CN109795991A - Safe and energy-saving purification treatment process for fluorosulfuric acid - Google Patents
Safe and energy-saving purification treatment process for fluorosulfuric acid Download PDFInfo
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- CN109795991A CN109795991A CN201910287526.5A CN201910287526A CN109795991A CN 109795991 A CN109795991 A CN 109795991A CN 201910287526 A CN201910287526 A CN 201910287526A CN 109795991 A CN109795991 A CN 109795991A
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- 238000000034 method Methods 0.000 title claims abstract description 45
- 238000000746 purification Methods 0.000 title claims abstract description 21
- 230000008569 process Effects 0.000 title claims abstract description 19
- UQSQSQZYBQSBJZ-UHFFFAOYSA-N fluorosulfonic acid Chemical compound OS(F)(=O)=O UQSQSQZYBQSBJZ-UHFFFAOYSA-N 0.000 title 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims abstract description 242
- KRHYYFGTRYWZRS-UHFFFAOYSA-N Fluorane Chemical compound F KRHYYFGTRYWZRS-UHFFFAOYSA-N 0.000 claims abstract description 80
- 229910000040 hydrogen fluoride Inorganic materials 0.000 claims abstract description 50
- 239000002253 acid Substances 0.000 claims abstract description 37
- 238000002156 mixing Methods 0.000 claims abstract description 36
- 229910052731 fluorine Inorganic materials 0.000 claims abstract description 26
- 239000011737 fluorine Substances 0.000 claims abstract description 26
- 239000007789 gas Substances 0.000 claims abstract description 22
- 238000010521 absorption reaction Methods 0.000 claims abstract description 21
- 239000002994 raw material Substances 0.000 claims abstract description 19
- 238000001704 evaporation Methods 0.000 claims abstract description 11
- 230000008020 evaporation Effects 0.000 claims abstract description 10
- 235000011149 sulphuric acid Nutrition 0.000 claims description 32
- 239000001117 sulphuric acid Substances 0.000 claims description 32
- YCKRFDGAMUMZLT-UHFFFAOYSA-N Fluorine atom Chemical compound [F] YCKRFDGAMUMZLT-UHFFFAOYSA-N 0.000 claims description 25
- 239000000463 material Substances 0.000 claims description 14
- 238000010025 steaming Methods 0.000 claims description 9
- 230000002745 absorbent Effects 0.000 claims description 8
- 239000002250 absorbent Substances 0.000 claims description 8
- 238000010926 purge Methods 0.000 claims description 8
- 239000010959 steel Substances 0.000 claims description 8
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 claims description 7
- 229910010271 silicon carbide Inorganic materials 0.000 claims description 7
- 229910000831 Steel Inorganic materials 0.000 claims description 6
- 229910052739 hydrogen Inorganic materials 0.000 claims description 4
- 239000001257 hydrogen Substances 0.000 claims description 4
- 239000012141 concentrate Substances 0.000 claims description 3
- 229910000976 Electrical steel Inorganic materials 0.000 claims description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims 1
- 239000005864 Sulphur Substances 0.000 claims 1
- 238000003682 fluorination reaction Methods 0.000 claims 1
- 238000009833 condensation Methods 0.000 abstract description 6
- 230000005494 condensation Effects 0.000 abstract description 6
- PXGOKWXKJXAPGV-UHFFFAOYSA-N Fluorine Chemical compound FF PXGOKWXKJXAPGV-UHFFFAOYSA-N 0.000 abstract 1
- 238000006115 defluorination reaction Methods 0.000 abstract 1
- 238000005406 washing Methods 0.000 abstract 1
- 239000000872 buffer Substances 0.000 description 6
- 238000012545 processing Methods 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000000605 extraction Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000003860 storage Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910003978 SiClx Inorganic materials 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000010924 continuous production Methods 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000011549 displacement method Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 210000001035 gastrointestinal tract Anatomy 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000002085 irritant Substances 0.000 description 1
- 231100000021 irritant Toxicity 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 210000004400 mucous membrane Anatomy 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 210000002345 respiratory system Anatomy 0.000 description 1
- 210000003491 skin Anatomy 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000001228 spectrum Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Abstract
The invention discloses a safe and energy-saving purification treatment process of sulfuric acid containing fluorine, which comprises a preheating evaporation section, a mixing removal section and a sulfuric acid concentration section; the preheating evaporation section evaporates the raw material acid under vacuum condition to increase the concentration of sulfuric acid, the concentrated sulfuric acid is sent to the mixing removal section, and hydrogen fluoride steam generated in the evaporation process enters a hydrogen fluoride absorption tower; the mixed removal section sends the sulfuric acid from the preheating evaporation section and the sulfuric acid from the sulfuric acid concentration section to a removal rectifying tower, hydrogen fluoride contained in the sulfuric acid is removed in a mixed manner, the sulfuric acid after defluorination is sent to the sulfuric acid concentration section, and hydrogen fluoride steam generated in the removal process enters a hydrogen fluoride absorption tower; and the sulfuric acid concentration section sends concentrated sulfuric acid from the mixing and removing section to a sulfuric acid concentrator, the concentration of the sulfuric acid is increased under a high vacuum condition, one part of the obtained high-concentration sulfuric acid is continuously extracted out of the system, the other part of the obtained high-concentration sulfuric acid is sent back to the mixing and removing section to be mixed, and tail gas enters a tail gas condensation tower and a gas washing tower and is discharged after reaching the standard.
Description
Technical field
The present invention relates to chemical industry post-processing field more particularly to a kind of purified treatment works of the fluorine-containing sulfuric acid of energy-saving safe
Skill.
Background technique
Hydrogen fluoride, a kind of gas of colourless irritant smell, itself and its toxic and very strong corruption of aqueous solution
Corrosion can penetrate skin, mucous membrane, respiratory tract and gastrointestinal tract, generate strong impulse, corrosion to these positions, can cause
Human body is burnt.Existing hydrogen fluoride recovery process mostly uses concentrated sulfuric acid displacement method, therefore generates a large amount of fluorine-containing waste sulfuric acids, it is extremely difficult to
Processing, huge environmental protection treatment cost can be not only brought to enterprise, will also result in great pollution to environment.
For above situation, the present invention provides a kind of purification process technique of the fluorine-containing sulfuric acid of energy-saving safe, can be by conduct
The hydrofluoric acid of impurity is separated with sulfuric acid, while dilute sulfuric acid being concentrated as the concentrated sulfuric acid, is absorbed in concentration process and is produced by absorption system
Raw steam, reduce exhaust emissions, improve recovery efficiency, method is simple, can continuous production, separation and concentrated effect it is good, operation
While enhancement of environment, operating cost is saved, system is run under negative pressure, and safe and stable, energy-saving and environmental protection do not generate secondary dirt
Dye.
Summary of the invention
In order to solve the above-mentioned technical problems, the present invention provides a kind of purified treatment works of the fluorine-containing sulfuric acid of energy-saving safe
Skill comprising preheating evaporator section, mixing removing section and sulphuric acid concentration section；
The preheating evaporator section evaporates raw material acid under vacuum conditions, promotes sulfuric acid concentration, and the sulfuric acid after concentrate is sent into
Mixing removes section, and the hydrogen fluoride steam generated in evaporation process enters hydrogen fluoride absorption tower；
Sulfuric acid from preheating evaporator section and the sulfuric acid from sulphuric acid concentration section are sent into removing essence by the mixing removing section
Tower, hydrogen fluoride contained in mixing removing sulfuric acid are evaporated, the sulfuric acid after defluorinate is sent into sulphuric acid concentration section, is generated in subtractive process
Hydrogen fluoride steam enters hydrogen fluoride absorption tower；
The concentrated sulfuric acid from mixing removing section is sent into sulphuric acid concentration device by the sulphuric acid concentration section, is mentioned in high vacuum conditions
Sulfuric acid concentration is risen, obtained high-concentration sulfuric acid a part is continuously produced system, and another part sends mixing removing section mixing, tail back to
Gas enters tail gas condensing tower, air purge tower, discharges after up to standard.
As a kind of perferred technical scheme, the preheating evaporator section includes preheater and pre- steaming evaporator.
As a kind of perferred technical scheme, the material of the preheater is silicon carbide, and the pre- material for steaming evaporator is carbon
SiClx or steel are sintered tetrafluoro.
As a kind of perferred technical scheme, the sulfuric acid concentration of the raw material acid is 30~40wt%, and hydrogen fluoride concentration is
10~20wt%.
As a kind of perferred technical scheme, the concentration of raw material acid is promoted to 80~88wt% by the preheating evaporator section.
As a kind of perferred technical scheme, the hydrogen fluoride absorption tower converts hydrogen fluorine for hydrogen fluoride by condensed absorbent
Acid.
As a kind of perferred technical scheme, sulfuric acid concentration is promoted to 90~95wt% by the sulphuric acid concentration section.
As a kind of perferred technical scheme, the sulfuric acid concentration of the mixing removing section is 88~90wt%.
As a kind of perferred technical scheme, the material of the removing rectifying column is that steel is sintered tetrafluoro.
As a kind of perferred technical scheme, the material of the sulphuric acid concentration device is silicon carbide.
The utility model has the advantages that the present invention provides a kind of purification process technique of the fluorine-containing sulfuric acid of energy-saving safe, impurity can will be used as
Hydrofluoric acid separated with sulfuric acid, while dilute sulfuric acid being concentrated as the concentrated sulfuric acid, passes through absorption system and absorb and generated in concentration process
Steam, reduce exhaust emissions, improve recovery efficiency, method is simple, can continuous production, separation and concentrated effect it is good, operating environment
While improvement, operating cost is saved, system is run under negative pressure, and safe and stable, energy-saving and environmental protection do not generate secondary pollution.
Detailed description of the invention
In order to further explain energy-saving safe provided in the present invention fluorine-containing sulfuric acid purification process technique process,
Provide corresponding attached drawing, it is pointed out that attached drawing provided in the present invention be elected in all attached drawings individually show
Example, purpose are also not as limitations on the claims, all other corresponding figures obtained by attached drawing provided herein
Spectrum is it is believed that within the scope of the application protection
Fig. 1 is the flow chart of the purification process technique of the fluorine-containing sulfuric acid of the energy-saving safe.
Specific embodiment
The contents of the present invention can be further understood that in conjunction with the detailed description of preferred implementation method of the invention below.Unless otherwise
Illustrate, all technologies used herein and scientific term all have the usual reason with the application one skilled in the art
Solve identical meaning.If defining for the concrete term disclosed in the prior art is different with any definition provided herein
It causes, then term provided herein of being subject to defines.
It is used in the present context, unless being clearly dictated in context, otherwise without the spy of the single plural form of restriction
Sign is also intended to the feature including plural form.Will also be appreciated that term "comprising" as used herein, with " comprising ", " including
Have ", " having ", "comprising" and/or " including " etc. it is synonymous, indicate when used in this manual stated composition,
Step, method, product or device, but do not preclude the presence or addition of one or more of the other composition, step, method, product or
Device.In addition, use " preferred ", " preferably ", " preferred " etc. to refer to when describing presently filed embodiment,
It can provide the embodiment of the present invention of certain beneficial effects in some cases.However, under identical circumstances or in the case of other,
Other embodiments are also likely to be preferred.In addition to this, it is not implied that the statement of one or more preferred embodiments
His embodiment is unavailable, is also not intended to exclude other embodiments except the scope of the present invention.
The meaning of heretofore described "and/or" refers to that the case where respective individualism or both exists simultaneously wraps
Including including.
The meaning of heretofore described " inside and outside " refers to relative to equipment itself, the side inside sensing equipment
To in, on the contrary is outer, rather than the specific restriction to the device of the invention mechanism.
When the meaning of heretofore described " left and right " refers to reader's face attached drawing, the left side of reader is a left side,
The right of reader is the right side, rather than the specific restriction to the device of the invention mechanism.
The meaning of heretofore described " connection " can be between component be directly connected to be also possible to pass through between component
Other component is indirectly connected with.
The present invention provides a kind of purification process technique of the fluorine-containing sulfuric acid of energy-saving safe comprising preheating evaporator section, mixing
Remove section and sulphuric acid concentration section；
The preheating evaporator section evaporates raw material acid under vacuum conditions, promotes sulfuric acid concentration, and the sulfuric acid after concentrate is sent into
Mixing removes section, and the hydrogen fluoride steam generated in evaporation process enters hydrogen fluoride absorption tower；
Sulfuric acid from preheating evaporator section and the sulfuric acid from sulphuric acid concentration section are sent into removing essence by the mixing removing section
Tower, hydrogen fluoride contained in mixing removing sulfuric acid are evaporated, the sulfuric acid after defluorinate is sent into sulphuric acid concentration section, is generated in subtractive process
Hydrogen fluoride steam enters hydrogen fluoride absorption tower；
The concentrated sulfuric acid from mixing removing section is sent into sulphuric acid concentration device by the sulphuric acid concentration section, is mentioned in high vacuum conditions
Sulfuric acid concentration is risen, obtained high-concentration sulfuric acid a part is continuously produced system, and another part sends mixing removing section mixing, tail back to
Gas enters tail gas condensing tower, air purge tower, discharges after up to standard.
With reference to the accompanying drawing 1, the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe of the present invention is carried out specifically
It is bright.
Preheat evaporator section
It includes preheater and pre- steaming evaporator that the capital equipment in evaporator section is preheated in the application, and raw material acid passes through feed pump
It is continuously sent through elevated dosing vessel to preheater and is preheated by storage tank.
In some preferred embodiments, the inlet amount of the raw material acid is 850 kgs/hour, sulfuric acid concentration 30
~40wt%, hydrogen fluoride concentration are 10~20wt%.
In some preferred embodiments, the material of the preheater is silicon carbide, and operating pressure is normal pressure, shell side temperature
Degree is 90~95 DEG C, and tube side temperature is 25~60 DEG C.
Raw material acid after preheating enters pre- steaming evaporator, most of water is sloughed herein under vacuum condition, after improving concentration
Sulfuric acid gravity flow enters mixing removing section, and the hydrogen fluoride steam generated in evaporation process enters hydrogen fluoride absorption tower, after condensed absorbent
Obtained hydrofluoric acid is collected to hydrofluoric acid buffer tank, remains to be further processed.
In some preferred embodiments, the pre- material for steaming evaporator is that silicon carbide or steel are sintered tetrafluoro, operation
Pressure is 0.012MPa, and running temperature is 140~160 DEG C.
In some preferred embodiments, the concentration of raw material acid is promoted to 80~88wt% by the preheating evaporator section；
It is further preferred that the concentration of raw material acid is promoted to 86~88wt% by the preheating evaporator section.
In some preferred embodiments, the hydrogen fluoride absorption tower passes through condensation concentration hydrogen fluoride；Further preferably
, hydrogen fluoride is concentrated by multiple condensation in the hydrogen fluoride absorption tower.
In some preferred embodiments, the material on the hydrogen fluoride absorption tower is steel lining tetrafluoro, and operating pressure is normal
Pressure, running temperature are not higher than 40 DEG C.
Mixing removing section
The capital equipment of mixing removing section is removing rectifying column in the application, from preheating evaporator section and sulphuric acid concentration section
Sulfuric acid mixes herein, and sulfuric acid is sufficiently separated with hydrogen fluoride in the case where high-temperature and high concentration, and the sulfuric acid after separation flows into sulphuric acid concentration
Section, hydrogen fluoride steam enters hydrogen fluoride absorption tower, and the hydrofluoric acid obtained after condensed absorbent is collected to hydrofluoric acid buffer tank, remain into
The processing of one step.
In some preferred embodiments, the sulfuric acid concentration of the mixing removing section is 88~90wt%.
In some preferred embodiments, the material of the removing rectifying column is that steel is sintered tetrafluoro, and operating pressure is normal
Pressure, running temperature are not higher than 150 DEG C.
Sulphuric acid concentration section
The capital equipment of sulphuric acid concentration section includes sulphuric acid concentration device, concentrated acid cooler, tail gas condensing tower, air purge in the application
Tower.After sulfuric acid from removing destilling tower is concentrated in high vacuum conditions, a part enters concentrated acid cooler by continuous extraction, cold
But the concentrated sulfuric acid after is transferred to finished acid tank by finished acid pump, and another part is back to mixing removing section to improve the dense of wherein sulfuric acid
Degree.The tail gas generated in concentration process enters tail gas condensing tower, and remaining gas enters air purge tower after condensation, after processing is up to standard again
Row discharge.
In some preferred embodiments, sulfuric acid concentration is promoted to 90~95wt% by the sulphuric acid concentration section；Into one
Step is preferred, and sulfuric acid concentration is promoted to 91~94wt% by the sulphuric acid concentration section.
In some preferred embodiments, the sulphuric acid concentration device, concentrated acid cooler, tail gas condensing tower material be carbon
SiClx, the material of the air purge tower are that steel is sintered tetrafluoro.
In some preferred embodiments, the operating pressure of the sulphuric acid concentration device is 0.008MPa, and running temperature is
170~190 DEG C.
In some preferred embodiments, the operating pressure of the concentrated acid cooler is 0.008MPa, and uneven shell-side temperature is
25~35 DEG C, tube side temperature is 50~180 DEG C.
In the embodiment of some pre-selections, the operating pressure of the tail gas condensing tower is 0.008MPa, and running temperature is not
More than 120 DEG C.
Embodiment
Technical solution of the present invention is described in detail by the following examples, but protection scope of the present invention is not limited to
In the embodiment.
Embodiment 1
Embodiment 1 provides a kind of purification process technique of the fluorine-containing sulfuric acid of energy-saving safe comprising following steps:
A. preheat evaporator section: raw material acid is continuously sent to preheater through elevated dosing vessel by storage tank by feed pump and is carried out in advance
Heat, the uneven shell-side temperature of preheater are 90 DEG C, and tube side temperature is 40 DEG C.Sulfuric acid content is 35wt%, hydrogen fluoride in the raw material acid
Content is 16wt%, and inlet amount is 850 kgs/hour, i.e., 20 ton/days.Raw material acid after preheating enters pre- steaming evaporator, is pressing
Most of water is sloughed under power 0.012MPa, 150 DEG C of temperature of service condition, gravity flow enters mixed after sulfuric acid concentration is improved to 85wt%
Removing section is closed, the hydrogen fluoride steam generated in evaporation process enters hydrogen fluoride absorption tower, and the hydrofluoric acid obtained after condensed absorbent is received
Collection remains to be further processed to hydrofluoric acid buffer tank.
B. mixing removes section: the sulfuric acid from preheating evaporator section and sulphuric acid concentration section is mixed to get concentration in removing destilling tower
For the sulfuric acid of 88wt%, sulfuric acid is sufficiently separated with hydrogen fluoride under conditions of high-temperature and high concentration, and it is dense that the sulfuric acid after separation flows into sulfuric acid
Contracting section, hydrogen fluoride steam enter hydrogen fluoride absorption tower, and the hydrofluoric acid obtained after condensed absorbent is collected to hydrofluoric acid buffer tank, remained
It is further processed.
C. sulphuric acid concentration section: the sulfuric acid from removing destilling tower is sent to sulphuric acid concentration device, in pressure 0.008MPa, temperature
After being concentrated into 93wt% under 180 DEG C of service condition, a part is sent into concentrated acid cooler, the fortune of concentrated acid cooler by continuous extraction
Row pressure is 0.008MPa, uneven shell-side temperature is 25 DEG C, tube side temperature is 100 DEG C, and the concentrated sulfuric acid after cooling is transferred to by finished acid pump
Finished acid tank, another part are back to mixing removing section to improve the concentration of wherein sulfuric acid.The tail gas generated in concentration process into
Enter tail gas condensing tower, remaining gas enters air purge tower after condensation, row discharge again after processing is up to standard.
After handling according to this example, the concentrated sulfuric acid of about 310 kilograms of 93wt%, 133 kilograms of 25wt% hydrogen fluorine can be produced per hour
Acid.
Embodiment 2
Embodiment 2 provides a kind of purification process technique of the fluorine-containing sulfuric acid of energy-saving safe comprising following steps:
A. preheat evaporator section: raw material acid is continuously sent to preheater through elevated dosing vessel by storage tank by feed pump and is carried out in advance
Heat, the uneven shell-side temperature of preheater are 95 DEG C, and tube side temperature is 50 DEG C.Sulfuric acid content is 35wt%, hydrogen fluoride in the raw material acid
Content is 16wt%, and inlet amount is 850 kgs/hour, i.e., 20 ton/days.Raw material acid after preheating enters pre- steaming evaporator, is pressing
Most of water is sloughed under power 0.012MPa, 160 DEG C of temperature of service condition, gravity flow enters mixed after sulfuric acid concentration is improved to 86wt%
Removing section is closed, the hydrogen fluoride steam generated in evaporation process enters hydrogen fluoride absorption tower, and the hydrofluoric acid obtained after condensed absorbent is received
Collection remains to be further processed to hydrofluoric acid buffer tank.
B. mixing removes section: the sulfuric acid from preheating evaporator section and sulphuric acid concentration section is mixed to get concentration in removing destilling tower
For the sulfuric acid of 89wt%, sulfuric acid is sufficiently separated with hydrogen fluoride under conditions of high-temperature and high concentration, and it is dense that the sulfuric acid after separation flows into sulfuric acid
Contracting section, hydrogen fluoride steam enter hydrogen fluoride absorption tower, and the hydrofluoric acid obtained after condensed absorbent is collected to hydrofluoric acid buffer tank, remained
It is further processed.
C. sulphuric acid concentration section: the sulfuric acid from removing destilling tower is sent to sulphuric acid concentration device, in pressure 0.008MPa, temperature
After being concentrated into 94wt% under 190 DEG C of service condition, a part enters concentrated acid cooler, the fortune of concentrated acid cooler by continuous extraction
Row pressure is 0.008MPa, uneven shell-side temperature is 35 DEG C, tube side temperature is 110 DEG C, and the concentrated sulfuric acid after cooling is transferred to by finished acid pump
Finished acid tank, another part are back to mixing removing section to improve the concentration of wherein sulfuric acid.The tail gas generated in concentration process into
Enter tail gas condensing tower, remaining gas enters air purge tower after condensation, row discharge again after processing is up to standard.
After handling according to this example, the concentrated sulfuric acid of about 300 kilograms of 94wt%, 127 kilograms of 25wt% hydrogen fluorine can be produced per hour
Acid.
Other changes within mentality of designing and protection scope of the invention, to above-mentioned specific embodiment or embodiment
Or modification is obvious to those skilled in the art.Although the present invention be control particular implementation or embodiment into
Row description, but the purpose of these embodiments or embodiment is illustration rather than is defined that correspondingly, this patent is not
It is only limitted to the range and effect of several particular implementations or embodiment described herein, is also not necessarily limited to and in the art by this hair
Bright acquired other inconsistent to a certain extent any modes that are in progress.
Claims (10)
1. a kind of purification process technique of the fluorine-containing sulfuric acid of energy-saving safe, which is characterized in that the technique include preheating evaporator section,
Mixing removing section and sulphuric acid concentration section；
The preheating evaporator section evaporates raw material acid under vacuum conditions, promotes sulfuric acid concentration, and the sulfuric acid after concentrate is sent into mixing
Section is removed, the hydrogen fluoride steam generated in evaporation process enters hydrogen fluoride absorption tower；
Sulfuric acid from preheating evaporator section and the sulfuric acid from sulphuric acid concentration section are sent into removing rectifying column by the mixing removing section,
Hydrogen fluoride contained in mixing removing sulfuric acid, the sulfuric acid after defluorinate are sent into sulphuric acid concentration section, the fluorination generated in subtractive process
Hydrogen steam enters hydrogen fluoride absorption tower；
The concentrated sulfuric acid from mixing removing section is sent into sulphuric acid concentration device by the sulphuric acid concentration section, promotes sulphur in high vacuum conditions
Acid concentration, obtained high-concentration sulfuric acid a part are continuously produced system, and another part sends mixing removing section mixing back to, tail gas into
Enter tail gas condensing tower, air purge tower, is discharged after up to standard.
2. the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe as described in claim 1, which is characterized in that the preheating is steamed
Sending out section includes preheater and pre- steaming evaporator.
3. the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe as claimed in claim 2, which is characterized in that the preheater
Material be silicon carbide, the pre- material for steaming evaporator is that silicon carbide or steel are sintered tetrafluoro.
4. the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe as described in claim 1, which is characterized in that the raw material acid
Sulfuric acid concentration be 30~40wt%, hydrogen fluoride concentration be 10~20wt%.
5. the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe as described in claim 1, which is characterized in that the preheating is steamed
It sends out section and the concentration of raw material acid is promoted to 80~88wt%.
6. the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe as described in claim 1, which is characterized in that the hydrogen fluoride
Absorption tower converts hydrofluoric acid for hydrogen fluoride by condensed absorbent.
7. the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe as described in claim 1, which is characterized in that the sulfuric acid is dense
Sulfuric acid concentration is promoted to 90~95wt% by contracting section.
8. the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe as described in claim 1, which is characterized in that the mixing is de-
Except the sulfuric acid concentration of section is 88~90wt%.
9. the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe as described in claim 1, which is characterized in that the removing essence
The material for evaporating tower is that steel is sintered tetrafluoro.
10. the purification process technique of the fluorine-containing sulfuric acid of energy-saving safe as described in claim 1, which is characterized in that the sulfuric acid
The material of inspissator is silicon carbide.
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| CN110812935A (en) * | 2019-09-30 | 2020-02-21 | 金川集团股份有限公司镍冶炼厂 | Device and process method for removing fluorine and chlorine in dilute acid purified by sulfuric acid |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110812935A (en) * | 2019-09-30 | 2020-02-21 | 金川集团股份有限公司镍冶炼厂 | Device and process method for removing fluorine and chlorine in dilute acid purified by sulfuric acid |
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| CN109795991B (en) | 2020-12-29 |
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