CN107399745A - A kind of Cymag power production system and production method - Google Patents
A kind of Cymag power production system and production method Download PDFInfo
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- CN107399745A CN107399745A CN201710724005.2A CN201710724005A CN107399745A CN 107399745 A CN107399745 A CN 107399745A CN 201710724005 A CN201710724005 A CN 201710724005A CN 107399745 A CN107399745 A CN 107399745A
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- MNWBNISUBARLIT-UHFFFAOYSA-N sodium cyanide Chemical compound [Na+].N#[C-] MNWBNISUBARLIT-UHFFFAOYSA-N 0.000 title claims abstract description 82
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 39
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 39
- LELOWRISYMNNSU-UHFFFAOYSA-N hydrogen cyanide Chemical compound N#C LELOWRISYMNNSU-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000002425 crystallisation Methods 0.000 claims abstract description 31
- 230000008025 crystallization Effects 0.000 claims abstract description 31
- 238000004806 packaging method and process Methods 0.000 claims abstract description 21
- 239000000843 powder Substances 0.000 claims abstract description 18
- 238000007493 shaping process Methods 0.000 claims abstract description 18
- 238000001704 evaporation Methods 0.000 claims abstract description 16
- 238000007599 discharging Methods 0.000 claims abstract description 15
- 239000006096 absorbing agent Substances 0.000 claims abstract description 14
- 230000008020 evaporation Effects 0.000 claims abstract description 9
- 238000004891 communication Methods 0.000 claims abstract description 5
- 239000010413 mother solution Substances 0.000 claims abstract description 5
- 238000004064 recycling Methods 0.000 claims abstract description 5
- 239000000463 material Substances 0.000 claims description 105
- 238000006243 chemical reaction Methods 0.000 claims description 48
- 239000007788 liquid Substances 0.000 claims description 37
- 239000000243 solution Substances 0.000 claims description 34
- 239000007789 gas Substances 0.000 claims description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- 238000001816 cooling Methods 0.000 claims description 19
- 239000012452 mother liquor Substances 0.000 claims description 19
- 239000002245 particle Substances 0.000 claims description 18
- 238000011084 recovery Methods 0.000 claims description 18
- 239000000047 product Substances 0.000 claims description 15
- 238000001035 drying Methods 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 11
- 239000000203 mixture Substances 0.000 claims description 10
- 239000006228 supernatant Substances 0.000 claims description 10
- 239000012141 concentrate Substances 0.000 claims description 9
- 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 claims description 8
- 239000012071 phase Substances 0.000 claims description 8
- 229910052708 sodium Inorganic materials 0.000 claims description 8
- 239000011734 sodium Substances 0.000 claims description 8
- 230000007246 mechanism Effects 0.000 claims description 7
- 238000012544 monitoring process Methods 0.000 claims description 6
- 238000010025 steaming Methods 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 5
- 230000008859 change Effects 0.000 claims description 4
- 238000007701 flash-distillation Methods 0.000 claims description 4
- 238000006386 neutralization reaction Methods 0.000 claims description 4
- 239000008710 crystal-8 Substances 0.000 claims description 3
- 238000011049 filling Methods 0.000 claims description 3
- 239000007792 gaseous phase Substances 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 239000011261 inert gas Substances 0.000 claims description 3
- 238000002156 mixing Methods 0.000 claims description 2
- 239000003826 tablet Substances 0.000 claims 5
- 239000013078 crystal Substances 0.000 claims 2
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 claims 2
- 239000007932 molded tablet Substances 0.000 claims 1
- 239000001301 oxygen Substances 0.000 claims 1
- 229910052760 oxygen Inorganic materials 0.000 claims 1
- 230000002093 peripheral effect Effects 0.000 claims 1
- 230000008901 benefit Effects 0.000 abstract description 4
- 238000000034 method Methods 0.000 description 17
- 230000008569 process Effects 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 238000005119 centrifugation Methods 0.000 description 3
- KXZJHVJKXJLBKO-UHFFFAOYSA-N chembl1408157 Chemical compound N=1C2=CC=CC=C2C(C(=O)O)=CC=1C1=CC=C(O)C=C1 KXZJHVJKXJLBKO-UHFFFAOYSA-N 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000002000 scavenging effect Effects 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 238000009987 spinning Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000003905 agrochemical Substances 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- KDFQYGBJUYYWDJ-UHFFFAOYSA-N azane;sodium Chemical compound N.[Na] KDFQYGBJUYYWDJ-UHFFFAOYSA-N 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000009713 electroplating Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 231100000004 severe toxicity Toxicity 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000009897 systematic effect Effects 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C3/00—Cyanogen; Compounds thereof
- C01C3/08—Simple or complex cyanides of metals
- C01C3/10—Simple alkali metal cyanides
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
- C01P2006/82—Compositional purity water content
Landscapes
- Health & Medical Sciences (AREA)
- General Health & Medical Sciences (AREA)
- Toxicology (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of Cymag power production system and production method, production system includes reactor, reactor discharging pump, cooler of reactor, evaporation and crystallization system, centrifugal separator, flash dryer, cyclone separator and shaping packaging system, feature：Evaporation and crystallization system includes evaporator, evaporator-condenser, evaporator circulating pump, crystallizer and underflow pump, reactor sets hydrogen cyanide charging aperture and sodium hydroxide charging aperture, reactor by reactor discharging pump respectively with cooler of reactor, top absorber portion and the evaporator connection of reactor, the upper end Recycling Mother Solution inlet communication of cooler of reactor and reactor, evaporator connects with crystallizer, crystallizer is connected by underflow pump with centrifugal separator, centrifugal separator connects with flash dryer, flash dryer connects with cyclone separator, cyclone separator and shaping packaging system connectivity, advantage is：It is simple and reasonable, ensure Cymag powder safety, continue, efficient industrialized production.
