CN202876623U - Continuous absorption tower system of hydrogen sulfide in process of sulphide isobutene production - Google Patents
Continuous absorption tower system of hydrogen sulfide in process of sulphide isobutene production Download PDFInfo
- Publication number
- CN202876623U CN202876623U CN 201220588771 CN201220588771U CN202876623U CN 202876623 U CN202876623 U CN 202876623U CN 201220588771 CN201220588771 CN 201220588771 CN 201220588771 U CN201220588771 U CN 201220588771U CN 202876623 U CN202876623 U CN 202876623U
- Authority
- CN
- China
- Prior art keywords
- absorption tower
- liquid back
- liquid return
- back pipe
- mixing pit
- 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.)
- Expired - Fee Related
Links
Images
Abstract
The utility model discloses a continuous absorption tower system of hydrogen sulfide in the process of sulphide isobutene production, which comprises a hydrogen sulphide inlet end, an exhaust end, a sodium sulphide recovery pool, absorption towers, liquid return pipes, mixing pools and a sodium hydroxide supplementing pool; and the continuous absorption tower system is characterized in that the number of the absorption tower is 3-5, the liquid return pipes include a liquid return pipe I and a liquid return pipe II, the hydrogen sulphide inlet end is connected with the bottom of the first absorption tower, adjacent absorption towers are connected in series with each other, and the top of the tail absorption tower is provided with an exhaust pipe; the bottom of each absorption tower is provided with a drain pipe, and a corresponding mixing pool is arranged below each absorption tower; and the mixing pool is connected with the upper part of the corresponding absorption tower through the liquid return pipe II, the sodium hydroxide supplementing pool is connected with the first mixing pool through the liquid return pipe I, adjacent mixing pools are connected through the liquid return pipe I, and the tail mixing pool is connected with the sodium sulphide recovery pool through the liquid return pipe I. According to the utility model, tail gas is concentrated, and after orderly absorbed by an absorption system, the tail gas is subjected to pollution-free discharge; and a situation that H2S gas is completely converted into Na2S and NaHS is ensured, wherein a situation that the tail gas subjected to absorption does not contain H2S gas is ensured.
Description
Technical field
The utility model relates to a kind of waste gas absorbing system, relates in particular to the recovery system of hydrogen sulfide in a kind of sulfide isobutene production process, belongs to field of fine chemical.
Background technology
Sulfide isobutene (T321) is a kind of lubricated oil additive, and oil-soluble is good, and sulfur-bearing is high, and is little to the corrosivity of non-ferrous metal, is widely used in modulating in the complexing agent of automotive gear oil, instrument gear oil, and there is no at present alternative product.But the dechlorination reaction in the production process of sulfide isobutene can produce a large amount of hydrogen sulfide, if deal with improperly, not only reduces air quality, and wastes a large amount of sulphur resources, has improved production cost.
Summary of the invention
For addressing the above problem, of the present utility modelly provide a kind of waste gas absorption circulation recycling system, be the continuous absorption tower group of hydrogen sulfide in a kind of sulfide isobutene production process specifically.
The purpose of this utility model is achieved in that the continuous absorption tower group of hydrogen sulfide in this sulfide isobutene production process, comprise that hydrogen sulfide inlet end, exhaust end, vulcanized sodium recovery pond, absorption tower, liquid back pipe, mixing pit, NaOH replenish the pond, its technical essential is: described absorption tower is 3-5, described liquid back pipe comprises liquid back pipe I and liquid back pipe II, the hydrogen sulfide inlet end links to each other with bottom, first absorption tower, adjacent absorption tower is connected in series each other, and top, last absorption tower is provided with blast pipe; The bottom, absorption tower is provided with discharging tube, and corresponding mixing pit is set under the absorption tower; Mixing pit links to each other with respective absorption tower top by liquid back pipe II, and described NaOH replenishes the pond and links to each other with first mixing pit by liquid back pipe I, and adjacent mixing pit links to each other by liquid back pipe I, and last mixing pit links to each other with the vulcanized sodium recovery pond by liquid back pipe I.
Described absorption tower is spray absorber.
Between the described adjacent absorption tower pressue device is set.
Compared with prior art, the utlity model has following advantage: the equipment in the utility model adopts total closed type, tail gas is concentrated, in an orderly manner non-pollution discharge after absorption system absorbs; By the multitower of many reactions column plate, multistage alkali liquor absorption, guaranteed H
2S gas is converted into Na fully
2S and NaHS wherein do not contain H for the tail gas after guaranteeing to absorb
2S gas.
Description of drawings
Fig. 1 is the utility model structural representation.
Main symbol description in the accompanying drawing: A. hydrogen sulfide gas; 1. vulcanized sodium recovery pond; 2. liquid back pipe I; 3. pressue device; 4. the first spray absorber; 5. the 4th mixing pit; 6. liquid back pipe II; 7. breather pipe; 8. NaOH replenishes the pond.
Water pump partly omits among the figure.
The below will be described in further detail the utility model by drawings and Examples; but following example only is the utility model example wherein; do not represent the rights protection scope that the utility model limits, rights protection scope of the present utility model is as the criterion with claims.
The specific embodiment
Embodiment 1
The continuous absorption tower group of hydrogen sulfide in this sulfide isobutene production process, comprise that hydrogen sulfide inlet end, exhaust end, vulcanized sodium recovery pond 1, four spray absorbers, six pressue devices, liquid back pipe I, liquid back pipe II, breather pipe 7, mixing pit 5, NaOH replenish pond 8, the hydrogen sulfide inlet end is provided with the first pressue device 3, the first pressue device bottom links to each other with bottom, first absorption tower, adjacent absorption tower serial connection, be provided with the second to the 4th pressue device between the adjacent absorption tower, top, the 4th absorption tower is provided with the blast pipe blast pipe and is provided with the slender acanthopanax pressure device; Corresponding mixing pit is set under each absorption tower; Mixing pit links to each other with respective absorption tower top by liquid back pipe II, and described NaOH replenishes the pond and links to each other with first mixing pit by liquid back pipe I, and adjacent mixing pit links to each other by liquid back pipe I, and last mixing pit links to each other with the vulcanized sodium recovery pond by liquid back pipe I.
The utility model workflow is as follows: hydrogen sulfide gas A enters the first absorption tower after at first entering the first pressue device, with enter the second pressue device by top, the first absorption tower in the NaOH solution in the tower and afterwards, then enter second absorption tower, absorb one by one until hydrogen sulfide absorbs fully, finally by behind the slender acanthopanax pressure device discharged in the atmosphere.
Each arranges corresponding mixing pit under absorbing, and the absorption tower is in absorption and H
2To contain Na from the bottom behind the S gas
2The solution of S, NaOH, NaHS be disposed in the corresponding mixing pit with the next stage mixing pit in have higher concentration NaOH mixed liquor and mix, by liquid back pipe II mixed liquor is pumped in the corresponding absorption tower of this mixing pit again after mixing.
For guaranteeing the NaOH concentration in the absorption system, a NaOH replenishes the pond in the terminal serial connection of the first mixing pit; Main component in first to fourth mixing pit is Na
2S, NaOH, NaHS, wherein the NaOH solution concentration is successively decreased in gradient, NaOH concentration＜0.5% in the 4th mixing pit wherein, NaHS concentration＜0.5%, Na
2S concentration is 15-20%; NaOH concentration is 6-12% in the 3rd mixing pit; NaOH concentration is 12-16% in the second mixing pit; NaOH concentration is 16-20% in the first mixing pit; It is 21-25% that NaOH replenishes the NaOH concentration of preparing in the pond.
The Na in the 4th mixing pit the most at last
2S solution pumps into the vulcanized sodium recovery pond, enters next reaction system after the mensuration concentration and recycles.
Claims (3)
1. the continuous absorption tower group of hydrogen sulfide in the sulfide isobutene production process, comprise that hydrogen sulfide inlet end, exhaust end, vulcanized sodium recovery pond, absorption tower, liquid back pipe, mixing pit, NaOH replenish the pond, it is characterized in that: described absorption tower is 3-5, described liquid back pipe comprises liquid back pipe I and liquid back pipe II, the hydrogen sulfide inlet end links to each other with bottom, first absorption tower, adjacent absorption tower is connected in series each other, and top, last absorption tower is provided with blast pipe; The bottom, absorption tower is provided with discharging tube, and corresponding mixing pit is set under the absorption tower; Mixing pit links to each other with respective absorption tower top by liquid back pipe II, and described NaOH replenishes the pond and links to each other with first mixing pit by liquid back pipe I, and adjacent mixing pit links to each other by liquid back pipe I, and last mixing pit links to each other with the vulcanized sodium recovery pond by liquid back pipe I.
2. absorption tower according to claim 1 group, it is characterized in that: described absorption tower is spray absorber.
3. absorption tower according to claim 1 and 2 group is characterized in that: between the described adjacent absorption tower pressue device is set.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220588771 CN202876623U (en) | 2012-11-09 | 2012-11-09 | Continuous absorption tower system of hydrogen sulfide in process of sulphide isobutene production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220588771 CN202876623U (en) | 2012-11-09 | 2012-11-09 | Continuous absorption tower system of hydrogen sulfide in process of sulphide isobutene production |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202876623U true CN202876623U (en) | 2013-04-17 |
Family
ID=48068089
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220588771 Expired - Fee Related CN202876623U (en) | 2012-11-09 | 2012-11-09 | Continuous absorption tower system of hydrogen sulfide in process of sulphide isobutene production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202876623U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104826465A (en) * | 2014-02-10 | 2015-08-12 | 中国石油化工股份有限公司 | Multi-stage countercurrent absorption process and system for acidic gas |
| CN104826464A (en) * | 2014-02-10 | 2015-08-12 | 中国石油化工股份有限公司 | Novel acidic gas treating process and apparatus |
-
2012
- 2012-11-09 CN CN 201220588771 patent/CN202876623U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104826465A (en) * | 2014-02-10 | 2015-08-12 | 中国石油化工股份有限公司 | Multi-stage countercurrent absorption process and system for acidic gas |
| CN104826464A (en) * | 2014-02-10 | 2015-08-12 | 中国石油化工股份有限公司 | Novel acidic gas treating process and apparatus |
| CN104826464B (en) * | 2014-02-10 | 2017-05-17 | 中国石油化工股份有限公司 | Novel acidic gas treating process and apparatus |
| CN104826465B (en) * | 2014-02-10 | 2017-05-17 | 中国石油化工股份有限公司 | Multi-stage countercurrent absorption process and system for acidic gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101703883B (en) | Method for depriving sulfureted hydrogen in biogas and device | |
| CN105664693A (en) | Sulfuric acid tail gas desulphurization apparatus by oxidation process and usage method thereof | |
| CN102921277A (en) | Hydrogen sulfide tail gas treatment system and method | |
| CN202876623U (en) | Continuous absorption tower system of hydrogen sulfide in process of sulphide isobutene production | |
| CN104208987A (en) | Tail gas recovery device for urea ammonium nitrate solution production | |
| CN201735309U (en) | Unitization efficient tail gas absorbing device for leather tail gas treatment | |
| CN202881200U (en) | Desulfurizing device for gas of finery | |
| CN202070285U (en) | Device for removing sulfur dioxides in sulphuric acid industrial tail gas and recovering sulphuric acid | |
| CN204237560U (en) | A kind of device preparing Sodium sulfhydrate | |
| CN104971597B (en) | A kind of sour gas produces NaHS process and device | |
| CN203725014U (en) | Hydrogen sulfide gas purification device | |
| CN104383800A (en) | Flue gas desulfurizing device | |
| CN212383460U (en) | Treatment system for absorbing tail gas sulfur dioxide gas | |
| CN104971600B (en) | A kind of sour gas tubular reactor and handling process method | |
| CN104971601B (en) | Acid gas vertical reactor and processing method | |
| CN102908970A (en) | Dual-circulation injection reactor | |
| CN206577587U (en) | Sulfurous gas liquid phase regenerating desulfurization integral system | |
| CN203017976U (en) | Concentrated nitric acid mist recycling device | |
| CN203700309U (en) | Integrated marsh gas biological desulfuration device | |
| CN106082538B (en) | A kind of processing system and its processing method for producing vulcanized sodium using sewage | |
| CN204619685U (en) | A kind of injecting type membrane filtration fine de-sulfur equipment being applicable to refinery | |
| CN203507809U (en) | Circulating desulfurization device of spandex waste liquid | |
| CN205055817U (en) | High -efficient natural gas hypergravity desulfurization process device of marine sled dress type | |
| CN104971599B (en) | A kind of sour gas reactor and handling process | |
| CN102886194A (en) | Sulphur melting odor removing absorbing device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130417 Termination date: 20201109 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |