impregnant is coiled to the stove tail that feeder and feed screw are sent into carbonization-activation stove by garden, at 480 ℃, activate 60min.The activated material obtaining is taken out to the cooling rear suitable quantity of water drip washing of using, and washing lotion separately puts to reclaim phosphoric acid.Then being delivered to of solid after drip washing is washed till to pH value in water washing device and is washed till 4 left and right, then in the second drying installation, dry successively to weight water content and be less than 200 orders being crushed to granularity below 10%, in shredding unit, obtain finished product gac.
The utility model adopts the scheme of the test Properties of Activated Carbon of recording in GB/T12496-1999, and the finished product gac obtaining is carried out to performance test, and result is as shown in table 1, the performance test results of the gac that table 1 obtains for the utility model embodiment.
Embodiment 6
Adopt the technical scheme of embodiment 5 to prepare finished product gac, different is, the furfural dregs that the embodiment 2 that the present embodiment adopts obtains, the solid content of furfural dregs is 40%, furfural dregs oven dry weight and pure phosphoric acid mass ratio are 1:3.0, and the mass concentration of phosphoric acid is 50%, and the time of the dipping of kneading is 15min, the temperature of carbonization-activation is 450 ℃, and the time of carbonization-activation is 90min.
The utility model adopts the testing method described in embodiment 5 to test the performance of the gac obtaining, and test result is as shown in table 1, the performance test results that table 1 obtains for the utility model embodiment 5～8.
Embodiment 7
Adopt the technical scheme of embodiment 5 to prepare finished product gac, different is, the xylose residue that the present embodiment adopts embodiment 3 to obtain, the solid content of xylose residue is 65%, the mass ratio of xylose residue oven dry weight and pure phosphoric acid is 1:1.5, and the mass concentration of phosphoric acid is 65%, and the time of the dipping of kneading is 18min, the temperature of carbonization-activation is 500 ℃, and the time of carbonization-activation is 40min.
The utility model adopts the testing method described in embodiment 5 to test the performance of the gac obtaining, and test result is as shown in table 1, the performance test results that table 1 obtains for the utility model embodiment 5～8.
Embodiment 8
Adopt the technical scheme of embodiment 5 to prepare finished product gac, different is, the xylose residue that the present embodiment adopts embodiment 4 to obtain, the solid content of xylose residue is 70%, the mass ratio of xylose residue oven dry weight and pure phosphoric acid is 1:1.2, and the mass concentration of phosphoric acid is 70%, and the time of the dipping of kneading is 10min, the temperature of carbonization-activation is 460 ℃, and the time of carbonization-activation is 70min.
The utility model adopts the testing method described in embodiment 5 to test the performance of the gac obtaining, and test result is as shown in table 1, the performance test results that table 1 obtains for the utility model embodiment 5～8.
The performance test results of the gac that table 1 the utility model embodiment 5～8 obtains
As can be seen from Table 1, it is suitable with the performance index of the gac that art methods obtains that the method that the utility model provides obtains the performance index of gac, and the gac that can substitute prior art is completely sold as commercial goods.
The equipment that the utility model provides is prepared gac and is had huge economical effectiveness:
Take that to prepare 1 ton of furfural be example, prior art is prepared after 1 ton of furfural, and remaining furfural dregs is without any economic benefit, and undressed furfural dregs can not arbitrarily discharge in order to avoid contaminate environment.The equipment that the utility model provides is prepared gac, can utilize efficiently furfural dregs to improve the recycle value of furfural dregs, has avoided the pollution of direct discharge furfural dregs to environment, has the higher value of environmental protection; Produce 1 ton of furfural, can produce the furfural dregs of 10 tons of left and right, the equipment that the utility model provides adopts 10 tons of furfural dregs at least can prepare 3 tons of gacs.
The phosphoric acid adding while preparing furfural almost all remains in furfural dregs, can give tacit consent to almost not loss.When the equipment that adopts the utility model to provide is prepared gac, can reduce the phosphoric acid amount of adding afterwards according to the phosphorus acid content in furfural dregs.The all phosphoric acid adding is recovered in later stage acid recovery process, and the phosphoric acid amount of gac consumption per ton is about 250kg～300kg; Yet in the furfural preparation of traditional technology, the catalyzer of use is sulfuric acid, but sulfuric acid can not reuse; Existing technique is to take phosphoric acid as catalyzer, but phosphoric acid reuse.So existing technique can be thought not spent catalyst, saved the cost of catalyzer, approximately 300 yuan/ton.
And prior art is prepared the producer of gac and be take wood chip, coal or shell as raw material, cost is at 2000 yuan/ton of gacs, and the equipment that the utility model provides to prepare gac be that to adopt discarded furfural dregs be raw material, there is no raw materials cost.The production cost of gac can reduce by 2000 yuan/ton.
During furfural production, can produce a large amount of exhaust steam, used heat, this part steam cannot store can only be emptying.And the equipment providing with the utility model is while preparing gac, need to be dried starting material and the gac of having washed.The exhaust steam of furfural just in time can be used to dry starting material and finished product.The reasonable utilization of exhaust steam, has reduced the production cost of gac effectively.It is 20% that the furfural dregs that 1 ton of water ratio is 70% is dried to water ratio, needs to consume the standard coal of 0.2 ton.Producing 1 ton of gac needs the furfural dregs of 2.5 tons of water ratio 20%, so need to dry the furfural dregs of 8 tons of water ratio 70%, produces 1 ton of gac and need consume 1.5 tons of coals oven dry starting material.And the exhaust steam, the used heat that produce during by furfural production collect effective utilization, can replace drying raw-material 1.5 tons of coals, can reduce significantly like this production cost of gac.
From the analysis of above three aspects, the equipment that the utility model provides is prepared gac can save a large amount of production costs, and has huge economic benefit.
The above is only preferred implementation of the present utility model; it should be pointed out that for those skilled in the art, do not departing under the prerequisite of the utility model principle; can also make some improvements and modifications, these improvements and modifications also should be considered as protection domain of the present utility model.
Claims (10)
1. an equipment of preparing gac, comprises waste residue feeding unit;
The material mixing device that the first opening for feed is connected with described waste residue feeding unit discharge port;
The catalyst charge device that discharge port is connected with the second opening for feed of described material mixing device;
The carbonization-activation device that opening for feed is connected with the discharge port of described material mixing device.
2. equipment according to claim 1, is characterized in that, described waste residue feeding unit comprises waste residue storing unit;
The first drying installation that opening for feed is connected with the discharge port of described waste residue storing unit;
The filtration unit that opening for feed is connected with described the first drying installation discharge port.
3. equipment according to claim 2, is characterized in that, described filtration unit comprises shredding unit and filter sieve;
Described filter sieve is that aperture is 6 order～16 object double deck screens.
4. equipment according to claim 1, it is characterized in that, also comprise the catalyst recovery devices that opening for feed is connected with the discharge port of described carbonization-activation device, the first discharge port of described catalyst recovery devices is connected with the 3rd opening for feed of described material mixing device;
The water washing device that opening for feed is connected with the second discharge port of described catalyst recovery devices;
The second drying installation that opening for feed is connected with described water washing device discharge port;
The shredding unit that opening for feed is connected with described the second drying installation discharge port.
5. equipment according to claim 4, is characterized in that, described catalyst recovery devices is pulsed extraction tower, filter or whizzer.
6. equipment according to claim 4, is characterized in that, described shredding unit comprises the pulverizer that opening for feed is connected with described the second drying installation discharge port;
The separator that opening for feed is connected with described pulverizer discharge port;
The collector that opening for feed is connected with described separator discharge port.
7. equipment according to claim 1, is characterized in that, described mixtures of materials device comprises measuring apparatus and material kneading unit;
The first opening for feed of described measuring apparatus is connected with the discharge port of described waste residue feeding unit;
The second opening for feed of described measuring apparatus is connected with the discharge port of described catalyst charge device;
The discharge port of described measuring apparatus is connected with the opening for feed of described material kneading unit;
The discharge port of described material kneading unit is connected with the opening for feed of described carbonization-activation device.
8. equipment according to claim 1, it is characterized in that, described carbonization-activation device is obliquely installed horizontal by angle, and the discharge port of described carbonization-activation device is positioned at the bottom of described carbonization-activation device opening for feed, and the discharge port place of described carbonization-activation device is provided with combustion chamber;
The mixture being transported by described material mixing device is delivered to the opening for feed place of described carbonization-activation device, and described mixture is moved to described discharge port by described opening for feed along the angle of described inclination;
Heat-carrying gas and described mixture counter current contact that described combustion chamber produces.
9. equipment according to claim 1, is characterized in that, between described material mixing device and described carbonization-activation device, is provided with mixture e Foerderanlage;
Described mixture e Foerderanlage comprises feeder and feeder;
The opening for feed of described feeder is connected with the discharge port of described mixture e Foerderanlage;
The discharge port of described feeding machine is connected with the opening for feed of described feeder;
The discharge port of described feeder is connected with the opening for feed of described carbonization-activation device.
10. equipment according to claim 4, is characterized in that, described water washing device comprises charcoal pond;
The opening for feed in described charcoal pond is connected with the second discharge port of described catalyst recovery devices;
The discharge port in described charcoal pond is connected with described the second drying installation.
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| CN201320869620.XU CN203820466U (en) | 2013-12-26 | 2013-12-26 | Equipment for preparing activated carbon |
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| CN201320869620.XU CN203820466U (en) | 2013-12-26 | 2013-12-26 | Equipment for preparing activated carbon |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104528719A (en) * | 2014-12-17 | 2015-04-22 | 中国林业科学研究院林产化学工业研究所 | Method for preparing activated carbon by using alkali xylose residues as raw material |
| CN104743554A (en) * | 2013-12-26 | 2015-07-01 | 济南圣泉集团股份有限公司 | Active carbon preparation method and device |
-
2013
- 2013-12-26 CN CN201320869620.XU patent/CN203820466U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104743554A (en) * | 2013-12-26 | 2015-07-01 | 济南圣泉集团股份有限公司 | Active carbon preparation method and device |
| CN104528719A (en) * | 2014-12-17 | 2015-04-22 | 中国林业科学研究院林产化学工业研究所 | Method for preparing activated carbon by using alkali xylose residues as raw material |
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