CN207142844U - A kind of system of hydrochloric acid method treated coal ash production aluminum oxide - Google Patents
A kind of system of hydrochloric acid method treated coal ash production aluminum oxide Download PDFInfo
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- CN207142844U CN207142844U CN201720812192.5U CN201720812192U CN207142844U CN 207142844 U CN207142844 U CN 207142844U CN 201720812192 U CN201720812192 U CN 201720812192U CN 207142844 U CN207142844 U CN 207142844U
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Abstract
The utility model discloses a kind of system of hydrochloric acid method treated coal ash production aluminum oxide, including stripping equipment, flashing apparatus, mixing channel, subsider, refined filtration unit, iron-removing unit, deliming unit, evaporative crystallization unit, roasting unit, washing unit, it is characterised in that：Also include upgrading unit.System of the present utility model improves AlCl in solution by increasing upgrading unit on the basis of existing system3Concentration, the efficiency of resin deliming unit in aluminum oxide preparation process is improved, the usage amount of resin is reduced, improves economic benefit.
Description
Technical field
The utility model belongs to coal chemical technology, is related to a kind of system of hydrochloric acid method treated coal ash production aluminum oxide.
Background technology
The master operation of hydrochloric acid method treated coal ash production aluminum oxide is dispensing, dissolution, separating, washing, removal of impurities, steaming successively
Hair crystallization, roasting and acid recovery.Specifically, system flow as shown in Figure 1, it is to match somebody with somebody flyash and hydrochloric acid by a certain percentage
Material, the dissolved mineral slurry of aluminium chloride is included using the dissolution of stripping equipment 1 under certain temperature and pressure；Then dissolved mineral slurry is by dodging
Steam equipment 2 and further improve AlCl therein3Concentration, obtain flashing ore pulp；Flash distillation ore pulp enters dilution trap 3 '；Subsider 4
The overflow that underflow enters the first order sink that washing unit 10 obtains is mixed to get dilution in dilution trap 3 ' with flash distillation ore pulp
Liquid；Dilution is settled into subsider 4, obtains the underflow of subsider 4 and the overflow of subsider 4, and the underflow of subsider 4 is entered
Enter washing unit 10 to be washed, the overflow of subsider 4 enters iron-removing unit 6, deliming unit 7 after refined filtration unit 5, then passes through
Evaporative crystallization unit 8, roasting unit 9, finally give aluminum oxide.As shown in figure 1, the hydrochloric acid method treated coal ash life of prior art
The overflow for producing first order sink in the system of aluminum oxide directly mixes with the flash distillation ore pulp of flashing apparatus 2 in dilution trap 3 ',
Cause AlCl in ore pulp3Dilution, in addition, the condensed water evaporated in evaporative crystallization unit 8 also enter washing unit 10 in,
This also results in AlCl in slurry3It is diluted.
From high concentration Al by the way of resin adsorption in hydrochloric acid method production alumina process3+It is miscellaneous that Fe, Ca are removed in ore pulp
Matter ion.Using the method for resin deliming, Ca in its solution that discharges2+Concentration can be reduced to 0.05g/L, meet that acid oxidation aluminium is given birth to
The requirement of production.Pilot plant test research shows：High AlCl3The performance of removal of the deliming resin to calcium ion is more excellent under concentration.
At present, acid oxidation aluminium production separating, washing process has used for reference the mode of alkaline process aluminum oxide, in dissolution process ore pulp
AlCl3Concentration is by 280~350g/L, using white in secondary air cooling condensate washing and depositing system caused by evaporative crystallization process
Mud, first order washing overflow is returned into dilution so that AlCl in solution3Concentration is reduced to 220g/L, causes deliming resin to reach
To peak efficiency.Therefore need to be by improving AlCl in solution3Concentration further optimizes the disposal ability of resin deliming system, reduces
Deliming resin demand, reduce investment and operating cost.
Utility model content
The purpose of this utility model is to provide a kind of system of hydrochloric acid method treated coal ash production aluminum oxide, existing to solve
The problem of technology.
