CN208182650U - Ammonium sulphate waste liquor desalting processing equipment - Google Patents
Ammonium sulphate waste liquor desalting processing equipment Download PDFInfo
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- CN208182650U CN208182650U CN201820532154.9U CN201820532154U CN208182650U CN 208182650 U CN208182650 U CN 208182650U CN 201820532154 U CN201820532154 U CN 201820532154U CN 208182650 U CN208182650 U CN 208182650U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model relates to a kind of desalting processing equipment more particularly to a kind of ammonium sulphate waste liquor desalting processing equipments.The utility model includes preheating device, evaporated crystallization device, condensate device, Crystallization Separation device, the utility model carries out condensing crystallizing by the Matter Transfer between inward turning circulating evaporator and crystallizer, material carries out salt separation through centrifuge after by crystallisation by cooling, secondary steam is purified by steam washing tower, energy cycling and reutilization is carried out as heat source to the secondary steam recompression of evaporation using vapour compression machine to realize the crystallization desalination of whole process, the equipment operation is convenient, it is energy-efficient, it can continuous work, stable operation, be conducive to industry energy conservation consumption reduction.
Description
Technical field
The utility model relates to a kind of desalting processing equipment more particularly to a kind of ammonium sulphate waste liquor desalting processing equipments.
Background technique
Ammonium sulphate waste liquor is mainly derived from chemical production field and total amount is huge, and the processing method of ammonium sulphate waste liquor is mainly adopted
Evaporation process is taken to separate salt in solid form.Existing method uses single-action or multiple-effect evaporation method, and needs constantly to mention
For heating steam, steam consumption is high.But energy prices increasingly go up in recent years, lead to cost promotion in traditional evaporation process.
Evaporation equipment mainly uses forced-circulation evaporator at present, heats room vertical structure, liquid circulation velocity size by
Pump is adjusted, and is that flowing of the material in heating tube is maintained by powerful forced circulation pump, so needing to consume a large amount of electric energy.
With the increasingly growing tension of raising and Energy situation of environmental requirement, energy-saving and emission-reduction more come by various passes
Note.In order to preferably adapt to the policy of the energy and environment, energy-saving and environment-friendly treatment process technology and equipment is researched and developed and carried out
It is inexorable trend.
Utility model content
The purpose of this utility model is that proposing a kind of ammonium sulphate waste liquor desalting processing equipment, pass through inward turning circulating evaporator
Matter Transfer between crystallizer carries out condensing crystallizing, and material carries out salt separation through centrifuge after by crystallisation by cooling, leads to
Steam washing tower is crossed to purify secondary steam, using vapour compression machine to the recompression of the secondary steam of evaporation as heat source into
Row energy cycling and reutilization realizes the crystallization desalination of whole process, and the equipment operation is convenient, energy-efficient, can continuous work,
Stable operation is conducive to industry energy conservation consumption reduction.
The utility model includes preheating device, evaporated crystallization device, condensate device, Crystallization Separation device, preheating device packet
Material pot, feed pump, tail gas pre-heater, condensate preheater, vapor preheater are included, the material pot is sequentially connected charging by the road
Pump, condensate preheater tube side, tail gas pre-heater shell side, vapor preheater tube side；
Evaporated crystallization device includes inward turning circulating evaporator, crystallizer, steam washing tower, vapour liquid separator, internal circulation pump, steam
By the road with connection, inward turning, which recycles, steams for compressor, the inward turning circulating evaporator feed inlet and vapor preheater tube side discharge end
It sends out device discharge port and connects crystallizer, crystallizer circulation port is sequentially connected internal circulation pump through circulation pipe, inward turning circulating evaporator recycles
Feed inlet, the inward turning circulating evaporator vaporium by pipeline be sequentially connected steam washing tower, vapour liquid separator, vapour compression machine,
Inward turning circulating evaporator heating chamber；
Condensate device includes water segregator, condensate preheater, condensate tank, condensate pump, and water segregator first end connects inward turning circulation
Evaporator condensate chamber, water segregator second end connect the tube side import of tail gas pre-heater, water segregator third end and tail gas pre-heater bottom
Portion's interface connects the shell side import of condensate preheater, and condensate preheater shell-side outlet is sequentially connected condensate tank, condensate pump；
Crystallization Separation device includes discharging pump, crystallisation by cooling tank, centrifuge, mother liquor tank, mother liquor pump, the discharging pump inlet
Crystallizer discharge port is connected, discharging pump discharge is sequentially connected crystallisation by cooling tank, centrifuge, mother liquor tank, mother liquor by pipeline and pumps.
Operation principle and process: material storing is successively pumped into condensate preheater tube side and system in material pot through feed pump
Enter tail gas pre-heater tube side after condensate preheating to be exchanged heat again with system tail gas, is then heated to technique item through vapor preheater
Enter inward turning circulating evaporator after bubble point under part to be evaporated, material is concentrated by evaporation into knot in inward turning circulating evaporator
Brilliant device sedimentation crystallization, solution are recycled in inward turning circulating evaporator through internal circulation pump are concentrated again, repeatedly；Evaporate the object completed
Material by discharging pump be successively pumped into crystallisation by cooling tank carry out the processing of crystallisation by cooling system, and through centrifuge apparatus isolate crystal and
Mother liquor, mother liquor are pumped out after entering mother liquor tank by mother liquor；The secondary steam warp that material is generated in inward turning circulating evaporator vaporization chamber
Steam washing tower reaches vapour compression machine after entering vapour liquid separator, and the steam by increasing temperature and pressure is through entering inward turning circulating evaporator
Heating chamber, the steam of increasing temperature and pressure in inward turning circulating evaporator with material-heat-exchanging to being condensed into water, condensed water is followed from inward turning
Ring evaporator condensate chamber sequentially enters condensate preheater shell side through water segregator, carries out with the material in condensate preheater tube side abundant
Condensate tank is stored in after heat exchange, by the online discharge system of condensate pump.
Described, it further include vacuum system, the vacuum system includes vacuum pump, vacuum buffer tank, vacuum pump exhaust port
Material pot is accessed by pipeline, air-inlet of vacuum pump is sequentially connected vacuum buffer tank, the outlet of tail gas pre-heater tube side.
The steam tail gas generated in water segregator enters the import of tail gas pre-heater tube side under the action of vacuum pump, tail gas preheats
Heat exchange is completed with the material in tail gas pre-heater shell side in the outlet of device tube side, and the steam tail gas after completing heat exchange is cold by tail gas
Condenser tube side enters vacuum buffer tank, empties after being pumped into the purification of material pot top by vacuum pump.
Described, it further include tail gas condenser, the vacuum buffer tank is sequentially connected end interface on tail gas condenser, tail gas
Preheater tube side exports, and end interface is connect by pipeline with condensate preheater shell side import under tail gas condenser.
Tail gas condenser is set to steam tail gas cooling, the steam tail gas after completing heat exchange is condensed into water by under condenser
End interface enters condensate preheater shell side.
Described, vapour liquid separator liquid return hole is connect by pipeline with inward turning circulating evaporator recycle feed mouth.
Described, discharging pump is connect by pipeline with inward turning circulating evaporator recycle feed mouth.
Described, crystallisation by cooling tank includes level-one crystallisation by cooling tank, second level crystallisation by cooling tank, level-one crystallisation by cooling tank and two
Grade crystallisation by cooling tank passes through piping connection.
The beneficial effects of the utility model are:
(1) ammonium sulphate waste liquor desalting processing equipment described in the utility model, is provided with inward turning circulating evaporator and crystallization
Device carries out circulating and evaporating to material, and condensing crystallizing can continuous work；
(2) ammonium sulphate waste liquor desalting processing equipment described in the utility model, is provided with steam washing tower, vapour liquid separator and steaming
Vapour compressor, purifies secondary steam, flows back to separation liquid, while recompressing secondary steam as heating heat
Source carries out energy circulation；
(3) ammonium sulphate waste liquor desalting processing equipment described in the utility model, is provided with vacuum system, passes through vacuum pumping
Dynamic steam tail gas completes heat exchange, is conducive to waste heat and recycles, recycles.
Detailed description of the invention
Fig. 1 is a kind of example structure schematic diagram；
In figure: 1, vacuum pump；2, vacuum buffer tank；3, tail gas condenser；4, tail gas pre-heater；5, water segregator；6, steam
Preheater；7, inward turning circulating evaporator；8, steam washing tower；9, vapour liquid separator；10, vapour compression machine；11, level-one crystallisation by cooling
Tank；12, second level crystallisation by cooling tank；13, centrifuge；14, mother liquor tank；15, mother liquor pumps；16, discharging pump；17, internal circulation pump；18,
Crystallizer；19, condensate preheater；20, condensate tank；21, condensate pump；22, feed pump；23, material pot.
Specific embodiment
The utility model is described in further detail with reference to the accompanying drawing.
As shown in Figure 1, ammonium sulphate waste liquor desalting processing equipment described in the utility model includes: preheating device, evaporation knot
Brilliant device, condensate device, Crystallization Separation device, vacuum system, tail gas condenser；
Preheating device, including material pot 23, feed pump 22, tail gas pre-heater 4, condensate preheater 19, vapor preheater 6,
The material pot 23 is sequentially connected feed pump 22,19 tube side of condensate preheater, 4 shell side of tail gas pre-heater, steam preheating by the road
6 tube side of device；
Evaporated crystallization device, including inward turning circulating evaporator 7, crystallizer 18, steam washing tower 8, vapour liquid separator 9, interior circulation
17, vapour compression machine 10 are pumped, 7 feed inlet of inward turning circulating evaporator by the road and connects with 6 tube side discharge end of vapor preheater
It connects, 7 discharge port of inward turning circulating evaporator connects crystallizer 18, and 18 circulation port of crystallizer is sequentially connected internal circulation pump through circulation pipe
17,7 recycle feed mouth of inward turning circulating evaporator, 7 vaporium of inward turning circulating evaporator are sequentially connected steam washing tower by pipeline
8, vapour liquid separator 9, vapour compression machine 10,7 heating chamber of inward turning circulating evaporator；
Condensate device, including water segregator 5, condensate preheater 19, condensate tank 20, condensate pump 21, the connection of 5 first end of water segregator
7 condensate chamber of inward turning circulating evaporator, 5 second end of water segregator connect tail gas pre-heater 4 tube side import, 5 third end of water segregator and
4 bottom interface of tail gas pre-heater connects the 19 shell side import of condensate preheater, and 19 shell-side outlet of condensate preheater is sequentially connected condensate
Tank 20, condensate pump 21；
Crystallization Separation device, including discharging pump 16, crystallisation by cooling tank, centrifuge 13, mother liquor tank 14, mother liquor pump 15, it is described
16 import of discharging pump connects 18 discharge port of crystallizer, and the outlet of discharging pump 16 is sequentially connected crystallisation by cooling tank, centrifuge by pipeline
13, mother liquor tank 14, mother liquor pump 15；
Vacuum system, including vacuum pump 1, vacuum buffer tank 2,1 exhaust outlet of vacuum pump access material pot 23 by pipeline, very
Sky 1 air inlet of pump is sequentially connected vacuum buffer tank 2, the outlet of 4 tube side of tail gas pre-heater；
Tail gas condenser 3, vacuum buffer tank 2 is sequentially connected end interface on tail gas condenser 3,4 tube side of tail gas pre-heater goes out
Mouthful, the lower end interface of tail gas condenser 3 is connect by pipeline with the 19 shell side import of condensate preheater；Wherein vapour liquid separator 9 returns liquid
Mouth is connect by pipeline with 7 recycle feed mouth of inward turning circulating evaporator；Discharging pump 16 is followed by pipeline with inward turning circulating evaporator 7
The connection of ring feed inlet；Crystallisation by cooling tank includes level-one crystallisation by cooling tank 11, second level crystallisation by cooling tank 12, level-one crystallisation by cooling tank 11
Pass through piping connection with second level crystallisation by cooling tank 12.
Ammonium sulphate waste liquor material storing is successively pumped into 19 tube side of condensate preheater and is in material pot 23 through feed pump 22
Enter 3 shell side of tail gas pre-heater after system condensate preheating to be exchanged heat again with system tail gas, then be heated through 6 tube side of vapor preheater
Enter inward turning circulating evaporator 7 after bubble point under to process conditions to be evaporated；Material evaporates in inward turning circulating evaporator 7
Enter the sedimentation crystallization of crystallizer 18 after concentration, solution is recycled in inward turning circulating evaporator 7 through internal circulation pump 17 is concentrated again, so
Repeatedly；The material that evaporation is completed successively is pumped into level-one crystallisation by cooling tank 11, the cooling of second level crystallisation by cooling tank 12 by discharging pump 16
Crystallization carries out crystallisation by cooling processing, and isolates crystal and mother liquor through centrifuge 13, and mother liquor is pumped after entering mother liquor tank 14 by mother liquor
15 pump out；Material is in the secondary steam that 7 vaporization chamber of inward turning circulating evaporator generates after steam washing tower 8 enters vapour liquid separator 9
Reach vapour compression machine 10, the steam by increasing temperature and pressure enters 7 heating chamber of inward turning circulating evaporator, and the steam of increasing temperature and pressure exists
With material-heat-exchanging to be condensed into water in inward turning circulating evaporator 7, condensed water is from 7 condensate chamber of inward turning circulating evaporator through water segregator
5 sequentially enter 19 shell side of condensate preheater, carry out being stored in condensate after sufficiently exchanging heat with the material in 19 tube side of condensate preheater
Tank 20, by the online discharge system of condensate pump 21, the steam tail gas generated in water segregator 5 enters tail gas under the action of vacuum pump 1
4 tube side import of preheater, the outlet of 4 tube side of tail gas pre-heater, on tail gas condenser 3 in end interface, with 4 shell side of tail gas pre-heater
Material completes heat exchange and to steam tail gas cooling, and the steam tail gas after completing heat exchange enters vacuum by tail gas condenser 3
Surge tank 2 empties after being pumped into the purification of 23 top of material pot by vacuum pump 1.
Wherein, it is 60-80 DEG C that material, which enters vapor preheater 6 to be evaporated temperature, and the temperature rise of vapour compression machine 10 is optional
16 DEG C, secondary steam passes through the ammonia in spray acid mist with escape in steam washing tower 8；In tail gas condenser 3 and tail gas pre-heater 4
The condensed water formed after heat exchange is completed with steam tail gas, and 19 shell side of condensate preheater is accessed by pipeline；Vapour liquid separator 9 returns
Liquid mouth and discharging pump 16 are connect by pipeline with 7 recycle feed mouth of inward turning circulating evaporator, feeding cycle；Dense after material concentration
Degree, which is pumped into after level-one crystallisation by cooling tank when reaching 45-50% by discharging pump 16, to be entered back into second level crystallisation by cooling tank and is sufficiently tied
It is brilliant.
Certainly, above content is only the preferred embodiment of the utility model, be should not be construed as limiting practical new to this
The scope of embodiments of type.The utility model is also not limited to the example above, and those skilled in the art are in this reality
With all the changes and improvements etc. made in novel essential scope, the patent covering scope of the utility model should all be belonged to
It is interior.
Claims (6)
1. a kind of ammonium sulphate waste liquor desalting processing equipment, characterized by comprising:
Preheating device, including material pot (23), feed pump (22), tail gas pre-heater (4), condensate preheater (19), steam preheating
Device (6), the material pot (23) are sequentially connected feed pump (22), condensate preheater (19) tube side, tail gas pre-heater (4) by the road
Shell side, vapor preheater (6) tube side；
Evaporated crystallization device, including it is inward turning circulating evaporator (7), crystallizer (18), steam washing tower (8), vapour liquid separator (9), interior
Circulating pump (17), vapour compression machine (10), inward turning circulating evaporator (7) feed inlet and vapor preheater (6) tube side discharge
End connect by the road, inward turning circulating evaporator (7) discharge port connect crystallizer (18), crystallizer (18) circulation port through circulation pipe according to
Secondary connection internal circulation pump (17), inward turning circulating evaporator (7) recycle feed mouth, inward turning circulating evaporator (7) vaporium are logical
It crosses pipeline and is sequentially connected steam washing tower (8), vapour liquid separator (9), vapour compression machine (10), inward turning circulating evaporator (7) heating chamber；
Condensate device, including water segregator (5), condensate preheater (19), condensate tank (20), condensate pump (21), water segregator (5) first
End connection inward turning circulating evaporator (7) condensate chamber, water segregator (5) second end connect the shell side import of tail gas pre-heater (4), divide water
Device (5) third end connects condensate preheater (19) shell side import, condensate preheater (19) shell with tail gas pre-heater (4) bottom interface
Journey outlet is sequentially connected condensate tank (20), condensate pump (21)；
Crystallization Separation device, including discharging pump (16), crystallisation by cooling tank, centrifuge (13), mother liquor tank (14), mother liquor pump (15),
Discharging pump (16) import connects crystallizer (18) discharge port, and discharging pump (16) outlet is sequentially connected crystallisation by cooling by pipeline
Tank, centrifuge (13), mother liquor tank (14), mother liquor pump (15).
2. ammonium sulphate waste liquor desalting processing equipment according to claim 1, it is characterised in that: it further include vacuum system, institute
Stating vacuum system includes vacuum pump (1), vacuum buffer tank (2), and vacuum pump (1) exhaust outlet accesses material pot (23) by pipeline,
Vacuum pump (1) air inlet is sequentially connected vacuum buffer tank (2), the outlet of tail gas pre-heater (4) tube side.
3. ammonium sulphate waste liquor desalting processing equipment according to claim 2, it is characterised in that: further include tail gas condenser
(3), the vacuum buffer tank (2) is sequentially connected end interface on tail gas condenser (3), the outlet of tail gas pre-heater (4) tube side, tail gas
End interface is connect by pipeline with condensate preheater (19) shell side import under condenser (3).
4. ammonium sulphate waste liquor desalting processing equipment according to claim 1, it is characterised in that: the vapour liquid separator (9)
Liquid return hole is connect by pipeline with inward turning circulating evaporator (7) recycle feed mouth.
5. ammonium sulphate waste liquor desalting processing equipment according to claim 1, it is characterised in that: the discharging pump (16) passes through
Pipeline is connect with inward turning circulating evaporator (7) recycle feed mouth.
6. ammonium sulphate waste liquor desalting processing according to claim 1 equipment, it is characterised in that: the crystallisation by cooling tank includes
Level-one crystallisation by cooling tank (11), second level crystallisation by cooling tank (12), level-one crystallisation by cooling tank (11) and second level crystallisation by cooling tank (12)
Pass through piping connection.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820532154.9U CN208182650U (en) | 2018-04-13 | 2018-04-13 | Ammonium sulphate waste liquor desalting processing equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820532154.9U CN208182650U (en) | 2018-04-13 | 2018-04-13 | Ammonium sulphate waste liquor desalting processing equipment |
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| Publication Number | Publication Date |
|---|---|
| CN208182650U true CN208182650U (en) | 2018-12-04 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201820532154.9U Active CN208182650U (en) | 2018-04-13 | 2018-04-13 | Ammonium sulphate waste liquor desalting processing equipment |
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| CN (1) | CN208182650U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110342719A (en) * | 2019-08-08 | 2019-10-18 | 上海晶宇环境工程股份有限公司 | A kind of technique and special equipment of carnallite desiccation |
| CN115055034A (en) * | 2022-07-26 | 2022-09-16 | 北京清新环境技术股份有限公司 | Semi-dry treatment method and system for flue gas purification |
-
2018
- 2018-04-13 CN CN201820532154.9U patent/CN208182650U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110342719A (en) * | 2019-08-08 | 2019-10-18 | 上海晶宇环境工程股份有限公司 | A kind of technique and special equipment of carnallite desiccation |
| CN115055034A (en) * | 2022-07-26 | 2022-09-16 | 北京清新环境技术股份有限公司 | Semi-dry treatment method and system for flue gas purification |
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