CN107161950A - The thickening device and method of a kind of low concentration waste hydrochloric acid - Google Patents
The thickening device and method of a kind of low concentration waste hydrochloric acid Download PDFInfo
- Publication number
- CN107161950A CN107161950A CN201710513889.7A CN201710513889A CN107161950A CN 107161950 A CN107161950 A CN 107161950A CN 201710513889 A CN201710513889 A CN 201710513889A CN 107161950 A CN107161950 A CN 107161950A
- Authority
- CN
- China
- Prior art keywords
- tower
- level
- pump
- absorption tower
- spray head
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
- C01B7/0712—Purification ; Separation of hydrogen chloride by distillation
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a kind of thickening device of low concentration waste hydrochloric acid and method, the device be liquid pool by pipeline successively with pump, one-level Analytic Tower, the bottom connection of one-level condensing tower and first grade absorption tower, the bottom of first grade absorption tower is connected with pump, product collecting tank successively by pipeline, and product collecting tank connects first, second spray head；Bottom of the bottom of one-level Analytic Tower by pipeline successively with pump, two grades of Analytic Towers, B-grade condensation tower and two-level absorption tower is connected, and the bottom of two-level absorption tower is connected with first, second spray head respectively again after being connected by pipeline with pump；Bottom of the bottom of two grades of Analytic Towers by pipeline successively with pump, evaporator, steam condensing tower and recovery tower is connected, and recovery tower is provided with the 3rd spray head of connection alkali liquor pipe；The bottom of evaporator is connected with pump, liquid pool successively by pipeline；The present invention is to watery hydrochloric acid enrichment, and its equipment is simple, and the rate of recovery is high, and Matter Transfer is used, after abraum salt aqueous acid enrichment, realizes waste hydrochloric acid zero-emission, environmental protection.
Description
Technical field
The present invention discloses the enrichment technology and device of a kind of low concentration waste hydrochloric acid, belongs to chemical field.
Background technology
With continuing to develop for metal industry, the processing and surface treatment of steel cause the extensive concern of various countries.Hydrochloric acid
It is widely used as a kind of cheap corrosivity strong acid in field of metallurgy.15%~20% dilute hydrochloric acid solution is 60~70
The oxide of metal surface can be removed by being passed through at DEG C in descaling bath, solve the problem that steel gets rusty in air or water.Institute
Since nearly half a century, hydrochloric acid is always as the optimal selection of acid solution in acid cleaning process.In addition to steel industry, hydrochloric acid exists
Chemical industry, medicine and other fields also have extremely important effect, such as being bleachinged and dyeing with salt acids medicine organic synthesis, clothing.
In recent years, being continuously increased due to consumption demand, can also produce a large amount of low dense containing impurity in the industrial production
Spent acid is spent, the recycling of hydrochloric acid is significantly limit.Industrially in order to avoid bringing environmental pollution, it is frequently utilized that substantial amounts of
Lime stone and waste hydrochloric acid carry out neutralization reaction, are just discharged after acidity is up to standard.So do and not only cause the wasting of resources, and
And processing cost is higher, or even secondary pollution equivalent risk can be brought.So, it is always scientist that hydrochloride waste is handled for a long time
The focus studied.
At present, the concentration technology of the watery hydrochloric acid of domestic and international application comparative maturity mainly have conventional desorption method, variable-pressure rectification method,
The processes such as extraction fractional distillation, membrane separation process.But these methods all respectively have advantage and disadvantage, often in actual applications by each
Plant limitation.Such as conventional desorption method is suitable only for the desorption operations of hydrochloric acid solution of the mass fraction higher than 20.24%, is applicable model
Enclose narrow.Although variable-pressure rectification method need not add other materials, the purpose of concentrate hydrochloric acid just can reach；But also require simultaneously
Tower will have preferable tolerance to pressure and temperature, consume energy also relatively high, up to not in actual production process
To optimal economic benefit.And sulfuric acid extraction fractional distillation has certain difficulty, the severe corrosive of sulfuric acid during operational control
Also there is higher requirement to appliance arrangement, these can all limit this method and widely apply.The application of extractive distillation with salt method is most
Many salt is CaCl2But, although it is relatively low using the addition cost of calcium chloride, but can not only make the easy fouling of equipment, operation temperature
Degree is high, there is higher limitation to equipment requirement.Simultaneously it has also been found that there is the research method for adding magnesium chloride solution, but all it is difficult to solve
The problem of environmental pollution that its waste liquid is brought.Membrane separation process is applied to heat of dissociation allergin and difficult separate substance, with separation
Effect is good, energy consumption is relatively low, equipment volume is small, be easy to amplification the advantages of.But also need further to study it in the industrial production
Using, and to consider reduction production cost increase economic benefit.In summary, the concentration technology of all kinds of watery hydrochloric acid is being controlled at present
All exist in financial cost processed, the scope of application, equipment requirement and control condition and much denounce.Need the concentration work to watery hydrochloric acid
Skill is further studied.
The content of the invention
The purpose of the present invention is to overcome the deficiencies in the prior art there is provided a kind of thickening device of low concentration waste hydrochloric acid.
Second object of the present invention is to provide a kind of thickening method of low concentration waste hydrochloric acid.
Technical scheme is summarized as follows：
A kind of thickening device of low concentration waste hydrochloric acid, liquid pool 10 by pipeline successively with the first pump 11, one-level Analytic Tower
1, the bottom connection of one-level condensing tower 4 and first grade absorption tower 7, the bottom of first grade absorption tower 7 by pipeline successively with the 5th pump 21,
Product collecting tank 23 is connected, and product collecting tank 23 passes through pipeline and the first spray head 18, two of the internal upper part of first grade absorption tower 7 respectively
Second spray head 19 of level absorption tower 8 internal upper part is connected；The bottom of one-level Analytic Tower 1 is connected with the first reboiler 15；One-level solution
Analyse the bottom of tower 1 by pipeline successively with the second pump 12, two grades of Analytic Towers 2, B-grade condensation tower 5 and two-level absorption tower 8 bottom
Connection, the bottom of two-level absorption tower 8 be connected by pipeline with the 6th pump 22 after again respectively with the internal upper part of first grade absorption tower 7 first
Second spray head 19 of spray head 18 and the internal upper part of two-level absorption tower 8 is connected；The bottom of two grades of Analytic Towers 2 is connected with second and boiled again
Device 16, the bottom of the bottoms of two grades of Analytic Towers 2 by pipeline successively with the 3rd pump 13, evaporator 3, steam condensing tower 6 and recovery tower 9
Portion is connected, the top of recovery tower 9 is provided with atmospheric valve 24, and the internal upper part of recovery tower 9 is provided with the 3rd spray head 20, the 3rd spray
First 20 are connected with alkali liquor pipe 25；The bottom of evaporator 3 is connected with the 3rd reboiler 17, and the bottom of evaporator 3 passes through pipeline and
It is connected after the connection of four pumps 14 with liquid pool 10；Cooling water pipe 26 is condensed with one-level condensing tower 4, B-grade condensation tower 5 and steam successively
Tower 6 is connected；The top of first grade absorption tower 7 is connected by pipeline with the bottom of two-level absorption tower 8, and the top of two-level absorption tower 8 leads to
Piping is connected with the bottom of recovery tower 9, and the bottom of recovery tower 9 is provided with waste liquid discharge pipe 27, and the bottom of steam condensing tower 6 is set
It is equipped with condensed water outlet pipe 28.
A kind of thickening method of low concentration waste hydrochloric acid, comprises the following steps：
(1) a kind of above-mentioned thickening device of low concentration waste hydrochloric acid is used；
(2) magnesium chloride brine that weight/mass percentage composition is 25-33% is prepared, places to room temperature, is added to liquid pool 10；
(3) mass concentration is added separately to product collecting tank 23 for the abraum salt aqueous acid in the range of 5%-20% and matched somebody with somebody
In liquid bath 10, the volume ratio of magnesium chloride brine and abraum salt aqueous acid is in 0.8-1 in adjustment liquid pool 10：In the range of 1；
(4) by the mixed liquor in liquid pool 10, it is driven into through the first pump 11 in one-level Analytic Tower 1, is warming up to 105-120
DEG C, parsing balance 80-130min, the hydrogen chloride gas that one-level Analytic Tower 1 is parsed is after the condensation of one-level condensing tower 4 from one-level
The bottom on absorption tower 7 enters in first grade absorption tower 7；The temperature of the cooling water of one-level condensing tower 4 is 5-20 DEG C, and regulation product is collected
The flow of tank 23, the flow rate for making the first spray head 18 of the internal upper part of first grade absorption tower 7 is 15-25ml/min, passes through first order absorption
The hydrochloric acid solution that tower 7 is produced, squeezes into product collecting tank 23 through the 5th pump 21 and carries out circulated sprinkling absorption and product collection；Through one-level
Hydrochloric acid raffinate after the desorption of Analytic Tower 1, squeezes into two grades of Analytic Towers 2 through the second pump 12 and is further desorbed, the chlorination desorbed
The tail gas that hydrogen comes out after the condensation of B-grade condensation tower 5 with first grade absorption tower 7 together enters from the bottom of two-level absorption tower 8,
The flow rate for controlling the second spray head 19 is 15-25ml/min, passes through the low concentration of salt acid solution produced by two-level absorption tower 8, warp
6th pump 22 squeezes into the first spray head 18 and the second spray head 19 respectively；Hydrochloric acid raffinate after being desorbed through two grades of Analytic Towers 2, with the
Three pumps 13 squeeze into evaporator 3 and are evaporated concentration, and the solution after evaporation and concentration is squeezed into liquid pool 10 through the 4th pump 14, evaporation
The hydrogen chloride and water vapour that device 3 is produced are by steam condensing tower 6, and condensed water vapour is cold from the bottom of steam condensing tower 6
Solidifying water outlet pipe 28 is discharged, and the tail gas of hydrogen chloride gas and two-level absorption tower 8 together enters recovery tower 9, by the 3rd spray head 20
The sodium hydrate aqueous solution of ejection is neutralized, and the liquid after neutralization is discharged from waste liquid discharge pipe 27, and gas is discharged from atmospheric valve 24.
Advantages of the present invention：
The present invention using magnesium chloride as strippant, and desorbed by two-stage, the method that two-stage is absorbed, one-level is reclaimed carry out it is dilute
Hydrochloric acid enrichment, its equipment is simple, and the rate of recovery is high, and Matter Transfer is used, and after abraum salt aqueous acid enrichment, realizes waste hydrochloric acid zero-emission
Put, environmental protection.
Brief description of the drawings
Fig. 1 is a kind of thickening device structural representation of low concentration waste hydrochloric acid of the present invention.
Embodiment
The present invention is further illustrated with specific embodiment below in conjunction with the accompanying drawings.
A kind of thickening device of low concentration waste hydrochloric acid, is shown in Fig. 1, liquid pool 10 by pipeline successively with the first pump 11, one-level
The bottom connection of Analytic Tower 1, one-level condensing tower 4 and first grade absorption tower 7, the bottom of first grade absorption tower 7 is by pipeline successively with the
Five pumps 21, product collecting tank 23 are connected, and product collecting tank 23 passes through pipeline and the first spray of the internal upper part of first grade absorption tower 7 respectively
First 18, the second spray head 19 of the internal upper part of two-level absorption tower 8 is connected；The bottom of one-level Analytic Tower 1 is connected with the first reboiler 15；
The bottom of one-level Analytic Tower 1 by pipeline successively with the second pump 12, two grades of Analytic Towers 2, B-grade condensation tower 5 and two-level absorption tower 8
Bottom connection, the bottom of two-level absorption tower 8 be connected by pipeline with the 6th pump 22 after again respectively with the internal upper part of first grade absorption tower 7
The first spray head 18 and the second spray head 19 of the internal upper part of two-level absorption tower 8 connect；The bottom of two grades of Analytic Towers 2 is connected with
Two reboilers 16, the bottoms of two grades of Analytic Towers 2 is by pipeline successively with the 3rd pump 13, evaporator 3, steam condensing tower 6 and reclaiming
The bottom connection of tower 9, the top of recovery tower 9 is provided with atmospheric valve 24, and the internal upper part of recovery tower 9 is provided with the 3rd spray head 20,
3rd spray head 20 is connected with alkali liquor pipe 25；The bottom of evaporator 3 is connected with the 3rd reboiler 17, and the bottom of evaporator 3 passes through
Pipeline is connected after being connected with the 4th pump 14 with liquid pool 10；Cooling water pipe 26 successively with one-level condensing tower 4, the He of B-grade condensation tower 5
Steam condensing tower 6 is connected；The top of first grade absorption tower 7 is connected by pipeline with the bottom of two-level absorption tower 8, two-level absorption tower 8
Top be connected by pipeline with the bottom of recovery tower 9, the bottom of recovery tower 9 is provided with waste liquid discharge pipe 27, steam condensing tower 6
Bottom be provided with condensed water outlet pipe 28.
Embodiment 1
A kind of thickening method of low concentration waste hydrochloric acid, comprises the following steps：
(1) a kind of thickening device of low concentration waste hydrochloric acid is used；
(2) magnesium chloride brine that weight/mass percentage composition is 30% is prepared, places to room temperature, is added to liquid pool 10；
(3) mass concentration is added separately to product collecting tank 23 for the abraum salt aqueous acid in the range of 5%-20% and matched somebody with somebody
In liquid bath 10, the volume ratio of magnesium chloride brine and abraum salt aqueous acid is 1 in adjustment liquid pool 10：1；
(4) by the mixed liquor in liquid pool 10, it is driven into through the first pump 11 in one-level Analytic Tower 1, is warming up to 110 DEG C, solution
Analysis balance 100min, due to the effect of common-ion effect so that gas phase chlorination hydrogen dividing potential drop increases, so as to change hydrochloric acid-water group
/ relative volatility, increase the constant boiling point of hydrochloric acid-aqueous systems, reduce the saturated vapour pressure of solution, be more beneficial for
The desorption of hydrogen chloride gas；The hydrogen chloride gas that one-level Analytic Tower 1 is parsed is after the condensation of one-level condensing tower 4 from first order absorption
The bottom of tower 7 enters in first grade absorption tower 7；The temperature of the cooling water of one-level condensing tower 4 is 5-20 DEG C, regulation product collecting tank 23
Flow, make the internal upper part of first grade absorption tower 7 the first spray head 18 flow rate be 15-25ml/min, in the tower top of first grade absorption tower 7
Absorbed with spraying mode, the hydrochloric acid solution produced by first grade absorption tower 7, squeeze into product collecting tank 23 through the 5th pump 21 and followed
Ring spray-absorption and product are collected；Hydrochloric acid raffinate after being desorbed through one-level Analytic Tower 1, two grades of Analytic Towers 2 are squeezed into through the second pump 12
Further desorbed, the tail gas that the hydrogen chloride gas desorbed comes out after the condensation of B-grade condensation tower 5 with first grade absorption tower 7
Together enter from the bottom of two-level absorption tower 8, the flow rate for controlling the second spray head 19 is 15-25ml/min, in the tower of two-level absorption tower 8
Top is absorbed with spraying mode, and by the low concentration of salt acid solution produced by two-level absorption tower 8, first is squeezed into respectively through the 6th pump 22
The spray head 19 of spray head 18 and second；Hydrochloric acid raffinate after being desorbed through two grades of Analytic Towers 2, squeezes into evaporator 3 with the 3rd pump 13 and enters
Row is concentrated by evaporation, and the solution after evaporation and concentration is squeezed into liquid pool 10 through the 4th pump 14, hydrogen chloride and water that evaporator 3 is produced
Steam is discharged by steam condensing tower 6, condensed water vapour from the condensed water outlet pipe 28 of the bottom of steam condensing tower 6, chlorine
The tail gas for changing hydrogen and two-level absorption tower 8 together enters recovery tower 9, the sodium hydrate aqueous solution sprayed by the 3rd spray head 20
Neutralize, the liquid after neutralization is discharged from waste liquid discharge pipe 27, and gas is discharged from atmospheric valve 24.
Embodiment 2
A kind of thickening method of low concentration waste hydrochloric acid, comprises the following steps：
(1) a kind of thickening device of low concentration waste hydrochloric acid is used；
(2) magnesium chloride brine that weight/mass percentage composition is 25% is prepared, places to room temperature, is added to liquid pool 10；
(3) mass concentration is added separately to product collecting tank 23 for the abraum salt aqueous acid in the range of 5%-20% and matched somebody with somebody
In liquid bath 10, the volume ratio of magnesium chloride brine and abraum salt aqueous acid is 0.8 in adjustment liquid pool 10：1；
(4) by the mixed liquor in liquid pool 10, it is driven into through the first pump 11 in one-level Analytic Tower 1, is warming up to 105 DEG C, solution
Analysis balance 130min, due to the effect of common-ion effect so that gas phase chlorination hydrogen dividing potential drop increases, so as to change hydrochloric acid-water group
/ relative volatility, increase the constant boiling point of hydrochloric acid-aqueous systems, reduce the saturated vapour pressure of solution, be more beneficial for
The desorption of hydrogen chloride gas；The hydrogen chloride gas that one-level Analytic Tower 1 is parsed is after the condensation of one-level condensing tower 4 from first order absorption
The bottom of tower 7 enters in first grade absorption tower 7；The temperature of the cooling water of one-level condensing tower 4 is 5-20 DEG C, regulation product collecting tank 23
Flow, make the internal upper part of first grade absorption tower 7 the first spray head 18 flow rate be 15-25ml/min, in the tower top of first grade absorption tower 7
Absorbed with spraying mode, the hydrochloric acid solution produced by first grade absorption tower 7, squeeze into product collecting tank 23 through the 5th pump 21 and followed
Ring spray-absorption and product are collected；Hydrochloric acid raffinate after being desorbed through one-level Analytic Tower 1, two grades of Analytic Towers 2 are squeezed into through the second pump 12
Further desorbed, the tail gas that the hydrogen chloride gas desorbed comes out after the condensation of B-grade condensation tower 5 with first grade absorption tower 7
Together enter from the bottom of two-level absorption tower 8, the flow rate for controlling the second spray head 19 is 15-25ml/min, in the tower of two-level absorption tower 8
Top is absorbed with spraying mode, and by the low concentration of salt acid solution produced by two-level absorption tower 8, first is squeezed into respectively through the 6th pump 22
The spray head 19 of spray head 18 and second；Hydrochloric acid raffinate after being desorbed through two grades of Analytic Towers 2, squeezes into evaporator 3 with the 3rd pump 13 and enters
Row is concentrated by evaporation, and the solution after evaporation and concentration is squeezed into liquid pool 10 through the 4th pump 14, hydrogen chloride and water that evaporator 3 is produced
Steam is discharged by steam condensing tower 6, condensed water vapour from the condensed water outlet pipe 28 of the bottom of steam condensing tower 6, chlorine
The tail gas for changing hydrogen and two-level absorption tower 8 together enters recovery tower 9, the sodium hydrate aqueous solution sprayed by the 3rd spray head 20
Neutralize, the liquid after neutralization is discharged from waste liquid discharge pipe 27, and gas is discharged from atmospheric valve 24.
Embodiment 3
A kind of thickening method of low concentration waste hydrochloric acid, comprises the following steps：
(1) a kind of thickening device of low concentration waste hydrochloric acid is used；
(2) magnesium chloride brine that weight/mass percentage composition is 33% is prepared, places to room temperature, is added to liquid pool 10；
(3) mass concentration is added separately to product collecting tank 23 for the abraum salt aqueous acid in the range of 5%-20% and matched somebody with somebody
In liquid bath 10, the volume ratio of magnesium chloride brine and abraum salt aqueous acid is 0.9 in adjustment liquid pool 10：1；
(4) by the mixed liquor in liquid pool 10, it is driven into through the first pump 11 in one-level Analytic Tower 1, is warming up to 120 DEG C, solution
Analysis balance 80min, due to the effect of common-ion effect so that gas phase chlorination hydrogen dividing potential drop increases, so as to change hydrochloric acid-water component
Between relative volatility, increase the constant boiling point of hydrochloric acid-aqueous systems, reduce the saturated vapour pressure of solution, be more beneficial for chlorine
Change the desorption of hydrogen；The hydrogen chloride gas that one-level Analytic Tower 1 is parsed is after the condensation of one-level condensing tower 4 from first grade absorption tower
7 bottom enters in first grade absorption tower 7；The temperature of the cooling water of one-level condensing tower 4 is 5-20 DEG C, regulation product collecting tank 23
Flow, make the internal upper part of first grade absorption tower 7 the first spray head 18 flow rate be 15-25ml/min, the tower top of first grade absorption tower 7 with
Spray mode is absorbed, the hydrochloric acid solution produced by first grade absorption tower 7, and squeezing into product collecting tank 23 through the 5th pump 21 is circulated
Spray-absorption and product are collected；Hydrochloric acid raffinate after being desorbed through one-level Analytic Tower 1, squeezes into two grades of Analytic Towers 2 through the second pump 12 and enters
Row further desorption, the tail gas one that the hydrogen chloride gas desorbed comes out after the condensation of B-grade condensation tower 5 with first grade absorption tower 7
Enter with from the bottom of two-level absorption tower 8, the flow rate for controlling the second spray head 19 is 15-25ml/min, in the tower top of two-level absorption tower 8
Absorbed with spraying mode, by the low concentration of salt acid solution produced by two-level absorption tower 8, the first spray is squeezed into respectively through the 6th pump 22
The spray head 19 of pouring first 18 and second；Hydrochloric acid raffinate after being desorbed through two grades of Analytic Towers 2, squeezes into evaporator 3 with the 3rd pump 13 and carries out
It is concentrated by evaporation, the solution after evaporation and concentration is squeezed into liquid pool 10 through the 4th pump 14, the hydrogen chloride and water that evaporator 3 is produced steams
Vapour is discharged by steam condensing tower 6, condensed water vapour from the condensed water outlet pipe 28 of the bottom of steam condensing tower 6, chlorination
The tail gas of hydrogen and two-level absorption tower 8 together enters in recovery tower 9, the sodium hydrate aqueous solution sprayed by the 3rd spray head 20
With the liquid after neutralization is discharged from waste liquid discharge pipe 27, and gas is discharged from atmospheric valve 24.
Claims (2)
1. a kind of thickening device of low concentration waste hydrochloric acid, it is characterised in that liquid pool (10) by pipeline successively with the first pump
(11) the bottom connection of, one-level Analytic Tower (1), one-level condensing tower (4) and first grade absorption tower (7), the bottom of first grade absorption tower (7)
It is connected successively with the 5th pump (21), product collecting tank (23) by pipeline, product collecting tank (23) passes through pipeline and one-level respectively
The second spray head (19) connection of first spray head (18), two-level absorption tower (8) internal upper part of absorption tower (7) internal upper part；One-level
The bottom of Analytic Tower (1) is connected with the first reboiler (15)；The bottom of one-level Analytic Tower (1) by pipeline successively with the second pump
(12), two grades of Analytic Towers (2), B-grade condensation towers (5) are connected with the bottom of two-level absorption tower (8), the bottom of two-level absorption tower (8)
Inhaled respectively with first spray head (18) of first grade absorption tower (7) internal upper part and two grades again after being connected by pipeline with the 6th pump (22)
Receive the second spray head (19) connection of tower (8) internal upper part；The bottom of two grades of Analytic Towers (2) is connected with the second reboiler (16), two
Level Analytic Tower (2) bottom by pipeline successively with the 3rd pump (13), evaporator (3), steam condensing tower (6) and recovery tower (9)
Bottom connection, be provided with atmospheric valve (24) at the top of recovery tower (9), recovery tower (9) internal upper part is provided with the 3rd spray head
(20), the 3rd spray head (20) is connected with alkali liquor pipe (25)；The bottom of evaporator (3) is connected with the 3rd reboiler (17), evaporation
The bottom of device (3) is connected after being connected by pipeline with the 4th pump (14) with liquid pool (10)；Cooling water pipe (26) successively with one-level
Condensing tower (4), B-grade condensation tower (5) and steam condensing tower (6) connection；The top of first grade absorption tower (7) passes through pipeline and two grades
The bottom connection on absorption tower (8), the top of two-level absorption tower (8) is connected by pipeline with the bottom of recovery tower (9), recovery tower
(9) bottom is provided with waste liquid discharge pipe (27), and the bottom of steam condensing tower (6) is provided with condensed water outlet pipe (28).
2. a kind of thickening method of low concentration waste hydrochloric acid, it is characterized in that comprising the following steps：
(1) thickening device of a kind of low concentration waste hydrochloric acid of usage right requirement 1；
(2) magnesium chloride brine that weight/mass percentage composition is 25-33% is prepared, places to room temperature, is added to liquid pool (10)；
(3) mass concentration is added separately to product collecting tank (23) and with liquid for the abraum salt aqueous acid in the range of 5%-20%
In groove (10), the volume ratio of adjustment liquid pool (10) interior magnesium chloride brine and abraum salt aqueous acid is in 0.8-1：In the range of 1；
(4) by the mixed liquor in liquid pool (10), it is driven into through the first pump (11) in one-level Analytic Tower (1), is warming up to 105-120
DEG C, parsing balance 80-130min, the hydrogen chloride gas that one-level Analytic Tower (1) is parsed by one-level condensing tower (4) condense after from
The bottom of first grade absorption tower (7) enters in first grade absorption tower (7)；The temperature of the cooling water of one-level condensing tower (4) is 5-20 DEG C, is adjusted
The flow of product collecting tank (23) is saved, the flow rate for making first spray head (18) of first grade absorption tower (7) internal upper part is 15-25ml/
Min, the hydrochloric acid solution produced by first grade absorption tower (7) squeezes into product collecting tank (23) through the 5th pump (21) and carries out circulation spray
Drench and absorb and product collection；Hydrochloric acid raffinate after being desorbed through one-level Analytic Tower (1), two grades of Analytic Towers are squeezed into through the second pump (12)
(2) further desorbed, the hydrogen chloride gas desorbed goes out after B-grade condensation tower (5) condensation with first grade absorption tower (7)
The tail gas come together enters from two-level absorption tower (8) bottom, and the flow rate for controlling the second spray head (19) is 15-25ml/min, is led to
The low concentration of salt acid solution crossed produced by two-level absorption tower (8), the first spray head (18) and are squeezed into through the 6th pump (22) respectively
Two spray heads (19)；Through the hydrochloric acid raffinate after two grades of Analytic Tower (2) desorptions, squeeze into evaporator (3) with the 3rd pump (13) and steamed
Hair concentration, the solution after evaporation and concentration is squeezed into liquid pool (10) through the 4th pump (14), evaporator (3) produce hydrogen chloride and
Water vapour passes through steam condensing tower (6), condensed water outlet pipe (28) of the condensed water vapour from the bottom of steam condensing tower (6)
The tail gas of discharge, hydrogen chloride gas and two-level absorption tower (8) together enters recovery tower (9), is sprayed by the 3rd spray head (20)
Sodium hydrate aqueous solution is neutralized, and the liquid after neutralization is discharged from waste liquid discharge pipe (27), and gas is discharged from atmospheric valve (24).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710513889.7A CN107161950B (en) | 2017-06-29 | 2017-06-29 | A kind of thickening device and method of low concentration waste hydrochloric acid |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710513889.7A CN107161950B (en) | 2017-06-29 | 2017-06-29 | A kind of thickening device and method of low concentration waste hydrochloric acid |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107161950A true CN107161950A (en) | 2017-09-15 |
| CN107161950B CN107161950B (en) | 2019-04-23 |
Family
ID=59827107
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710513889.7A Active CN107161950B (en) | 2017-06-29 | 2017-06-29 | A kind of thickening device and method of low concentration waste hydrochloric acid |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107161950B (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107720697A (en) * | 2017-11-17 | 2018-02-23 | 李玉美 | A kind of method of multistage plus salt desorption absorbing coupling processing watery hydrochloric acid |
| CN110386591A (en) * | 2019-07-04 | 2019-10-29 | 南通星球石墨设备有限公司 | A kind of waste hydrochloric acid differential pressure regeneration treatment system |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08109007A (en) * | 1994-09-30 | 1996-04-30 | Sulzer Chemtech Ag | Method and apparatus for forming hydrogen chloride from chlorine waste |
| JPH09188502A (en) * | 1995-11-27 | 1997-07-22 | Andritz Patentverwaltungs Gmbh | Method and device for extracting or recovering acid from acid solution |
| CN1948129A (en) * | 2006-09-20 | 2007-04-18 | 河北沧州大化集团有限责任公司 | Method of preparing hydrochloric acid using TDI byproduct hydrogen chloride gas and its device |
| CN101623584A (en) * | 2009-07-28 | 2010-01-13 | 仇晓丰 | Hydrochloric acid full stripping method |
| CN106745420A (en) * | 2016-12-01 | 2017-05-31 | 南通京通石墨设备有限公司 | A kind of processing unit of waste hydrochloric acid |
-
2017
- 2017-06-29 CN CN201710513889.7A patent/CN107161950B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH08109007A (en) * | 1994-09-30 | 1996-04-30 | Sulzer Chemtech Ag | Method and apparatus for forming hydrogen chloride from chlorine waste |
| JPH09188502A (en) * | 1995-11-27 | 1997-07-22 | Andritz Patentverwaltungs Gmbh | Method and device for extracting or recovering acid from acid solution |
| CN1948129A (en) * | 2006-09-20 | 2007-04-18 | 河北沧州大化集团有限责任公司 | Method of preparing hydrochloric acid using TDI byproduct hydrogen chloride gas and its device |
| CN101623584A (en) * | 2009-07-28 | 2010-01-13 | 仇晓丰 | Hydrochloric acid full stripping method |
| CN106745420A (en) * | 2016-12-01 | 2017-05-31 | 南通京通石墨设备有限公司 | A kind of processing unit of waste hydrochloric acid |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107720697A (en) * | 2017-11-17 | 2018-02-23 | 李玉美 | A kind of method of multistage plus salt desorption absorbing coupling processing watery hydrochloric acid |
| CN110386591A (en) * | 2019-07-04 | 2019-10-29 | 南通星球石墨设备有限公司 | A kind of waste hydrochloric acid differential pressure regeneration treatment system |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107161950B (en) | 2019-04-23 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102502500A (en) | Device for producing hydrogen chloride by resolving hydrochloric acid | |
| CN102030672A (en) | Process for reclaiming super-high-purity N,N-dimethyl acetamide solvent in polyurethane fibre production process | |
| CN102531260A (en) | Steam stripping technology of high-concentration ammonia nitrogen effluent | |
| CN111330412B (en) | System and process for absorbing and purifying byproduct hydrogen chloride gas in chlorination section into acid | |
| CN102757019A (en) | System and method for concentrating and purifying hydrogen peroxide | |
| CN107161950B (en) | A kind of thickening device and method of low concentration waste hydrochloric acid | |
| CN203436836U (en) | Efficient and energy-saving type three-effect negative-pressure graphite evaporative crystallization device of hydrochloric acid pickling waste liquid | |
| CN103394206A (en) | High-efficiency energy-saving hydrochloric acid pickling waste liquor triple-effect negative-pressure graphite evaporation crystallizer | |
| CN107082407B (en) | A kind of method of purification of anhydrous hydrofluoric acid | |
| CN104771926B (en) | The rectifier unit of a kind of recovery of acetic acid from aqueous acetic acid and process | |
| CN110937744A (en) | Dimethylamine treatment process in synthetic leather DMF (dimethyl formamide) wastewater heat pump rectification process | |
| CN109647160B (en) | Method for treating tail gas of ammonium sulfate mother liquor circulation tank | |
| CN109467239A (en) | A kind of method for recovering acid from iron and steel pickling waste liquor | |
| CN107792904A (en) | A kind of technique and device of continuous removal of ammonia and nitrogen light component organic matter and salt | |
| CN106966865A (en) | The system that a kind of technique in three-effect countercurrent evaporation rectification process handles glycine crystallization mother liquid | |
| CN114436293B (en) | Method for directly producing sodium bromide from low-concentration brine | |
| CN217264857U (en) | Concentration and reuse device for chlorine gas drying waste acid | |
| CN104418723B (en) | The recovery method of trade effluent dilute formic acid and device | |
| CN106431836A (en) | A process for coupling extraction, rectification and flash distillation to separate ethanol-water system | |
| CN215249583U (en) | Waste acid concentration regeneration sulfuric acid production line | |
| CN207002611U (en) | The DMF wastewater treatment energy savers that a kind of low pressure heat pump distillation is combined with double-effect rectification | |
| CN206244421U (en) | A device for producing concentrated ammonia water by negative pressure operation | |
| CN214680106U (en) | High-purity anhydrous alcohol production system | |
| CN115738340A (en) | Method and system for preparing high-concentration or anhydrous hydrofluoric acid by using extracting agent | |
| CN205368182U (en) | System for triple effect evaporates rectification against current handles glycine mother liquor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |