CN1142810A - Vaporizing and concentration drying apparatus and method - Google Patents

Vaporizing and concentration drying apparatus and method Download PDF

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Publication number
CN1142810A
CN1142810A CN94194698A CN94194698A CN1142810A CN 1142810 A CN1142810 A CN 1142810A CN 94194698 A CN94194698 A CN 94194698A CN 94194698 A CN94194698 A CN 94194698A CN 1142810 A CN1142810 A CN 1142810A
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China
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steam
vaporizer
heat
wet feed
conduit
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CN94194698A
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Chinese (zh)
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CN1097559C (en
Inventor
辛根
李大成
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Pu Longyi
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Pu Longyi
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/28—Evaporating with vapour compression
    • B01D1/284—Special features relating to the compressed vapour
    • B01D1/2846—The compressed vapour is not directed to the same apparatus from which the vapour was taken off
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D1/00—Evaporating
    • B01D1/0011—Heating features
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/02—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping in boilers or stills
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/006—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with evaporation or distillation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
    • B01D5/0075—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes with heat exchanging
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/009—Collecting, removing and/or treatment of the condensate
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
    • B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
    • B01D5/0096—Cleaning
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/048—Purification of waste water by evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W10/00—Technologies for wastewater treatment
    • Y02W10/40—Valorisation of by-products of wastewater, sewage or sludge processing

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Drying Of Solid Materials (AREA)
  • Treatment Of Sludge (AREA)

Abstract

Vaporizing and concentration drying apparatus and method are disclosed. The apparatus and method prepare good quality of condensed water and save evaporation energy and are wide used in making contamined waste water become distilled water and in purification of the waste water and in concentration and drying of varieties of environmental polluting sludge. The apparatus and method recover and reuse the heating energy, which energy was applied to the vapor so as to heat the vapor to a high temperature and to remove the environmental polluting impurities, such as odor, B.O.D. and C.O.D. laden in the vapor, so that the apparatus and method remarkably save the cost for the heating energy. The apparatus saves the energy by 2-10 times in comparison with the conventional apparatus.

Description

Evaporation and concentration and drying equipment and method
Relate generally to evaporation of the present invention and concentration and drying equipment and method, the particularly improvement of a this apparatus and method for aspect, be used for reclaiming and utilize again the vaporization heat by liquefaction under a certain high temperature, that is appear at latent heat in supercharging or the reduction vaporization process, so that save heat energy, and the various impurity that are used under a certain high temperature oxidation or carbonization evaporation, such as the smell, B.O.D. and the C.O.D. that are filled in the steam, so that remove the various impurity of evaporation and the water of condensation of better quality is provided.
In traditional evaporation equipment, be used for vapour coagulate steam water coolant must with the required heat of evaporation, that is boiling heat (100Kcal) and vaporize that (vaporization heat 539Kcal/l) is added on equipment to heat together.Stating evaporation equipment in the use prepares under the situation of distilled water such as wet feeds such as wet mud or waste water by evaporating and concentrating, part environmental pollution impurity, smell, B.O.D. and C.O.D. such as being filled in the wet feed evaporate with steam, thereby are full of in steam.The various impurity of injection in steam itself are liquefied with steam when condensing steam again.Distilled water thereby can not reach the standard water quality of permission, thus distilled water need handle again, so that reach the standard quality of permission.
General evaporation equipment and general evaporation method can not reclaim and utilize again the vaporization heat (539 Kcal/l) of steam, but be used for cooling off the vapour system of coagulating that is full of the steam of various impurity with condensation by one latent heat have been discarded.Secondly, this discarded must the accompanying of latent heat with great amount of cost.
In addition, general evaporation equipment or general evaporation method can not be removed various impurity, and such as smell, B.O.D. and C.O.D., these impurity evaporate with steam and liquefy and reduced the quality of distilled water.In this connection, distilled water must be handled so that improve the quality of distilled water through an other water treatment procedure.The other water treatment procedure that is used to improve the distilled water quality is very complicated and has improved the cost of preparation distilled water.
When using a decompression evaporation method to evaporate the water to become steam, the vaporization heat can be saved by the size corresponding to the reduction pressure of a certain vacuum tightness.But, still there is a difficult problem in this decompression evaporation method, and promptly water of condensation is full of smell, B.O.D. and C.O.D., thereby water of condensation need be handled by other deodorization and water purification process.
