CN107161950B - A kind of thickening device and method of low concentration waste hydrochloric acid - Google Patents
A kind of thickening device and method of low concentration waste hydrochloric acid Download PDFInfo
- Publication number
- CN107161950B CN107161950B CN201710513889.7A CN201710513889A CN107161950B CN 107161950 B CN107161950 B CN 107161950B CN 201710513889 A CN201710513889 A CN 201710513889A CN 107161950 B CN107161950 B CN 107161950B
- Authority
- CN
- China
- Prior art keywords
- tower
- level
- absorption tower
- pump
- pipeline
- 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.)
- Active
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 the thickening devices and method of a kind of low concentration waste hydrochloric acid, the device be liquid pool by pipeline successively with pump, level-one Analytic Tower, level-one condensing tower is connected with the lower part of first grade absorption tower, the lower part of first grade absorption tower is successively connect with pump, product collecting tank by pipeline, and product collecting tank connects the first, second spray head；The bottom of level-one Analytic Tower is successively connect with the lower part of pump, second level Analytic Tower, B-grade condensation tower and two-level absorption tower by pipeline, and the lower part of two-level absorption tower with the first, second spray head by connecting respectively again after pipeline and pump connection；The bottom of second level Analytic Tower is successively connect with the bottom of pump, evaporator, steam condensing tower and recovery tower by pipeline, and recovery tower is provided with the third spray head of connection alkali liquor pipe；The bottom of evaporator is successively connect with pump, liquid pool by pipeline；For the present invention to dilute hydrochloric acid enrichment, equipment is simple, and the rate of recovery is high, and Matter Transfer uses, and 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 technique
With the continuous development of metal industry, the processing and surface treatment of steel cause the extensive concern of various countries.Hydrochloric acid
It is widely used in field of metallurgy as a kind of cheap corrosivity strong acid.15%~20% dilute hydrochloric acid solution is 60~70
It is passed through the oxide that can remove metal surface in descaling bath at DEG C, solves the problems, such as that steel gets rusty in air or water.Institute
Since nearly half a century, hydrochloric acid is used as always the optimal selection of acid solution in acid cleaning process.Other than steel industry, hydrochloric acid exists
Chemical industry, medicine and other fields also have an extremely important effect, such as organic synthesis, clothing are bleachinged and dyeing with salt acids drug etc..
In recent years, being continuously increased due to consumption demand can also generate largely low dense containing impurity in the industrial production
Spent acid is spent, the recycling and reusing of hydrochloric acid is significantly limited.Industrially in order to avoid bringing environmental pollution, it is frequently utilized that a large amount of
Lime stone and waste hydrochloric acid carry out neutralization reaction, are just discharged after acidity is up to standard.It does so and not only causes the wasting of resources, and
And processing cost is higher, or even can bring the risks such as secondary pollution.So processing hydrochloride waste is always scientist for a long time
The hot spot studied.
Currently, the concentration technology of the dilute 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 practical applications by each
Kind 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 in model
It encloses narrow.Although variable-pressure rectification method does not need that other materials are added, can achieve the purpose that concentrate hydrochloric acid；But it also requires simultaneously
Tower will have preferable tolerance to pressure and temperature, consume energy also relatively high, in the actual production process up to not
To optimal economic benefit.And sulfuric acid extraction fractional distillation has certain difficulty, the strong corrosive of sulfuric acid in operation control process
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
More salt is CaCl2Although but cost is relatively low for the addition of utilization calcium chloride, but equipment can not only be made to be easy fouling, operation temperature
Degree is high, has higher limitation to equipment requirement.Simultaneously it has also been found that there is the research method that magnesium chloride solution is added, but all it is difficult to solve
Problem of environmental pollution brought by its waste liquid.Membrane separation process is suitable for heat of dissociation allergin and difficult separate substance, has separation
Effect is good, energy consumption is lower, equipment volume is small, is easy to the advantages that amplifying.But also need further to study it in the industrial production
Using, and to consider that reducing production cost increases economic benefit.In conclusion the concentration technology of all kinds of dilute hydrochloric acid is being controlled at present
All exist in economic cost processed, the scope of application, equipment requirement and control condition and much denounces.Need the concentration work to dilute hydrochloric acid
Skill conducts further research.
