CN109337726B - A kind of lignite process equipment - Google Patents
A kind of lignite process equipment Download PDFInfo
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- CN109337726B CN109337726B CN201810970455.4A CN201810970455A CN109337726B CN 109337726 B CN109337726 B CN 109337726B CN 201810970455 A CN201810970455 A CN 201810970455A CN 109337726 B CN109337726 B CN 109337726B
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- lignite
- processing system
- alkali pool
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- 238000000034 method Methods 0.000 title claims abstract description 85
- 239000003077 lignite Substances 0.000 title claims abstract description 70
- 238000012545 processing Methods 0.000 claims abstract description 108
- 239000003513 alkali Substances 0.000 claims abstract description 89
- 239000002253 acid Substances 0.000 claims abstract description 78
- 239000007788 liquid Substances 0.000 claims abstract description 45
- 229910052782 aluminium Inorganic materials 0.000 claims abstract description 37
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000004411 aluminium Substances 0.000 claims abstract description 34
- 239000012530 fluid Substances 0.000 claims description 38
- 238000003756 stirring Methods 0.000 claims description 20
- 238000002156 mixing Methods 0.000 claims description 15
- 239000000463 material Substances 0.000 claims description 14
- 230000001105 regulatory effect Effects 0.000 claims description 13
- 239000007787 solid Substances 0.000 claims description 13
- 210000000538 tail Anatomy 0.000 claims description 13
- 239000006210 lotion Substances 0.000 claims description 12
- 238000005406 washing Methods 0.000 claims description 12
- 230000029219 regulation of pH Effects 0.000 claims description 11
- 239000000203 mixture Substances 0.000 claims description 10
- 238000001035 drying Methods 0.000 claims description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 6
- 239000011343 solid material Substances 0.000 claims description 4
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 238000003786 synthesis reaction Methods 0.000 claims description 3
- 238000004140 cleaning Methods 0.000 claims 1
- QJZYHAIUNVAGQP-UHFFFAOYSA-N 3-nitrobicyclo[2.2.1]hept-5-ene-2,3-dicarboxylic acid Chemical compound C1C2C=CC1C(C(=O)O)C2(C(O)=O)[N+]([O-])=O QJZYHAIUNVAGQP-UHFFFAOYSA-N 0.000 abstract description 33
- 239000004021 humic acid Substances 0.000 abstract description 33
- 238000005516 engineering process Methods 0.000 abstract description 17
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 abstract description 14
- 238000000926 separation method Methods 0.000 abstract description 10
- 239000002994 raw material Substances 0.000 abstract description 9
- 238000012546 transfer Methods 0.000 abstract description 7
- 238000010924 continuous production Methods 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000000243 solution Substances 0.000 description 83
- HEMHJVSKTPXQMS-UHFFFAOYSA-M sodium hydroxide Inorganic materials [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 46
- 238000000605 extraction Methods 0.000 description 23
- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 12
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 9
- 239000000284 extract Substances 0.000 description 8
- 238000005189 flocculation Methods 0.000 description 8
- 229910021502 aluminium hydroxide Inorganic materials 0.000 description 7
- REDXJYDRNCIFBQ-UHFFFAOYSA-N aluminium(3+) Chemical compound [Al+3] REDXJYDRNCIFBQ-UHFFFAOYSA-N 0.000 description 6
- 238000004090 dissolution Methods 0.000 description 6
- 230000000694 effects Effects 0.000 description 6
- 238000001556 precipitation Methods 0.000 description 6
- 230000008901 benefit Effects 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000001914 filtration Methods 0.000 description 5
- 230000016615 flocculation Effects 0.000 description 5
- 239000003245 coal Substances 0.000 description 4
- 238000013461 design Methods 0.000 description 4
- PUKLDDOGISCFCP-JSQCKWNTSA-N 21-Deoxycortisone Chemical compound C1CC2=CC(=O)CC[C@]2(C)[C@@H]2[C@@H]1[C@@H]1CC[C@@](C(=O)C)(O)[C@@]1(C)CC2=O PUKLDDOGISCFCP-JSQCKWNTSA-N 0.000 description 3
- FCYKAQOGGFGCMD-UHFFFAOYSA-N Fulvic acid Natural products O1C2=CC(O)=C(O)C(C(O)=O)=C2C(=O)C2=C1CC(C)(O)OC2 FCYKAQOGGFGCMD-UHFFFAOYSA-N 0.000 description 3
- -1 aluminum ions Chemical class 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000002509 fulvic acid Substances 0.000 description 3
- 229940095100 fulvic acid Drugs 0.000 description 3
- 239000004615 ingredient Substances 0.000 description 3
- 238000004064 recycling Methods 0.000 description 3
- 229910000029 sodium carbonate Inorganic materials 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 238000002604 ultrasonography Methods 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- IMQLKJBTEOYOSI-GPIVLXJGSA-N Inositol-hexakisphosphate Chemical compound OP(O)(=O)O[C@H]1[C@H](OP(O)(O)=O)[C@@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@@H]1OP(O)(O)=O IMQLKJBTEOYOSI-GPIVLXJGSA-N 0.000 description 2
- IMQLKJBTEOYOSI-UHFFFAOYSA-N Phytic acid Natural products OP(O)(=O)OC1C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C1OP(O)(O)=O IMQLKJBTEOYOSI-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 239000003480 eluent Substances 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 229940068041 phytic acid Drugs 0.000 description 2
- 235000002949 phytic acid Nutrition 0.000 description 2
- 239000000467 phytic acid Substances 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 238000011160 research Methods 0.000 description 2
- BHPQYMZQTOCNFJ-UHFFFAOYSA-N Calcium cation Chemical compound [Ca+2] BHPQYMZQTOCNFJ-UHFFFAOYSA-N 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- JLVVSXFLKOJNIY-UHFFFAOYSA-N Magnesium ion Chemical compound [Mg+2] JLVVSXFLKOJNIY-UHFFFAOYSA-N 0.000 description 1
- 239000000654 additive Substances 0.000 description 1
- 230000000996 additive effect Effects 0.000 description 1
- 208000012826 adjustment disease Diseases 0.000 description 1
- 238000005273 aeration Methods 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 159000000013 aluminium salts Chemical class 0.000 description 1
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical class Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 229910001424 calcium ion Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 230000035568 catharsis Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 238000010494 dissociation reaction Methods 0.000 description 1
- 230000005593 dissociations Effects 0.000 description 1
- 238000010828 elution Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-M hydroxide Chemical compound [OH-] XLYOFNOQVPJJNP-UHFFFAOYSA-M 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910001425 magnesium ion Inorganic materials 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 229930014626 natural product Natural products 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920001596 poly (chlorostyrenes) Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000001376 precipitating effect Effects 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 238000005070 sampling Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000003860 storage Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L5/00—Solid fuels
- C10L5/02—Solid fuels such as briquettes consisting mainly of carbonaceous materials of mineral or non-mineral origin
Landscapes
- Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
A kind of lignite process equipment, the present invention relates to a kind of lignite processing equipment fields, and in particular to a kind of to extract humic acid apparatus field by raw material of lignite.A kind of with the equipment that lignite utilizes includes that lignite processing system, alkali pool processing system, sour pond processing system and four part of separate tank processing system form.The present invention is cooperated by each device realizes the separation of product and soda acid, soda acid dosage is reduced, and exchange device technique has cooperatively formed aluminium circulation, lye circulation and acid solution and has recycled, and avoids and generates pollution of the waste to environment in production process, reducing soda acid usage amount reduces cost.The reverse mass transfer of solid-liquid improves " compatibility " of production technology, realizes continuous production, easily controllable.
Description
Technical field
The present invention relates to a kind of lignite processing equipment fields, and in particular to a kind of to extract adding for humic acid by raw material of lignite
Construction equipment field.
Background technique
Lignite is the minimum pit coal of degree of coalification, is not easy storage and remote fortune, and when burning is serious to air pollution.However it is brown
But contain a large amount of humic acid and fulvic acid in coal；Humic acid content accounts for the 80% of its organic matter in the lignite of part.In recent years, rotten
Phytic acid is widely used in multiple industries because of its unique physicochemical property, therefore using lignite as raw material, has extracted humic acid
Hot spot as related fields research.
The humic acid method extracted from lignite in research at present is mainly " alkali carries acid out ", is extracted under alkaline condition brown
Then humic acid in coal is adjusted to highly acid, humic acid is precipitated.Outstanding problem existing for this method is concentrated mainly on following
Two aspects:
The first, " alkali carries acid out " soda acid dosage is big, and environmental pollution is serious.
The pH value of lye when lignite extracts is typically larger than 10, and precipitation process then needs stronger acid condition, by strong
Alkali environment is transferred to strong acid environment, to consume a large amount of acid, and these soda acids are generally difficult to be recycled.
The second, lignite component difference is big, and corresponding extraction process is difficult to meet the requirement of humic acid actual extracting.
Due to the difference of the degree of coalification of lignite, there is also very big difference for the content of humic acid；Even same area
The lignite of domain different coal, there are biggish differences for ingredient.Therefore for lignite extract humic acid technique and equipment aspect all
There should be corresponding " compatibility ", to adapt to the difference of raw material.This is very important the extraction of natural products.
Such as in lye extraction process, humic acid content is low to will cause lye residue, and remaining lye not only wastes, and
A large amount of acid are needed to go to neutralize；It is insufficient that humic acid content height will cause rotten plant extraction.Prior art is using in extraction process
PH is monitored, control pH is not less than 10, actually to improve extraction effect, keeps lye superfluous.
Summary of the invention
Based on above-mentioned technical problem, the present invention proposes following inventive concept
Design 1: soda acid usage amount is reduced
1, it is not necessarily to entire solution being adjusted to acidity after alkali carries, poly-aluminium is added into the humic acid solution of extraction, flocculates,
Humic acid collectively constitutes flocculate with aluminium element and separates with lye, and lye return system can be recycled.
2, the precondition that lye is recycled is that lye should be clean.The present invention is first is that lignite passes through pretreatment, as
Processing of the acid solution to lignite guarantees introducing impurity as few as possible in lye from raw material level；Second is that poly-aluminium is flocculated, inherently
For the purification process of lye.
3, acid solution is used for multiple times: as shown in Fig. 1-C, in acid condition, flocculated state is destroyed flocculate, aluminium with from
Sub- form enters in solution, and humic acid is precipitated with precipitation form.Part acid solution in the acid solution of this part is as lignite pretreatment liquid
Acid solution is purified with aluminium hydroxide.
4, compared with prior art；Present invention introduces poly-aluminiums as flocculant, but poly-aluminium is the byproduct in the present invention, nothing
It need to additionally introduce, and can recycling with aluminium element.
Design 2: the reverse mass transfer of solid-liquid
During lignite extracts aluminum ions, acid solution is advanced from left to right；Lignite is advanced from right to left；The reverse row of the two
Into.Reverse mass transfer the utility model has the advantages that
(1) meet extraction process requirement.Acid used is extracted with the progress of extraction, sour intensity acid can gradually weaken,
The intensity of the reverse mass transport process acid of solid-liquid can gradually weaken along direction of travel；The extraction difficulty of lignite intermediate ion can be along traveling
Direction gradually increases.During existing actual extracting: when starting, substance to be extracted is easy to extract, with the progress of extraction, after
The phase concentration of acid is low, but substance to be extracted is difficult to extract.Therefore the reverse mass transfer of solid-liquid is the effective ways for solving the problems, such as this.
(2) " compatibility " for improving production technology realizes continuous production, easily controllable.Due to the difference of lignite ingredient, mention
Be difficult to during taking configure corresponding suitable number of acid solution for the raw material of different content, this problem in continuous production especially
It is prominent.
(3) the prominent advantage of reverse mass transfer shows " total amount maintains an equal level, and part is excessive ": firstly, reaction-ure mixture with it is existing
Technique dosage maintains an equal level: it is 1 that the mark that fully reacting is finally reached during said extracted, which is the pH of exit solution of lignite, i.e.,
Lignite passes through the processing of strong acid, and lignite can be kept to pass through the processing of strong acid by addition acid solution；The mark of corresponding acid solution
Will is that the exit pH value of solution of acid solution is 4, this can be realized by adjusting the additive amount of lignite.Secondly, reactant part mistake
Amount: in the reaction process of lignite, it is obvious excess during final reaction, ensure that the abundant progress of reaction.
The above inventive concept is realized by technical solution in detail below.A kind of method that lignite utilizes includes at lignite
Reason system, alkali pool processing system, sour pond processing system and four part of separate tank processing system composition.
First part: lignite processing system:
Equipment:
It is formed as shown in Fig. 2, lignite processing unit (1) is sequentially connected by 7 the first process chambers (1-1), the first process chamber
The left end (1-1) is equipped with the first grid (1-2)；4-8 the first agitating paddles (1-6) are equipped in first process chamber (1-1)；Process chamber
First inlet tube (1-10) above right side, the first inlet tube (1-10) pass through the first liquid feed valve (1-8) and the first gathering tube (1-
12) it is connected；First leakage fluid dram (1-7), the first leakage fluid dram (1-7) and the first drain pipe (1-3) phase below first grid (1-2)
Connection, the first drain pipe (1-3) are connected by the first liquid valve (1-4) with the first gathering tube (1-12), the first drain pipe (1-
3) it is connected by the second liquid valve (1-5) with the second gathering tube (1-11)；Spaced valve (1-9) on first gathering tube (1-12)
Between adjacent 2 the first process chambers (1-1)；As shown in fig. 6, the first grid (1-2) of the first process chamber of the leftmost side (1-1)
It is connected by first material conveyer belt (1-14) with the first centrifuge (1-13)；4-8 are uniformly distributed on first agitating paddle (1-6)
Stirring blade (1-61), connects 2 caudas (1-62) on the outside of stirring blade (1-61), stirring blade (1-61) and cauda (1-62)
Between angle be 120 degree, the angle between two caudas (1-62) is 120 degree.
Technique:
Lignite is advanced by No. 1 process chamber to No. 7 process chamber directions, and is spaced a process chamber and material is added；Initial acid solution
A1 is advanced from No. 7 process chambers to No. 1 process chamber direction, and is spaced a process chamber and material is added；Lignite passes through n-1 process chamber
First grid (1-2) enters n process chamber, and acid solution enters n process chamber by the first inlet tube (1-10), in the first agitating paddle
Extracted under (1-6) stirring action, after extraction starting the first grid (1-2) simultaneously acid solution by the first leakage fluid dram (1-3) arrange
N process chamber is entered by the first inlet tube (1-10) again out, forms circulation in acid solution, when lignite passes through the first lattice of n process chamber
After grid (1-2) enter n+1 process chamber, acid solution enters the first gathering tube (1- by the first leakage fluid dram (1-3) in n process chamber
12) enter n-1 process chamber, enter the first centrifuge (1-13) after lignite passes through No. 7 process chambers, solid A after centrifuge separation
Into in the first alkali pool (2-1)；When acid solution pH value is greater than 4, by the second gathering tube (1-11), being labeled as W, W, which enters, to be divided
From in pond processing system (4).
Technology illustrates 1-1: reverse mass transfer in extraction process, as described in inventive concept 2, details are not described herein.
Technology illustrates 1-2: acid solution used by this step is studied is the acid solution in sour pond, and the main function in sour pond is to slough
Aluminium ion in flocculate, ingredient are the acid solutions containing aluminium ion pH=1-2, and extracting using the part solution can be abundant
Extract fulvic acid, while in lignite there is it is a certain number of be easy to extract aluminium salts, using hydrochloric acid may be implemented for aluminium from
The extraction of son, raw material of the aluminium ion extracted as preparation polychlorostyrene.
Technology illustrates 1-3: the effect of the first agitating paddle (1-6) is to guarantee sufficiently connecing for lignite and acid solution during the extraction process
Touching and the displacement for realizing solid material horizontal direction.Cauda (1-62), can be by underlying solid " shovel " at bottom
It rises, the solid being clipped between two the first agitating paddles (1-6), the first of lower section during falling in company with two the first agitating paddles
The cauda (1-62) of agitating paddle (1-6) can change the direction of solid whereabouts, so that it is fallen forwards, into next agitating paddle
Range is stirred, is to realize the movement of horizontal direction under the cooperation of fluent solution.
Technology illustrates 1-4: the reverse mass transfer of solid-liquid, solves the technical problem of aluminium extracted in separation process.When pH value is
When 3-5, aluminium ion is precipitated from solution with precipitation form, this pH value range is big, it is difficult to select suitable pH value for lignite
It is separated with extracting solution.
Lignite is carried out when selective extraction liquid is in lower ph and extracting solution is separated, such as will extract acid solution when pH=3
It is separated with lignite, extraction acid solution is adjusted to pH value can be such that the aluminium in solution is sufficiently recycled greater than 5, but pH is greater than 3
Acid solution, which has neither part nor lot in, extracts lignite, and needs to adjust pH, additionally consumes lye.
If pH value is higher, extracting solution is separated when such as pH=4-5 with lignite, is adjusted to pH value greater than 5 although disappearing
The alkali number of consumption is less, and acid solution utilization is more abundant, but aluminum hydroxide precipitation has been produced when pH=3-4, the aluminium hydroxide of precipitating
It is mixed with lignite, is difficult to dissolve in alkali pool extraction process, be eventually discharged, can not recycle in company with filter residue.
Acid used by this invention expects reversed mode, solves the above problem, selects to isolate solution when pH=4
Come, acid solution utilization is more abundant, while the aluminium hydroxide being settled out in pH=3-4 with lignite it is mobile, the acid of the acid solution contacted
Property gradually increase aluminium atom and re-dissolve into extracting solution, as acid solution movement carries out above-mentioned precipitation process again, realize aluminium
Be sufficiently separated.
Second part alkali pool processing system
Equipment:
As shown in figure 3, alkali pool system (2) is divided into the first alkali pool (2-1) and the second alkali pool (2-11)；First alkali pool (2-1)
And second be equipped with first pipe (2-10), changeable the first surge tank (2-21) and the second surge tank in parallel between alkali pool (2-11)
(2-22)；The third leakage fluid dram (2-13) of second alkali pool (2-11) is connect with the one end second pipe (2-15), second pipe (2-
15) other end is connect with the first decanter centrifuge (2-16), the first decanter centrifuge (2-16) by third pipeline (2-17) with
First alkali pool (2-1) is connected；
One end of first alkali pool (2-1) is highest point (2-4), and highest point (2-4) to minimum point (2-5) is by 20-100 grades of phases
Same ladder (2-6) connection, each ladder (2-6) is interior 3-5 identical solarization air caps (2-7), the horizontal length of ladder (2-6)
20-50cm is spent, is one-way cock (2-8) on the outside of solarization air cap (2-7)；The second grid bottom (2-2) is located at minimum point (2-5) institute
Plane, have the second leakage fluid dram (2-9) at minimum point (2-5) on side wall, the second leakage fluid dram (2-9) and first pipe (2-10)
Between be connected with the first surge tank (2-21) and the second surge tank (2-22)；The third grid bottom end (2-3) is located at highest point (2-4) institute
In the plane；It is above third grid (2-3) the second inlet tube (2-18)；Adjacent first of plane where highest point (2-4)
It is above ladder (2-6) feed points (2-19)；Feed points (2-19) middle side part is equipped with the 6th pH value and exists in first alkali pool (2-1)
Line regulating device (2-30)；
The one end second alkali pool (2-11) has third leakage fluid dram (2-13), has subregion plate at third leakage fluid dram (2-13)
(2-12), the second alkali pool (2-11) top are first pipe (2-10) nozzle and poly-aluminium feed pipe (2-25) nozzle；Second alkali pool
(2-11) connects second pipe (2-15) equipped with 4-8 the second agitating paddles (2-14), third leakage fluid dram (2-13), second pipe
First pump (2-20) is installed on (2-15) and provides power, second pipe (2-15) other end and first for flocculated mixture advance
The feed inlet of decanter centrifuge (2-16) is connected；First decanter centrifuge (2-16) liquid outlet passes through third pipeline (2-17) and the
Two inlet tubes (2-18) are connected；The solid material that first decanter centrifuge (2-16) is isolated enters the 1 of sour pond processing system (3)
In number second processing room (3-1)；
It is equipped with 4-8 the first on-line pH value regulating devices (2-24) in second alkali pool (2-11), adjusts the second alkali pool (2-
11) pH value is equipped with the second pH value on-line control device (2-23) between 10.0-11.0 in third pipeline (2-17), adjusts
PH value is saved between 11.0-11.5；
First alkali pool (2-1) is designed using ramp type, and slope angle with horizontal plane is 5-30 degree.
Technique:
Solid A is entered in the first alkali pool (2-1) by feed points (2-19) after centrifuge separation, and lye is in aeration and gravity
It is mobile to the second grid (2-2) under collective effect, and realized and be separated by solid-liquid separation by the second grid (2-2), solid is after extracting
Lignite waste residue B, liquid are the second extracting solution C containing humic acid, and the second extracting solution C enters the first surge tank (2-21), when mentioning
Take liquid C volume be the first surge tank (2-21) 80% when, the second extracting solution C enter the second surge tank (2-22), the first surge tank
(2-21) sampling carries out flocculation detection, and extracting solution C is put into the second alkali pool (2-11) in the first surge tank (2-21)；First buffering
Tank (2-21) and the second surge tank (2-22) alternately carry the second extracting solution C, are put into the second alkali pool (2-11) after sample detection,
Extracting solution is put into during the second alkali pool (2-11) and concentration is added according to the ratio that 0.05-0.5 grams of poly-aluminium is added in every gram of humic acid
For the poly-aluminium solution of 1-10g/L, humic acid enters the second alkali pool (2-11) to flocculate shape by first pipe (2-10) nozzle
Formula is 10-300 minutes by third leakage fluid dram (2-13) discharge time used, by the first decanter centrifuge (2- after flocculation
16) it is separated by solid-liquid separation, solid is flocculate D, and liquid is lye E；Lye E passes through third pipeline (2-17) and the second inlet tube (2-
18) the first alkali pool (2-1) is returned to, be recycled, it is online to be equipped with the 6th for feed points (2-19) middle side part in the first alkali pool (2-1)
PH value regulating device (2-30) adjusts pH value between 10.5-11.0；The second on-line pH value is equipped in third pipeline (2-17)
Regulating device (2-23) adjusts pH value between 11.0-11.5.
Technology illustrates 2-1: in the industrial production of this step, the maximum problem faced is the object in continuous production process
Material proportion is unable to control, and is caused poly-aluminium superfluous or is flocculated incomplete.The inventive concept of this step remains: being matched with circulation adjustment reaction
Than improving the compatibility of industrial manufacture process.
If sodium humate is excessive in solution, remaining humic acid can be recycled back to flocculate next time as extracting solution participation；
If poly-aluminium is excessive, residual Al enters dealuminzation device (3), further reuse, the raw material as preparation poly-aluminium.It is most closed in this step
The technical controlling point of key is to guarantee that superfluous aluminium ion does not dissolve (pH value is higher than 12) in alkali pool (2-11), returns to the first alkali pool
(2-1) is precipitated, and is discharged with lignite waste residue B.Therefore pH value control area and numerical value are important control point.Using slope flow model
Design function: 1) continuous extract is realized；2) the pH value control of multiple spot multizone may be implemented；3) class pipeline type designs.
Technology illustrates 2-2: showing mixed solution the mentioning for humic acid of sodium carbonate and sodium hydroxide by previous experiments
Effect is taken to be higher than simple sodium carbonate and sodium hydroxide.Therefore, present study be passed through carbon dioxide benefit it is as follows: 1), improve
The extraction efficiency of humic acid.2) the abundant dissolution to humic acid, is realized by the gradient of air-flow promotion and alkali pool.3), sodium carbonate
The dissolution of calcium ions and magnesium ions in extraction process can effectively be controlled.
Technology illustrates 2-3: it is that alkali acid conversion consumption is largely sour that humic acid alkali carries acid out, which extracts most important problem, at present
Liquid, while there are a large amount of chloride ions in mother liquor, it is difficult to it is effectively treated.In the present invention by the way that experimental results demonstrate in alkali
Property solution (pH value 11) when, suitable poly-aluminium is added, can realize that humic acid flocculate from lye and come out by flocculation mode,
It is separated with lye, it is not necessary to adjust solution as acidity, reduce the consumption of a large amount of acid solutions.
Technology illustrates 2-4: this item extraction process is extracted using on-line pH value regulative mode, it is possible to prevente effectively from highly basic
Destruction for humic acid bioactivity.Throughout the extraction process, pH value can not only reduce the dissolution of silicon less than 11.5, but also
It can be to avoid the loss that aluminium in flocculation process is added.In flocculation process, if aluminium ion is excessive, pH value can be generated higher than 12 can
Dissolubility meta-aluminate is returned after dissolution in the first alkali pool (2-1), and pH value decline generates aluminium hydroxide again, after centrifuge separation
It is removed in company with solid filter residue, causes unnecessary loss.
Part III acid pond processing system
Equipment:
As shown in figure 4, sour pond processing system (3) is sequentially connected by 4 second processing rooms (3-1) and is formed, number consecutively is
No. 1-4, second processing room (3-1) right end is equipped with the 4th grid (3-2), the 4th grid lower end (3-2) and third conveyer belt (3-
11) it is connected；2-4 third agitating paddle (3-3) is equipped in second processing room (3-1)；The 4th in No. 4 second processing rooms (3-1)
Grid (3-2) discharge port is connected by second material conveyer belt (3-4) with the feed inlet of the second decanter centrifuge (3-5)；No. 2-4
Second processing room (3-1) is designed with fluid level control device (3-6)；When liquid level declines in n second processing room (3-1), liquid level
The solution chosen in concentrated acid and n-1 second processing room (3-1) in proportion is added to n second processing room by control device (3-6)
In (3-1), the volume and pH value of solution in n second processing room (3-1) are kept；Liquid level declines in No. 1 second processing room (3-1)
When, the solution chosen in washing lotion tank (3-7) in proportion and water are added to No. 1 second processing room (3- by fluid level control device (3-6)
1) in, the volume and pH value of solution in No. 1 second processing room (3-1) are kept；
The liquid circulation that second decanter centrifuge (3-5) liquid outlet comes out returns to No. 4 second processing rooms (3-1), and solid is handed over
It is cleaned and dried in tank (3-8) or the second cleaning-drying tank (3-9) for entering first, first is cleaned and dried tank (3-8) or second clearly
It washes drying chamber (3-9) washing lotion outlet and is connected with washing lotion tank (3-7) by pipeline；No. 4 second processing rooms bottom (3-1) is equipped with and takes
Acid tube (3-10).
Technique:
Flocculate enters in sour pond processing system (3), in 1-4 second processing room (3-1) pH value of acid solution be respectively 6,
4,2,1, flocculate is moved by solution flowing and the 4th grid (3-2), successively from No. 1 second processing room (3-1) to No. 4 second
Process chamber (3-1) movement, is centrifugated, and cleaned with clear water to neutrality, then wash through alcohol by the second decanter centrifuge (3-5)
Afterwards, 2-6 hours dry at 80 DEG C；
In No. 4 second processing rooms (3-1) after acid liquor filtering, as acid solution A1 initial in lignite processing system；At No. 3 second
It manages in room (3-1) after acid liquor filtering and enters in No. 4 second processing rooms (3-1) after concentrated hydrochloric acid mixing, keep No. 4 second processing rooms
The stabilization of (3-1) pH value and volume；Enter No. n+1 the in n second processing room (3-1) after acid liquor filtering and after concentrated hydrochloric acid mixing
In two process chambers (3-1)；Enter in No. 1 second processing room (3-1) after washing lotion and concentrated hydrochloric acid mixing in washing lotion tank (3-7).
Technology illustrates 3-1: although flocculate, which is directly added into strong acid, can achieve the aluminum ions effect of removal, quickly
Soda acid variation, will affect the activity of humic acid, will lead to eluent by the way of simple gradient elution and be difficult to abundant benefit
With, and it will appear floccule body and be destroyed, the phenomenon that part humic acid dissolution is pulled away with eluent.Therefore this step is adopted
With the method for grad enhancement acidity, the solid transmitting in the same direction of liquid can make the humic acid of dissolution finally obtain recycling.
Technology illustrates 3-2: since humic acid flocculation process has catharsis, flocculate dissociation process for water body
In have impurity and be discharged into acid solution, acid solution can be used for multiple times, but need to constantly update, and the acid solution of update is as extracting solution.
Part IV: separate tank processing system
Equipment:
As shown in figure 5, separate tank processing system (4) is equipped with the knockout drum (4-1) of filter plate by poly-aluminium synthesis tank, two bottoms
It is formed with a third process chamber (4-3)；Knockout drum (4-1) and third process chamber (4-3) are connected by rapid mixing chamber (4-2)
It connects；
First charging aperture (4-11) at the top of knockout drum (4-1) is connected with the second gathering tube (1-11)；Knockout drum (4-1)
The second charging aperture (4-12) at top is connect with acid tube (3-10) is taken by pipeline, and the 3rd pH is equipped in knockout drum (4-1) and is regulated and controled
Device (4-13)；
It is mixed that the 4th online pH regulation device (4-21), agitating device (4-22) and ultrasound are equipped in rapid mixing chamber (4-2)
It attaches together and sets (4-23)；
Third process chamber is diagonally divided into two parts by the 5th grid (4-31) in third process chamber (4-3), the
The 5th pH regulation device (4-32) is equipped in three process chambers (4-3).
Technique:
Acid solution W of the pH value greater than 4 enters in knockout drum (4-1), adjusts pH=7 of solution, is separated by filtration, in liquid Y is rich
Acid solution；The acid solution in No. 4 second processing rooms (3-1) is added to knockout drum (4-1), until pH value of solution≤3, solution is put into quickly
In mixing channel (4-2), solution is in the 4th online pH regulation device (4-21), agitating device (4-22) and ultrasonic mixing device (4-
23) under the action of, after quickly adjusting pH=7, into third process chamber (4-3), by the 5th grid (4-31) by solid hydroxide
Aluminium separation, solution produce the raw material of fulvic acid by being incorporated as after the multiple circulating filtration of the circulatory system with solution Y；
4mol/L hydrochloric acid is added in aluminium hydroxide by the ratio for being 10:1-5:1 according to the molar ratio of hydrochloric acid and aluminium hydroxide
In, 110 DEG C stirring 3-5 hours, a small amount of aluminium powder is added to solution no longer vigorous reaction, 90 DEG C of adjusting PH to 4.5, after staticly settling
It refilters, obtains polymeric aluminum chlorides solution, adjust concentration, the humic acid that flocculates is added in the second alkali pool (2-11).
Technology illustrates that 4-1 aluminum hydroxide precipitation can adsorb the substances such as 3 acid in corresponding richness in the process, needs to purify ability
Guarantee the product quality of poly-aluminium.
After solution is put into rapid mixing chamber (4-2), by quickly stirring, the aluminium hydroxide that the operations such as ultrasound ensure to generate
It is separated as early as possible, adsorption bridging, net is avoided to catch phenomena such as volume is swept, avoid the generation of flocculation phenomenon.
The utility model has the advantages that
1, it is not necessarily to entire solution being adjusted to acidity after alkali carries, poly-aluminium is added in the humic acid solution of extraction, flocculates, it is rotten
Phytic acid collectively constitutes flocculate with aluminium element and separates with lye, and lye can be recycled.
2, the separation of humic acid and lye can be thus achieved in poly-aluminium flocculation, and is the purification process for lye.
3, byproduct of the poly-aluminium in present study, and can recycling with aluminium element.
4, " compatibility " of production technology is improved, realizes continuous production, it is easily controllable.
Figure of description:
Attached drawing 1: process flow chart A；Aluminium element circulation figure B；Soda acid moves towards figure C.
Attached drawing 2: lignite processing system side elevational cross-section Local map A；Lignite processing system top view B；Lignite processing system bottom
View C, the first agitating paddle (1-6) enlarged drawing D.
Attached drawing 3: alkali pool processing system schematic diagram A；First alkali pool (2-1) top view B；Second alkali pool (2-11) top view C；
First alkali pool (2-1) is along auxiliary line AA sectional view D；First alkali pool (2-1) is along auxiliary line AA section partial enlarged view E.
Attached drawing 4: sour pond processing system side elevational cross-section Local map A；Second material conveyer belt (3-4) and the second decanter centrifuge
(3-5) partial schematic diagram B；It is cleaned and dried tank part partial schematic diagram C.
Attached drawing 5: enter lignite processing equipment figure before alkali pool.
Attached drawing 6: lignite processing system Local map.
