CN110422827A - A kind of the Waste Sulfuric Acid recycling device and technique of dry chlorine gas - Google Patents
A kind of the Waste Sulfuric Acid recycling device and technique of dry chlorine gas Download PDFInfo
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- CN110422827A CN110422827A CN201910715665.3A CN201910715665A CN110422827A CN 110422827 A CN110422827 A CN 110422827A CN 201910715665 A CN201910715665 A CN 201910715665A CN 110422827 A CN110422827 A CN 110422827A
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- sulfuric acid
- acid
- cooler
- chlorine
- heat exchanger
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- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 title claims abstract description 292
- 239000002699 waste material Substances 0.000 title claims abstract description 56
- 238000000034 method Methods 0.000 title claims abstract description 33
- 238000004064 recycling Methods 0.000 title claims abstract description 30
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 title claims abstract description 29
- 239000002253 acid Substances 0.000 claims abstract description 74
- 239000007788 liquid Substances 0.000 claims abstract description 60
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 58
- 239000000460 chlorine Substances 0.000 claims abstract description 58
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 58
- 239000000463 material Substances 0.000 claims abstract description 42
- 238000005406 washing Methods 0.000 claims description 19
- 239000012141 concentrate Substances 0.000 claims description 18
- 239000002994 raw material Substances 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 14
- 238000001035 drying Methods 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 11
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 7
- 239000005864 Sulphur Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 6
- 239000010865 sewage Substances 0.000 claims description 5
- 239000002826 coolant Substances 0.000 claims description 3
- 238000006298 dechlorination reaction Methods 0.000 claims description 3
- 230000032696 parturition Effects 0.000 claims description 3
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 239000007789 gas Substances 0.000 description 36
- 239000000047 product Substances 0.000 description 12
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 238000005260 corrosion Methods 0.000 description 8
- 238000000926 separation method Methods 0.000 description 8
- 239000000243 solution Substances 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 6
- 239000003513 alkali Substances 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 230000007797 corrosion Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 3
- 230000008020 evaporation Effects 0.000 description 3
- 239000003517 fume Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 235000011121 sodium hydroxide Nutrition 0.000 description 3
- 229910052715 tantalum Inorganic materials 0.000 description 3
- GUVRBAGPIYLISA-UHFFFAOYSA-N tantalum atom Chemical compound [Ta] GUVRBAGPIYLISA-UHFFFAOYSA-N 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 239000005708 Sodium hypochlorite Substances 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000008235 industrial water Substances 0.000 description 2
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000001117 sulphuric acid Substances 0.000 description 2
- 235000011149 sulphuric acid Nutrition 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000005997 Calcium carbide Substances 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910001018 Cast iron Inorganic materials 0.000 description 1
- 239000004366 Glucose oxidase Substances 0.000 description 1
- 239000004365 Protease Substances 0.000 description 1
- 238000010793 Steam injection (oil industry) Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- -1 buffer tank Chemical compound 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 210000003298 dental enamel Anatomy 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 235000011194 food seasoning agent Nutrition 0.000 description 1
- 239000010439 graphite Substances 0.000 description 1
- 229910002804 graphite Inorganic materials 0.000 description 1
- 239000010440 gypsum Substances 0.000 description 1
- 229910052602 gypsum Inorganic materials 0.000 description 1
- 229910000856 hastalloy Inorganic materials 0.000 description 1
- 239000001573 invertase Substances 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 229910000360 iron(III) sulfate Inorganic materials 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 239000004810 polytetrafluoroethylene Substances 0.000 description 1
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 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
- C01B11/00—Oxides or oxyacids of halogens; Salts thereof
- C01B11/04—Hypochlorous acid
- C01B11/06—Hypochlorites
- C01B11/062—Hypochlorites of alkali metals
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/88—Concentration of sulfuric acid
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/90—Separation; Purification
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Geology (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses the Waste Sulfuric Acid recycling devices and technique of a kind of dry chlorine gas, belong to waste acid recycling technical field.It includes buffer tank, the sour heat exchanger of acid, acid cooler, dilute sulfuric acid concentration kettle and sulfuric acid knockout tower, buffer tank is used to store the material liquid of the Waste Sulfuric Acid containing chlorine, the outlet of buffer tank is connected with the material liquid feed inlet of sour heat exchanger, the gelled acid discharge port of sour heat exchanger is connected with the feed inlet of acid cooler, and the discharge port of acid cooler is connected with finished product pans；The material liquid discharge port of sour heat exchanger is connected with the feed inlet of sulfuric acid knockout tower, the discharge port of sulfuric acid knockout tower is connected with the feed inlet of dilute sulfuric acid concentration kettle, the gelled acid discharge port of dilute sulfuric acid concentration kettle is connected with the gelled acid feed inlet of sour heat exchanger, and the steam (vapor) outlet of dilute sulfuric acid concentration kettle is connected with the steam inlet of sulfuric acid knockout tower.The present invention realizes the recycling of dilute sulfuric acid and the subsequent concentrated sulfuric acid, saves production cost and mitigates protection pressure.
Description
Technical field
The invention belongs to waste acid recycling technical fields, follow more specifically to a kind of Waste Sulfuric Acid of dry chlorine gas
Ring utilizes device and technique.
Background technique
The dry chlorine device of Current Domestic mostly uses greatly sulfuric acid seasoning, this process caustic soda per ton needs to consume
98% concentrated sulfuric acid about 12-16Kg.Stop by the end of in December, 2016, domestic caustic soda gross annual output amount is about 33,000,000 tons；It presses
Caustic soda actual production calculates within 2016, every year the Waste Sulfuric Acid of ten thousand tons of 75%-80% of about by-product 49.5-66 or so.Current chlor-alkali
Enterprise is mainly to be sold to the enterprise of production chemical fertilizer for producing chemical fertilizer or using calcium carbide to the processing mode of dry chlorine Waste Sulfuric Acid
Mud neutralization is made outside gypsum and sells.Due to being dissolved with 0.2% or so chlorine in dry chlorine spent acid, so having than finished product sulfuric acid
Stronger corrosivity, the chlorine to volatilize in transport, use process seriously pollute environment.
Continuous improvement recently as country to environmental requirement, Waste Sulfuric Acid concentrate recycling is trend of the times.In
Europe and North America developed economies in, the dry chlorine Waste Sulfuric Acid of chlor-alkali enterprises almost 100% concentration after recycle.From now on
With the development of environmental protection policy and law-enforcing environment, generate in foreseeable future China chlor-alkali and PVC enterprise nearly 700,000 tons/
Year, Waste Sulfuric Acid was impossible to handle by current extensive method, and recycling will be mainstream development direction.
Summary of the invention
1, it to solve the problems, such as
In view of the problems of the existing technology, the present invention provides the Waste Sulfuric Acid recycling device and work of a kind of dry chlorine gas
Skill, it solve the problems, such as dilute sulfuric acid processing and the subsequent concentrated sulfuric acid recycling the problem of, save production cost and mitigate protection
Pressure.
2, technical solution
To solve the above problems, the present invention adopts the following technical scheme that.
A kind of Waste Sulfuric Acid recycling device of dry chlorine gas, including buffer tank, acid sour heat exchanger, acid cooler, dilute sulphur
Sour concentration kettle and sulfuric acid knockout tower,
The buffer tank is used to store the material liquid of the Waste Sulfuric Acid containing chlorine, and the outlet of the buffer tank and the acid acid exchange heat
The material liquid feed inlet of device is connected,
The gelled acid discharge port of the sour heat exchanger of acid is connected with the feed inlet of the acid cooler,
The discharge port of the acid cooler is connected with the finished product pans；
The material liquid discharge port of the sour heat exchanger of acid is connected with the feed inlet of the sulfuric acid knockout tower, the sulfuric acid separation
The discharge port of tower is connected with the feed inlet of the dilute sulfuric acid concentration kettle, the gelled acid discharge port of the dilute sulfuric acid concentration kettle with it is described
The gelled acid feed inlet of sour heat exchanger is connected,
The steam (vapor) outlet of the dilute sulfuric acid concentration kettle is connected with the steam inlet of the sulfuric acid knockout tower.
It further include raw material pump in the Waste Sulfuric Acid recycling device of above-mentioned dry chlorine gas, the raw material pump will be for that will cache
Feed liquid in tank is delivered in the sour heat exchanger of the acid.
It further include discharging pump in the Waste Sulfuric Acid recycling device of above-mentioned dry chlorine gas, the discharging pump is used for acid is cold
But the feed liquid in device is delivered in the finished product pans.
In the Waste Sulfuric Acid recycling device of above-mentioned dry chlorine gas, the condensation-water drain and steam of the dilute sulfuric acid concentration kettle
Condensate water pot is connected.
In the Waste Sulfuric Acid recycling device of above-mentioned dry chlorine gas, also set up in the dilute sulfuric acid concentration kettle for giving birth to steam
The air inlet of entrance.
In the Waste Sulfuric Acid recycling device of above-mentioned dry chlorine gas, the steam (vapor) outlet and tail gas of the sulfuric acid knockout tower are cooling
The air inlet of device is connected, and the condensate outlet of the exhaust gas cooler is connected with the feed inlet of chlorine tail gas washing tower.
In the Waste Sulfuric Acid recycling device of above-mentioned dry chlorine gas, the exhaust gas cooler passes through the chlorine water storage tank and institute
Chlorine tail gas washing tower is stated to be connected.
In the Waste Sulfuric Acid recycling device of above-mentioned dry chlorine gas, the gas outlet of the exhaust gas cooler passes through three-level steam
Injection vacuum system and vacuum cooler are connected with the air inlet of the chlorine tail gas washing tower.
A kind of Waste Sulfuric Acid utilization process of dry chlorine gas, comprising the following steps:
(1) by the feedstock transportation to buffer tank outside battery limit (BL), for use；
(2) it is pumped using raw material and the material liquid in buffer tank is delivered in sour heat exchanger, material liquid is then conveyed into sulphur
In acid separation column；
(3) sulfuric acid knockout tower separates material liquid, and separating liquid is made and generates steam, is then delivered to separating liquid
In dilute sulfuric acid concentration kettle；
(4) separating liquid is concentrated in dilute sulfuric acid concentration kettle, and concentrate is made and generates steam, then concentrate is delivered to
It in sour heat exchanger and is transferred in acid cooler, steam is delivered in sulfuric acid knockout tower；
(5) acid cooler carries out cooling treatment to concentrate and is delivered in finished product pans；
(6) concentrate of finished product pans conveys dechlorination drying section；
Wherein the progress dividing wall type heat in sour heat exchanger exchanges material liquid with concentrate in step (4) in step (2)；
The steam that wherein sulfuric acid knockout tower generates in step (3) is delivered to exhaust gas cooler and is condensed, and condenses generation
Condensate liquid is delivered to chlorine tail gas washing tower through chlorine water storage tank；The gas that can not be condensed be delivered to three-level steam jet vacuum system into
Row suction discharge, the gas for aspirating discharge carry out cooling and the cooling coolant liquid generated are delivered to chlorine tail by vacuum cooler
Gas wash tower；
Sewage disposal system outside battery limit (BL) is gone in the waste liquid conveying that wherein chlorine tail gas washing tower generates.
In the Waste Sulfuric Acid utilization process of above-mentioned dry chlorine gas, the raw material in step (1) outside battery limit (BL) includes containing chlorine
The material liquid of gas Waste Sulfuric Acid.
3, beneficial effect
Compared with the prior art, the invention has the benefit that
The device of the invention and technique, using the material liquid of the Waste Sulfuric Acid containing chlorine as raw material, buffer tank is arranged in upstream, and downstream is set
Product pans are set to, separation concentration is carried out through devices such as sour heat exchanger, sulfuric acid separator and dilute sulfuric acid concentration kettles, is concentrated into matter
Amount concentration is sent dry chlorine device back to for 98% or so respectively and is recycled, and generates during separation concentration technology a small amount of
Exhaust gas, which is sent back to, to be made sodium hypochlorite with Alkali absorption in chlorine tail gas washing tower and is recycled, and the waste water of generation is sent to sewage disposal system
Make industrial water use after being handled.Compared with traditional Waste Sulfuric Acid circulator and technique, it is entirely avoided evaporation of high concentrated liquor
When acid fume pollution, the discharge amount of good operational environment, the three wastes is small, fully utilizes the superior anti-corrosion material of multiple performance, avoids
Frequent replacement after equipment corrosion, ensure that system continuous and steady operation, ensure that acid solution and service are surveyed between medium most
Big mean temperature difference, makes full use of the energy, and low energy consumption, and labor intensity is small, and operator is few.
Detailed description of the invention
Fig. 1 is the process flow chart of the Waste Sulfuric Acid recycling device of dry chlorine gas of the invention.
Specific embodiment
The present invention will be described in detail in the following with reference to the drawings and specific embodiments.
In addition, the present invention is based on how being recycled of the processing for solving the problems, such as dilute sulfuric acid and the subsequent concentrated sulfuric acid, how to save
It saves production cost and how to mitigate the problem of protecting pressure and propose, the spent acid currently used for dry chlorine generation is due to concentration
Less than 85%, the chlorine in acid containing 0.2% or so, which can not reuse, can only go waste to handle, and environmental protection pressure is huge, every year
The fresh concentrated sulfuric acid is also constantly put into, the cost of enterprise's production is increased.
The feasibility analysis of dry chlorine is carried out using concentrating regenerative sulfuric acid:
It is dried due to its steam partial pressure very little when water content has dropped down to very low in chlorine (such as 0.01% or so)
The mass transfer force of journey also accordingly drops to very low value, and process can become extremely difficult, so domestic dry chlorine dress
Moisture content being set in guarantee chlorine less than 0.01% (V/V%), the supplement sulfuric acid concentration of the chlorine drying device of addition is >=
98%, and vacuum concentration technique for dilute sulphuric acid is limited from economy by the cost factor being concentrated, device sulfuric acid concentration control out
System is 96% or so.The mass transfer force of drying process is equal to the balance of steam partial pressure and sulfuric acid in gas phase in sulfuric acid drying tower
The pressure difference of steam partial pressure.When water content is dried to 0.01% (V/V%) below in chlorine, by 92KPa in combination drying tower
The steam partial pressure that (absolute pressure) calculates in chlorine at this time is about 9.2Pa, looks into the steam partial pressure on figure sulfuric acid, at 25 DEG C, often
It depresses, it is 0.1Pa that it, which balances steam partial pressure, on the sulfuric acid of about 93% concentration；Steam partial pressure on 98% sulfuric acid is at 25 DEG C
When, level off to zero under normal pressure.The mass transfer force of drying process in combined column can be calculated in this way: when the sulphur with 93% concentration
About 9.1Pa when sour；It is approximately equal to 9.2Pa when using the sulfuric acid of 98% concentration.Therefore exist it can be concluded that sulfuric acid concentration is added
When between 93%-98%, the mass transfer force difference of drying process is little in sulfuric acid drying tower, so being concentrated in vacuo with dilute sulfuric acid
96% or so the concentrated sulfuric acid that technique concentrate obtains can satisfy the requirement of dry chlorine technique.The technology of sulphuric acid concentration has very much
Kind, wherein cooking-pot type concentration technique earlier, because energy consumption is high, environmental pollution is big, and high-silicon cast iron pot is reacted with high-temperature sulfuric acid
Generate Fe2(SO4)3, make the yellowish of acid, Fe be also easy to produce in drying tower2(SO4)3Crystallization Plugging filler gradually fades out market.
It is external also just like wave woods (Pauling) method；From the staircase method for being arranged to stepped evaporating dish and flowing down；It is flowed down into tower
Acid send the method for hot wind and in acid solution spray hot wind day iron processes and Kai meter Ke Fa be representative submerged combustion；Make in vertical tank
As vacuum, Man Tesi (Mantius) method being intermittently concentrated with heating coil etc..In these methods, there is one
A little problems, be such as not applied for largely handling, energy consumption is high, yield is low, fluctuation of service, cannot highly concentrated, device for mechanical damage
The problem of consuming serious, generation gas and public hazards aspect.
As shown in Figure 1, the Waste Sulfuric Acid recycling device of dry chlorine gas, including the sour heat exchanger of buffer tank, acid, acid are cooling
Device, dilute sulfuric acid concentration kettle and sulfuric acid knockout tower,
The buffer tank is used to store the material liquid of the Waste Sulfuric Acid containing chlorine, and the outlet of the buffer tank and the acid acid exchange heat
The material liquid feed inlet of device is connected, and the raw material pump is for the feed liquid in buffer tank to be delivered in the sour heat exchanger of the acid；Its
The tank inner volume of middle buffer tank is 10 cubes, and material is fibre reinforced composites；Wherein the model specification of preheater is
YKB40-15, material are graphite/CS anti-corrosion, and shell side serves as a contrast rubber；Wherein raw material pump is for by the feed liquid in raw material buffer tank
It is delivered in the preheater, wherein the 2 cubes/h of flow of raw material pump, 30 meters of lift, material is steel lining tetrafluoro；
The gelled acid discharge port of the sour heat exchanger of acid is connected with the feed inlet of the acid cooler；The wherein sour heat exchanger of acid
Model E1102, be a kind of two-way corrosion-resistant tubular heat exchanger；The wherein model E1101 of acid cooler；
The discharge port of the acid cooler is connected with the finished product pans；Wherein finished product pans can vacuum-resistant, tank
Inner volume is 1 cube, material PTFE/CS；The discharging pump is used to the feed liquid in acid cooler being delivered to the finished product
In pans, the wherein 1 cube/h of flow of discharging pump, 20 meters of lift, material is steel lining tetrafluoro；
The material liquid discharge port of the sour heat exchanger of acid is connected with the feed inlet of the sulfuric acid knockout tower, the sulfuric acid separation
The discharge port of tower is connected with the feed inlet of the dilute sulfuric acid concentration kettle, the gelled acid discharge port of the dilute sulfuric acid concentration kettle with it is described
The gelled acid feed inlet of sour heat exchanger is connected；The wherein model T1101 of sulfuric acid knockout tower, the wherein type of dilute sulfuric acid concentration kettle
It number is also T1101, dilute sulfuric acid concentration kettle is the tower reactor of sulfuric acid knockout tower, and dilute sulfuric acid concentration kettle is that the battleax formula of tantalum material manufacture is boiled again
Device.Under 90 kPas or more of high vacuum condition, above-mentioned dilute sulfuric acid concentration kettle uses horizontal vacuum concentration technique, the technology spent acid
Low boiling point, energy consumption be small, sour best in quality after concentration, is advanced and comprehensive technology；The technique of related dilute sulfuric acid vacuum concentration
Principle: dilute sulfuric acid enters dilute sulfuric acid concentration kettle according to the flow and flow rate of technology controlling and process, in high vacuum condition after heating
Under, multiple indoor acid solution explosive evaporations at a lower temperature of concentration, dilute sulfuric acid concentration kettle casing lining in dilute sulfuric acid concentration kettle
Enamel is heated using tantalum pipe, while will be separated into multiple enriched chambers in dilute sulfuric acid concentration kettle, and dilute sulfuric acid is along the dense of concentration kettle
The flowing of contracting room, concentration improves step by step, and the partition of enriched chambers at different levels prevents the reflux of acid solution, ensure that acid solution and heating steam it
Between maximum mean temperature difference, take full advantage of the heating surface (area) (HS of tantalum pipe surface, thus make afterbody enriched chamber flow out sulfuric acid
Reach aimed concn；Above-mentioned dilute sulfuric acid vacuum concentration wage is compared with the obvious advantage with other method for concentration, and it is good to be operated first environment,
The pollution of acid fume is completely avoided, the discharge amount of the three wastes is small, secondly uses the superior anti-corrosion material of multiple performance, avoids and set
Frequent replacement after standby corrosion, greatly reduces labor intensity, multiple enriched chamber's continuous operations, operator is few, and low energy consumption；
The steam (vapor) outlet of the dilute sulfuric acid concentration kettle is connected with the steam inlet of the sulfuric acid knockout tower.
In addition, the condensation-water drain of the dilute sulfuric acid concentration kettle is connected with steam condensate (SC) tank, it can effective recovered steam band
The condensed water come；
The air inlet for giving birth to steam entrance is also set up in the dilute sulfuric acid concentration kettle, the life steam outside battery limit (BL) passes through
Sub-cylinder is delivered in dilute sulfuric acid concentration kettle；
The steam (vapor) outlet of the sulfuric acid knockout tower is connected with the air inlet of exhaust gas cooler, the condensation of the exhaust gas cooler
Liquid outlet is connected with the feed inlet of chlorine tail gas washing tower；The wherein model E1103 of exhaust gas cooler；
The exhaust gas cooler is connected by the chlorine water storage tank with the chlorine tail gas washing tower；The exhaust gas cooler
Gas outlet is connected by three-level steam jet vacuum system and vacuum cooler with the air inlet of the chlorine tail gas washing tower；Wherein
The model J1101-1103 of three-level steam jet vacuum system, for a kind of hydraulic jet pump (the literary mound of Hastelloy production
In)；The wherein model V1102 of chlorine water storage tank；
The Waste Sulfuric Acid utilization process of above-mentioned dry chlorine gas, comprising the following steps:
(1) by the feedstock transportation to buffer tank outside battery limit (BL), for use；Raw material packet in step (1) outside battery limit (BL)
Include the material liquid of the Waste Sulfuric Acid containing chlorine；The concentrated sulfuric acid for dry chlorine generation becomes concentration after absorbing the moisture content in chlorine
In 75% Waste Sulfuric Acid (as material liquid), but the chlorine in Waste Sulfuric Acid containing 0.2% or so can not reuse, and need to carry out
Filter just can transport to buffer tank；
(2) it is pumped using raw material and the material liquid in buffer tank is delivered in sour heat exchanger, material liquid is then conveyed into sulphur
In acid separation column；After the steam (sulfur sesquioxide) of the dilute sulfuric acid concentration kettle of material liquid absorption at this time, temperature and concentration are promoted,
The temperature of material liquid is increased to 115 DEG C, and the mass concentration of material liquid is increased to 83%；
(3) sulfuric acid knockout tower separates material liquid, and separating liquid is made and generates steam, is then delivered to separating liquid
In dilute sulfuric acid concentration kettle；
(4) separating liquid is concentrated in dilute sulfuric acid concentration kettle, and concentrate (mass concentration of concentrate is 96%) is made simultaneously
Steam is generated, then concentrate is delivered in sour heat exchanger and is transferred in acid cooler, and steam is delivered to sulfuric acid knockout tower
It is interior；
(5) acid cooler carries out cooling treatment to concentrate and is delivered in finished product pans；
(6) concentrate conveying dechlorination drying section (dry chlorine device) of finished product pans is recycled, in turn
Promote recycling for heat；
Wherein the progress dividing wall type heat in sour heat exchanger exchanges material liquid with concentrate in step (4) in step (2)；
The steam that wherein sulfuric acid knockout tower generates in step (3) is delivered to after the dilute sulfuric acid washing that mass concentration is 80%
Exhaust gas cooler is condensed, and condenses the condensate liquid of generation through chlorine water storage tank (and by waste water delivery pump (model
P1102AB)) it is delivered to chlorine tail gas washing tower；The gas that can not be condensed is delivered to three-level steam jet vacuum system and is aspirated
Discharge, the gas for aspirating discharge carry out cooling and the cooling coolant liquid generated are delivered to chlorine washing tail gas by vacuum cooler
Tower；
Sewage disposal system outside battery limit (BL) is gone in the waste liquid conveying that wherein chlorine tail gas washing tower generates.
In conclusion in conjunction with Fig. 1 and table 1, the Waste Sulfuric Acid recycling device and technique of the dry chlorine gas of the present embodiment, with
The material liquid of the Waste Sulfuric Acid containing chlorine is raw material, and buffer tank is arranged in upstream, and finished product pans are arranged in downstream, through sour heat exchanger, sulphur
The devices such as acid separator and dilute sulfuric acid concentration kettle carry out separation concentration, are concentrated into mass concentration as 98% or so and send chlorine back to respectively
Drying device is recycled, and a small amount of exhaust gas generated during separation concentration technology is sent back in chlorine tail gas washing tower to be inhaled with alkali
Receipts are made sodium hypochlorite and are recycled, the waste water of generation is sent to sewage disposal system handled after make industrial water use.With
Traditional Waste Sulfuric Acid circulator and technique are compared, it is entirely avoided the pollution of acid fume, good operational environment, the three wastes when evaporation of high concentrated liquor
Discharge amount it is small, fully utilize the superior anti-corrosion material of multiple performance, avoid equipment corrosion after frequent replacement, ensure that
System continuous and steady operation ensure that acid solution and service survey the maximum mean temperature difference between medium, make full use of the energy, energy consumption
Low, labor intensity is small, and operator is few.
The economic effect analysis of table 1 is (by taking 8000 tons/year of device as an example；Direct economic benefit is 391.72 ten thousand yuan/year)
Schematically the present invention and embodiments thereof are described above, description is not limiting, institute in attached drawing
What is shown is also one of embodiments of the present invention, and actual structure is not limited to this.So if the common skill of this field
Art personnel are enlightened by it, without departing from the spirit of the invention, are not inventively designed and the technical solution
Similar frame mode and embodiment, are within the scope of protection of the invention.
Claims (10)
1. a kind of Waste Sulfuric Acid recycling device of dry chlorine gas, it is characterised in that:
Including buffer tank, the sour heat exchanger of acid, acid cooler, dilute sulfuric acid concentration kettle and sulfuric acid knockout tower,
The buffer tank is used to store the material liquid of the Waste Sulfuric Acid containing chlorine, the outlet of the buffer tank and the sour heat exchanger of the acid
Material liquid feed inlet is connected,
The gelled acid discharge port of the sour heat exchanger of acid is connected with the feed inlet of the acid cooler,
The discharge port of the acid cooler is connected with the finished product pans；
The material liquid discharge port of the sour heat exchanger of acid is connected with the feed inlet of the sulfuric acid knockout tower, the sulfuric acid knockout tower
Discharge port is connected with the feed inlet of the dilute sulfuric acid concentration kettle, the gelled acid discharge port of the dilute sulfuric acid concentration kettle and the acid acid
The gelled acid feed inlet of heat exchanger is connected,
The steam (vapor) outlet of the dilute sulfuric acid concentration kettle is connected with the steam inlet of the sulfuric acid knockout tower.
2. the Waste Sulfuric Acid recycling device of dry chlorine gas according to claim 1, it is characterised in that:
It further include raw material pump, the raw material pump is for the feed liquid in buffer tank to be delivered in the sour heat exchanger of the acid.
3. the Waste Sulfuric Acid recycling device of dry chlorine gas according to claim 1, it is characterised in that:
It further include discharging pump, the discharging pump is for the feed liquid in acid cooler to be delivered in the finished product pans.
4. the Waste Sulfuric Acid recycling device of dry chlorine gas according to claim 1, it is characterised in that:
The condensation-water drain of the dilute sulfuric acid concentration kettle is connected with steam condensate (SC) tank.
5. the Waste Sulfuric Acid recycling device of dry chlorine gas according to claim 1, it is characterised in that:
The air inlet for giving birth to steam entrance is also set up in the dilute sulfuric acid concentration kettle.
6. the Waste Sulfuric Acid recycling device of dry chlorine gas according to claim 1, it is characterised in that:
The steam (vapor) outlet of the sulfuric acid knockout tower is connected with the air inlet of exhaust gas cooler, and the condensate liquid of the exhaust gas cooler goes out
Mouth is connected with the feed inlet of chlorine tail gas washing tower.
7. the Waste Sulfuric Acid recycling device of dry chlorine gas according to claim 6, it is characterised in that:
The exhaust gas cooler is connected by the chlorine water storage tank with the chlorine tail gas washing tower.
8. the Waste Sulfuric Acid recycling device of dry chlorine gas according to claim 1, it is characterised in that:
The gas outlet of the exhaust gas cooler is washed by three-level steam jet vacuum system and vacuum cooler with the chlorine tail gas
The air inlet for washing tower is connected.
9. a kind of Waste Sulfuric Acid utilization process of dry chlorine gas, it is characterised in that:
The following steps are included:
(1) by the feedstock transportation to buffer tank outside battery limit (BL), for use；
(2) it is pumped using raw material and the material liquid in buffer tank is delivered in sour heat exchanger, then by material liquid conveying sulfuric acid point
From in tower；
(3) sulfuric acid knockout tower separates material liquid, and separating liquid is made and generates steam, separating liquid is then delivered to dilute sulphur
In sour concentration kettle；
(4) separating liquid is concentrated in dilute sulfuric acid concentration kettle, and concentrate is made and generates steam, and then concentrate is delivered to sour
It in heat exchanger and is transferred in acid cooler, steam is delivered in sulfuric acid knockout tower；
(5) acid cooler carries out cooling treatment to concentrate and is delivered in finished product pans；
(6) concentrate of finished product pans conveys dechlorination drying section；
Wherein the progress dividing wall type heat in sour heat exchanger exchanges material liquid with concentrate in step (4) in step (2)；
The steam that wherein sulfuric acid knockout tower generates in step (3) is delivered to exhaust gas cooler and is condensed, and condenses the condensation of generation
Liquid is delivered to chlorine tail gas washing tower through chlorine water storage tank；The gas that can not be condensed is delivered to three-level steam jet vacuum system and is taken out
Suction goes out, and the gas for aspirating discharge carries out cooling and the cooling coolant liquid generated is delivered to chlorine tail gas to wash by vacuum cooler
Wash tower；
Sewage disposal system outside battery limit (BL) is gone in the waste liquid conveying that wherein chlorine tail gas washing tower generates.
10. a kind of Waste Sulfuric Acid utilization process of dry chlorine gas according to claim 9, it is characterised in that:
Raw material in step (1) outside battery limit (BL) includes the material liquid of the Waste Sulfuric Acid containing chlorine.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910715665.3A CN110422827A (en) | 2019-08-05 | 2019-08-05 | A kind of the Waste Sulfuric Acid recycling device and technique of dry chlorine gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201910715665.3A CN110422827A (en) | 2019-08-05 | 2019-08-05 | A kind of the Waste Sulfuric Acid recycling device and technique of dry chlorine gas |
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| CN201910715665.3A Pending CN110422827A (en) | 2019-08-05 | 2019-08-05 | A kind of the Waste Sulfuric Acid recycling device and technique of dry chlorine gas |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114455551A (en) * | 2022-02-11 | 2022-05-10 | 宣达实业集团有限公司 | Concentration and reuse device for chlorine gas drying waste acid and control method thereof |
| CN115159462A (en) * | 2022-07-21 | 2022-10-11 | 宜宾海丰和锐有限公司 | Chlorine drying method for chlor-alkali production process |
| CN115448261A (en) * | 2022-08-18 | 2022-12-09 | 湖北东方化工有限公司 | Production method of waste sulfuric acid vacuum concentration treatment technology |
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| CN205953515U (en) * | 2016-08-18 | 2017-02-15 | 杭州中昊科技有限公司 | Regeneration system of peace and quiet spent acid of acetylene |
| CN108358176A (en) * | 2018-05-15 | 2018-08-03 | 杭州东日节能技术有限公司 | A kind of dilute sulfuric acid vacuum concentrating apparatus and method |
| CN210595271U (en) * | 2019-08-05 | 2020-05-22 | 贵州兰鑫石墨机电设备制造有限公司 | Waste sulfuric acid recycling device for drying chlorine |
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| US6387345B1 (en) * | 1995-09-26 | 2002-05-14 | Bayer Aktiengesellschaft | Process for working up reaction gases during the oxidation HCI to chlorine |
| CN205953515U (en) * | 2016-08-18 | 2017-02-15 | 杭州中昊科技有限公司 | Regeneration system of peace and quiet spent acid of acetylene |
| CN108358176A (en) * | 2018-05-15 | 2018-08-03 | 杭州东日节能技术有限公司 | A kind of dilute sulfuric acid vacuum concentrating apparatus and method |
| CN210595271U (en) * | 2019-08-05 | 2020-05-22 | 贵州兰鑫石墨机电设备制造有限公司 | Waste sulfuric acid recycling device for drying chlorine |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114455551A (en) * | 2022-02-11 | 2022-05-10 | 宣达实业集团有限公司 | Concentration and reuse device for chlorine gas drying waste acid and control method thereof |
| CN114455551B (en) * | 2022-02-11 | 2024-08-16 | 宣达实业集团有限公司 | Concentration recycling device for chlorine drying waste acid and control method thereof |
| CN115159462A (en) * | 2022-07-21 | 2022-10-11 | 宜宾海丰和锐有限公司 | Chlorine drying method for chlor-alkali production process |
| CN115448261A (en) * | 2022-08-18 | 2022-12-09 | 湖北东方化工有限公司 | Production method of waste sulfuric acid vacuum concentration treatment technology |
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