CN110127615A - Mannheim proeess produces the online purification process of hydrochloric acid in Process of Potassium Sulfate - Google Patents
Mannheim proeess produces the online purification process of hydrochloric acid in Process of Potassium Sulfate Download PDFInfo
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- CN110127615A CN110127615A CN201910380684.5A CN201910380684A CN110127615A CN 110127615 A CN110127615 A CN 110127615A CN 201910380684 A CN201910380684 A CN 201910380684A CN 110127615 A CN110127615 A CN 110127615A
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- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 title claims abstract description 220
- OTYBMLCTZGSZBG-UHFFFAOYSA-L potassium sulfate Chemical compound [K+].[K+].[O-]S([O-])(=O)=O OTYBMLCTZGSZBG-UHFFFAOYSA-L 0.000 title claims abstract description 26
- 229910052939 potassium sulfate Inorganic materials 0.000 title claims abstract description 26
- 235000011151 potassium sulphates Nutrition 0.000 title claims abstract description 26
- 238000000746 purification Methods 0.000 title claims abstract description 8
- 238000000034 method Methods 0.000 title claims description 26
- 239000007789 gas Substances 0.000 claims abstract description 77
- 238000010521 absorption reaction Methods 0.000 claims abstract description 38
- 229910000041 hydrogen chloride Inorganic materials 0.000 claims abstract description 36
- IXCSERBJSXMMFS-UHFFFAOYSA-N hydrogen chloride Substances Cl.Cl IXCSERBJSXMMFS-UHFFFAOYSA-N 0.000 claims abstract description 36
- 238000005201 scrubbing Methods 0.000 claims abstract description 27
- 238000002485 combustion reaction Methods 0.000 claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000001816 cooling Methods 0.000 claims abstract description 17
- 239000008367 deionised water Substances 0.000 claims abstract description 17
- 229910021641 deionized water Inorganic materials 0.000 claims abstract description 17
- 238000004519 manufacturing process Methods 0.000 claims abstract description 17
- 238000005406 washing Methods 0.000 claims abstract description 14
- 238000004140 cleaning Methods 0.000 claims abstract description 10
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 claims description 10
- 239000007788 liquid Substances 0.000 claims description 7
- 239000000498 cooling water Substances 0.000 claims 1
- 238000004821 distillation Methods 0.000 abstract description 10
- 239000002918 waste heat Substances 0.000 abstract description 5
- 239000002253 acid Substances 0.000 description 16
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 10
- 150000003467 sulfuric acid derivatives Chemical class 0.000 description 10
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 6
- 239000012535 impurity Substances 0.000 description 6
- 238000003860 storage Methods 0.000 description 6
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 4
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 description 2
- 239000000428 dust Substances 0.000 description 2
- 239000011591 potassium Substances 0.000 description 2
- 229910052700 potassium Inorganic materials 0.000 description 2
- 239000001103 potassium chloride Substances 0.000 description 2
- 235000011164 potassium chloride Nutrition 0.000 description 2
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000005660 chlorination reaction Methods 0.000 description 1
- 239000000460 chlorine Substances 0.000 description 1
- 229910052801 chlorine Inorganic materials 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000007654 immersion Methods 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/02—Preparation of sulfates from alkali metal salts and sulfuric acid or bisulfates; Preparation of bisulfates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D5/00—Sulfates or sulfites of sodium, potassium or alkali metals in general
- C01D5/06—Preparation of sulfates by double decomposition
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses the online purification process of hydrochloric acid in a kind of Mannheim proeess production Process of Potassium Sulfate, the gas come out from mannheim furnace is cooling through cooler, empties after then sequentially entering first grade scrubber, secondary scrubber, three-level film-falling absorption tower and level Four scrubbing tower；The cleaning solution that deionized water obtain after washing absorption to environmentally friendly tail gas sequentially enters secondary scrubber and first grade scrubber is washed, finally obtain hydrochloric acid B, hydrochloric acid B enters destilling tower and is distilled, the fraction distilled obtains food grade hydrochloric acid through cooling, deionized water washs the hydrogen chloride gas in level Four scrubbing tower, the gas distilled into three-level film-falling absorption tower absorbing hydrogen chloride gas and destilling tower enters three-level film-falling absorption tower and absorbs to obtain hydrochloric acid A；Destilling tower institute's calorific requirement is provided by the tail gas that the combustion chamber for providing heat for mannheim furnace generates.The present invention carries out distillation purifying, the hydrochloric acid of available food-grade to hydrochloric acid online using combustion chamber waste heat from tail gas.
Description
Technical field
The invention belongs to chemical fields, and in particular to a kind of Mannheim proeess produces the online purifying of hydrochloric acid in Process of Potassium Sulfate
Method.
Background technique
Mannheim proeess production potassium sulfate is to use sulfuric acid and potassium chloride in mannheim furnace, is reacted under the high temperature conditions,
Potassium sulfate is generated, and generates hydrogen chloride, hydrogen chloride is only absorbed by the water generation hydrochloric acid, is product after potassium sulfate is cooling.Mannheim proeess is
The method of the most stable of production potassium sulfate of technology most mature and reliable, quality so far.
But contain a small amount of vapor, sulfuric acid gas, potassium sulfate dust, chlorine in hydrogen chloride gas since Mannheim proeess generates
Change impurity, these impurity and the hydrogen chloride gas such as potassium dust to exist with mist, according to the technical method of current maturation (as schemed
1) the hydrochloric acid impurity content obtained after absorbing is high, and poor quality, purposes is limited, and enterprise even also needs in addition to go out expense to entrust
Other people consume use, bring certain economic loss for enterprise.
Summary of the invention
The present invention provides the online purification process of hydrochloric acid in a kind of Mannheim proeess production Process of Potassium Sulfate, can utilize Man Hai
Nurse method produces the combustion chamber waste heat from tail gas in Process of Potassium Sulfate and carries out distillation purifying to hydrochloric acid online, obtains the hydrochloric acid of food-grade.
The technical solution adopted by the present invention is that Mannheim proeess produces the online purification process of hydrochloric acid in Process of Potassium Sulfate,
It is characterized in that, comprising the following steps:
The gas come out from mannheim furnace is cooling through cooler, then sequentially enters first grade scrubber, secondary scrubber, three
It is emptied after grade film-falling absorption tower and level Four scrubbing tower；Deionized water to environmentally friendly tail gas carry out after washing absorption obtained cleaning solution according to
It is secondary to be washed into secondary scrubber and first grade scrubber, hydrochloric acid B is finally obtained, hydrochloric acid B enters destilling tower and distilled, and steams
It distillating the fraction come and obtains food grade hydrochloric acid through cooling, deionized water washs the hydrogen chloride gas in level Four scrubbing tower,
The gas distilled into three-level film-falling absorption tower absorbing hydrogen chloride gas and destilling tower enters the suction of three-level film-falling absorption tower
Receipts obtain hydrochloric acid A；Destilling tower institute's calorific requirement is provided by the tail gas that the combustion chamber for providing heat for mannheim furnace generates.The burning
For temperature between 245~295 DEG C, exhaust flow is 10~14m to the tail gas that room generates after cooler is cooling3/s。
Further, the environmentally friendly tail gas is the tail in the production environment collected in Mannheim proeess production Process of Potassium Sulfate
Gas.
Further, the raffinate part of destilling tower enters first grade scrubber as cleaning solution and carries out circulation washing.
Further, the hydrochloric acid B enters the flow of destilling tower and the flow-rate ratio that vinasse enters first grade scrubber is
2:1~4:1.
Further, when the concentration of sulfate in vinasse is more than 30wt%, raffinate is evaporated, residue is directly entered
Mannheim furnace produces potassium sulfate.
Further, the gas generated in mannheim furnace introduces cooler using the subsequent air-introduced machine of level Four scrubbing tower and carries out
It is cooling, then sequentially enter first grade scrubber, secondary scrubber three-level film-falling absorption tower, level Four scrubbing tower.
The invention has the following advantages:
1, it is directly entered destilling tower without cooling from the hydrochloric acid B that first grade scrubber comes out and is distilled, slip out liquid warp
Condensation enters storage acid tank, obtains food grade hydrochloric acid, greatly improves value-added content of product, solves hydrochloric acid impurity content height and be difficult to be utilized
The problem of.And the hydrogen chloride tail gas generated in distillation process is practically free of impurity, being directly entered three-level film-falling absorption tower is absorbed,
Obtain hydrochloric acid A.Hydrochloric acid B is without cooling, it is possible to reduce distills required energy, while shortening the time of distillation.
2, heat needed for hydrochloric acid B distillation process is mentioned by the tail gas that the combustion chamber for providing heat for mannheim furnace generates
For, this partial tail gas temperature at 500 DEG C or so, 10~14m of exhaust flow3/s.It is typically all by cooling in original technique
It is directly discharged in air after 300 DEG C or less.The present invention is needed using the distillation purifying that combustion chamber tail gas heat quantity fully meets hydrochloric acid B
It asks, combustion chamber tail gas is introduced into destilling tower through air-introduced machine, hydrochloric acid B is heated using immersion, the tail gas after heat exchange passes through row again
Air hose is discharged into air, makes full use of the waste heat in Mannheim proeess production process.
3, hydrochloric acid B in distillation process, inhaled into three-level film-falling absorption tower by the hydrogen chloride gas purity is high distilled
It receives, therefore improves the quality of hydrochloric acid A.
4, hydrochloric acid B is in distillation process, keeps in destilling tower by certain raffinate, and in raffinate hydrogen chloride content compared with
It is low, first grade scrubber can be directly entered and continue washing absorption hydrogen chloride gas, can be reduced in level Four scrubbing tower with simultaneous equal
The dosage of deionized water.But sulfate is (with SO in the raffinate4 2-Meter) concentration it is higher when, need for raffinate to be evaporated, residue is direct
Potassium sulfate is produced into mannheim furnace, the main component in residue is potassium chloride and potassium sulfate.It can be by the part by processing
Impurity is recycled.
5, the method for the present invention is utilized as mannheim furnace and provides the tail gas offer heat that the combustion chamber of heat generates, to absorption
Hydrochloric acid carries out distillation purifying, may be implemented to purify online, and without additional energy consumption, hydrochloric acid purifying is at low cost, obtains after purification
Hydrochloric acid it is high-quality, whole process three-waste free discharge.
Detailed description of the invention
Fig. 1 is the gas absorption technique flow chart come out using mannheim furnace before the method for the present invention.
Fig. 2 is the online purifying process flow chart that Mannheim proeess of the present invention produces hydrochloric acid in Process of Potassium Sulfate.
Specific embodiment
Below with reference to embodiment (for producing 30 tons of potassium sulfate production lines daily), the present invention is furture elucidated.
Comparative example:
As shown in Figure 1, (flow 13500L/min, flow velocity 3.7m/s, HCl content are about for the gas come out from mannheim furnace
50%) it is cooled down through cooler, then successively through first grade scrubber (tower height 10m, tower diameter 1.45m, interior internal circulating load 40L/
Min), secondary scrubber (tower height 10m, tower diameter 1.45m, interior internal circulating load 40L/min), three-level film-falling absorption tower (tower height 10m, tower
Diameter 1.45m, interior internal circulating load 40L/min) and level Four scrubbing tower (tower height 10m, tower diameter 1.45m, interior internal circulating load 40L/min) washing after
Emptying, deionized water (flow 9.44L/min) carries out washing absorption hydrogen chloride gas from level Four scrubbing tower, subsequently into three-level
Film-falling absorption tower absorbing hydrogen chloride gas obtains 32% hydrochloric acid A, and the yield of hydrochloric acid A is 20 ton/days.Mannheim proeess produces sulfuric acid
Tail gas uses deionized water (flow 7.08L/min) to be washed in the production environment collected during potassium, collects after washing
Cleaning solution successively after secondary scrubber, first grade scrubber washing absorption from first grade scrubber be discharged, obtain 32% hydrochloric acid
The yield of B, hydrochloric acid B are 15 ton/days.
Flow into the cleaning solution of secondary scrubber, first grade scrubber is 7.08L/min.
Through detecting, the quality of gained hydrochloric acid such as the following table 1:
| Project | Sulfate (SO4 2-, %) | Fe3+(%) | HCl (%) | Color |
| Hydrochloric acid A | 0.02 | 0.0008 | 32.2 | Micro- Huang |
| Hydrochloric acid B | 1.25 | 0.003 | 32.3 | Yellow |
Table 1
The content of hydrogen chloride in tail gas are as follows: 5.11mg/m3, meet environmental emission standard.
For mannheim furnace heating combustion chamber waste heat from tail gas temperature at 500 DEG C or so, by cooling to 245~295 DEG C
After be directly discharged in air, 10~14m of exhaust flow3/s。
The online purification process of hydrochloric acid, process flow such as Fig. 2 in Mannheim proeess production Process of Potassium Sulfate provided by the invention
Shown, (flow 13500L/min, flow velocity 3.7m/s, HCl content are about 50%) through cooler for the gas come out from mannheim furnace
It is cooling, then sequentially enter first grade scrubber (tower height 10m, tower diameter 1.45m, interior internal circulating load 40L/min), secondary scrubber (tower
High 10m, tower diameter 1.45m, interior internal circulating load 40L/min), three-level film-falling absorption tower (tower height 10m, tower diameter 1.45m, interior internal circulating load
40L/min) and level Four scrubbing tower (tower height 10m, tower diameter 1.45m, interior internal circulating load 40L/min) empties afterwards；(flow is deionized water
After 7.08L/min) carrying out washing absorption to environmentally friendly tail gas (Mannheim proeess of collection prepares the gas in potassium sulfate production environment)
Obtained cleaning solution sequentially enters secondary scrubber and first grade scrubber is washed, and finally obtains hydrochloric acid B, and (flow is hydrochloric acid B
7.08~14.16L/min) it is distilled into destilling tower, the fraction distilled obtains food grade hydrochloric acid (yield 10 through cooling
~15 ton/days), the gas distilled enters three-level film-falling absorption tower and is absorbed to obtain hydrochloric acid A；(flow is deionized water
9.44~11.8L/min) hydrogen chloride gas in level Four scrubbing tower is washed, chlorination is absorbed into three-level film-falling absorption tower
Hydrogen obtains hydrochloric acid A (20~25 ton/days of yield)；Destilling tower institute's calorific requirement is by providing the combustion chamber of heat for mannheim furnace
Generation tail gas (exhaust temperature: 245~295 DEG C, exhaust flow: 10~14m3/ s) it provides.It can be produced using Mannheim proeess
Combustion chamber waste heat from tail gas in Process of Potassium Sulfate carries out distillation purifying to hydrochloric acid online, obtains the hydrochloric acid of food-grade.
Further, for the exhaust temperature that the combustion chamber generates between 245~295 DEG C, exhaust flow is 10~14m3/
s。
Further, the gas phase of destilling tower obtains food grade hydrochloric acid (10~15 ton/days of yield), remaining gas through cooling
Three-level film-falling absorption tower is introduced to be absorbed to obtain hydrochloric acid A (20~25 ton/days of yield)；Raffinate a part of destilling tower enters level-one
Scrubbing tower carries out circulation washing as cleaning solution.
Further, tail gas is carried out using deionized water in the production environment collected in Mannheim proeess production Process of Potassium Sulfate
Washing, the cleaning solution collected after washing sequentially enters secondary scrubber and first grade scrubber is washed, and finally obtains hydrochloric acid B.
Further, the hydrochloric acid B enters the flow of destilling tower and the flow-rate ratio that slops enters first grade scrubber is
2:1~4:1.
Further, when the concentration of sulfate in raffinate is more than 30%, raffinate is evaporated, obtain bottoms 297~
301kg, residue are directly entered mannheim furnace production potassium sulfate.
The quality standard of food grade hydrochloric acid is as shown in table 2 below.
Table 2
Concrete case is as follows:
Embodiment 1:
Hydrochloric acid B in first grade scrubber is pumped into (flow 14.16L/min) hydrochloric acid destilling tower, 245 DEG C, stream are introduced
Measure 10m3The combustion chamber tail gas of/s is distilled.The flow that raffinate enters first grade scrubber is 7.08L/min, slips out liquid through condensing
Into storage acid tank, food grade hydrochloric acid is obtained.Food grade hydrochloric acid color is limpid, sulphates content 0.002%, molysite content
0.0005%, acid concentration 32.7%, 15 ton/days of yield.
Deionized water (flow 9.44L/min) washs the hydrogen chloride gas in level Four scrubbing tower, into three-level
Film-falling absorption tower absorbing hydrogen chloride gas, the hydrogen chloride tail gas generated in destilling tower are also directly entered three-level film-falling absorption tower and are inhaled
It receives, finally obtains hydrochloric acid A.Hydrochloric acid A color is limpid, sulphates content 0.003%, molysite content 0.0005%, acid concentration
32.5%, 20 ton/days of yield.
When the concentration of sulfate in raffinate is more than 30%, raffinate is evaporated, bottoms 298kg is obtained.
Embodiment 2:
Hydrochloric acid B in first order scrubbing tower is pumped into (flow 14.16L/min) hydrochloric acid destilling tower, 295 DEG C of introducing,
Flow 14m3The combustion chamber tail gas of/s is distilled.The flow that raffinate enters first grade scrubber is 3.54L/min, slips out liquid through cold
It is solidifying to enter storage acid tank, obtain food grade hydrochloric acid.Food grade hydrochloric acid color is limpid, sulphates content 0.001%, molysite content are without clear
Value, acid concentration 33.6%, 10 ton/days of yield.
Deionized water (flow 11.80L/min) washs the hydrogen chloride gas in level Four scrubbing tower, into three-level
Film-falling absorption tower absorbing hydrogen chloride gas, the hydrogen chloride tail gas generated in destilling tower are also directly entered three-level film-falling absorption tower and are inhaled
It receives, finally obtains hydrochloric acid A.Hydrochloric acid A color is limpid, sulphates content 0.003%, molysite content 0.0005%, acid concentration
32.6%, 25 ton/days of yield.
When the concentration of sulfate in raffinate is more than 30%, raffinate is evaporated, bottoms 301kg is obtained.
Embodiment 3:
Hydrochloric acid B in first order scrubbing tower is pumped into (flow 9.44L/min) hydrochloric acid destilling tower, 260 DEG C, stream are introduced
Measure 13.7m3The combustion chamber tail gas of/s is distilled.The flow that raffinate enters first order scrubbing tower is 3.14L/min, slips out liquid warp
Condensation enters storage acid tank, obtains food grade hydrochloric acid.Food grade hydrochloric acid color is limpid, sulphates content 0.001%, molysite content
0.0005%, acid concentration 32.1%, yield are 13.3 ton/days.
Deionized water (flow 10.24L/min) washs the hydrogen chloride gas in level Four scrubbing tower, into three-level
Film-falling absorption tower absorbing hydrogen chloride gas, the hydrogen chloride tail gas generated in destilling tower are also directly entered three-level film-falling absorption tower and are inhaled
It receives, finally obtains hydrochloric acid A.Hydrochloric acid A color is limpid, sulphates content 0.003%, molysite content 0.0005%, acid concentration
32.4%, 21.7 ton/days of yield.
When the concentration of sulfate in raffinate is more than 30%, raffinate is evaporated, bottoms 297kg is obtained.
Embodiment 4:
Hydrochloric acid B in first order scrubbing tower is pumped into (flow 7.08L/min) hydrochloric acid destilling tower, 285 DEG C, stream are introduced
Measure 14m3The combustion chamber tail gas of/s is distilled.The flow that raffinate enters first grade scrubber is 3.54L/min, slips out liquid through condensing
Into storage acid tank, food grade hydrochloric acid is obtained.Food grade hydrochloric acid color is limpid, sulphates content 0.001%, molysite content
0.0005%, acid concentration 32.8%, 10 ton/days of yield.
Deionized water (flow 11.80L/min) washs the hydrogen chloride gas in level Four scrubbing tower, into three-level
Film-falling absorption tower absorbing hydrogen chloride gas, the hydrogen chloride tail gas generated in destilling tower are also directly entered three-level film-falling absorption tower and are inhaled
It receives, finally obtains hydrochloric acid A.Hydrochloric acid A color is limpid, sulphates content 0.003%, molysite content 0.0005%, acid concentration
32.5%, 25 ton/days of yield.
When the concentration of sulfate in raffinate is more than 30%, raffinate is evaporated, bottoms 300kg is obtained.
Embodiment 5:
Hydrochloric acid B in first order scrubbing tower is pumped into (flow 12.03L/min) hydrochloric acid destilling tower, 258 DEG C of introducing,
Flow 12.2m3The combustion chamber tail gas of/s is distilled.The flow that raffinate enters first order scrubbing tower is 6.00L/min, slips out liquid
Enter storage acid tank through condensation, obtains food grade hydrochloric acid.Food grade hydrochloric acid color is limpid, sulphates content 0.001%, molysite content
0.0005%, acid concentration 32.3%, 12.8 ton/days of yield.
Deionized water (flow 10.48L/min) washs the hydrogen chloride gas in level Four scrubbing tower, into three-level
Film-falling absorption tower absorbing hydrogen chloride gas, the hydrogen chloride tail gas generated in destilling tower are also directly entered three-level film-falling absorption tower and are inhaled
It receives, finally obtains hydrochloric acid A.Hydrochloric acid A color is limpid, sulphates content 0.003%, molysite content 0.0005%, acid concentration
32.7%, 22.3 ton/days of yield.
When the concentration of sulfate in raffinate is more than 30%, raffinate is evaporated, bottoms 299kg is obtained.
Claims (7)
1. the online purification process that Mannheim proeess produces hydrochloric acid in Process of Potassium Sulfate, which comprises the following steps:
The gas come out from mannheim furnace is cooling through cooler, then sequentially enters first grade scrubber, secondary scrubber, three-level drop
It is emptied after film absorption tower and level Four scrubbing tower；Deionized water to environmentally friendly tail gas carry out after washing absorption obtained cleaning solution successively into
Enter secondary scrubber and first grade scrubber is washed, finally obtain hydrochloric acid B, hydrochloric acid B enters destilling tower and distilled, distilled out
The fraction come obtains food grade hydrochloric acid through cooling, and deionized water washs the hydrogen chloride gas in level Four scrubbing tower, enters
The gas that three-level film-falling absorption tower absorbing hydrogen chloride gas and destilling tower distill enters three-level film-falling absorption tower and absorbs
To hydrochloric acid A；Destilling tower institute's calorific requirement is provided by the tail gas that the combustion chamber for providing heat for mannheim furnace generates.
2. according to method described in right 1, it is characterised in that: the environmentally friendly tail gas is in Mannheim proeess production Process of Potassium Sulfate
Tail gas in the production environment of collection.
3. according to method described in right 1, it is characterised in that: the raffinate part of destilling tower enters first grade scrubber as cleaning solution
Carry out circulation washing.
4. according to method described in right 3, it is characterised in that: the hydrochloric acid B enters the flow of destilling tower and vinasse enters
The flow-rate ratio of first grade scrubber is 2:1~4:1.
5. according to method described in right 3, it is characterised in that:, will be residual when the concentration of sulfate in vinasse is more than 30wt%
Liquid is evaporated, and residue is directly entered mannheim furnace production potassium sulfate.
6. according to method described in right 1, it is characterised in that: the gas generated in mannheim furnace is subsequent using level Four scrubbing tower
Air-introduced machine introduces cooler and is cooled down, and then sequentially enters first grade scrubber, secondary scrubber three-level film-falling absorption tower, level Four
Scrubbing tower.
7. according to method described in right 1, it is characterised in that: the tail gas that the combustion chamber generates temperature after cooler is cooling exists
Between 245~295 DEG C.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112158862A (en) * | 2020-05-15 | 2021-01-01 | 青岛碱业钾肥科技有限公司 | Production method of low-chlorine potassium sulfate |
| CN112794345A (en) * | 2021-01-20 | 2021-05-14 | 宁夏中泰富瑞科技有限公司 | Equipment for preparing potassium sulfate from potassium chloride and manufacturing process thereof |
| CN114288841A (en) * | 2021-12-31 | 2022-04-08 | 山东三方化工集团有限公司 | Mannheim method potassium sulfate tail gas processing system |
Citations (2)
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| CN106554019A (en) * | 2015-09-29 | 2017-04-05 | 新特能源股份有限公司 | A kind of technique of trichlorosilane synthetic tail gas cleaning system |
| CN206424751U (en) * | 2016-12-23 | 2017-08-22 | 青上化工（惠州）有限公司 | A kind of 7th grade of recovery tower of hydrochloric acid tail gas |
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| CN106554019A (en) * | 2015-09-29 | 2017-04-05 | 新特能源股份有限公司 | A kind of technique of trichlorosilane synthetic tail gas cleaning system |
| CN206424751U (en) * | 2016-12-23 | 2017-08-22 | 青上化工（惠州）有限公司 | A kind of 7th grade of recovery tower of hydrochloric acid tail gas |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112158862A (en) * | 2020-05-15 | 2021-01-01 | 青岛碱业钾肥科技有限公司 | Production method of low-chlorine potassium sulfate |
| CN112158862B (en) * | 2020-05-15 | 2021-06-29 | 青岛碱业钾肥科技有限公司 | Production method of low-chlorine potassium sulfate |
| CN112794345A (en) * | 2021-01-20 | 2021-05-14 | 宁夏中泰富瑞科技有限公司 | Equipment for preparing potassium sulfate from potassium chloride and manufacturing process thereof |
| CN114288841A (en) * | 2021-12-31 | 2022-04-08 | 山东三方化工集团有限公司 | Mannheim method potassium sulfate tail gas processing system |
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| CN110127615B (en) | 2022-07-22 |
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