In figure: 1: lignite processing unit；1-1: the first process chamber；1-2: the first grid；1-3: the first drain pipe；1-4: the
One liquid valve；1-5: the second liquid valve；1-6: the first agitating paddle；1-7: the first leakage fluid dram；1-8: the first liquid feed valve；1-9: interval
Valve；1-10: the first inlet tube；1-11: the second gathering tube；1-12: the first gathering tube；1-13: the first centrifuge；1-14: the first
Material conveyor belt；1-61: stirring blade；1-62: cauda；
2: alkali pool processing system；2-1: the first alkali pool；2-2: the second grid；2-3: third grid；2-4: highest point；2-5:
Minimum point；2-6: ladder；2-7: solarization air cap；2-8: one-way cock；2-9: the second leakage fluid dram；2-10: first pipe；2-11: the
Two alkali pools；2-12: subregion plate；2-13: third leakage fluid dram (2-13)；The second agitating paddle of 2-14；2-15: second pipe；2-16: the
One decanter centrifuge；2-17: third pipeline；2-18: the second inlet tube；2-19: feed points；2-20: the first pump；2-21: the first
Surge tank；2-22: the second surge tank；2-23: the second on-line pH value regulating device；2-24: the first on-line pH value regulating device；2-
25: poly-aluminium feed pipe；2-30: the six on-line pH value regulating device；
3: sour pond processing system；3-1: second processing room；3-2: the four grid；3-3: third agitating paddle；3-4: the second object
Expect conveyer belt；3-5: the second decanter centrifuge；3-6: fluid level control device；3-7: washing lotion tank；3-8: the first is cleaned and dried tank；
3-9: the second is cleaned and dried tank；3-10: acid tube is taken；3-11: third conveyer belt；
4: separate tank processing system: 4-1: knockout drum；4-2: rapid mixing chamber；4-3: third process chamber；4-11: the first into
Material mouth；4-12: second charging aperture；4-13: the online pH regulation device of third；4-21: the four online pH regulation device；4-22: it stirs
Mix device；4-23: ultrasonic mixing device；4-31: the five grid；4-32: the five online pH regulation device.
Specific embodiment:
Embodiment 1
A kind of lignite process equipment, the equipment is by lignite processing system, alkali pool processing system, sour pond processing system and separation
Four part of pond processing system composition；
Lignite processing unit (1)It is sequentially connected and is formed by 7 the first process chambers (1-1), the first process chamber left end (1-1) peace
Equipped with the first grid (1-2)；4-8 the first agitating paddles (1-6) are equipped in first process chamber (1-1)；Top the on the right side of process chamber
One inlet tube (1-10), the first inlet tube (1-10) are connected by the first liquid feed valve (1-8) with the first gathering tube (1-12)；The
The first leakage fluid dram (1-7), the first leakage fluid dram (1-7) are connected with the first drain pipe (1-3) below one grid (1-2), first row
Liquid pipe (1-3) is connected by the first liquid valve (1-4) with the first gathering tube (1-12), and the first drain pipe (1-3) passes through second
Liquid valve (1-5) is connected with the second gathering tube (1-11)；Spaced valve (1-9) on first gathering tube (1-12) is located at adjacent 2
Between a first process chamber (1-1)；As shown in fig. 6, the first grid (1-2) of the first process chamber of the leftmost side (1-1) passes through first
Material conveyor belt (1-14) is connected with the first centrifuge (1-13)；4-8 stirring blade is uniformly distributed on first agitating paddle (1-6)
(1-61), stirring blade (1-61) outside connect 2 caudas (1-62), the angle between stirring blade (1-61) and cauda (1-62)
It is 120 degree, the angle between two caudas (1-62) is 120 degree；
Alkali pool processing system (2)It is divided into the first alkali pool (2-1) and the second alkali pool (2-11)；First alkali pool (2-1) and second
First pipe (2-10), changeable the first surge tank (2-21) and the second surge tank (2- in parallel are equipped between alkali pool (2-11)
22)；The third leakage fluid dram (2-13) of second alkali pool (2-11) is connect with the one end second pipe (2-15), and second pipe (2-15) is another
One end is connect with the first decanter centrifuge (2-16), and the first decanter centrifuge (2-16) passes through third pipeline (2-17) and the first alkali
Pond (2-1) is connected；
One end of first alkali pool (2-1) is highest point (2-4), and highest point (2-4) to minimum point (2-5) is by 20-100 grades of phases
Same ladder (2-6) connection, each ladder (2-6) is interior 3-5 identical solarization air caps (2-7), the horizontal length of ladder (2-6)
20-50cm is spent, is one-way cock (2-8) on the outside of solarization air cap (2-7)；The second grid bottom (2-2) is located at minimum point (2-5) institute
Plane, have the second leakage fluid dram (2-9) at minimum point (2-5) on side wall, the second leakage fluid dram (2-9) and first pipe (2-10)
Between be connected with the first surge tank (2-21) and the second surge tank (2-22)；The third grid bottom end (2-3) is located at highest point (2-4) institute
In the plane；It is above third grid (2-3) the second inlet tube (2-18)；Adjacent first of plane where highest point (2-4)
It is above ladder (2-6) feed points (2-19)；Feed points (2-19) middle side part is equipped with the 6th pH value and exists in first alkali pool (2-1)
Line regulating device (2-30)；
The one end second alkali pool (2-11) has third leakage fluid dram (2-13), has subregion plate at third leakage fluid dram (2-13)
(2-12), the second alkali pool (2-11) top are first pipe (2-10) nozzle and poly-aluminium feed pipe (2-25) nozzle；Second alkali pool
(2-11) connects second pipe (2-15) equipped with 4-8 the second agitating paddles (2-14), third leakage fluid dram (2-13), second pipe
First pump (2-20) is installed on (2-15) and provides power, second pipe (2-15) other end and first for flocculated mixture advance
The feed inlet of decanter centrifuge (2-16) is connected；First decanter centrifuge (2-16) liquid outlet passes through third pipeline (2-17) and the
Two inlet tubes (2-18) are connected；The solid material that first decanter centrifuge (2-16) is isolated enters the 1 of sour pond processing system (3)
In number second processing room (3-1)；
It is equipped with 4-8 the first on-line pH value regulating devices (2-24) in second alkali pool (2-11), adjusts the second alkali pool (2-
11) pH value is equipped with the second pH value on-line control device (2-23) between 10.0-11.0 in third pipeline (2-17), adjusts
PH value is saved between 11.0-11.5；
First alkali pool (2-1) is designed using ramp type, and slope angle with horizontal plane is 5-30 degree；
Sour pond processing system (3)Be sequentially connected and formed by 4 second processing rooms (3-1), number consecutively be No. 1-4, second
Process chamber (3-1) right end is equipped with the 4th grid (3-2), and the 4th grid lower end (3-2) is connected with third conveyer belt (3-11)；The
2-4 third agitating paddle (3-3) is equipped in two process chambers (3-1)；The 4th grid (3-2) in No. 4 second processing rooms (3-1) goes out
Material mouth is connected by second material conveyer belt (3-4) with the feed inlet of the second decanter centrifuge (3-5)；2-4 second processing room
(3-1) is designed with fluid level control device (3-6)；When liquid level declines in n second processing room (3-1), fluid level control device (3-
6) solution chosen in concentrated acid and n-1 second processing room (3-1) in proportion is added in n second processing room (3-1), is kept
The volume and pH value of solution in n second processing room (3-1)；When liquid level declines in No. 1 second processing room (3-1), Liquid level
Device (3-6) adds to the solution chosen in washing lotion tank (3-7) in proportion and water in No. 1 second processing room (3-1), keeps 1
The volume and pH value of solution in number second processing room (3-1)；
The liquid circulation that second decanter centrifuge (3-5) liquid outlet comes out returns to No. 4 second processing rooms (3-1), and solid is handed over
It is cleaned and dried in tank (3-8) or the second cleaning-drying tank (3-9) for entering first, first is cleaned and dried tank (3-8) or second clearly
It washes drying chamber (3-9) washing lotion outlet and is connected with washing lotion tank (3-7) by pipeline；No. 4 second processing rooms bottom (3-1) is equipped with and takes
Acid tube (3-10)；
Separate tank processing system (4)The knockout drum (4-1) and a third of filter plate are equipped with by poly-aluminium synthesis tank, two bottoms
Process chamber (4-3) composition；Knockout drum (4-1) and third process chamber (4-3) are connected by rapid mixing chamber (4-2)；
First charging aperture (4-11) at the top of knockout drum (4-1) is connected with the second gathering tube (1-11)；Knockout drum (4-1)
The second charging aperture (4-12) at top is connect with acid tube (3-10) is taken by pipeline, and the 3rd pH is equipped in knockout drum (4-1) and is regulated and controled
Device (4-13)；
It is mixed that the 4th online pH regulation device (4-21), agitating device (4-22) and ultrasound are equipped in rapid mixing chamber (4-2)
It attaches together and sets (4-23)；
Third process chamber is diagonally divided into two parts by the 5th grid (4-31) in third process chamber (4-3), the
The 5th pH regulation device (4-32) is equipped in three process chambers (4-3).
Embodiment 2
A kind of lignite process equipment, the present embodiment is substantially the same manner as Example 1, the difference is that: alkali pool processing system
(2) in, ladder (2-6) horizontal length 20-50cm is preferably ladder (2-6) horizontal length 30cm,.
Technology explanation: the too short solarization air cap (2-7) that will appear of ladder (2-6) horizontal length is directly continuously by material " blowing off "
Phenomenon causes to extract insufficient；Horizontal length is too long, will lead to it and is detained in the ladder end (2-6), flowing velocity is slow.
Embodiment 3
A kind of lignite process equipment, the present embodiment is substantially the same manner as Example 2, the difference is that: alkali pool processing system
(2) the first alkali pool (2-1) is designed using ramp type in, and slope angle with horizontal plane is that 5-30 degree is preferably the first alkali pool (2-1)
It is designed using ramp type, slope angle with horizontal plane is 5 degree.
Technology explanation: slope angle with horizontal plane is too small, and flowing velocity is slow；Slope angle with horizontal plane is excessive, flowing speed
Degree is difficult to control.
Embodiment 4
A kind of lignite process equipment, the present embodiment is essentially identical with embodiment 1 or 3, the difference is that: lignite processing
Being uniformly distributed 4-8 stirring blade (1-61) in device (1) on first agitating paddle (1-6) is preferably on the first agitating paddle (1-6)
It is uniformly distributed 4 stirring blades (1-61).
Technology explanation: the angle between stirring blade (1-61) is 60 degree, between stirring blade (1-61) and cauda (1-62)
Angle is 120 degree.Two angles cooperate, and may be implemented to be conveyed horizontally to next first agitating paddle for particle is biggish
The bottom of (1-6).
Claims (4)
1. a kind of lignite process equipment, the equipment is by lignite processing system, alkali pool processing system, sour pond processing system and separate tank
Four part of processing system composition, it is characterised in that:
Lignite processing unit (1) is sequentially connected by 7 the first process chambers (1-1) and is formed, and the left end the first process chamber (1-1) is equipped with
First grid (1-2)；4-8 the first agitating paddles (1-6) are equipped in first process chamber (1-1)；It is equipped in the upper right side of process chamber
First inlet tube (1-10), the first inlet tube (1-10) are connected by the first liquid feed valve (1-8) with the first gathering tube (1-12)；
It is equipped with the first leakage fluid dram (1-7) below first grid (1-2), the first leakage fluid dram (1-7) is connected with the first drain pipe (1-3),
First drain pipe (1-3) is connected by the first liquid valve (1-4) with the first gathering tube (1-12), and the first drain pipe (1-3) is logical
The second liquid valve (1-5) is crossed to be connected with the second gathering tube (1-11)；Spaced valve (1-9) on first gathering tube (1-12) is located at
Between adjacent 2 the first process chambers (1-1)；The first grid (1-2) of the first process chamber of the leftmost side (1-1) is passed by first material
Band (1-14) is sent to be connected with the first centrifuge (1-13)；4-8 stirring blade (1- is uniformly distributed on first agitating paddle (1-6)
61) 2 caudas (1-62), are connected on the outside of stirring blade (1-61), the angle between stirring blade (1-61) and cauda (1-62) is
120 degree, the angle between two caudas (1-62) is 120 degree；
Alkali pool processing system (2) is divided into the first alkali pool (2-1) and the second alkali pool (2-11)；First alkali pool (2-1) and the second alkali pool
First pipe (2-10), changeable the first surge tank (2-21) and the second surge tank (2-22) in parallel are equipped between (2-11)；The
The third leakage fluid dram (2-13) of two alkali pools (2-11) is connect with the one end second pipe (2-15), second pipe (2-15) other end with
First decanter centrifuge (2-16) connection, the first decanter centrifuge (2-16) pass through third pipeline (2-17) and the first alkali pool (2-
1) it is connected；
One end of first alkali pool (2-1) is highest point (2-4), and highest point (2-4) to minimum point (2-5) is identical by 20-100 grades
Ladder (2-6) connection, each ladder (2-6) is interior 3-5 identical solarization air caps (2-7), ladder (2-6) horizontal length
20-50cm, solarization air cap (2-7) outside are one-way cock (2-8)；The second grid bottom (2-2) is located at where minimum point (2-5)
