CN101486445B - Oxidation and blowout technological process and apparatus for bittern bromine process - Google Patents
Oxidation and blowout technological process and apparatus for bittern bromine process Download PDFInfo
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- CN101486445B CN101486445B CN2009100736654A CN200910073665A CN101486445B CN 101486445 B CN101486445 B CN 101486445B CN 2009100736654 A CN2009100736654 A CN 2009100736654A CN 200910073665 A CN200910073665 A CN 200910073665A CN 101486445 B CN101486445 B CN 101486445B
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- rotary packed
- bittern
- oxidation
- bromine
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- WKBOTKDWSSQWDR-UHFFFAOYSA-N Bromine atom Chemical compound [Br] WKBOTKDWSSQWDR-UHFFFAOYSA-N 0.000 title claims abstract description 72
- GDTBXPJZTBHREO-UHFFFAOYSA-N bromine Substances BrBr GDTBXPJZTBHREO-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 229910052794 bromium Inorganic materials 0.000 title claims abstract description 72
- 238000007254 oxidation reaction Methods 0.000 title claims abstract description 66
- 230000003647 oxidation Effects 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 41
- 241001131796 Botaurus stellaris Species 0.000 title claims description 65
- 239000007788 liquid Substances 0.000 claims abstract description 86
- 239000000460 chlorine Substances 0.000 claims abstract description 47
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 claims abstract description 45
- 229910052801 chlorine Inorganic materials 0.000 claims abstract description 45
- 238000003860 storage Methods 0.000 claims abstract description 34
- 239000000945 filler Substances 0.000 claims description 19
- 239000012530 fluid Substances 0.000 claims description 17
- CPELXLSAUQHCOX-UHFFFAOYSA-M Bromide Chemical compound [Br-] CPELXLSAUQHCOX-UHFFFAOYSA-M 0.000 claims description 14
- 238000012856 packing Methods 0.000 claims description 13
- 238000003672 processing method Methods 0.000 claims description 12
- 229910001220 stainless steel Inorganic materials 0.000 claims description 12
- 239000010935 stainless steel Substances 0.000 claims description 12
- 238000007664 blowing Methods 0.000 claims description 11
- BFKJFAAPBSQJPD-UHFFFAOYSA-N tetrafluoroethene Chemical group FC(F)=C(F)F BFKJFAAPBSQJPD-UHFFFAOYSA-N 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 9
- 230000002411 adverse Effects 0.000 claims description 7
- 238000010521 absorption reaction Methods 0.000 claims description 6
- 230000007797 corrosion Effects 0.000 claims description 5
- 238000005260 corrosion Methods 0.000 claims description 5
- 230000008676 import Effects 0.000 claims description 3
- 238000005304 joining Methods 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims 1
- 239000012267 brine Substances 0.000 abstract description 12
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 abstract description 12
- 238000000605 extraction Methods 0.000 abstract description 7
- 239000000243 solution Substances 0.000 abstract description 5
- 239000002253 acid Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- -1 bromonium ions Chemical class 0.000 abstract 1
- 150000003839 salts Chemical class 0.000 abstract 1
- 238000012546 transfer Methods 0.000 description 16
- 238000006243 chemical reaction Methods 0.000 description 9
- 230000001590 oxidative effect Effects 0.000 description 7
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000002699 waste material Substances 0.000 description 3
- 238000001704 evaporation Methods 0.000 description 2
- 229910052742 iron Inorganic materials 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 238000006479 redox reaction Methods 0.000 description 2
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 1
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 238000005452 bending Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003518 caustics Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 231100001010 corrosive Toxicity 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000003340 retarding agent Substances 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 125000006850 spacer group Chemical group 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 238000001256 steam distillation Methods 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 235000011149 sulphuric acid Nutrition 0.000 description 1
- 239000001117 sulphuric acid Substances 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
The invention pertains to the technical field of extraction of bromine from brine, more particularly relates to the technique of oxidation and blow-out during the process of extraction of bromine from brine, and a device thereof, which improve the oxidation rate and blow-out rate of bromine during the extraction process and reduce energy consumption. The method is as follows: acid brine and chlorine are introduced into a rotating packed bed I, and the formed oxidation solution and air enter a rotating packed bed II to blow out free bromine. The device comprises two rotating packed beds, the liquid inlet of the rotating packed bed I is connected with a pump and the gas inlet thereof is connected with a chlorine pipe; the rotating packed bed I and the rotating packed bed II are connected bya storage tank; and the gas inlet of the rotating packed bed II is connected with a fan. The method has the advantages of improving the oxidation rate of bromonium ions, the utilization ratio of chlorine and the blow-out rate of free bromine, and reducing chlorine adding ratio, chlorine consumption amount, the causticity of the device during the process after the extraction of bromine and the process of salt extraction, gas-liquid ratio and operation cost; and the device occupies less land and is easy to be start and shut off and maintained.
Description
Technical field
The invention belongs to the technical field of bittern bromine, be specifically related to oxidation and the processing method and the device that blow out in a kind of bittern bromine process.
Background technology
Bromine is an important chemical material, is widely used in efficient flame-retarding agent, refrigeration agent, oil and finishes fields such as liquid, medicine, fuel intermediate and chemical reagent.At present, the method for extraction bromine has following several from bittern: steam distillation, air blow out method (acid solution absorption process, alkali absorption method), resin adsorption method, extraction process and the precipitator method etc.At China's bittern resource bromine content this present situation on the low side, consider the reason of aspects such as production technology maturity and cost, the domestic air that generally adopts blows out acid solution absorption legal system bromine.This technology liquid chlorine consumption is big at present, power consumption is high, and the bromine yield is on the low side.This directly causes the waste of the energy and resource.Bromine is a kind of limited resources product, also is the very strong one-level corrosives of toxicity.Therefore, no matter how the angle from making full use of the natural resources still from point of view of environment protection, cuts down the consumption of energy, improves the bromine yield, and reducing to blow residue bromine in the bromine waste liquid all is noticeable problem to the destruction of environment and lower procedure equipment; And in this technology oxidation with blow out the operation outbalance, oxidation ratio and the size that blows out rate affect the raising of bromine yield to a great extent.
Summary of the invention:
The present invention to improve the oxidation ratio of bromine in the bittern bromine process and blows out rate in order to realize, the purpose that cuts down the consumption of energy provides oxidation and the processing method and the device that blow out in a kind of bittern bromine process.
The present invention adopts following technical scheme to realize:
Oxidation and the processing method that blows out in a kind of bittern bromine process is characterized in that step is as follows:
1) opens rotary packed bed I and rotary packed bed II, respectively, and regulate rotary packed bed I and rotary packed bed II rotating speed at 400～2000r/min;
2), acidifying bittern and chlorine are introduced rotary packed bed I by inlet mouth and fluid inlet respectively at normal temperatures; Joining chlorine rate (ratio of bromide anion in chlorine and the acidifying bittern) is 100～150%, in rotary packed bed I chlorine with bittern in bromide anion be oxidized to free bromine;
3), the oxidation liquid of oxidized bittern formation enters storage tank after the liquid outlet of rotary packed bed I is discharged;
4), oxidation liquid in the storage tank and air are entered rotary packed bed II by fluid inlet and the inlet mouth of rotary packed bed II respectively, the gas-liquid volume ratio of air and oxidation liquid is 50～300m
3/ m
3, air blows out free bromine in the oxidation liquid in rotary packed bed II;
5), brominated air enters absorption unit from the air outlet of rotary packed bed II free bromine absorbed, the bittern that blows behind the bromine is discharged from the liquid outlet of rotary packed bed II.
Bittern utilizes potential difference to realize to the conveying the rotary packed bed II from rotary packed bed I to storage tank again.The gas-to-liquid contact mode is cross-flow or adverse current.The bittern bromine content is 50～450mg/L.The pH value of acidifying bittern is 3～3.5.
Realize oxidation and the device that blows out processing method in the bittern bromine process, comprise the rotary packed bed I and the rotary packed bed II that have fluid inlet, liquid outlet, inlet mouth, air outlet, the fluid inlet of rotary packed bed I connects the pump of carrying acidifying bittern; The liquid outlet of rotary packed bed I connects the storage tank import, and the storage tank outlet links to each other with the fluid inlet of rotary packed bed II; The inlet mouth of rotary packed bed I connects the chlorine pipeline; The inlet mouth of rotary packed bed II connects the blower fan outlet.Device that contacts with liquid and pipeline are corrosion resistant material, and rotary packed bed filler is corrosion resistant stainless steel, tetrafluoroethylene and wire packing.
The super gravity field that the present invention utilizes rotary packed bed rotation to produce makes different alternate materials make enforceable contact movement, and liquid phase is dispersed into liquid film, brin or drop, and the gas-to-liquid contact specific surface area increases greatly; In high dispersive, high turbulence, mix and interface rapidly more under the news by force, liquid film or drop contact in the duct of bending with great speed of relative movement with gas, have greatly strengthened mass transfer process, and mass-transfer efficiency is than 1～3 order of magnitude of conventional tower equipment raising.
The present invention has following beneficial effect:
(1) oxidation operation employing of the present invention is rotary packed bed, has improved the oxidation ratio of bromide anion, makes chlorine utilization improve, reduce to join the chlorine rate, has reduced the chlorine consumption.
The conventional oxidation operation adopts static mixer, and chlorine and bittern and stream pass through this mixing tank, no turbulence and Forced Mixing process between gas-liquid, and interphase mass transfer efficient is low, causes to join the increase of chlorine rate, (being chlorine consumption height), and the oxidation ratio of bromide anion has only about 80%.And rotary packed bed be a kind of high efficient gas and liquid mass transfer apparatus, help strengthening contacting of chlorine and bittern, mass-transfer efficiency significantly improves, and obviously is increased to 90%～95% in identical oxidation ratio of joining bromide anion under the chlorine rate situation, the consumption of chlorine reduces.
(2) raising of bromide anion oxidation ratio has reduced and has put forward behind the bromine corrodibility of equipment in the operation and the operation of evaporating brine.
Under specific pH value, after the oxidation ratio of bromide anion improves, discharge and to enter the bromide anion that blows the bromine waste liquid on multiple solarization beach and obviously reduce from blowing out operation, having hindered superfluous chlorine continues to generate free bromine with the bromide anion reaction, free bromine is to the corrodibility of the metallic copper and the iron utmost point in the presence of water molecules thereby reduced, and the extent of corrosion of propeller pump in the beach is shone in alleviation again.
(3) the present invention blows out operation and adopts the rotary packed bed rate that blows out that has improved free bromine, has reduced vapour-liquid ratio, has reduced running cost.
Be used to blow out operation with rotary packed bed, under the rotary packed bed hypergravity environment that provides, the liquid less turbulence increases, liquid-gas interface is brought in constant renewal in, lower floor's liquid in the oxidation liquid reaches fluid surface rapidly, free bromine can fully be contacted with air within a short period of time, finish mass transfer process, make the rate of blowing out under identical vapour-liquid ratio, blow out 75%～85% of operation and be increased to 90%～95% by tradition.Because the characteristic that rotary packed bed gas phase drag is little and to blow out in the operation vapour-liquid ratio little, needed air quantity of the process that blows out and blast all reduce, thereby have reduced the power consumption of blower fan.
(4) material residence time in rotary packed bed extremely short (10～100ms), for blowing out operation, can in time the free bromine in the oxidation liquid be blown out, avoid the influence of hydrolysis to the stripping rate.
(5) compare with conventional tower equipment, rotary packed bed height is 1/5～1/10 of a conventional tower equipment only, and the energy consumption of liquid circulating pump is reduced, and has reduced floor space, is easy to the start-stop car, and is easy to maintenance.This situation such as bittern bromine of proposing bromine or periodical operation for distributing bittern resource is easy to implement.
Description of drawings
Fig. 1 is the schematic flow sheet (rotary packed bed with cross flow type is example) of oxidation and the processing method that blows out in the bittern bromine process.
Fig. 2 is cross flow type rotary packed bed (being that the gas-to-liquid contact mode is a cross-flow) structural representation
Fig. 3 is adverse current type rotary packed bed (being that the gas-to-liquid contact mode is an an adverse current) structure iron
Among the figure: the rotary packed bed I of 1-, the rotary packed bed II of 2-, 3-storage tank, 4-pump, 5-blower fan, 6-liquid meter I, 7-liquid meter II, 8-gas meter I, 9-gas meter II, 10-valve I, 11-valve II, 12-valve III, 13-valve IV, 14-frequency transformer I, 15-frequency transformer II
Among the figure: 16-motor, 17-shaft seal, 18-liquid distributor, 19-air outlet, 20-filler lower clapboard, 21-liquid outlet, 22-fluid inlet, 23-inlet mouth, 24-filler, 25-filler upper spacer, 26-shell, 27-rotor, 28-rotating shaft
Embodiment
In conjunction with the accompanying drawings the specific embodiment of the present invention is described further.
As Fig. 1, main device of the present invention comprises rotary packed bed I1, rotary packed bed II2 and storage tank 3.Acidifying bittern is squeezed among the rotary packed bed I1 by pump 4, and pump 4 is connected with the fluid inlet of rotary packed bed I1, and the liquid outlet of rotary packed bed I1 links to each other with the import of storage tank 3, and the outlet of storage tank 3 links to each other with the fluid inlet of rotary packed bed II2; Be the controlled liq flow, be connected with liquid meter I6 and liquid meter II7 between the pipeline of pump and rotary packed bed I1 and storage tank and rotary packed bed II2.The inlet mouth of rotary packed bed I1 links to each other with the chlorine line, and chlorine enters from the inlet mouth of rotary packed bed I1, and the outlet of blower fan 5 links to each other with the inlet mouth of rotary packed bed II2; On the chlorine pipeline and on the intake ducting of rotary packed bed II2 gas meter I8 and gas meter II9 are being housed respectively.
Concrete technical process is as follows:
A: open rotary packed bed I1, control its rotating speed at 400～2000r/min by frequency transformer I14, treat to open valve I10 after stable, regulator solution flowmeter body I6, with the pH value is that 3～3.5 acidifying bittern are squeezed in the rotary packed bed I1 by fluid inlet pipe introducing rotor internal cavity by pump 4 at normal temperatures, radially evenly be sprayed on the rotor inner edge through liquid distributor, under the effect of filler, acidifying bittern is dispersed into nano level film or fine mist in rotor; Open valve II11 again, adjustments of gas under meter I8, control is joined the chlorine rate 100%～150%, contacts with the chlorine that feeds, and redox reaction takes place, and bromide anion is oxidized to free bromine.
Wherein, bromide anion by the reaction equation of chlorine oxidation is: Cl
2+ Br
-→ Br
2+ Cl
-
B: owing to still have the minority redox reaction also carrying out in the oxidation liquid that spinning bed of packings I1 discharges, consider the overall oxidized degree of bromide anion, oxidation liquid is to be collected in the operation that blows out that enters next step in the storage tank 3 again under the dynamic action earlier in the potential difference with rotary packed bed I1 and storage tank 3, and storage tank 3 plays shock absorption herein.
C: open rotary packed bed II2, control its rotating speed at 400～2000r/min by frequency transformer II15, treat to open valve III12 after stable, adjustments of gas under meter II9, air is after metering delivered to rotary packed bed II2 inlet tube by blower fan 5, passes through packing layer vertically by its bottom under the effect of gaseous tension; Open valve IV13 again, regulator solution flowmeter body II7, the control vapour-liquid ratio is in 50～300m
3/ m
3Oxidation liquid is to introduce rotor internal cavity by the fluid inlet pipe under the dynamic action in the potential difference with storage tank 3 and rotary packed bed II2, radially evenly be sprayed on the rotor inner edge through liquid distributor, under the effect of filler, oxidation liquid is dispersed into nano level film or fine mist in rotor, realizes contacting with air, mass transfer, under the effect of the mass transfer force that gas, liquid two-phase concentration difference produce, free bromine is blown, and enters then to put forward operation behind the bromine, finishes the integrated artistic of bittern bromine.Remove bittern behind the free bromine and be thrown to shell by rotor and compile, leave rotary packed bed II2 through the leakage fluid dram pipe and enter the downstream process system of evaporating brine.
Wherein, free bromine is blown out this procedure expression by air and is from oxidation liquid:
Embodiment one: bittern bromine content 50mg/L, its main equipment: two rotary packed bed Stainless Steel Cloth fillers that adopt respectively, two rotary packed bed housings and storage tank all adopt the tetrafluoroethylene material.The gas-to-liquid contact mode is cross-flow.
With dilute sulphuric acid raw brine pH value is transferred to 3.Open rotary packed bed I, control its rotating speed at 400r/min by frequency transformer I, join the chlorine rate 120%, acidifying bittern contacts with chlorine in packing layer, and oxidizing reaction takes place; Oxidation liquid stays for some time in storage tank and treats that bromide anion joins under the chlorine rate oxidation and open rotary packed bed II in the back fully specific, controls its rotating speed at 800r/min by frequency transformer II, opens blower fan again, and the control vapour-liquid ratio is at 50m
3/ m
3Oxidation liquid contacts in filler with air, finishes mass transfer process, and free bromine blows out from bittern.Wherein, oxidation ratio is 70%, and the rate of blowing out is 60%.
Embodiment two: bittern bromine content 350mg/L, its main equipment: two rotary packed bed Stainless Steel Cloth fillers that adopt respectively, two rotary packed bed housings and storage tank all adopt stainless steel.The gas-to-liquid contact mode is cross-flow.
Raw brine pH value is transferred to 3.2, open rotary packed bed I, control its rotating speed at 600r/min by frequency transformer I, join the chlorine rate 130%, acidifying bittern contacts with chlorine in packing layer, and oxidizing reaction takes place; Open rotary packed bed II after oxidation liquid stays for some time in storage tank, control its rotating speed at 1000r/min by frequency transformer II, open blower fan again, the control vapour-liquid ratio is at 300m
3/ m
3Oxidation liquid contacts in filler with air, finishes mass transfer process, and free bromine is blown out from bittern.Wherein, oxidation ratio is 73%, and the rate of blowing out is 89%.
Embodiment three: bittern bromine content 250mg/L, its main equipment: two rotary packed bed Stainless Steel Cloth fillers that adopt respectively, two rotary packed bed housings and storage tank adopt stainless steel and tetrafluoroethylene material respectively.The gas-to-liquid contact mode is an adverse current.
Raw brine pH value is transferred to 3.3, open rotary packed bed I, control its rotating speed at 800r/min by frequency transformer I, join the chlorine rate 110%, acidifying bittern contacts with chlorine in packing layer, and oxidizing reaction takes place; Open rotary packed bed II after oxidation liquid stays for some time in storage tank, control its rotating speed at 600r/min by frequency transformer II, open blower fan again, the control vapour-liquid ratio is at 200m
3/ m
3Oxidation liquid contacts in filler with air, finishes mass transfer process, and free bromine is blown out from bittern.Wherein, oxidation ratio is 80%, and the rate of blowing out is 75%.
Embodiment four: bittern bromine content 50mg/L, its main equipment: two rotary packed bed tetrafluoroethylene corrugated plate packings that adopt respectively, two rotary packed bed housings and storage tank adopt tetrafluoroethylene and stainless steel respectively.The gas-to-liquid contact mode is cross-flow.
Raw brine pH value is transferred to 3.3, open rotary packed bed I, control its rotating speed at 1000r/min by frequency transformer I, join the chlorine rate 105%, acidifying bittern contacts with chlorine in packing layer, and oxidizing reaction takes place; Open rotary packed bed II after oxidation liquid stays for some time in storage tank, control its rotating speed at 400r/min by frequency transformer II, open blower fan again, the control vapour-liquid ratio is at 250m
3/ m
3Oxidation liquid contacts in filler with air, finishes mass transfer process, and free bromine is blown out from bittern.Wherein, oxidation ratio is 85%, and the rate of blowing out is 53%.
Embodiment five: bittern bromine content 450mg/L, its main equipment: two rotary packed bed polytetrafluoroethylstephanoporate stephanoporate plate fillers that adopt respectively, two rotary packed bed housings and storage tank adopt stainless steel and tetrafluoroethylene material respectively.The gas-to-liquid contact mode is an adverse current.
Raw brine pH value is transferred to 3.5, open rotary packed bed I, control its rotating speed at 1200r/min by frequency transformer I, join the chlorine rate 150%, acidifying bittern contacts with chlorine in packing layer, and oxidizing reaction takes place; Open rotary packed bed II after oxidation liquid stays for some time in storage tank, control its rotating speed at 1800r/min by frequency transformer II, open blower fan again, the control vapour-liquid ratio is at 110m
3/ m
3Oxidation liquid contacts in filler with air, finishes mass transfer process, and free bromine is blown out from bittern.Wherein, oxidation ratio is 90%, and the rate of blowing out is 95%.
Embodiment six: bittern bromine content 150mg/L, its main equipment: two rotary packed bed Stainless Steel Cloth fillers that adopt respectively, two rotary packed bed housings and storage tank adopt tetrafluoroethylene and stainless steel respectively.The gas-to-liquid contact mode is an adverse current.
Raw brine pH value is transferred to 3, open rotary packed bed I, control its rotating speed at 1800r/min by frequency transformer I, join the chlorine rate 102%, acidifying bittern contacts with chlorine in packing layer, and oxidizing reaction takes place; Open rotary packed bed II after oxidation liquid stays for some time in storage tank, control its rotating speed at 2000r/min by frequency transformer II, open blower fan again, the control vapour-liquid ratio is at 90m
3/ m
3Oxidation liquid contacts in filler with air, finishes mass transfer process, and free bromine is blown out from bittern.Wherein, oxidation ratio is 97%, and the rate of blowing out is 92%.
Embodiment seven: bittern bromine content 150mg/L, its main equipment: two rotary packed bed tetrafluoroethylene corrugated plate packings that adopt respectively, two rotary packed bed housings and storage tank adopt stainless steel and tetrafluoroethylene material respectively.The gas-to-liquid contact mode is cross-flow.
Raw brine pH value transfers to 3.2, opens rotary packed bed I, controls its rotating speed at 2000r/min by frequency transformer I, joins the chlorine rate 100%, and acidifying bittern contacts with chlorine in packing layer, and oxidizing reaction takes place; Open rotary packed bed II after oxidation liquid stays for some time in storage tank, control its rotating speed at 1200r/min by frequency transformer II, open blower fan again, the control vapour-liquid ratio is at 150m
3/ m
3Oxidation liquid contacts in filler with air, finishes mass transfer process, and free bromine is blown out from bittern.Wherein, oxidation ratio is 93%, and the rate of blowing out is 85%.
Claims (7)
1. oxidation and the processing method that blows out in the bittern bromine process is characterized in that step is as follows:
1) open rotary packed bed I and rotary packed bed II, respectively, and the rotating speed of regulating rotary packed bed I and rotary packed bed II is at 400～2000r/min;
2), acidifying bittern and chlorine are introduced rotary packed bed I by inlet mouth and fluid inlet respectively at normal temperatures, joining the chlorine rate is 100～150%, in rotary packed bed I chlorine with bittern in bromide anion be oxidized to free bromine;
3), the oxidation liquid of oxidized bittern formation enters storage tank after the liquid outlet of rotary packed bed I is discharged;
4), oxidation liquid in the storage tank and air are entered rotary packed bed II by fluid inlet and the inlet mouth of rotary packed bed II respectively, the gas-liquid volume ratio of air and oxidation liquid is 50～300m
3/ m
3, air blows out free bromine in the oxidation liquid in rotary packed bed II;
5), brominated air enters absorption unit from the air outlet of rotary packed bed II free bromine absorbed, the bittern that blows behind the bromine is discharged from the liquid outlet of rotary packed bed II.
2. oxidation and the processing method that blows out is characterized in that bittern utilizes potential difference to realize to the conveying the rotary packed bed II from rotary packed bed I to storage tank again in the bittern bromine process according to claim 1.
3. oxidation and the processing method that blows out is characterized in that described gas-to-liquid contact mode is cross-flow or adverse current in a kind of bittern bromine process according to claim 1.
4. oxidation and the processing method that blows out is characterized in that described bittern bromine content is 50～450mg/L in a kind of bittern bromine process according to claim 1.
5. oxidation and the processing method that blows out in a kind of bittern bromine process according to claim 1, the pH value that it is characterized in that described acidifying bittern is 3～3.5.
6. realize oxidation and the device that blows out processing method in the described bittern bromine process of one of claim 1～5 for one kind, it is characterized in that comprising the rotary packed bed I (1) and the rotary packed bed II (2) that have fluid inlet, liquid outlet, inlet mouth, air outlet, the fluid inlet of rotary packed bed I (1) connects the pump (4) of carrying acidifying bittern; The liquid outlet of rotary packed bed I (1) connects storage tank (3) import, and storage tank (3) outlet links to each other with the fluid inlet of rotary packed bed II (2); The inlet mouth of rotary packed bed I (1) connects the chlorine pipeline; The inlet mouth of rotary packed bed II (2) connects blower fan (5) outlet.
7. oxidation and blowing out device in the bittern bromine process according to claim 6 is characterized in that the device and the pipeline that contact with liquid are corrosion resistant material, and rotary packed bed filler is corrosion resistant stainless steel, tetrafluoroethylene and wire packing.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100736654A CN101486445B (en) | 2009-01-14 | 2009-01-14 | Oxidation and blowout technological process and apparatus for bittern bromine process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009100736654A CN101486445B (en) | 2009-01-14 | 2009-01-14 | Oxidation and blowout technological process and apparatus for bittern bromine process |
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| Publication Number | Publication Date |
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| CN101486445B true CN101486445B (en) | 2010-12-08 |
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Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101691239B (en) * | 2009-09-30 | 2013-02-13 | 达州市恒成能源（集团）有限责任公司 | Comprehensive utilization method for bittern |
| CN104229738B (en) * | 2014-10-08 | 2016-06-15 | 潍坊北海绿洲太阳能科技股份有限公司 | A kind of vacuum distillation method extracts the method for bromine from sea water |
| CN108529561B (en) * | 2018-03-29 | 2020-11-17 | 山东特检科技有限公司 | Method and device for improving bromine stripping rate and extraction rate in air blowing method |
| CN111039447B (en) * | 2019-12-11 | 2022-06-10 | 中北大学 | Method and device for treating ammonia nitrogen wastewater by using supergravity to strengthen |
| CN112266119A (en) * | 2020-09-01 | 2021-01-26 | 中北大学 | Bromine extraction process and device for waste water generated in production of brominated butyl rubber |
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2009
- 2009-01-14 CN CN2009100736654A patent/CN101486445B/en not_active Expired - Fee Related
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