CN101591006A - Purifying sulfur containing salts and device - Google Patents
Purifying sulfur containing salts and device Download PDFInfo
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- CN101591006A CN101591006A CNA2009101505657A CN200910150565A CN101591006A CN 101591006 A CN101591006 A CN 101591006A CN A2009101505657 A CNA2009101505657 A CN A2009101505657A CN 200910150565 A CN200910150565 A CN 200910150565A CN 101591006 A CN101591006 A CN 101591006A
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Abstract
The invention discloses a kind of purifying sulfur containing salts, may further comprise the steps: solid-state sulfur containing salt and water are mixed with the sulphur slurries; The sulphur slurries are heated to 120 ℃～160 ℃, make the sulphur fusion in the sulphur slurries, keep working pressure, make fusion sulphur and brackish water carry out the gravity settling layering, obtain high purity sulphur greater than water saturation vapour pressure under the service temperature.The invention also discloses a kind of device that is used to implement above-mentioned purifying sulfur containing salts, it comprises pulping tank, melting device, preseparator and separator with pipe connection.By sulfur purification of the present invention and equipment, can obtain purity and be 99.8% sulphur, reduce the content of sulphur in the waste discharge simultaneously; By the recycling of heat recuperation and water, reduced the consumption of energy consumption and water, and improved the processing power of sulphur fusion recovery system.
Description
Technical field
The present invention relates to a kind of from sulfur containing salt the method for purification sulphur, and the device of implementing this method.
Background technology
In petrochemical complex, Coal Chemical Industry and natural gas conditioning process, the sulphur in the raw material is converted into H after processing, conversion
2S, and H
2S often adopts liquid phase catalytic oxidation to remove.In liquid phase catalytic oxidation, H
2S is absorbed by catalyst solution (for example vanadium compound or chelated iron catalyzer), and oxygenant is with H
2S is oxidized to the solid elemental sulfur.In order to keep this technology to move continuously, the solid sulfur particle of generation need be separated from catalyst solution.
Sulphur separates and the legacy equipment of recovery is a sulfur melting kettle, is mainly used in the desulfurization process of small nitrogenous fertilizer plant and coke-oven gas.The sulphur that nitrogen fertilizer plant and coke oven gas desulfurization operation form exists with form of foam, contains sulphur about 6%.The continous way sulfur melting kettle separates the sulphur foamy with melting sulphur and concentrates in same the equipment and finish, and the top of equipment is heated to about 90 ℃ with the sulphur foam, makes the sulphur bubble coalescence, and with water sepn, temperature of lower is higher, is used for molten sulphur.Parting liquid is back to desulfurization process continuation use from the top of sulfur melting kettle, and fusion sulphur is interrupted from the bottom discharges.The sulfur melting kettle flow process is simple, but also has wretched insufficiency, and comprising: 1) volume of equipment is limited, only is fit to 300～900 tons/year sulphur fusion usually; 2) the sulphur foam separation is incomplete, returns suspension sulphur content height in the clear liquid of desulphurization system; 3) owing to separate sulfur foamy service temperature higher (being about 90 ℃), doctor solution easily produces side reaction, so the effective constituent reduction, is unfavorable for the normal operation of desulphurization system.Especially for being the sulfur removal technology of catalyzer with the chelated iron, sequestrant causes catalyst failure decomposing more than 58 ℃, therefore, can't use the continous way sulfur melting kettle, and must adopt sulphur slurries sedimentation after-filtration (or centrifugal), isolate the sulphur cake, and filtrate cycle is returned desulphurization system to utilize catalyzer wherein.
The purity of the sulphur cake that filtration or centrifugal back form is lower, contains sulphur, water, inorganic salt and other impurity of trace.With the chelated iron liquid phase catalytic oxidation is example, and its typical sulfur product consists of: 65%～75% sulphur, 23%～33% water, about 1.2% (NH
4)
2S
2O
3, a spot of (NH
4) HCO
3(NH
4)
2CO
3And the iron ion of trace.These sulphur cakes do not meet the quality regulation of GB/T2449-2006 national standard to sulfur product, need further be refined into the industrial sulphur of sulfur-bearing more than 99%.
Summary of the invention
In view of the above-mentioned problems in the prior art, one object of the present invention is to provide a kind of method of extracting high purity sulphur from sulfur containing salt.
Another object of the present invention is to provide a kind of device that from sulfur containing salt, extracts high purity sulphur.
For achieving the above object, the invention provides a kind of purifying sulfur containing salts, it may further comprise the steps: (1) is mixed with the sulphur slurries with solid-state sulfur containing salt and water; (2) the sulphur slurries are heated to 120 ℃～160 ℃, make the sulphur fusion in the sulphur slurries, keep working pressure, make fusion sulphur and brackish water carry out the gravity settling layering, obtain high purity sulphur greater than water saturation vapour pressure under the service temperature.
Purifying sulfur containing salts of the present invention, wherein the sulphur slurries described in the step (1) contain the sulphur of 15%～20% weight.
Purifying sulfur containing salts of the present invention, wherein the stratified operation of gravity settling described in the step (2) is divided into pre-separation operation and lock out operation, and the brackish water and the fusion sulphur that produce in the pre-separation operation are proceeded the gravity settling layering in lock out operation.
Purifying sulfur containing salts of the present invention, wherein the stratified service temperature of gravity settling described in the step (2) is 130 ℃～140 ℃.
Purifying sulfur containing salts of the present invention, wherein the stratified working pressure of gravity settling described in the step (2) is 0.4MPa.
The present invention also provides a kind of device that is used to implement purifying sulfur containing salts, and wherein this device comprises: a pulping tank and a separator; Separator comprises a top opening for feed, a top discharge mouth and a bottom discharge mouth; Wherein, the top opening for feed of the discharge port of pulping tank and separator is by a pipe connection.
Device of the present invention wherein also comprises: a preseparator comprises an opening for feed, a upper part discharge port and a bottom discharge mouth; Separator also comprises a bottom opening for feed; Wherein, the upper part discharge port of preseparator is connected by a pipeline with the top opening for feed of separator, and the bottom discharge mouth of preseparator is connected by a pipeline with the underfeed mouth of separator; The discharge port of pulping tank and the opening for feed of preseparator are by a pipe connection.
Device of the present invention, wherein also comprise a melting device, melting device is vertically arranged tube and shell heat exchanger, and an opening for feed of the discharge port of pulping tank and melting device is by a pipe connection, and a discharge port of melting device and the opening for feed of preseparator are by a pipe connection.
Device of the present invention, wherein also comprise a flash tank, one top opening for feed, one pipe connection of the top discharge mouth of separator and flash tank, flash drum overhead one outlet is connected with an its top feed mouth of pulping tank by a pipeline, and one outlet of flash tank bottom is connected with an its top feed mouth of pulping tank by a pipeline.
Device of the present invention, wherein also comprise a slurry feed jar, one first interchanger and one second interchanger, the top of slurry feed jar is connected with the bottom of pulping tank by a pipeline, the slurry feed pot bottom is connected with melting device by a pipeline, the outlet at bottom of flash tank and a pipe connection, serial connection is respectively applied for described first interchanger and second interchanger that carries out thermal exchange with sulphur slurries and de-mineralized water on the pipeline.
By sulfur purification of the present invention and equipment, can obtain purity and be 99.8% sulphur, reduce the content of sulphur in the waste discharge simultaneously; By the recycling of heat recuperation and water, reduced the consumption of energy consumption and water, and improved the processing power of sulphur fusion recovery system.
With reference to the accompanying drawing description of a preferred embodiment, above-mentioned and other purpose of the present invention, feature and advantage will be more obvious by following.
Description of drawings
Fig. 1 is the synoptic diagram of first embodiment of sulfur containing salt method of purification of the present invention and device;
Fig. 2 is the synoptic diagram of second embodiment of sulfur containing salt method of purification of the present invention and device;
Fig. 3 is the synoptic diagram of the 3rd embodiment of sulfur containing salt method of purification of the present invention and device;
Fig. 4 is the synoptic diagram of the 4th embodiment of sulfur containing salt method of purification of the present invention and device; And
Fig. 5 is the synoptic diagram of the 5th embodiment of sulfur containing salt method of purification of the present invention and device.
Embodiment
To describe specific embodiments of the invention in detail below.Should be noted that the embodiments described herein only is used to illustrate, be not limited to the present invention.
Embodiment one
As shown in Figure 1, the sulphur purifying plant of the first embodiment of the present invention comprises a sulphur pulping tank 110, a slurries transferpump 130 and a separator 170.Wherein, sulphur pulping tank 110 is equipped with mechanical stirring device, injects the pipeline 12 of de-mineralized water (b) and the opening that is used to add solid sulfur containing salt (a).
The discharge port of pulping tank 110 links to each other with the import of slurries transferpump 130 by pipeline 13, and the outlet of slurries transferpump 130 is connected by pipeline 1 with the top opening for feed 172 of separator.
Being operating as of the method for purification of present embodiment: earlier sulfur containing salt (a) is mixed with water in pulping tank 110, stir, be mixed with the slurries that contain 15～20% sulphur with agitator.Slurries transferpump 130 extracts slurries from pulping tank 110 bottoms, send into separator 170.Slurries are heated in separator 170, the sulphur that wherein contains is melt into liquid state, because the density of fusion sulphur is bigger than water, fusion sulphur and water can pass through the gravity settling layering, the salt that contains in the sulphur can be dissolved in the water, thereby realize the purification to sulfur containing salt, the stratified service temperature of gravity settling is preferably 130 ℃～140 ℃, and working pressure is preferably 0.4MPa.Brackish water is discharged from the top discharge mouth 173 of separator 170, and fusion sulphur is discharged from the bottom discharge mouth 174 of separator 170.In the present embodiment, the slurries limit enters separator 170, is heated in separator 170, and the settlement separate of brackish water and fusion sulphur carried out on the limit.
Embodiment two
As shown in Figure 2, the sulphur purifying plant of second embodiment of the invention has increased by a preseparator 160 on the basis of first embodiment, and preseparator 160 is containers of carrying vapour chuck thermal insulation layer.Preseparator 160 comprises an opening for feed 161 and two discharge ports 162,163, its opening for feed 161 is positioned at the middle part of container, discharge port 162 and 163 lays respectively at the top and the bottom of container, and the height of opening for feed 161 should be lower than discharge port 162, but is higher than discharge port 163.
At this moment, separator 170 also comprises two opening for feeds 171,172, opening for feed 171 is positioned at the bottom of separator 170, opening for feed 172 is positioned at the top of separator 170, the upper part discharge port 162 of preseparator 160 is in same level height with the top opening for feed 172 of separator 170, and is communicated with by the pipeline 4 of steam jacket insulation; The bottom discharge mouth 163 of preseparator 160 is communicated with the pipeline 5 of the bottom discharge port 171 of separator 170 by the steam jacket insulation, and preseparator 160 and separator 170 are the equipment of two platform independent, and the pipeline 4 between them and 5 should be short as far as possible.The opening for feed 161 of preseparator 160 is connected to the outlet of slurries transferpump 130 by pipeline 1.
Owing to increased preseparator 160 in the present embodiment, therefore the difference with embodiment one is, the sulphur slurries can be earlier by slurries transferpump 130 input preseparators 160, the fusion in preseparator 160 earlier of sulphur in the slurries, and in preseparator 160, carry out pre-separation and operate, its principle and operational condition are with the operation of the gravity settling separation in the separator 170, and the fusion sulphur of formation and brackish water can enter in the separator 170 by pipeline 5 and 4 and proceed lock out operation.In the present embodiment, brackish water and fusion sulphur at first carry out pre-separation in preseparator 160, separate at last in separator 170 then, and separating effect significantly improves.
