CN102728082B - Steam evaporating, concentrating and crystallizing system without live steam - Google Patents
Steam evaporating, concentrating and crystallizing system without live steam Download PDFInfo
- Publication number
- CN102728082B CN102728082B CN201210229248.6A CN201210229248A CN102728082B CN 102728082 B CN102728082 B CN 102728082B CN 201210229248 A CN201210229248 A CN 201210229248A CN 102728082 B CN102728082 B CN 102728082B
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- outlet
- evaporation
- steam
- import
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Classifications
-
- 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
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a steam evaporating, concentrating and crystallizing system without live steam. The system comprises an evaporation and concentration device, wherein the evaporation and concentration device comprises a first stage live steam free evaporation system; and the first stage live steam free evaporation system comprises devices such as a spraying type evaporator, a liquid storage tank, a circulation liquid pump, a heat exchanger, a steam compressor, an evaporated liquid receiving trough, an evaporated liquid pump and the like. According to the system, the structure is reasonable and steam or waste heat are not needed; a circulation water cooling device is unnecessary; renewable energy sources such as wind power, solar power generation and tidal power generation and the like are completely adopted without carbon emission; various production lines can be arranged in open-air or inside a house; the investment and the energy consumption are low; the operation and management are convenient; and the comprehensive cost is low.
Description
Technical field
The present invention relates to a kind of evaporation and concentrating, crystal system, comprise the fields such as inorganic or organic chemicals solution evaporation and concentrating, evaporative crystallization, bittern salt manufacturing, desalinization, sewage disposal.
Background technology
Existing evaporation technique is mostly: multiple-effect evaporation technology, the UTILIZATION OF VESIDUAL HEAT IN multiple-effect evaporation technology of logical raw steam, have the compression distillation technique of steam primary starting, these evaporation techniques all need steam or waste heat, evaporating temperature is higher, need to consume a large amount of fossil fuels, be difficult in the place that there is no heat supply realize.Although a lot of enterprises constantly undergo technological transformation, Technological Economy level improves, but the indexs such as the investment of above-mentioned various vaporising devices, energy consumption, operating cost are still higher, and seldom adopt regenerative resource, need to work out more economical, the evaporation technique of low-carbon (LC) more.
Summary of the invention
The object of the present invention is to provide one rational in infrastructure, do not need the evaporation and concentrating that need not give birth to steam, the crystal system of raw steam or other heat medium.
Technical solution of the present invention is:
Evaporation and concentrating, the crystal system that need not give birth to steam, is characterized in that: comprise evaporation and concentrating device; Described evaporation and concentrating device comprises that one-level is without raw steam raising system, one-level comprises fluid reservoir without raw steam raising system, fluid reservoir is arranged on spray-type evaporator below, recycle liquid pump import is connected with fluid reservoir, recycle liquid pump outlet is connected with the circulation fluid import of First Heat Exchanger, and the hot circulating solution outlet of First Heat Exchanger is connected with the spray liquid import of spray-type evaporator; The import of vapour compression machine is connected with the steam drain of spray-type evaporator, the outlet of vapour compression machine and the air intake of First Heat Exchanger are connected, the condensate outlet of First Heat Exchanger is connected with the hot condensate liquid import of the second heat exchanger, the condensate outlet of the second heat exchanger is connected with distillate groove, distillate groove is connected with distillate delivery pump, and distillate delivery pump outlet is delivered to out-of-bounds; The exhaust outlet of First Heat Exchanger is connected with the air inlet of the 3rd heat exchanger, and the exhaust outlet discharging directly into atmosphere of the 3rd heat exchanger or adapter are arrived out-of-bounds; Raw material is from out-of-bounds sending into the cold feed(raw material)inlet of the 3rd heat exchanger, and the material outlet of the 3rd heat exchanger is connected with the feed(raw material)inlet of the second heat exchanger, and the material outlet of the second heat exchanger is connected with the circulation fluid pipe of the circulation fluid import of First Heat Exchanger.
What evaporation and concentrating device was made up of without raw steam raising Cascade System multiple one-levels is multistage without raw steam raising system, or the raw steam raising system of multistage nothing being composed in parallel without raw steam raising system by multiple one-levels.
Cascade evaporation crystallization apparatus after evaporation and concentrating device; Described evaporated crystallization device comprises crystallizing tank, crystallizing tank is arranged on spray-type evaporator below, recycle liquid pump import is connected with crystallizing tank side mouth, recycle liquid pump outlet connects with the circulation fluid import of I heat exchanger, and hot circulating solution outlet and the import of spray-type evaporator spray liquid of I heat exchanger connect; Vapour compression machine import and spray-type evaporator steam drain connect, vapour compression machine outlet connects with the air intake of I heat exchanger, the hot condensate liquid import of the condensate outlet of I heat exchanger and II heat exchanger connects, the condensate outlet of II heat exchanger and distillate groove connect, distillate groove and distillate delivery pump connect, and distillate pump discharge pipe is delivered to out-of-bounds; The air inlet of the exhaust outlet of I heat exchanger and III heat exchanger connects, and the exhaust outlet discharging directly into atmosphere of III heat exchanger or adapter are arrived out-of-bounds; Raw material is from out-of-bounds sending into the cold feed(raw material)inlet of III heat exchanger, and the feed(raw material)inlet of the material outlet of III heat exchanger and II heat exchanger connects, the circulation fluid Guan Lian of the circulation fluid import of the material outlet of II heat exchanger and I heat exchanger; Adopt brilliant pump inlet and crystallizing tank end opening and connect, adopt brilliant pump discharge and cyclone hydraulic separators import and connect, cyclone hydraulic separators end opening and brilliant mud head tank connect, and the inlet tube of cyclone hydraulic separators liquid outlet and I heat exchanger connects; Centrifuge charge door and brilliant mud head tank end opening connect, and mother liquor tank and centrifuge liquid outlet connect, and mother liquor pump inlet and mother liquor tank connect, and the inlet tube of mother liquor pump discharge and I heat exchanger connects.
Evaporative crystallization is made up of plural serial stage.
The present invention is rational in infrastructure, does not need steam or waste heat, does not need circulating water cooling device, can all adopt the regenerative resources such as wind-powered electricity generation, solar electrical energy generation, tidal power generation, can not produce carbon emission; Various production lines can outdoor layout also can indoor layout, investment and energy consumption are low, operational management facilitates, integrated cost is low.
For the bittern salt making apparatus of producing 500000 tons of purified salts per year, folding hundred purified salt production costs per ton, 100 yuan of left and right, are only the half left and right of existing multiple-effect evaporation production cost.And, can produce 4600 tons of accurate pure water every day.
For the sea water desalinating unit of 2000 tons of desalination waters of daily output, 75 tons of salt, by net electricity electricity price, do not remember the value of salt, 16 yuan of left and right of fresh water production cost per ton; Salt is by 250 yuan/ton of calculating, 12 yuan of left and right of fresh water production cost per ton.
Below in conjunction with embodiment, the invention will be further described.
The specific embodiment
Evaporation and concentrating, the crystal system that need not give birth to steam, comprise evaporation and concentrating device; Described evaporation and concentrating device comprises that one-level is without raw steam raising system, one-level comprises fluid reservoir without raw steam raising system, fluid reservoir is arranged on spray-type evaporator below, recycle liquid pump import is connected with fluid reservoir, recycle liquid pump outlet is connected with the circulation fluid import of First Heat Exchanger, and the hot circulating solution outlet of First Heat Exchanger is connected with the spray liquid import of spray-type evaporator; The import of vapour compression machine is connected with the steam drain of spray-type evaporator, the outlet of vapour compression machine and the air intake of First Heat Exchanger are connected, the condensate outlet of First Heat Exchanger is connected with the hot condensate liquid import of the second heat exchanger, the condensate outlet of the second heat exchanger is connected with distillate groove, distillate groove is connected with distillate delivery pump, and distillate delivery pump outlet is delivered to out-of-bounds; The exhaust outlet of First Heat Exchanger is connected with the air inlet of the 3rd heat exchanger, and the exhaust outlet discharging directly into atmosphere of the 3rd heat exchanger or adapter are arrived out-of-bounds; Raw material is from out-of-bounds sending into the cold feed(raw material)inlet of the 3rd heat exchanger, and the material outlet of the 3rd heat exchanger is connected with the feed(raw material)inlet of the second heat exchanger, and the material outlet of the second heat exchanger is connected with the circulation fluid pipe of the circulation fluid import of First Heat Exchanger.
What evaporation and concentrating device was made up of without raw steam raising Cascade System multiple one-levels is multistage without raw steam raising system, or the raw steam raising system of multistage nothing being composed in parallel without raw steam raising system by multiple one-levels.
Cascade evaporation crystallization apparatus after evaporation and concentrating device; Described evaporated crystallization device comprises crystallizing tank, crystallizing tank is arranged on spray-type evaporator below, recycle liquid pump import is connected with crystallizing tank side mouth, recycle liquid pump outlet connects with the circulation fluid import of I heat exchanger, and hot circulating solution outlet and the import of spray-type evaporator spray liquid of I heat exchanger connect; Vapour compression machine import and spray-type evaporator steam drain connect, vapour compression machine outlet connects with the air intake of I heat exchanger, the hot condensate liquid import of the condensate outlet of I heat exchanger and II heat exchanger connects, the condensate outlet of II heat exchanger and distillate groove connect, distillate groove and distillate delivery pump connect, and distillate pump discharge pipe is delivered to out-of-bounds; The air inlet of the exhaust outlet of I heat exchanger and III heat exchanger connects, and the exhaust outlet discharging directly into atmosphere of III heat exchanger or adapter are arrived out-of-bounds; Raw material is from out-of-bounds sending into the cold feed(raw material)inlet of III heat exchanger, and the feed(raw material)inlet of the material outlet of III heat exchanger and II heat exchanger connects, the circulation fluid Guan Lian of the circulation fluid import of the material outlet of II heat exchanger and I heat exchanger; Adopt brilliant pump inlet and crystallizing tank end opening and connect, adopt brilliant pump discharge and cyclone hydraulic separators import and connect, cyclone hydraulic separators end opening and brilliant mud head tank connect, and the inlet tube of cyclone hydraulic separators liquid outlet and I heat exchanger connects; Centrifuge charge door and brilliant mud head tank end opening connect, and mother liquor tank and centrifuge liquid outlet connect, and mother liquor pump inlet and mother liquor tank connect, and the inlet tube of mother liquor pump discharge and I heat exchanger connects.
One-level isolated operation without raw steam raising system operating procedure and operational factor: first the liquid of needs evaporation is filled it up with to fluid reservoir and the downspout of spray-type evaporator below, is just full of liquid to the lower cone of evaporimeter.Start recycle liquid pump, the evaporated liquor in evaporimeter, downspout and fluid reservoir is beaten to circulated sprinkling, supplement fresh evaporated liquor according to the liquid level decline situation in evaporimeter, in automatic control evaporimeter lower cone, be just full of liquid.Starting vapour compression machine bleeds, pressure in evaporimeter progressively declines, during to saturated vapour pressure corresponding to evaporated liquor temperature, liquid evaporates in a large number, steam is compressed to pressure-fired, 40 ℃ of left and right laggard First Heat Exchanger heat cycles liquid of intensification through compressor, steam-condensation becomes liquid, after metering, approaching under dew-point temperature from flowing into the take fresh evaporated liquor of the second heat exchanger heating the 3rd heat exchanger, the second heat exchanger distillate out flows into distillate groove, and automatic control groove liquid level is sent battery limit (BL) with pump by distillate; The hot exhaust gas that First Heat Exchanger is discharged is direct emptying or go further processing after the 3rd heat exchanger is cooling with cold evaporated liquor; Fresh evaporated liquor after the 3rd heat exchanger is heated by hot exhaust gas, enter the second heat exchanger by the heating of hot condensate liquid after, go First Heat Exchanger further to heat with circulation fluid is mixed.Along with the carrying out of evaporation, circulation fluid is by heat temperature raising progressively, evaporation capacity further strengthens, after 4-6 hour, the parameters such as circulation fluid temperature, fresh evaporated liquor temperature, evaporation capacity, vapor (steam) temperature all tend to balance stable, due to weather conditions difference, balance parameters changes, for aqueous solution system, equilibrium vaporization temperature is at 70-90 ℃, and evaporating pressure is at 0.04-0.07MPa (A).While reaching qualified index to fluid reservoir concentration, according to steaming, liquid measure regulates and controls fresh evaporated liquor inlet amount and recycle liquid pump exports the product flow of drawing.When parking, stop into fresh evaporated liquor, liquid to be recycled reaches qualified products concentration requirement, and sending all material in evaporimeter as qualified products can be out of service.
Plural serial stage is without giving birth to steam raising system operating procedure and operational factor: fluid reservoir and the downspout of first the liquid of needs evaporation being filled it up with to spray-type evaporators at different levels below, lower cone to each evaporimeter is just full of liquid, restart recycle liquid pumps at different levels, by evaporimeters at different levels, evaporated liquor in downspout and fluid reservoir is beaten circulated sprinkling, according to the liquid level decline situation in each evaporimeter, start to supplement fresh evaporated liquor to the first order, from first order circulating-pump outlet through second level circulating-pump outlet pipe to secondary evaporimeter feed supplement, from second level circulating-pump outlet through the feed supplement of third level circulating-pump outlet Guan Xiangsan level evaporimeter, the rest may be inferred, one direct subsidy is to afterbody evaporimeter, in the each evaporimeter lower cone of automatic control, be just full of liquid.Starting vapour compression machines at different levels bleeds, pressure in each evaporimeter progressively declines, during to saturated vapour pressure corresponding to evaporated liquor temperature, liquid evaporates in a large number, steam arrives pressure-fired, 40 ℃ of laggard First Heat Exchanger heat cycles liquid at different levels in left and right of intensification through compressor compresses at different levels, steam-condensation becomes liquid, after each self-measuring, approaching under dew-point temperature from flowing into total system distillate groove, automatic control groove liquid level heats fresh evaporated liquor with being pumped into system-wide the second heat exchanger continuously, and cooled condensate liquid is sent battery limit (BL) continuously, the hot exhaust gas that First Heat Exchangers at different levels are discharged imports house steward, heats through total system the 3rd heat exchanger the fresh cold evaporated liquor of out-of-bounds sending here, and tail gas is emptying or go further processing, enter the second heat exchanger heating through the fresh evaporated liquor of total system the 3rd heat exchanger heating, add overheated fresh evaporated liquor and add one-level evaporimeter (mixed through the further laggard one-level evaporimeter of heating of one-level First Heat Exchanger with one-level circulation fluid), addition is according to the liquid automatic control of first evaporator, simultaneously, feed supplement amount according to from the liquid automatic control one-level circulating pump of second level evaporimeter to secondary evaporimeter, the rest may be inferred, according to the rear one-level evaporimeter liquid level control previous stage feed supplement amount of one-level backward, feed supplement backward step by step, one direct subsidy is to afterbody evaporimeter, keep evaporimeter level stabilities at different levels.Along with the carrying out of evaporation, circulation fluids at different levels are by heat temperature raising progressively, evaporation capacity further strengthens, after 4-6 hour, the parameters such as circulation fluid temperature, fresh evaporated liquor temperature, evaporation capacity, vapor (steam) temperature all tend to balance stable, due to weather conditions difference, balance parameters changes, for aqueous solution system, equilibrium vaporization temperature is at 70-90 ℃, and evaporating pressure is at 0.04-0.07MPa (A).While reaching qualified index to the fluid reservoir concentration of afterbody, steam according to total system that liquid measure regulates and controls fresh evaporated liquor inlet amount and afterbody recycle liquid pump exports the product flow of drawing.When parking, first, stop to a grading fresh evaporated liquor, continue the liquid level of automatic control evaporimeters at different levels, move backward material step by step; Secondly, during to low limit value, stop vapour compression machine and the circulation fluid circulated sprinkling of one-level until one-level evaporimeter liquid level, continue to turn material to secondary, automatic control secondary evaporimeter liquid level, until the material of one-level while all turning sky all devices of one-level out of service; Then, the rest may be inferred, until the second last stage material turns empty, corresponding device is out of service; Finally, in the time that material in final evaporator reaches qualified products concentration requirement, wherein all material are sent as qualified products, and total system is out of service.Also can stop immediately all evapn, each stage material is proceeded to blow tank or stay wait in evaporimeter and drive next time.
Plural parallel stage is without giving birth to steam raising system operating procedure and operational factor: first, add evaporated liquor to evaporimeters at different levels, then, automatically control fresh evaporated liquor house steward pressure stability, start recycle liquid pumps at different levels, by each evaporimeter, evaporated liquor in downspout and fluid reservoir is beaten circulated sprinkling, supplement fresh evaporated liquor according to the liquid level decline situation in each evaporimeter, valve opening on the fresh evaporated liquor feed pipe of the each evaporimeter of automatic control, make to be just full of liquid in each evaporimeter lower cone, start vapour compression machines at different levels according to " one-level isolated operation is without raw steam raising system operating procedure and operational factor " above again, carry out the operation of vapo(u)rization systems at different levels, control.After steam condensate meterings at different levels, approaching under dew-point temperature from flowing into system-wide distillate groove, automatic control groove liquid level is sent into the fresh cold evaporated liquor of system-wide the second heat exchanger heating continuously with pump, cooled condensate liquid is sent battery limit (BL) continuously, the hot exhaust gas that First Heat Exchangers at different levels are discharged imports house steward, through further heating the second heat exchanger fresh evaporated liquor out of total system the 3rd heat exchanger, tail gas is emptying or go further processing, adds overheated fresh evaporated liquor and gets back to fresh evaporated liquor house steward.Parking steps at different levels are with the parking step in " one-level isolated operation without raw steam raising system operating procedure and operational factor ".
For the system that has crystal to separate out, the concentration during according to inventory and beginning crystallization determines corresponding without raw steam raising system configuration, is made up of the some grades of raw steam raising systems of nothing and some grades of evaporated crystallization devices.
First be just full of liquid to spray-type evaporators at different levels with evaporated liquor to the lower cone of each evaporimeter.Start recycle liquid pumps at different levels, evaporated liquor in evaporimeters at different levels, downspout, fluid reservoir or crystallizing tank is beaten to circulated sprinkling, according to the liquid level decline situation in each evaporimeter, supplement fresh evaporated liquor to the evaporation and concentrating device first order, from first order circulating-pump outlet through second level circulating-pump outlet pipe to secondary evaporimeter feed supplement, from second level circulating-pump outlet through the feed supplement of third level circulating-pump outlet Guan Xiangsan level evaporimeter, the rest may be inferred, one direct subsidy, to afterbody evaporimeter, is just full of liquid in the each evaporimeter lower cone of automatic control.Starting vapour compression machines at different levels bleeds, pressure in each evaporimeter progressively declines, during to saturated vapour pressure corresponding to evaporated liquor temperature, liquid evaporates in a large number, steam arrives pressure-fired, 40 ℃ of laggard First Heat Exchanger heat cycles liquid at different levels in left and right of intensification through compressor compresses at different levels, steam-condensation becomes liquid, after each self-measuring, approaching under dew-point temperature from flowing into total system distillate groove, automatic control groove liquid level is continuously with the fresh evaporated liquor that is pumped into system-wide the second heat exchanger, the 3rd heating heat exchanger and comes, and cooled condensate liquid is sent battery limit (BL) continuously; The hot exhaust gas that First Heat Exchangers at different levels are discharged heats through total system the 3rd heat exchanger the fresh cold evaporated liquor of out-of-bounds sending here, and tail gas is emptying or go further processing; Fresh evaporated liquor adds one-level evaporimeter after the 3rd heat exchanger, the second heat exchanger heating, addition is according to the liquid automatic control of first evaporator, simultaneously, feed supplement amount according to from the liquid automatic control one-level circulating pump of second level evaporimeter to secondary evaporimeter, the rest may be inferred, according to the feed supplement amount of one-level, the step by step feed supplement backward backward of rear one-level evaporimeter liquid level control previous stage, one direct subsidy, to afterbody evaporimeter, keeps evaporimeter level stabilities at different levels.Along with the carrying out of evaporation, circulation fluids at different levels are by heat temperature raising progressively, evaporation capacity further strengthens, after 4-6 hour, the parameters such as circulation fluid temperature, fresh evaporated liquor temperature, evaporation capacity, vapor (steam) temperature all tend to balance stable, due to weather conditions difference, balance parameters changes, for aqueous solution system, equilibrium vaporization temperature is at 70-90 ℃, and evaporating pressure is at 0.04-0.07MPa (A).Start there is crystallization to the evaporator system of evaporated crystallization device, start and respectively adopt brilliant pump, send cyclone hydraulic separators from taking out continuously material at the bottom of each crystallizing tank, observe isolated crystal situation by each cyclone hydraulic separators blanking visor and regulate each baiting valve aperture, keep blanking solid content to enter the brilliant mud head tank of total system in preferable states, each cyclone hydraulic separators top liquid out returns to crystallizing tank separately, while having 1/3 material in the brilliant mud head tank of total system, can start centrifuge, to centrifuge charging, the centrifugal solid separating goes post processing, centrifuge mother liquor enters mother liquor tank, control flow and send into continuously the one-level evaporimeter of evaporated crystallization device with mother liquor pump.While reaching qualified products index to the liquid in afterbody crystallizing tank, according to total system steam liquid measure, isolated amount of solid regulates and controls fresh evaporated liquor inlet amount and afterbody recycle liquid pump exports the fluid product flow of drawing, and keeps total system stable operation.If do not need fluid product, afterbody evaporimeter circulation fluid all returns evaporimeter, not extraction system.When parking, first, stop to a grading fresh evaporated liquor, continue the liquid level of automatic control evaporimeters at different levels, move backward material step by step; Secondly, during to low limit value, stop vapour compression machine and the circulation fluid circulated sprinkling of one-level until one-level evaporimeter liquid level, continue to turn material to secondary, automatic control secondary evaporimeter liquid level, until the material of one-level while all turning sky all devices of one-level out of service; Again, the rest may be inferred, and while all turning sky to the material of afterbody evaporation and concentrating device, all devices of afterbody evaporation and concentrating device is out of service, and evaporated crystallization device continues operation; Then, evaporated crystallization device, with above-mentioned evaporation and concentrating device shut-down operation, stops step by step containing adopting brilliant pump in interior all devices operation, until the second last stage material turns empty, corresponding device is out of service; Finally, in the time that evaporated liquor in final evaporator reaches qualified products requirement, all liq material wherein can be sent as qualified products, if do not need fluid product, when final stage liquid level can be out of service during to lower bound.Also can stop immediately all evapn, each stage material is proceeded to blow tank or stay wait in evaporimeter and drive next time.
Example:
1, bittern salt manufacturing
With evaporation and crystallization system configuration and operations requirement.
Preferred example: compose in parallel a production line without raw steam vaporizer with 23 grades of Type Bs, the refining bittern of salt content 300 grams per liters is made to purified salt, 500,000 tons of annual productions (folding 100% sodium chloride)., containing brine refining expense, folding hundred purified salt production costs per ton are not 100 yuan of left and right.In addition, can produce 4600 tons of peace and quiet water containing trace salt every day.
This evaporation and crystallization system comprises: 23 φ 3000 spray-type evaporators, 23 φ 2000 crystallizing tanks, 23 recycle liquid pumps, 1,23 vapour compression machines of 23 heat exchangers, 1 distillate groove, 2 steam liquid pump, 1 refining bittern groove, 2 refining brine pumps, 3,23,2,1 heat exchanger of 1 heat exchanger and adopt the equipment such as salt pump, 23 cyclone hydraulic separators, some salt slurry head tanks, some desk centrifuges, 1 mother liquor tank, 2 mother liquor pumps.
2, desalinization
With evaporation and crystallization system configuration and operations requirement.
Preferred example: be composed in series a production line without raw steam vaporizer, the seawater of desalination salt content 3.5% left and right, 2000 tons of desalination waters of the daily output, 75 tons of salt without raw steam vaporizer and 2 grades of Type Bs by 8 grades of A types.With net electricity, do not remember the value of salt, 16 yuan of left and right of fresh water production cost per ton; Salt is by 250 yuan/ton of calculating, 12 yuan of left and right of fresh water production cost per ton.
This evaporation and crystallization system comprises: 10 φ 3000 spray-type evaporators, 8 φ 1000 fluid reservoirs, 2 φ 2000 crystallizing tanks, 10 recycle liquid pumps, 1,10 vapour compression machines of 10 heat exchangers, 1 fresh water groove, 2 fresh water pumps, 1 clarification seawater groove, 2 Taiwan Straits water pumps, 3,2,2,1 heat exchanger of 1 heat exchanger are adopted the equipment such as salt pump, 2 cyclone hydraulic separators, 1 salt slurry head tank, 1 desk centrifuge, 1 mother liquor tank, 1 mother liquor pump.
Claims (4)
1. evaporation and concentrating, the crystal system that need not give birth to steam, is characterized in that: comprise evaporation and concentrating device; Described evaporation and concentrating device comprises that one-level is without raw steam raising system, one-level comprises fluid reservoir without raw steam raising system, fluid reservoir is arranged on the first spray-type evaporator below, recycle liquid pump import is connected with fluid reservoir, recycle liquid pump outlet is connected with the circulation fluid import of First Heat Exchanger, and the hot circulating solution outlet of First Heat Exchanger is connected with the spray liquid import of the first spray-type evaporator; The import of vapour compression machine is connected with the steam drain of the first spray-type evaporator, the outlet of vapour compression machine and the air intake of First Heat Exchanger are connected, the condensate outlet of First Heat Exchanger is connected with the hot condensate liquid import of the second heat exchanger, the condensate outlet of the second heat exchanger is connected with distillate groove, distillate groove is connected with distillate delivery pump, and distillate delivery pump outlet is delivered to out-of-bounds; The exhaust outlet of First Heat Exchanger is connected with the air inlet of the 3rd heat exchanger, and the exhaust outlet discharging directly into atmosphere of the 3rd heat exchanger or adapter are arrived out-of-bounds; Raw material is from out-of-bounds sending into the cold feed(raw material)inlet of the 3rd heat exchanger, and the material outlet of the 3rd heat exchanger is connected with the feed(raw material)inlet of the second heat exchanger, and the material outlet of the second heat exchanger is connected with the circulation fluid pipe of the circulation fluid import of First Heat Exchanger.
2. evaporation and concentrating, the crystal system that need not give birth to steam according to claim 1, it is characterized in that: what evaporation and concentrating device was made up of without raw steam raising Cascade System multiple one-levels is multistage without raw steam raising system, or the raw steam raising system of multistage nothing being composed in parallel without raw steam raising system by multiple one-levels.
3. evaporation and concentrating, the crystal system that need not give birth to steam according to claim 1 and 2, is characterized in that: cascade evaporation crystallization apparatus after evaporation and concentrating device; Described evaporated crystallization device comprises crystallizing tank, crystallizing tank is arranged on the second spray-type evaporator below, recycle liquid pump import is connected with crystallizing tank side mouth, recycle liquid pump outlet is connected with the circulation fluid import of I heat exchanger, and the hot circulating solution outlet of I heat exchanger is connected with the second spray-type evaporator spray liquid import; Vapour compression machine import is connected with the second spray-type evaporator steam drain, vapour compression machine outlet is connected with the air intake of I heat exchanger, the condensate outlet of I heat exchanger is connected with the hot condensate liquid import of II heat exchanger, the condensate outlet of II heat exchanger is connected with distillate groove, distillate groove is connected with distillate delivery pump, and distillate pump discharge pipe is delivered to out-of-bounds; The exhaust outlet of I heat exchanger is connected with the air inlet of III heat exchanger, and the exhaust outlet discharging directly into atmosphere of III heat exchanger or adapter are arrived out-of-bounds; Raw material is from out-of-bounds sending into the cold feed(raw material)inlet of III heat exchanger, and the material outlet of III heat exchanger is connected with the feed(raw material)inlet of II heat exchanger, and the material outlet of II heat exchanger is connected with the circulation fluid pipe of the circulation fluid import of I heat exchanger; Adopt brilliant pump inlet and be connected with crystallizing tank end opening, adopt brilliant pump discharge and be connected with cyclone hydraulic separators import, cyclone hydraulic separators end opening is connected with brilliant mud head tank, and cyclone hydraulic separators liquid outlet is connected with the inlet tube of I heat exchanger; Centrifuge charge door is connected with brilliant mud head tank end opening, and mother liquor tank is connected with centrifuge liquid outlet, and mother liquor pump inlet is connected with mother liquor tank, and mother liquor pump discharge is connected with the inlet tube of I heat exchanger.
4. evaporation and concentrating, the crystal system that need not give birth to steam according to claim 3, is characterized in that: evaporative crystallization is made up of plural serial stage.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210229248.6A CN102728082B (en) | 2012-07-04 | 2012-07-04 | Steam evaporating, concentrating and crystallizing system without live steam |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210229248.6A CN102728082B (en) | 2012-07-04 | 2012-07-04 | Steam evaporating, concentrating and crystallizing system without live steam |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102728082A CN102728082A (en) | 2012-10-17 |
| CN102728082B true CN102728082B (en) | 2014-06-25 |
Family
ID=46984814
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210229248.6A Expired - Fee Related CN102728082B (en) | 2012-07-04 | 2012-07-04 | Steam evaporating, concentrating and crystallizing system without live steam |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102728082B (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103007553B (en) * | 2012-12-05 | 2015-11-11 | 中国科学院理化技术研究所 | A kind of function of mechanical steam recompression continuous evaporative crystallization system and method |
| CN105477894B (en) * | 2016-01-22 | 2017-12-15 | 江西天鑫冶金装备技术有限公司 | Cu, Ni and Co electrodeposition, electrolyte evaporation concentration device |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994022546A1 (en) * | 1993-03-31 | 1994-10-13 | ABB Fläkt AB | Method and device for precipitating crystals from a solution |
| CN1188020A (en) * | 1997-11-21 | 1998-07-22 | 四川省环境保护科学研究院 | Evaporating concentrating method for product without steam |
| CN201093905Y (en) * | 2007-06-14 | 2008-07-30 | 西北工业大学 | Inorganic heat tube spraying type evaporator |
| CN101450266A (en) * | 2007-12-04 | 2009-06-10 | 石家庄工大化工设备有限公司 | Sodium sulfide evaporation concentration system and method |
| CN101497465A (en) * | 2008-02-02 | 2009-08-05 | 上海达源环境科技工程有限公司 | Process for evaporating high-concentration sewage |
| CN201553609U (en) * | 2009-11-10 | 2010-08-18 | 西陇化工股份有限公司 | Sulfuric acid purifying device |
| EP2252384A1 (en) * | 2008-03-10 | 2010-11-24 | Ridel | Evaporator with mechanical vapour compression including an expansion device at the separator inlet |
-
2012
- 2012-07-04 CN CN201210229248.6A patent/CN102728082B/en not_active Expired - Fee Related
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1994022546A1 (en) * | 1993-03-31 | 1994-10-13 | ABB Fläkt AB | Method and device for precipitating crystals from a solution |
| CN1188020A (en) * | 1997-11-21 | 1998-07-22 | 四川省环境保护科学研究院 | Evaporating concentrating method for product without steam |
| CN201093905Y (en) * | 2007-06-14 | 2008-07-30 | 西北工业大学 | Inorganic heat tube spraying type evaporator |
| CN101450266A (en) * | 2007-12-04 | 2009-06-10 | 石家庄工大化工设备有限公司 | Sodium sulfide evaporation concentration system and method |
| CN101497465A (en) * | 2008-02-02 | 2009-08-05 | 上海达源环境科技工程有限公司 | Process for evaporating high-concentration sewage |
| EP2252384A1 (en) * | 2008-03-10 | 2010-11-24 | Ridel | Evaporator with mechanical vapour compression including an expansion device at the separator inlet |
| CN201553609U (en) * | 2009-11-10 | 2010-08-18 | 西陇化工股份有限公司 | Sulfuric acid purifying device |
Non-Patent Citations (2)
| Title |
|---|
| 刘庆江.大型海水淡化技术综述.《锅炉制造》.(第06期), |
| 大型海水淡化技术综述;刘庆江;《锅炉制造》(第06期);29-32,37页 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102728082A (en) | 2012-10-17 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101955238A (en) | Seawater desalting method and device | |
| CN103203116A (en) | MVR (Mechanical Vapor Recompression) continuous evaporative crystallization system and continuous evaporative crystallization method | |
| CN204298090U (en) | Industrial exhaust heat type low temperature multi-effect seawater desalting system | |
| CN102092808B (en) | Device for desalinating seawater by utilizing residual heat of tail gas exhausted by diesel engine | |
| CN104402079A (en) | Industrial waste heat type low-temperature multi-effect sea water desaltation system and sea water desaltation method thereof | |
| CN102381796B (en) | Solar photovoltaic photothermal integrated device for seawater desalination | |
| CN102336448B (en) | Saline treatment system and method | |
| CN205170431U (en) | Solar energy absorption heat pump sea water desalination device | |
| CN106115825A (en) | A kind of low temperature multiple-effect distillation seawater desalination system | |
| CN103613155B (en) | Heat pipe-type low temperature two sea water desalting equipment | |
| CN101205087A (en) | Highly effective sea-water brackish water distillatory using renewable energy | |
| CN201587871U (en) | Multi-stage vacuum distillation sea water desalinating device | |
| CN108314121B (en) | Brackish water desalination device and brackish water desalination method | |
| CN2835215Y (en) | Directly-heated solar seawater desalinating apparatus | |
| CN205035108U (en) | A light water condenser for sea water desalination device | |
| CN201834781U (en) | Single-stage vacuum distillation seawater desalination device | |
| CN202080914U (en) | Composite solar seawater desalting device | |
| CN103663589A (en) | Seawater desalinization method and seawater desalinization device | |
| CN201660457U (en) | Novel multiple-effect distilled sea water desalination device | |
| CN102728082B (en) | Steam evaporating, concentrating and crystallizing system without live steam | |
| CN101792190B (en) | Novel solar seawater desalination system | |
| CN201537402U (en) | High-efficient evaporation crystallizer | |
| CN102874969A (en) | Interactive absorption type solar energy and wind energy sea water desalting device | |
| CN106082378B (en) | A kind of low temperature (1+n) effect distillation seawater desalination technique | |
| CN106966462A (en) | A kind of multistage seawater desalting coupled system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20140625 Termination date: 20160704 |