CN105887108B - Hydrochloric acid exhausted liquid reclaiming process and system - Google Patents
Hydrochloric acid exhausted liquid reclaiming process and system Download PDFInfo
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- CN105887108B CN105887108B CN201610208932.4A CN201610208932A CN105887108B CN 105887108 B CN105887108 B CN 105887108B CN 201610208932 A CN201610208932 A CN 201610208932A CN 105887108 B CN105887108 B CN 105887108B
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- C—CHEMISTRY; METALLURGY
- C23—COATING METALLIC MATERIAL; COATING MATERIAL WITH METALLIC MATERIAL; CHEMICAL SURFACE TREATMENT; DIFFUSION TREATMENT OF METALLIC MATERIAL; COATING BY VACUUM EVAPORATION, BY SPUTTERING, BY ION IMPLANTATION OR BY CHEMICAL VAPOUR DEPOSITION, IN GENERAL; INHIBITING CORROSION OF METALLIC MATERIAL OR INCRUSTATION IN GENERAL
- C23G—CLEANING OR DE-GREASING OF METALLIC MATERIAL BY CHEMICAL METHODS OTHER THAN ELECTROLYSIS
- C23G1/00—Cleaning or pickling metallic material with solutions or molten salts
- C23G1/36—Regeneration of waste pickling liquors
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
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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
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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
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Abstract
The present invention relates to a kind of hydrochloric acid exhausted liquid reclaiming process, this method uses spray roasting, is used to preheat a part at least within for the hydrochloride waste for entering Venturi preconcentrator by recycling the part of waste heat of circulation fluid of first order washing mechanism.Further relate to a kind of hydrochloride waste regenerative system, including passing through the sequentially connected roaster of flue, Venturi preconcentrator, absorption tower and at least one level washing mechanism, in being provided with heat exchange mechanisms on the circulation liquid pipeline of first order washing mechanism, the refrigerant inlet of heat exchange mechanisms is connect with hydrochloride waste storage tank, and refrigerant exit is connect with Venturi preconcentrator.Hydrochloride waste is preheated by the circulation fluid of first order washing mechanism, it is energy-saving, the efficiency of regeneration of hydrochloric acid recycling can be improved；Cool down simultaneously to the circulation fluid of first order washing mechanism, the circulation fluid of low temperature and the heat exchange amount of flue gas are bigger, and the washing effect of first order washing mechanism and the assimilation effect on absorption tower can be improved.
Description
Technical field
The present invention relates to a kind of hydrochloric acid exhausted liquid reclaiming process and regenerative systems.
Background technique
The hydrochloric acid pickling waste liquor that steel or chemical company generate, generally carries out hydrochloride waste using spray roasting at present
Regeneration treatment, include the following steps: (1) hydrochloride waste be directly entered Venturi preconcentrator heating concentration after, through venturi
Roaster is sprayed into misty drop after pre-concentrator circulating pump and the pressurization of roaster charging pump, drop is in roaster through chemistry
After reaction, generates and contain HCl, H2O、O2、CO2、N2With a small amount of Fe2O3The high-temperature flue gas (390~410 DEG C) of powder；(2) above-mentioned high temperature
Flue gas enters in Venturi preconcentrator to exchange heat with hydrochloride waste, and flue gas cooled down, dedusting, and hydrochloride waste is then heated,
The temperature of flue gas is reduced to 95~100 DEG C；(3) enter absorption tower from bottom from the flue gas that Venturi preconcentrator comes out, absorb
Tower sprays into rinse water from top, and the rinse water reverse convection of high-temperature flue gas and spray carries out a large amount of heat exchange, cigarette in packing area
The rinse water that HCl in gas is sprayed absorbs, and flue-gas temperature is reduced to 85~90 DEG C；(3) text is entered by the flue gas that absorption tower is discharged
In mound the washing facilitys such as washer, scrubbing tower cooled down, dedusting, flue-gas temperature is down to 82~87 DEG C, is discharged into atmosphere from chimney.
Hydrochloride waste, which enters, carries out heating concentration in Venturi preconcentrator, roaster is just sprayed into after reaching a certain concentration
It is inside chemically reacted, this process needs to provide a large amount of heat and is just able to achieve；This partial heat is mainly by roaster system
It provides, need to expend a large amount of fuel can realize, not meet energy-saving requirement.And from roaster, Venturi preconcentrator
The mixed flue gas temperature of middle discharge is still up to 95~100 DEG C, by the routine such as absorption tower, washing facility cooling, at dedusting
After reason, the flue-gas temperature being discharged from chimney is still up to 80~85 DEG C, and under conventional ambient temperature conditions, the tail gas of discharge is general
For white, misty steam gaseous mixture, sensory effects are poor, and autumn and winter is more very.If above-mentioned hydrochloride waste regenerates unit distance
Residential block is closer, and " white cigarette the is billowing " tail gas being discharged from chimney usually can also become hydrochloride waste regeneration unit nearby residents area and occupy
The object that the people complain, can bring biggish pressure to steel or chemical company.
Summary of the invention
The embodiment of the present invention provides a kind of hydrochloric acid exhausted liquid reclaiming process and regenerative system, can at least solve the portion of the prior art
Divide defect.
The present embodiments relate to a kind of hydrochloric acid exhausted liquid reclaiming process, the methods are as follows: hydrochloride waste is pre- dense in venturi
In contracting device after heated concentration spray into roaster in, the baking flue gas of generation successively pass through Venturi preconcentrator, absorption tower and
At least one level washing mechanism is handled, wherein cooling dedusting is carried out to flue gas in Venturi preconcentrator, in absorption tower
HCl in further cooled flue gas and recovered flue gas carries out further cooling dedusting to flue gas by each washing mechanism；
The part of waste heat for recycling the circulation fluid of first order washing mechanism is used to give up to the hydrochloric acid for entering Venturi preconcentrator
A part at least within of liquid is preheated, and the circulation fluid after heat exchange sprays into the first order washing mechanism and/or absorption tower.
As one of embodiment, into the hydrochloride waste of Venturi preconcentrator, there are also part by with the roasting
Flue gas heat exchange is preheated.
As one of embodiment, the washing mechanism is multistage, at least with circulating in first order washing mechanism and second
The hydrochloride waste of flue gas and corresponding part between grade washing mechanism exchanges heat.
As one of embodiment, flue gas generation when exchanging heat with the hydrochloride waste wait preheat includes that the cooling of condensed water is mixed
Liquid is closed, which is discharged into first order washing mechanism as cleaning solution and/or is discharged into rinsing water pot as absorption
Spray liquid in tower.
The present embodiment further relates to a kind of hydrochloride waste regenerative system, including by the sequentially connected roaster of flue,
Venturi preconcentrator, absorption tower and at least one level washing mechanism are provided on the circulation liquid pipeline of first order washing mechanism
The refrigerant inlet of second heat exchange mechanisms, second heat exchange mechanisms is connect with hydrochloride waste storage tank, refrigerant exit and the literary mound
In preconcentrator connect；The circulation fluid tube outlet end of the first order washing mechanism be connected to the first order washing mechanism and/
Or absorption tower.
As one of embodiment, the first heat exchange mechanisms are provided with until being less than on wherein one section of flue, each described first
The refrigerant inlet of heat exchange mechanisms is connect with hydrochloride waste storage tank, and refrigerant exit is connect with the Venturi preconcentrator.
As one of embodiment, the system comprises multistage washing mechanisms, until being less than first order washing mechanism and the second level
First heat exchange mechanisms are provided on flue between washing mechanism.
As one of embodiment, each first heat exchange mechanisms also have cooling mixed liquid outlet, each cooling mixing
Liquid outlet is connect with the first order washing mechanism and/or rinsing water pot.
The embodiment of the present invention at least realizes as follows the utility model has the advantages that using this method and system, has recycled first order washing
Hydrochloride waste (room temperature hydrochloride waste wait enter Venturi preconcentrator in) of the part of waste heat of the circulation fluid of mechanism to cold conditions
It is preheated, makes full use of the heat of circulation fluid, reduce the waste of circulation fluid residual heat, it is energy-saving, and hydrochloric acid can be improved again
The efficiency of raw recycling；The low temperature that hydrochloride waste is utilized simultaneously cools down to the circulation fluid of first order washing mechanism, low temperature
It is bigger with the heat exchange amount of flue gas when circulation fluid is sprayed into first order washing mechanism or in absorption tower, circulation fluid can be improved first
Washing effect in grade washing mechanism and the assimilation effect in absorption tower, are effectively reduced moisture, HCl and iron oxide in flue gas
Powder particles content, exhaust gas volumn also greatly reduce, and the discharge index that chimney can be made final is far superior to the requirement of national standard, solve
Chimney exhaust emissions easily forms the defect of " white cigarette ".Based on above-mentioned beneficial effect, roaster, Venturi preconcentrator, each can be made
The lectotype selection of washing facility etc. is smaller, energy consumption is lower, to save equipment construction cost and improvement cost, reduces engineering and throws
Money.
Detailed description of the invention
In order to more clearly explain the embodiment of the invention or the technical proposal in the existing technology, to embodiment or will show below
There is attached drawing needed in technical description to be briefly described, it should be apparent that, the accompanying drawings in the following description is only this
Some embodiments of invention for those of ordinary skill in the art without creative efforts, can be with
Other attached drawings are obtained according to these attached drawings.
Fig. 1 is the structural schematic diagram of the hydrochloride waste regenerative system provided in embodiment 11；
Fig. 2 is the structural schematic diagram of the hydrochloride waste regenerative system provided in embodiment 12；
Fig. 3 is the structural schematic diagram of the hydrochloride waste regenerative system provided in embodiment 13.
Specific embodiment
Following will be combined with the drawings in the embodiments of the present invention, and technical solution in the embodiment of the present invention carries out clear, complete
Site preparation description, it is clear that described embodiments are only a part of the embodiments of the present invention, instead of all the embodiments.It is based on
Embodiment in the present invention, those of ordinary skill in the art without making creative work it is obtained it is all its
Its embodiment, shall fall within the protection scope of the present invention.
Embodiment one
The present embodiment is related to a kind of regeneration treating method of hydrochloride waste, includes the following steps:
(1) after hydrochloride waste is directly entered the heating concentration of Venturi preconcentrator 3, through Venturi preconcentrator recycle liquid pump
9 and roaster charging pump 10 pressurize after roaster 1 sprayed into misty drop, drop in roaster 1 after chemically reacting, it is raw
At containing HCl, H2O、O2、CO2、N2With a small amount of Fe2O3The high-temperature flue gas (390~410 DEG C) of powder.
(2) above-mentioned high-temperature flue gas enters in Venturi preconcentrator 3 and exchanges heat with hydrochloride waste, and flue gas is cooled down, removed
Dirt, hydrochloride waste are then heated, and the temperature of flue gas is reduced to 95~100 DEG C.
(3) enter absorption tower 4 from the flue gas that Venturi preconcentrator 3 comes out from bottom, absorption tower 4 sprays into from top and rinses
The rinse water reverse convection of water, high-temperature flue gas and spray carries out a large amount of heat exchange in packing area, and the HCl in flue gas is sprayed
Rinse water absorb, flue-gas temperature is reduced to 85~90 DEG C.
(4) enter the washing facilitys such as Venturi scrubber 5, scrubbing tower 6 by the flue gas that absorption tower 4 is discharged to be cooled down, remove
Dirt, flue-gas temperature are down to 82~87 DEG C, are discharged into atmosphere from chimney.
In the above method, in step (4), washing facility quantity can be arranged according to actual condition, but that there are problems is as follows: set
Negligible amounts are set, the exhaust temperature of discharge and dustiness etc. are all higher, easily cause environmental pollution；When setting quantity is more, energy consumption
It is higher.Generally, two-stage washing facility is set；In the present embodiment, shape is sequentially connected using Venturi scrubber 5 and scrubbing tower 6
It is washed at two-stage.
Above-mentioned regeneration treating method is spray roasting hydrochloride waste regeneration and treatment technique commonly used in the prior art, is existed
The problems such as energy consumption is higher, and the exhaust temperature of smoke stack emission is higher, easily forms " white cigarette ".
Corresponding to the above method, the present embodiment also provides a kind of hydrochloride waste regenerative system commonly used in the prior art, should
System includes by the sequentially connected roaster 1 of flue, dedusting mechanism 2, Venturi preconcentrator 3, absorption tower 4 and at least
Level-one washing mechanism.The cinder-discharging port of dedusting mechanism 2 is connect by ash-unloading tube road with 1 middle part of roaster or lower part.Venturi is pre- dense
Hydrochloride waste inlet is equipped at the top of contracting device 3, bottom is equipped with concentrating hydrochloric acid waste liquid outlet, and concentrating hydrochloric acid waste liquid outlet passes through
Supply lines are connect with 1 inlet of roaster, and supply lines are equipped with Venturi preconcentrator recycle liquid pump 9 and roaster is fed
Pump 10.Each washing mechanism is equipped with circulation liquid pipeline, realizes recycling for spray liquid；The circulation fluid of first order washing mechanism 5
There are also a branches to connect with the spraying mechanism on absorption tower 4 for pipeline, to supply rinse water to absorption tower 4.Afterbody washing mechanism
Exhanst gas outlet be connected with liquid drop separator 7 and chimney 8, by the flue gas outlet of processing.
It is general using multistage washing mechanism in above system, to improve the cooling dust removing effects to flue gas.The present embodiment
In, using Venturi scrubber 5 and the sequentially connected two-stage washing mechanism of scrubbing tower 6.Above-mentioned dedusting mechanism 2 is preferably using double
Cyclone dust collectors 2.
Embodiment two
The present embodiments relate to a kind of hydrochloric acid exhausted liquid reclaiming process, can at least solve the subproblem of the prior art.It should
Method and the regeneration treating method step of the hydrochloride waste in above-described embodiment one are essentially identical, and specific steps are no longer superfluous herein
It states；It is improved on the basis of the method for this method in example 1, specifically: hydrochloride waste is in Venturi preconcentrator
It is sprayed into roaster 1 after heated concentration in 3, the baking flue gas of generation carries out subsequent regeneration of hydrochloric acid processing and purified treatment；
Into in the hydrochloride waste of Venturi preconcentrator 3, at least partially preheated hydrochloride waste.
By preheating hydrochloride waste, hydrochloride waste can be reduced and heated in Venturi preconcentrator 3 needed for concentration
Heat, i.e., reduction hydrochloride waste in Venturi preconcentrator 3 with the heat exchange amount of baking flue gas, thus in venturi pre-concentration
Same amount of baking flue gas can heat more hydrochloride wastes in device 3, and the processing effect of Venturi preconcentrator 3 first can be improved
Rate improves the efficiency of hydrochloride waste regeneration treatment, second can reduce by 1 energy consumption of roaster.
Preferably, the preheating method of above-mentioned hydrochloride waste are as follows: baking flue gas is carried out to utilize roasting in subsequent processes
A part at least within of flue gas and the hydrochloride waste wait enter Venturi preconcentrator 3 exchanges heat, to reach to the part
The purpose that hydrochloride waste is preheated.Above-mentioned subsequent processing includes that the baking flue gas successively passes through Venturi preconcentrator 3, inhales
It receives tower 4 and at least one level washing mechanism is handled, wherein baking flue gas connects with hydrochloride waste in Venturi preconcentrator 3
Concentration heat exchange is realized in touching, and baking flue gas forms certain cooling dedusting effect in heat transfer process, and hydrochloride waste is then heated, is inhaling
The HCl in further cooled flue gas and recovered flue gas is received in tower 4, is further cooled down by each washing mechanism to flue gas
Dedusting.
Based on the subsequent treatment process of above-mentioned baking flue gas, using the exhanst gas outlet of wherein any one subsequent processing device
The flue gas to circulate in the flue of connection preheats hydrochloride waste, higher closer to 1 flue-gas temperature of roaster, then preheats
Effect is better；But in view of the needs of the 4 reclaiming hydrochloric acid of corrosivity and absorption tower of HCl heat exchanging equipment in flue gas, generally
The flue gas to circulate between Venturi preconcentrator 3 and absorption tower 4 is not used to exchange heat with hydrochloride waste.Preferably at least in
It is connected on the flue of 5 exhanst gas outlet of first order washing mechanism and is provided with the first heat exchange mechanisms 13, it is pre- dense into venturi
In the hydrochloride waste of contracting device 3, hydrochloride waste at least partially is preheated with the first of flue gas heat exchange through each first heat exchange mechanisms 13.If
Washing mechanism has multistage, it is contemplated that is respectively provided with above-mentioned first on the flue for being connected to washing mechanism exhanst gas outlets at different levels and changes
Heat engine structure 13, but increase with series, the temperature of flue gas gradually decreases, and flue gas is also poorer to the pre-heat effect of hydrochloride waste；It can also
Consider that above-mentioned first heat exchange mechanisms 13 are arranged on the flue between absorption tower 4 and first order washing mechanism 5.The present embodiment
In, be sequentially connected the second level washing mechanism constituted using by Venturi scrubber 5 and scrubbing tower 6, Venturi scrubber 5 with wash
It washs and above-mentioned first heat exchange mechanisms 13 is set on the flue between tower 6.
Hydrochloride waste is extracted by hydrochloride waste storage tank and is used as refrigerant and flue gas heat exchange into above-mentioned each first heat exchange mechanisms 13,
Realize the purpose preheated to hydrochloride waste.Both the part of waste heat for having recycled baking flue gas is (literary wait enter to the hydrochloride waste of cold conditions
Room temperature hydrochloride waste in mound in preconcentrator 3) it is preheated, the heat of baking flue gas is made full use of, fume afterheat is reduced
Waste, it is energy-saving；The low temperature for also utilizing hydrochloride waste cools down to baking flue gas, be effectively reduced moisture in flue gas,
HCl and brown iron oxide granule content, exhaust gas volumn also greatly reduce, and have more apparent dustproof function, can reduce subsequent wash
The operating pressure of mechanism, the discharge index that chimney 8 can be made final are far superior to the requirement of national standard, solve 8 tail gas of chimney row
Put the defect for easily forming " white cigarette ".Based on above-mentioned beneficial effect, roaster 1, Venturi preconcentrator 3, each washing facility can be made
Deng lectotype selection is smaller, energy consumption is lower, to save equipment construction cost and improvement cost, reduce construction investment.
Above-mentioned first heat exchange mechanisms 13 using flue gas heat-exchange unit to be preferred.Flue gas produces when exchanging heat in the first heat exchange mechanisms 13
Life includes the cooling mixed liquid of condensed water, the part cooling mixed liquid can be discharged into first order washing mechanism 5 as cleaning solution and/
Or it is discharged into rinsing water pot as the spray liquid in absorption tower 4.
Embodiment three
The present embodiments relate to a kind of hydrochloric acid exhausted liquid reclaiming process, can at least solve the subproblem of the prior art.It should
Method and the regeneration treating method step of the hydrochloride waste in above-described embodiment one are essentially identical, and specific steps are no longer superfluous herein
It states；It is improved on the basis of the method for this method in example 1, specifically: recycling first order washing mechanism 5 follows
The part of waste heat of ring liquid is used to preheat a part at least within for the hydrochloride waste for entering Venturi preconcentrator 3, changes
Circulation fluid after heat sprays into the first order washing mechanism 5 and/or absorption tower 4.I.e. in the circulation liquid pipe of first order washing mechanism 5
Setting the second heat exchange mechanisms 15 in road extract hydrochloride waste by hydrochloride waste storage tank and enter above-mentioned second heat exchange mechanisms 15 as cold
The circulation fluid of matchmaker and the first order washing mechanism 5 exchanges heat, and achievees the purpose that preheat hydrochloride waste, and the hydrochloric acid of part preheating is useless
Liquid is the second preheating hydrochloride waste.Above-mentioned second heat exchange mechanisms 15 using water water- to-water heat exchanger to be preferred.
Using the above method, hydrochloride waste of the part of waste heat to cold conditions of the circulation fluid of first order washing mechanism 5 has been recycled
(the room temperature hydrochloride waste wait enter in Venturi preconcentrator 3) is preheated, and the heat of circulation fluid is made full use of, and reduces circulation
The waste of fluid residual heat, it is energy-saving, and the efficiency of regeneration of hydrochloric acid recycling can be improved；The low temperature pair of hydrochloride waste is utilized simultaneously
The circulation fluid of first order washing mechanism 5 cools down, and the circulation fluid of low temperature sprays into first order washing mechanism 5 or in absorption tower 4
When, it is bigger with the heat exchange amount of flue gas, circulation fluid can be improved in the washing effect in first order washing mechanism 5 and in absorption tower 4
Assimilation effect, the moisture being effectively reduced in flue gas, HCl and brown iron oxide granule content, exhaust gas volumn also greatly reduce, and can make cigarette
The final discharge index of chimney 8 is far superior to the requirement of national standard, solves the defect that 8 exhaust emissions of chimney easily forms " white cigarette ".
Based on above-mentioned beneficial effect, it can make that the lectotype selection of roaster 1, Venturi preconcentrator 3, each washing facility etc. is smaller, energy consumption
It is lower, to save equipment construction cost and improvement cost, reduce construction investment.
Example IV
The present embodiments relate to a kind of hydrochloric acid exhausted liquid reclaiming process, can at least solve the subproblem of the prior art.It should
Method and the regeneration treating method step of the hydrochloride waste in above-described embodiment one are essentially identical, and specific steps are no longer superfluous herein
It states；It is improved on the basis of the method for this method in example 1, specifically: using multistage washing mechanism, the first order
In each washing mechanism after washing mechanism 5, until less than third heat exchange is provided on the wherein circulation liquid pipeline of a washing mechanism
Mechanism 14；Into in the hydrochloride waste of Venturi preconcentrator 3, at least partially through each third heat exchange mechanisms 14 and corresponding circulation
The third of liquid heat exchange preheats hydrochloride waste.Above-mentioned each third heat exchange mechanisms 14 using water water- to-water heat exchanger to be preferred.
For washing mechanism quantity more than three-level, can every level-one washing mechanism in the second level and later circulation fluid
Above-mentioned third heat exchange mechanisms 14 are respectively provided on pipeline, but flue-gas temperature is lower more rearward, flue-gas temperature is corresponding also lower, then at different levels
The temperature of the circulation fluid of washing mechanism is also lower, poorer to the pre-heat effect of hydrochloride waste.In the present embodiment, using by venturi
Washer 5 and scrubbing tower 6 are sequentially connected the second level washing mechanism of composition, are arranged on the circulation liquid pipeline of the scrubbing tower 6 above-mentioned
Third heat exchange mechanisms 14.
Hydrochloride waste is extracted by hydrochloride waste storage tank and is used as refrigerant and flue gas heat exchange into above-mentioned each third heat exchange mechanisms 14,
Realize the purpose preheated to hydrochloride waste.Using the above method, the circulation of the second level and washing mechanisms at different levels later has been recycled
The part of waste heat of liquid preheats the hydrochloride waste (the room temperature hydrochloride waste wait enter in Venturi preconcentrator 3) of cold conditions,
The heat of circulation fluid is made full use of, the waste of circulation fluid residual heat is reduced, it is energy-saving, and the effect of regeneration of hydrochloric acid recycling can be improved
Rate；The low temperature that hydrochloride waste is utilized simultaneously cools down to the circulation fluid of corresponding each washing mechanism, the circulation fluid spray of low temperature
It is bigger with the heat exchange amount of flue gas when entering in corresponding each washing mechanism, washing effect of the circulation fluid in each washing mechanism can be improved
Fruit improves the dedusting cooling effect of each washing mechanism, and exhaust gas volumn also greatly reduces, and the discharge index that chimney 8 can be made final is much
Better than the requirement of national standard, the defect that 8 exhaust emissions of chimney easily forms " white cigarette " is solved.Based on above-mentioned beneficial effect, can make
The lectotype selection of roaster 1, Venturi preconcentrator 3, each washing facility etc. is smaller, energy consumption is lower, to save equipment construction
Cost and improvement cost reduce construction investment.
Embodiment five
The present embodiments relate to a kind of hydrochloric acid exhausted liquid reclaiming process, can at least solve the subproblem of the prior art.This
The technical solution of the method hydrochloric acid exhausted liquid reclaiming process in the hydrochloric acid exhausted liquid reclaiming process and embodiment three in two in conjunction with the embodiments,
That is: baking flue gas is carried out in subsequent processes, utilizes baking flue gas and the hydrochloride waste wait enter Venturi preconcentrator 3
A portion exchange heat, obtain first preheating hydrochloride waste；More than the part for recycling the circulation fluid of first order washing mechanism 5
The a portion of heat for the hydrochloride waste for entering Venturi preconcentrator 3 preheats, and it is useless to obtain the second preheating hydrochloric acid
Liquid, the circulation fluid after heat exchange spray into the first order washing mechanism 5 and/or absorption tower 4.
Above-mentioned baking flue gas and the specific embodiment of hydrochloride waste heat exchange are identical as the mode in embodiment two, and above-mentioned the
The specific embodiment of circulation fluid and the hydrochloride waste heat exchange of level-one washing mechanism 5 is identical as the mode in embodiment three, herein
It repeats no more.
As shown in Figure 1, this method, which is used, is sequentially connected the second level rinsing maching constituted by Venturi scrubber 5 and scrubbing tower 6
The first heat exchange mechanisms 13 are arranged on the flue between Venturi scrubber 5 and scrubbing tower 6, in Venturi scrubber 5 in structure
Circulation liquid pipeline on the second heat exchange mechanisms 15 are set；Specific step is as follows for this method:
(1) entered in the first heat exchange mechanisms 13 by hydrochloride waste storage tank extraction section hydrochloride waste, the part hydrochloride waste
The first preheating hydrochloride waste is obtained with flue gas heat exchange；Second heat exchange mechanisms are entered by hydrochloride waste storage tank extraction section hydrochloride waste
In 15, the circulation fluid of the part hydrochloride waste and Venturi scrubber 5 exchanges heat to obtain the second preheating hydrochloride waste.
Above-mentioned first preheating hydrochloride waste and the second preheating hydrochloride waste enter in Venturi preconcentrator 3, in venturi
The high temperature mixed flue gas counter current contact being discharged in preconcentrator 3 and by roaster 1, hydrochloride waste absorb HCl and quilt in flue gas
Flue gas, the partial moisture in hydrochloride waste are evaporated, to realize heating concentration.
(2) hydrochloride waste after being concentrated is injected into roasting through Venturi preconcentrator recycle liquid pump 9, roaster charging pump 10
In furnace 1, the heat provided by combustion gas and combustion fan, the FeCl in hydrochloride waste2、FeCl3It is generated as by chemical reaction
Fe2O3Powder and high temperature mixed flue gas, Fe2O3Powder drops down onto the discharge of 1 bottom of roaster, and high temperature mixed flue gas contains HCl, H2O、
O2、CO2、N2And Fe2O3Powder etc., the temperature of high temperature mixed flue gas are 390~410 DEG C.
(3) above-mentioned high temperature mixed flue gas is after the processing of double-cyclone dust collector 2, about 50% Fe in flue gas2O3Powder passes through back
Expects pipe returns to the bottom discharge of roaster 1.Subsequent high-temperature flue gas enter in Venturi preconcentrator 3 cooled down, dedusting, high temperature
The temperature of flue gas is reduced to 95~100 DEG C by 390~410 DEG C.
(4) absorption tower 4 is entered from the high-temperature flue gas that Venturi preconcentrator 3 comes out, sprays into a part at the top of absorption tower 4
The rinse water of rinse water after the pressurization of Venturi scrubber recycle liquid pump 11, flue gas and spray reverse convection in absorption tower 4,
Heat exchange and absorbing reaction are carried out in packing area, and the rinse water that about 99% HCl is sprayed in flue gas absorbs, and forms regenerated acid row
Out, and flue-gas temperature is then reduced to 85~90 DEG C.
(5) enter Venturi scrubber 5 from the flue gas that absorption tower 4 comes out, by extracting hydrochloride waste in hydrochloride waste storage tank
It is passed through in the second heat exchange mechanisms 15 as refrigerant and Venturi scrubber circulation fluid is cooled down, circulation fluid scripture after cooling mound
In washer recycle liquid pump 11 pressurize after spray into the top of Venturi scrubber 5 cooled down to the flue gas entered from bottom, dedusting.
Wherein, in the second heat exchange mechanisms 15, hydrochloride waste temperature is increased to 36~40 DEG C by 25~35 DEG C, circulation fluid temperature by 70~
75 DEG C are reduced to 38~42 DEG C.After 38~42 DEG C of Venturi scrubber circulation fluid spray, Venturi scrubber 5 goes out
Mouth flue-gas temperature is reduced to 70~75 DEG C by 85~90 DEG C；
(6) flue gas enters the first heat exchange mechanisms 13 after coming out from Venturi scrubber 5, by the hydrochloric acid in hydrochloride waste storage tank
Waste liquid is passed through in the first heat exchange mechanisms 13 as refrigerant and cools down to flue gas.Flue gas by the first heat exchange mechanisms 13 top into
Enter, exhaust gas conveying fan and scrubbing tower 6 are discharged by lower part；Hydrochloride waste enters from the lower part of the first heat exchange mechanisms 13, from
Top outflow；The cooling condensed water generated of flue gas is then discharged into (or the rinsing of Venturi scrubber 5 from the bottom of the first heat exchange mechanisms 13
Water pot) in.Through exchanging heat, hydrochloride waste temperature is increased to 36~40 DEG C by 25~35 DEG C, and flue-gas temperature is reduced to by 70~75 DEG C
45~50 DEG C, during this, the moisture in flue gas reduces 50~70%, the Fe that flue gas carries2O3Particle and HCl remnants are also reduced
About 50%, exhaust gas volumn also reduces about 30~40%.
(7) flue gas after cooling enters scrubbing tower 6, further cooling, dedusting, 6 exiting flue gas of scrubbing tower in scrubbing tower 6
Temperature is reduced to 40~45 DEG C, is discharged after the processing of liquid drop separator 7 by chimney 8, without " white cigarette " phenomenon.
Embodiment six
The present embodiments relate to a kind of hydrochloric acid exhausted liquid reclaiming process, can at least solve the subproblem of the prior art.This
The technical solution of the method hydrochloric acid exhausted liquid reclaiming process in the hydrochloric acid exhausted liquid reclaiming process and example IV in two in conjunction with the embodiments,
That is: baking flue gas is carried out in subsequent processes, utilizes baking flue gas and the hydrochloride waste wait enter Venturi preconcentrator 3
A portion exchange heat, obtain first preheating hydrochloride waste；Using multistage washing mechanism, first order washing mechanism 5 it
In each washing mechanism afterwards, until entering less than third heat exchange mechanisms 14 are provided on the wherein circulation liquid pipeline of a washing mechanism
In the hydrochloride waste of Venturi preconcentrator 3, at least partially exchange heat through each third heat exchange mechanisms 14 with corresponding circulation fluid
Three preheating hydrochloride wastes.
Above-mentioned baking flue gas and the specific embodiment of hydrochloride waste heat exchange are identical as the mode in embodiment two, and above-mentioned the
Side in the circulation fluid of second level and washing mechanisms at different levels later and the specific embodiment and example IV of hydrochloride waste heat exchange
Formula is identical, and details are not described herein again.
As shown in Fig. 2, this method, which is used, is sequentially connected the second level rinsing maching constituted by Venturi scrubber 5 and scrubbing tower 6
The first heat exchange mechanisms 13 are arranged on the flue between Venturi scrubber 5 and scrubbing tower 6, in the circulation of scrubbing tower 6 in structure
Third heat exchange mechanisms 14 are set on liquid pipeline；Specific step is as follows for this method:
(1) entered in the first heat exchange mechanisms 13 by hydrochloride waste storage tank extraction section hydrochloride waste, the part hydrochloride waste
The first preheating hydrochloride waste is obtained with flue gas heat exchange；Third heat exchange mechanisms are entered by hydrochloride waste storage tank extraction section hydrochloride waste
In 14, the circulation fluid of the part hydrochloride waste and scrubbing tower 6 exchanges heat to obtain third preheating hydrochloride waste.
Above-mentioned first preheating hydrochloride waste and third preheating hydrochloride waste enter in Venturi preconcentrator 3, in venturi
The high temperature mixed flue gas counter current contact being discharged in preconcentrator 3 and by roaster 1, hydrochloride waste absorb HCl and quilt in flue gas
Flue gas, the partial moisture in hydrochloride waste are evaporated, to realize heating concentration.
(2) hydrochloride waste after being concentrated is injected into roasting through Venturi preconcentrator recycle liquid pump 9, roaster charging pump 10
In furnace 1, the heat provided by combustion gas and combustion fan, the FeCl in hydrochloride waste2、FeCl3It is generated as by chemical reaction
Fe2O3Powder and high temperature mixed flue gas, Fe2O3Powder drops down onto the discharge of 1 bottom of roaster, and high temperature mixed flue gas contains HCl, H2O、
O2、CO2、N2And Fe2O3Powder etc., the temperature of high temperature mixed flue gas are 390~410 DEG C.
(3) above-mentioned high temperature mixed flue gas is after the processing of double-cyclone dust collector 2, about 50% Fe in flue gas2O3Powder passes through back
Expects pipe returns to the bottom discharge of roaster 1.Subsequent high-temperature flue gas enter in Venturi preconcentrator 3 cooled down, dedusting, high temperature
The temperature of flue gas is reduced to 95~100 DEG C by 390~410 DEG C.
(4) absorption tower 4 is entered from the high-temperature flue gas that Venturi preconcentrator 3 comes out, sprays into a part at the top of absorption tower 4
The rinse water of rinse water after the pressurization of Venturi scrubber recycle liquid pump 11, flue gas and spray reverse convection in absorption tower 4,
Heat exchange and absorbing reaction are carried out in packing area, and the rinse water that about 99% HCl is sprayed in flue gas absorbs, and forms regenerated acid row
Out, and flue-gas temperature is then reduced to 85~90 DEG C.
(5) enter Venturi scrubber 5 from the flue gas that absorption tower 4 comes out, add by Venturi scrubber recycle liquid pump 11
Circulation fluid after pressure is sprayed into from the time mouth of Venturi scrubber 5, and flue gas carries out heat with circulation fluid and exchanges, and is further dropped
Temperature, dedusting, flue-gas temperature are reduced to 82~87 DEG C；
(6) flue gas enters the first heat exchange mechanisms 13 after coming out from Venturi scrubber 5, by the hydrochloric acid in hydrochloride waste storage tank
Waste liquid is passed through in the first heat exchange mechanisms 13 as refrigerant and cools down to flue gas.Flue gas by the first heat exchange mechanisms 13 top into
Enter, exhaust gas conveying fan (having illustrated, do not mark) and scrubbing tower 6 are discharged by lower part；Hydrochloride waste is from the first heat exchange mechanisms
13 lower part enters, and flows out from top；The cooling condensed water generated of flue gas is then discharged into Wen Qiu from the bottom of the first heat exchange mechanisms 13
In in washer 5 (or rinsing water pot).Through exchanging heat, hydrochloride waste temperature is increased to 36~40 DEG C by 25~35 DEG C, flue-gas temperature
63~68 DEG C are reduced to by 82~87 DEG C, during this, the moisture in flue gas reduces 50~70%, the Fe that flue gas carries2O3Particle
About 50% is also reduced with HCl remnants, exhaust gas volumn also reduces about 30~40%.
(7) flue gas after cooling enters scrubbing tower 6, is passed through the by extracting hydrochloride waste in hydrochloride waste storage tank as refrigerant
Scrubbing tower circulation fluid is cooled down in three heat exchange mechanisms 14, the washed tower recycle liquid pump 12 of circulation fluid after cooling sprays after pressurizeing
Enter the top of scrubbing tower 6 cooled down to the flue gas entered from bottom, dedusting.Wherein, in third heat exchange mechanisms 14, hydrochloride waste
Temperature is increased to 36~40 DEG C by 25~35 DEG C, and circulation fluid temperature is reduced to 38~42 DEG C by 50~55 DEG C, is passing through 38~42
DEG C scrubbing tower circulation fluid spray after, 6 exit gas temperature of scrubbing tower is reduced to 40~42 DEG C by 63~68 DEG C, through drop point
It is discharged from after the processing of device 7 by chimney 8, without " white cigarette " phenomenon.
Embodiment seven
The present embodiments relate to a kind of hydrochloric acid exhausted liquid reclaiming process, can at least solve the subproblem of the prior art.This
Method in conjunction with the embodiments two, the technical solution of embodiment three and the hydrochloric acid exhausted liquid reclaiming process in example IV, it may be assumed that roasting cigarette
Gas carries out in subsequent processes, utilizes baking flue gas and wherein one of the hydrochloride waste wait enter Venturi preconcentrator 3
Divide and exchange heat, obtains the first preheating hydrochloride waste；Using multistage washing mechanism, the circulation fluid of first order washing mechanism 5 is recycled
Part of waste heat be used to preheat a portion of hydrochloride waste for entering Venturi preconcentrator 3, it is pre- to obtain second
Hot hydrochloride waste, the circulation fluid after heat exchange spray into the first order washing mechanism 5 and/or absorption tower 4；First order washing mechanism 5
In each washing mechanism later, until less than third heat exchange mechanisms 14 are provided on the wherein circulation liquid pipeline of a washing mechanism, into
In the hydrochloride waste for entering Venturi preconcentrator 3, at least partially exchange heat through each third heat exchange mechanisms 14 with corresponding circulation fluid
Third preheats hydrochloride waste.
Above-mentioned baking flue gas and the specific embodiment of hydrochloride waste heat exchange are identical as the mode in embodiment two, and above-mentioned the
The specific embodiment of circulation fluid and the hydrochloride waste heat exchange of level-one washing mechanism 5 is identical as the mode in embodiment three, above-mentioned
In the circulation fluid of the second level and washing mechanisms at different levels later and the specific embodiment and example IV of hydrochloride waste heat exchange
Mode is identical, and details are not described herein again.
As shown in figure 3, this method, which is used, is sequentially connected the second level rinsing maching constituted by Venturi scrubber 5 and scrubbing tower 6
The first heat exchange mechanisms 13 are arranged on the flue between Venturi scrubber 5 and scrubbing tower 6, in Venturi scrubber 5 in structure
Circulation liquid pipeline on the second heat exchange mechanisms 15 are set, on the circulation liquid pipeline of scrubbing tower 6 be arranged third heat exchange mechanisms 14；This
Specific step is as follows for method:
(1) entered in the first heat exchange mechanisms 13 by hydrochloride waste storage tank extraction section hydrochloride waste, the part hydrochloride waste
The first preheating hydrochloride waste is obtained with flue gas heat exchange；Second heat exchange mechanisms are entered by hydrochloride waste storage tank extraction section hydrochloride waste
In 15, the circulation fluid of the part hydrochloride waste and Venturi scrubber 5 exchanges heat to obtain the second preheating hydrochloride waste；By hydrochloride waste
Storage tank extraction section hydrochloride waste enters in third heat exchange mechanisms 14, and the circulation fluid of the part hydrochloride waste and scrubbing tower 6 exchanges heat
Obtain third preheating hydrochloride waste.
It is pre- dense that above-mentioned first preheating hydrochloride waste, the second preheating hydrochloride waste and third preheating hydrochloride waste enter venturi
In contracting device 3, the high temperature mixed flue gas counter current contact being discharged in Venturi preconcentrator 3 and by roaster 1, hydrochloride waste absorbs
HCl in flue gas and by flue gas, the partial moisture in hydrochloride waste is evaporated, to realize heating concentration.
(2) hydrochloride waste after being concentrated is injected into roasting through Venturi preconcentrator recycle liquid pump 9, roaster charging pump 10
In furnace 1, the heat provided by combustion gas and combustion fan, the FeCl in hydrochloride waste2、FeCl3It is generated as by chemical reaction
Fe2O3Powder and high temperature mixed flue gas, Fe2O3Powder drops down onto the discharge of 1 bottom of roaster, and high temperature mixed flue gas contains HCl, H2O、
O2、CO2、N2And Fe2O3Powder etc., the temperature of high temperature mixed flue gas are 390~410 DEG C.
(3) above-mentioned high temperature mixed flue gas is after the processing of double-cyclone dust collector 2, about 50% Fe in flue gas2O3Powder passes through back
Expects pipe returns to the bottom discharge of roaster 1.Subsequent high-temperature flue gas enter in Venturi preconcentrator 3 cooled down, dedusting, high temperature
The temperature of flue gas is reduced to 95~100 DEG C by 390~410 DEG C.
(4) absorption tower 4 is entered from the high-temperature flue gas that Venturi preconcentrator 3 comes out, sprays into a part at the top of absorption tower 4
The rinse water of rinse water after the pressurization of Venturi scrubber recycle liquid pump 11, flue gas and spray reverse convection in absorption tower 4,
Heat exchange and absorbing reaction are carried out in packing area, and the rinse water that about 99% HCl is sprayed in flue gas absorbs, and forms regenerated acid row
Out, and flue-gas temperature is then reduced to 85~90 DEG C.
(5) enter Venturi scrubber 5 from the flue gas that absorption tower 4 comes out, by extracting hydrochloride waste in hydrochloride waste storage tank
It is passed through in the second heat exchange mechanisms 15 as refrigerant and Venturi scrubber circulation fluid is cooled down, circulation fluid scripture after cooling mound
In washer recycle liquid pump 11 pressurize after spray into the top of Venturi scrubber 5 cooled down to the flue gas entered from bottom, dedusting.
Wherein, in the second heat exchange mechanisms 15, hydrochloride waste temperature is increased to 36~40 DEG C by 25~35 DEG C, circulation fluid temperature by 70~
75 DEG C are reduced to 38~42 DEG C.After 38~42 DEG C of Venturi scrubber circulation fluid spray, Venturi scrubber 5 goes out
Mouth flue-gas temperature is reduced to 70~75 DEG C by 85~90 DEG C；
(6) flue gas enters the first heat exchange mechanisms 13 after coming out from Venturi scrubber 5, by the hydrochloric acid in hydrochloride waste storage tank
Waste liquid is passed through in the first heat exchange mechanisms 13 as refrigerant and cools down to flue gas.Flue gas by the first heat exchange mechanisms 13 top into
Enter, exhaust gas conveying fan and scrubbing tower 6 are discharged by lower part；Hydrochloride waste enters from the lower part of the first heat exchange mechanisms 13, from
Top outflow；The cooling condensed water generated of flue gas is then discharged into (or the rinsing of Venturi scrubber 5 from the bottom of the first heat exchange mechanisms 13
Water pot) in.Through exchanging heat, hydrochloride waste temperature is increased to 36~40 DEG C by 25~35 DEG C, and flue-gas temperature is reduced to by 70~75 DEG C
45~50 DEG C, during this, the moisture in flue gas reduces 50~70%, the Fe that flue gas carries2O3Particle and HCl remnants are also reduced
About 50%, exhaust gas volumn also reduces about 30~40%.
(7) flue gas after cooling enters scrubbing tower 6, is passed through the by extracting hydrochloride waste in hydrochloride waste storage tank as refrigerant
Scrubbing tower circulation fluid is cooled down in three heat exchange mechanisms 14, the washed tower recycle liquid pump 12 of circulation fluid after cooling sprays after pressurizeing
Enter the top of scrubbing tower 6 cooled down to the flue gas entered from bottom, dedusting.Wherein, in third heat exchange mechanisms 14, hydrochloride waste
Temperature is increased to 35~39 DEG C by 25~35 DEG C, and circulation fluid temperature is reduced to 38~42 DEG C by 40~45 DEG C, is passing through 38~42
DEG C scrubbing tower circulation fluid spray after, 6 exit gas temperature of scrubbing tower reduce by 40~42 DEG C, through liquid drop separator 7 processing after
It is discharged by chimney 8, without " white cigarette " phenomenon.
Embodiment eight
The present embodiment is related to a kind of hydrochloride waste regenerative system, the hydrochloride waste regeneration that this system provides in example 1
On the basis of system structure, until less than the first heat exchange mechanisms 13 are provided on wherein one section of flue, by hydrochloride waste storage tank
Interior extraction hydrochloride waste enters each first heat exchange mechanisms 13 and is used as refrigerant and flue gas heat exchange, and the refrigerant of each first heat exchange mechanisms 13 goes out
Mouth is connect with the hydrochloride waste inlet of Venturi preconcentrator 3.
It flue between double-cyclone dust collector 2 and Venturi preconcentrator 3, Venturi preconcentrator 3 and can inhale
Receive the flue between tower 4, the flue between absorption tower 4 and first order washing mechanism 5, between adjacent two washing mechanism
Flue, one of in the flue between afterbody washing mechanism and chimney 8 or on multiple flues
Above-mentioned first heat exchange mechanisms 13 are set, it is higher closer to 1 flue-gas temperature of roaster, then it is better to the pre-heat effect of hydrochloride waste.
But it in view of the needs of the 4 reclaiming hydrochloric acid of corrosivity and absorption tower of HCl heat exchanging equipment in flue gas, does not use in text generally
The flue gas to circulate between preconcentrator 3 and absorption tower 4 in mound exchanges heat with hydrochloride waste.Preferably at least in being connected to first
The first heat exchange mechanisms 13 are provided on the flue of grade 5 exhanst gas outlet of washing mechanism, into the hydrochloric acid of Venturi preconcentrator 3
In waste liquid, hydrochloride waste at least partially is preheated with the first of flue gas heat exchange through each first heat exchange mechanisms 13.If washing mechanism has
It is multistage, it is contemplated that above-mentioned first heat exchange mechanisms 13 are respectively provided on the flue for being connected to washing mechanism exhanst gas outlets at different levels,
But increase with series, the temperature of flue gas gradually decreases, and flue gas is also poorer to the pre-heat effect of hydrochloride waste；Also it is contemplated that absorbing
Above-mentioned first heat exchange mechanisms 13 are set on the flue between tower 4 and first order washing mechanism 5.In the present embodiment, using by
Venturi scrubber 5 and scrubbing tower 6 are sequentially connected the second level washing mechanism of composition, between Venturi scrubber 5 and scrubbing tower 6
Flue on above-mentioned first heat exchange mechanisms 13 are set.
Above-mentioned first heat exchange mechanisms 13 using flue gas heat-exchange unit to be preferred.Flue gas produces when exchanging heat in the first heat exchange mechanisms 13
Life includes the cooling mixed liquid of condensed water, the part cooling mixed liquid can be discharged into first order washing mechanism 5 as cleaning solution and/
Or it is discharged into rinsing water pot as the spray liquid in absorption tower 4.
Embodiment nine
The present embodiment is related to a kind of hydrochloride waste regenerative system, the hydrochloride waste regeneration that this system provides in example 1
On the basis of system structure, in being provided with the second heat exchange mechanisms 15 on the circulation liquid pipeline of first order washing mechanism 5, described second
The refrigerant inlet of heat exchange mechanisms 15 is connect with hydrochloride waste storage tank, and refrigerant exit is connect with the Venturi preconcentrator 3；It is described
The circulation fluid tube outlet end of second level washing mechanism is connected to the first order washing mechanism 5 and/or absorption tower 4.Above-mentioned second
Heat exchange mechanisms 15 using water water- to-water heat exchanger to be preferred.
Embodiment ten
The present embodiment is related to a kind of hydrochloride waste regenerative system, the hydrochloride waste regeneration that this system provides in example 1
On the basis of system structure, using multistage washing mechanism, in each washing mechanism after first order washing mechanism 5, until being less than it
In a washing mechanism circulation liquid pipeline on be provided with third heat exchange mechanisms 14；Into the hydrochloride waste of Venturi preconcentrator 3
In, at least partially hydrochloride waste is preheated with the third that corresponding circulation fluid exchanges heat through each third heat exchange mechanisms 14.
In the present embodiment, using Venturi scrubber 5 and the sequentially connected two-stage washing mechanism of scrubbing tower 6, in scrubbing tower 6
Circulation liquid pipeline on be provided with above-mentioned third heat exchange mechanisms 14.
Above-mentioned third heat exchange mechanisms 14 using water water- to-water heat exchanger to be preferred.
Embodiment 11
Such as Fig. 1, the present embodiment is related to a kind of hydrochloride waste regenerative system, this system in conjunction with the embodiments eight in embodiment nine
The structure of provided hydrochloride waste regenerative system, it may be assumed that be provided with the first heat exchange mechanisms on less than wherein one section of flue
13, by hydrochloride waste storage tank extract hydrochloride waste enter each first heat exchange mechanisms 13 be used as refrigerant and flue gas heat exchange, each first
The refrigerant exit of heat exchange mechanisms 13 is connect with the hydrochloride waste inlet of Venturi preconcentrator 3；In first order washing mechanism 5
Circulation liquid pipeline on be provided with the second heat exchange mechanisms 15, the refrigerant inlet and hydrochloride waste storage tank of second heat exchange mechanisms 15
Connection, refrigerant exit are connect with the Venturi preconcentrator 3.
Setting position, specific structure about the first heat exchange mechanisms 13 etc. and the corresponding set-up mode and knot in embodiment eight
Structure is identical, and details are not described herein again.
Embodiment 12
Such as Fig. 2, the present embodiment is related to a kind of hydrochloride waste regenerative system, this system in conjunction with the embodiments eight in embodiment ten
The structure of provided hydrochloride waste regenerative system, it may be assumed that be provided with the first heat exchange mechanisms on less than wherein one section of flue
13, by hydrochloride waste storage tank extract hydrochloride waste enter each first heat exchange mechanisms 13 be used as refrigerant and flue gas heat exchange, each first
The refrigerant exit of heat exchange mechanisms 13 is connect with the hydrochloride waste inlet of Venturi preconcentrator 3；Using multistage washing mechanism,
In each washing mechanism after first order washing mechanism 5, until less than being provided with the on the wherein circulation liquid pipeline of a washing mechanism
The refrigerant inlet of three heat exchange mechanisms 14, each third heat exchange mechanisms 14 is connect with hydrochloride waste storage tank, refrigerant exit with
The Venturi preconcentrator 3 connects.
About the setting position of the first heat exchange mechanisms 13 and third heat exchange mechanisms 14, specific structure etc. in embodiment eight and
Corresponding set-up mode and structure in embodiment ten is identical, and details are not described herein again.
Embodiment 13
Such as Fig. 3, the present embodiment is related to a kind of hydrochloride waste regenerative system, this system in conjunction with the embodiments eight, embodiment nine and
The structure of hydrochloride waste regenerative system provided in embodiment ten, it may be assumed that less than being provided with the on wherein one section of flue
One heat exchange mechanisms 13 are changed as refrigerant with flue gas by extracting hydrochloride waste in hydrochloride waste storage tank into each first heat exchange mechanisms 13
Heat, the refrigerant exit of each first heat exchange mechanisms 13 are connect with the hydrochloride waste inlet of Venturi preconcentrator 3；Using multistage
Washing mechanism, in being provided with the second heat exchange mechanisms 15, second heat exchange mechanisms on the circulation liquid pipeline of first order washing mechanism 5
15 refrigerant inlet is connect with hydrochloride waste storage tank, and refrigerant exit is connect with the Venturi preconcentrator 3；First order rinsing maching
In each washing mechanism after structure 5, until less than third heat exchange mechanisms 14 are provided on the wherein circulation liquid pipeline of a washing mechanism,
The refrigerant inlet of each third heat exchange mechanisms 14 is connect with hydrochloride waste storage tank, and refrigerant exit is pre- dense with the venturi
Contracting device 3 connects.
About the setting position of the first heat exchange mechanisms 13 and third heat exchange mechanisms 14, specific structure etc. in embodiment eight and
Corresponding set-up mode and structure in embodiment ten is identical, and details are not described herein again.
Each hydrochloride waste regenerative system provided in above-described embodiment eight to embodiment 13 is used equally for implementing
Each hydrochloric acid exhausted liquid reclaiming process provided in example two to embodiment seven, can obtain corresponding technical effect, details are not described herein again.
The foregoing is merely illustrative of the preferred embodiments of the present invention, is not intended to limit the invention, all in essence of the invention
Within mind and principle, any modification, equivalent replacement, improvement and so on be should all be included in the protection scope of the present invention.
Claims (4)
1. a kind of hydrochloric acid exhausted liquid reclaiming process, it is characterised in that: hydrochloride waste is in Venturi preconcentrator after heated concentration
It sprays into roaster, the baking flue gas of generation successively passes through at Venturi preconcentrator, absorption tower and second level washing mechanism
Reason, second level washing mechanism includes sequentially connected Venturi scrubber and scrubbing tower；
Wherein, the baking flue gas temperature that roaster generates is 390~410 DEG C, is dropped in Venturi preconcentrator to flue gas
Warm dedusting, flue-gas temperature are reduced to 95~100 DEG C by 390~410 DEG C, further cooled flue gas and recovered flue gas in absorption tower
In HCl, flue-gas temperature is reduced to 85~90 DEG C；
Venturi scrubber exit gas temperature is reduced to 70~75 DEG C by 85~90 DEG C, recycles the circulation fluid of Venturi scrubber
Part of waste heat be used to preheat a portion of hydrochloride waste for entering Venturi preconcentrator, hydrochloride waste temperature
36~40 DEG C are increased to by 25~35 DEG C, the circulation fluid temperature of heat exchange is reduced to 38~42 DEG C by 70~75 DEG C, following after heat exchange
Ring liquid sprays into the Venturi scrubber and/or absorption tower；
Into in the hydrochloride waste of Venturi preconcentrator, there are also parts by being preheated with baking flue gas heat exchange, benefit
It is exchanged heat with the hydrochloride waste of the flue gas and corresponding part that circulate between Venturi scrubber and scrubbing tower, through exchanging heat, salt
Acid waste liquid temperature is increased to 36~40 DEG C by 25~35 DEG C, and flue-gas temperature is reduced to 45~50 DEG C by 70~75 DEG C；
Flue gas after cooling enters scrubbing tower, and further cooling, dedusting, scrubbing tower exit gas temperature are reduced in scrubbing tower
40~45 DEG C.
2. hydrochloric acid exhausted liquid reclaiming process according to claim 1, it is characterised in that: flue gas with hydrochloride waste to be preheated
Generation includes the cooling mixed liquid of condensed water when heat exchange, which is discharged into Venturi scrubber as cleaning solution
And/or it is discharged into rinsing water pot as the spray liquid in absorption tower.
3. a kind of hydrochloride waste regenerative system, including pass through the sequentially connected roaster of flue, Venturi preconcentrator, suction
Receive tower and at least one level washing mechanism, it is characterised in that: washing mechanism is second level, and second level washing mechanism includes sequentially connected text
Washer and scrubbing tower in mound；
In being provided with the second heat exchange mechanisms, the refrigerant inlet of second heat exchange mechanisms on the circulation liquid pipeline of Venturi scrubber
It is connect with hydrochloride waste storage tank, refrigerant exit is connect with the Venturi preconcentrator；The circulation fluid of the Venturi scrubber
Tube outlet end is connected to the Venturi scrubber and/or absorption tower；
The first heat exchange mechanisms, first heat exchange mechanisms are provided on flue between Venturi scrubber and scrubbing tower
Refrigerant inlet connect with hydrochloride waste storage tank, refrigerant exit is connect with the Venturi preconcentrator；
Wherein, the baking flue gas temperature that roaster generates is 390~410 DEG C, is dropped in Venturi preconcentrator to flue gas
Warm dedusting, flue-gas temperature are reduced to 95~100 DEG C by 390~410 DEG C, further cooled flue gas and recovered flue gas in absorption tower
In HCl, flue-gas temperature is reduced to 85~90 DEG C；
Venturi scrubber exit gas temperature is reduced to 70~75 DEG C by 85~90 DEG C, exchanges heat through second heat exchange mechanisms,
Hydrochloride waste temperature is increased to 36~40 DEG C by 25~35 DEG C, and circulation fluid temperature is reduced to 38~42 DEG C by 70~75 DEG C；
It exchanges heat through first heat exchange mechanisms, hydrochloride waste temperature is increased to 36~40 DEG C by 25~35 DEG C, and flue-gas temperature is by 70
~75 DEG C are reduced to 45~50 DEG C；
Flue gas after cooling enters scrubbing tower, and further cooling, dedusting, scrubbing tower exit gas temperature are reduced in scrubbing tower
40~45 DEG C.
4. hydrochloride waste regenerative system according to claim 3, it is characterised in that: first heat exchange mechanisms also have cold
But mixture export, the cooling mixed liquid outlet are connect with the Venturi scrubber and/or rinsing water pot.
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|---|---|---|---|---|
| CN106422680B (en) * | 2016-11-22 | 2022-09-09 | 杭州东日节能技术有限公司 | Smelting flue gas purification treatment device and method with byproduct sulfuric acid of more than 40% |
| CN107010598B (en) * | 2017-04-24 | 2023-08-11 | 鞍山创鑫环保科技股份有限公司 | High-concentration acid washing waste liquid regeneration process and system |
| CN107540038A (en) * | 2017-08-25 | 2018-01-05 | 金川集团股份有限公司 | A kind of device and method that tower exiting flue gas concentrated acidic waste water is inhaled using two |
| CN107555511A (en) * | 2017-08-25 | 2018-01-09 | 金川集团股份有限公司 | A kind of device of acid waste water evaporation emission reduction |
| CN109569205A (en) * | 2018-12-26 | 2019-04-05 | 中冶南方工程技术有限公司 | Acid regeneration flue gas processing method and system |
| CN111809191A (en) * | 2020-06-28 | 2020-10-23 | 中冶南方工程技术有限公司 | Method and system for regenerating hydrochloric acid waste liquid based on fluidized bed method |
| CN113042481A (en) * | 2021-03-03 | 2021-06-29 | 广西柳州钢铁集团有限公司 | Method for on-line cleaning regular packing of absorption tower by hydrochloric acid regeneration system |
| CN114574870B (en) * | 2022-02-23 | 2022-11-29 | 宁波渤川废液处置有限公司 | Waste acid treatment automatic control system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4197139A (en) * | 1978-08-23 | 1980-04-08 | Hjersted Norman B | Process for the reclamation of acid from spent pickle liquor |
| CN1851320A (en) * | 2006-04-28 | 2006-10-25 | 中冶南方工程技术有限公司 | Hydrochloride waste regenerating process for spray roasting |
| CN104344741A (en) * | 2014-10-28 | 2015-02-11 | 中冶南方工程技术有限公司 | System for performing hydrochloric acid waste fluid spray roasting through industrial waste heat and control method |
| CN204460148U (en) * | 2014-12-10 | 2015-07-08 | 中江能源回收(上海)有限公司 | A kind of residual neat recovering system of Waste Sulfuric Acid Pintsch process regeneration |
| CN105240826A (en) * | 2015-11-16 | 2016-01-13 | 江苏昌明环保科技有限公司 | Recovery system and method for low-temperature flue gas waste heat |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59169902A (en) * | 1983-03-14 | 1984-09-26 | Tadayoshi Karasawa | Improvement in procedures for waste acid purification |
-
2016
- 2016-04-06 CN CN201610208932.4A patent/CN105887108B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4197139A (en) * | 1978-08-23 | 1980-04-08 | Hjersted Norman B | Process for the reclamation of acid from spent pickle liquor |
| CN1851320A (en) * | 2006-04-28 | 2006-10-25 | 中冶南方工程技术有限公司 | Hydrochloride waste regenerating process for spray roasting |
| CN104344741A (en) * | 2014-10-28 | 2015-02-11 | 中冶南方工程技术有限公司 | System for performing hydrochloric acid waste fluid spray roasting through industrial waste heat and control method |
| CN204460148U (en) * | 2014-12-10 | 2015-07-08 | 中江能源回收(上海)有限公司 | A kind of residual neat recovering system of Waste Sulfuric Acid Pintsch process regeneration |
| CN105240826A (en) * | 2015-11-16 | 2016-01-13 | 江苏昌明环保科技有限公司 | Recovery system and method for low-temperature flue gas waste heat |
Non-Patent Citations (1)
| Title |
|---|
| 盐酸再生改进工艺运行分析;高俊峰;《冶金动力》;20140115(第1期);第49-52页 * |
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