In general heating evaporation equipment, the required total heat of water of under atmospheric pressure evaporating one liter of zero degree (0 ℃) is 639Kcal.That is making water is 100Kcal at 100 ℃ of ebullient boiling heats, and the vaporization heat that is used to evaporate boiled water is 539 Kcal, thereby the total heat that is used to evaporate a premium on currency is 639 Kcal, that is, 100Kcal+539Kcal=639Kcal.When using the water of decompression evaporation device 1 liter of zero degree of evaporation (0 ℃), be that water seethes with excitement in the time of 35 ℃ under the condition of about 10Torr (750mmHg) in vacuum tightness, so that the total heat that is used to evaporate 1 premium on currency is 605Kcal, and promptly (at evaporating pressure is 0.1Kg/cm to 35Kcal+570Kcal=605Kcal 2During A, latent heat can be about 570Kcal).
But, general evaporation equipment must use a vapour condenser with condensation and liquefaction steam, so that is used for the water coolant that vapour coagulates in a large number and must be added on equipment.Secondly, the latent heat of steam (539Kcal) can not reclaim and reuse, but has discarded.
Schematic illustration mistake is being used or general decompression evaporation method or general heating evaporation method when under atmospheric pressure evaporating the water of one liter of zero degree (0 ℃), and the total heat that remains to be applied to water is 574Kcal or 639Kcal.Secondly, be used for providing the additional energy of water coolant must be added on equipment to condenser.In the process of condensing steam, vaporization heat (539Kcal) can not reclaim and discard.In addition, general evaporation equipment itself can not be removed various environmental pollution impurity from water of condensation, and such as smell, B.O.D. and C.O.D., so that water of condensation need be handled by other deodorization and water purification process.
Thereby, the purpose of this invention is to provide a kind of evaporation and concentration and drying equipment and method, wherein, above variety of issue is overcome and the high-quality water of condensation can be provided and save vaporization energy, so that by utilizing the potential that in supercharging or reduction vaporization process, is occurred to save heat energy again, and can be widely used in and make pollutant effluents become distilled water, purify liquid waste and the various environmental pollution mud of concentrate drying.
Equipment of the present invention and method are recyclable and utilize heat energy again, this energy is applied to steam so that steam-heated cal(l)andria is carried out oxidation or carbonization to a certain high temperature, and remove the various environmental pollution impurity that are filled in the steam, such as smell, B.O.D. and C.O.D. etc., thereby this equipment and method can be saved the cost that is used for heat energy significantly.
The present invention compares with traditional equipment, can reduce the production cost of evaporation equipment and the running cost of equipment, thereby provides economic benefit for the user.Compare present device with traditional equipment and also can save 2 to 10 times of energy.In equipment of the present invention, being full of smell in steam and various impurity can be oxidized during to a certain high temperature and carbonization and removing fully from steam in steam-heated cal(l)andria, so that this equipment can provide high-quality distilled water and need not use other water-purification plant.
The above and other projects of the present invention, characteristics and other every advantages will obtain understanding more clearly by the detailed description of doing below in conjunction with each accompanying drawing, wherein
Fig. 1 is the evaporation of one embodiment of the present invention and the part sectioned view of concentration and drying equipment;
Fig. 2 is the skeleton view of a heat reclaim unit of Fig. 1 equipment, shows the internal structure of this device;
Fig. 3 is the partial cutaway frontview of Fig. 2 heat reclaim unit, shows the heat exchange state between adverse current high-temperature vapour and the drag flow low-temperature steam in this device;
Fig. 4 is the fragmentary, perspective view of agitation blades and board-like sweating room, and these blades and chamber are installed among the vaporizer of Fig. 1 equipment; And
Fig. 5 is the partial enlarged view of presentation graphs 4 each board-like sweating room.
Referring to Fig. 1, wherein show the evaporation of one embodiment of the present invention and the structure of concentration and drying equipment with part sectioned view.Among this figure, Reference numeral 1 expression one is used to hold and remains the container of the wet feed (wet material) handled by evaporation.Wherein be equipped with the container 1 of a coil pipe R to be provided with one first inlet 15a at its top, be used to be filled with pending wet feed, such as water or wet mud.The shell of container 1 is the dual structure wallboard, and this dual structure wallboard is used for from reclaiming used heat container 1 round-robin water of condensation.Container 1 is connected with being used to evaporate with the vaporizer 10 of concentrate drying wet feed, this vaporizer 10 be a stirring type vaporizer and therein splendid attire such as wet feeds such as waste water or wet mud.This vaporizer 10 is provided with one second inlet 15b at its top, be used for optionally loading the wet feed that remains to be evaporated.This vaporizer 10 is done circular on its bottom and in the bottom of rounded bottom next door sidewall one groove 11 is arranged.One is used for the spiral 11s that mud drains into vaporizer 10 outsides is placed among the groove 11.In order to stir the wet feed in the vaporizer 10, many board-like semicircle sweating rooms 13 are arranged among the vaporizer 10 vertically, so that these chamber 13 along continuous straight runs arrangements and equidistantly spaced apart each other, shown in Figure 4 and 5.Many agitation blades 12 are arranged between each chamber 13.Each blade 12 all can rotate along opposite both direction in the space of being defined by each chamber 13, thereby stir wet feed to be evaporated is arranged.As shown in Figure 5, the inner end portion of the opposing sidewalls of each board-like sweating room 13 is tapered to a single spine smoothly, thereby makes each agitation blades 12 between each board-like sweating room 13 do level and smooth the rotation.Each agitation blades 12 is sleeved on the blades axes S, and this S extends along the center of vaporizer 10 in the longitudinal direction.Each board-like sweating room 13 is connected with a sweating room 14 in the dual structure wallboard that is formed on vaporizer 10.The top of vaporizer 10 is connected in an overflow preventing chamber 17 via a pipe connecting 16, and this overflow preventing chamber 17 itself is connected in the inside of vaporizer 10 again via a U-bend 18.Bend pipe 18 stretches to the inside of vaporizer 10 from the bottom of chamber 17.
One first conduit R 1Stretch to a steam compressed turbine (va-por compressing turbine) 20 from the top of overflow preventing chamber 17.Conduit R 1Be provided with a control valve 21, be used for to flowing in conduit R 1Among the steam supply preheated air.The rear end of steam compressed turbine 20 itself is again via one second conduit R 2Be connected in a steam compressed pump 30.One the 3rd conduit R 3Stretch to a heat reclaim unit 60 from steam compressed pump 30.As shown in Figures 1 to 3, be suitable for reclaiming heat and this heat reclaim unit 60 that the heat that reclaims is used further to the preheating low-temperature steam being equipped with a branch of the 9th conduit or steam duct R from high-temperature vapour 9, these conduits R 9Along continuous straight runs extends and is equidistantly spaced apart among device 60.The opposite ends of heat reclaim unit 60 itself is again respectively via the 4th and the 6th conduit R 4And R 6Be connected in a donkey boiler 40 and the vaporizer 10 with the heating unit of oneself.In donkey boiler 40, the 4th conduit R 4Be connected in a steam-heated cal(l)andria coil pipe 42 of a burner 41 nozzle fronts.Burner 41 is contained in the antetheca of boiler 40 and generates the flame that will be directed to boiler 40 inside.Around the coil pipe 42 of the steam-heated cal(l)andria chamber 43 in the boiler 40 itself again via one the 5th conduit R 5Be connected in heat reclaim unit 60.Like this, the latent heat of steam can be reclaimed and is reused for preheating and be flowing in steam duct R by device 60 9Among low-temperature steam.
The 7th conduit R with a pressure-regulator 51 and a dump valve 52 7Extend and be connected in container 1 from the sweating room 14 of vaporizer 10 at the rounded bottom place of vaporizer 10.In container 1, water of condensation loses heat by coil pipe R the time.After this, water of condensation is admitted to a condensation pond 50, thereby is collected among the pond 50.
In the operation of aforesaid device, wet feed to be evaporated is arranged, such as waste water, by the first inlet 15a threading container 1 of container 1, this container 1 can reclaim used heat from water of condensation.Waste water itself is again via one the 8th conduit R 8Be sent to vaporizer 10, thereby in vaporizer 10, be evaporated or concentrate drying and become steam.Steam itself flows to overflow preventing chamber 17 via pipe connecting 16 again, and subsequently via the first conduit R 1Be sent to turbine 20.Before steam is sent to turbine 20, the first conduit R 1Control valve 21 add the preheated air of proper amt to steam.At this, the preheated air that makes an addition to steam according to the characteristic that is full of the various impurity that are evaporated in steam is in order to promote the oxidation of these impurity.But, should be appreciated that and not add under the situation of preheated air that the steam that is full of various impurity at high temperature may carbonization according to the characteristic of evaporation main body.At this moment, evaporator room 10 is because vacuum is pumped in the effect of steam compressed turbine 20 and steam compressed pump 30, so that vaporizer 10 has about 60 ℃ internal temperature and the vacuum tightness of scope from about 300mmHg (mmhg) to about 400mmHg.After this steam is compressed by steam compressed pump 30 again, so that vapor pressure increases.
High compressed steam itself is again via the 3rd conduit R 3Send the steam duct R of heat reclaim unit 60 to 9And from installing 60 via the 4th conduit R 4Be discharged into donkey boiler 40.In donkey boiler 40, steam is heated by vapor heating equipment by steam heating pipe 42 and steam-heated cal(l)andria chamber 43 time, thereby becomes high-temperature vapour, and the temperature range of this steam is from about 600 ℃ to 800 ℃.Because steam is heated in boiler 40, be full of the various impurity in steam, such as smell, B.O.D. and C.O.D., removed by oxidation and carbonization.Steam after by boiler 40 heating via the 5th conduit R 5Return heat reclaim unit 60.In device 60,600 ℃ to 800 ℃ steam and live steam heat-shift, the conduit R of the new feeder 60 of this live steam 9And has scope from 60 ℃ to 100 ℃ low temperature.In heat reclaim unit 60, respectively guided dividing plate guiding steam duct R by the steam of the vapor heating equipment of boiler 40 heating by device 60 9On every side, low-temperature steam is from conduit R 9By.That is, the high-temperature vapour of device in 60 in a zigzag path from install 60 rear portion flow to anterior and with from the front portion backward portion by conduit R 9The low-temperature steam heat-shift.
As shown in Figure 2, each is guided dividing plate and can be placed among the heat reclaim unit 60 vertically, so that each dividing plate is spaced apart with equidistant from distance.The heat exchanger time of steam in each dividing plate meeting extension fixture 60, thereby the heat exchange effect of raising device 60.But, in the fs of operation of equipment, the water in the boiler 40 is heated by the heating unit of boiler 40, thereby becomes high-temperature steam.The high-temperature steam of the boiler 40 of process carbonization or oxidation is again via 1 the tenth conduit R 10, have the 3rd a conduit R of setter 51 3, heat reclaim unit 60, the 4th conduit R 4, boiler 40, the 5th conduit R 5, the device the 60 and the 6th conduit R 6Offer each board-like sweating room 13 and sweating room 14 of vaporizer 10.In vaporizer 10,, thereby make waste water become about 60 ℃ to 100 ℃ low-temperature steam from the high-temperature steam and the waste water heat-shift of boiler 40 supplies.About 60 ℃ to 100 ℃ steam is sent to heat reclaim unit 60 through said process and absorbs via the 5th conduit R 5The heat of the high-temperature vapour of supplying with from boiler 40.Because heat exchange, the temperature of low-temperature steam increases to 450 ℃ to 600 ℃ from 60 ℃ to 100 ℃.450 ℃ to 600 ℃ pre-heat steam itself is again via the 4th conduit R 4Be discharged into boiler 40 from installing 60.Simultaneously, temperature is reduced to 150 ℃ to 200 ℃ steam via the 6th conduit R owing to carry out heat exchange in heat reclaim unit 60 6Be discharged into vaporizer 10.
Via the 4th conduit R 4From install 60 450 ℃ to 600 ℃ pre-heat steams that are discharged into boiler 40 boiler 40 by the heat of steam device heating of boiler 40 and be sent to steam-heated cal(l)andria coil pipe 42 and steam-heated cal(l)andria chamber 43, thereby oxidized or carbonization and become 600 ℃ to 800 ℃ high-temperature vapour.Boiler 40 through the steam of peroxidation or carbonization via the 5th conduit R 5Be sent to device 60, and along zigzag channel from install 60 rear portion flow to anterior, with from the front portion backward portion by conduit R 960 ℃ to 100 ℃ low-temperature steam heat-shifts.At this, in boiler 40, put on steam and heating steam and vapour temperature brought up to 600 ℃ to 800 ℃ heat energy and in heat reclaim unit 60, reclaimed by vapor heating equipment.That is, be filled in 600 ℃ to the 800 ℃ heat energy in the high-temperature vapour and be recovered and be reused for pre-heated flow through installing 60 steam duct R 9Steam, as shown in Figure 3.Because preheating, the temperature of the steam of sending here from vaporizer 10 is brought up to 450 ℃ to 600 ℃ from 60 ℃ to 80 ℃.Bring up to 450 ℃ to 600 ℃ by carry out heat exchange in device 60 from 60 ℃ to 80 ℃ owing to will be sent to the temperature of the steam of boiler 40, the heat energy of boiler 40 heating units can greatly be saved.
Via the 6th conduit R 6Discharge and have each board-like sweating room 13 and sweating room 14 that 150 ℃ to 200 ℃ temperature and its various impurity steam oxidized or carbonization are supplied to vaporizer 10 from installing 60.In vaporizer 10, from installing 60 steam and the waste water heat-shifts of supplying with, thereby lose its vaporization heat and be liquefied and become the water of condensation of relatively-high temperature, so that the water of vaporizer 10 or wet feed reclaim 539Kcal by means of liquefaction at high temperature from steam (at evaporating pressure is 1.013Kg/cm 2During A) latent heat.About 80 ℃ to 120 ℃ this water of condensation itself is again via having the two the 7th conduit R of pressure-regulator 51 and dump valve 52 concurrently 7Be sent to the coil pipe R of container 1.Coil pipe R reclaims used heat once more from water of condensation.Water of condensation is collected among the condensation pond 50.Behind filter freezing water in pond 50, be removed from water of condensation through the various impurity of peroxidation or carbonization, thereby make water of condensation become good distilled water.
In the above-described embodiments, waste water is evaporated by reducing to method of evaporating.But, should be appreciated that waste water can be evaporated being not less than under the atmospheric a certain high pressure.That is equipment of the present invention can evaporate waste water under the pressurization situation.
Operating effect of the present invention will be illustrated following.
There are wet feed to be evaporated or waste water to absorb used heat in the container 1 from the high-temperature condensation water of the coil pipe R that flows through.After this, because the hypotensive effect of steam compressed turbine 20 and the hypotensive effect of steam compressed pump 30, the waste water of process preheating is via the 8th conduit R 8Naturally and understandably be introduced into vaporizer 10.In vaporizer 10, each agitation blades 12 stirs evenly waste water, so that waste water will be evaporated as following.After mixing pre-thermal wastewater, the screenings of waste water is collected among the groove 11 of vaporizer 10.Screenings in the groove 11 itself is discharged into the outside of vaporizer 10 again by screenings discharging spiral 11s.Simultaneously, stay not with the waste water of screenings among each the board-like sweating room 13 that is flowing in vaporizer 10 and 150 ℃ to 200 ℃ the high-temperature vapour that is flowing among the sweating room 14 absorb the vaporization heat, thereby be evaporated and become low-temperature steam.The waste water itself that is in vapor state is sent to overflow preventing chamber 17 via pipe connecting 16 from vaporizer 10 again, this overflow preventing chamber 17 has U-bend 18, extends to the inside of vaporizer 10 from the bottom of chamber 17 and is suitable for preventing that waste water from may overflow vaporizer 10 during the evaporation vaporizer 10.The steam of waste water is after this via the first conduit R that stretches to steam compressed turbine 20 from the top of chamber 17 1Be sent to steam compressed turbine 20.Before steam was sent turbine 20 to, steam can optionally add the preheated air of pre-determined quantity under the control of control valve 21, and this valve 21 is placed in the front of the vapour inlet of turbine 20.
The steam of steam compressed turbine 20 itself is sent to steam compressed pump 30 again, and wherein steam is compressed to increase its pressure.At this moment, the waste water in the vaporizer 10 evaporates under about 60 ℃ temperature owing to the step-down situation in the vaporizer 10.In addition, because the hypotensive effect of steam compressed turbine 20 and because the hypotensive effect of steam compressed pump 30, vaporizer 10 reach are from about 300mmHg to the about vacuum tightness of 400mmHg.(E-1) is indicated as following fundamental equation about perfect gas, and vapor pressure both can also can be improved by pump 30 by turbine 20, so that steam is liquefied under a certain high pressure and a certain high temperature.Certainly, equipment of the present invention can use a kind of vacuum gooster pump (vacuum booster), a kind of vacuum molecular pump or a kind of steam compressor arrangement, replaces the steam compressed turbine 20 of above-mentioned main embodiment.
PV=n tRT......................... (E-1) wherein
The P-vapor pressure;
The V-vapor volume;
The absolute temperature of T-steam;
The R-gas law constant; And
n t-be included in the total mole number of all gases in the steam of volume V.
Steam itself passes through the steam duct R of heat reclaim unit 60 again under the condition that vapor pressure is increased by turbine 20 and pump 30 9Passing through steam duct R 9The time, steam is from centering on conduit R device 60 9The high-temperature vapour of adverse current absorbs heat.Be full of the steam of various impurity, at conduit R 9In through after the preheating, be sent to the steam-heated cal(l)andria chamber 43 of boiler 40 and be heated to 600 ℃ to 800 ℃ temperature by the vapor heating equipment of boiler 40, thus oxidized or carbonization.High-temperature vapour oxidized or carbonization turns back to heat reclaim unit 60 and center on steam duct R along the zigzag path in device 60 9Countercurrent flow.At this moment, by new feeder 60 and have 60 ℃ to the new steam of 100 ℃ of lesser tempss steam duct R at device 60 9Among flow.In device 60, once the steam that is heated by the vapor heating equipment of boiler 40 by device 60 along vertical direction lay respectively guide the dividing plate guiding and around steam duct R 9Thereby, with the live steam heat-shift, shown in Fig. 2 and 3.
Be preheated to 450 ℃ of steams to 600 ℃ of temperature via the 4th conduit R 4Be sent to steam heating pipe 42 and steam-heated cal(l)andria chamber 43, thereby become 600 ℃ to 800 ℃ high-temperature vapour of oxidized or carbonization.Simultaneously, lose heat energy and temperature and be lowered to 150 ℃ to 200 ℃ steam via conduit R 6Be sent to each board-like sweating room 13 and sweating room 14 of vaporizer 10.When each board-like sweating room 13 by vaporizer 10 and sweating room 14,150 ℃ to 200 ℃ steam and waste water heat-shift, thus be liquefied and become about 80 ℃ to 120 ℃ water of condensation.This is because as indicated in the above-mentioned equation E-1, owing to steam liquefies under a certain temperature that is proportional to vapor pressure, high compressed steam liquefies under a certain high temperature that is proportional to its vapor pressure.
About 80 ℃ to 120 ℃ water of condensation itself is again via the 7th conduit R with pressure-regulator 51 and dump valve 52 7Be sent to the coil pipe R of container 1.Coil pipe R reclaims used heat and used heat is given the waste water of container 1 from water of condensation once more.Water of condensation is collected in condensation pond 50 after losing used heat.On the other hand, utilizing the latent heat that reclaimed by vaporizer 10 is that 60 ℃ to 100 ℃ steam is sent to heat reclaim unit 60 via overflow preventing chamber 17 by the prepared temperature of evaporation waste water.
Various impurity in the steam, such as smell, B.O.D. and C.O.D., they and steam together evaporate and are full of among steam, and with the preheated air blending mutually of the pre-determined quantity of being supplied with by control valve 21, this valve 21 is placed in the front of the vapour inlet of turbine 20.Because with preheated air blending mutually, the various impurity of steam become oxidable impurity.Oxidable impurity is sent to the vapor heating equipment of boiler 40, that is steam heating pipe 42 and steam-heated cal(l)andria chamber 43.Thereby various impurity are oxidized and burning under 600 ℃ to 800 ℃ high temperature atmosphere in boiler 40, thereby removes from steam.In addition, do not adding according to the steam characteristic under the situation of preheated air, from steam, removing such as various impurity such as smell, B.O.D. and C.O.D. thereby the steam that is full of various impurity can be carbonized under 600 ℃ to 800 ℃ high temperature atmosphere.Once be applied to steam by the vapor heating equipment of boiler 40 and reclaim and be reused for low-temperature steams in the primary heater unit 60 by device 60 with the steam-heated cal(l)andria energy that produces the high temperature atmosphere.In this connection, the equipment of the present invention steam-heated cal(l)andria amount of energy of saving equals to be used for the recovered energy of primary heater unit 60 steams.
Should be appreciated that equipment of the present invention can improve its energy efficiency by container 1, vaporizer 10, donkey boiler 40 etc. are done heat insulation disposal.
In order to measure the utilization effect of present device and method, once carried out a following example.That is, as the movement that wet feed to be evaporated is arranged once be heated under 620 ℃, oxidation and burning or under 620 ℃, be heated and carbonization.The result is shown in following table (T-1).Shown in table (T-1), use present device and can be purified the most effectively according to the handled wet feed of the inventive method.
Table (T-1) ingredient standard result
(A) (B) pH 5.8-8.6 9.0 9.8COD 150 (mg/l) 6.4 (mg/l) 6.6 (mg/l) BOD 150 (mg/l) 5.6 (mg/l) 5.9 (mg/l) SS 150 (mg/l) 4.0 (mg/l) 4.5 (mg/l) n-hexanes 30 (mg/l) 0.8 (mg/l) 4.0 (mg/l) T-N 60 (mg/l) 16.1 (mg/l) 16.5 (mg/l) T-P 8 (mg/l) 0.033 (mg/l) 0.034 (mg/l) NH3-N-5.358 (mg/l) 4.632 (mg/l)
As mentioned above, the present invention compares with traditional evaporation equipment and can reduce the cost of producing evaporation and concentration and drying equipment and the running cost of this equipment, thereby provides economic benefit for the user.This equipment also can keep its improved performance, so that this equipment can prepare good distilled water and be widely used in poisonous waste water and the evaporation and the concentrate drying of environmental pollution waste water with low cost, and the evaporation of discarded slurry, concentrates and dry.Secondly, the recyclable steam-heated cal(l)andria energy of the heat reclaim unit of present device, this energy once be applied to steam by the heating unit of boiler in case steam-heated cal(l)andria to a certain high temperature and remove injection in steam such as various impurity such as smell, B.O.D. and C.O.D..The energy that reclaims is reused for the steam that heat reclaim unit is newly sent in preheating to.In this connection, the heat energy quantity saved of present device equals to be used for the recovered energy of preheating quantity retrieving arrangement steam.
Although the every preferred embodiment of the present invention is disclosed for the purpose of illustration, but person skilled in the art are to be understood that, do not deviating under appended every claim condition illustrated, category of the present invention and spirit, various changes, additional and replacement all are possible.

Claims (3)

1, a kind of evaporation and concentration and drying equipment, wherein improvements comprise:
One is used for holding therein the container of wet feed, and described container has a pair of double wall plate structure and is equipped with a coil pipe, its top to be provided with one first inlet therein, is used for wet feed is loaded in container, and described coil pipe is connected in a condensation pond;
One is used to reclaim steam latent heat and utilizes the stirring formula vaporizer of the latent heat evaporation wet feed that reclaims, and described vaporizer is via a bottom that is used for being connected in from the conduit that container receives wet feed described container, and described vaporizer comprises:
One is located at second inlet at vaporizer top;
The bottom of one circle;
One is located near on the sidewall of rounded bottom and be equipped with a groove that is used for screenings is discharged into the vaporizer outside;
A plurality of board-like semicircle sweating rooms that communicate with each other, each described board-like sweating room is installed in the inside of vaporizer vertically, thereby each board-like chamber along continuous straight runs is arranged and is spaced apart equally spacedly, and the conduit that described each board-like chamber had not only had a pressure-regulator via but also had a dump valve is connected in the described coil pipe of container;
A plurality of agitation blades that are used for stirring the vaporizer wet feed, described each blade are between described each board-like chamber, and each blade can two-wayly rotate, so that stir wet feed equably;
One extends and supports the blades axes of each agitation blades at length direction along the center of described vaporizer; And
One is used for preventing that liquid from overflowing the overflow preventing chamber of described vaporizer during evaporating, described overflow preventing chamber is connected in the top of vaporizer via a pipe connecting and has one stretches into the U-bend of vaporizer inside from its bottom;
One is used to reclaim the latent heat of steam and be used for low-temperature steam is wherein sent in preheating to from vaporizer heat reclaim unit, described device via each relevant conduit be connected in described vaporizer, around inlet, each board-like sweating room of described vaporizer and the outlet of steam-heated cal(l)andria coil pipe of the steam-heated cal(l)andria coil pipe of the steam-heated cal(l)andria chamber of a donkey boiler, described device comprises:
Many the steam ducts that along continuous straight runs extends, each bar steam duct that described along continuous straight runs extends therefrom passes through low-temperature steam; And
A plurality of being installed in the device and dividing plate equidistantly spaced apart vertically;
Described donkey boiler be used for from heat reclaim unit accept pre-heat steam and the preheating steam-heated cal(l)andria to a certain high temperature so that oxidation or carbonization steam, described donkey boiler is connected in heat reclaim unit and has a burner, described steam-heated cal(l)andria coil pipe and steam-heated cal(l)andria chamber;
An one steam compressed turbine and a steam compressed pump are used to compress the steam supplied with from vaporizer improving vapor pressure, and the two all is located at turbine and pump from the overflow preventing chamber of vaporizer and stretches on the conduit of heat reclaim unit; And
One preheated air supply control valve is located on the conduit of described steam compressed turbine front, and described valve is suitable for controlling and feeds to the preheated air that flows to the steam of heat reclaim unit from vaporizer via conduit.
2, according to the described equipment of claim 1, wherein, the inner end portion of the opposed side walls of each board-like sweating room of vaporizer is the single spine of tandem to smoothly, thereby described each agitation blades that is placed between each board-like sweating room is smoothly rotated.
3, a kind of evaporation and concentrate drying method comprise following each step:
Heat water in the donkey boiler to produce steam, and from described steam, remove various impurity by carbonization or oxidation steam, steam is fed to a plurality of board-like sweating room of a vaporizer so that the wet feed heat-shift in steam and the vaporizer, and a conduit that via existing pressure-regulator dump valve is arranged again after heat exchange drains into the coil pipe of a wet feed container to steam, thereby from vapor recovery used heat;
Steam compressed turbine and steam compressed pump improve or the interior pressure of reduction vaporizer by operating, thereby send wet feed to vaporizer from container, and mix wet feed equably by the rightabout rotation of a plurality of agitation blades of vaporizer, so that wet feed be flowing in each board-like sweating room 150 ℃ to 200 ℃ through the steam heat-shift of carbonization and evaporate wet feed, and, simultaneously the screenings of wet feed is collected in a groove of vaporizer so that screenings is discharged into the outside discharging from vaporizer via a pipe connecting by 60 ℃ to 100 ℃ steam of wet feed generation;
Make and be included in 60 ℃ to the 100 ℃ overflow liquid in the steam and turn back to vaporizer via a U-bend of overflow preventing chamber, supply with control valve and optionally preheated air is fed to described 60 ℃ to 100 ℃ steam by operating a preheated air, and the two sends many steam ducts of heat reclaim unit to by means of steam compressed turbine and steam compressed pump 60 ℃ to 100 ℃ steam;
Make 60 ℃ to 100 ℃ steam in each steam duct of heat reclaim unit and 600 ℃ to 800 ℃ high-temperature vapour heat-shift, described 600 ℃ to 800 ℃ steam for from described donkey boiler and under each dividing plate guiding that the equi-spaced apart of device comes in device along zigzag channel, around each steam duct reversed flow, steam is preheating to 450 ℃ to 600 ℃ from 60 ℃ to 100, and being discharged into each board-like sweating room of vaporizer from heat reclaim unit, simultaneously steam-heated cal(l)andria coil pipe and the steam-heated cal(l)andria chamber of sending described donkey boiler through 450 ℃ to 600 ℃ steam of preheating to because its temperature of heat exchange is reduced to 150 ℃ to 200 ℃ steam from 600 ℃ to 800 ℃;
Use the burner heating to flow in the steam-heated cal(l)andria coil pipe of described donkey boiler and steam-heated cal(l)andria chamber 450 ℃ to 600 ℃ pre-heat steam among the two, thereby the temperature of steam is brought up to the smell of 600 ℃ to 800 ℃ and oxidation or the pre-heat steam of carbonization and various impurity so that remove smell and various impurity from 450 ℃ to 600 ℃, and the steam that makes 600 ℃ to 800 ℃ returns described heat reclaim unit, so that make 600 ℃ to 800 ℃ high-temperature vapour make thermal exchange with 60 ℃ to 100 ℃ low-temperature steam in each steam duct that is flowing in heat reclaim unit; And
Make 150 ℃ to 200 ℃ steam and the water and the wet feed heat-shift of vaporizer in each board-like sweating room of vaporizer, from steam, reclaim the latent heat of 539 Kcal by means of liquefaction under a certain high temperature, thereby make steam become about 80 ℃ to 120 ℃ water of condensation, there is the conduit of dump valve about 80 ℃ to 120 ℃ water of condensation to be sent to the described coil pipe of container again by means of described existing pressure-regulator, thereby make water of condensation once more with the wet feed heat-shift of container and from water of condensation, reclaim used heat, and vapour is coagulated water be collected among the condensation pond.
CN94194698A 1993-11-23 1994-11-17 Vaporizing and concentration drying apparatus and method Expired - Fee Related CN1097559C (en)

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CN101730665B (en) * 2007-06-04 2012-01-25 莱德尔控股有限公司 System and method for drying a water-containing substance
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CN109734234A (en) * 2019-02-22 2019-05-10 江苏和顺环保有限公司 A kind of processing unit of copper-containing wastewater
CN109734249A (en) * 2019-02-22 2019-05-10 江苏和顺环保有限公司 A kind of heavy-metal waste water treatment device
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AU1121895A (en) 1995-06-13
JPH09507036A (en) 1997-07-15
RU2145573C1 (en) 2000-02-20
BR9408150A (en) 1997-08-05
KR950014827A (en) 1995-06-16
AU690172B2 (en) 1998-04-23
WO1995014640A1 (en) 1995-06-01
CN1097559C (en) 2003-01-01
EP0730561A1 (en) 1996-09-11
KR0119766B1 (en) 1997-10-29
CA2177161A1 (en) 1995-06-01
CA2177161C (en) 2001-09-11

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