CN105944561B - A kind of synthesis gas acid gas separation and sulfur recovery integrated apparatus and method - Google Patents
A kind of synthesis gas acid gas separation and sulfur recovery integrated apparatus and method Download PDFInfo
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
- B01D53/8612—Hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
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Abstract
A kind of synthesis gas acid gas separation and sulfur recovery integrated apparatus and method, using alkaline solution as H2The absorbent of S and wet oxidation sulfur recovery principle, solution wash synthesis aspiration H with pressure in absorption tower2After S, decompression is first passed around, is sent into after the fuel gas that solution carrying is discharged and recycled in vacuum tower, then send to regenerator, large quantity of air is sent into solution by air blast, catalysis oxidation generation solid sulfur is carried out, regenerates solution；The later actified solution of separation sulphur first passes through heating deoxygenation, and then sending to absorption tower again by supercharging relaunders synthesis gas；Two technical process of synthetic gas desulfurization and sulfur recovery are combined into one by the present invention, only use a kind of solution, and it is specially provided with combustible gas recycling and actified solution deoxyprocess link, reduce the loss of synthesis gas active ingredient, under the premise of desulfurization and sulphur recovery efficiency are undiminished so that system is simplified.
Description
Technical field
It is more particularly to a kind of to H in synthesis gas the invention belongs to purified synthesis gas technical field2S removes and carries out sulphur and returns
The integrated apparatus and method of receipts.
Background technology
The energy and chemical field of the coal in China are play an important role for a long time, and the cleaning of coal and recycling are solutions
The certainly important channel of China's adjoint inefficient and pollution problem of direct burning coal for a long time.Wherein by gasification furnace by coal gas
Generation synthesis gas is one of the cleaning of coal and the important channel of recycling after changing.Either combine in integral coal gasification and follow
Ring power generation (IGCC) or coal chemical technology, synthesis gas will be converted coal into the utilization of coal by gasification furnace first.
Due to containing certain sulphur content in gasified raw material, that is, coal, so usual sulfur-bearing in gasification product, that is, synthesis gas.Mesh
Preceding domestic and international application is most widely airflow bed gasification furnace technology, gasification reaction temperature generally between about 1300~1700 DEG C,
Contained sulphur content is most of all with H in coal2The form of S enters in reaction product i.e. synthesis gas.The synthesis generated for gasification furnace
No matter gas sends to gas turbine power generation in IGCC power plants or subsequent chemical synthesis process is sent in chemical plant, all
It needs first to carry out desulfurization.
The desulfurization method of synthesis gas is broadly divided into two kinds of process routes of high-temperature dry desulfurization and low temperature wet desulphurization.Wherein
Wet desulphurization is the widely used technology path of technology maturation, and overwhelming majority synthetic gas desulfurization all uses wet desulphurization skill at present
Art.General synthesis gas Wet Flue Gas Desulfurization Technique route is generally divided into acid gas separation and two step of sulfur recovery, wherein acid gas separation process
It is by H2S gases are separated from synthesis gas, more commonly used process include chemically with physical absorption process, such as
MDEA methods, low-temp methanol are washed, NHD methods, Selexol methods etc., and absorbent solution carries out synthesis gas first in an absorption tower
Washing absorbs the H in synthesis gas2Then S ingredients are regenerated in another tower by heating up or being depressured, the suction regenerated
It receives agent solution to be recycled, the H regenerated2S gases send to special sulfur recovery flow.Common sulfur recovery mode has more
Kind, for example, the Claus sulfur recovery flow of high-temperature dry and wet method LO_CAT sulfur recoveries flow and both methods basis
Upper improved flow etc..Wherein there are complex process for Claus sulfur recovery flow, need the accurate control of oxygen amount, operating flexibility
Small, the rate of recovery is relatively low, the problems such as needing vent gas treatment, and wet method sulfur recovery flow is insensitive to handled gas concentration, behaviour
It is big to make elasticity, sulfur recovery rate is high.
Synthesis gas acid gas (the H generally used at present2S) technique that separation and sulfur recovery separately carry out is asked along with many
Topic, if technological process is long, equipment is various, system complexity is high, using two or more solution mediums, organic suction of the sulphur content from use
Agent medium is received easily to degrade aging etc..
Invention content
For acid gas separation and sulfur recovery in synthetic gas desulfurization technique is overcome to be divided into two independent flows, complex process lacks
Point, the present invention propose a kind of synthesis gas acid gas separation and sulfur recovery integrated apparatus and method.
In order to achieve the above object, the technical scheme is that：
A kind of synthesis gas acid gas separation and sulfur recovery integrated apparatus, including absorption tower 2,2 bottom of absorption tower is bonded into gas
1,2 top exit of absorption tower connects water recirculator 3, and the outlet of water recirculator 3 connects dispenser 4, and 4 top exit of dispenser connects
Decontaminating syngas 5,4 outlet at bottom of dispenser are connected with 2 top of absorption tower；Absorption tower 2 rich bottoms liquid outlet connection pressure reducing valve 8,
Vacuum tower 9 is connected after pressure reducing valve 8,9 top exit of vacuum tower connection supercharger 6, the outlet of supercharger 6 is connected to 2 lower part of absorption tower
Entrance；9 outlet at bottom of vacuum tower is connected to hypotonic solution and pumps 14 entrances, and 14 outlet of hypotonic solution pump is connected to regenerator 16, then
Raw 16 outlet at bottom of tower is connected to separator 17, and 17 outlet at bottom of separator is connected to solution storage trough 18,18 bottom of solution storage trough
Outlet is connected to actified solution pump 15, and 15 outlet of actified solution pump is connected to 10 cold-side inlet of regenerator, and 10 cold end of regenerator goes out
Mouth is connected to oxygen-eliminating device 11, and 11 outlet at bottom of oxygen-eliminating device is connected to 10 hot-side inlet of regenerator, 10 hot junction of regenerator outlet connection
Supreme pressure solution liquid pump 13,13 outlet of high-pressure solution pump are connected to 2 top entry of absorption tower；The outlet of air filter 22 is connected to drum
Wind turbine 21, the outlet of air blower 21 are connected to regenerator 16, and 16 top exit of regenerator, which connects, drops a hint 23；11 top entry of oxygen-eliminating device
Connect low-pressure heating steam 12；Solution storage trough 18 connects make-up solution 19.
The regenerator 16 is atmospheric pressure device.
21 entrance of air blower is equipped with air filter.
Synthesis gas acid gas separation described above carries out acid gas with sulfur recovery integrated apparatus and detaches and the integration of sulfur recovery
Method, the working media recycled between absorption tower 2 and regenerator 16 are absorbent solution, and absorbent solution carries out in a device
It recycles, H is absorbed on absorption tower 22Absorbent solution later S is known as rich solution, after regenerator 16 is regenerated
Absorbent solution is known as actified solution；Sulfur-bearing synthesis gas 1 enters from 2 bottom of absorption tower, and at the same time, actified solution is from absorption tower
2 tops enter, regenerated liquid and synthesis gas adverse current, the H in the interior washing process completed to synthesis gas in absorption tower 2, synthesis gas2S
Solution absorption is reproduced, clean synthesis gas comes out from 2 top of absorption tower, after the cooling of water recirculator 3, into liquid separation
Device 4 isolates the solution of synthesis gas carrying；Clean synthesis gas is sent out from 4 top of dispenser, and the solution isolated is from dispenser
4 bottoms are flowed out, and are then sent into from 2 top of absorption tower；Regenerated liquid absorbs H in absorption tower 22Become rich solution after S and collect in suction
It receives 2 bottom of tower and flows out, enter vacuum tower 9 after pressure reducing valve 8 reduces pressure；In vacuum tower 9, pass through the reduction of pressure
The H for carrying rich solution2It is released with CO fuel gas and from 9 Base top contact of vacuum tower, suction is sent back to after the pressurization of supercharger 6
Receive tower 2；The solution of 9 bottom of vacuum tower convergence after 14 extraction of hypotonic solution pump by being sent into regenerator 16, at the same time, air blower 21
Large quantity of air is blasted into regenerator 16, under the effect of the catalyst, catalysis oxidation occurs in regenerator 16, dissolves in the solution
H2S is oxidized to solid sulfur, and solution is regenerated；Extra air is discharged from tower top in regenerator 16, and regenerated liquid carries bubble
Foam shape sulphur is sent to separator 17 from the outflow of 16 bottom of towe of regenerator；It is separated by filtration by separator 17, regenerated liquid is from separator 17
Solution storage trough 18 is sent into bottom outflow, and sulphur filter residue is sent out from 17 top of separator；Actified solution pump 15 is from solution storage trough 18
Extraction regenerated liquid is sent to oxygen-eliminating device 11 and carries out heating deoxygenation.It to be carried out before and after actified solution disengaging oxygen-eliminating device 11 by regenerator 10
Heat exchange with recovery section thermal energy, to reduce the flow of low-pressure heating steam 12, saves energy consumption；It is exported out from 10 hot junction of regenerator
The regenerated liquid come is sent to absorption tower 2 after 13 pressurization of high-pressure solution pump, enters in tower from the top of absorption tower 2, to synthesis gas into
Row washing.
Using synthetic gas desulfurization and the integrated flow of sulfur recovery, synthetic gas desulfurization and sulfur recovery only by the use of a kind of solution as
Working medium, H during solution is completed in absorption tower 2 to synthesis gas2The absorption of S, mainly complete in the regenerator 16 solution regeneration and
The recycling of sulphur.
To prevent solution from causing with oxygen the oxidation to CO in synthesis gas, actified solution send to absorption tower 2 wash synthesis gas it
Before to pass through oxygen-eliminating device 11 and carry out deoxygenation, solution will exchange heat before and after entering oxygen-eliminating device 11 by regenerator 10.
It is lost to reduce synthesis gas, before the rich solution sent for regeneration tower 16 that 2 bottom of absorption tower comes out, to first pass through pressure reducing valve 8
Decompression, and the fuel gas CO and H that solution carries are released in vacuum tower 92, the gas that vacuum tower 9 comes out is by supercharger 6
Send absorption tower 2 after recompression back to.
The absorbent solution uses Na2CO3Solution uses Complexing Iron as catalyst, utilizes Lo-cat wet oxidation principles
Carry out sulfur recovery.
The present invention operation principle be：
The absorbent solution uses Na2CO3Solution uses iron ion complex compound liquid catalyst, i.e. Complexing Iron
Na2CO3-NaHCO3System.In absorption tower, H2After S is dissolved in water, it is ionized into HS- and H+, Na in solution2CO3Addition, make new
Solution alkaline increases solution to H2The absorbability of S.Catalyst Fe in solution3+Redox reaction occurs with HS-,
HS- is oxidized to elemental sulfur, while iron ion catalyst Fe3+It is reduced ferrous ion Fe2+.In regenerator, due to air
It is continually fed into, the continuous oxidation by air of iron ion catalyst, by Fe2+It is oxidized to Fe3+, Fe3+Continue to aoxidize the HS- in solution
Into sulphur simple substance, sulphur simple substance is a kind of solid particle, is detached from solution by separator filtering.
All reactions in technical process can all occur and meet chemical equilibrium condition, main chemical reactions at room temperature
It is as follows：
Absorb (oxidation) reaction：
H2S absorbs：H2S(g)+H2O(l)→H2S(l)
H2S is ionized：H2S(l)→HS-+H+
HS- is aoxidized：HS-+2Fe3+→S(s)+2Fe2++H+
Regenerate (reduction) reaction：
O2It absorbs：1/2O2(g)+H2O(l)→1/2O2(l)
Fe2+Oxidation regeneration：1/2O2(l)+2Fe2++H2O→2Fe3++2OH-
Overall reaction：
H2S(g)+1/2O2(g)→H2O(l)+S(s)
The course of work is：Under synthesis gas pressure condition, absorbent solution washs synthesis gas in absorption tower and will synthesis
H in gas2S absorbs, and synthesis gas is purified.The rich solution come out from absorption tower is sent to vacuum tower, and solution is released by decompression
The CO and H of middle dissolving2, the CO and H that release2Absorption tower is sent back to using pressurization, and the rich solution that vacuum tower comes out is sent to regenerator
It is regenerated.Air is passed through in regenerator, under the catalysis of iron ion, HS- is oxidized to solid sulfur.Carry the regeneration of sulphur
Liquid is filtered by separator, and solid sulfur send solution storage trough by separating treatment, solution.Due to being passed through excess during raw
Oxygen so oxygen content is excessively high in solution, washs the CO ingredients in synthesis gas during synthesis gas in absorption tower in order to prevent
It is aoxidized, increases oxygen scavenging step.The operation principle of oxygen-eliminating device is, using low-pressure steam heated solution, to reach solution temperature
The saturation temperature of normal pressure state, the oxygen dissolved in solution are desorbed out and discharge.In addition, one regenerator of setting, makes to remove
Solution before and after oxygen does a heat exchange, to reduce low-pressure heating steam consumption quantity, reaches energy-efficient purpose.
Beneficial effect of the present invention is：
1st, two cyclic processes of acid gas separation and sulfur recovery in synthesis gas conventional wet lay sweetening process are closed two by the present invention
It is one, system equipment is greatly decreased, reduces equipment investment expense, meanwhile, the reduction of system complexity is but also operation behaviour
It is greatly simplified.Due to not needing to using the organic solvents such as MDEA, NHD or Selexol, cycle fluid degradation
Problem is greatly improved, and saves the supplement and update cost of working medium.
2nd, using alkaline solution Na2CO3Synthesis gas is washed, it, can be to synthesis between the pH value of circulation solution maintains 8~9
H in gas2S more effectively absorb and remove, and can bear H in synthesis gas2The wide swings of S contents.Desulfuration efficiency can
Up to 99.9%.
3rd, solution and catalyst are nontoxic, and reaction speed is fast, and sulphur recovery efficiency is discharged up to 99.97%~99.99%
H in tail gas2S residual quantities are less than 10-6, meet discharging standards.
3rd, solution is inorganic salt solution, not volatile, and secondary pollution is not caused to synthesis gas, and high temperature is non-degradable, operation temperature
Spend insensitive, operation control is steady.Technological process is simple, and control parameter is less, and whole system operating flexibility is big, equipment operation peace
It is complete reliable.
4th, the combustible gas carried in high-pressure solution is recycled there is provided solution decompression ring tower, makes synthesis gas H2It is dropped to CO losses
It is minimum.
5th, there is provided deoxygenation links, reduce the oxygen content of solution, avoid since solution band oxygen causes to have in absorption tower
CO is aoxidized.
Description of the drawings
Fig. 1 is synthesis gas acid gas separation of the present invention and sulfur recovery integrated apparatus and flow chart.
Specific embodiment
With reference to specific implementation example, description of specific embodiments of the present invention.
As shown in Figure 1, present embodiment is applied to IGCC plant with apparatus of the present invention and method carries out desulfurization to synthesis gas
And sulfur recovery illustrates.In IGCC plant, coal completes gasification in gasification furnace first, and generates and contain H2S pollutants
Crude synthesis gas before synthesis gas is sent into gas turbine power generation, first carry out cleaning and desulfurization to synthesis gas.
After the synthesis gas come from gasification furnace first passes around ash disposal and water washing cleaning, H is only remained in synthesis gas2S pollutants into
Point, synthesize atmospheric pressure 3.0MPag, 40 DEG C of temperature, wherein H2S constituent contents are determined according to coal used, about of the total volume
0.147%.As shown in drawings, sulfur-bearing synthesis gas 1 enters from 2 bottom of absorption tower, and at the same time, actified solution is at the top of absorption tower
Into regenerated liquid and synthesis gas adverse current complete, H in synthesis gas complete to the washing process of synthesis gas in absorption tower2S is molten
Liquid absorbs, and clean synthesis gas comes out at the top of absorption tower, after the cooling of water recirculator 3, into dispenser 4, separation
Go out the solution of synthesis gas carrying.Clean synthesis gas is sent out from 4 top of dispenser, and the solution isolated is flowed from dispenser bottom
Go out, be then sent into from 2 top of absorption tower.Regenerated liquid absorbs H in absorption tower2Become rich solution after S and collect in 2 bottom of absorption tower
And flow out, from the rich solution that absorb the bottom of the tower comes out since pressure is higher, in addition to absorbing H2Other than S gases, part has also been dissolved
CO and H2, in order to reduce flow rate loss, need to recycle this part CO and H2, from the rich solution with pressure of absorb the bottom of the tower out
Enter vacuum tower 9 after pressure reducing valve 8 reduces pressure.In vacuum tower 9, the H of rich solution carrying is made by the reduction of pressure2With
The fuel gas such as CO release and from 9 Base top contact of vacuum tower, absorption tower 2 are sent back to after the pressurization of supercharger 6.From vacuum tower
The rich solution that bottom comes out has fallen to about normal pressure state, and the solution of 9 bottom of vacuum tower convergence after 14 extraction of hypotonic solution pump by sending
Enter regenerator 16, regenerator is the equipment of a normal pressure, continues input air, blower inlet into regenerator using air blower
Air filter is installed, impurity is avoided to enter regenerator foul solution with air.Large quantity of air is blasted regeneration by air blower 21
Tower 16 under the effect of the catalyst, occurs catalysis oxidation, dissolves H in the solution in regenerator 162S is oxidized to solid sulfur
Sulphur, solution are regenerated.Extra air is discharged from tower top in regenerator 16, and regenerated liquid entrained foam shape sulphur is from regenerator 16
Separator 17 is sent in bottom of towe outflow.It is separated by filtration by separator 17, regenerated liquid is flowed out from 17 bottom of separator is sent into solution storage
Slot 18, sulphur filter residue 20 are sent out from 17 top of separator.According to solution consumption situation, make-up solution is added in from solution storage trough；By
In thering is air to be passed through from regenerator 16, the oxygen of part is dissolved in actified solution, meeting when solution contacts again with synthesis gas
The oxidation of CO in synthesis gas is caused, causes the loss of flow rate.Therefore, actified solution pump 15 is extracted out from solution storage trough 18
Regenerated liquid is sent to oxygen-eliminating device 11 and carries out heating deoxygenation.It to be changed before and after actified solution disengaging oxygen-eliminating device 11 by regenerator 10
Heat with recovery section thermal energy, to reduce the flow of low-pressure heating steam 12, saves energy consumption.It exports out from 10 hot junction of regenerator
Regenerated liquid be sent to absorption tower 2 after 13 pressurization of high-pressure solution pump, enter in tower from the top of absorption tower 2, restart pairing
Desulfurization washing process is carried out into gas.
In the embodiment, the design parameter of acid gas separation and the operation of sulfur recovery integrated apparatus is provided by table 1.
Claims (6)
1. a kind of synthesis gas acid gas separation and sulfur recovery integrated apparatus, it is characterised in that：Including absorption tower (2), absorption tower (2)
Bottom is bonded into gas (1), and absorption tower (2) top exit connects water recirculator (3), and water recirculator (3) outlet connects liquid separation
Device (4), dispenser (4) top exit connect decontaminating syngas (5), are connected at the top of dispenser (4) outlet at bottom and absorption tower (2)；
Absorption tower (2) rich bottoms liquid outlet connection pressure reducing valve (8), pressure reducing valve (8) connect vacuum tower (9), vacuum tower (9) top exit afterwards
Supercharger (6) is connected, supercharger (6) outlet is connected to absorption tower (2) lower entrances；Vacuum tower (9) outlet at bottom is connected to low
Pressure solution liquid pump (14) entrance, hypotonic solution pump (14) outlet are connected to regenerator (16), and regenerator (16) outlet at bottom is connected to
Separator (17), separator (17) outlet at bottom are connected to solution storage trough (18), and solution storage trough (18) outlet at bottom is connected to again
Raw solution pump (15), actified solution pump (15) outlet are connected to regenerator (10) cold-side inlet, and regenerator (10) cold side outlet connects
Oxygen-eliminating device (11) is connected to, oxygen-eliminating device (11) outlet at bottom is connected to regenerator (10) hot-side inlet, the outlet of regenerator (10) hot junction
High-pressure solution pump (13) is connected to, high-pressure solution pump (13) outlet is connected to absorption tower (2) top entry；Air filter (22)
Outlet is connected to air blower (21), and air blower (21) outlet is connected to regenerator (16), and regenerator (16) top exit connects emptying
Gas (23)；Oxygen-eliminating device (11) top entry connects low-pressure heating steam (12)；Solution storage trough (18) connects make-up solution (19)；
The regenerator (16) is atmospheric pressure device；
Air blower (21) entrance is equipped with air filter.
2. synthesis gas acid gas separation described in claim 1 carries out acid gas with sulfur recovery integrated apparatus and detaches and the one of sulfur recovery
Change method, it is characterised in that：The working media recycled between absorption tower (2) and regenerator (16) is absorbent solution, is absorbed
Agent solution is recycled in a device, and H is absorbed in absorption tower (2)2Absorbent solution later S is known as rich solution, again
Raw tower (16), which carries out regenerating later absorbent solution, is known as actified solution；Sulfur-bearing synthesis gas (1) from absorption tower (2) bottom into
Enter, at the same time, regenerated liquid enters from absorption tower (2) top, regenerated liquid and synthesis gas adverse current, the completion pair in absorption tower (2)
The washing process of synthesis gas, the H in synthesis gas2S is reproduced solution absorption, and clean synthesis gas comes out at the top of absorption tower (2),
After water recirculator (3) cooling, into dispenser (4), the solution of synthesis gas carrying is isolated；Clean synthesis gas from
It is sent out at the top of dispenser (4), the solution isolated is flowed out from dispenser (4) bottom, is then sent at the top of absorption tower (2)；Again
Raw liquid absorbs H in absorption tower (2)2Become rich solution after S to collect in absorption tower (2) bottom and flow out, be dropped by pressure reducing valve (8)
Enter vacuum tower (9) after low-pressure；In vacuum tower (9), the H of rich solution carrying is made by the reduction of pressure2With CO combustible gases
Body releases and from vacuum tower (9) Base top contact, absorption tower (2) is sent back to after supercharger (6) pressurization；Vacuum tower (9) bottom
The solution of portion's convergence is sent into regenerator (16) after pumping (14) extraction by hypotonic solution, and at the same time, air blower (21) will be a large amount of empty
Tympanites enters regenerator (16), under the effect of the catalyst, catalysis oxidation occurs in regenerator (16), dissolves H in the solution2S
Solid sulfur is oxidized to, solution is regenerated；Extra air is discharged from tower top in regenerator (16), regenerated liquid entrained foam
Shape sulphur is sent to separator (17) from the outflow of regenerator (16) bottom of towe；It is separated by filtration by separator (17), regenerated liquid is from separation
Solution storage trough (18) is sent into the outflow of device (17) bottom, and sulphur filter residue is sent out from separator (17) top；Actified solution pump 15 is from molten
Extraction regenerated liquid is sent to oxygen-eliminating device (11) and carries out heating deoxygenation in liquid storage tank (18), and actified solution disengaging oxygen-eliminating device (11) is front and rear
It to be exchanged heat by regenerator (10), with recovery section thermal energy, to reduce the flow of low-pressure heating steam (12), save energy
Consumption；Absorption tower (2) is sent to after high-pressure solution pump (13) pressurization from the regenerated liquid that regenerator (10) hot junction exports out, from suction
It receives and enters in tower at the top of tower (2), synthesis gas is washed.
3. according to the method described in claim 2, it is characterized in that：Using synthetic gas desulfurization and the integrated flow of sulfur recovery,
Synthetic gas desulfurization and sulfur recovery complete solution to synthesis only by the use of a kind of absorbent solution as working media in absorption tower (2)
H in gas2The regeneration of solution and the recycling of sulphur are mainly completed in the absorption of S in regenerator (16).
4. according to the method described in claim 2, it is characterized in that：To prevent solution from causing with oxygen the oxygen to CO in synthesis gas
Change, actified solution will pass through oxygen-eliminating device (11) before sending to absorption tower (2) washing synthesis gas and carry out deoxygenation, and solution enters oxygen-eliminating device
(11) it is front and rear to exchange heat by regenerator (10).
5. according to the method described in claim 2, it is characterized in that：To reduce synthesis gas loss, the richness that absorption tower (2) bottom comes out
Before liquid sent for regeneration tower (16), to first pass through pressure reducing valve (8) decompression, and release solution carrying in the vacuum tower (9) can
Combustion gas body CO and H2, vacuum tower (9) come out gas by supercharger (6) recompress after send absorption tower (2) back to.
6. according to the method described in claim 2, it is characterized in that：The absorbent solution uses Na2CO3Solution, using complexing
Iron is catalyst, and sulfur recovery is carried out using Lo-cat wet oxidations principle.
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| CN1546206A (en) * | 2003-12-09 | 2004-11-17 | 南化集团研究院 | Method for removing sulfides and carbon dioxide by high pressure |
| CN1665582A (en) * | 2002-07-03 | 2005-09-07 | 卢吉股份公司 | System unit for desorbing carbon dioxide from methanol |
| CN101208145A (en) * | 2005-04-29 | 2008-06-25 | 弗劳尔科技公司 | Configurations and methods for acid gas absorption and solvent regeneration |
| CN101674875A (en) * | 2007-02-22 | 2010-03-17 | 氟石科技公司 | Configurations and methods for carbon dioxide and hydrogen production from gasification streams |
| CN205796959U (en) * | 2016-06-16 | 2016-12-14 | 中国华能集团公司 | A kind of synthesis gas acid gas separates and sulfur recovery integrated apparatus |
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| FR2942972B1 (en) * | 2009-03-10 | 2012-04-06 | Inst Francais Du Petrole | METHOD FOR DEACIDIFYING GAS BY ABSORBENT SOLUTION WITH VAPORIZATION AND / OR PURIFICATION OF A FRACTION OF THE REGENERATED ABSORBENT SOLUTION |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1665582A (en) * | 2002-07-03 | 2005-09-07 | 卢吉股份公司 | System unit for desorbing carbon dioxide from methanol |
| CN1546206A (en) * | 2003-12-09 | 2004-11-17 | 南化集团研究院 | Method for removing sulfides and carbon dioxide by high pressure |
| CN101208145A (en) * | 2005-04-29 | 2008-06-25 | 弗劳尔科技公司 | Configurations and methods for acid gas absorption and solvent regeneration |
| CN101674875A (en) * | 2007-02-22 | 2010-03-17 | 氟石科技公司 | Configurations and methods for carbon dioxide and hydrogen production from gasification streams |
| CN205796959U (en) * | 2016-06-16 | 2016-12-14 | 中国华能集团公司 | A kind of synthesis gas acid gas separates and sulfur recovery integrated apparatus |
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