The utility model provides a kind of system of hydrochloric acid method treated coal ash production aluminum oxide, including stripping equipment, flash distillation
Equipment, mixing channel, subsider, refined filtration unit, iron-removing unit, deliming unit, evaporative crystallization unit, roasting unit, washing unit,
Also include upgrading unit；The stripping equipment is used to obtain the progress dissolution of the mixture of flyash and hydrochloric acid comprising aluminium chloride
Dissolved mineral slurry；The flashing apparatus is used to be flashed the dissolved mineral slurry to obtain flash distillation ore pulp；The mixing channel is used to connect
Receive and mix the low temperature concentrate of the flash distillation ore pulp and the upgrading unit；The subsider is used to settle the mixing channel
Mixed liquor；The refined filtration unit, iron-removing unit, deliming unit, evaporative crystallization unit, roasting unit are sequentially connected by pipeline and connect
The overflow of subsider is received, finally gives aluminum oxide；The washing unit is used for the washing of the underflow of subsider, discharges white clay；Institute
State upgrading unit to be used to the overflow of the washing unit being concentrated to give low temperature concentrate, upgrading unit is condensed by pipeline
Water is back to the washing unit.
Preferably, the washing unit is countercurrent washing groove.
Preferably, the countercurrent washing groove is multi-stage countercurrent sink, level sink last by pipeline with it is described
Upgrading unit is connected to receive the condensed water of upgrading unit, and first order sink passes through other pipeline and the upgrading unit
It is connected to its overflow being passed through the upgrading unit.
Preferably, the multi-stage countercurrent sink is six stage countercurrent sinks, and the six stage countercurrents sink is in underflow side
Upwards according to first order sink, second level sink, third level sink, fourth stage sink, level V sink and
The order of six grades of sinks is sequentially connected by pipeline, according to the 6th grade of sink, level V sink, on overflow direction
Level Four sink, third level sink, the order of second level sink and first order sink are sequentially connected by pipeline.
Preferably, the upgrading unit is triple effect following current enrichment facility or three-effect counter flow enrichment facility.
Preferably, the refined filtration unit is sandfiltration pot and/or plate and frame filter press.
Preferably, the iron-removing unit is resin iron-removing unit.
Preferably, the deliming unit is resin deliming unit.
Preferably, the evaporative crystallization unit is triple effect following current enrichment facility or three-effect counter flow enrichment facility.
Preferably, the roasting unit is fluidized-solids roaster or rotary kiln.
The system of hydrochloric acid method treated coal ash production aluminum oxide of the present utility model on the basis of existing technology, adds
The upgrading unit of thickening and washing unit overflow, has obtained following technique effect：
1st, the overflow of washing unit is concentrated by upgrading unit, by the flash distillation of obtained low temperature concentrate and flashing apparatus
Ore pulp mixes, and reduces slurry temperature, makes flocculant because temperature is higher during subsider sedimentation separation so as to solve
Denaturation, the problem of finally causing effect of settling undesirable.
2nd, upgrading unit improves AlCl in solution3Concentration, low temperature concentrate mix not with the flash distillation ore pulp of flashing apparatus
Ore pulp can be diluted, improve AlCl in solution3Concentration, not only reduce the energy consumption in evaporative crystallization process, Er Qieke
To improve the service efficiency of deliming resin.
3rd, the secondary air cooling condensate of upgrading unit is used to wash the white clay that separation sedimentation obtains, whole separation sedimentation in-process
Water is not introduced into, whole process does not introduce other impurities without outer row's material yet.
Brief description of the drawings
Fig. 1 is the system that the hydrochloric acid method treated coal ash of prior art produces aluminum oxide.
Fig. 2 is the system that hydrochloric acid method treated coal ash of the present utility model produces aluminum oxide.
Fig. 3 is six stage countercurrent sinks 10 in the system of hydrochloric acid method treated coal ash of the present utility model production aluminum oxide
Schematic diagram.
Embodiment
The utility model is described in further detail with reference to accompanying drawing 2 and following embodiment, but it is of the present utility model
Content not limited to this.
A kind of embodiment of the system of hydrochloric acid method treated coal ash production aluminum oxide of the present utility model includes：Dissolution is set
Standby 1, flashing apparatus 2, mixing channel 3, subsider 4, refined filtration unit 5, iron-removing unit 6, deliming unit 7, evaporative crystallization unit 8, roasting
Burn unit 9, washing unit 10, in addition to upgrading unit 11；Stripping equipment 1 is used for the progress of the mixture of flyash and hydrochloric acid is molten
Go out to obtain the dissolved mineral slurry for including aluminium chloride；Flashing apparatus 2 is used to be flashed the dissolved mineral slurry to obtain flash distillation ore pulp；It is mixed
Close the low temperature concentrate that groove 3 is used to receiving and mixing the flash distillation ore pulp and upgrading unit 11；Subsider 4 is used to settle mixing channel
3 mixed liquor；Refined filtration unit 5, iron-removing unit 6, deliming unit 7, evaporative crystallization unit 8, roasting unit 9 are connected successively by pipeline
The overflow of subsider 4 is received, finally gives aluminum oxide；Washing unit 10 is used for the underflow of washing settling groove 4, is discharged after washing
White clay；Upgrading unit 11 is used to the overflow of washing unit 10 being concentrated to give low temperature concentrate, and upgrading unit 11 will by pipeline
Condensed water is back to washing unit 10.
Washing unit 10 can be countercurrent washing groove, preferably multi-stage countercurrent sink, as Pyatyi countercurrent washing groove, six grades
Countercurrent washing groove.In the present embodiment, the washing unit 10 used is six stage countercurrent sinks, as shown in figure 3, six stage countercurrents
Sink is on underflow direction according to first order sink 101, second level sink 102, third level sink 103, the fourth stage
The order of sink 104, level V sink 105 and the 6th grade of sink 106 is sequentially connected by pipeline, on overflow direction
Washed according to the 6th grade of sink 106, level V sink 105, fourth stage sink 104, third level sink 103, the second level
The order for washing groove 102 and first order sink 101 is sequentially connected by pipeline.
Upgrading unit 11 can be triple effect following current enrichment facility or three-effect counter flow enrichment facility.In the present embodiment, make
Upgrading unit 11 is triple effect following current enrichment facility.
Refined filtration unit 5 can be sandfiltration pot or plate and frame filter press, and both can also be selected to combine.In the present embodiment,
The refined filtration unit 5 used is plate and frame filter press.
Iron-removing unit 6 can be resin iron-removing unit.
Deliming unit 7 can be resin deliming unit.
Evaporative crystallization unit 8 can be triple effect following current enrichment facility or three-effect counter flow enrichment facility.In the present embodiment,
The evaporative crystallization unit 8 used is triple effect following current enrichment facility.
Roasting unit 9 can be fluidized-solids roaster or rotary kiln.In the present embodiment, the roasting unit 9 used is
Fluidized-solids roaster.
The course of work of the system of hydrochloric acid method treated coal ash of the present utility model production aluminum oxide is：
Flyash and hydrochloric acid dissolution in stripping equipment 1 are obtained into dissolved mineral slurry, make aluminium in flyash and hydrochloric acid abundant
React for AlCl3.Dissolved mineral slurry is passed through flashing apparatus 2, makes the reduction of its temperature, obtains flashing ore pulp (under high temperature, condition of high voltage
Dissolved mineral slurry enter in the lower container of pressure, because its boiling point reduces, partially liq vaporization, so as to improve dissolved mineral slurry
In AlCl3Concentration).(the flash distillation ore pulp is solidliquid mixture to the flash distillation ore pulp of flashing apparatus 2, and its liquid phase ingredient is mainly
AlCl3And impurity F eCl3、FeCl2、CaCl2Deng；Solid-phase component is mainly SiO2And fail the aluminium of dissolution) concentrated with triple effect following current
Low temperature concentrate derived from the outlet 1 of device 11 is mixed to get mixed liquor in mixing channel 3, and temperature further reduces.Mixed liquor
Into after subsider 4, flocculant is added, makes solid matter Accelerated subsidence, the overflow of subsider 4 sequentially enters follow-up sheet frame pressure
Filter 5 removes the micro floating material in solution, resin iron-removing unit 6, resin deliming unit 7, triple effect following current enrichment facility 8, stream
Change bed roaster 9, finally give aluminum oxide；The underflow of subsider 4 enters six stage countercurrent sinks 10, finally discharges white clay；The
The overflow of one-level sink 101 enters triple effect following current enrichment facility 11 and carries out low temperature concentration, obtains low temperature concentrate, concentrates simultaneously
Afterwards, AlCl3Concentration raises.Low temperature concentrate is mixed with the flash distillation ore pulp of flashing apparatus 2 in mixing channel 3, obtains mixed liquor,
Into subsider 4.Condensed water derived from the outlet 2 of triple effect following current enrichment facility 11 returns to the 6th grade of sink by pipeline.
Embodiment 1,
1st, dissolution：Flyash and mass fraction are pressed 1 for 20%~30% hydrochloric acid:3~1:5 (tons：m3) ratio mix
Dispensing is closed, through stripping equipment 1 under conditions of 130~170 DEG C of temperature, 0.5~0.7MPa of pressure, dissolution time 1.5~3 hours
Dissolution, the aluminium in flyash is set fully to be reacted for AlCl with hydrochloric acid3。
2nd, flash：Dissolved mineral slurry after dissolution is entered into flashing apparatus 2, its temperature is reduced to 90~110 DEG C.High temperature,
Dissolved mineral slurry under condition of high voltage enters in the lower container of pressure, because its boiling point reduces, partially liq vaporization, so as to improve
AlCl in dissolved mineral slurry3Concentration.
3rd, mix：(the flash distillation ore pulp is solidliquid mixture to the flash distillation ore pulp of flashing apparatus 2, and its liquid phase ingredient is mainly
AlCl3And impurity F eCl3、FeCl2、CaCl2Deng；Solid-phase component is mainly SiO2And fail the aluminium of dissolution) with step 5 obtain three
Imitate 40~60 DEG C, AlCl of the outlet 1 of following current enrichment facility 113280~320g/L of concentration low temperature concentrate is in mixing channel 3
Mixed liquor is mixed to get, temperature is further reduced to 80~100 DEG C.
4th, solid-liquid sedimentation separation：
Sedimentation：After the mixed liquor that step 3 obtains enters subsider 4, PAMC CPAM flocculants, control are added
The addition of flocculant processed is 0.05~0.2kg/t- extra dry white wine mud, makes solid matter Accelerated subsidence, the overflow of subsider 4 is entered successively
Enter the micro floating material in the follow-up removal solution of plate and frame filter press 5, the iron removaling of resin iron-removing unit 6, resin deliming unit 7 removes
Calcium, the evaporative crystallization of triple effect following current enrichment facility 8, fluidized-solids roaster 9 are calcined, and finally give aluminum oxide.
Washing：The underflow of subsider 4 enters six stage countercurrent sinks 10, and the first order to the 6th grade of sink adds anion
Polyacrylamide HPAM flocculants, each sink addition are 0.01~0.1kg/t- extra dry white wine mud.The underflow of subsider 4 and the
The overflow mixing of two level sink 102, into first order sink 101；The overflow of first order sink 101 enters triple effect following current
Enrichment facility 11, the underflow of first order sink 101 are mixed into second level sink with the overflow of third level sink 103
102；The underflow of second level sink 102 is mixed into third level sink 103 with the overflow of fourth stage sink 104；3rd
The level underflow of sink 103 is mixed into fourth stage sink 104 with the overflow of level V sink 105；Fourth stage sink
104 underflow and the overflow of the 6th grade of sink 106 are mixed into level V sink 105；The underflow of level V sink 105
The condensed water of the outlet of triple effect following current enrichment facility 11 2 with returning to the 6th grade of sink 106 by pipeline is mixed into the 6th grade
Sink；The underflow of 6th grade of sink is arranged after plate-frame filtering outside white clay, and overflow enters level V sink 105.
5th, concentrate：The overflow of first order sink 101 enters triple effect following current enrichment facility 11, using system of three-effect downstream evaporator
The overflow of mode (that is, triple effect concentrates) to first order sink 101 concentrates, and obtains the low temperature that temperature is 40~60 DEG C and concentrates
Liquid, while after concentration, AlCl3Concentration is increased to low temperature concentration by about 90~150g/L in the overflow of first order sink 101
280~320g/L in liquid.Low temperature concentrate mixes through the export of outlet 1 with the flash distillation ore pulp of flashing apparatus 2 in mixing channel 3,
Mixed liquor is obtained, into subsider 4.The condensed water of triple effect following current enrichment facility 11 returns to the 6th through the export of outlet 2 by pipeline
Level sink.
Pass through AlCl in the overflow of this method subsider 43Concentration is 310g/L, and floating material content is relatively low, and it can not only expire
Sufficient resin deliming system is to AlCl in solution3The requirement (it is required that being >=240g/L) of content, the efficiency of deliming resin is improved, and
And the energy consumption of evaporative crystallization process can be reduced.On the other hand, settling temperature is suitable in subsider, and the solid sedimentation time shorten to
30min。
Comparative example 1,
Filled using present in prior art as shown in figure 1, only lacking triple effect following current concentration compared with the utility model
11 are put, but the hydrochloric acid method treated coal ash that the overflow of first order sink 101 is directly back to dilution trap 3 ' produces oxidation
The system of aluminium, the experiment of above-described embodiment 1, AlCl in the overflow of obtained subsider 4 are carried out under the same conditions3Concentration is
200-220g/L, it can not meet resin deliming system to AlCl in solution3The requirement of content, on the other hand, due to subsider 4
In settling temperature it is of a relatively high, the solid sedimentation time is 60-120min.
Claims (10)
1. a kind of system of hydrochloric acid method treated coal ash production aluminum oxide, including stripping equipment, flashing apparatus, mixing channel, sedimentation
Groove, refined filtration unit, iron-removing unit, deliming unit, evaporative crystallization unit, roasting unit, washing unit, it is characterised in that：Also wrap
Include upgrading unit；The stripping equipment is used for the dissolution that the progress dissolution of the mixture of flyash and hydrochloric acid is obtained including to aluminium chloride
Ore pulp；The flashing apparatus is used to be flashed the dissolved mineral slurry to obtain flash distillation ore pulp；The mixing channel is used to receive simultaneously
Mix the low temperature concentrate of the flash distillation ore pulp and the upgrading unit；The subsider is used for the mixing for settling the mixing channel
Liquid；The refined filtration unit, iron-removing unit, deliming unit, evaporative crystallization unit, roasting unit are sequentially connected reception by pipeline and sunk
The overflow of groove is dropped, finally gives aluminum oxide；The washing unit is used for the washing of the underflow of subsider, discharges white clay；It is described dense
Contracting unit is used to the overflow of the washing unit being concentrated to give low temperature concentrate, and upgrading unit is returned its condensed water by pipeline
It is back to the washing unit.
2. the system of hydrochloric acid method treated coal ash production aluminum oxide according to claim 1, it is characterised in that：The washing
Unit is countercurrent washing groove.
3. the system of hydrochloric acid method treated coal ash production aluminum oxide according to claim 2, it is characterised in that：The adverse current
Sink is multi-stage countercurrent sink, and level sink last is connected to receive concentration by pipeline and the upgrading unit
The condensed water of unit, first order sink are connected to its overflow being passed through described by other pipeline and the upgrading unit
Upgrading unit.
4. the system of hydrochloric acid method treated coal ash production aluminum oxide according to claim 3, it is characterised in that：The multistage
Countercurrent washing groove is six stage countercurrent sinks.
5. the system of the hydrochloric acid method treated coal ash production aluminum oxide according to claim any one of 1-4, it is characterised in that：
The upgrading unit is triple effect following current enrichment facility or three-effect counter flow enrichment facility.
6. the system of the hydrochloric acid method treated coal ash production aluminum oxide according to claim any one of 1-4, it is characterised in that：
The refined filtration unit is sandfiltration pot and/or plate and frame filter press.
7. the system of the hydrochloric acid method treated coal ash production aluminum oxide according to claim any one of 1-4, it is characterised in that：
The iron-removing unit is resin iron-removing unit.
8. the system of the hydrochloric acid method treated coal ash production aluminum oxide according to claim any one of 1-4, it is characterised in that：
The deliming unit is resin deliming unit.
9. the system of the hydrochloric acid method treated coal ash production aluminum oxide according to claim any one of 1-4, it is characterised in that：
The evaporative crystallization unit is triple effect following current enrichment facility or three-effect counter flow enrichment facility.
10. the system of the hydrochloric acid method treated coal ash production aluminum oxide according to claim any one of 1-4, its feature exist
In：The roasting unit is fluidized-solids roaster or rotary kiln.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720812192.5U CN207142844U (en) | 2017-07-06 | 2017-07-06 | A kind of system of hydrochloric acid method treated coal ash production aluminum oxide |
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| CN201720812192.5U CN207142844U (en) | 2017-07-06 | 2017-07-06 | A kind of system of hydrochloric acid method treated coal ash production aluminum oxide |
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| CN207142844U true CN207142844U (en) | 2018-03-27 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109811371A (en) * | 2019-01-05 | 2019-05-28 | 沈阳工业大学 | A kind of method that low-grade bauxite resource prepares alusil alloy |
| CN111661859A (en) * | 2020-07-10 | 2020-09-15 | 中铝山东工程技术有限公司 | Evaporation and dissolution integrated process equipment and process flow thereof |
-
2017
- 2017-07-06 CN CN201720812192.5U patent/CN207142844U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109811371A (en) * | 2019-01-05 | 2019-05-28 | 沈阳工业大学 | A kind of method that low-grade bauxite resource prepares alusil alloy |
| CN111661859A (en) * | 2020-07-10 | 2020-09-15 | 中铝山东工程技术有限公司 | Evaporation and dissolution integrated process equipment and process flow thereof |
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