CN202962276U - Reactor for recovering sulfur in acid gases - Google Patents
Reactor for recovering sulfur in acid gases Download PDFInfo
- Publication number
- CN202962276U CN202962276U CN 201220355881 CN201220355881U CN202962276U CN 202962276 U CN202962276 U CN 202962276U CN 201220355881 CN201220355881 CN 201220355881 CN 201220355881 U CN201220355881 U CN 201220355881U CN 202962276 U CN202962276 U CN 202962276U
- Authority
- CN
- China
- Prior art keywords
- reactor
- gas
- catalytic oxidation
- chamber
- hydrogenation
- 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 - Lifetime
Links
Images
Abstract
The utility model discloses a reactor for recovering sulfur in acid gases. The reactor integrates a hydrogenation hydrolysis reactor and a catalytic oxidation reactor, is horizontal, and is internally separated into at least two chambers by a vertical baffle plate, wherein at least one chamber is a heat insulation reaction chamber for organic sulfur hydrogenation hydrolysis, and the rest are water cooling heat exchanging reaction chambers for catalytic oxidation; and the heat insulation reaction chambers can be equipped with a water pump, a gas bag and byproduct steam. The reactor provided by the utility model is suitable for recovering acid gases containing low-concentration H2S content, lowers the content of sulfide in tail gas by utilizing tail gas of alcoholic liquid after washing treatment and desulfurization in a low-temperature alcohol washing technology, and protects the environment; and meanwhile the reactor provided by the utility model is simple and reasonable in structure, can save equipment occupied spaces, and can lower the project investment.
Description
Technical field
The utility model relates to the sulfur containing gas processing technology field, relates in particular to a kind of reactor that reclaims sulphur for sour gas, is applicable to refine oil, the sulfur recovery in producing of Coal Chemical Industry, petrochemical industry, natural gas processing.
Background technology
In existing acid sulfur containing gas treatment technology, Crouse (Claus) technique (original Claus technique) commonly used, react as follows:
This technique can only carried out under low-speed for controlling reaction temperature very much, is difficult to use at Large Scale Industrial Process, improvement Claus technique occurs afterwards, with H
2The S oxidation divides two stages to carry out, and reacts as follows:
Can find out from above-mentioned reaction equation, the first step only reacts away H
2Therefore 1/3 of S total amount, second step are 2/3, enter H in the gas of beds after first step reaction
2S and SO
2Ratio should be 2: 1, this is that the control of improvement claus process is crucial.After Crouse's recovery process realizes industrialization from the thirties in 20th century, be widely used in having and directly to process H in the process of the coals such as the production of synthetic ammonia and methanol feedstock gas, refinery gas production, natural gas purification, oil, natural gas
2S generates sulphur, saves SO than relieving haperacidity
2Pipeline is carried cost and the advantages such as relieving haperacidity desulphurization cost, security height, but reclaims H with relieving haperacidity
2S compares, and one time cost of investment is high.
The conventional sour gas H that improves the Claus unit sulfur recovery unit processing
2The S concentration limit is 15～20%, and China's Coal Chemical Industry sour gas complicated component, often directly from purified synthesis gas such as low-temperature rectisols, therefore sulfur content relatively generally (≤15%) on the low side, and fluctuation of concentration large (7～20%), these two kinds of characteristics cause existing Coal Chemical Industry sour gas claus sulphur recovery units main reaction section combustion furnace normally to move, and are difficult to obtain quantitative SO
2Guarantee the H that the conversion zone claus reaction requires
2S/SO
2=2: 1 ratio causes tail gas to exceed standard, and whole sulfur recovery unit can't move.Therefore, should select to adapt to the sulfur recovery technique of hanging down sour gas concentration, high resiliency scope, can process complicated gas, simultaneously reduce plant investment and operating cost.
The process for purifying of existing large-scale coal gasifying process back substantially all adopts low-temp methanol washing process.Low-temp methanol washing process is that a kind of methyl alcohol that adopts is the sour gas physics washing system of solvent, is applicable to process contain high-concentration acidic wastewater gas, utilizes larger to the sour gas solubility at low temperatures characteristic of methyl alcohol, removes the sour gas in unstripped gas.The main flow process of low-temp methanol washing process is the combination of multistage absorption and desorption, therefore can consider sulfur recovery technique and low-temp methanol washing process are combined.
The utility model content
For the problems referred to above; the purpose of this utility model is to provide a kind of reactor that reclaims sulphur for sour gas; simple and reasonable; be used for sour gas and reclaim sulphur technique; in conjunction with the tail gas after the alcoholic liquor carrying out washing treatment desulfurization that utilizes in low-temp methanol washing process; reduce tail gas medium sulphide content content, protection of the environment.
For achieving the above object, the utility model is taked following technical scheme:
A kind of reactor that reclaims sulphur for sour gas, integrate hydrogenation hydrolytic reaction device and catalyst oxidation reactor, described reactor is horizontal, inside reactor is divided at least two chambers with upright dividing plate, wherein at least one chamber is the adiabatic reaction chamber that the organic sulfur hydrogenation hydrolyzation is used, and all the other are the water-cooled heat exchange reative cell of catalytic oxidation use.But described water-cooled heat exchange reative cell distribution pump, drum, byproduct steam.
When described inside reactor was divided into two chambers with upright dividing plate, a Room was the adiabatic reaction chamber, was used for the organic sulfur hydrogenation hydrolytic reaction, and another chamber is water-cooled heat exchange reative cell, was used for catalytic oxidation.
When described inside reactor was divided into three chambers with two upright dividing plates, a middle Room was the adiabatic reaction chamber, and both sides are respectively a water-cooled heat exchange reative cell.Described sour gas first through the left side or the water-cooled heat exchange reative cell on the right carry out 60% above H
2S selective oxidation reaction of Salmon-Saxl, then COS, CS are carried out in the adiabatic reaction chamber in the middle of advancing under 300～390 ℃
2Tempreture organic sulphur hydrolysis reaction is carried out H in sour gas after tempreture organic sulphur hydrolysis finally by the water-cooled heat exchange reative cell of another side
2The S selective oxidation reaction.
Another kind of technical scheme of the present utility model: described reactor is vertical reactor, be that described inside reactor is divided into heat insulation layer and heat exchange conversion zone up and down, described heat insulation layer filling hydrogenation hydrolyzation catalyst, distribute some water-cooleds with U-shaped elbow in bottom heat exchange conversion zone around pipe, load catalyst for selective oxidation around between pipe.
Above-mentioned reactor is applicable to following technique:
Reclaim the method for sulphur in a kind of sour gas, comprise the following steps: with catalytic hydrogenation reaction, the organic sulfur hydrogenation hydrolyzation in sour gas is become inorganic sulphide, again the inorganic sulphide Catalytic Oxygen is changed into sulphur, again the reaction gas cooling condensation after catalytic oxidation is separated liquid sulfur, the contain residual sulfur compound in pure washing lotion washing absorption tail gas of tail gas after separate sulfur from low-temperature rectisol workshop section realizes the recovery fully of sulphur.
When inside reactor is divided into three chambers, be applicable to following technique: first carry out catalytic oxidation for the first time before described catalytic hydrogenation reaction, partial vulcanization hydrogen and oxygen reaction generate sulphur and water, carry out again catalytic hydrogenation reaction tempreture organic sulphur hydrolysis is become inorganic sulphide, carrying out for the second time, catalytic oxidation changes into sulphur with the inorganic sulfur Catalytic Oxygen in sour gas again, again the reactor cooling condensation is separated liquid sulfur, again the tail gas after separate sulfur is used from containing of low-temperature rectisol of pure washing lotion washing, absorb the residual sulfur compound in tail gas, realize that sulfur recovery is complete.
As a kind of preferred, the absorption liquid that has absorbed the residual sulfur compound in tail gas is sent low-temperature rectisol workshop section back to and is absorbed sulphur, then is treated as sour gas through regeneration, and sour gas can utilize the utility model method to reclaim the processing of sulphur again.
As a kind of preferred, described tail gas is first through catalytic hydrogenation treatment, with SO
2Catalytic hydrogenation becomes H
2Wash with containing pure washing lotion again after S.
Described catalytic hydrogenation reaction temperature is 300～390 ℃.
Described catalytic oxidation adopts air or oxygen-enriched air or pure oxygen as oxidant.
Described catalytic oxidation preferably carries out in the water-cooled heat transfer reactor, and reaction temperature is 210～280 ℃.
H in sour gas
2Not too high (the H for example of S
2S is Shang Xia 25%) time, can be directly with above-mentioned sulfur recovery technique; When being high concentration H
2S (oil-extraction plant acidic gas H for example
2S＞40% even＞80%) time, after can being used in high temperature combustion furnace burning total sulfur 60%.
Adopt the sulfur recovery technique of the utility model reactor to compare with traditional Claus method, have following remarkable advantage:
1. can be used for low concentration H
2The sulfur recovery of the sour gas of S content (for example＜20%) is avoided in Claus method high temperature combustors because of H
2Low or the H of S concentration
2S content is unstable, and make in the Claus combustion chamber can not self-heating, makes combustion reaction unstable, affects the sulphur changing effect, reduces sulfur recovery rate, increases the tail gas medium sulphide content and exceeds standard, and affects environmental protection.
2. compare with a plurality of catalytic oxidation use adiabatic reactors of existing employing, avoid H
2High reaction heat in the S oxidation and cause reaction temperature too high causes catalysqt deactivation, and prior art generally needs H in sour gas
2S is diluted to 6% from 25%, it is reported domesticly to carry out catalytic oxidation after it is diluted to 1～3% left and right, and this just makes sulfur recovery process acid tolerance and is increased to 10 times, has greatly increased equipment and investment.
3. be successfully applied to the methyl alcohol of the strong exothermal reaction horizontal and vertical water-cooled heat exchange byproduct steam homogeneous temperature type catalytic reactor in synthetic with the applicant, the reliable reaction temperature of controlling, give full play to catalyst activity, reduce catalyst amount and expense, increase the service life, improve sulphur conversion ratio and sulfur recovery rate, reach＞99.9%, near 100%.
4. the utility model reactor integrates hydrogenation hydrolytic reaction device and catalyst oxidation reactor, and is simple and reasonable, can take up an area the space by saving equipment, reduces project investment.
Description of drawings
Fig. 1 is the structural representation that the utlity model has the reactor of two chambers.
Fig. 2 is the structural representation that the utility model specifically has the reactor of three chambers.
Fig. 3 is for adopting the application apparatus schematic diagram of the reactor that the utlity model has three chambers.
Fig. 4 is the schematic diagram of the reactor of vertical water-cooled heat exchange structure of the present utility model.
Fig. 5 is the enlarged diagram of the return bend coupling part in reactor shown in Figure 4.
Fig. 6 is the schematic diagram of the external drum of reactor shown in Figure 4, water pump.
Fig. 7 is the applicable technological process schematic block diagram of the utility model reactor.
Fig. 8 is the applicable technological process schematic block diagram of the utility model reactor, and wherein sour gas is through the quadric catalysis oxidation.
Fig. 9 is the applicable technological process schematic block diagram of the utility model reactor, and wherein tail gas first washs with containing pure washing lotion through catalytic hydrogenation again.
Description of reference numerals:
R
1a-hydrogenation hydrolytic reaction chamber
R
2aThe-the first catalytic oxidation chamber R
2bThe-the second catalytic oxidation chamber E
1-First Heat Exchanger
E
2The-the second heat exchanger E
3-air heater
V
1-molten sulfur separator C
1-tail gas washing tower
1-housing 2-heat exchanger tube 3-air inlet
5-gas outlet 6-catalyst unloads outlet 7-around the tubular axis core
81-gas distribution grid 82-porous gas collection plate 9a-inlet header
9b-outlet header 10-longitudinal register plate 23-supporting member
A-heat insulation layer B-heat exchange conversion zone
The descending heat exchanger tube 18a-U of the up heat exchanger tube 2b-of 2a-shape elbow
12-drum 13-circulating pump 14-steam outlet pipe
15-outlet pipe 16-heat transferring medium circulation pipe 17-replenishes water pipe
The specific embodiment
Below in conjunction with drawings and Examples, the utility model is described in detail.
Embodiment 1
When realizing technique as shown in Figure 7, two steps of catalytic hydrogenation wherein and catalytic oxidation can be carried out in same reactor, be the horizontal reactor as shown in Figure 1 of the utility model design, inside reactor is divided into two chambers with upright dividing plate: heat-insulating hydrogenation hydrolytic reaction chamber R
1aWith water-cooled heat exchange type catalytic oxidation chamber R
2a, sour gas is from hydrogenation hydrolytic reaction chamber R
1aThe top enters, and carries out hydrogenation hydrolytic reaction at catalyst layer, and the organic sulfur in sour gas is hydrolyzed into inorganic sulphide, and reactor is from hydrogenation catalyst reative cell R
1aThe bottom goes out reactor, then advances catalytic oxidation chamber R
2aCarry out catalytic oxidation, catalytic oxidation chamber R
2aIn structure of reactor when be the water-cooled heat exchange, reaction heat is for byproduct steam, the inorganic sulphide in reaction gas is changed into sulphur by Catalytic Oxygen.
Realize technique as shown in Figure 8, catalytic oxidation for the first time wherein, catalytic hydrogenation and for the second time three steps of catalytic oxidation can carry out in same reactor, adopt horizontal reactor as shown in Figure 2, inside reactor is divided into three chambers with two upright dividing plates, and a middle Room is hydrogenation hydrolytic reaction chamber R
1a, two sides are respectively the first catalytic oxidation chamber R
2aWith the second catalytic oxidation chamber R
2b
Advanced the first catalytic oxidation chamber R of sour gas
1a, partial vulcanization hydrogen and oxygen reaction generate sulphur and water, then advance hydrogenation hydrolytic reaction chamber R
1aCarry out catalytic hydrogenation reaction, tempreture organic sulphur hydrolysis is become inorganic sulphide, sour gas advances the second catalytic oxidation chamber R again
2bCarry out catalytic oxidation for the second time, the inorganic sulfur Catalytic Oxygen in sour gas is changed into sulphur.
Embodiment 3
As shown in Figure 3, inside is divided into three chamber horizontal reactors, is used for realization technique as shown in Figure 8, and a middle Room is hydrogenation hydrolytic reaction chamber R
1a, two sides are respectively the first catalytic oxidation chamber R
2aWith the second catalytic oxidation chamber R
2b, the first catalytic oxidation chamber R
2aTop entrance and First Heat Exchanger E
1Shell side outlet connect, the first catalytic oxidation chamber R
2aOutlet at bottom and First Heat Exchanger E
1The tube side import connect, First Heat Exchanger E
1Tube side outlet and the second heat exchanger E
2The shell side import connect, the second heat exchanger E
2Shell side outlet and hydrogenation hydrolytic reaction chamber R
1aThe top entrance connect, hydrogenation hydrolytic reaction chamber R
1aOutlet at bottom and the second heat exchanger E
2The tube side import connect, the second heat exchanger E
2Tube side outlet and the second catalytic oxidation chamber R
2bTop inlet connect, the second catalytic oxidation chamber R
2bOutlet at bottom and air heater E
3The shell side import connect, air heater E
3Shell side outlet is connected with the shell side import of water cooler, the shell side of water cooler exports and molten sulfur separator V
1, tail gas washing tower C
1Connect successively.
Sour gas is through First Heat Exchanger E
1With go out the first catalytic oxidation chamber R
2aLaggard the first catalytic oxidation chamber R of reactor heat exchange rising temperature
2a, through catalyst layer generation catalytic oxidation, partial vulcanization hydrogen and oxygen reaction generate sulphur and water, go out the first catalytic oxidation chamber R
2aReactor through First Heat Exchanger E
1, the second heat exchanger E
2Enter hydrogenation hydrolytic reaction chamber R after heat exchange
1a, at catalyst layer generation hydrogenation hydrolytic reaction, tempreture organic sulphur hydrolysis becomes inorganic sulphide, goes out hydrogenation hydrolytic reaction chamber R
1aReaction gas through the second heat exchanger E
2Enter the second catalytic oxidation chamber R after heat exchange
2b, catalytic oxidation changes into sulphur with the inorganic sulfur Catalytic Oxygen in sour gas for the second time, goes out the second catalytic oxidation chamber R
2bReactor through air heater E
3Cooling, then feed liquor sulphur separator V
1Isolate sulphur, remaining gas is advanced tail gas washing tower C
1, use the alcohol washing water washing that contains from low-temperature rectisol to absorb residual sulfur compound in tail gas, the absorption liquid that absorbs the residual sulfur compound in tail gas send back to low-temperature rectisol workshop section absorb sulphur, again through being regenerated as sour gas, can again reclaim sulphur.
Embodiment 4
Employing reactor as shown in Figure 4 can be used for technique as shown in Figure 7, this structure of reactor obtains for increase heat insulation layer A improvement on the architecture basics of the application for a patent for invention (201210033806.1) that the applicant has applied for, comprise housing 1 and heat exchanging piece, described housing 1 top is provided with air inlet 3 and manhole (not shown), air inlet 3 is furnished with gas distribution grid 81, is not provided with a pair of header with tube sheet on housing: inlet header 9a and outlet header 9b.Described heat exchanging piece comprises some heat exchanger tubes 2, the bottom of the adjacent two described heat exchanger tubes of Internal and external cycle or same circle footpath connects (as shown in Figure 5) by return bend 18a, in consisting of, the up heat exchanger tube 2a of logical heat transferring medium and descending heat exchanger tube 2b arrange, descending heat exchanger tube 2b is communicated with inlet header 9a, and up heat exchanger tube 2a is communicated with outlet header 9b.Each layer heat exchanger tube is by longitudinal register plate 10 location.Housing 1 inside center also is provided with around tubular axis core 7, the up heat exchanger tube of same return bend connection and descending heat exchanger tube are along arranging by counter clockwise direction or clockwise direction spirality separately respectively around tubular axis core 7, at the bottom of tubular axis core 7 bottoms are bearing in by supporting member 23 tin, around the upper not retractable of tubular axis core 7.The up heat exchanger tube that same return bend connects is opposite with the winding direction of descending heat exchanger tube.Housing bottom is provided with gas outlet 5 and catalyst unloads outlet 6, and gas outlet 5 is furnished with porous gas collection plate 82.Heat transferring medium adopts water.Heat insulation layer A is positioned at the space of heat exchanging piece top, gas distribution grid 81 belows, the in-built hydrogen hydrolyst of dosing of heat insulation layer, be heat exchange conversion zone B between the heat exchanging piece pipe, filling catalyst for catalytic oxidation (being the parts clear display that makes the reactor lower part space in Fig. 4, not at the lower illustration catalyst).
As shown in Figure 9, when above-mentioned reactor used, outlet header 9b connected drum 12 by steam outlet pipe 14, and drum 12 connects circulating pump 13 by outlet pipe 15, circulating pump 13 also connects additional water pipe 17, and inlet header 9a connects circulating pumps 13 by heat transferring medium circulation pipe 16.Sour gas enters from air inlet 3, first enter heat insulation layer A through air inlet 3, gas distribution grid 81 hydrogenation hydrolytic reaction occurs, the tempreture organic sulphur hydrolysis in sour gas becomes inorganic sulphide, and reactor enters heat exchange conversion zone B again, catalytic oxidation occurs, and the inorganic sulfur Catalytic Oxygen is changed into sulphur.Heat transferring medium enters into each heat exchanger tube 2 from inlet header 9a, descending with spirality along descending heat exchanger tube, change up heat exchanger tube over to through return bend again, up with the spirality direction opposite with down direction, during this time with the sour gas heat exchange of axially passing catalyst layer, in pipe, the part water vapor is steam, removes drum 12 separate vapours with control valve through outlet header 9b, all the other water with converge from the supplementing water of replenishing water pipe 17 that again to enter inlet header 9a by circulating pump 13 career recycling.Reaction gas after catalytic oxidation 5 goes out reactor through porous gas collection plate 82 from the gas outlet, go the condensation separation liquid sulfur, tail gas is sent to scrubbing tower and is used from the residual sulfur compound in containing of low-temperature rectisol of pure washing water washing absorption tail gas, the absorption liquid that has absorbed the residual sulfur compound in tail gas send back to low-temperature rectisol workshop section absorb sulphur, again through being regenerated as sour gas, sour gas can be again with above-mentioned method and apparatus recovery sulphur.
Claims (3)
1. one kind is used for the reactor that sour gas reclaims sulphur, it is characterized in that: described inside reactor is divided at least two chambers with vertical clapboard, wherein at least one chamber is the adiabatic reaction chamber of catalytic hydrogenation hydrolysis use, and all the other are the water-cooled heat exchange reative cell of catalytic oxidation use.
2. reactor as claimed in claim 1, it is characterized in that: described inside reactor is divided into three chambers with vertical clapboard, chamber wherein is the water-cooled heat exchange reative cell of filling catalyst for selective oxidation for the adiabatic reaction chamber of dress hydrogenation hydrolyzation catalyst, two Room, left and right.
3. one kind is used for the reactor that sour gas reclaims sulphur, it is characterized in that: described inside reactor is divided into heat insulation layer and heat exchange conversion zone up and down, described heat insulation layer filling hydrogenation hydrolyzation catalyst, distribute some water-cooleds with U-shaped elbow in bottom heat exchange conversion zone around pipe, load catalyst for selective oxidation around between pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220355881 CN202962276U (en) | 2012-07-19 | 2012-07-19 | Reactor for recovering sulfur in acid gases |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220355881 CN202962276U (en) | 2012-07-19 | 2012-07-19 | Reactor for recovering sulfur in acid gases |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN202962276U true CN202962276U (en) | 2013-06-05 |
Family
ID=48503407
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220355881 Expired - Lifetime CN202962276U (en) | 2012-07-19 | 2012-07-19 | Reactor for recovering sulfur in acid gases |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN202962276U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107441875A (en) * | 2017-09-08 | 2017-12-08 | 中冶焦耐(大连)工程技术有限公司 | A kind of Claus tail gases condensation process device |
| CN108579620A (en) * | 2018-06-08 | 2018-09-28 | 南京敦先化工科技有限公司 | A kind of combined type thermal insulation water shifting heat reactor |
-
2012
- 2012-07-19 CN CN 201220355881 patent/CN202962276U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107441875A (en) * | 2017-09-08 | 2017-12-08 | 中冶焦耐(大连)工程技术有限公司 | A kind of Claus tail gases condensation process device |
| CN108579620A (en) * | 2018-06-08 | 2018-09-28 | 南京敦先化工科技有限公司 | A kind of combined type thermal insulation water shifting heat reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104138713A (en) | Method, device and reactor for recovery of sulfur from acidic gas | |
| CN103303872B (en) | System device and method for recycling sulfur dioxide from fume to prepare sulfur | |
| CN101912718B (en) | Device and method for absorbing carbon disulfide in hydrogen sulfide gas by using solvent | |
| CN201052456Y (en) | Wrapped-tube catalytic oxidation reactor | |
| CN104548902B (en) | Acetylene gas purifier and technique thereof | |
| CN203183905U (en) | Low-content carbon dioxide absorption and analysis system in industrial waste gas | |
| CN109569193A (en) | It is a kind of to absorb the sulfur method synchronous with regeneration | |
| CN113233415A (en) | Process and device for preparing hydrogen from hydrogen iodide in iodine-sulfur cycle | |
| CN113274755A (en) | Process and device for preparing oxygen by phase thermal decomposition of sulfuric acid in iodine-sulfur cycle | |
| CN210826085U (en) | Blast furnace gas catalytic desulfurization device | |
| CN103566754A (en) | Method and device for recovering sulphur in acidic gas, and reactor | |
| CN103189124A (en) | System and method for recovering gas containing c02 and h2s | |
| CN202962276U (en) | Reactor for recovering sulfur in acid gases | |
| CN114011231A (en) | System and method for desulfurizing blast furnace gas by using hot alkali liquor | |
| CN107789969B (en) | Method and device for treating refinery acid gas | |
| CN105502302A (en) | Method and system for preparing smelting flue gas into sulphur | |
| CN103910342A (en) | Nitrogen purification device | |
| CN205269356U (en) | Device is washed to methyl alcohol for low temperature | |
| CN102659102B (en) | Technology and device for preparing industrial carbon monoxide with water gas | |
| CN204412040U (en) | A kind of combined type Gas Purification Factory low concentration acid gas processing device | |
| CN111470476A (en) | Method for recycling and recovering sulfur from regenerated sulfur-containing tail gas subjected to active coke dry method flue gas treatment | |
| CN110591769A (en) | Blast furnace gas catalytic desulfurization device and method | |
| CN216377479U (en) | Plasma reforming distributed natural gas hydrogen production device | |
| CN113528196B (en) | Shifted gas treatment or improvement process and low-temperature methanol washing device and process | |
| CN205556590U (en) | Double tower that is suitable for transportation of sled piece absorbs palingenetic natural gas deacidification equipment of double tower |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term |
Granted publication date: 20130605 |
|
| CX01 | Expiry of patent term |