Embodiment three
As shown in Figure 3, the sulphur purifying plant of third embodiment of the invention has increased by a melting device 150 that is specifically designed to the sulphur in the fusion slurries on the basis of second embodiment, melting device 150 can be one group of tube and shell heat exchanger, be generally and be arranged vertically, can prevent like this that sulfur granule in the slurries from depositing and the equipment that causes stops up in tubulation.The inlet of melting device 150 is connected to the outlet of slurries transferpump 130 by pipeline 1, and the outlet 151 of melting device 150 is connected to the inlet 161 of preseparator by pipeline 3.
Owing to increased premelter 150 in the present embodiment, therefore the difference with embodiment two is, slurries can be earlier by slurries transferpump 130 input melting devices 150, the fusion in melting device 150 earlier of sulphur in the slurries, and rear slurry enters preseparator 160 again, and the temperature of the slurries at outlet 151 places of melting device 150 is not higher than 160 ℃.Obviously, in the present embodiment, the separating effect of brackish water and fusion sulphur further improves than embodiment two.
Embodiment four
As shown in Figure 4, the sulphur purifying plant of fourth embodiment of the invention has increased by a flash tank 180 on the basis of the 3rd embodiment, and flash tank 180 is used to handle the brackish water that is produced by separator 170, and flash tank 180 also is equipped with liquidometer 181.
Flash tank 180 is connected with the top discharge mouth 173 of separator 170 by the pipeline 7 that pressure controlled valve 71 is housed.The top of flash tank 180 is connected with the pipeline 8 that steam is transferred to sulphur pulping tank 110, the bottom of flash tank 180 is equipped with the pipeline 9 that brackish water is transferred to sulphur pulping tank 110, and the pipeline in the discharging brine waste 10, flowrate control valve 91 is installed on pipeline 9, in order to control the temperature of prepared slurries, also temperature-control device TT need be installed in the sulphur pulping tank 110 simultaneously.
Owing to increased flash tank 180 in the present embodiment, therefore the difference with embodiment three is, the brackish water from discharge by pipeline 7 at the top of separator 170 is introduced into flash tank 180.In flash tank 180, a part of brackish water is vaporized into steam, gets back to pulping tank 110 by pipeline 8, and another part brackish water is discharged as brackish water from the bottom of flash tank 180 simultaneously, and wherein the part brackish water recycles from 9 times sulphur pulping tanks 110 of pipeline.In the present embodiment, the high-temperature steam and the part high temperature brackish water of discharging from flash tank 180 enter into pulping tank 110, high-temperature steam and part high temperature brackish water can improve the temperature of sulphur slurries, help solid sulphur and water uniform mixing and the slurries in pulping tank and enter melting device 150 fusion of sulphur afterwards.
Embodiment five
As shown in Figure 5, the sulphur purifying plant of fifth embodiment of the invention has increased by a slurry feed jar 120 on the basis of the 4th embodiment, slurry feed jar 120 also is equipped with mechanical stirring device and fluid level control device, and is connected by the bottom of pipeline 13 with pulping tank 110.
As shown in the figure, the pipeline 10 from flash tank 180 discharging brine wastes can also be connected with first interchanger 140 and second interchanger 190 in turn.The slurries inlet of first interchanger 140 links to each other with the outlet of slurries transferpump 130 by pipeline 1, and the slurries outlet of first interchanger 140 links to each other with the inlet of melting device 150 by pipeline 2.Second interchanger 190 also is connected on the pipeline 12 of carrying de-mineralized water (b).