Description
Technical field
The present invention relates to Cymag preparation field, more particularly to a kind of Cymag power production system and production method.
Background technology
Cymag is widely used, China's Cymag product be mainly used in the refinement of noble metal and rare metal, chemical industry synthesis,
The fields such as agricultural chemicals, medicine, electroplating industry, Cymag product have solid and liquid two types.Cymag product is produced at present
Process mainly has：Ammonia sodium method, cyanide melt method, iS-One method, methanol ammonoxidation method, acrylonitrile by-product method and light oil cracking method,
But wherein ammonia sodium method, cyanide melt method are eliminated by national explicit order.Flow using acrylonitrile by-product method production Cymag product is big
Cause identical：By the hydrogen cyanide of acrylonitrile installation by-product with after sodium hydroxide neutralization reaction, liquid cyaniding sodium solution being obtained, by steaming
The process such as hair, crystallization, separation, dry, produces Cymag product.
But due to Cymag in heated, ingress of air or under having moisture existence condition, the inflammable hydrogen cyanide of severe toxicity can be produced
Gas, so that Cymag product goes bad, hence in so that the synthesis of Cymag product, evaporative crystallization, separation drying and shaping
Become difficult etc. technical process.And it is existing less for industrialization Sodium Cyanide Production systematic research, and most of production systems
Device structure is complex in system, and the loss of Cymag product is more.
The content of the invention
In order to solve above-mentioned the deficiencies in the prior art, the present invention provides a kind of Cymag power production system and life
Production method, structural manufacturing process advantages of simple, Cymag powder safety can be ensured, continued, efficiently industrialized production.
Technical scheme is used by the present invention solves above-mentioned technical problem：A kind of Cymag power production system, including
Reactor, reactor discharging pump, cooler of reactor, at least one evaporation and crystallization system, centrifugal separator, flash dryer,
Cyclone separator and shaping packaging system, described evaporation and crystallization system include evaporator, evaporator-condenser, evaporator circulation
Pump, crystallizer and underflow pump, described reactor are provided with hydrogen cyanide charging aperture and sodium hydroxide charging aperture, described reactor
Material outlet pass through the material inlet with described cooler of reactor, the described reaction respectively of described reactor discharging pump
The lower end material inlet connection of the top absorber portion and described evaporator of device, the material outlet of described cooler of reactor
With the upper end Recycling Mother Solution inlet communication of described reactor, the bottom material outlet of described evaporator and described crystallizer
The connection of upper end material inlet, the head gas outlet and the gas feed of described evaporator-condenser of described evaporator connect
Logical, the supernatant liquor outlet of described crystallizer is connected with adjustment tank, and the middle level liquid of described crystallizer is exported by described
Evaporator circulating pump connects with the material inlet of described evaporator, and lower floor's underflow material of described crystallizer passes through described dense
Stock pump is delivered to the material inlet of described centrifugal separator, and the material outlet of described centrifugal separator is done with described flash distillation
The material inlet connection of dry machine, the bottom of described flash dryer is provided with the pulverizer being connected, described expansion drying
The top material outlet of machine connects with the material inlet of described cyclone separator, and the bottom material of described cyclone separator goes out
Mouth is connected by conveying worm with the material inlet of described shaping packaging system.
What described evaporation and crystallization system also included be connected with described evaporator is used to keep in described evaporator very
The water ring vacuum pump of reciprocal of duty cycle.Thus only evaporated water need to be just can adjust by changing the pressure-regulating valve of water ring vacuum pump, so as to
Control Cymag slurry concentration, and the structure of water ring vacuum pump is simple, and floor space is small, easy-maintaining, and energy consumption is low, blowdown flow rate compared with
It is few.
