CN102060312A - Method and device for preventing bittern delivery pipeline from scaling - Google Patents
Method and device for preventing bittern delivery pipeline from scaling Download PDFInfo
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- CN102060312A CN102060312A CN 201010544094 CN201010544094A CN102060312A CN 102060312 A CN102060312 A CN 102060312A CN 201010544094 CN201010544094 CN 201010544094 CN 201010544094 A CN201010544094 A CN 201010544094A CN 102060312 A CN102060312 A CN 102060312A
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Abstract
The invention discloses a method for preventing a bittern delivery pipeline from scaling. The method is characterized by comprising the following steps of: directly inputting bittern output from a mining area into a cooling tower for cooling; delivering bittern output from the cooling tower to a reaction pot, wherein in the reaction pot, calcium sulfate molecules in the bittern react with gypsum seed crystals and are adhered on the suspended gypsum seed crystals so that the saturation degree of calcium sulfate in the bittern is reduced; inputting the bittern output from the reaction pot into a precipitating vat; after separated calcium sulfate precipitate is precipitated, delivering a supernate of which the engineering experience value of the supersaturation degree of the calcium sulfate is smaller than or equal to 1.02 into a bittern storage vat, and then delivering to enterprises for subsequent processing; delivering supernates which do not conform to the bittern delivery requirement into a diluting pot; and adding fresh water to dilute or adding soda ash to separate out carbon ions in the form of calcium carbonate precipitate so as to reduce the content of calcium carbonate and further eliminate the supersaturation degree of the calcium carbonate in the bittern. The method solves the scaling problem of the calcium carbonate on the delivery pipeline and improves the bittern delivery capacity and efficiency of the bittern delivery pipeline.
Description
Technical field
The present invention relates to a kind of method and corresponding device thereof that prevents the calcium sulfate composition of bittern in the transport pipe fouling, belong to the salt industry field.
Background technology
Because of containing a certain amount of calcium sulfate, in its course of conveying, there is the calcium sulfate scaling phenomenon in the brine pipeline road, usually causes the obstruction of pipeline in the halogen of sodium sulfate type ore deposit, causes transport capacity to descend, and energy consumption increases.Calcium sulfate dirt quality is hard, and adhere firmly is difficult to remove.In general, industrial have three kinds by the method that suppresses calcium sulfate scaling:
(1) chemical method: this method is used more general, generally is to be the fouling component to be separated in advance reach the purpose that suppresses fouling from system by changing the process operation conditioned disjunction.The operational condition of change process comprises temperature, concentration, pH value and solution composition.Generally be effectively to stop the formation of dirt or suppress its further growth by compound such as organic polymer, tensio-active agent or the inorganic phosphate that adds trace.The cost height; The technology relative complex expends a large amount of pharmaceutical chemicalss, causes production cost to increase greatly, is unfavorable for large-scale industrial production, and in construction process fragile pipeline, contaminate environment, the time is long, therefore, is subjected to serious restriction in practical application;
(2) physical method: by promoting dirt crystallization or make dirt just be disintegrated the formation that suppresses dirt in the initial period that forms in solution.Major technique has: gypsum seed method, ultrasonic wave preventing fouling or impel by the magnetic field that adds or electric field that dirty component precipitates in advance in the solution.At present, and the physics descaling method can only use under given conditions, but operates heavyly, and cost is bigger.The pipeline calcium sulfate dirt layer that the applicant is short for the formation cycle, quality is loose and fed distance is short, adopt light salt brine to wash removing back and forth, certain effect is arranged, handle but need to stop production, and this method is to being difficult to carry out on the fed distance longer pipe road engineering, and poor effect.
(3) mechanical means.Adopt the method for machinery to remove the fouling duricrust on surface or control the further growth of dirt in the adhesion of plane of crystal by reducing dirt.Commonly used has: rely on such as can and having the material of grinding with liquid-flow as sand, Glass lamp etc.; Use mechanical friction power in equipment surface operation or periodic rotation.
Press for a kind of can the solution from mining area to workshop in the actual production than the method for calcium sulfate scaling in the long transport pipe.
Summary of the invention
Technical problem to be solved by this invention provides a kind of method that prevents that effectively calcium sulfate scaling is separated out in the halogen bittern.
For solving the problems of the technologies described above, the present invention is achieved in that
Prevent the device of bittern transport pipe fouling, it is characterized in that, comprise cooling tower, retort, settling vat, storage halogen bucket and thinning tank, cooling tower wherein, retort, settling vat connect successively, and storage halogen bucket and thinning tank are connected to settling vat side by side.
Prevent the method for bittern transport pipe fouling, it is characterized in that directly import the cooling tower cooling from the bittern of mining area output, bittern is cooled to than the high 8-10 of envrionment temperature ℃ in cooling tower.
Be transported to retort from the bittern of cooling tower output, crystallization is separated out in calcium sulfate in retort in the bittern and gypsum seed reaction;
Input in the settling vat from the bittern of retort output, the calcium sulfate precipitation of separating out is through post precipitation, and the supernatant liquor that meets defeated halogen requirement is delivered in the storage halogen bucket, is delivered to enterprise then and carries out other processing; The supernatant liquor that does not meet defeated halogen requirement is delivered in the thinning tank, adds the degree of supersaturation of fresh water dilution, reduction calcium sulfate, perhaps adds soda ash, and the reaction back reduces the content of calcium sulfate in the bittern.
(engineering experience value)≤1.01 that are controlled at of calcium sulfate degree of supersaturation promptly meet defeated halogen requirement in the supernatant liquor.
Principle of the present invention is as follows:
Detect through the applicant, the principal constituent of the transport pipe dirt layer of sodium sulfate type ore deposit halogen is a terra alba, and content contains a spot of sodium sulfate and sodium-chlor in addition greater than 90%.
From the fouling Analysis on Mechanism, the factor that influences calcium sulfate scaling is more, but the temperature reduction is calcium sulfate supersaturation in the halogen water in bittern exploitation and course of conveying, causes calcium sulfate in pipeline crystallization, fouling.Make a concrete analysis of as follows: in ore deposit halogen exploitation and course of conveying, just from the temperature of the ore deposit halogen that underground mining goes out generally about 42 ℃, and the envrionment temperature of bittern conveying on average has only 10-20 ℃.Sodium sulphate content is much smaller than its solubleness, sodium-chlor solubleness temperature influence not substantially in the halogen of ore deposit, and when temperature reduced, sodium sulfate and sodium-chlor generally can not produce crystallization.The calcium sulfate that just goes out the bittern from underground mining is in state of saturation substantially, calcium sulfate is non-crystallizable, bittern is in being transported to the process of enterprise, be subjected to the influence of envrionment temperature, its temperature make the calcium sulfate supersaturation, and degree of supersaturation increases constantly in continuous decline, make calcium sulfate enter into labile state and spontaneous crystallization, in the fouling of brine pipeline road from stable state or inferior stable state.Temperature descends low more, and the degree of supersaturation increase is many more, and calcium sulfate just is easy to crystallize out more, and brine pipeline road scale formation is serious, and this is the particularly serious reason of fouling in winter just.
Therefore, suppress or eliminate and carry sodium sulfate type ore deposit halogen pipeline calcium sulfate scaling, just brine temperature must be reduced near envrionment temperature,, also will eliminate temperature decline simultaneously and cause the calcium sulfate degree of supersaturation that produces in the bittern to eliminate Temperature Influence.
Characteristics of the present invention are as follows:
The United Technologies technology that the present invention organically combines falling temperature method, gypsum seed method, thin up method (or chemical purification).
Falling temperature method is to utilize the degree of supersaturation of calcium sulfate in bittern to reduce with temperature to raise, and bittern is lowered the temperature makes the calcium sulfate in the bittern enter into unstable region and crystallization because temperature reduces from the saturation region, reduces the content of calcium sulfate in the bittern; The gypsum seed method is to utilize the gypsum seed structure identical with calcium sulfate dirt thing, plane of crystal is big than the pipeline material wall to the avidity of dirty thing calcium sulfate, adding gypsum seed in bittern makes the calcium sulfate molecule of separating out in the bittern preferentially attached on the gypsum crystal that suspends, the calcium sulfate degree of supersaturation is in time eliminated, thereby reduce the impellent of crystal of calcium sulfate, avoid the one-tenth crystalline nucleation of calcium sulfate on tube wall; The thin up method is utilize to add a small amount of solvent, and as water, calcium sulfate in the dilution bittern makes that the degree of supersaturation of calcium sulfate reduces in the bittern; Chemical purification is utilization CaSO
4With dissolving back Na
2CO
3Reaction generates CaCO
3Sedimentary mechanism, the content of reduction bittern calcium sulfate, its reactive ion formula is: Ca
2++ CO
3 2-=CaCO
3↓.Like this calcium sulphate content in the bittern is controlled in the calcium sulfate solubleness of envrionment temperature permission, the brine pipeline road can not produce scale formation.In addition; engineering experience according to actual production; keep certain calcium sulfate degree of supersaturation, pipeline produces a spot of calcium sulfate scaling, can prevent corrosive pipeline; pipeline is played a protective role; therefore, the calcium sulfate degree of supersaturation in the bittern is not necessarily all eliminated, and keeps and the interior degree of supersaturation of control certain limit; on industrial applications, allowing, the engineering experience value of control calcium sulfate degree of supersaturation is about≤and 1.02.
Present method is to utilize temperature to reduce and the existence of calcium sulfate degree of supersaturation is the principle of calcium sulfate scaling, before carrying, bittern initiatively reduces brine temperature, and adding calcium sulfate crystal seed, most of crystal of calcium sulfate is come out, auxiliary again thin up method or chemical purification, eliminate the degree of supersaturation of calcium sulfate in the bittern, solved the scale problems of calcium sulfate on transport pipe.Effectively in conjunction with the comprehensive advantage of falling temperature method, gypsum seed method, thin up method (or chemical purification processing), operation is easy to control, cost is low; Features high scale-removing effect can meet the needs of production fully.Improve the defeated halogen ability and the efficient in brine pipeline road, reduced the production cost of salt manufacturing.
Description of drawings
Fig. 1 schematic representation of apparatus of the present invention;
The synoptic diagram of Fig. 2 technical process of the present invention.
Embodiment
The present invention is described in further detail below in conjunction with embodiment.
Fig. 1 schematic representation of apparatus of the present invention, with reference to shown in Figure 1, prevent the device of bittern transport pipe fouling, comprise cooling tower 1, retort 2, sedimentation device 3, storage halogen device 4 and thinning tank 5, wherein cooling tower 1, and retort 2, sedimentation device 3 connect successively, and storage halogen device 4 and thinning tank 5 are connected to settling vat side by side.
The synoptic diagram of Fig. 2 technical process of the present invention.With reference to shown in Figure 2, at first, utilize temperature to reduce, the degree of supersaturation of calcium sulfate produces and increase in the bittern, is easy to the crystalline principle, and bittern is passed through cooling tower 1 cooling; Secondly, utilization adds gypsum seed and carries out crystallization in bittern, can obviously reduce the principle of calcium sulfate degree of supersaturation in the bittern, bittern is pumped into retort, and in retort, add gypsum seed, stir, make bittern and crystal seed thorough mixing, time generally is controlled at 15-30min, make most of crystal of calcium sulfate come out, the calcium sulfate degree of supersaturation reduces, and the quality and the granularity that add gypsum seed by control are controlled the preferable clearance of the degree of supersaturation of calcium sulfate in the bittern, experimental study proves: because the crystalline growth is relevant with the active growth point of plane of crystal, certain when the crystal seed particle diameter that adds, consumption is big more, and corresponding active growth point is also more, calcium sulfate in the solution just can comparatively fast crystallize out, and therefore can obtain degree of supersaturation clearance faster; In like manner, at the consumption one that adds crystal seed regularly, the particle of crystal seed is more little, and specific surface area is big more, and then the degree of supersaturation clearance is fast more.That the present invention to its add-on be controlled at about 1.5g/l, particle size restrictions is at 30-40 μ m; Then bittern is pumped in the settling vat, in settling vat, calcium sulfate obtains further crystallization and fully precipitates; At last, the clear liquid that overflows in the settling vat, difference according to circumstances can enter into thinning tank or storage halogen bucket: less when the calcium sulfate degree of supersaturation, can satisfy when failing the halogen needs, can directly enter into and store up the halogen bucket and store, wait to carry; When the calcium sulfate degree of supersaturation also bigger, can not satisfy when failing the halogen needs, can be pumped into thinning tank, select to add the concentration of a small amount of fresh water dilution bittern, or add soda ash, further eliminate the calcium sulfate degree of supersaturation in the bittern, stirring sedimentation through certain hour, reach defeated halogen requirement, send into again in the storage halogen bucket and store, wait to carry.
To explaining of involved data among the embodiment 1 to 4: 1, because the ununiformity of underground rock salt sodium sulfate, calcium sulphate content, add that the subsurface geology situation is complicated, the ore deposit alkali quantitative changeization of exploitation is big, so the compositional data of each component of embodiment chats halogen is averaged; 2, sodium sulfate, calcium sulphate content difference in the rock salt of different areas, sodium sulfate, calcium sulphate content also have nothing in common with each other in the rock salt of the different mines of areal, and the composition of the ore deposit halogen that embodiment adopted herein is: NaCl content is about 300g/l, Na
2SO
4Content is about 20g/l, CaSO
4Content is about 1.96g/l: the composition of denitration bittern: NaCl content is about 310g/l, Na
2SO
4Content is about 0.285g/l, CaSO
4Content is about 6.5g/l.
Calcium sulfate the saturation solubility (being saturation ratio) of differing temps (unit: g/L) as follows:
Test-results proves: add the 1.5g/L granularity and be 34 μ m gypsum seed and calcium sulfate degree of supersaturation clearance is reached 87%, 15 ℃ at 25 ℃ reach 78%.
Engineering experience: the sodium sulfate in the brine degree of supersaturation is controlled at≤and 1.02, the brine pipeline road seldom or not can produce scale formation.
Embodiment one
In winter, when external temperature is 10 ℃, to the processing in the former halogen: the temperature of just having exploited former halogen is 42 ℃, and calcium sulphate content is 1.96g/l, is in state of saturation, and calcium sulfate is non-crystallizable; After cooling tower 1 cooling, bittern is cooled to about 20 ℃ from 42 ℃, and the calcium sulfate degree of supersaturation is elevated to 1.153 from 1.013, because the meta regional extent of calcium sulfate is bigger in theory, calcium sulfate substantially can crystallization, or crystallization is seldom arranged, therefore, calcium sulphate content is slightly less than 1.96g/l; Then in retort to adding gypsum seed through overcooled bittern, making its content in bittern is 1.5g/l, stirs 30min, the temperature of this process bittern is reduced to about 15 ℃, the calcium sulfate mass crystallization comes out, and calcium sulphate content is reduced to 1.736g/l from 1.96g/l, and degree of supersaturation is 1.0333.According to actual needs, if the calcium sulfate degree of supersaturation is still higher, can select the thin up method to add the pure water that accounts for bittern total mass 2%, make the content of calcium sulfate be reduced to 1.70g/l, degree of supersaturation is 1.013; Or the selection chemical purification is to add 28.06g soda ash (NaCO in every cube of bittern
3), make the content of calcium sulfate reach 1.70g/l, degree of supersaturation is 1.006, after handling through these two kinds of methods, all less than calcium sulfate degree of supersaturation control experience value 1.02, this is in the degree of supersaturation scope that industry is allowed for the calcium sulfate degree of supersaturation in the bittern.Therefore such bittern is outwards carried, and pipeline seldom or not can produce scale formation.
Embodiment two
When the winter environment temperature is 10 ℃, to the processing in the denitration bittern: the temperature of just having exploited former halogen is 42 ℃, and calcium sulphate content is 6.5g/l, is in state of saturation, and calcium sulfate is non-crystallizable; Behind atmosphere cooling tower 1, bittern is cooled to about 20 ℃ from 42 ℃, this moment, the calcium sulfate degree of supersaturation was elevated to 1.115 from 1.037, because the meta regional extent of calcium sulfate is bigger in theory, calcium sulfate substantially can crystallization, or seldom crystallization is arranged, therefore, calcium sulphate content is slightly less than 6.5g/l; Adding gypsum seed then in reaction container in bittern, to make its content in bittern be 1.5g/l, make crystal of calcium sulfate, stir 30min, the temperature of this process bittern will be reduced to about 15 ℃, calcium sulfate comes out mass crystallization, calcium sulphate content is reduced to 5.93g/l from 6.5g/l, and degree of supersaturation is 1.025.According to actual needs, if the calcium sulfate degree of supersaturation is still higher, can select the thin up method to add the pure water that accounts for bittern total mass 3%, the content of calcium sulfate then reaches 5.75g/l, and degree of supersaturation is 1.002; Or add 140.29g soda ash in every cube of bittern of selection chemical purification rule, make the content of calcium sulfate reach 5.75g/l, degree of supersaturation is 1.002, after these two kinds of methods processing, calcium sulphate content is 5.74g/l a little more than the saturation solubility under the envrionment temperature all in the bittern, but its degree of supersaturation is in the degree of supersaturation scope that industry allows, and such bittern is outwards carried, and the brine pipeline road seldom or not can produce scale formation.
Embodiment three
In summer, envrionment temperature is 20 ℃, and to the processing in the former halogen: the temperature of just having exploited former halogen is 42 ℃, and the content of calcium sulfate is 1.96g/l, is in state of saturation, and calcium sulfate is non-crystallizable; Behind the atmosphere cooling tower, bittern is cooled to about 30 ℃ from 42 ℃, this moment, the calcium sulfate degree of supersaturation was elevated to 1.101 from 1.013, because the meta regional extent of calcium sulfate is bigger in theory, calcium sulfate substantially can crystallization, or seldom crystallization is arranged, therefore, calcium sulphate content is slightly less than 1.96g/l; Add gypsum seed then in reaction container in bittern, making its content is 1.5g/l, crystal of calcium sulfate, stir 30mi n, the temperature of this process bittern will be reduced to about 25 ℃, and calcium sulfate comes out mass crystallization, calcium sulphate content is reduced to 1.763g/l from 1.96g/l, and degree of supersaturation is 1.0132.According to actual needs, if the calcium sulfate degree of supersaturation is still higher, can select the thin up method to add the pure water that accounts for bittern total mass 4% quality, the content of calcium sulfate then reaches 1.712g/l, and degree of supersaturation is 1.007; Or adding 39.75g soda ash (NaCO in every cube of bittern of selection chemical purification rule
3), also can make the content of calcium sulfate reach 1.712g/l, degree of supersaturation is 1.007, after these two kinds of methods processing, calcium sulphate content is all a little more than the saturation solubility 1.70g/l under the envrionment temperature in the bittern, but its degree of supersaturation is in the degree of supersaturation scope that industry allows, and such bittern is outwards carried, and the brine pipeline road seldom or not can produce scale formation.
Embodiment four
When the summer environment temperature is 20 ℃, to the processing in the denitration bittern: the temperature of just having exploited former halogen is 42 ℃, and calcium sulfate 6.5g/l is in state of saturation, and calcium sulfate is non-crystallizable; Through behind the atmosphere cooling tower, bittern is cooled to about 30 ℃ from 42 ℃, and this moment, the calcium sulfate degree of supersaturation was elevated to 1.087 from 1.037, because the meta regional extent of calcium sulfate is bigger in theory, calcium sulfate substantially can crystallization, or crystallization is seldom arranged, therefore, calcium sulphate content is slightly less than 6.5g/l; In reaction container, in bittern, add the 1.5g/l gypsum seed then and make crystal of calcium sulfate, stir 30min, the temperature of this process bittern will be reduced to about 25 ℃, calcium sulfate comes out mass crystallization, and calcium sulphate content is reduced to 5.97g/l from 6.5g/l, and degree of supersaturation is 1.0113, its value is less than calcium sulfate degree of supersaturation control experience value 1.02, this is in the degree of supersaturation scope that industry allows, and therefore such bittern is outwards carried, and the brine pipeline road seldom or not can produce scale formation.
Above-mentioned embodiment does not limit technical scheme of the present invention in any form, and the technical scheme that mode obtained that every employing is equal to replacement or equivalent transformation all drops on protection scope of the present invention.
Claims (4)
1. prevent the device of bittern transport pipe fouling, it is characterized in that comprising cooling tower, retort, sedimentation device, storage halogen device and thinning tank, cooling tower wherein, retort, sedimentation device connect successively, and storage halogen device and thinning tank are connected to settling vat side by side.
2. prevent the method for bittern transport pipe fouling, it is characterized in that comprising the steps:
(1) directly imports the cooling tower cooling from the bittern of mining area output;
(2) bittern from cooling tower output is transported to retort, calcium sulfate molecule in retort in the bittern and gypsum seed reaction, and on the gypsum crystal that suspends, the saturation ratio of the calcium sulfate in the bittern reduces;
(3) bittern from retort output inputs in the settling vat, and the calcium sulfate precipitation of separating out is through post precipitation, and the supernatant liquor that meets defeated halogen requirement is delivered in the storage halogen bucket, is delivered to enterprise then and carries out following process; The supernatant liquor that does not meet defeated halogen requirement is delivered in the thinning tank, adds the degree of supersaturation of fresh water dilution, reduction calcium sulfate, perhaps adds soda ash, by reaction precipitation of calcium carbonate is separated out, and reduces the content of calcium sulfate in the bittern;
Described defeated halogen require be the engineering experience value of calcium sulfate degree of supersaturation of bittern be controlled at≤1.01.
3. according to the described method that prevents the fouling of bittern transport pipe of claim (3), it is characterized in that the add-on of gypsum seed described in the step (2) is controlled at about 1.5g/l, particle size restrictions is at 30-40 μ m.
4. the method that prevents the fouling of bittern transport pipe according to claim 1 is characterized in that in the step (1) that bittern is cooled to than the high 8-10 of envrionment temperature ℃ in cooling tower.
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104019087A (en) * | 2014-06-13 | 2014-09-03 | 山东大学 | Method for reducing flow resistance of halogen collecting and conveying pipeline |
| CN104402124A (en) * | 2014-12-05 | 2015-03-11 | 杭州水处理技术研究开发中心有限公司 | Calcium sulfate seed crystal crystallization device and calcium sulfate seed crystal crystallization method |
| CN106391597A (en) * | 2016-10-21 | 2017-02-15 | 淮安信息职业技术学院 | Online non-production-halt cleaning process for brine transportation pipeline |
| CN107651714A (en) * | 2017-06-28 | 2018-02-02 | 青岛清健怡水技术咨询有限公司 | Molybdenum containing high concentration, zr element sewage disposal process in antiscaling method |
| CN110104664A (en) * | 2019-04-24 | 2019-08-09 | 孝感广盐华源制盐有限公司 | A kind of antiscaling method mentioning nitre heat exchanger surface |
| WO2020253182A1 (en) * | 2019-06-20 | 2020-12-24 | 中国科学院理化技术研究所 | Gypsum magnetic seed crystal scale inhibition and removal system and evaporation and crystallization system |
| CN112681481A (en) * | 2020-11-26 | 2021-04-20 | 安徽聚云环保设备制造有限责任公司 | Domestic sewage treatment device based on water quantity dynamic regulation |
| CN113941567A (en) * | 2020-07-15 | 2022-01-18 | 湖南中天青鼎工程科技股份有限公司 | Drainage pipeline scale inhibition and removal method for phosphogypsum tailings recycling |
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| CN104019087A (en) * | 2014-06-13 | 2014-09-03 | 山东大学 | Method for reducing flow resistance of halogen collecting and conveying pipeline |
| CN104402124A (en) * | 2014-12-05 | 2015-03-11 | 杭州水处理技术研究开发中心有限公司 | Calcium sulfate seed crystal crystallization device and calcium sulfate seed crystal crystallization method |
| CN106391597A (en) * | 2016-10-21 | 2017-02-15 | 淮安信息职业技术学院 | Online non-production-halt cleaning process for brine transportation pipeline |
| CN106391597B (en) * | 2016-10-21 | 2019-06-28 | 淮安信息职业技术学院 | Halogen transportation pipeline does not stop production cleaning process online |
| CN107651714A (en) * | 2017-06-28 | 2018-02-02 | 青岛清健怡水技术咨询有限公司 | Molybdenum containing high concentration, zr element sewage disposal process in antiscaling method |
| CN110104664A (en) * | 2019-04-24 | 2019-08-09 | 孝感广盐华源制盐有限公司 | A kind of antiscaling method mentioning nitre heat exchanger surface |
| WO2020253182A1 (en) * | 2019-06-20 | 2020-12-24 | 中国科学院理化技术研究所 | Gypsum magnetic seed crystal scale inhibition and removal system and evaporation and crystallization system |
| CN113941567A (en) * | 2020-07-15 | 2022-01-18 | 湖南中天青鼎工程科技股份有限公司 | Drainage pipeline scale inhibition and removal method for phosphogypsum tailings recycling |
| CN112681481A (en) * | 2020-11-26 | 2021-04-20 | 安徽聚云环保设备制造有限责任公司 | Domestic sewage treatment device based on water quantity dynamic regulation |
| CN112681481B (en) * | 2020-11-26 | 2022-05-24 | 安徽聚云环保设备制造有限责任公司 | Domestic sewage treatment device based on water quantity dynamic regulation |
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| CN102060312B (en) | 2012-07-04 |
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Application publication date: 20110518 Assignee: JIANGXI JINGHAO SALT CHEMICAL CO.,LTD. Assignor: JIANGSU SUYAN JINGSHEN Co.,Ltd.|JIANGSU SALT INDUSTRY RESEARCH INSTITUTE Co.,Ltd. Contract record no.: X2023990000704 Denomination of invention: Method and device for preventing scaling in brine transportation pipelines Granted publication date: 20120704 License type: Exclusive License Record date: 20230712 |