CN112225183B - System and method for purifying sodium salt in coal gas desulfurization - Google Patents
System and method for purifying sodium salt in coal gas desulfurization Download PDFInfo
- Publication number
- CN112225183B CN112225183B CN202011075791.6A CN202011075791A CN112225183B CN 112225183 B CN112225183 B CN 112225183B CN 202011075791 A CN202011075791 A CN 202011075791A CN 112225183 B CN112225183 B CN 112225183B
- Authority
- CN
- China
- Prior art keywords
- kettle
- pipeline
- evaporation
- tank
- condensation cooler
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/64—Thiosulfates; Dithionites; Polythionates
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
- C01C3/00—Cyanogen; Compounds thereof
- C01C3/20—Thiocyanic acid; Salts thereof
Abstract
The invention relates to the technical field of coking tail gas treatment, in particular to a system and a method for purifying coal gas desulfurization sodium salt. The device comprises a first evaporation kettle, a second evaporation kettle, a first condensation cooler, a second condensation cooler, a first vacuum tank, a second vacuum tank, an evaporation kettle, a storage kettle, a decoloring kettle, a filter press, a centrifuge and a new underground tank, wherein the first evaporation kettle, the second evaporation kettle, the first condensation cooler, the second condensation cooler, the first vacuum tank and the second vacuum tank are connected; store up the cauldron and link to each other with the condensation cooler through the pipeline, the condensation cooler passes through the pipeline and links to each other with the vacuum tank, stores up the cauldron and links to each other with centrifuge through the pipeline, and centrifuge passes through the pipeline and links to each other with new underground tank, and the decoloration cauldron passes through the pipeline and links to each other with the pressure filter, and the pressure filter passes through the pipeline and links to each other with new underground tank. The method can realize the decolorization and purification of sodium thiosulfate and sodium thiocyanate in the gas desulfurization solution, purify the desulfurization solution, ensure the qualified environmental index of hydrogen sulfide after the tower and realize the increase of economic benefit.
Description
Technical Field
The invention relates to the technical field of coking tail gas treatment, in particular to a system and a method for purifying coal gas desulfurization sodium salt.
Background
The fine desulfurization process of the recovery operation area of the coking plant contains a salt extraction part, and the prior system and method for purifying the sodium salt of the coal gas desulfurization have the following defects: firstly, it is little to carry salt system ability, only 2 evaporation kettles and affiliated condensing cooler, vacuum pump, only move two evaporation kettles, if vice salt content continues to rise, when vice salt content exceedes 350g/L, easy undulant, the easy crystallization of sulfur melter of H2S content behind the second grade tower is blockked up, influences pelletizing, power boiler, the normal production of coal gas user. Secondly, when the content of the secondary salt is more than or equal to 300g/L, the sulfur melter, the settling tank and the front and rear pipelines are easy to block, the temperature of the middle section of the sulfur melter is low, the sulfur yield is low, and the suspension sulfur of a clear liquid and desulfurization liquid system is easy to be high; thirdly, the product of the originally designed device is a mixture of sodium thiosulfate and sodium thiocyanate, namely mixed salt which is not decolored, the mixed salt product has no market demand and can only be processed in a coal blending mode, and once the only processing mode is interrupted, a large amount of accumulated mixed salt can be caused and stored everywhere, so that the online production and the coal gas desulfurization are influenced.
Disclosure of Invention
In order to overcome the defects of the prior art, the invention provides a system and a method for purifying sodium sulfide in coal gas desulfurization solution, so that the sodium thiosulfate and sodium thiocyanate in the coal gas desulfurization solution are decolorized and purified, the desulfurization solution is purified, the qualified environmental-friendly indexes of hydrogen sulfide after a tower can be ensured, and the increase of economic benefits can be realized.