Described shaping packaging system includes feeder, forming machine, vibratory sieve, cooling feed bin and metering packaging machine, described
The bottom material outlet of cyclone separator connected by conveying worm with the material inlet of described feeder, it is described plus
The material outlet of glassware connects with the material inlet of described forming machine, the material outlet of described forming machine and described vibration
The material inlet connection of sieve, the material outlet of described vibratory sieve connect with the top material inlet of described cooling feed bin, institute
The the first particle outlet for the vibratory sieve stated is connected by hoisting mechanism with the material inlet of described feeder, described cooling material
The bottom material outlet in storehouse connects with described metering packaging machine.
Including dissolving recovery system, the mother liquor outlet of described centrifugal separator and the material of described dissolving recovery system
Inlet communication, the second particle outlet of described vibratory sieve connect with the material inlet of described dissolving recovery system.Thus, it is possible to
The rate of recovery of Cymag is enough improved, reduces and wastes.
Described centrifugal separator uses reciprocating centrifugal separator.Thus, it is possible to continuous feed and discharging, its feed and
Load is controlled by inlet valve completely, reduces scavenging period and the loss of unnecessary product.
Cooling heat exchange device is provided with outside described reactor, multi-layer rotational flow piece is set in described flash dryer.By
This can remove reaction heat to the further cooling of reactor；And multi-layer rotational flow piece is set to form relatively stable fluidised form
Change bed, while spinning disk also plays a part of residence time and classification necessary to ensureing to dry.
A kind of Cymag power production method, comprises the following steps：
1. liquid hydrogen cyanide is pressed into 1.2~1.5m/s by 1~1.8m/s flow velocity, the sodium hydroxide solution that concentration is 30~60%
Flow velocity be continuously introduced into respectively in reactor, carry out mixing complete neutralization reaction, Cymag reaction solution is obtained, wherein in reactor
Operating pressure is normal pressure, and filling gas is inert gas, and reactor temperature is kept for 30~60 DEG C, reacts liquid level in reactor
Highly maintain 65%~85%, the concentration of sodium hydroxide is 0.5%~5% in reaction solution；
2. extracting part Cymag reaction solution from reactor according to 35~75t/h flow using reactor discharging pump, and make
1~8m/s flow velocity is kept in reactor, the part Cymag reaction solution is distinguished into circulation conveying to reactor absorber portion, reaction
In device cooler and evaporator, wherein cooler of reactor is delivered in reactor again after being cooled down to Cymag reaction solution
As reaction mother liquor, the circular flow of reactor absorber portion is 10~35t/h, and the circular flow of reaction mother liquor is 10~45t/h；
3. the step Cymag reaction solution that 2. middle conveying comes is entered from the material inlet of evaporator lower end, by the heating of evaporator
Steam is passed through in cylinder, Cymag reaction solution is carried out to be evaporated in vacuo removing moisture, obtains gas phase and Cymag concentrate, cyaniding
Sodium concentrate falls into crystallizer from the material outlet of evaporator bottom, and gas phase enters evaporator from the gaseous phase outlet on evaporator top
Condenser, the fixed gas of evaporator-condenser are evacuated to exhaust treatment system by vavuum pump, wherein keeping steaming by water ring vacuum pump
Evaporating pressure in hair device is 25~40mmHg, and evaporating temperature is 30~50 DEG C, and evaporated water is 2000~2800kg/h；
4. after Cymag concentrate is stopped into 1~10 hour in crystallizer, be layered as supernatant liquor, middle level particulate liquid and under
Layer underflow liquid, supernatant liquor overflow to adjustment tank, material inlet of the middle level particulate liquid by evaporator circulating pump from evaporator
Return in evaporator and be used as nucleus, and circulated with this, keep the Cymag reaction solution supersaturation in evaporator, lower floor's underflow liquid is led to
Underflow pump output is crossed, wherein crystallization temperature is 30~50 DEG C, and underflow liquid key component includes NaCN crystal 8%~18%, cyaniding
Sodium solution 30%~45% and water 40%~50%；
5. being sent into centrifugal separator after underflow liquid is thickened, moistening crystallization and separation mother liquor are separated into, moistening crystallization is through spiral transferring
Machine is sent to be delivered to flash dryer, wherein centrifuging temperature is 30~45 DEG C, and the moisture for moistening crystallization is 5~10wt%；
It is passed through 6. air is heated to being not less than after 185 DEG C from the bottom of flash dryer, and is formed rotate at a high speed from the bottom to top
Thermal current, after less moistening crystallization is quickly dried in flash dryer, dried powder is obtained, whirlwind is expelled to from top
Separator, larger moistening crystallization fall into the pulverizer of expansion drying motor spindle, rotated together with after crushed with thermal current
Rise and dried, obtain dried powder, be expelled to cyclone separator from top, wherein drying temperature is 45~70 DEG C, xeraphium
Moisture≤the 0.9wt% at end；
7. dried powder is obtained into Cymag powder after cyclone separator separates.
By step 7. in obtained Cymag powder be delivered to feeder through conveying worm, be then sent in forming machine and press
System, the tablet mixture including shaping tablet and particle is obtained after compacting, will after tablet mixture is delivered into vibratory sieve
First particle outlet of the particle through vibratory sieve is recycled in feeder by hoisting mechanism re-starts compacting, by shaping tablet through shaking
The material outlet of dynamic sieve enters metering packaging machine after falling into cooling feed bin cooling, obtains Cymag product.
Tablet mixture includes block, after tablet mixture is delivered into vibratory sieve, by block through vibratory sieve
The outlet of second particle is delivered to dissolving recovery system, by step 5. in obtained separation mother liquor be delivered to after gas-liquid separator it is molten
Solve recovery system.
To hydrogen cyanide flow, sodium hydroxide flow, the circular flow of reactor absorber portion, reaction mother liquor circular flow,
The pressure in circular flow and reactor in reactor is monitored in real time, is entered if closing hydrogen cyanide when monitoring to occur exception
Expect valve；The thing position of temperature in flash dryer and pressure, the thing position of cyclone separator and feeder is monitored in real time, together
When the working condition of conveying worm, feeder and forming machine is monitored in real time, if stop when monitoring to occur exception from
Centrifugal separator is fed.
Compared with prior art, the advantage of the invention is that：Whole operation system structure simple and compact, production technology obtain
Largely simplify, efficient energy-saving；In the stage of reaction, maintain to carry out in the basic conditions all the time, can effectively prevent hydrogen cyanide
Generation autohemagglutination；Keep evaporating required vacuum using water ring vacuum pump in evaporation and crystallization system, make total it is compact,
Energy consumption is low, blowdown flow rate is few；There is provided dissolving recovery system can reduce material waste, by setting reaction system and centrifugation to feed
The interlock circuit of system, it can stop reacting or stopping centrifugation charging in time in exception, it is ensured that production security, reduce material
Waste, be advantageous to industrialized production.
Brief description of the drawings
Fig. 1 is a kind of equipment flowsheet of Cymag power production of the present invention.
Wherein, reactor 1, reactor discharging pump 2, cooler of reactor 3, evaporator 4, evaporator-condenser 5, evaporator
Circulating pump 6, crystallizer 7, underflow pump 8, centrifugal separator 9, flash dryer 10, cyclone separator 11, feeder 12, forming machine
13, vibratory sieve 14, cooling feed bin 15, metering packaging machine 16, reactor absorber portion 17, cyclone 18, the first conveying worm 19,
Air blower 20, heater 21, pulverizer 22, the second conveying worm 23, hoisting mechanism 24, dissolve recovery system 25.
Embodiment
A kind of the Cymag power production system and production method of the present invention are made further specifically below in conjunction with accompanying drawing
It is bright but not as a limitation of the invention.
As shown in figure 1, a kind of Cymag power production system, mainly includes reactor 1, reactor discharging pump 2, reactor
Cooler 3, evaporator 4, evaporator-condenser 5, evaporator circulating pump 6, crystallizer 7, underflow pump 8, centrifugal separator 9, flash distillation
Drying machine 10, cyclone separator 11 and shaping packaging system.
In reaction process, reactor 1 is provided with hydrogen cyanide charging aperture and sodium hydroxide charging aperture, and the material of reactor goes out
Mouthful by reactor discharging pump 2 respectively the material inlet with cooler of reactor 3, the top of reactor 1 reactor absorber portion 17
And the lower end material inlet connection of evaporator 4, the material outlet of cooler of reactor 3 and the upper end Recycling Mother Solution of reactor 1
Inlet communication.By the forced circulation of reactor discharging pump 2, so that keeping 1~8m/s flow velocity in reactor 1, can make anti-
Raw material is answered to be sufficiently mixed.After the reacted extraction of device discharging pump 2 of Cymag reaction solution is obtained after reaction, a part is directly entered reaction
The reactor absorber portion 17 at the top of device 1, for absorbing unreacted hydrogen cyanide；After a part is cooled down by cooler of reactor 3
Enter from the upper end Recycling Mother Solution import of reactor 1, certain reaction heat can be taken away by circulating a part of mother liquor；Another portion
Cymag reaction solution is divided then to be sent to evaporization process.Cooling heat exchange device is additionally provided with outside reactor 1, can be cooling coil or
Heat exchanger, for further cooling, remove reaction heat.
In evaporative crystallization process, evaporative crystallization process is two sets of systems arranged side by side, in order to more flexible adjustment life
Produce load.The saturation sodium cyanide solution sent from reaction process, enter from the material inlet of two lower ends of evaporator 4 arranged side by side
Enter, the Cymag amount of two evaporators 4 of respectively enteing can be adjusted by regulating valve according to needs of production.Evaporator 4
Bottom material outlet connects with the upper end material inlet of crystallizer 7, and the Cymag concentrate obtained after evaporation falls into phase from bottom
In corresponding crystallizer 7, potential difference is kept by vacuum between crystallizer 7 and evaporator 4.Evaporator 4 head gas outlet with
The gas feed connection of evaporator-condenser 5, the fixed gas of evaporator-condenser 5 are evacuated to exhaust treatment system by vavuum pump.Knot
The supernatant liquor outlet of brilliant device 7 connects with adjustment tank, and the middle level liquid outlet of crystallizer 7 passes through evaporator circulating pump 6 and evaporator 4
Material inlet connection, lower floor's underflow liquid of crystallizer 7 is delivered to separation drying process by underflow pump 8.Evaporation and crystallization system
Also include be connected with evaporator 4 is used to keep the water ring vacuum pump of vacuum in evaporator 4, the suction inlet of water ring vacuum pump and
The gas phase connection of evaporator 4, the outlet of water ring vacuum pump are connected to exhaust treatment system, thus only need to be true by changing water ring
The pressure-regulating valve of empty pump just can adjust evaporated water, so as to control Cymag slurry concentration, and the structure letter of water ring vacuum pump
Single, floor space is small, easy-maintaining, and energy consumption is low, and blowdown flow rate is less.
In drying process is separated, by underflow pump 8 convey Lai underflow liquid after cyclone 18 thickens, pass through centrifugation point
9 material inlet of disembarking enters centrifugal separator 9, and the material outlet of centrifugal separator 9 passes through the first conveying worm 19 with dodging
Steam the material inlet connection of drying machine 10.Centrifugal separator 9 uses reciprocating centrifugal separator, thus, it is possible to continuous feed and goes out
Material, it is fed and load is controlled by inlet valve completely, reduces scavenging period and the loss of unnecessary product.Air blower 20 is inhaled
The heated device 21 of air entered is entered after heating by the air inlet of the lower section of flash dryer 10, and similar spout is formed in king-tower
The high speed swirling eddy of wind, while bottom annular space size is adjusted according to different Cymag material properties, it is in wind speed and compares
Suitable state.Heater 21 can considering according to practice in factory and up-front investment later maintenance expense, select steam to add
Hot device or electric heater, the air themperature after heating are not less than 185 DEG C.The bottom of flash dryer 10 is provided with what is be connected
Pulverizer 22, the crystallization of some bulks moistening are insufficient to allow it broken and rotated at a high speed, fall under gravity because of high velocity air
Crush simultaneously micronized by force into pulverizer 22, then rotate rising in the lump with high velocity air and complete drying process.In order that
Dry while the material final moisture exported reaches extremely low is not influenceed product quality by the fluctuation of initial moisture, dry in flash distillation
Multi-layer rotational flow piece is set in dry machine 10, is consequently formed relatively stable fluidized-bed, while spinning disk also plays guarantee and dries institute
Necessary residence time and the effect of classification.The top material outlet of flash dryer 10 and the material inlet of cyclone separator 11
Connection, cyclone separator 11 are II grade of cyclone separator 11, and twist state rotates material in cyclone separator 11, finished product
Material flows out from the star-shaped discharge valve of bottom, is connected by the second conveying worm 23 with the material inlet of shaping packaging system.
The air-flow of a small amount of residuum retinue top outflow enters exhaust treatment system through air-introduced machine.Using expansion drying system, tool
There is SR small, energy consumption is low, and labor intensity is low, the advantages of good operational environment.
In shaping and metering packing process, shaping packaging system specifically includes feeder 12, forming machine 13, vibratory sieve
14th, feed bin 15 and metering packaging machine 16 are cooled down.The bottom material outlet of cyclone separator 11 by the second conveying worm 23 with
The material inlet connection of feeder 12, the material outlet of feeder 12 connect with the material inlet of forming machine 13, forming machine 13
Material outlet connects with the material inlet of vibratory sieve 14, the top material inlet of the material outlet and cooling feed bin 15 of vibratory sieve 14
Connection, the first particle outlet of vibratory sieve 14 are connected by hoisting mechanism 24 with the material inlet of feeder 12, cool down feed bin 15
Bottom material outlet connected with metering packaging machine 16.
Also include dissolving recovery system 25, mother liquor outlet and the dissolving recovery system 25 of centrifugal separator 9 in the present embodiment
Material inlet connection, vibratory sieve 14 the second particle outlet with dissolving recovery system 25 material inlet connects.
A kind of Cymag power production method, comprises the following steps：1. by liquid hydrogen cyanide by 1~1.8m/s flow velocity,
The sodium hydroxide solution that concentration is 30~60% is continuously introduced into reactor 1 respectively by 1.2~1.5m/s flow velocity, is mixed
Neutralization reaction is completed, obtains Cymag reaction solution.Operating pressure is normal pressure wherein in reactor 1, and filling gas is inert gas,
Be nitrogen in the present embodiment, temperature is kept for 30~60 DEG C in reactor 1, in reactor 1 height of reaction liquid level maintain 65%~
85%, the concentration of sodium hydroxide is 0.5%~5% in reaction solution, and the flow velocity of reaction solution in reactor 1 is 2m/s or so, is thus prevented
Only the fluctuation of hydrogen cyanide inlet amount or local concentration are too high and cause autohemagglutination, produce dangerous.
2. extract part Cymag from reactor 1 according to 35~75t/h flow using reactor discharging pump 2 to react
Liquid, and make the flow velocity that 1~8m/s is kept in reactor 1, the part Cymag reaction solution is distinguished into circulation conveying to reactor and inhaled
Receive in section 17, cooler of reactor 3 and evaporator 4, wherein cooler of reactor 3 Cymag reaction solution is cooled down after again
It is delivered in reactor 1 and is used as reaction mother liquor, the circular flow of reactor absorber portion 17 is 10~35t/h, and reaction mother liquor follows
Circulation is 10~45t/h.
3. the step Cymag reaction solution that 2. middle conveying comes is entered from the material inlet of the lower end of evaporator 4, by evaporator 4
Heating cylinder in be passed through steam, to Cymag reaction solution carry out be evaporated in vacuo remove moisture, obtain gas phase and Cymag concentration
Liquid, Cymag concentrate fall into crystallizer 7, gaseous phase outlet of the gas phase from the top of evaporator 4 from the material outlet of the bottom of evaporator 4
Into evaporator-condenser 5, the fixed gas of evaporator-condenser 5 is evacuated to exhaust treatment system by vavuum pump.Wherein pass through water ring
It is 25~40mmHg that vavuum pump, which keeps the evaporating pressure in evaporator, and evaporating temperature is 30~50 DEG C, evaporated water for 2000~
2800kg/h。
4. after Cymag concentrate is stopped 1~10 hour in crystallizer 7, supernatant liquor, middle level particulate are layered as
Liquid and lower floor's underflow liquid, supernatant liquor overflow to adjustment tank, middle level particulate liquid is by evaporator circulating pump 6 from evaporator 4
Material inlet returns in evaporator 4 and is used as nucleus, and is circulated with this, keeps the Cymag reaction solution supersaturation in evaporator 4, under
Layer underflow liquid is exported by underflow pump 8.Wherein crystallization temperature is 30~50 DEG C, and underflow liquid key component includes NaCN crystal 8%
~18%, sodium cyanide solution 30%~45% and water 40%~50%, the general proportions of material are as follows in crystallizer, supernatant liquor: circulation
With middle particulate liquid: centrifuge and use lower floor underflow liquid=6: 44: 10.
5. being sent into centrifugal separator 9 after underflow liquid is thickened, moistening crystallization and separation mother liquor are separated into, moistening crystallization is through the
One conveying worm 19 is delivered to flash dryer 10, and separation mother liquor is delivered to dissolving recovery system 25 after gas-liquid separator.
Wherein centrifuging temperature is 30~45 DEG C, and the moisture for moistening crystallization is 5~10wt%.
It is passed through, and is formed from the bottom to top high from the bottom of flash dryer 10 6. air is heated to being not less than after 185 DEG C
Speed rotation thermal current, after less moistening crystallization is quickly dried in flash dryer 10, dried powder is obtained, is arranged from top
Go out to cyclone separator 11, larger moistening crystallization is fallen into the pulverizer 22 of the bottom of flash dryer 10, after crushed with heat
Air-flow, which rotates together with, to be risen and is dried, and obtains dried powder, cyclone separator 11 is expelled to from top.Wherein drying temperature is
45~70 DEG C, moisture≤0.9wt% of dried powder.
7. dried powder is obtained into Cymag powder after cyclone separator 11 separates.
By step 7. in obtained Cymag powder be delivered to feeder 12 through the second conveying worm 23, be then sent into
Suppressed in type machine 13, the tablet mixture including shaping tablet, block and particle is obtained after compacting, by tablet mixture
After being delivered to vibratory sieve 14, first particle outlet of the particle through vibratory sieve 14 is recycled to weight in feeder 12 by hoisting mechanism 24
Newly suppressed, second particle outlet of the block through vibratory sieve 14 is delivered to dissolving recovery system 25, by shaping tablet warp
The material outlet of vibratory sieve 14, which is fallen into after cooling feed bin 15 cools down, enters metering packaging machine 16, finally gives Cymag product.