Owing to increased slurry feed jar 120, first interchanger 140 and second interchanger 190 in the present embodiment, therefore the difference with embodiment four is, the sulphur slurries that prepare enter slurry feed jar 120 from pulping tank 110 bottoms earlier, and rear slurry transferpump 130 with slurries in charging stock tank 120 bottom suction first interchanger 140, slurries through with the brine waste heat exchange of discharging from flash tank 180 bottoms after enter melting device 150 again.In addition, the brine waste that carried out heat exchange with slurries from first interchanger 140 comes out enters second interchanger 190, carries out heat exchange once more with the de-mineralized water of transporting to pulping tank 110 (b).In the present embodiment, increasing slurry feed jar 120 can make solid sulphur carry out more uniform the mixing with water; Increasing by first interchanger 140 and second interchanger 190 is fully used the heat of the high temperature brackish water of discharging from flash tank 180 bottoms.
The 5th embodiment is a most preferred embodiment of the present invention, becomes apparent more for making purifying sulfur containing salts of the present invention and device, and now the method for purification with this embodiment is described in detail.
Please continue with reference to figure 5, at first be to pack into solid-state sulfur containing salt (a) in the pulping tank 110 and add entry, with the agitator mixing that stirs, be mixed with the slurries that contain sulphur 15～20% (W), salt in the sulphur can be dissolved in the water, because sulphur is not dissolved in water, formed slurries are a kind of suspension.Sulphur concentration in the slurries also can be higher or lower, and higher sulphur concentration means less amount of makeup water, helps conserving water and consumption of heat energy, if but sulphur excessive concentration, blocking pipe and interchanger easily.
The water that is used to prepare the sulphur slurries can have three sources, comprises the flash-off steam that discharge at flash tank 180 tops, the part brackish water that discharge flash tank 180 bottoms, and the outside de-mineralized water of supplying with.Secondly the preferential flash-off steam that uses is brackish water in these three kinds of water, and insufficient part is replenished with de-mineralized water.De-mineralized water also can substitute with the softening water of hyposaline, but should not use the water of easy fouling.The temperature of sulphur slurries should be controlled at below 60 ℃, to prevent too high temperature sulfur granule is assembled, and avoids slurries transferpump 130 to produce cavitation erosion simultaneously.
The sulphur slurries that prepare enter slurry feed jar 120 from pulping tank 110 bottoms, and slurries also will stir in charging stock tank 120, to prevent the sulphur deposition.Slurries transferpump 130 extracts slurries from charging stock tank 120 bottoms, through first interchanger 140 and melting device 150, send into preseparator 160.Melting device 150 is heated to fusion with sulphur, and the temperature of the slurries at outlet 151 places of melting device 150 should not be higher than 160 ℃, is generally 130 ℃～140 ℃.
In preseparator 160, sulphur after the fusion and brackish water are because immiscible, and meeting be divided into two-layer because of density is different, and the upper strata is a brackish water, but has a small amount of sulfur granule to suspend, and lower floor is a fusion sulphur.In operation, the interface 164 in the preseparator between fusion sulphur and the brackish water should be lower than opening for feed 161, influences settlement separate effect to prevent liquid flow direction mutually on the contrary with sulphur sedimentation direction.As shown in the figure, brackish water and the fusion sulphur in the preseparator 160 enters separator 170 through pipeline 4 and 5 opening for feeds 172 and 171 from separator 170 respectively.
In separator 170, brackish water further relies on density difference with fusion sulphur and separates, and fusion sulphur (c) is discharged along pipeline 6 through discharge port 174 from the bottom of separator 170, and brackish water is discharged along pipeline 7 through discharge port 173 from the top of separator 170.Separator 170 is in same level height with the interface 176 and the interface 164 of preseparator 160 interior brackish waters and fusion sulphur, and interfacial level is by liquidometer 175 and regulated valve 61 controls.In order to prevent the condensation in equipment and pipeline of fusion sulphur, after the outlet 151 of melting device 150, the equipment and the pipeline that have liquid molten sulphur to exist, all adopt the steam jacket insulation, make temperature maintenance more than the sulphur fusing point, the temperature of steam is not less than 120 ℃, but also is no more than 150 ℃, the stratified service temperature of gravity settling is preferably 130 ℃～140 ℃, and working pressure is preferably 0.4MPa.
Brackish water from discharge by pipeline 7 at the top of separator 170 by pressure controlled valve 71, enters in the flash tank 180.The effect of pressure controlled valve 71 is to keep enough pressure in the separator 170, prevents the water boiling in the separator 170.In flash tank 180, because the pressure reduction, a part of brackish water is vaporized into steam, and another part brackish water temperature reduces simultaneously, is formed with liquid level 182 between steam and the brackish water, and its height can be controlled by liquidometer 181 and the regulated valve 101 on the pipeline 10.Steam returns sulphur pulping tank 110 by pipeline 8 and recycles, brackish water is discharged from the bottom of flash tank 180, thereby take inorganic salt out of system, wherein the part brackish water recycles from 9 times sulphur pulping tanks 110 of pipeline, the flow of this part brackish water is determined according to the temperature and the inorganic salt content in the brackish water of sulphur pulping tank 110, by flowrate control valve 91 controls.
Still very high from flash tank 180 by the temperature of the brine waste of pipeline 10 discharges, need to recycle heat wherein, can under the control of pressure controlled valve 101, at first obtain the brine waste that temperature reduces, and then continue the discharging of cooling back by second interchanger 190 and de-mineralized water (b) heat exchange by first interchanger 140 and sulphur slurries heat exchange cooling.
Though described the present invention with reference to exemplary embodiments, should be appreciated that used term is explanation and exemplary and nonrestrictive term.The spirit or the essence that do not break away from invention because the present invention can specifically implement in a variety of forms, so be to be understood that, the foregoing description is not limited to any aforesaid details, and should be in the spirit and scope that claim limited of enclosing explain widely, therefore fall into whole variations in claim or its equivalent scope and remodeling and all should be the claim of enclosing and contain.
Claims (10)
1. a purifying sulfur containing salts is characterized in that, may further comprise the steps:
(1) solid-state sulfur containing salt and water are mixed with the sulphur slurries;
(2) the sulphur slurries are heated to 120 ℃～160 ℃, make the sulphur fusion in the sulphur slurries, keep working pressure, make fusion sulphur and brackish water carry out the gravity settling layering, obtain high purity sulphur greater than water saturation vapour pressure under the service temperature.
2. purifying sulfur containing salts as claimed in claim 1 is characterized in that, the sulphur slurries described in the step (1) contain the sulphur of 15%～20% weight.
3. purifying sulfur containing salts as claimed in claim 1, it is characterized in that, the stratified operation of gravity settling described in the step (2) is divided into pre-separation operation and lock out operation, and the brackish water and the fusion sulphur that produce in the pre-separation operation are proceeded the gravity settling layering in lock out operation.
4. purifying sulfur containing salts as claimed in claim 1 is characterized in that, the stratified service temperature of gravity settling described in the step (2) is 130 ℃～140 ℃.
5. purifying sulfur containing salts as claimed in claim 1 is characterized in that, the stratified working pressure of gravity settling described in the step (2) is 0.4MPa.
6. a device that is used to implement the purifying sulfur containing salts of claim 1 is characterized in that this device comprises: a pulping tank and a separator;
Separator comprises a top opening for feed, a top discharge mouth and a bottom discharge mouth;
Wherein, the top opening for feed of the discharge port of pulping tank and separator is by a pipe connection.
7. device as claimed in claim 6 is characterized in that, also comprises:
One preseparator comprises an opening for feed, a upper part discharge port and a bottom discharge mouth;
Separator also comprises a bottom opening for feed;
Wherein, the upper part discharge port of preseparator is connected by a pipeline with the top opening for feed of separator, and the bottom discharge mouth of preseparator is connected by a pipeline with the underfeed mouth of separator;
The discharge port of pulping tank and the opening for feed of preseparator are by a pipe connection.
8. device as claimed in claim 7, it is characterized in that, also comprise a melting device, melting device is vertically arranged tube and shell heat exchanger, one opening for feed of the discharge port of pulping tank and melting device is by a pipe connection, and a discharge port of melting device and the opening for feed of preseparator are by a pipe connection.
9. device as claimed in claim 8, it is characterized in that, also comprise a flash tank, one top opening for feed, one pipe connection of the top discharge mouth of separator and flash tank, flash drum overhead one outlet is connected with an its top feed mouth of pulping tank by a pipeline, and one outlet of flash tank bottom is connected with an its top feed mouth of pulping tank by a pipeline.
10. device as claimed in claim 9, it is characterized in that, also comprise a slurry feed jar, one first interchanger and one second interchanger, the top of slurry feed jar is connected with the bottom of pulping tank by a pipeline, the slurry feed pot bottom is connected with melting device by a pipeline, the outlet at bottom of flash tank and a pipe connection, serial connection is respectively applied for described first interchanger and second interchanger that carries out thermal exchange with sulphur slurries and de-mineralized water on the pipeline.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009101505657A CN101591006A (en) | 2009-06-26 | 2009-06-26 | Purifying sulfur containing salts and device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2009101505657A CN101591006A (en) | 2009-06-26 | 2009-06-26 | Purifying sulfur containing salts and device |
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| CN101591006A true CN101591006A (en) | 2009-12-02 |
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| CNA2009101505657A Pending CN101591006A (en) | 2009-06-26 | 2009-06-26 | Purifying sulfur containing salts and device |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109160492A (en) * | 2018-09-04 | 2019-01-08 | 宜宾丝丽雅股份有限公司 | A kind of sulphur cream washing system and method |
| CN109467058A (en) * | 2018-12-21 | 2019-03-15 | 浙江埃森化学有限公司 | A kind of melting and oxidative purification of diethylaluminum monochloride by-product sulphur |
| CN111807331A (en) * | 2020-06-30 | 2020-10-23 | 浙江佳运能源技术有限公司 | Efficient and energy-saving sulfur purification device and process thereof |
| CN114806649A (en) * | 2022-04-19 | 2022-07-29 | 武汉国力通能源环保股份有限公司 | Coke oven gas complex iron desulfurization recycling process method and device |
| CN116425120A (en) * | 2023-04-23 | 2023-07-14 | 武汉国力通能源环保股份有限公司 | Method and device for producing high-quality sulfur by refining sulfur paste |
-
2009
- 2009-06-26 CN CNA2009101505657A patent/CN101591006A/en active Pending
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109160492A (en) * | 2018-09-04 | 2019-01-08 | 宜宾丝丽雅股份有限公司 | A kind of sulphur cream washing system and method |
| CN109160492B (en) * | 2018-09-04 | 2022-04-12 | 宜宾丝丽雅股份有限公司 | Sulfur paste washing system and method |
| CN109467058A (en) * | 2018-12-21 | 2019-03-15 | 浙江埃森化学有限公司 | A kind of melting and oxidative purification of diethylaluminum monochloride by-product sulphur |
| CN109467058B (en) * | 2018-12-21 | 2022-06-17 | 浙江埃森化学有限公司 | Melting and oxidation purification method of ethyl chloride byproduct sulfur |
| CN111807331A (en) * | 2020-06-30 | 2020-10-23 | 浙江佳运能源技术有限公司 | Efficient and energy-saving sulfur purification device and process thereof |
| CN114806649A (en) * | 2022-04-19 | 2022-07-29 | 武汉国力通能源环保股份有限公司 | Coke oven gas complex iron desulfurization recycling process method and device |
| CN114806649B (en) * | 2022-04-19 | 2023-11-24 | 武汉国力通能源环保股份有限公司 | Coke oven gas complex iron desulfurization resource processing method and device |
| CN116425120A (en) * | 2023-04-23 | 2023-07-14 | 武汉国力通能源环保股份有限公司 | Method and device for producing high-quality sulfur by refining sulfur paste |
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