CN208362277U - A kind of device of gas material removing organic sulfur - Google Patents
A kind of device of gas material removing organic sulfur Download PDFInfo
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- CN208362277U CN208362277U CN201820931859.8U CN201820931859U CN208362277U CN 208362277 U CN208362277 U CN 208362277U CN 201820931859 U CN201820931859 U CN 201820931859U CN 208362277 U CN208362277 U CN 208362277U
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Abstract
The utility model discloses a kind of devices of gas material removing organic sulfur, sulfurous gas material enters desulfurization extraction tower by gas distributor, desulfurizing agent enters desulfurization extraction tower from liquid distribution trough after the pressurization of desulfurizing agent circulating pump, gas-liquid two-phase reverse flow simultaneously passes through extracting tower packing contact in desulfurization extraction tower, carbonyl sulfur in sulfurous gas material hydrolyzes in desulfurization extraction tower generates hydrogen sulfide and carbon dioxide, original hydrogen sulfide is absorbed in desulfurizing agent in the hydrogen sulfide and sulfurous gas material of generation, hydrogen sulfide containing richness desulfurizing agent part self-loopa, it send to regeneration unit part, gas material is sent out from desulfurization extraction tower top gas material discharge nozzle after desulfurization.It reverse flow and is come into full contact in desulfurization extraction tower by gaseous phase materials and desulfurizing agent, the carbonyl sulfur in gaseous phase materials can be removed to 10mg/Nm3Hereinafter, total sulfur can be removed to 20mg/Nm3It is regenerated, is recycled hereinafter, rich desulfurizing agent can heat parsing hydrogen sulfide.
Description
Technical field
The utility model relates to technical field of desulfurization, it particularly relates to a kind of device of gas material removing organic sulfur.
Background technique
Refinery decompressioning device, catalytic unit, delayed coking unit etc. can all have the fuel gas (also referred to as dry gas) of gas phase
It generates, oil gas field also has the natural gas of gas phase to generate.Fuel gas and natural gas main component are all hydrogen, methane and ethane.
The boiling point of hydrogen and lower molecular weight lighter hydrocarbons is as shown in the table:
| Name of material | Boiling point DEG C |
| Hydrogen | -252.8 |
| Methane | -161.5 |
| Ethane | -88.6 |
| Ethylene | -104 |
| Propane | -42 |
| Propylene | -47 |
| Butane | -0.5 |
| Butylene | -6.9 |
The boiling point of part low molecule Sulfur is as shown in the table:
| Sulfur title | Boiling point DEG C |
| Hydrogen sulfide | -60.4 |
| Carbonyl sulfur | -50 |
| Methyl mercaptan | 6 |
| Ethyl mercaptan | 36.2 |
| Methyl sulfide | 37.3 |
The boiling point for compareing above-mentioned two tables hydrogen, the boiling point of lower molecular weight lighter hydrocarbons and part low molecule Sulfur can be seen
Out, most hydrogen sulfide enter in boiling point minimum fuel gas or gas component, if the crude oil or oil gas field of processing are former
Expect that cos-containing, part carbonyl sulfur can also enter in fuel gas or gas component.
The fuel gas of oil plant production, is partially used as hydrogenation plant hydrogen gas production raw material, is partially used as fuel, at present oil gas
Field produces natural gas mainly as fuel.Fuel gas is such as used as hydrogenation plant hydrogen feed, it is desirable that total sulfur takes off to 0.5mg/Nm3With
Under.Water and carbon dioxide are generated when fuel gas and combustion of natural gas, then generate sulfur dioxide when not removing combustion of sulfur.People at any time
To the pay attention to day by day of living environment, nearly 2 years most areas require content of sulfur dioxide in discharge atmospheric air off-gas to be no more than
400mg/Nm3, some importance city requirement is no more than 100mg/Nm3, surrounding Beijing areas requirement is no more than 50mg/Nm3。
Fuel gas and selexol process generally use the vulcanization in packed extraction column amine liquid extraction process removing fuel gas at present
Sulfur content in gas material is removed to following 20mg/Nm by hydrogen, most low energy3, or even do not measure.
According to investigation, total sulfur is sometimes still high after the fuel gas and Natural Gas Amine elution vulcanization hydrogen production device of Some Enterprises production are de-
Up to 50-200mg/Nm3, hydrogen sulfide content therein is analyzed in 20mg/Nm3Hereinafter, hydrogen sulfide index reaches design requirement.Sampling
Sulfur speciation analysis is carried out, gas material is in addition to remaining trace hydrogen sulfide, and other sulphur almost all are carbonyl sulfur, and carbonyl sulfur is adopted
Doctor treatment is washed with amine to be difficult to remove.This carbonyl for just needing that other effective technologies is taken further to remove in above-mentioned gas material
Sulphur.
Carbonyl sulfur, which meets water, can occur hydrolysis, generate hydrogen sulfide and carbon dioxide, then pass through alkaline matter or adsorbent,
Hydrogen sulfide and carbon dioxide are removed, achievees the purpose that remove carbonyl sulfur.
Use more de- carbonyl sulfur technology for the hydrolyst of solid and desulfurizing agent technique at present.The technique desulfurization
Precision is high, but since solid hydrolyst and desulfurizing agent are more demanding to material cleannes, Gu method desulfurization process compared with
Long, number of devices is more, needs replacing hydrolyst and desulfurizing agent after device operation 1-2, operation is cumbersome, while also
Solid waste generates, if directly filled, can cause secondary pollution.It is more than 30mg/Nm especially for COS content3, need
Hydrolysis tower and fine de-sulfur tower each two are designed, serial operation, installation area is bigger, and investment increases, solid hydrolyst
It can be more frequent with desulfurizing agent replacement.
For the problems in the relevant technologies, currently no effective solution has been proposed.
Utility model content
For above-mentioned technical problem in the related technology, the utility model proposes a kind of dresses of gas material removing organic sulfur
It sets, is able to solve above-mentioned technical problem.
To realize the above-mentioned technical purpose, the technical solution of the utility model is achieved in that
A kind of device of gas material removing organic sulfur, including desulfurization extraction tower, the desulfurization extraction tower upper inside are set
There is liquid distribution trough, the desulfurization extraction tower inner lower is equipped with gas distributor, the liquid distribution trough and the gas point
Filled with tower packing is extracted between cloth device, gas material discharge nozzle, the liquid point are connected at the top of the desulfurization extraction tower
The upper end of cloth device is connected to one end of desulfurizing agent circulation pipe, and the other end of desulfurizing agent circulation pipe and the bottom end of desulfurization extraction tower connect
Logical, the desulfurizing agent circulation pipe is connected with desulfurizing agent circulating pump, and the lower end of the gas distributor and gas material inlet tube connect
Siphunculus, the desulfurizing agent circulation pipe are also connected with rich desulfurizing agent pipe, and the richness desulfurizing agent pipe passes through desulfurizing agent heat exchanger and regeneration
Unit connection.
Further, the regeneration unit includes regenerator, passes through return pipe and return tank top at the top of the regenerator
Left side phegma inlet communication is connected with reflux cooler, the return tank top right side and non-condensable gas pipe on the return pipe
Connection, the return tank bottom right are connect by reflux pump with regeneration overhead side；The regeneration tower bottom passes through poor desulfurization
Agent pipe is connected to desulfurizing agent heat exchanger, and the poor desulfurizing agent pipe is connected with poor desulfurizing agent pump, the desulfurizing agent heat exchanger and desulfurization
Desulfurizing agent cooler is also connected between agent circulation pipe；The poor desulfurizing agent pipe also passes through the left side for boiling desulfurizing agent pipe and reboiler again
Lower end connection, the left upper end of the reboiler is connected to regenerator bottom side, the right side of the reboiler respectively with steam pipe and
Condensate pipe connection.
Further, the regenerator is sieve-plate tower or packed tower.
Further, foam removal net is equipped between the liquid distribution trough at the top of the desulfurization extraction tower.
Further, coalescing-plate is equipped between the desulfurization extracting tower bottom and gas distributor.
Based on the sulfur method of gas material removing organic sulfur device, sulfurous gas material enters de- by gas distributor
Sulphur extraction tower, desulfurizing agent enter desulfurization extraction tower, gas-liquid two-phase reverse flow from liquid distribution trough after the pressurization of desulfurizing agent circulating pump
Extracting tower packing contact in desulfurization extraction tower is moved and passes through, the carbonyl sulfur in sulfurous gas material hydrolyzes life in desulfurization extraction tower
At hydrogen sulfide and carbon dioxide, original hydrogen sulfide is absorbed in desulfurizing agent in the hydrogen sulfide and sulfurous gas material of generation, is contained
The rich desulfurizing agent part self-loopa of hydrogen sulfide is partially sent to regeneration unit, and gas material is from gas at the top of desulfurization extraction tower after desulfurization
Body material discharge nozzle is sent out.
Further, regeneration unit includes regenerator, and rich desulfurizing agent and the poor desulfurizing agent heat exchange from regenerator bottom are laggard
Enter regenerator, reenters regenerator, hydrogen sulphide in the vapor phase and a small amount of desulfurizing agent steam from regeneration after desulfurizing agent heating in regenerator
Tower top is sent out, and enters return tank after cooling, and rich hydrogen sulfide containing fixed gas sends out return tank, and the desulfurizing agent of condensation returns to regeneration
Tower, the poor desulfurizing agent of the another way at regenerator bottom and rich desulfurizing agent, using cooling, merge after heat exchange with self-loopa desulfurizing agent
Into desulfurization extraction tower.
Further, the desulfurizing agent by mass percentage, is prepared by following raw material, the content of organic amine compound
For 39.999%wt-79.999%wt, the content of phase transfer catalyst is 20%wt-60%wt, the content 0.001%wt- of inorganic assistant
0.01%wt。
Further, in the desulfurization extraction tower mass ratio of gas material and desulfurizing agent be 50-300, gas material with
The reaction temperature of desulfurizing agent is 0-50 DEG C, pressure 0.2-1.5MPa.
Further, the regeneration column bottom temperature is 110-130 DEG C, and regenerator head temperature is 70-105 DEG C.
The utility model has the beneficial effects that the reverse flow and abundant in desulfurization extraction tower by gaseous phase materials and desulfurizing agent
It contacts, the carbonyl sulfur in gaseous phase materials can be removed to 10mg/Nm3Hereinafter, total sulfur can be removed to 20mg/Nm3Hereinafter, rich desulfurizing agent
Parsing hydrogen sulfide can be heated to be regenerated, be recycled, the sour gas that rich desulfurizer regeneration generates can send raw to sulphur unit
Produce sulphur, three-waste free discharge.
Detailed description of the invention
In order to illustrate the embodiment of the utility model or the technical proposal in the existing technology more clearly, below will be to embodiment
Needed in attached drawing be briefly described, it should be apparent that, the accompanying drawings in the following description is only the utility model
Some embodiments for those of ordinary skill in the art without creative efforts, can also be according to this
A little attached drawings obtain other attached drawings.
Fig. 1 is a kind of apparatus structure signal of gas material removing organic sulfur according to the utility model embodiment
Figure.
In figure: 1. desulfurization extraction towers；2. foam removal net；3. liquid distribution trough；4. extracting tower packing；5. gas is distributed
Device；6. coalescing-plate；7. desulfurizing agent circulating pump；8. regenerator；9. tower tray；10. reflux cooler；11. return tank；12.
Reflux pump；13. reboiler；14. poor desulfurizing agent pump；15. desulfurizing agent heat exchanger；16. desulfurizing agent cooler；17. steam
Pipe；18. condensate pipe；19. return pipe；20. boiling desulfurizing agent pipe again；21. gas material inlet tube；22. gas material goes out
Expects pipe；23. desulfurizing agent circulation pipe；24. rich desulfurizing agent pipe；25. poor desulfurizing agent pipe；26. non-condensable gas pipe.
Specific embodiment
The following will be combined with the drawings in the embodiments of the present invention, carries out the technical scheme in the embodiment of the utility model
Clearly and completely describe, it is clear that the described embodiments are only a part of the embodiments of the utility model, rather than whole
Embodiment.Based on the embodiments of the present invention, those of ordinary skill in the art's every other embodiment obtained, all belongs to
In the range of the utility model protection.
As shown in Figure 1, a kind of device of gas material removing organic sulfur according to the utility model embodiment, including
Desulfurization extraction tower 1,1 upper inside of desulfurization extraction tower are equipped with liquid distribution trough 3, and 1 inner lower of desulfurization extraction tower is set
There is gas distributor 5, filled with extracting tower packing 4, the desulfurization between the liquid distribution trough 3 and the gas distributor 5
The top of extraction tower 1 is connected with gas material discharge nozzle 22, the upper end of the liquid distribution trough 3 and the one of desulfurizing agent circulation pipe 23
End connection, the other end of desulfurizing agent circulation pipe 23 are connected to the bottom end of desulfurization extraction tower 1, and the desulfurizing agent circulation pipe 23 is connected with
Desulfurizing agent circulating pump 7, the lower end of the gas distributor 5 and 21 communicating pipe of gas material inlet tube, the desulfurizing agent circulation pipe
23 are also connected with rich desulfurizing agent pipe 24, and the richness desulfurizing agent pipe 24 is connected to by desulfurizing agent heat exchanger 15 with regeneration unit.
In a specific example, the regeneration unit includes regenerator 8, at the top of the regenerator 8 by return pipe 19 with
11 top left side phegma inlet communication of return tank is connected with reflux cooler 10, the return tank 11 on the return pipe 19
Top right side is connected to non-condensable gas pipe 26, and 11 bottom right of return tank is connect by reflux pump 12 with 8 top side portion of regenerator；
8 bottom of regenerator is connected to by poor desulfurizing agent pipe 25 with desulfurizing agent heat exchanger 15, and the poor desulfurizing agent pipe 25 is connected with poor
Desulfurizing agent pump 14, is also connected with desulfurizing agent cooler 16 between the desulfurizing agent heat exchanger 15 and desulfurizing agent circulation pipe 23；It is described
Poor desulfurizing agent pipe 25 is also connected to the lower-left end of reboiler 13 by boiling desulfurizing agent pipe 20 again, the left upper end of the reboiler 13 and
The connection of 8 bottom side of regenerator, the right side of the reboiler 13 is connect with steam pipe 17 and condensate pipe 18 respectively.
In a specific example, the regenerator 8 is sieve-plate tower or packed tower.
In a specific example, foam removal net 2 is equipped between 1 top of desulfurization extraction tower and the liquid distribution trough 3.
In a specific example, coalescing-plate 6 is equipped between 1 bottom of desulfurization extraction tower and gas distributor 5.
In a specific example, sulfurous gas material enters desulfurization extraction tower 1 by gas distributor 5, and desulfurizing agent is through de-
Enter desulfurization extraction tower 1 from liquid distribution trough 2 after the pressurization of sulphur agent circulating pump 7, gas-liquid two-phase reverse flow simultaneously passes through desulfurization and extracts
Extracting tower packing 4 contacts in tower 1, and the carbonyl sulfur in sulfurous gas material hydrolyzes in desulfurization extraction tower 1 generates hydrogen sulfide and two
Carbonoxide, original hydrogen sulfide is absorbed in desulfurizing agent in the hydrogen sulfide and sulfurous gas material of generation, hydrogen sulfide containing rich de-
Sulphur agent part self-loopa is partially sent to regeneration unit, and gas material is from 1 top gas material discharge nozzle of desulfurization extraction tower after desulfurization
22 send out.
In a specific example, regeneration unit includes regenerator 8, rich desulfurizing agent and the poor desulfurizing agent from 8 bottom of regenerator
Enter regenerator 8 after heat exchange, reenters regenerator 8, hydrogen sulphide in the vapor phase and a small amount of desulfurizing agent after desulfurizing agent heating in regenerator 8
Steam is pushed up from regenerator 8 and is sent out, and enters return tank 11 after cooling, and rich hydrogen sulfide containing fixed gas sends out return tank 11, condensation
Desulfurizing agent return to regenerator 8, the poor desulfurizing agent of another way at 8 bottom of regenerator and rich desulfurizing agent after heat exchange using cooling,
Desulfurization extraction tower 1 is combined into self-loopa desulfurizing agent.
In a specific example, the desulfurizing agent by mass percentage, is prepared, organic amine compound by following raw material
Content be 39.999%wt-79.999%wt, the content of phase transfer catalyst is 20%wt-60%wt, the content of inorganic assistant
0.001%wt-0.01%wt。
In a specific example, the mass ratio of gas material and desulfurizing agent is 50-300, gas in the desulfurization extraction tower 1
The reaction temperature of material and desulfurizing agent is 0-50 DEG C, pressure 0.2-1.5MPa.
In a specific example, 8 bottom temp of regenerator is 110-130 DEG C, and 8 head temperature of regenerator is 70-105
℃。
In order to facilitate the above-mentioned technical proposal for understanding the utility model, below by way of practical new to this in specifically used mode
The above-mentioned technical proposal of type is described in detail.
When specifically used, the device of organic sulfur is removed according to gas material described in the utility model, including desulfurization is taken out
Stripper 1, foam removal net 2, liquid distribution trough 3, extracting tower packing 4, gas distributor 5, coalescing-plate 6, desulfurizing agent circulating pump 7, regeneration
Tower 8, tower tray 9, reflux cooler 10, return tank 11, reflux pump 12, reboiler 13, poor desulfurizing agent pump 14, desulfurizing agent heat exchanger
15, desulfurizing agent cooler 16, steam pipe 17, condensate pipe 18, return pipe 19, boil desulfurizing agent pipe 20, gas material inlet tube again
21, gas material discharge nozzle 22, desulfurizing agent circulation pipe 23, rich desulfurizing agent pipe 24, poor desulfurizing agent pipe 25, non-condensable gas pipe 26, it is described
Desulfurization extraction tower 1 in be equipped with from top to bottom foam removal net 2, liquid distribution trough 3, extracting tower packing 4, gas distributor 5, coalescence
Plate 6 is equipped with tower tray 9 in regenerator 8, and regenerator 8 is sieve-plate tower or packed tower, and filler is structured packing or random packing, material
Matter is stainless steel, and the gas distributor 5 connects gas material inlet tube 21, and the liquid distribution trough 3 connects desulfurizing agent
Circulation pipe 23, gas material discharge nozzle 22 is connected at the top of the desulfurization extraction tower 1, and described 23 one end of desulfurizing agent circulation pipe connects
1 bottom of desulfurization extraction tower is connect, the other end connects desulfurizing agent circulating pump 7, is also connected on the desulfurizing agent circulation pipe 23 rich de-
Sulphur agent pipe 24 is connected with desulfurizing agent heat exchanger 15 and the rich desulfurizing agent import of regenerator 8 on the rich desulfurizing agent pipe 24, described
Connect return pipe 19 at the top of regenerator 8, the return pipe 19 connect reflux cooler 10 and 11 overhead reflux liquid of return tank into
Mouthful, non-condensable gas pipe 26 is connected at the top of the return tank 11,11 bottom of return tank connects back to fluid tube, the reflux
Liquid pipe connects reflux pump 12 and 8 top side portion of regenerator, and 8 bottom of regenerator connects poor desulfurizing agent pipe 25, and described is poor de-
It being connected on sulphur agent pipe 25 and boils desulfurizing agent pipe 20 again, the desulfurizing agent pipe 20 that boils again connects reboiler 13 and 8 bottom side of regenerator,
It is connected with the condensate pipe of steam pipe 17 and 18 on the reboiler 13, is also connected with poor desulfurization on the poor desulfurizing agent pipe 25
Agent pump 14, desulfurizing agent heat exchanger 15 and desulfurizing agent cooler 16, poor 25 other end of desulfurizing agent pipe connect sulphur agent circulation pipe
23 to desulfurization extraction tower desulfurizing agent entrance.
Specific sulfur method are as follows: sulfurous gas material enters desulfurization extraction tower 1, circulation desulfurization by gas distributor 5
Agent enters desulfurization extraction tower 1 from liquid distribution trough 3 after the pressurization of desulfurizing agent circulating pump 7, and gas-liquid two-phase reverse flow simultaneously passes through de-
Filler shearing comes into full contact in sulphur extraction tower 1, the hydrolytic catalyst of carbonyl sulfur in desulfurization extraction tower 1 of the carbonyl sulfur in gas material
The lower hydrolysis of effect generates hydrogen sulfide and carbon dioxide, and original hydrogen sulfide is absorbed in desulfurization in the hydrogen sulfide and gas material of generation
In agent, hydrogen sulfide containing richness desulfurizing agent part self-loopa is partially sent to regeneration unit, and gas material is from desulfurization extraction tower after desulfurization
It sends out on top.Wherein the desulfurizing agent by mass percentage, is prepared, the content of organic amine compound is by following raw material
39.999%wt-79.999%wt, the content of phase transfer catalyst are 20%wt-60%wt, the content 0.001%wt- of inorganic assistant
0.01%wt, desulfurizing agent are alkalinity, and organic amine compound includes more than one primary amine compound, more than one tertiary amine
Class compound and/or more than one secondary-amine compound；The phase transfer catalyst is selected from polyethylene glycol 200, polyethylene glycol
400, tetrabutylammonium bromide, tetrabutylammonium chloride, dodecyl trimethyl ammonium chloride, tetradecyl trimethyl ammonium chloride, pyridine
Or one or more of tri-n-butylamine；The inorganic assistant is selected from the one of sulfonation titanium cyanines cobalt, poly- titanium cyanines cobalt or titanium cyanines cobalt ichthyodin
Kind is several.The gas liquid ratio of desulfurizing agent and gas material is 50-300, and reaction temperature is 0-50 DEG C, operating pressure 0.2-
1.5MPa.Desulfurizing agent can all remove regenerator 8, can also part self-loopa, partially remove regenerator 8.
Rich desulfurizing agent and the poor desulfurizing agent from 8 bottom of regenerator enter regenerator 8 after the heat exchange of desulfurizing agent heat exchanger 15,
In regenerator 8 desulfurizing agent by 8 bottom reboiler 13 of regenerator heating after reenter regenerator 8, in rich desulfurizing agent hydrogen sulfide by
It is separated after heat with desulfurizing agent parsing, hydrogen sulphide in the vapor phase and a small amount of desulfurizing agent steam are pushed up from regenerator 8 and sent out, through reflux cooler 10
Enter return tank 11 after cooling, rich hydrogen sulfide containing fixed gas carrying device, the desulfurizing agent of condensation by reflux pump 12 be pressurized from
8 top side portion of regenerator returns to regenerator 8.The poor desulfurizing agent of another way at 8 bottom of regenerator and rich desulfurizing agent pass through desulfurizing agent heat exchanger
It is cooling using desulfurizing agent cooler 16 after 15 heat exchange, desulfurization extraction tower 1 is combined into self-loopa desulfurizing agent.Rich desulfurizing agent is again
Raw tower, operating pressure 0.1-0.2MPa, 8 bottom temp of regenerator are 110-130 DEG C, and 8 head temperature of regenerator is 70-105 DEG C,
Hydrogen sulfide parsing separation, desulfurizing agent are regenerated in desulfurizing agent, send the use of 1 ring of desulfurization extraction tower back to.
Embodiment 1
Certain oil gas field produces natural gas sample, the total sulfur 375mg/Nm after amine liquid extraction desulfurization3, wherein hydrogen sulfide content
12mg/ Nm3, desulfurization test is carried out using the utility model method, test result is as follows:
Selexol process test temperature is 24 DEG C, after the processing of the utility model methods experiment device, natural gas total sulfur
5mg/ Nm3。
Embodiment 2:
Certain petrochemical corporation's catalytic unit produces dry gas 15000-20000 Nm3/ h, it is total after amine liquid extraction desulfurization
Sulphur 100-200mg/ Nm3, wherein hydrogen sulfide content is less than 10mg/Nm3, a set of gas material is built using the utility model method
The device of organic sulfur is removed, device operation result is as follows:
Dry gas desulfurization extraction tower operation temperature is 25-40 DEG C, pressure 0.8-1.1MPa, desulfurizing agent global cycle flow 12-
15m3/ h send regenerator richness desulfurization agent flux 2-3m3/ h, regenerator operating pressure 0.12MPa regenerate column bottom temperature 115-120
DEG C, tower top temperature is 90-95 DEG C, and dry gas total sulfur is no more than 10mg/Nm after desulfurization3。
In conclusion being taken out by gaseous phase materials and desulfurizing agent in desulfurization by means of the above-mentioned technical proposal of the utility model
It reverse flow and is come into full contact in stripper, the carbonyl sulfur in gaseous phase materials can be removed to 10mg/Nm3Hereinafter, total sulfur can be removed to
20mg/Nm3It is regenerated, is recycled, the acidity that rich desulfurizer regeneration generates hereinafter, rich desulfurizing agent can heat parsing hydrogen sulfide
Gas can send to sulphur unit and produce sulphur, three-waste free discharge.
The above is only the preferred embodiment of the utility model only, is not intended to limit the utility model, all at this
Within the spirit and principle of utility model, any modification, equivalent replacement, improvement and so on should be included in the utility model
Protection scope within.
Claims (5)
1. a kind of device of gas material removing organic sulfur, which is characterized in that including desulfurization extraction tower (1), the desulfurization extracting
Tower (1) upper inside is equipped with liquid distribution trough (3), and desulfurization extraction tower (1) inner lower is equipped with gas distributor (5), institute
It states and is filled with extracting tower packing (4) between liquid distribution trough (3) and the gas distributor (5), the desulfurization extraction tower (1)
Top is connected with gas material discharge nozzle (22), the upper end of the liquid distribution trough (3) and the one end of desulfurizing agent circulation pipe (23)
Connection, the other end of desulfurizing agent circulation pipe (23) are connected to the bottom end of desulfurization extraction tower (1), and the desulfurizing agent circulation pipe (23) is even
It is connected to desulfurizing agent circulating pump (7), the lower end of the gas distributor (5) and gas material inlet tube (21) communicating pipe, it is described de-
Sulphur agent circulation pipe (23) is also connected with rich desulfurizing agent pipe (24), the richness desulfurizing agent pipe (24) by desulfurizing agent heat exchanger (15) with
Regeneration unit connection.
2. a kind of device of gas material removing organic sulfur according to claim 1, which is characterized in that the regeneration unit packet
It includes regenerator (8), is connected at the top of the regenerator (8) by return pipe (19) and return tank (11) top left side phegma import
It is logical, it is connected with reflux cooler (10) on the return pipe (19), return tank (11) top right side and non-condensable gas pipe (26)
Connection, return tank (11) bottom right are connect by reflux pump (12) with regenerator (8) top side portion；The regenerator (8)
Bottom is connected to by poor desulfurizing agent pipe (25) with desulfurizing agent heat exchanger (15), and the poor desulfurizing agent pipe (25) is connected with poor desulfurizing agent
It pumps (14), is also connected with desulfurizing agent cooler (16) between the desulfurizing agent heat exchanger (15) and desulfurizing agent circulation pipe (23)；Institute
It states poor desulfurizing agent pipe (25) to be also connected to by boiling desulfurizing agent pipe (20) again with the lower-left end of reboiler (13), the reboiler (13)
Left upper end be connected to regenerator (8) bottom side, the right side of the reboiler (13) respectively with steam pipe (17) and condensate pipe
(18) it connects.
3. a kind of device of gas material removing organic sulfur according to claim 2, which is characterized in that the regenerator (8)
For sieve-plate tower or packed tower.
4. a kind of device of gas material removing organic sulfur according to claim 1, which is characterized in that the desulfurization extraction tower
(1) foam removal net (2) are equipped between top and the liquid distribution trough (3).
5. a kind of device of gas material removing organic sulfur according to claim 1, which is characterized in that the desulfurization extraction tower
(1) coalescing-plate (6) are equipped between bottom and gas distributor (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201820931859.8U CN208362277U (en) | 2018-06-15 | 2018-06-15 | A kind of device of gas material removing organic sulfur |
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|---|---|---|---|
| CN201820931859.8U CN208362277U (en) | 2018-06-15 | 2018-06-15 | A kind of device of gas material removing organic sulfur |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108641764A (en) * | 2018-06-15 | 2018-10-12 | 宁波章甫能源科技有限公司 | A kind of device and method of gas material removing organic sulfur |
| CN114456851A (en) * | 2022-01-18 | 2022-05-10 | 宁波章甫能源科技有限公司 | Environment-friendly coal gas desulfurization device and method |
-
2018
- 2018-06-15 CN CN201820931859.8U patent/CN208362277U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108641764A (en) * | 2018-06-15 | 2018-10-12 | 宁波章甫能源科技有限公司 | A kind of device and method of gas material removing organic sulfur |
| CN114456851A (en) * | 2022-01-18 | 2022-05-10 | 宁波章甫能源科技有限公司 | Environment-friendly coal gas desulfurization device and method |
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