In addition, in reaction process to hydrogen cyanide flow, sodium hydroxide flow, reactor absorber portion 17 circular flow,
Circular flow, the circular flow in reactor 1 and the pressure in reactor 1 of reaction mother liquor are monitored in real time, if monitoring
Hydrogen cyanide inlet valve is closed when generation is abnormal, ensure that the safety in production of Cymag.To dodging in separation, dry and molding procedure
The thing position for steaming the temperature in drying machine 10 and pressure, the thing position of cyclone separator 11 and feeder 12 is monitored in real time, simultaneously
The working condition of heater 21, the second conveying worm 23, feeder 12 and forming machine 13 is monitored in real time, if monitoring
Stop centrifugal separator 9 when generation is abnormal to feed, to reduce material waste, after pending fault releases, then recover centrifugal separator 9 and enter
Material.
It is worth noting that, the foregoing is only presently preferred embodiments of the present invention, the patent of the present invention is not thereby limited
Protection domain, the present invention can also carry out the improvement of material and structure to the construction of above-mentioned various parts, or using skill
Art equivalent is replaced.Therefore it is all with the present invention specification and diagramatic content made equivalent structure change, or directly or
Apply to other correlative technology fields indirectly to be similarly all contained in the range of of the invention cover.
Claims (10)
1. a kind of Cymag power production system, including reactor, reactor discharging pump, cooler of reactor, at least one steaming
Send out crystal system, centrifugal separator, flash dryer, cyclone separator and shaping packaging system, it is characterised in that described steaming
Hair crystal system includes evaporator, evaporator-condenser, evaporator circulating pump, crystallizer and underflow pump, and described reactor is set
Hydrogen cyanide charging aperture and sodium hydroxide charging aperture are equipped with, the material outlet of described reactor passes through described reactor discharging pump
Material inlet with described cooler of reactor, the top absorber portion of described reactor and described evaporator respectively
Lower end material inlet connection, the upper end Recycling Mother Solution import of the material outlet of described cooler of reactor and described reactor
Connection, the bottom material outlet of described evaporator connect with the upper end material inlet of described crystallizer, described evaporator
Head gas outlet connect with the gas feed of described evaporator-condenser, the supernatant liquor of described crystallizer export and
Adjustment tank connects, and the middle level liquid outlet of described crystallizer passes through described evaporator circulating pump and the material of described evaporator
Inlet communication, lower floor's underflow material of described crystallizer are delivered to the material of described centrifugal separator by described underflow pump
Import, the material outlet of described centrifugal separator are connected with the material inlet of described flash dryer, and described flash distillation is done
The bottom of dry machine is provided with the pulverizer being connected, the top material outlet of described flash dryer and described cyclonic separation
The material inlet connection of device, the bottom material outlet of described cyclone separator pass through conveying worm and described shaping packaging
The material inlet connection of system.
A kind of 2. Cymag power production system according to claim 1, it is characterised in that described evaporation and crystallization system
Also include the water ring vacuum pump for keeping vacuum in described evaporator be connected with described evaporator.
A kind of 3. Cymag power production system according to claim 1 or 2, it is characterised in that described shaping packaging system
System includes feeder, forming machine, vibratory sieve, cooling feed bin and metering packaging machine, the bottom material of described cyclone separator and gone out
Mouthful connected by conveying worm with the material inlet of described feeder, the material outlet of described feeder and it is described into
The material inlet connection of type machine, the material outlet of described forming machine connects with the material inlet of described vibratory sieve, described
The material outlet of vibratory sieve connects with the top material inlet of described cooling feed bin, the first particle outlet of described vibratory sieve
Connected by hoisting mechanism with the material inlet of described feeder, the bottom material outlet of described cooling feed bin with it is described
Metering packaging machine connects.
4. a kind of Cymag power production system according to claim 3, it is characterised in that including dissolving recovery system, institute
The mother liquor outlet for the centrifugal separator stated connects with the material inlet of described dissolving recovery system, and the second of described vibratory sieve
Particle outlet connects with the material inlet of described dissolving recovery system.
A kind of 5. Cymag power production system according to claim 1 or 2, it is characterised in that described centrifugal separator
Using reciprocating centrifugal separator.
A kind of 6. Cymag power production system according to claim 1 or 2, it is characterised in that described reactor peripheral hardware
Cooling heat exchange device is equipped with, multi-layer rotational flow piece is set in described flash dryer.
A kind of 7. Cymag power production method, it is characterised in that comprise the following steps：
1. liquid hydrogen cyanide is pressed into 1.2~1.5m/s by 1~1.8m/s flow velocity, the sodium hydroxide solution that concentration is 30~60%
Flow velocity be continuously introduced into respectively in reactor, carry out mixing complete neutralization reaction, Cymag reaction solution is obtained, wherein in reactor
Operating pressure is normal pressure, and filling gas is inert gas, and reactor temperature is kept for 30~60 DEG C, reacts liquid level in reactor
Highly maintain 65%~85%, the concentration of sodium hydroxide is 0.5%~5% in reaction solution；
2. extracting part Cymag reaction solution from reactor according to 35~75t/h flow using reactor discharging pump, and make
1~8m/s flow velocity is kept in reactor, the part Cymag reaction solution is distinguished into circulation conveying to reactor absorber portion, reaction
In device cooler and evaporator, wherein cooler of reactor is delivered in reactor again after being cooled down to Cymag reaction solution
As reaction mother liquor, the circular flow of reactor absorber portion is 10~35t/h, and the circular flow of reaction mother liquor is 10~45t/h；
3. the step Cymag reaction solution that 2. middle conveying comes is entered from the material inlet of evaporator lower end, by the heating of evaporator
Steam is passed through in cylinder, Cymag reaction solution is carried out to be evaporated in vacuo removing moisture, obtains gas phase and Cymag concentrate, cyaniding
Sodium concentrate falls into crystallizer from the material outlet of evaporator bottom, and gas phase enters evaporator from the gaseous phase outlet on evaporator top
Condenser, the fixed gas of evaporator-condenser are evacuated to exhaust treatment system by vavuum pump, wherein keeping steaming by water ring vacuum pump
Evaporating pressure in hair device is 25~40mmHg, and evaporating temperature is 30~50 DEG C, and evaporated water is 2000~2800kg/h；
4. after Cymag concentrate is stopped into 1~10 hour in crystallizer, be layered as supernatant liquor, middle level particulate liquid and under
Layer underflow liquid, supernatant liquor overflow to adjustment tank, material inlet of the middle level particulate liquid by evaporator circulating pump from evaporator
Return in evaporator and be used as nucleus, and circulated with this, keep the Cymag reaction solution supersaturation in evaporator, lower floor's underflow liquid is led to
Underflow pump output is crossed, wherein crystallization temperature is 30~50 DEG C, and underflow liquid key component includes NaCN crystal 8%~18%, cyaniding
Sodium solution 30%~45% and water 40%~50%；
5. being sent into centrifugal separator after underflow liquid is thickened, moistening crystallization and separation mother liquor are separated into, moistening crystallization is through spiral transferring
Machine is sent to be delivered to flash dryer, wherein centrifuging temperature is 30~45 DEG C, and the moisture for moistening crystallization is 5~10wt%；
It is passed through 6. air is heated to being not less than after 185 DEG C from the bottom of flash dryer, and is formed rotate at a high speed from the bottom to top
Thermal current, after less moistening crystallization is quickly dried in flash dryer, dried powder is obtained, whirlwind is expelled to from top
Separator, larger moistening crystallization fall into the pulverizer of expansion drying motor spindle, rotated together with after crushed with thermal current
Rise and dried, obtain dried powder, be expelled to cyclone separator from top, wherein drying temperature is 45~70 DEG C, xeraphium
Moisture≤the 0.9wt% at end；
7. dried powder is obtained into Cymag powder after cyclone separator separates.
A kind of 8. Cymag power production method according to claim 7, it is characterised in that by step 7. in obtained cyanogen
Change sodium powder body and be delivered to feeder through conveying worm, be then sent in forming machine and suppress, obtain including being molded tablet after compacting
With the tablet mixture including particle, after tablet mixture is delivered into vibratory sieve, first particle of the particle through vibratory sieve is gone out
Mouth is recycled in feeder by hoisting mechanism re-starts compacting, and shaping material outlet of the tablet through vibratory sieve is fallen into cooling material
Enter metering packaging machine after the cooling of storehouse, obtain Cymag product.
9. a kind of Cymag power production method according to claim 8, it is characterised in that tablet mixture includes block
Shape thing, after tablet mixture is delivered into vibratory sieve, second particle outlet of the block through vibratory sieve is delivered to dissolving recovery
System, by step 5. in obtained separation mother liquor dissolving recovery system is delivered to after gas-liquid separator.
10. a kind of Cymag power production method according to claim 9, it is characterised in that to hydrogen cyanide flow, hydrogen-oxygen
Change sodium flow, the circular flow of reactor absorber portion, the circular flow of reaction mother liquor, circular flow and reactor in reactor
Interior pressure is monitored in real time, if closing hydrogen cyanide inlet valve when monitoring to occur exception；To the temperature in flash dryer
And the thing position of pressure, cyclone separator and the thing position of feeder are monitored in real time, at the same to conveying worm, feeder and into
The working condition of type machine is monitored in real time, if stopping centrifugal separator charging when monitoring to occur exception.
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| CN111994920A (en) * | 2020-08-31 | 2020-11-27 | 营创三征(营口)精细化工有限公司 | Production method and system of solid sodium cyanide |
| CN114588871A (en) * | 2022-03-16 | 2022-06-07 | 安徽省安庆市曙光化工股份有限公司 | Potassium cyanide production system and production method |
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