Summary of the invention
The purpose of the present invention is overcome the deficiencies of the prior art and provide a kind of thickening device of low concentration waste hydrochloric acid.
A second object of the present invention is to provide a kind of thickening methods of low concentration waste hydrochloric acid.
Technical solution of the present invention is summarized as follows:
A kind of thickening device of low concentration waste hydrochloric acid, liquid pool 10 successively pump 11 with first by pipeline, level-one Analytic Tower
1, level-one condensing tower 4 is connected with the lower part of first grade absorption tower 7, the lower part of first grade absorption tower 7 by pipeline successively with the 5th pump 21,
Product collecting tank 23 connects, and product collecting tank 23 passes through the first spray head 18, two of pipeline and 7 internal upper part of first grade absorption tower respectively
The second spray head 19 connection of 8 internal upper part of grade absorption tower；The lower part of level-one Analytic Tower 1 is connected with the first reboiler 15；Level-one solution
Analyse the lower part that the bottom of tower 1 successively pumps 12, second level Analytic Tower 2, B-grade condensation tower 5 and two-level absorption tower 8 with second by pipeline
Connection, the lower part of two-level absorption tower 8 by pipeline with the 6th pump 22 connect after again respectively with 7 internal upper part of first grade absorption tower first
Second spray head 19 of 8 internal upper part of spray head 18 and two-level absorption tower connects；The lower part of second level Analytic Tower 2 is connected with second and boils again
Device 16, the bottom of second level Analytic Tower 2 successively pump the bottom of 13, evaporator 3, steam condensing tower 6 and recovery tower 9 by pipeline with third
Portion's connection, the top of recovery tower 9 are provided with blow valve 24, and 9 internal upper part of recovery tower is provided with third spray head 20, third spray
First 20 connect with alkali liquor pipe 25；The lower part of evaporator 3 is connected with third reboiler 17, and the bottom of evaporator 3 passes through pipeline and the
It is connect after four pumps, 14 connection with liquid pool 10；Cooling water pipe 26 is successively condensed with level-one condensing tower 4, B-grade condensation tower 5 and steam
Tower 6 connects；The top of first grade absorption tower 7 is connect by pipeline with the lower part of two-level absorption tower 8, and the top of two-level absorption tower 8 is logical
Piping is connect with the lower part of recovery tower 9, and the lower part 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, includes the following steps:
(1) a kind of above-mentioned thickening device of low concentration waste hydrochloric acid is used；
(2) magnesium chloride brine that mass percentage 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 within the scope of 5%-20% and matched
In liquid bath 10, the volume ratio of magnesium chloride brine and abraum salt aqueous acid is in the range of 0.8-1:1 in adjustment liquid pool 10；
(4) it by the mixed liquor in liquid pool 10, is driven into level-one Analytic Tower 1 through the first pump 11, is warming up to 105-120
DEG C, parsing balance 80-130min, the hydrogen chloride gas that level-one Analytic Tower 1 parses is after the condensation of level-one condensing tower 4 from level-one
The lower part on absorption tower 7 enters in first grade absorption tower 7；The temperature of the cooling water of level-one condensing tower 4 is 5-20 DEG C, adjusts product and collects
The flow of tank 23 makes the flow rate 15-25ml/min of the first spray head 18 of 7 internal upper part of first grade absorption tower, passes through first order absorption
The hydrochloric acid solution that tower 7 generates squeezes into the progress circulated sprinkling absorption of product collecting tank 23 through the 5th pump 21 and product is collected；Through level-one
Hydrochloric acid raffinate after the desorption of Analytic Tower 1 is squeezed into second level Analytic Tower 2 through the second pump 12 and is further desorbed, the chlorination desorbed
Hydrogen enters together with the tail gas that first grade absorption tower 7 comes out from 8 lower part of two-level absorption tower after the condensation of B-grade condensation tower 5,
The flow rate for controlling the second spray head 19 is 15-25ml/min, passes through low concentration of salt acid solution caused 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 the desorption of second level Analytic Tower 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, is evaporated
For the hydrogen chloride and water vapour that device 3 generates by steam condensing tower 6, condensed water vapour is cold from the bottom of steam condensing tower 6
Condensate outlet pipe 28 is discharged, and the tail gas of hydrogen chloride gas and two-level absorption tower 8 enters recovery tower 9 together, by third spray head 20
The sodium hydrate aqueous solution of ejection neutralizes, and the liquid after neutralization is discharged from waste liquid discharge pipe 27, and gas is discharged from blow valve 24.
Advantages of the present invention:
The present invention using magnesium chloride as strippant, and by two-stage desorption, two-stage absorb, level-one recycling method carry out it is dilute
Hydrochloric acid enrichment, equipment is simple, and the rate of recovery is high, and Matter Transfer uses, and after abraum salt aqueous acid enrichment, realizes waste hydrochloric acid zero-emission
It puts, environmental protection.
Detailed description of the invention
Fig. 1 is a kind of thickening device structural schematic diagram of low concentration waste hydrochloric acid of the invention.
Specific embodiment
The present invention is further illustrated in the following with reference to the drawings and specific embodiments.
A kind of thickening device of low concentration waste hydrochloric acid is shown in that Fig. 1, liquid pool 10 successively pump 11 with first by pipeline, level-one
Analytic Tower 1, level-one condensing tower 4 are connected with the lower part of first grade absorption tower 7, and the lower part of first grade absorption tower 7 is by pipeline successively with the
Five pumps 21, product collecting tank 23 connect, and product collecting tank 23 passes through the first spray of pipeline and 7 internal upper part of first grade absorption tower respectively
First 18, the second spray head 19 connection of 8 internal upper part of two-level absorption tower；The lower part of level-one Analytic Tower 1 is connected with the first reboiler 15；
The bottom of level-one Analytic Tower 1 successively pumps 12, second level Analytic Tower 2, B-grade condensation tower 5 and two-level absorption tower 8 with second by pipeline
Lower part connection, the lower part of two-level absorption tower 8 by pipeline with the 6th pump 22 connect after again respectively with 7 internal upper part of first grade absorption tower
8 internal upper part of the first spray head 18 and two-level absorption tower the second spray head 19 connection；The lower part of second level Analytic Tower 2 is connected with
The bottom of two reboilers 16, second level Analytic Tower 2 successively pumps 13, evaporator 3, steam condensing tower 6 and recycling by pipeline with third
The bottom of tower 9 connects, and the top of recovery tower 9 is provided with blow valve 24, and 9 internal upper part of recovery tower is provided with third spray head 20,
Third spray head 20 is connect with alkali liquor pipe 25；The lower part of evaporator 3 is connected with third reboiler 17, and the bottom of evaporator 3 passes through
Pipeline is connect after connecting with the 4th pump 14 with liquid pool 10；Cooling water pipe 26 successively with level-one condensing tower 4,5 He of B-grade condensation tower
Steam condensing tower 6 connects；The top of first grade absorption tower 7 is connect by pipeline with the lower part of two-level absorption tower 8, two-level absorption tower 8
Top connect with the lower part of recovery tower 9 by pipeline, the lower part 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, includes the following steps:
(1) using a kind of thickening device of low concentration waste hydrochloric acid；
(2) magnesium chloride brine that mass percentage 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 within the scope of 5%-20% and matched
In liquid bath 10, adjusting the volume ratio of magnesium chloride brine and abraum salt aqueous acid in liquid pool 10 is 1:1；
(4) it by the mixed liquor in liquid pool 10, is driven into level-one Analytic Tower 1 through the first pump 11, 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 partial pressure increases, to change hydrochloric acid-water group
/ relative volatility, increase hydrochloric acid-aqueous systems constant boiling point, reduce the saturated vapour pressure of solution, be more advantageous to
The desorption of hydrogen chloride gas；The hydrogen chloride gas that level-one Analytic Tower 1 parses is after the condensation of level-one condensing tower 4 from first order absorption
The lower part of tower 7 enters in first grade absorption tower 7；The temperature of the cooling water of level-one condensing tower 4 is 5-20 DEG C, adjusts product collecting tank 23
Flow, make the flow rate 15-25ml/min of the first spray head 18 of 7 internal upper part of first grade absorption tower, in 7 tower top of first grade absorption tower
It is absorbed in a manner of spraying, the hydrochloric acid solution generated by first grade absorption tower 7, squeezes into product collecting tank 23 through the 5th pump 21 and followed
Ring spray-absorption and product are collected；Hydrochloric acid raffinate after the desorption of level-one Analytic Tower 1 squeezes into second level Analytic Tower 2 through the second pump 12
It is 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
Enter together from 8 lower part of two-level absorption tower, the flow rate of the second spray head 19 of control is 15-25ml/min, in 8 tower of two-level absorption tower
Top is absorbed in a manner of spraying, and by low concentration of salt acid solution caused by two-level absorption tower 8, squeezes into first respectively through the 6th pump 22
Spray head 18 and the second spray head 19；Through second level Analytic Tower 2 desorption after hydrochloric acid raffinate, with third pump 13 squeeze into evaporator 3 into
Row is concentrated by evaporation, and 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 generates
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 enters recovery tower 9 together, the sodium hydrate aqueous solution sprayed by third spray head 20
It neutralizes, the liquid after neutralization is discharged from waste liquid discharge pipe 27, and gas is discharged from blow valve 24.
Embodiment 2
A kind of thickening method of low concentration waste hydrochloric acid, includes the following steps:
(1) using a kind of thickening device of low concentration waste hydrochloric acid；
(2) magnesium chloride brine that mass percentage 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 within the scope of 5%-20% and matched
In liquid bath 10, adjusting the volume ratio of magnesium chloride brine and abraum salt aqueous acid in liquid pool 10 is 0.8:1；
(4) it by the mixed liquor in liquid pool 10, is driven into level-one Analytic Tower 1 through the first pump 11, 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 partial pressure increases, to change hydrochloric acid-water group
/ relative volatility, increase hydrochloric acid-aqueous systems constant boiling point, reduce the saturated vapour pressure of solution, be more advantageous to
The desorption of hydrogen chloride gas；The hydrogen chloride gas that level-one Analytic Tower 1 parses is after the condensation of level-one condensing tower 4 from first order absorption
The lower part of tower 7 enters in first grade absorption tower 7；The temperature of the cooling water of level-one condensing tower 4 is 5-20 DEG C, adjusts product collecting tank 23
Flow, make the flow rate 15-25ml/min of the first spray head 18 of 7 internal upper part of first grade absorption tower, in 7 tower top of first grade absorption tower
It is absorbed in a manner of spraying, the hydrochloric acid solution generated by first grade absorption tower 7, squeezes into product collecting tank 23 through the 5th pump 21 and followed
Ring spray-absorption and product are collected；Hydrochloric acid raffinate after the desorption of level-one Analytic Tower 1 squeezes into second level Analytic Tower 2 through the second pump 12
It is 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
Enter together from 8 lower part of two-level absorption tower, the flow rate of the second spray head 19 of control is 15-25ml/min, in 8 tower of two-level absorption tower
Top is absorbed in a manner of spraying, and by low concentration of salt acid solution caused by two-level absorption tower 8, squeezes into first respectively through the 6th pump 22
Spray head 18 and the second spray head 19；Through second level Analytic Tower 2 desorption after hydrochloric acid raffinate, with third pump 13 squeeze into evaporator 3 into
Row is concentrated by evaporation, and 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 generates
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 enters recovery tower 9 together, the sodium hydrate aqueous solution sprayed by third spray head 20
It neutralizes, the liquid after neutralization is discharged from waste liquid discharge pipe 27, and gas is discharged from blow valve 24.
Embodiment 3
A kind of thickening method of low concentration waste hydrochloric acid, includes the following steps:
(1) using a kind of thickening device of low concentration waste hydrochloric acid；
(2) magnesium chloride brine that mass percentage 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 within the scope of 5%-20% and matched
In liquid bath 10, adjusting the volume ratio of magnesium chloride brine and abraum salt aqueous acid in liquid pool 10 is 0.9:1；
(4) it by the mixed liquor in liquid pool 10, is driven into level-one Analytic Tower 1 through the first pump 11, 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 partial pressure increases, to change hydrochloric acid-water component
Between relative volatility, increase hydrochloric acid-aqueous systems constant boiling point, reduce the saturated vapour pressure of solution, be more advantageous to chlorine
Change the desorption of hydrogen；The hydrogen chloride gas that level-one Analytic Tower 1 parses is after the condensation of level-one condensing tower 4 from first grade absorption tower
7 lower part enters in first grade absorption tower 7；The temperature of the cooling water of level-one condensing tower 4 is 5-20 DEG C, adjusts product collecting tank 23
Flow makes the flow rate 15-25ml/min of the first spray head 18 of 7 internal upper part of first grade absorption tower, 7 tower top of first grade absorption tower with
Spray mode absorbs, the hydrochloric acid solution generated by first grade absorption tower 7, squeezes into product collecting tank 23 through the 5th pump 21 and is recycled
Spray-absorption and product are collected；Through level-one Analytic Tower 1 desorption after hydrochloric acid raffinate, through second pump 12 squeeze into second level Analytic Tower 2 into
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 8 lower part of two-level absorption tower, the flow rate of the second spray head 19 of control is 15-25ml/min, in 8 tower top of two-level absorption tower
It is absorbed in a manner of spraying, by low concentration of salt acid solution caused by two-level absorption tower 8, squeezes into the first spray respectively through the 6th pump 22
Drench head 18 and the second spray head 19；Hydrochloric acid raffinate after the desorption of second level Analytic Tower 2 is squeezed into evaporator 3 with third pump 13 and is carried 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 generates steam
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 enters recovery tower 9 together, in the sodium hydrate aqueous solution sprayed by third spray head 20
With liquid after neutralization is discharged from waste liquid discharge pipe 27, and gas is discharged from blow valve 24.
Claims (2)
1. a kind of thickening device of low concentration waste hydrochloric acid, it is characterised in that liquid pool (10) is successively pumped with first by pipeline
(11), level-one Analytic Tower (1), level-one condensing tower (4) are connected with the lower part of first grade absorption tower (7), the lower part of first grade absorption tower (7)
It is successively connect with the 5th pump (21), product collecting tank (23) by pipeline, product collecting tank (23) passes through pipeline and level-one 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；Level-one
The lower part of Analytic Tower (1) is connected with the first reboiler (15)；The bottom of level-one Analytic Tower (1) is successively pumped with second by pipeline
(12), second level Analytic Tower (2), B-grade condensation tower (5) are connect with the lower part of two-level absorption tower (8), the lower part of two-level absorption tower (8)
It is inhaled respectively with first spray head (18) of first grade absorption tower (7) internal upper part and second level again after being connect by pipeline with the 6th pump (22)
Receive the second spray head (19) connection of tower (8) internal upper part；The lower part of second level Analytic Tower (2) is connected with the second reboiler (16), and two
The bottom of grade Analytic Tower (2) successively pumps (13), evaporator (3), steam condensing tower (6) and recovery tower (9) with third by pipeline
Bottom connection, be provided with blow valve (24) at the top of recovery tower (9), recovery tower (9) internal upper part is provided with third spray head
(20), third spray head (20) is connect with alkali liquor pipe (25)；The lower part of evaporator (3) is connected with third reboiler (17), evaporation
The bottom of device (3) is connect after being connect by pipeline with the 4th pump (14) with liquid pool (10)；Cooling water pipe (26) successively with level-one
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 second level
The lower part on absorption tower (8) connects, and the top of two-level absorption tower (8) is connect by pipeline with the lower part of recovery tower (9), recovery tower
(9) lower part 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 including the following steps:
(1) using a kind of thickening device of low concentration waste hydrochloric acid of claim 1；
(2) magnesium chloride brine that mass percentage 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 within the scope of 5%-20% and matches liquid
In slot (10), the volume ratio of the interior magnesium chloride brine of adjustment liquid pool (10) and abraum salt aqueous acid is in the range of 0.8-1:1；
(4) it by the mixed liquor in liquid pool (10), is driven into level-one Analytic Tower (1) through the first pump (11), is warming up to 105-120
DEG C, parsing balance 80-130min, the hydrogen chloride gas that level-one Analytic Tower (1) parses by level-one condensing tower (4) condensation after from
The lower part of first grade absorption tower (7) enters in first grade absorption tower (7)；The temperature of the cooling water of level-one condensing tower (4) is 5-20 DEG C, is adjusted
The flow for saving product collecting tank (23), makes the flow rate 15-25ml/ of first spray head (18) of first grade absorption tower (7) internal upper part
Min, the hydrochloric acid solution generated by first grade absorption tower (7) squeeze into product collecting tank (23) through the 5th pump (21) and carry out circulation spray
Leaching absorbs and product is collected；Hydrochloric acid raffinate after level-one Analytic Tower (1) desorption squeezes into second level Analytic Tower through the second pump (12)
(2) it is further desorbed, the hydrogen chloride gas desorbed goes out after B-grade condensation tower (5) condense with first grade absorption tower (7)
The tail gas come enters from two-level absorption tower (8) lower part together, and the flow rate of control the second spray head (19) is 15-25ml/min, leads to
Low concentration of salt acid solution caused by two-level absorption tower (8) is crossed, squeezes into the first spray head (18) and the respectively through the 6th pump (22)
Two spray heads (19)；Hydrochloric acid raffinate after second level Analytic Tower (2) desorption, squeezes into evaporator (3) with third pump (13) and is steamed
Hair concentration, by the solution after evaporation and concentration through the 4th pump (14) squeeze into liquid pool (10), evaporator (3) generate 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) enters recovery tower (9) together, is sprayed by third spray head (20)
Sodium hydrate aqueous solution neutralizes, and the liquid after neutralization is discharged from waste liquid discharge pipe (27), and gas is discharged from blow 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 CN107161950A (en) | 2017-09-15 |
| CN107161950B true 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) |
Families Citing this family (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 |
Family Cites Families (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 |
| AT403698B (en) * | 1995-11-27 | 1998-04-27 | Andritz Patentverwaltung | METHOD FOR RECOVERY OR RECOVERY OF ACIDS FROM METAL SOLUTIONS OF THESE ACIDS |
| CN100460312C (en) * | 2006-09-20 | 2009-02-11 | 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
Also Published As
| Publication number | Publication date |
|---|---|
| CN107161950A (en) | 2017-09-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102210964B (en) | Gas phase silicon dioxide tail gas treatment process and system | |
| CN103285614A (en) | Gas-phase rectifying method for steam containing ammonia in APT (ammonium paratungstate) production process and equipment | |
| CN104437055A (en) | A negative pressure ammonia distillation process and equipment for deammonization treatment of ammonia vapor before the vacuum pump | |
| CN106673012B (en) | A process and device for producing concentrated ammonia water by negative pressure operation | |
| CN102757019A (en) | System and method for concentrating and purifying hydrogen peroxide | |
| CN110606470B (en) | Device for concentrating, resolving and producing hydrogen chloride from hydrochloric acid | |
| CN107161950B (en) | A kind of thickening device and method of low concentration waste hydrochloric acid | |
| 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 | |
| CN208130543U (en) | The de- analysis purification device of hydrogen chloride in a kind of chloroethanes production process | |
| CN107311884A (en) | DMF wastewater treatments energy saving technique and device that a kind of low pressure heat pump distillation is combined with double-effect rectification | |
| CN109647160B (en) | Method for treating tail gas of ammonium sulfate mother liquor circulation tank | |
| CN108658095A (en) | The energy-saving reclaiming process and system that a kind of ammonium hydroxide recycling concentration is easily adjusted | |
| CN113457381A (en) | Energy-saving process for capturing and recovering carbon dioxide from chimney exhaust gas | |
| CN106966865A (en) | The system that a kind of technique in three-effect countercurrent evaporation rectification process handles glycine crystallization mother liquid | |
| CN106966869B (en) | System for four-effect evaporation rectification process handles glycine mother liquor | |
| CN107792904A (en) | A kind of technique and device of continuous removal of ammonia and nitrogen light component organic matter and salt | |
| CN114436293B (en) | Method for directly producing sodium bromide from low-concentration brine | |
| CN217264857U (en) | Concentration and reuse device for chlorine gas drying waste acid | |
| CN215249583U (en) | Waste acid concentration regeneration sulfuric acid production line | |
| CN211946257U (en) | Hydrochloric acid deep analysis system | |
| CN206244421U (en) | A device for producing concentrated ammonia water by negative pressure operation | |
| CN207002611U (en) | The DMF wastewater treatment energy savers that a kind of low pressure heat pump distillation is combined with double-effect rectification | |
| CN206476756U (en) | A device for producing concentrated ammonia water by negative pressure operation | |
| 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 |