CN106006806A - Hot air and tubular heater combined waste acid concentration treatment method and device - Google Patents
Hot air and tubular heater combined waste acid concentration treatment method and device Download PDFInfo
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- CN106006806A CN106006806A CN201610584094.0A CN201610584094A CN106006806A CN 106006806 A CN106006806 A CN 106006806A CN 201610584094 A CN201610584094 A CN 201610584094A CN 106006806 A CN106006806 A CN 106006806A
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- waste acid
- hot blast
- air inlet
- vertical pipe
- inlet vertical
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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
- C02F1/048—Purification of waste water by evaporation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/06—Evaporators with vertical tubes
- B01D1/12—Evaporators with vertical tubes and forced circulation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D1/00—Evaporating
- B01D1/14—Evaporating with heated gases or vapours or liquids in contact with the liquid
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/88—Concentration of sulfuric acid
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- 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
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
- C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/02—Temperature
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/08—Corrosion inhibition
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
Abstract
The invention discloses a hot air and tubular heater combined waste acid concentration treatment method and a device. The method includes steps: (1) adding to-be-concentrated waste acid solution into a waste acid container; (2) delivering hot air into a vertical air inlet pipeline of the waste acid container; (3) delivering the waste acid solution from the waste acid container to a tubular heater through a circulating pump to realize heating, delivering heated waste acid solution into the vertical air inlet pipeline of the waste acid container to realize countercurrent contact with the hot air, and enabling the waste acid solution subjected to countercurrent contact to flow into the bottom of the waste acid container; (4) repeating the step (2) and the step (3) to cyclically evaporate and concentrate the waste acid solution. The hot air and tubular heater combined waste acid concentration treatment method is low in required hot air temperature and circulating liquid temperature, equipment corrosion caused by acid solution can be reduced, and high practicality, less proneness to blockage, wide application range and high concentration efficiency are realized.
Description
Technical field
The invention belongs to liquid waste disposal technique field, particularly relate to a kind of hot blast and waste acid concentration that tube still heater combines processes
Method and the device used thereof.
Background technology
Sulphuric acid is extensively applied at chemical industry, steel industry, but in most production process, the utilization rate of sulphuric acid is the lowest, in a large number
Sulphuric acid emit in company with acid-bearing wastewater, if the most treated direct discharge of these waste water, will make water body or soil acidification, pollution
Also the waste of resource is will result in while environment.
For making spent acid to recycle, main method is to separate the impurity in spent acid, and to spent acid enrichment.Compare at present
Common method for concentration has hot blast concentration method and evaporation concentration method.
Hot blast concentration method is to utilize vapor heat exchanger that cool exterior air is heated to more than 180 DEG C, utilizes the hot blast after heating and follows
Ring acid pickle reacts, and hot blast takes away moisture, reaches the effect concentrated.The method requires that hot blast temperature is more than 180 DEG C, therefore heat exchange
Shi Yaoqiu provides high steam or plant area to possess the high-temperature flue gas that can directly utilize, and in process of production, a lot of plant areas are often only
Being provided that low-pressure steam, and do not have ready-made high-temperature flue gas to be available for utilizing, after so causing heat exchange, hot blast temperature does not reaches life
Producing requirement, system will be unable to properly functioning.
Evaporation concentration method typically directly heats evaporation by tubular heat exchanger or evaporating kettle to spent acid, makes waste acid concentration.But during evaporation
Circulation fluid temperature can be caused too high, will shorten the service life of equipment, simultaneously as spent acid complicated component, the equipment that there is also blocks up
The problems such as plug.
Past has the method that Patents technology relates to waste acid concentration, but the most only considers single hot blast concentration method or evaporation
Concentration method, or the series connection of two methods successively uses, and there is certain limitation in former capital.
Patent CN200510019017 discloses the industrial method that during a kind of sulfuric acid method titanium pigment produces, waste acid concentration recycles,
The method includes that spent acid flue gas concentrates and spent acid steam concentrates two steps, and it is by the room temperature spent acid of about 20% that spent acid flue gas concentrates
High temperature rotary kiln flue gas circulating contact in spray column with 300 DEG C～400 DEG C, is concentrated to give the spent acid of 28%～about 30%；Spent acid steams
Vapour concentrate be by flue gas concentrate after obtain 28%～about 30% spent acid again in steam heater and concentration kettle closed cycle dense
Contracting, the spent acid obtaining about 55% enters ripening still, after filter filtration taken over by ripening still, acid solution reuse, filtering residue neutralisation treatment again.
In the method, spent acid flue gas concentrates and the concentration of spent acid steam is that concatenation between successive is carried out, therefore must provide for 300 DEG C when the first step concentrates
～400 DEG C of high-temperature flue gas just can be concentrated to give the spent acid of 28%～about 30%, and during actual production, the high-temperature flue gas of a lot of smelteries
The most it is sent to waste heat boiler recycling, it is impossible to supply waste acid concentration system uses.In the case of there is no hot blast, whole system
System will be unable to properly functioning.Therefore this patented technology has certain limitation.
Patent CN01821138.0 discloses a kind of method of concentrating waste acid, and this invention relates to a kind of by washing smelting furnace or roaster gas
The method for concentration of the spent acid produced.The steam produced first through dry separation, with after wash through wet separation, and the gas after washing
For the preparation of end-product, by utilizing the steam from 250 DEG C～400 DEG C of dry separation to carry out counter current contacting with dilute spent acid, from
And make waste acid concentration.This patent is to use single hot blast concentration method concentrating waste acid equally, and the scope being therefore suitable for is narrower, if factory
District cannot provide 250 DEG C～the hot blast of 400 DEG C, and system will be unable to run.Additionally this patent uses the counter current contacting method of routine,
I.e. in concentration tower, flue gas from bottom to top with the spent acid counter current contacting sprayed from top to bottom, occur heat exchange.Because of tower body sectional area
Relatively big, the effect that heat exchange concentrates is poor.
Summary of the invention
The technical problem to be solved is, overcomes the deficiency and defect mentioned in background above technology, it is provided that a kind of required
Hot blast temperature and circulation fluid temperature is relatively low, can reduce acid solution to the burn into of equipment be not susceptible to blocking, practical, be suitable for model
Enclose hot blast wide, that thickening efficiency is high and waste acid concentration processing method that tube still heater combines and providing used by the method
Device.
For solving above-mentioned technical problem, the technical scheme that the present invention proposes is:
The waste acid concentration processing method that a kind of hot blast and tube still heater combine, comprises the following steps:
(1) in spent acid container, add the waste acid liquor intending concentrating；
(2) hot blast is delivered in the air inlet vertical pipe of spent acid container；
(3) heat in the waste acid liquor in spent acid container being delivered to tube still heater by circulating pump, by molten for the spent acid after heating
Liquid carries out counter current contacting with hot blast in delivering to the air inlet vertical pipe of spent acid container, and the waste acid liquor after counter current contacting flows into spent acid
Container bottom；
(4) repeat the above steps (2) and (3), concentrate waste acid liquor circulating and evaporating.
Hot blast and waste acid liquor is used to carry out the waste acid concentration method of counter current contacting in the air inlet vertical pipe of waste acid column, compared to
The conventional direct method carrying out counter current contacting in waste acid column body, because of the cross section of the sectional area ratio spent acid tower body of air inlet vertical pipe
Long-pending much smaller, heat exchange effect is more preferable, and thickening efficiency is higher；It addition, waste acid liquor is first added in tube still heater by the present invention
Heat, then be passed through in air inlet vertical pipe and carry out counter current contacting with hot blast, required hot blast temperature is lower, and its temperature is more than 100 DEG C i.e.
Can, and in traditional single hot blast concentration method hot blast temperature must more than 180 DEG C, during heat exchange require provide high steam or
Plant area possesses the high-temperature flue gas that can directly utilize, and in process of production, a lot of plant areas often can only provide low-pressure steam, and
Ready-made high-temperature flue gas is not had to be available for utilizing.Additionally, temperature too high service life that also can shorten equipment, simultaneously as spent acid becomes
Divide complexity, there is also the problems such as equipment blocking.The method of the present invention is lower to technological requirement, less to equipment corrosion, is difficult to
Generation equipment blocks, and the scope of application is wider.
The waste acid concentration processing method that above-mentioned hot blast and tube still heater combine, it is preferred that in described step (4), spent acid
Solution circulating and evaporating is delivered in filter after concentrating filter, and obtains filtrate I and filtering residue I, and described filtrate I is back to spent acid appearance
Device.Carry out the spent acid after circulating and evaporating concentrates filtering and filtrate returning spent acid container, the solid in concentrated solution can be reduced
Content, it is to avoid equipment blocking occurs.
The waste acid concentration processing method that above-mentioned hot blast and tube still heater combine, it is preferred that described filtering residue I is delivered to pressure
Filter filter pressing, obtains filtrate II and filtering residue II, and described filtrate II is back to spent acid container, and filtering residue II recycles.To pass through
Filtering residue I after filter carries out filter pressing in pressure filter, can reduce the liquid content of filtering residue I further.
The waste acid concentration processing method that above-mentioned hot blast and tube still heater combine, it is preferred that in described step (2), by heat
Wind specifically refers in being delivered to the air inlet vertical pipe of spent acid container: hot blast is delivered to air inlet vertical pipe upper of spent acid container
Portion, hot blast flows in air inlet vertical pipe from top to bottom；In described step (3), by giving up after heating in tube still heater
Acid solution carries out counter current contacting with hot blast in delivering to the air inlet vertical pipe of spent acid container and specifically refers to: will add in tube still heater
Waste acid liquor after heat delivers to the bottom of the air inlet vertical pipe of spent acid container, along air inlet vertical pipe upward spraying, hangs down with air inlet
The hot blast flowed from top to bottom in straight pipeline carries out counter current contacting.Use hot blast from top to bottom, the adverse current of waste acid liquor upward spraying
The way of contact, can be effectively improved thickening efficiency, shortens concentration time.
The waste acid concentration processing method that above-mentioned hot blast and tube still heater combine, it is preferred that in described step (2), hot blast
Temperature be 100 DEG C～180 DEG C.The hot blast and the tube still heater that use the present invention combine, at the air inlet vertical tube of spent acid container
The processing method concentrated is carried out in road, compared to traditional single hot blast concentration method, relatively low to the temperature requirement of hot blast, 100 DEG C
～180 DEG C；In described step (3), the temperature of the waste acid liquor after heating in tube still heater is 80 DEG C～100 DEG C；
In described step (4), after circulating and evaporating concentration, the concentration of waste acid liquor is 50%～64%.
The waste acid concentration processing method that above-mentioned hot blast and tube still heater combine, it is preferred that above-mentioned hot blast and tubulation heating
The waste acid concentration processing method that device combines, it is preferred that in described step (1), the concentration of the waste acid liquor intending concentration is
10%～20%, the inbound traffics that add of the waste acid liquor intending concentration are 20m3/h。
As a total inventive concept, another aspect of the present invention provides the device used by a kind of above-mentioned waste acid concentration processing method,
Including waste acid column, the top of described waste acid column is provided with air inlet vertical pipe, and the upper end of described air inlet vertical pipe connects hot blast air inlet
Pipe, the bottom of air inlet vertical pipe is provided with one and carries out the spent acid in waste acid column preheating tailing edge air inlet vertical pipe upward spraying
Warm-up cycle device.
Above-mentioned device, it is preferred that described warm-up cycle device includes that tube still heater, one end of described tube still heater pass through
Pipeline is connected with the bottom of waste acid column, and the other end is connected with the bottom of air inlet vertical pipe, and tube still heater is connected with waste acid column
Pipeline is provided with a circulating pump.
Above-mentioned device, it is preferred that the bottom of described waste acid column connects a filter, described filter and waste acid column by pipeline
The pipeline connected is provided with one first delivery pump, and the top of filter is connected with waste acid column by a filtrate recovery tube.
Above-mentioned device, it is preferred that described filter and a pressure filter are connected by pipeline, and described pressure filter is connected with filter
Pipeline be provided with one second delivery pump, be provided with a pressing filtering liquid recovery tube between pressure filter and waste acid column.
Compared with prior art, it is an advantage of the current invention that:
(1) spent acid after heating in the present invention is not directly to contact in waste acid column with hot blast, but in the air inlet of waste acid column
Carrying out counter current contacting in vertical pipe, because the sectional area of the sectional area ratio waste acid column of air inlet vertical pipe is little, contact effect is more preferable,
Heat exchanger effectiveness is higher.
(2) present invention is combined by hot blast and tube still heater and uses hot blast and waste acid liquor at the air inlet vertical tube of waste acid column
The waste acid concentration processing method of counter current contacting is carried out so that heat in the more traditional single hot blast concentration method of temperature of required hot blast in road
The temperature of wind is low, and its temperature is more than 100 DEG C, thus only needs when heat exchange to provide low-pressure steam, requires process equipment relatively
Low so that the waste acid concentration method practicality of the present invention is higher, and range of application is wider.
(3) present invention is combined by hot blast and tube still heater and uses hot blast and waste acid liquor at the air inlet vertical tube of waste acid column
Carrying out the waste acid concentration processing method of counter current contacting in road, the waste acid liquor temperature after tube still heater heating is also than traditional single steaming
The waste acid liquor temperature sending out concentration method is low, can reduce the acid solution corrosion to equipment, extension device service life.
(4) present invention uses hot blast from top to bottom, and the counter current contacting mode of waste acid liquor upward spraying carries out concentrating and can be effectively improved
Acid solution thickening efficiency, shortens the concentration time.
(5) present invention uses the method that circulation concentrates, and the waste acid liquor after will concentrate in good time carries out filtering and filter pressing processes, and removes
Removing solid matter therein, when can avoid using tradition evaporation concentration method, the situation of equipment blocking occurs.
Accompanying drawing explanation
In order to be illustrated more clearly that the embodiment of the present invention or technical scheme of the prior art, below will be to embodiment or prior art
In description, the required accompanying drawing used is briefly described, it should be apparent that, the accompanying drawing in describing below is some realities of the present invention
Execute example, for those of ordinary skill in the art, on the premise of not paying creative work, it is also possible to according to these accompanying drawings
Obtain other accompanying drawing.
The process chart of the waste acid concentration processing method that Fig. 1 is hot blast of the present invention and tube still heater combines.
The structural representation sketch of the waste acid concentration processing method equipment therefor that Fig. 2 is hot blast of the present invention and tube still heater combines.
Marginal data:
1, waste acid column；2, air inlet vertical pipe；3, hot blast air inlet pipe；4, tube still heater；5, circulating pump；6, emptying
Pipe；7, filter；8, the first delivery pump；9, pressure filter；10, the second delivery pump.
Detailed description of the invention
For the ease of understanding the present invention, below in conjunction with Figure of description and preferred embodiment, the present invention is made more comprehensively, careful
Ground describes, but protection scope of the present invention is not limited to embodiment in detail below.
It should be strongly noted that when a certain element is described as on " be connected to or be communicated in " another element, it can be
It is directly connected to or connects on another element, it is also possible to being to be indirectly connected with by other intermediate connectors or connect on another element.
Unless otherwise defined, the implication that all technical term used hereinafter is generally understood that with those skilled in the art is identical.
Technical term used herein is intended merely to describe the purpose of specific embodiment, is not intended to limit the protection model of the present invention
Enclose.
Unless otherwise specified, the various raw materials used in the present invention, reagent, instrument and equipment etc. all can be purchased by market
Can buy or can be prepared by existing method.
Embodiment 1
The embodiment of the waste acid concentration processing method that the hot blast of a kind of present invention and tube still heater combine, its process chart is such as
Shown in Fig. 1, comprise the following steps: adding the waste acid liquor intending concentrating that acid strength is 10% in waste acid column, flow is
20m3/h；It is passed through, toward the air inlet vertical pipe top of waste acid column, the hot blast that temperature is 100 DEG C by gas pipeline；ON cycle pump,
Waste acid liquor in waste acid column is delivered to tube still heater, makes waste acid liquor temperature be increased to 80 DEG C through tube still heater heating；
Waste acid liquor after heating enters the air inlet vertical pipe bottom in waste acid column, sprays from bottom to top along air inlet vertical pipe, with edge
The top-down hot blast of air inlet vertical pipe carries out counter current contacting, is concentrated by the waste acid liquor of ejection；The most repeatedly, spent acid
Moisture in solution is gradually pulled away, and the concentration of waste acid liquor is gradually increased；When the concentration of waste acid liquor reaches 50%, open
Delivery pump I, delivers to filter by waste acid liquor high for concentrated rear solid content, obtains filtrate I and filtering residue I after filtering, by filtrate
I is back to waste acid column, and filtering residue I delivery pump II delivers to pressure filter；Filtering residue I obtains filtrate II and filtering residue II, filter after filter pressing processes
Liquid II returns again to waste acid column, and filtering residue II recycles；Waste acid liquor after concentration is expelled to subsequent step, its
The flow discharging waste acid liquor is 4m3/h。
The device used by waste acid concentration processing method that a kind of the hot blast implemented and tube still heater combine, its structural representation letter
Figure is as in figure 2 it is shown, this device includes waste acid column 1, and the top of this waste acid column 1 is provided with air inlet vertical pipe 2, this air inlet vertical tube
The upper end in road 2 connects a hot blast air inlet pipe 3, and the bottom of air inlet vertical pipe 2 is provided with a warm-up cycle device, waste acid column 1
Top be provided with an evacuated tube 6.This warm-up cycle device includes a tube still heater 4, and pipeline is passed through in one end of tube still heater 4
Being connected with the bottom of waste acid column 1, the other end is connected with the bottom of air inlet vertical pipe 2, and tube still heater 4 is with waste acid column 1 even
The pipeline connect is provided with circulating pump 5.Circulating pump 5 preheats in the spent acid of waste acid column 1 bottom is delivered to tube still heater 4,
Spent acid after preheated from the bottom upward spraying of air inlet vertical pipe 2 with flow from top to bottom from air inlet vertical pipe 2 upper end
Hot blast carries out counter current contacting and is concentrated by the spent acid after preheating, concentrated after spent acid flow into the bottom of waste acid column 1 again, through inverse
The top evacuated tube 6 from waste acid column 1 after stream contact is discharged.So repeatedly circulate, by the waste acid concentration in waste acid column 1 to pre-
Determine concentration.This waste acid concentration processing means is by arranging air inlet vertical pipe 2, by spent acid at air inlet vertical tube on waste acid column 1
Counter current contacting is carried out with hot blast in road 2, owing to the cross section of air inlet vertical pipe 2 is more much smaller than the cross section of waste acid column 1, this
The waste acid concentration processing means of invention than traditional Waste acid treatment device heat exchange effect being not provided with air inlet vertical pipe 2 more preferably,
Thickening efficiency is higher.It is additionally provided with warm-up cycle device, first to spent acid before carrying out counter current contacting in this waste acid concentration processing means
Preheating, it is possible to decrease the temperature of hot blast used, reduce the requirement to technique, reduce equipment corrosion, the scope of application is wider.Pass
The hot blast concentration device hot blast temperature of system need to be more than 180 DEG C, and hot blast used in the waste acid concentration processing means of the present invention
Temperature only generally need to may select in the range of 100 DEG C～180 DEG C more than 100 DEG C.This waste acid concentration processing means also includes
One filter 7 being connected with the bottom of waste acid column 1, it is defeated that the official road that this filter 7 is connected with waste acid column 1 is provided with one first
Sending pump 8, the top of filter 7 is connected with waste acid column 1 by a filtrate recovery tube.It is connected with waste acid column 1 by setting
Filter 7, filters the solid matter in the spent acid after circulation concentrates, then filtrate is back in waste acid column 1,
Can effectively reduce the solid content in spent acid, it is to avoid the situation that equipment blocks occurs.Filter 7 is by pipeline and pressure filter 9 phase
Even, the pipeline that pressure filter 9 is connected with filter 7 is provided with one second delivery pump 10, is provided with between pressure filter 9 and waste acid column 1
One pressing filtering liquid recovery tube.By arranging pressure filter 9, the filtering residue obtained after filter 7 filters is carried out filter pressing, reduce filtering residue
Liquid content, waste acid recovery.
Embodiment 2
The embodiment of the waste acid concentration processing method that the hot blast of a kind of present invention and tube still heater combine, its process chart is such as
Shown in Fig. 1, comprise the following steps: adding the waste acid liquor intending concentrating that acid strength is 15% in waste acid column, flow is
20m3/h；It is passed through, toward the air inlet vertical pipe top of waste acid column, the hot blast that temperature is 100 DEG C by gas pipeline；ON cycle pump,
Waste acid liquor in waste acid column is delivered to tube still heater, makes waste acid liquor temperature be increased to 80 DEG C through tube still heater heating；
Waste acid liquor after heating enters the air inlet vertical pipe bottom in waste acid column, sprays from bottom to top along air inlet vertical pipe, with edge
The top-down hot blast of air inlet vertical pipe carries out counter current contacting, is concentrated by the waste acid liquor of ejection；The most repeatedly, spent acid
Moisture in solution is gradually pulled away, and the concentration of waste acid liquor is gradually increased；When the concentration of waste acid liquor reaches 55%, open
Delivery pump I, delivers to filter by waste acid liquor high for concentrated rear solid content, obtains filtrate I and filtering residue I after filtering, by filtrate
I is back to waste acid column, and filtering residue I delivery pump II delivers to pressure filter；Filtering residue I obtains filtrate II and filtering residue II, filter after filter pressing processes
Liquid II returns again to waste acid column, and filtering residue II recycles；Waste acid liquor after concentration is expelled to subsequent step, its
The flow discharging waste acid liquor is 5.45m3/h.Device used by the processing method of the present embodiment is identical with the device in embodiment 1.
Embodiment 3
The embodiment of the waste acid concentration processing method that the hot blast of a kind of present invention and tube still heater combine, its process chart is such as
Shown in Fig. 1, comprise the following steps: adding the waste acid liquor intending concentrating that acid strength is 20% in waste acid column, flow is
20m3/h；It is passed through, toward the air inlet vertical pipe top of waste acid column, the hot blast that temperature is 100 DEG C by gas pipeline；ON cycle pump,
Waste acid liquor in waste acid column is delivered to tube still heater, makes waste acid liquor temperature be increased to 80 DEG C through tube still heater heating；
Waste acid liquor after heating enters the air inlet vertical pipe bottom in waste acid column, sprays from bottom to top along air inlet vertical pipe, with edge
Air inlet vertical pipe top-down hot blast counter current contacting, concentrates the waste acid liquor of ejection；The most repeatedly, waste acid liquor
In moisture be gradually pulled away, the concentration of waste acid liquor is gradually increased；When the concentration of waste acid liquor reaches 60%, open conveying
Pump I, delivers to filter by waste acid liquor high for concentrated rear solid content, obtains filtrate I and filtering residue I after filtering, is returned by filtrate I
Being back to waste acid column, filtering residue I delivery pump II delivers to pressure filter；Filtering residue I obtains filtrate II and filtering residue II, filtrate after filter pressing processes
II returns again to waste acid column, and filtering residue II recycles；Waste acid liquor after concentration is expelled to subsequent step, its row
The flow going out waste acid liquor is 6.67m3/h.Device used by the processing method of the present embodiment is identical with the device in embodiment 1.
Embodiment 4
The embodiment of the waste acid concentration processing method that the hot blast of a kind of present invention and tube still heater combine, its process chart is such as
Shown in Fig. 1, comprise the following steps: adding the waste acid liquor intending concentrating that acid strength is 12% in waste acid column, flow is
20m3/h；It is passed through, toward the air inlet vertical pipe top of waste acid column, the hot blast that temperature is 120 DEG C by gas pipeline；ON cycle pump,
Waste acid liquor in waste acid column is delivered to tube still heater, makes waste acid liquor temperature be increased to 85 DEG C through tube still heater heating；
Waste acid liquor after heating enters the air inlet vertical pipe bottom in waste acid column, sprays from bottom to top along air inlet vertical pipe, with edge
Air inlet vertical pipe top-down hot blast counter current contacting, concentrates the waste acid liquor of ejection；The most repeatedly, waste acid liquor
In moisture be gradually pulled away, the concentration of waste acid liquor is gradually increased；When the concentration of waste acid liquor reaches 64%, open conveying
Pump I, delivers to filter by waste acid liquor high for concentrated rear solid content, obtains filtrate I and filtering residue I after filtering, is returned by filtrate I
Being back to waste acid column, filtering residue I delivery pump II delivers to pressure filter；Filtering residue I obtains filtrate II and filtering residue II, filtrate after filter pressing processes
II returns again to waste acid column, and filtering residue II recycles；Waste acid liquor after concentration is expelled to subsequent step, its row
The flow going out waste acid liquor is 4.75m3/h.Device used by the processing method of the present embodiment is identical with the device in embodiment 1.
Embodiment 5
The embodiment of the waste acid concentration processing method that the hot blast of a kind of present invention and tube still heater combine, its process chart is such as
Shown in Fig. 1, comprise the following steps: adding the waste acid liquor intending concentrating that acid strength is 18% in waste acid column, flow is
20m3/h；It is passed through, toward the air inlet vertical pipe top of waste acid column, the hot blast that temperature is 140 DEG C by gas pipeline；ON cycle pump,
Waste acid liquor in waste acid column is delivered to tube still heater, makes waste acid liquor temperature be increased to 90 DEG C through tube still heater heating；
Waste acid liquor after heating enters the air inlet vertical pipe bottom in waste acid column, sprays from bottom to top along air inlet vertical pipe, with edge
Air inlet vertical pipe top-down hot blast counter current contacting, concentrates the waste acid liquor of ejection；The most repeatedly, waste acid liquor
In moisture be gradually pulled away, the concentration of waste acid liquor is gradually increased；When the concentration of waste acid liquor reaches 58%, open conveying
Pump I, delivers to filter by waste acid liquor high for concentrated rear solid content, obtains filtrate I and filtering residue I after filtering, is returned by filtrate I
Being back to waste acid column, filtering residue I delivery pump II delivers to pressure filter；Filtering residue I obtains filtrate II and filtering residue II, filtrate after filter pressing processes
II returns again to waste acid column, and filtering residue II recycles；Waste acid liquor after concentration is expelled to subsequent step, its row
The flow going out waste acid liquor is 6.21m3/h.Device used by the processing method of the present embodiment is identical with the device in embodiment 1.
Embodiment 6
The embodiment of the waste acid concentration processing method that the hot blast of a kind of present invention and tube still heater combine, its process chart is such as
Shown in Fig. 1, comprise the following steps: adding the waste acid liquor intending concentrating that acid strength is 10% in waste acid column, flow is
20m3/h；It is passed through, toward the air inlet vertical pipe top of waste acid column, the hot blast that temperature is 180 DEG C by gas pipeline；ON cycle pump,
Waste acid liquor in waste acid column is delivered to tube still heater, makes waste acid liquor temperature be increased to 95 DEG C through tube still heater heating；
Waste acid liquor after heating enters the air inlet vertical pipe bottom in waste acid column, sprays from bottom to top along air inlet vertical pipe, with edge
Air inlet vertical pipe top-down hot blast counter current contacting, concentrates the waste acid liquor of ejection；The most repeatedly, waste acid liquor
In moisture be gradually pulled away, the concentration of waste acid liquor is gradually increased；When the concentration of waste acid liquor reaches 60%, open conveying
Pump I, delivers to filter by waste acid liquor high for concentrated rear solid content, obtains filtrate I and filtering residue I after filtering, is returned by filtrate I
Being back to waste acid column, filtering residue I delivery pump II delivers to pressure filter；Filtering residue I obtains filtrate II and filtering residue II, filtrate after filter pressing processes
II returns again to waste acid column, and filtering residue II recycles；Waste acid liquor after concentration is expelled to subsequent step, its row
The flow going out waste acid liquor is 4.33m3/h.Device used by the processing method of the present embodiment is identical with the device in embodiment 1.
Embodiment 7
The embodiment of the waste acid concentration processing method that the hot blast of a kind of present invention and tube still heater combine, its process chart is such as
Shown in Fig. 1, comprise the following steps: adding the waste acid liquor intending concentrating that acid strength is 15% in waste acid column, flow is
20m3/h；It is passed through, toward the air inlet vertical pipe top of waste acid column, the hot blast that temperature is 160 DEG C by gas pipeline；ON cycle pump,
Waste acid liquor in waste acid column is delivered to tube still heater, makes waste acid liquor temperature be increased to 90 DEG C through tube still heater heating；
Waste acid liquor after heating enters the air inlet vertical pipe bottom in waste acid column, sprays from bottom to top along air inlet vertical pipe, with edge
Air inlet vertical pipe top-down hot blast counter current contacting, concentrates the waste acid liquor of ejection；The most repeatedly, waste acid liquor
In moisture be gradually pulled away, the concentration of waste acid liquor is gradually increased；When the concentration of waste acid liquor reaches 56%, open conveying
Pump I, delivers to filter by waste acid liquor high for concentrated rear solid content, obtains filtrate I and filtering residue I after filtering, is back to by filtrate I
Waste acid column, filtering residue I delivery pump II delivers to pressure filter；Filtering residue I through filter pressing process after filtrate II and filtering residue II, filtrate II return again to
Waste acid column, filtering residue II recycles；Waste acid liquor after concentration is expelled to subsequent step, and it discharges waste acid liquor
Flow be 5.36m3/h.Device used by the processing method of the present embodiment is identical with the device in embodiment 1.
The foregoing is only the preferred embodiments of the present invention, be not limited to the present invention, those skilled in the art is come
Saying, the present invention can have various modifications and variations.All within the spirit and principles in the present invention, any amendment of being made, equivalent
Replacement, improvement etc., should be included within the scope of the present invention.
Claims (10)
1. the waste acid concentration processing method that hot blast and tube still heater combine, comprises the following steps:
(1) in spent acid container, add the waste acid liquor intending concentrating；
(2) hot blast is delivered in the air inlet vertical pipe of spent acid container；
(3) heat in the waste acid liquor in spent acid container being delivered to tube still heater by circulating pump, by molten for the spent acid after heating
Liquid carries out counter current contacting with hot blast in delivering to the air inlet vertical pipe of spent acid container, and the waste acid liquor after counter current contacting flows into spent acid
Container bottom；
(4) repeat the above steps (2) and (3), concentrate waste acid liquor circulating and evaporating.
The waste acid concentration processing method that hot blast the most according to claim 1 and tube still heater combine, it is characterised in that:
In described step (4), waste acid liquor circulating and evaporating is delivered in filter after concentrating filter, and obtains filtrate I and filtering residue I, and will
Described filtrate I is back to spent acid container.
The waste acid concentration processing method that hot blast the most according to claim 2 and tube still heater combine, it is characterised in that:
Described filtering residue I is delivered to pressure filter filter pressing, obtains filtrate II and filtering residue II, and described filtrate II is back to spent acid container, filter
Slag II recycles.
The waste acid concentration processing method that hot blast the most according to claim 1 and tube still heater combine, it is characterised in that:
In described step (2), specifically refer in hot blast is delivered to the air inlet vertical pipe of spent acid container: hot blast is delivered to spent acid and holds
The top of the air inlet vertical pipe of device, hot blast flows in air inlet vertical pipe from top to bottom；In described step (3), will heating
After waste acid liquor deliver to the air inlet vertical pipe of spent acid container in carry out counter current contacting with hot blast and specifically refer to: will heat at tubulation
Waste acid liquor after heating delivers to the bottom of the air inlet vertical pipe of spent acid container in device, along air inlet vertical pipe upward spraying, with
The hot blast flowed from top to bottom in air inlet vertical pipe carries out counter current contacting.
5. the waste acid concentration processing method combined according to the hot blast according to any one of claim 1-4 and tube still heater, its
Being characterised by: in described step (2), the temperature of hot blast is 100 DEG C～180 DEG C；In described step (3), heat at tubulation
The temperature of the waste acid liquor after heating in device is 80 DEG C～100 DEG C；In described step (4), waste acid liquor after circulating and evaporating concentration
Concentration be 50%～64%.
6. the waste acid concentration processing method combined according to the hot blast according to any one of claim 1-4 and tube still heater, its
Being characterised by: in described step (1), the concentration of the waste acid liquor intending concentration is 10%～20%；Intend the waste acid liquor of concentration
Adding inbound traffics is 20m3/h。
7. the waste acid concentration processing method institute that the hot blast as according to any one of claim 1-6 and tube still heater combine
Device, including waste acid column (1), it is characterised in that: the top of described waste acid column (1) is provided with air inlet vertical pipe (2),
The upper end of described air inlet vertical pipe (2) connects hot blast air inlet pipe (3), and the bottom of air inlet vertical pipe (2) is provided with one will
Spent acid in waste acid column (1) carries out preheating the warm-up cycle device of tailing edge air inlet vertical pipe (2) upward spraying.
Device the most according to claim 7, it is characterised in that: described warm-up cycle device includes tube still heater (4),
One end of described tube still heater (4) is connected with the bottom of waste acid column (1) by pipeline, the other end and air inlet vertical pipe (2)
Bottom be connected, the pipeline that tube still heater (4) is connected with waste acid column (1) is provided with a circulating pump (5).
Device the most according to claim 7, it is characterised in that: the bottom of described waste acid column (1) connects one by pipeline
Filter (7), the pipeline that described filter (7) is connected with waste acid column (1) is provided with one first delivery pump (8), filter
(7) top is connected with waste acid column (1) by a filtrate recovery tube.
Device the most according to claim 9, it is characterised in that: described filter (7) passes through with a pressure filter (9)
Pipeline is connected, and the pipeline that described pressure filter (9) is connected with filter (7) is provided with one second delivery pump (10), pressure filter (9)
And it is provided with a pressing filtering liquid recovery tube between waste acid column (1).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610584094.0A CN106006806A (en) | 2016-07-22 | 2016-07-22 | Hot air and tubular heater combined waste acid concentration treatment method and device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610584094.0A CN106006806A (en) | 2016-07-22 | 2016-07-22 | Hot air and tubular heater combined waste acid concentration treatment method and device |
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| Publication Number | Publication Date |
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| CN106006806A true CN106006806A (en) | 2016-10-12 |
Family
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|---|---|---|---|
| CN201610584094.0A Pending CN106006806A (en) | 2016-07-22 | 2016-07-22 | Hot air and tubular heater combined waste acid concentration treatment method and device |
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Citations (25)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3074473A (en) * | 1957-12-23 | 1963-01-22 | H J Heinz Company Ltd | Vertical tube evaporators with downward pressure liquid flow |
| US3324632A (en) * | 1965-12-07 | 1967-06-13 | Combustion Eng | Apparatus for concentrating residual pulp liquor by direct contact with flue gases |
| GB1193559A (en) * | 1967-12-20 | 1970-06-03 | Knapsack Ag | Apparatus for Thickening or Concentrating Highly Fluid Solutions. |
| GB1326958A (en) * | 1969-12-30 | 1973-08-15 | Daido Chemical Eng Corp | Regeneration of sulphuric acid pickling waste |
| GB1336385A (en) * | 1970-07-18 | 1973-11-07 | Bayer Ag | Process for the continuous removal of distillation residues from crude isocyanates |
| CN2221412Y (en) * | 1995-06-12 | 1996-03-06 | 林载祁 | Hot-pump type liquid medicine evaporator |
| JPH10182114A (en) * | 1996-11-26 | 1998-07-07 | Haldor Topsoee As | Concentration of sulfuric acid |
| DE19741511A1 (en) * | 1997-09-20 | 1999-04-01 | Metallgesellschaft Ag | Process for concentrating thin acid by utilizing process heat in a forced circulation evaporator system |
| CN2402967Y (en) * | 1999-12-22 | 2000-10-25 | 钟涛 | Top-fired steam and boiling water boiler |
| CN2413178Y (en) * | 2000-03-24 | 2001-01-03 | 文茂林 | Alcohol waste liquor concentrator |
| CN1376633A (en) * | 2002-05-09 | 2002-10-30 | 四川龙蟒集团有限责任公司 | Process for concentrating diluted sulfuric acid and removing impurities |
| CN1843901A (en) * | 2006-04-27 | 2006-10-11 | 中国石化集团南京设计院 | Wet-process two-stage phosphoric acid concentration method |
| CN2829862Y (en) * | 2005-05-24 | 2006-10-25 | 吴康地 | Recovery appts for utilizing industrial waste gas to concentrate thin sulfuric acid |
| CN201034446Y (en) * | 2007-04-24 | 2008-03-12 | 胡杰 | Bobbin carriage type heat exchanger casing |
| CN201760114U (en) * | 2010-01-12 | 2011-03-16 | 天津海之凰科技有限公司 | Vapor compression distilling device employing nonmetallic heat conductive hollow fiber |
| US20110061867A1 (en) * | 2009-08-07 | 2011-03-17 | Bjorklund Daniel P | Method for production of high purity distillate from produced water for generation of high pressure steam |
| CN201815128U (en) * | 2010-10-21 | 2011-05-04 | 长沙新宇高分子科技有限公司 | Tapered tube type falling film evaporator |
| CN201819508U (en) * | 2010-08-30 | 2011-05-04 | 合肥天翔环境工程有限公司 | Shell-and-tube type water cooler with adjustable heat exchanging area of non-ferrous metal fine grain recovering equipment |
| CN102674281A (en) * | 2012-05-14 | 2012-09-19 | 瓮福（集团）有限责任公司 | Phosphoric acid refining device |
| CN103407973A (en) * | 2013-08-14 | 2013-11-27 | 天门福临化工有限责任公司 | Pyrite acid-preparing pre-drying self-condensation process |
| CN103663398A (en) * | 2013-11-29 | 2014-03-26 | 安徽六国化工股份有限公司 | Method and device for utilizing heat energy of diammonium phosphate neutralization tail gas |
| CN203602362U (en) * | 2013-11-29 | 2014-05-21 | 安徽六国化工股份有限公司 | Device for using heat energy of diammonium phosphate neutralizing tail gas |
| CN104147800A (en) * | 2014-08-27 | 2014-11-19 | 江苏凯茂石化科技有限公司 | Two-stage methanol evaporation column and methanol evaporation technology method |
| CN104843922A (en) * | 2015-04-30 | 2015-08-19 | 北京朗新明环保科技有限公司南京分公司 | Low-temperature evaporative type high-salt wastewater treatment device using wastewater waste heat |
| CN105344119A (en) * | 2015-11-30 | 2016-02-24 | 浙江奇彩环境科技有限公司 | Low-temperature spray evaporation waste water treatment device and waste water treatment method |
-
2016
- 2016-07-22 CN CN201610584094.0A patent/CN106006806A/en active Pending
Patent Citations (25)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3074473A (en) * | 1957-12-23 | 1963-01-22 | H J Heinz Company Ltd | Vertical tube evaporators with downward pressure liquid flow |
| US3324632A (en) * | 1965-12-07 | 1967-06-13 | Combustion Eng | Apparatus for concentrating residual pulp liquor by direct contact with flue gases |
| GB1193559A (en) * | 1967-12-20 | 1970-06-03 | Knapsack Ag | Apparatus for Thickening or Concentrating Highly Fluid Solutions. |
| GB1326958A (en) * | 1969-12-30 | 1973-08-15 | Daido Chemical Eng Corp | Regeneration of sulphuric acid pickling waste |
| GB1336385A (en) * | 1970-07-18 | 1973-11-07 | Bayer Ag | Process for the continuous removal of distillation residues from crude isocyanates |
| CN2221412Y (en) * | 1995-06-12 | 1996-03-06 | 林载祁 | Hot-pump type liquid medicine evaporator |
| JPH10182114A (en) * | 1996-11-26 | 1998-07-07 | Haldor Topsoee As | Concentration of sulfuric acid |
| DE19741511A1 (en) * | 1997-09-20 | 1999-04-01 | Metallgesellschaft Ag | Process for concentrating thin acid by utilizing process heat in a forced circulation evaporator system |
| CN2402967Y (en) * | 1999-12-22 | 2000-10-25 | 钟涛 | Top-fired steam and boiling water boiler |
| CN2413178Y (en) * | 2000-03-24 | 2001-01-03 | 文茂林 | Alcohol waste liquor concentrator |
| CN1376633A (en) * | 2002-05-09 | 2002-10-30 | 四川龙蟒集团有限责任公司 | Process for concentrating diluted sulfuric acid and removing impurities |
| CN2829862Y (en) * | 2005-05-24 | 2006-10-25 | 吴康地 | Recovery appts for utilizing industrial waste gas to concentrate thin sulfuric acid |
| CN1843901A (en) * | 2006-04-27 | 2006-10-11 | 中国石化集团南京设计院 | Wet-process two-stage phosphoric acid concentration method |
| CN201034446Y (en) * | 2007-04-24 | 2008-03-12 | 胡杰 | Bobbin carriage type heat exchanger casing |
| US20110061867A1 (en) * | 2009-08-07 | 2011-03-17 | Bjorklund Daniel P | Method for production of high purity distillate from produced water for generation of high pressure steam |
| CN201760114U (en) * | 2010-01-12 | 2011-03-16 | 天津海之凰科技有限公司 | Vapor compression distilling device employing nonmetallic heat conductive hollow fiber |
| CN201819508U (en) * | 2010-08-30 | 2011-05-04 | 合肥天翔环境工程有限公司 | Shell-and-tube type water cooler with adjustable heat exchanging area of non-ferrous metal fine grain recovering equipment |
| CN201815128U (en) * | 2010-10-21 | 2011-05-04 | 长沙新宇高分子科技有限公司 | Tapered tube type falling film evaporator |
| CN102674281A (en) * | 2012-05-14 | 2012-09-19 | 瓮福（集团）有限责任公司 | Phosphoric acid refining device |
| CN103407973A (en) * | 2013-08-14 | 2013-11-27 | 天门福临化工有限责任公司 | Pyrite acid-preparing pre-drying self-condensation process |
| CN103663398A (en) * | 2013-11-29 | 2014-03-26 | 安徽六国化工股份有限公司 | Method and device for utilizing heat energy of diammonium phosphate neutralization tail gas |
| CN203602362U (en) * | 2013-11-29 | 2014-05-21 | 安徽六国化工股份有限公司 | Device for using heat energy of diammonium phosphate neutralizing tail gas |
| CN104147800A (en) * | 2014-08-27 | 2014-11-19 | 江苏凯茂石化科技有限公司 | Two-stage methanol evaporation column and methanol evaporation technology method |
| CN104843922A (en) * | 2015-04-30 | 2015-08-19 | 北京朗新明环保科技有限公司南京分公司 | Low-temperature evaporative type high-salt wastewater treatment device using wastewater waste heat |
| CN105344119A (en) * | 2015-11-30 | 2016-02-24 | 浙江奇彩环境科技有限公司 | Low-temperature spray evaporation waste water treatment device and waste water treatment method |
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