Plane, have the second leakage fluid dram (2-9) at minimum point (2-5) on side wall, the second leakage fluid dram (2-9) and first pipe (2-10) it
Between be connected with the first surge tank (2-21) and the second surge tank (2-22)；The third grid bottom end (2-3) is located at where highest point (2-4)
In plane；It is above third grid (2-3) the second inlet tube (2-18)；First adjacent rank of plane where highest point (2-4)
It is above terraced (2-6) feed points (2-19)；It is online to be equipped with the 6th pH value for feed points (2-19) middle side part in first alkali pool (2-1)
Regulating device (2-30)；
The one end second alkali pool (2-11) has third leakage fluid dram (2-13), has subregion plate (2- at third leakage fluid dram (2-13)
It 12), is first pipe (2-10) nozzle and poly-aluminium feed pipe (2-25) nozzle above the second alkali pool (2-11)；Second alkali pool (2-
11) equipped with 4-8 the second agitating paddles (2-14), third leakage fluid dram (2-13) (2-13) connects second pipe (2-15), the second pipe
First pump (2-20) is installed on road (2-15) and provides power for flocculated mixture advance, second pipe (2-15) other end and the
The feed inlet of one decanter centrifuge (2-16) is connected；First decanter centrifuge (2-16) liquid outlet by third pipeline (2-17) with
Second inlet tube (2-18) is connected；The solid material that first decanter centrifuge (2-16) is isolated enters sour pond processing system (3)
No. 1 second processing room (3-1) in；
It is equipped with 4-8 the first on-line pH value regulating devices (2-24) in second alkali pool (2-11), adjusts in the second alkali pool (2-11)
PH value is equipped with the second pH value on-line control device (2-23) between 10.0-11.0 in third pipeline (2-17), adjust pH value
Between 11.0-11.5；
First alkali pool (2-1) is designed using ramp type, and slope angle with horizontal plane is 5-30 degree；
Sour pond processing system (3) is sequentially connected by 4 second processing rooms (3-1) and is formed, and number consecutively is No. 1-4, second processing
Room (3-1) right end is equipped with the 4th grid (3-2), and the 4th grid lower end (3-2) is connected with third conveyer belt (3-11)；At second
It manages and is equipped with 2-4 third agitating paddle (3-3) in room (3-1)；The 4th grid (3-2) discharge port in No. 4 second processing rooms (3-1)
It is connected by second material conveyer belt (3-4) with the feed inlet of the second decanter centrifuge (3-5)；2-4 second processing room (3-1)
It is designed with fluid level control device (3-6)；When liquid level declines in n second processing room (3-1), fluid level control device (3-6) will
The solution chosen in concentrated acid and n-1 second processing room (3-1) in proportion adds in n second processing room (3-1), is kept for No. n
The volume and pH value of solution in second processing room (3-1)；When liquid level declines in No. 1 second processing room (3-1), fluid level control device
(3-6) adds to the solution chosen in washing lotion tank (3-7) in proportion and water in No. 1 second processing room (3-1), is kept for No. 1 the
The volume and pH value of solution in two process chambers (3-1)；
The liquid circulation that second decanter centrifuge (3-5) liquid outlet comes out returns to No. 4 second processing rooms (3-1), solid alternately into
Enter in the first cleaning-drying tank (3-8) or the second cleaning-drying tank (3-9), the first cleaning-drying tank (3-8) or the second cleaning are dry
Dry tank (3-9) washing lotion outlet is connected with washing lotion tank (3-7) by pipeline；No. 4 second processing rooms bottom (3-1) is equipped with and takes acid tube
(3-10)；
Separate tank processing system (4) is equipped with the knockout drum (4-1) of filter plate by poly-aluminium synthesis tank, two bottoms and a third is handled
Room (4-3) composition；Knockout drum (4-1) and third process chamber (4-3) are connected by rapid mixing chamber (4-2)；
First charging aperture (4-11) at the top of knockout drum (4-1) is connected with the second gathering tube (1-11)；At the top of knockout drum (4-1)
Second charging aperture (4-12) connect with acid tube (3-10) is taken by pipeline, the 3rd pH regulation device is equipped in knockout drum (4-1)
(4-13)；
The 4th online pH regulation device (4-21), agitating device (4-22) and ultrasonic mixing dress are equipped in rapid mixing chamber (4-2)
Set (4-23)；
Third process chamber is diagonally divided into two parts by the 5th grid (4-31) in third process chamber (4-3), at third
It manages and is equipped with the 5th pH regulation device (4-32) in room (4-3).
2. a kind of lignite process equipment as described in claim 1, it is characterised in that ladder (2-6) water in alkali pool processing system (2)
Flat length 30cm.
3. a kind of lignite process equipment as described in claim 1, it is characterised in that the first alkali pool (2- in alkali pool processing system (2)
1) it is designed using ramp type, slope angle with horizontal plane is 5 degree.
4. a kind of lignite process equipment as claimed in claim 1 or 3, it is characterised in that the first stirring in lignite processing unit (1)
4 stirring blades (1-61) are uniformly distributed on paddle (1-6).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810970455.4A CN109337726B (en) | 2018-08-24 | 2018-08-24 | A kind of lignite process equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810970455.4A CN109337726B (en) | 2018-08-24 | 2018-08-24 | A kind of lignite process equipment |
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| Publication Number | Publication Date |
|---|---|
| CN109337726A CN109337726A (en) | 2019-02-15 |
| CN109337726B true CN109337726B (en) | 2019-06-04 |
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|---|---|---|---|
| CN201810970455.4A Expired - Fee Related CN109337726B (en) | 2018-08-24 | 2018-08-24 | A kind of lignite process equipment |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103804076A (en) * | 2014-01-21 | 2014-05-21 | 中国农业科学院农业资源与农业区划研究所 | Method for separating humic acid in pH mode and application thereof |
| CN105461758A (en) * | 2015-11-18 | 2016-04-06 | 河南理工大学 | A method of increasing a humic acid extraction ratio from brown coal |
| CN106946327A (en) * | 2017-03-13 | 2017-07-14 | 苏州顶裕生物科技有限公司 | A kind of modified humic acid flocculant and preparation method thereof |
-
2018
- 2018-08-24 CN CN201810970455.4A patent/CN109337726B/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103804076A (en) * | 2014-01-21 | 2014-05-21 | 中国农业科学院农业资源与农业区划研究所 | Method for separating humic acid in pH mode and application thereof |
| CN105461758A (en) * | 2015-11-18 | 2016-04-06 | 河南理工大学 | A method of increasing a humic acid extraction ratio from brown coal |
| CN106946327A (en) * | 2017-03-13 | 2017-07-14 | 苏州顶裕生物科技有限公司 | A kind of modified humic acid flocculant and preparation method thereof |
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| CN109337726A (en) | 2019-02-15 |
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