In order to achieve the purpose, the invention adopts the following technical scheme:
the utility model provides a coal gas desulfurization sodium salt purification system, includes first evaporation cauldron, second evaporation cauldron, third evaporation cauldron, fourth evaporation cauldron, first condensation cooler, second condensation cooler, third condensation cooler, fourth condensation cooler, fifth condensation cooler, first vacuum tank, second vacuum tank, third vacuum tank, fourth vacuum tank, fifth vacuum tank, store up the cauldron, first settling cask, second settling cask, first sulfur melter, second sulfur melter, first underground tank, second underground tank, first centrifuge, second centrifuge, first decoloration cauldron, second decoloration cauldron, first pressure filter and second pressure filter.
The first evaporation kettle is connected with a first condensation cooler through a pipeline, the second evaporation kettle is connected with a second condensation cooler through a pipeline, the first condensation cooler and the second condensation cooler are respectively connected with a first vacuum tank and a second vacuum tank through pipelines, and the first condensation cooler and the second condensation cooler are connected with a first underground tank through pipelines; the storage kettle is connected with a fifth condensation cooler through a pipeline, the fifth condensation cooler is connected with a fifth vacuum tank through a pipeline, the storage kettle is connected with a first centrifugal machine and a second centrifugal machine through pipelines, the first centrifugal machine and the second centrifugal machine are connected with a second underground tank through pipelines, the first decoloring kettle and the second decoloring kettle are connected with a first filter press and a second filter press through pipelines, and the first filter press and the second filter press are connected with the second underground tank through pipelines.
The third evaporation kettle is connected with a third condensation cooler through a pipeline, and the third condensation cooler is connected with a third vacuum tank through a pipeline; the fourth evaporation kettle is connected with a fourth condensation cooler through a pipeline, and the fourth condensation cooler is connected with a fourth vacuum groove through a pipeline.
The first decoloring kettle is connected with a first filter press through a pipeline, the first filter press is connected with a second underground tank through a pipeline, the second decoloring kettle is connected with a second filter press through a pipeline, and the second filter press is connected with the second underground tank through a pipeline.
One end of the first centrifugal machine is connected with the storage kettle through a pipeline, the other end of the first centrifugal machine is connected with the second underground groove through a pipeline, one end of the second centrifugal machine is connected with the storage kettle through a pipeline, and the other end of the second centrifugal machine is connected with the second underground groove through a pipeline.
The first evaporation kettle is connected with the first settling tank through a pipeline, the first settling tank is connected with the first sulfur melter through a pipeline, the second evaporation kettle is connected with the second settling tank through a pipeline, and the second settling tank is connected with the second sulfur melter through a pipeline.
A purification method of sodium salt for coal gas desulfurization specifically comprises the following steps:
1) after the fine desulfurization settling tank, the desulfurization solution enters a first decolorizing kettle and a second decolorizing kettle to remove color; pumping the decolored clear desulfurization liquid to a first filter press and a second filter press by a pump, filtering out activated carbon, and then automatically flowing to a second underground tank;
2) pumping the liquid in the second underground tank to a first evaporation kettle, a second evaporation kettle, a third evaporation kettle and a fourth evaporation kettle for evaporation and separation, wherein the vacuum degrees of the first evaporation kettle, the second evaporation kettle, the third evaporation kettle and the fourth evaporation kettle are controlled to be between 50Kpa and 80Kpa, and the temperature is controlled to be between 90 ℃ and 110 ℃;
3, emptying the materials to the storage kettle after the third evaporation kettle and the fourth evaporation kettle are evaporated, and pumping the qualified materials to the storage kettle through a storage kettle negative pressure pipeline after the salt in the first evaporation kettle and the second evaporation kettle is evaporated;
4) the materials in the storage kettle are pumped to a first centrifugal machine and a second centrifugal machine by a pump, clear liquid enters a second underground tank after centrifugal separation, white mixed salt enters a salt mixing pool, and the white mixed salt is weighed and bagged after being dried.
Compared with the prior art, the invention has the beneficial effects that:
1. the raw product is green and has no market demand, and the product produced by the method is white and has market demand, thereby avoiding the influence of coal blending on coking, belonging to the domestic initiative and being capable of being directly sold with certain economic benefit.
2. The method can ensure the balance of the auxiliary salt in the desulfurization solution, ensure the qualified hydrogen sulfide after the fine desulfurization device and the qualified quality of the pellet-feeding gas, and is of great importance for the overall economic benefit of iron and steel enterprises.
Drawings
FIG. 1 is a schematic diagram of the structure and process of the present invention;
FIG. 2 is a schematic block diagram of the process of the present invention.
In the figure: 1-first evaporation kettle 2-second evaporation kettle 3-third evaporation kettle 4-fourth evaporation kettle 5-first condensing cooler 6-second condensing cooler 7-third condensing cooler 8-fourth condensing cooler 9-first vacuum tank 10-second vacuum tank 11-third vacuum tank 12-fourth vacuum tank 13-storage kettle 14-fifth condensing cooler 15-fifth vacuum tank 16-first settling tank 17-second settling tank 18-first sulfur melter 19-second sulfur melter 20-first underground tank 21-second underground tank 22-first centrifuge 23-second centrifuge 24-first decolorizing kettle 25-second decolorizing kettle 26-first filter press 27-second filter press.
Detailed Description
The following further describes embodiments of the present invention with reference to the accompanying drawings:
as shown in fig. 1, a system for purifying sodium salts of coal gas desulfurization comprises a first evaporation kettle 1, a second evaporation kettle 2, a third evaporation kettle 3, a fourth evaporation kettle 4, a first condensation cooler 5, a second condensation cooler 6, a third condensation cooler 7, a fourth condensation cooler 8, a first vacuum tank 9, a second vacuum tank 10, a third vacuum tank 11, a fourth vacuum tank 12, a storage kettle 13, a fifth condensation cooler 14, a fifth vacuum tank 15, a first settling tank 16, a second settling tank 17, a first sulfur melter 18, a second sulfur melter 19, a first underground tank 20, a second underground tank 21, a first centrifuge 22, a second centrifuge 23, a first decolorizing kettle 24, a second decolorizing kettle 25, a first filter press 26 and a second filter press 27.
The first evaporation kettle 1 is connected with a first condensation cooler 5 through a pipeline, and the first condensation cooler 5 is connected with a first vacuum groove 9 through a pipeline. The first evaporator 1 is connected to a first settling tank 16 through a pipeline, and the first settling tank 16 is connected to a first sulfur melter 18 through a pipeline.
The second evaporation kettle 2 is connected with a second condensation cooler 6 through a pipeline, the second condensation cooler 6 is connected with a second vacuum groove 10 through a pipeline, the second evaporation kettle 2 is connected with a second settling tank 17 through a pipeline, and the second settling tank 17 is connected with a second sulfur melter 19 through a pipeline.
The third evaporation kettle 3 is connected with a third condensation cooler 7 through a pipeline, and the third condensation cooler 7 is connected with a third vacuum groove 11 through a pipeline.
The fourth evaporation kettle 4 is connected with a fourth condensation cooler 8 through a pipeline, and the fourth condensation cooler 8 is connected with a fourth vacuum groove 12 through a pipeline.
The storage tank 13 is connected with a fifth condensation cooler 14 through a pipeline, and the fifth condensation cooler 14 is connected with a fifth vacuum tank 15 through a pipeline. One end of the first centrifuge 22 is connected with the storage kettle 13 through a pipeline, and the other end is connected with the second underground tank 21 through a pipeline. One end of the second centrifugal machine 23 is connected with the storage kettle 13 through a pipeline, and the other end is connected with the second underground tank 21 through a pipeline.
The first decoloring tank 24 is connected to a first filter press 26 through a pipe, and the first filter press 26 is connected to a second underground tank 21 through a pipe. The second decoloring tank 25 is connected to a second filter press 27 through a pipe, and the second filter press 27 is connected to a second underground tank 21 through a pipe.
The first condensate cooler 5, the second condensate cooler 6, the third condensate cooler 7, the fourth condensate cooler 8 and the fifth condensate cooler 14 are respectively connected with a first underground tank 20 through pipelines, and the first vacuum tank 9, the second vacuum tank 10, the third vacuum tank 11, the fourth vacuum tank 12 and the fifth vacuum tank 15 are respectively connected with the first underground tank 20 through pipelines.
The circulating water pipeline is connected with the first condensation cooler 5, the second condensation cooler 6, the third condensation cooler 7, the fourth condensation cooler 8 and the fifth condensation cooler 14. The compressed air pipeline, the dead steam pipeline and the steam pipeline are connected with the first evaporation kettle 1, the second evaporation kettle 2, the third evaporation kettle 3, the fourth evaporation kettle 4 and the storage kettle 13.
As shown in fig. 2, a method for purifying sodium salt of coal gas desulfurization specifically comprises the following steps:
1) after the fine desulfurization settling tank, the desulfurization solution firstly enters a first decolorizing kettle 24 and a second decolorizing kettle 25 to remove color; the decolorized desulfurized clear solution is pumped to a first filter press 26 and a second filter press 27 by a pump, wherein the diameters of the first filter press 26 and the second filter press 27 are 60m2The activated carbon is filtered and then flows to a second underground tank 21(V is 35 m)3)；
2) Pumping the liquid in the second underground tank 21 to a first evaporation kettle 1, a second evaporation kettle 2, a third evaporation kettle 3 and a fourth evaporation kettle 4 for evaporation and separation, wherein the vacuum degrees of the first evaporation kettle 1, the second evaporation kettle 2, the third evaporation kettle 3 and the fourth evaporation kettle 4 are controlled between 50Kpa and 80Kpa, and the temperature is controlled between 90 ℃ and 110 ℃;
3, emptying the materials to a storage kettle 13 after the third evaporation kettle 3 and the fourth evaporation kettle 4 are evaporated, and pumping the qualified materials to the storage kettle 13 through a negative pressure pipeline of the storage kettle 13 after the salt in the first evaporation kettle 1 and the second evaporation kettle 2 is evaporated;
4) the materials in the storage kettle 13 are pumped to a first centrifuge 22 and a second centrifuge 23 by a pump, the clear liquid enters a second underground tank 21 after centrifugal separation, the white mixed salt enters a mixed salt pool, and the white mixed salt is dried, weighed and bagged.
The raw product is green and has no market demand, and the product produced by the method is white and has market demand, thereby avoiding the influence of coal blending on coking, belonging to the domestic initiative and being capable of being directly sold with certain economic benefit. The invention can ensure the balance of the secondary salt in the desulfurization solution, ensure the qualification of hydrogen sulfide after a fine desulfurization device and the qualification of the quality of the pellet-feeding gas, and is of great importance to the overall economic benefit of iron and steel enterprises.
The above description is only for the preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art should be considered to be within the technical scope of the present invention, and the technical solutions and their concepts should be equivalent or changed within the technical scope of the present invention. The methods used in the above examples are conventional methods unless otherwise specified.
Claims (6)
1. A coal gas desulfurization sodium salt purification system is characterized in that: the device comprises a first evaporation kettle, a second evaporation kettle, a third evaporation kettle, a fourth evaporation kettle, a first condensation cooler, a second condensation cooler, a third condensation cooler, a fourth condensation cooler, a fifth condensation cooler, a first vacuum tank, a second vacuum tank, a third vacuum tank, a fourth vacuum tank, a fifth vacuum tank, a storage kettle, a first settling tank, a second settling tank, a first sulfur melter, a second sulfur melter, a first underground tank, a second underground tank, a first centrifugal machine, a second centrifugal machine, a first decolorizing kettle, a second decolorizing kettle, a first filter press and a second filter press;
the first evaporation kettle is connected with a first condensation cooler through a pipeline, the second evaporation kettle is connected with a second condensation cooler through a pipeline, the first condensation cooler and the second condensation cooler are respectively connected with a first vacuum tank and a second vacuum tank through pipelines, and the first condensation cooler and the second condensation cooler are connected with a first underground tank through pipelines; the storage kettle is connected with a fifth condensation cooler through a pipeline, the fifth condensation cooler is connected with a fifth vacuum tank through a pipeline, the storage kettle is connected with a first centrifugal machine and a second centrifugal machine through pipelines, the first centrifugal machine and the second centrifugal machine are connected with a second underground tank through pipelines, the first decoloring kettle and the second decoloring kettle are connected with a first filter press and a second filter press through pipelines, and the first filter press and the second filter press are connected with the second underground tank through pipelines.
2. The system for purifying the sodium salt of coal gas desulfurization according to claim 1, wherein: the third evaporation kettle is connected with a third condensation cooler through a pipeline, and the third condensation cooler is connected with a third vacuum tank through a pipeline; the fourth evaporation kettle is connected with a fourth condensation cooler through a pipeline, and the fourth condensation cooler is connected with a fourth vacuum groove through a pipeline.
3. The system for purifying the sodium salt of coal gas desulfurization according to claim 1, wherein: the first decoloring kettle is connected with a first filter press through a pipeline, the first filter press is connected with a second underground tank through a pipeline, the second decoloring kettle is connected with a second filter press through a pipeline, and the second filter press is connected with the second underground tank through a pipeline.
4. The system for purifying the sodium salt of coal gas desulfurization according to claim 1, wherein: one end of the first centrifugal machine is connected with the storage kettle through a pipeline, the other end of the first centrifugal machine is connected with the second underground groove through a pipeline, one end of the second centrifugal machine is connected with the storage kettle through a pipeline, and the other end of the second centrifugal machine is connected with the second underground groove through a pipeline.
5. The system for purifying the sodium salt of coal gas desulfurization according to claim 1, wherein: the first evaporation kettle is connected with the first settling tank through a pipeline, the first settling tank is connected with the first sulfur melter through a pipeline, the second evaporation kettle is connected with the second settling tank through a pipeline, and the second settling tank is connected with the second sulfur melter through a pipeline.
6. The method for purifying the sodium salt of coal gas desulfurization based on the system for purifying the sodium salt of coal gas desulfurization as claimed in claim 1, 2, 3, 4 or 5 is characterized by comprising the following steps:
1) after the fine desulfurization settling tank, the desulfurization solution enters a first decolorizing kettle and a second decolorizing kettle to remove color; pumping the decolored clear desulfurization liquid to a first filter press and a second filter press by a pump, filtering out activated carbon, and then automatically flowing to a second underground tank;
2) pumping the liquid in the second underground tank to a first evaporation kettle, a second evaporation kettle, a third evaporation kettle and a fourth evaporation kettle for evaporation and separation, wherein the vacuum degrees of the first evaporation kettle, the second evaporation kettle, the third evaporation kettle and the fourth evaporation kettle are controlled to be between 50Kpa and 80Kpa, and the temperature is controlled to be between 90 ℃ and 110 ℃;
3) after the evaporation of the third evaporation kettle and the fourth evaporation kettle is finished, emptying the materials to the storage kettle, and pumping the qualified materials after the salt evaporation in the first evaporation kettle and the second evaporation kettle to the storage kettle through a storage kettle negative pressure pipeline;
4) the materials in the storage kettle are pumped to a first centrifugal machine and a second centrifugal machine by a pump, clear liquid enters a second underground groove after centrifugal separation, white mixed salt enters a mixed salt pond, and the white mixed salt is dried, weighed and bagged.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011075791.6A CN112225183B (en) | 2020-10-10 | 2020-10-10 | System and method for purifying sodium salt in coal gas desulfurization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011075791.6A CN112225183B (en) | 2020-10-10 | 2020-10-10 | System and method for purifying sodium salt in coal gas desulfurization |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112225183A CN112225183A (en) | 2021-01-15 |
| CN112225183B true CN112225183B (en) | 2022-05-10 |
Family
ID=74120700
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011075791.6A Active CN112225183B (en) | 2020-10-10 | 2020-10-10 | System and method for purifying sodium salt in coal gas desulfurization |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112225183B (en) |
Family Cites Families (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3412637B2 (en) * | 1992-11-19 | 2003-06-03 | 日本エクスラン工業株式会社 | Recovery of rodan salt |
| MXPA04005711A (en) * | 2001-12-13 | 2005-06-20 | Univ Lehigh | Oxidative desulfurization of sulfur-containing hydrocarbons. |
| CN101597522B (en) * | 2009-06-29 | 2011-02-23 | 朱春阳 | Desulfuration processing method of coke oven gas and special device thereof |
| CN103058442B (en) * | 2013-01-25 | 2014-08-20 | 甘肃银光聚银化工有限公司 | Method for processing secondary salt in desulphurization waste liquid |
| CN103979577B (en) * | 2014-05-21 | 2015-12-02 | 黄进前 | A kind of coking desulfurization mixed salt extracts the method for sodium sulfocyanate |
| CN108217690A (en) * | 2018-03-14 | 2018-06-29 | 湖南华菱涟源钢铁有限公司 | A kind of technique that secondary salt is extracted from desulfurization waste liquor |
| CN111675272A (en) * | 2020-06-12 | 2020-09-18 | 东方电气集团东方锅炉股份有限公司 | Steel plant desulfurization wastewater resource zero-discharge process and system |
-
2020
- 2020-10-10 CN CN202011075791.6A patent/CN112225183B/en active Active
Also Published As
| Publication number | Publication date |
|---|---|
| CN112225183A (en) | 2021-01-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102816619B (en) | Method and device for recovery coupling of biological sulfur and carbon dioxide for producing biogas | |
| CN109650413B (en) | Method and system for enriching lithium from sodium aluminate solution in alumina plant | |
| CN101323614B (en) | Acidum folicum production method without sewerage discharge | |
| CN103233083A (en) | Sugar juice settle low-ash low-temperature carbonating method | |
| CN105130854A (en) | Improved H acid production process | |
| CN103525887B (en) | A kind of crystalline dextrose production method of energy-conserving and environment-protective | |
| CN112225183B (en) | System and method for purifying sodium salt in coal gas desulfurization | |
| CN213977333U (en) | Zero-discharge treatment system for boiler desulfurization wastewater | |
| CN102336650A (en) | Stripping process and device for removing organic impurities in brufen sodium salt | |
| CN113955811A (en) | Method for producing crude cobalt hydroxide from industrial cobalt-containing low-copper raffinate | |
| CN112593016A (en) | Process for preparing high-quality white granulated sugar and fulvic acid dry powder from beet | |
| CN107540003A (en) | Lithium sulfate thickening-purification technology liquid and preparation method thereof in one kind production battery-level lithium carbonate technique | |
| CN108483463B (en) | Method for preparing high-quality ammonium sulfate by using coking desulfurization and decyanation waste liquid | |
| CN110746273A (en) | Purification process of biodiesel byproduct glycerol | |
| CN1629320A (en) | Process for cleaning sugar cane juice in sugar production from sugar cane | |
| CN101481097A (en) | Method for processing waste acid from sulphonation ester production | |
| CN114797171A (en) | Production device and production process for extracting lithium from brine by efficient adsorption method | |
| CN214570785U (en) | System for extracting magnesium sulfate and sodium chloride from desulfurization wastewater | |
| CN209974511U (en) | Desulfurization water zero release comprehensive utilization device | |
| CN204174288U (en) | A kind of ion film caustic soda production equipment improving bittern usage ratio | |
| CN217164375U (en) | Accelerator M purification device | |
| CN219907707U (en) | Purification system suitable for xylose solution prepared from waste alkali liquor containing hemicellulose | |
| CN1616352A (en) | Process for extracting sodium bromide | |
| CN108455775A (en) | A kind of twin flue embrane method denitrification apparatus and application method | |
| CN1081617C (en) | Method for prodn. of glycerin by using waste liquor from saponification process |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |