CN103964382A - Bittern bromine-blowing process - Google Patents
Bittern bromine-blowing process Download PDFInfo
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- CN103964382A CN103964382A CN201410242581.XA CN201410242581A CN103964382A CN 103964382 A CN103964382 A CN 103964382A CN 201410242581 A CN201410242581 A CN 201410242581A CN 103964382 A CN103964382 A CN 103964382A
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- bittern
- tower
- bromine
- absorption
- liquid
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Abstract
The invention discloses a bittern bromine-blowing process comprising oxidation, blowout, absorption and distillation. A blowout tower and a mixer are used in the process. The process comprises the steps of selecting bittern of which the bromine content is 1000-2500ppm as a raw material, and adjusting the pH value to 2-3.5 before the bittern raw material is fed into the blowout tower; and performing a bittern oxidation stage and a blowout stage on the bittern, then feeding the bittern into an absorption tower to perform concurrent flow gas liquid contact with absorption completed liquid, and performing absorption operation, wherein the bromine content of the absorption completed liquid is 80-100g/L. The bromine is extracted from the mother solution (bittern) of sea salt production by adopting the oxidation and blowout method, and the blowout tower and the mixer are used in the process, so that the bromine extraction process is scientific, the yield of the bromine is 2.5 times that of a water vapor distillation method, and the power consumption of the process is 60% of that of an intermediate bittern bromine-blowing process. The total extraction rate is over 85%. The process initiates the process equipment parameters of high bromine content, high viscosity and high specific gravity raw material condition, and is used for design and production.
Description
Technical field
The present invention relates to a kind of bromine extractive technique, particularly a kind of bittern blows bromine technique, this technique takes oxidation and the method that blows out from the mother liquor (bittern) of Salt production, to extract bromine, and the raw material that is also applicable to other brominated amounts higher (1000-2500ppm) extracts bromine.
Background technology
Bromine is important industrial chemicals, is mainly used in the aspects such as the energy, automobile, medicine, agricultural chemicals, dyestuff, fire retardant, fire-fighting medium, refrigeration agent, sensitive materials.
Bromine is mainly taken from seawater, concentrated seawater (comprising subsurface brine).The brominated amount 65ppm of seawater; The brominated amount 200ppm of Shandong Province of China subsurface brine; Israel Dead Sea 3000-10000ppm; India 3000-5000ppm; Ukraine shallow sea 600-1000ppm; U.S. Deep Formation Brine 2000-3000ppm.
700,000 tons of world's bromine production capacities, wherein 280,000 tons, Israel, accounts for 40%, and 210,000 tons, U.S. accounts for 30%, and 100,000 tons, China accounts for 15%, 20,000 tons, India, 20,000 tons, Japan, 1.2 ten thousand tons, Ukraine, other producers add up to 5.8 ten thousand tons.The raw material of the U.S. is taken from Deep Formation Brine, and cost is higher, and its production capacity declines the speed with 2%-3%; India's production capacity will expand 50,000 tons to.
Shandong Province accounts for 90% of national output, is controlling national market, but because its raw material reserves and grade decline year by year, output is on a declining curve.
Israel has bromine production technology and Dead Sea resource (Dead Sea Jin Wei Israel and two countries of Jordan have, and 80 kilometers of length are wide 18 kilometers, 400 meters, innermost, approximately 900,000,000 tons of bromine reserves), is controlling bromine market, the world.
China's bromine production major part combines with Salt production, in bittern from Salt production, extract, before the eighties, from dense halogen (7000-8000ppm), adopt extraction by steam distillation, because sea salt is produced the outdoor beach Tanaka of big area, bittern seepage loss is large, before extracting bromine, most of bromine resource has been fallen with bittern seepage loss, bromine output is not high, and with steam distillation from elementary bittern (100ppm), in middle rank bittern (200-300ppm), extract bromine cost too high, bring into use the nineties and blow bromine technology extract bromine from elementary bittern and intermediate bittern.
Mother liquor-the bittern (bittern) of Salt production is (2000ppm) after reeve solarization is concentrated at present, enter salt chemical engineering Workshop Production Repone K, bromine (steam distillation), magnesium chloride, but because shining the infiltration capacity that still has 30%-40% left and right in concentration process in bittern beach, and in KCl production, also cause the loss of bromine, therefore while extracting bromine to the dense halogen of last employing steam distillation, output is only for bittern blows 40% of bromine, that is to say and adopt bittern to blow after bromine technology, output is 2.5 times of left and right of steam distillation output.
The domestic technology information that does not still have bittern to blow bromine at present.
Summary of the invention
Goal of the invention of the present invention is the defect for prior art, provides a kind of bittern of the throughput that is applicable to 200-1000 ton/year, single cover to blow bromine technique.
The present invention adopts following technical scheme to realize:
A kind of bittern blows bromine technique, comprises oxidation, blows out, absorption, distil process, also comprises the stripping tower, the mixing tank that in technological process, use, and described processing step is as follows:
1) selecting the bittern of brominated amount 1000-2500ppm is raw material, before raw material bittern enters stripping tower, adjusts ph value by acid solution, by mixing tank, ph is adjusted to 2-3.5;
2) oxidation stage: bittern enters before stripping tower, the bittern that is 2-3.5 by ph value adds chlorine oxidation, joins chlorine rate control 110-130%, and mixes by mixing tank; Complex acid concentration 10-13%, bittern fully contacts with chlorine, and oxidation ratio is more than 90%;
3) blow out the stage: in stripping tower, parse the free bromine of gaseous state by gas-liquid counter current, air and bittern volume flow ratio 500-700:1, the rate that blows out is more than 95%;
4) by stripping tower discharge oxidized after free bromine gas and sulfurous gas be mixed into absorption tower, complete liquid with absorption and flow gas-to-liquid contact and carry out absorption operation, having absorbed the brominated amount of liquid is 80-100g/L;
5) having absorbed liquid enters distillation tower and carries out distillation procedure, tower top temperature control 80-85
oc; The thick bromine distilling out adopts after condensation to be washed bromine 2 times and improves the quality of products, and tail gas reclaims through recovery tower;
6) stripping tower, absorption tower, catch foam tower, gas blower and form gas phase closed circulation, improve bromine and obtain rate, avoid environmental pollution.
As preferred version, in described stripping tower, the vapor-liquid ratio of air flow quantity and bittern flow is 500-700:1.
As preferred version, the described tower height 13-16m of stripping tower, tower diameter 3-5m, specific liquid rate 8-13m
3/ m
2h.
As preferred version, the mixed gas pipeline height between described stripping tower to absorption tower is 13.5-15m.
As preferred version, height 7m at the bottom of described recovery tower tower, exports low 1m than distillation tower.
Adopt technique scheme, compared with prior art, the invention solves extraction bromine cost too high, KCl production causes the loss of bromine, while adopting the dense halogen of steam distillation to extract bromine, the problem yielding poorly, this technique is owing to adopting oxidation and the method that blows out to extract bromine from the mother liquor (bittern) of Salt production, the stripping tower, the mixing tank that in technological process, use, extract bromine craft science, output is 2.5 times of steam distillation, current consumption be intermediate bittern blow bromine technique 60%.Total extraction yield is more than 85%.This technique has been started the processing unit parameter of high brominated amount, high viscosity, high specific gravity material condition, for design and production.
Brief description of the drawings
Fig. 1 is process flow sheet of the present invention.
Fig. 2 is that sulfurous gas of the present invention is drawn process flow sheet.
Fig. 3 is liquid chlorine gasification process schema of the present invention.
In figure, bittern pump 1, mixing tank 2, stripping tower 3, gas blower 4, mist eliminator 5, absorbs
tower 6, recycle pump 7, completes liquid storage tank 8, completes liquid pump 9, and distillation tower 10, the second separating bottles 11, the second are washed bromine device 12, the first separating bottles 13, the first and are washed bromine device 14, condenser 15, recovery tower 16, filler 17, spray equipment 18, gas mixing pipe 19,
interchanger 20,incinerator
21, scrubber tower
22, heat exchanger
23, recycle pump
24, collecting tower
25, recycle pump
26, lye vat
27, chlorine cylinder
28, automatic linkage device
29, cleaner
30, collecting flexible pipe
31.
Embodiment
Below in conjunction with accompanying drawing, the present invention will be further described.
The invention discloses a kind of high density bittern and blow bromine technique, the method that this process using is oxidized, blows out, absorbs, distills is carried bromine to bittern (High Concentration Brine is referred to as bittern), and concrete technology step is:
1) selecting the bittern of brominated amount 1000-2500ppm is raw material, before raw material bittern enters stripping tower, adjusts ph value by acid solution, by mixing tank, ph is adjusted to 2-3.5;
2) oxidation stage: bittern pumps into efficient solution-air, liquid-liquid mixing mixing tank 2 with bittern pump 1, complex acid concentration 10-13%, controls ph=2.0-3.5, joins chlorine rate 110-130%, fully contacts with chlorine at the interior bittern of mixing tank 2, and oxidation ratio is more than 90%.
3) blow out the stage: enter stripping tower 3 through snperoxiaized bittern, the described tower height 13-16m of stripping tower, tower diameter 3-5m, there is spray equipment 18 top in stripping tower 3, specific liquid rate 8-13m
3/ m
2h, filler 17 is housed in stripping tower 3, the height 11-14m of filler 17, diameter 3-5m, in stripping tower, parse the free bromine of gaseous state by gas-liquid counter current, the vapor-liquid ratio of air flow quantity and bittern flow is 500-700:1(air and bittern volume flow ratio 500-700:1), the rate that blows out of stripping tower 3 is more than 95%.
4) absorption stage: the sulfurous gas blowing out through stripping tower 3 enters gas mixing pipe 19, sends into absorption tower 6 by gas mixing pipe 19, and absorption tower 6 is highly
13-16m, diameter 3-5m, spray equipment 18 is installed in the top on absorption tower 6, and filler 17 is housed in absorption tower 6.In absorption tower 6 interior employing filler mode, sulfurous gas being carried out to gas-liquid mass transfer absorbs, by stripping tower discharge oxidized after free bromine gas and sulfurous gas be mixed into absorption tower, complete liquid with absorption and flow gas-to-liquid contact and carry out absorption operation, it is 80-100g/L that absorption completes the brominated amount of liquid, absorption rate with blow out speeds match balance.
5) the mixed gas pipeline between stripping tower and absorption tower: the mixed gas pipeline height between stripping tower 3 to absorption tower 6 is 13.5-15m, than the long 6-7m of general design.By changing layout, lengthen pipeline distance, improve mixed effect, be conducive to the absorption of bromine vapor.
6) the distillation stage: absorbed liquid and entered distillation tower and carry out distillation procedure, tower top temperature control 80-85
oc; The thick bromine distilling out adopts secondary to wash bromine to improve the quality of products after condensation, and tail gas reclaims through recovery tower.
7) the distillation stage: heat reclaim unit is set, reclaims the heat of distillation mother liquor.
8) recovery stage: height 7m at the bottom of recovery tower 16 towers, export low 1m than distillation tower, lower 1.5m than general design.By suitable reduction recovery tower 16 positions, reduce factory building height, reduce construction investment.
9) stripping tower, absorption tower, catch foam tower, gas blower and form gas phase closed circulation, improve bromine and obtain rate, avoid environmental pollution.
This technique bromine extraction yield is more than 85%.
main processes is shown in Fig. 1:
1. bittern is passed to mixing tank 2 by bittern pump 1, after mixing, carries out oxidizing reaction with concentration 10-13% acid solution and chlorine, and pH controls 2-3.5, and chlorine rate 110-130% is joined in the control of chlorine add-on.In mixing tank 2 and transport pipe, carry out afterwards oxidizing reaction, reaction formula 2Br
-+ Cl
2=2 Cl
-+ Br
2, the bromide anion in bittern is oxidized to liquid free bromine molecule.
2. the bittern after oxidation evenly sprays by spray equipment 18 from stripping tower 3 tops, contact with the air inversion that gas blower 4 is blown into through each layer of filler 17, carry out the mass transfer process of liquid-gas interface, molecular bromine liquid in bittern is resolved in air, discharge from stripping tower 3 tops.
3. the brominated air (having a small amount of chlorine molecule) that discharge at stripping tower 3 tops, with produce operation from the sulfurous gas of gas mixing pipe 19 and carry the sulfurous gas of coming to mix to enter absorption tower 6, complete liquid stream with the absorption under evenly spraying by spray equipment 18, the liquid-gas interface providing through each layer of filler 17, airborne molecular bromine is reduced into bromide anion and proceeds in liquid phase, reduction reaction formula Br
2+ SO
2+ 2H
2o=2HBr+H
2sO
4.
4. the gas phase (being mainly air) after absorbing is carried out gas-liquid separation through catching foam tower 5, is blown into stripping tower 3 by gas blower 4.
5. the liquid phase (absorption completes liquid) after absorbing is squeezed into absorption tower 6 through recycle pump 7, so repeatedly absorbs, to be absorbed when completing liquid concentration and reaching 80-100gBr/L, has entered liquid storage tank 8.According to completing liquid concentration and quantity situation, in absorption tower 6, supplement fresh water in time.
6. complete liquid and absorb after heat by interchanger 20 through completing liquid pump 9, enter the packing layer 17 in distillation tower 10 towers from distillation tower 10 tops by spray equipment 18; Distillation tower 10 bottoms enter steam and chlorine, and complete bromide anion in liquid and react and be transformed into liquid bromine molecule, reaction formula 2HBr+Cl
2=Br
2+ 2HCl.
The gas phase that complete liquid and bottom rising dirty from top carried out mass-and heat-transfer, constantly the liquid bromine molecule completing in liquid is proceeded to gas phase, water vapour in gas phase progressively condensation proceed to liquid phase, the gas phase (being mainly gaseous bromine molecule and water vapour) distilling out changes the bromine water mixture containing part bromine water into through condenser 15, after the first washing device 14 carries out back washing, entering into the first separating bottle 13 separates bromine water, enter into again the second washing device 12 and carry out secondary back washing, then enter into after the second separating bottle 11 separates and become finished product.
Recovery tower 16 is for reclaiming bromine gas and the chlorine of a small amount of gas phase, absorbs liquid for completing liquid, squeezes into recovery tower through completing liquid pump 9, returns in distillation tower 10 towers after completing absorption operation.
auxiliary process process: sulfurous gas is produced and seen Fig. 2
1. sheet sulphur is delivered to incinerator 21 by metering device, and air is compressed in incinerator 21 and is participated in burning by roots blower, reaction formula S+O
2=SO
2.
2. the sulfur dioxide gas after burning enters scrubber tower
22lower the temperature and remove that impurity is laggard to be entered to participate in next step absorption reaction to mixed gas pipeline 19.
3. the liquid phase after gas washing is acid solution, by recycle pump Reusability, and approach heat exchanger
23remove heat.
4. the acid solution of gas washing is passed through recycle pump
24be delivered to mixing tank 2 and carry out complex acid.
5. according to acid strength situation, supplement in time fresh water to scrubber tower.
auxiliary process process: chlorine preparing is shown in Fig. 3
1. liquid chlorine is from chlorine cylinder
28enter vaporizer
30in complete gasification.
2. the mixing tank 2 that the chlorine after gasifying enters into Fig. 1 participates in oxidizing reaction.
3. chlorine cylinder
28outlet has automatic linkage device
29, after breaking down, can close by automatic emergency.
4. work as chlorine cylinder
28when leakage, can push lye vat
27process.
5. reveal the chlorine spreading by collecting tower in air
25, recycle pump
26, lye vat
27, collecting flexible pipe
31the collecting system forming is processed.
main technical data and technical characterstic:
1. vapour-liquid ratio 500-700:1;
2. specific liquid rate 8-13m
3/ m
2h, makes it be applicable to bittern and blows bromine;
3. 2 covers are set and wash bromine device, make quality product contain pure being stabilized in more than 99.7%;
4. adjust stripping tower, absorption tower, catch foam tower layout, will catch foam tower and be placed in centre, strengthen the distance on stripping tower and absorption tower, improve reaction times and effect;
5. bittern acidity pH2-3.5 after acidifying;
6. absorbed the brominated amount 80-100g/l of liquid;
7. distillation tower goes out bromine mouth temperature 80-85 DEG C;
8. oxidation ratio >90, blows out rate >, and 95%, specific absorption 100%, steam rate >99%, bromine is always obtained rate >85%.
9. 7) stripping tower, absorption tower, catch foam tower, gas blower forms gas phase closed circulation, improves bromine and obtains rate, avoids environmental pollution.
Above-described embodiment has only been expressed one embodiment of the present invention, but can not therefore be interpreted as limitation of the scope of the invention.It should be pointed out that for the person of ordinary skill of the art, without departing from the inventive concept of the premise, can also make some distortion and improvement, these all belong to protection scope of the present invention.
Claims (5)
1. bittern blows a bromine technique, comprises oxidation, blows out, absorption, distil process, also comprises the stripping tower, the mixing tank that in technological process, use, it is characterized in that, described processing step is as follows:
1) selecting the bittern of brominated amount 1000-2500ppm is raw material, before raw material bittern enters stripping tower, adjusts ph value by acid solution, by mixing tank, ph is adjusted to 2-3.5;
2) oxidation stage: bittern enters before stripping tower, the bittern that is 2-3.5 by ph value adds chlorine oxidation, joins chlorine rate control 110-130%, and mixes by mixing tank; Complex acid concentration 10-13%, bittern fully contacts with chlorine, and oxidation ratio is more than 90%;
3) blow out the stage: in stripping tower, parse the free bromine of gaseous state by gas-liquid counter current, air and bittern volume flow ratio 500-700:1, the rate that blows out is more than 95%;
4) by stripping tower discharge oxidized after free bromine gas and sulfurous gas be mixed into absorption tower, complete liquid with absorption and flow gas-to-liquid contact and carry out absorption operation, having absorbed the brominated amount of liquid is 80-100g/L;
5) having absorbed liquid enters distillation tower and carries out distillation procedure, tower top temperature control 80-85
oc; The thick bromine distilling out adopts secondary to wash bromine to improve the quality of products after condensation, and tail gas reclaims through recovery tower;
6) stripping tower, absorption tower, catch foam tower, gas blower and form gas phase closed circulation, improve bromine and obtain rate, avoid environmental pollution.
2. blow bromine technique according to the bittern described in claim 1, it is characterized in that, in described stripping tower, the vapor-liquid ratio of air flow quantity and bittern flow is 500-700:1.
3. blow bromine technique according to the bittern described in claim 1, it is characterized in that, the described tower height 13-16m of stripping tower, tower diameter 3-5m, specific liquid rate 8-13m
3/ m
2h.
4. blow bromine technique according to the bittern described in claim 1, it is characterized in that, the horizontal mixed gas pipeline height between described stripping tower to absorption tower is 13.5-15m.
5. blow bromine technique according to the bittern complete set described in claim 1, it is characterized in that, at the bottom of described recovery tower tower, height is 7m, exports low 1m than distillation tower.
Priority Applications (1)
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|---|---|---|---|
| CN201410242581.XA CN103964382A (en) | 2014-06-04 | 2014-06-04 | Bittern bromine-blowing process |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201410242581.XA CN103964382A (en) | 2014-06-04 | 2014-06-04 | Bittern bromine-blowing process |
Publications (1)
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|---|---|
| CN103964382A true CN103964382A (en) | 2014-08-06 |
Family
ID=51234455
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|---|---|---|---|
| CN201410242581.XA Pending CN103964382A (en) | 2014-06-04 | 2014-06-04 | Bittern bromine-blowing process |
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Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104229739A (en) * | 2014-10-09 | 2014-12-24 | 山东天一化学股份有限公司 | Processing method for extracting bromine from brine by composite blowing and absorbing method |
| CN104310311A (en) * | 2014-10-09 | 2015-01-28 | 山东天一化学股份有限公司 | Method for extracting bromine from brine |
| CN104627964A (en) * | 2015-01-14 | 2015-05-20 | 崔鑫 | Method for preparing bromine by using brine |
| CN105460895A (en) * | 2015-12-30 | 2016-04-06 | 山东昌邑廒里盐化有限公司 | Novel bromine production device |
| CN105600753A (en) * | 2015-12-30 | 2016-05-25 | 山东昌邑廒里盐化有限公司 | Method for extracting bromine from brine |
| WO2016132376A3 (en) * | 2015-02-19 | 2016-12-01 | Agrocel Industries Limited | Process for preparation of hydrobromic acid |
| CN107892276A (en) * | 2017-12-25 | 2018-04-10 | 潍坊兴泰电气有限公司 | One kind energy-conservation bromine production system |
| CN108862198A (en) * | 2018-08-22 | 2018-11-23 | 天津海晶科技发展有限公司 | The automatic adjustment technique of bromine Reducing and absorption water processed |
| CN109650342A (en) * | 2019-02-22 | 2019-04-19 | 唐山海港旭宁化工有限公司 | Pressure-vaccum tower group |
| CN111362343A (en) * | 2018-12-26 | 2020-07-03 | 国家海洋局天津海水淡化与综合利用研究所 | Method and equipment for extracting bromine from seawater by air blowing method |
| CN111686550A (en) * | 2019-03-11 | 2020-09-22 | 自然资源部天津海水淡化与综合利用研究所 | Packing sheet for extracting bromine by air blowing method, efficient packing, and preparation method and application thereof |
| CN112007586A (en) * | 2019-05-28 | 2020-12-01 | 自然资源部天津海水淡化与综合利用研究所 | Groove type liquid distributor for bromine extraction blow-out tower and application thereof |
| CN112010261A (en) * | 2019-05-28 | 2020-12-01 | 自然资源部天津海水淡化与综合利用研究所 | Novel air blowing method bromine extraction method and equipment |
| CN112010262A (en) * | 2019-05-28 | 2020-12-01 | 自然资源部天津海水淡化与综合利用研究所 | Improved bromine extraction method and equipment by air blowing method |
| CN116161622A (en) * | 2023-04-25 | 2023-05-26 | 天津长芦汉沽盐场有限责任公司 | Method for preparing bromine by using carnallite mother liquor |
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Cited By (23)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104310311A (en) * | 2014-10-09 | 2015-01-28 | 山东天一化学股份有限公司 | Method for extracting bromine from brine |
| CN104229739B (en) * | 2014-10-09 | 2016-08-17 | 山东天一化学股份有限公司 | A kind of compound pressure-vaccum extracts the process of bromine in bittern |
| CN104229739A (en) * | 2014-10-09 | 2014-12-24 | 山东天一化学股份有限公司 | Processing method for extracting bromine from brine by composite blowing and absorbing method |
| CN104627964A (en) * | 2015-01-14 | 2015-05-20 | 崔鑫 | Method for preparing bromine by using brine |
| CN104627964B (en) * | 2015-01-14 | 2017-01-25 | 崔鑫 | Method for preparing bromine by using brine |
| US10626015B2 (en) | 2015-02-19 | 2020-04-21 | Agrocel Industries Limited | Process for preparation of hydrobromic acid |
| WO2016132376A3 (en) * | 2015-02-19 | 2016-12-01 | Agrocel Industries Limited | Process for preparation of hydrobromic acid |
| CN107531480A (en) * | 2015-02-19 | 2018-01-02 | 阿戈洛赛尔实业有限公司 | Hydrobromic acid preparation method |
| CN107531480B (en) * | 2015-02-19 | 2020-12-18 | 阿戈洛赛尔实业有限公司 | Preparation method of hydrobromic acid |
| CN105460895A (en) * | 2015-12-30 | 2016-04-06 | 山东昌邑廒里盐化有限公司 | Novel bromine production device |
| CN105600753A (en) * | 2015-12-30 | 2016-05-25 | 山东昌邑廒里盐化有限公司 | Method for extracting bromine from brine |
| CN107892276A (en) * | 2017-12-25 | 2018-04-10 | 潍坊兴泰电气有限公司 | One kind energy-conservation bromine production system |
| CN108862198A (en) * | 2018-08-22 | 2018-11-23 | 天津海晶科技发展有限公司 | The automatic adjustment technique of bromine Reducing and absorption water processed |
| CN111362343A (en) * | 2018-12-26 | 2020-07-03 | 国家海洋局天津海水淡化与综合利用研究所 | Method and equipment for extracting bromine from seawater by air blowing method |
| CN109650342A (en) * | 2019-02-22 | 2019-04-19 | 唐山海港旭宁化工有限公司 | Pressure-vaccum tower group |
| CN111686550A (en) * | 2019-03-11 | 2020-09-22 | 自然资源部天津海水淡化与综合利用研究所 | Packing sheet for extracting bromine by air blowing method, efficient packing, and preparation method and application thereof |
| CN111686550B (en) * | 2019-03-11 | 2022-05-06 | 自然资源部天津海水淡化与综合利用研究所 | Packing sheet for extracting bromine by air blowing method, efficient packing, and preparation method and application thereof |
| CN112007586A (en) * | 2019-05-28 | 2020-12-01 | 自然资源部天津海水淡化与综合利用研究所 | Groove type liquid distributor for bromine extraction blow-out tower and application thereof |
| CN112010261A (en) * | 2019-05-28 | 2020-12-01 | 自然资源部天津海水淡化与综合利用研究所 | Novel air blowing method bromine extraction method and equipment |
| CN112010262A (en) * | 2019-05-28 | 2020-12-01 | 自然资源部天津海水淡化与综合利用研究所 | Improved bromine extraction method and equipment by air blowing method |
| CN112010262B (en) * | 2019-05-28 | 2023-08-15 | 自然资源部天津海水淡化与综合利用研究所 | Improved bromine extraction method and device by air blowing method |
| CN116161622A (en) * | 2023-04-25 | 2023-05-26 | 天津长芦汉沽盐场有限责任公司 | Method for preparing bromine by using carnallite mother liquor |
| CN116161622B (en) * | 2023-04-25 | 2024-01-02 | 天津长芦汉沽盐场有限责任公司 | Method for preparing bromine by using carnallite mother liquor |
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Application publication date: 20140806 |