CN206580557U - A kind of processing equipment for carbon disulphide production Process Gas - Google Patents
A kind of processing equipment for carbon disulphide production Process Gas Download PDFInfo
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- CN206580557U CN206580557U CN201720218185.2U CN201720218185U CN206580557U CN 206580557 U CN206580557 U CN 206580557U CN 201720218185 U CN201720218185 U CN 201720218185U CN 206580557 U CN206580557 U CN 206580557U
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Abstract
The utility model is related to sulphur chemical field, a kind of more particularly to processing equipment for carbon disulphide production Process Gas, including acid gas combustion furnace, one-level condensate cooler, one turn of heater, first-stage reactor, B-grade condensation cooler, trap, hydrogenation reactor and the hydrogenation cooler set gradually along the flow direction of Process Gas.The utility model in equipment by being improved, realize the high efficiente callback of sulphur in hydrogen sulfide containing Process Gas, total sulfur recovery also solves the concentration that SO2 contents in the problem of traditional handicraft is difficult to control on catalyzed conversion temperature, final emission are far below national standard up to more than 99.8%.
Description
Technical field
The utility model is related to sulphur chemical field, more particularly to a kind of oxidation catalysis for carbon disulphide production Process Gas
With the processing equipment of hydrogenating reduction.
Background technology
In carbon disulphide production technique, to containing H2Sulphur recovery and tail gas treatment process in S acid gas mostly around gram
Louth technique is deployed, and traditional claus process basic procedure is：H will be contained2S acid gas is sent into catalysis under conditions of air distribution and turned
Change in reactor, the catalytic reaction at a temperature of 200 DEG C ~ 350 DEG C, the Process Gas reflected passes through sulfur condenser, at 130 DEG C
At a temperature of ~ 200 DEG C, by condensation and separation of sulphur, while by-product low-pressure steam, uncooled tail gas gas phase portion do again into
It is vented after the processing of one step.Occurs main reaction as follows：
A kind of claus sulphur recovery units molten sulfur pond sulphur-containing exhaust gas processing work as disclosed in Patent No. CN103539077A
Skill, including molten sulfur pond（1）In addition to steam jet ejector（11）And claus oven（8）, molten sulfur pond（1）In molten sulfur evaporation produce
Sulphur steam and the hydrogen sulfide gas and the non-purification wind that blasts of molten sulfur abjection be mixed to form sulphur-containing exhaust gas, by steam jet ejector
（11）The sulphur-containing exhaust gas that molten sulfur pond is deviate from is delivered to sulphur claus oven（8）It is interior, will own in claus oven in sulphur-containing exhaust gas
Element sulphur is converted to sulphur simple substance, by sulfur condenser（14）Molten sulfur is condensed into return.
And for example a kind of High-efficiency sulfur recovery of sulfide hydrogen waste gas disclosed in Patent No. CN103318847A, will contain
H2S waste gas burning generation SO completely in incinerator2Gas and water vapour, are then cooled down by waste heat boiler, and generation temperature is
300 DEG C~500 DEG C of process gas, while producing 7.0~7.5MPa high steams；Process gas enter with conversion zone and
The oxidation reactor of cooling section, catalysis oxidation generates SO in oxidation reactor3And it is converted into sulfuric acid vapor；Sulfuric acid vapor enters
In cooler, sulfuric acid vapor is cooled down with air more than 250 DEG C, sulfate liquid and on-condensible gas is isolated；On-condensible gas passes through
Second of catalysis oxidation and second of refrigerated separation are carried out after Multi-stage heating again, discharge reaches the on-condensible gas of emission request, and
Collect the sulfate liquid isolated.
This technique be present：1）Conversion ratio is low, and only 80%~90%, 2）It is strongly exothermic, it is difficult to remain suitable
Reaction temperature.
Utility model content
One of the purpose of this utility model is to solve the sulfide hydrogen produced during existing carbon disulphide production
The above mentioned problem that the sulfur recovery of Process Gas is present is solved there is provided a kind of handling process for carbon disulphide production Process Gas
The problem of traditional handicraft is difficult to control on catalyzed conversion temperature, effectively raises the conversion ratio of process, final emission
（SO2 concentration is less than 30ppm）With the concentration far below national standard.
In order to achieve the above object, the utility model is adopted the following technical scheme that：One kind is used for carbon disulphide production mistake
The handling process of journey gas, including oxidation catalysis is reclaimed and hydrogenation catalyst reduces two Main Stages, specific steps include：（1）Will
Containing H2S acid gas and fuel gas air, which is first fed into acid gas combustion furnace in the case where temperature is 950 DEG C~1400 DEG C, occurs high temperature combustion
Burn reaction；（2）The Process Gas produced in acid gas combustion furnace is passed through conversion reactor, is catalyzed at a temperature of 170 DEG C~350 DEG C anti-
Should；（3）The Process Gas that conversion reactor is reflected isolates sulphur, and the tail gas of generation is in the presence of catalyst, in tail gas
Sulfur dioxide, elementary sulfur be hydrogenated and be reduced into hydrogen sulfide, organic sulfur is then hydrolyzed to hydrogen sulfide；（4）Step（3）In produced by
Pass through amine liquid circulation and stress H containing hydrogen sulfide tail gas2S and CO2, tail gas after purification enters the calcination of reclamation tail gas burning stove, discharge.
Above-mentioned technical proposal of the present utility model, is divided into oxidation catalysis by the processing of Process Gas and reclaims and hydrogenation catalyst reduction
It is divided into two stages, the main reaction difference occurred in acid gas combustion furnace and reactor converter is as follows：
Heat release is low compared with existing sulfur recovery technology, is easy to control catalyzed conversion temperature, the tail gas after purification enters tail gas
Incinerator calcination, finally（SO2 concentration is less than 30ppm）Air is discharged into the concentration far below national standard so that total sulfur recovery
Rate is up to more than 99.8%.
Preferably, step（2）In, on the one hand 210~250 DEG C of the inlet temperature of the conversion reactor ensures urging
Make COS and CS under agent effect2The hydrolysis endothermic reaction forward direction carry out, on the other hand this suitable temperature be conducive to H2S with
SO2Exothermic reaction forward direction occurs under bed catalyst effect to carry out with Recovered sulphur, but the unlikely low dew-point temperature to sulphur
Hereinafter, cause molten sulfur to separate out, and catalyst is lost activity, cause the decline of sulphur conversion ratio.
Preferably, step（2）In, the Process Gas produced in acid gas combustion furnace after heat recovery cools, is passed through and turned
Change reactor and carry out catalytic reaction, reclaim reaction heat, by-product goes out steam, reaches energy-saving recycling economy purpose.
Preferably, step（2）In, catalytic reaction is carried out using multi-stage conversion reactor, the rate of recovery can be improved.
Further preferably, catalytic reaction is carried out using two grades of conversion reactors, the third level and above conversion reactor are theoretical
On can lift the rate of recovery of sulphur again, but lifting amplitude only has 1 percent or so, so this is preferably ensureing higher sulfur recovery
While rate, equipment investment and space utilization are saved.
Preferably, in catalyzed conversion, one-level conversion reactor uses high temperature（290 DEG C~320 DEG C）, two grades of conversions are instead
The conversion temperature of device is answered then to use lower temperature (220 DEG C~240 DEG C).
Reached instead preferably, Process Gas is heated before the one-level conversion reactor and two grades of conversion reactors is passed through
The temperature is answered to send into the conversion reactor, it is to avoid the valve element of high-temp mixing valve is perishable, and valve head lining is easy to fall off, and temperature is difficult
Automatically control, and the short defect of usage cycles.
Preferably, the one-level, two grades of conversion reactors are using active aluminium-based catalyst, Process Gas（H2S、SO2Deng）
Complete to be converted into sulphur recovery under catalyst action.
Preferably, step（3）In, using cobaltmolybdate catalyst, sulfur dioxide, element in tail gas under catalyst action
Sulphur, which is hydrogenated, is reduced into hydrogen sulfide, and organic sulfur, which is hydrolyzed, changes into hydrogen sulfide.
Preferably, the conversion reactor uses heat-insulating fixed bed reactors, bed temperature deviation control can be realized
System is within 10 DEG C.
Preferably, air quantity is matched somebody with somebody in control 80%, the H of 1/3 volume is only allowed in acid gas combustion furnace2S burning generations SO2, separately
According to H in tail gas2S:SO2 = 2:1 come control remaining 20% match somebody with somebody air quantity.Acid gas furnace interior point H2S is converted into sulphur steam,
Remaining H2S continues to be converted in reactor converter.
Preferably, step（3）Hydrogenation reduction is carried out after middle tail gas is heated, heating is using the natural gas after purification
Heated for fuel direct-on-line, air distribution ratio had both met 280~300 DEG C of tail gas hydrogenation reactor inlet temperature 0.7~0.75
It is required that, ensure that the hydrogen source needed for tail gas hydrogenation reaction.
The two of the purpose of this utility model are to provide the processing equipment that above-mentioned handling process is used, including along Process Gas
Flow direction the acid gas combustion furnace, one-level condensate cooler, one turn of heater, first-stage reactor, the B-grade condensation that set gradually
Cooler, trap, hydrogenation reactor and hydrogenation cooler.
Preferably, provided with the two turns of heating set gradually between the B-grade condensation cooler and the trap
Device, second reactor and three-level condensate cooler.
Preferably, the one-level condensate cooler and B-grade condensation cooler are same condensate cooler.
Preferably, the one-level condensate cooler, B-grade condensation cooler and three-level condensate cooler are sealed by molten sulfur
Tank is connected with refined liquid sulfur pit.
Preferably, being provided with on-line heating stove between the trap and the hydrogenation reactor.
Preferably, the one-level conversion reactor and two grades of conversion reactors use heat-insulating fixed-bed conversion device.
Preferably, the primary heater is connected with one-level water distributing can.
Preferably, the secondary heater is connected with two grades of water distributing cans.
By implementing above-mentioned technical proposal, the utility model realizes Containing Sulfur by being improved in technique and equipment
The high efficiente callback of sulphur in the Process Gas of hydrogen, total sulfur recovery also solves traditional handicraft on catalyzed conversion temperature up to more than 99.8%
SO in the problem of degree is difficult to control to, final emission2Content is far below the concentration of national standard.
Brief description of the drawings
Accompanying drawing 1 is the schematic diagram of the embodiment of the utility model one.
Embodiment
Below in conjunction with the accompanying drawings and specific embodiment, the technical solution of the utility model is described in further detail.
Embodiment 1：
A kind of handling process for carbon disulphide production Process Gas, by the processing of Process Gas be divided into oxidation catalysis reclaim and
Hydrogenation catalyst reduction is divided into two stages, the Process Gas containing hydrogen sulfide after voltage stabilizing from upstream process, in acid gas
Burn, burnt completely with hydro carbons and the generation of 1/3 hydrogen sulfide at 950 DEG C with natural gas NG, compressed air CA in combustion furnace 1
Sulfur dioxide controls 80% air quantity, further accordance with H in tail gas2S:SO2= 2:1 controls remaining 20% air quantity.After burning
Pyroprocess gas enters the steam generating system of acid gas combustion furnace, and by-product 2.2MPa middle pressure steam MS is cooled to 350 after heat exchange
℃.Process Gas enters one-level condensate cooler 2,0.35Mpa low-pressure steam LS is produced in one-level condensate cooler 2, simultaneously
Process Gas is cooled to 160 DEG C in itself, and the molten sulfur condensed out is sealed from the outlet head bottom of one-level condensate cooler 2 through molten sulfur
The gravity flow of groove 10 enters refined liquid sulfur pit 11, it is cooled after Process Gas be warming up to 210 DEG C through primary heater 3 and enter first order reaction
Converter 4, catalytic reaction occurs in the case where temperature is 300 DEG C, and one-level conversion reactor 4 uses heat-insulating fixed bed reactors, bed
Layer temperature deviation control is within 10 DEG C.In the presence of catalyst, hydrogen sulfide reacts with sulfur dioxide, generates sulphur.
After the completion of reaction, temperature enters B-grade condensation cooler 2 for 300 DEG C of course of reaction gas, and by-product goes out 0.3Mpa steam, Process Gas
160 DEG C are cooled to, the molten sulfur condensed out enters refined from the bottom of B-grade condensation cooler 2 through the gravity flow of molten sulfur sealing groove 10
Liquid sulfur pit 11, the Process Gas after cooling is again after the further trap sulfur mist of trap 12, into on-line heating stove 13.Natural gas and
Enter the burning of places equivalent in air on-line heating stove 13 first, air distribution than 0.75 there is provided the hydrogen needed for hydrogenation reaction, and together
Shi Jiare tail gas is to 290 DEG C, in feeding hydrogenation reactor 14.In the presence of catalyst, sulfur dioxide, elementary sulfur in tail gas
It is hydrogenated and is reduced into hydrogen sulfide, organic sulfur (COS, CS2) then it is hydrolyzed to hydrogen sulfide.By the hydrogenation cooling of cooler 15
Afterwards, steam condenser SC discharges or recovery, waste heat recovery by-product 0.3Mpa steam is used for gas utilization unit, is that tail gas is further
The effect of precooling is served into chilling tower.
H in hydrogenating reduction tail gas2S and part CO2Enter absorption tower after over-quenching again, by the suction of amine liquid selectivity
Receive after desorption, remaining sulfide, by natural gas air calcination, is converted into SO2 by the tail gas after purification in reclamation tail gas burning stove,
Now SO2Content is less than 20ppm, meets discharge standard, air is drained into via chimney.
Embodiment 2：
A kind of handling process for carbon disulphide production Process Gas, as shown in Figure 1, is divided into oxygen by the processing of Process Gas
Change catalysis recovery and hydrogenation catalyst reduction is divided into two stages, the mistake containing hydrogen sulfide after voltage stabilizing from upstream process
Journey gas, is burnt at 1000 DEG C with natural gas NG, air CA in acid gas combustion furnace 1, is burnt completely with hydro carbons and 1/3 sulphur
Change hydrogen generation sulfur dioxide to control 80% air quantity, further accordance with H in tail gas2S:SO2= 2:1 controls remaining 20% air quantity.
Pyroprocess gas after burning enters the steam generating system of acid gas combustion furnace, by-product 2.2MPa middle pressure steam MS, after heat exchange
It is cooled to 350 DEG C.Process Gas enters one-level condensate cooler 2, and the low pressure that 0.35Mpa is produced in one-level condensate cooler 2 is steamed
Vapour LS, while Process Gas is cooled to 160 DEG C in itself, the molten sulfur condensed out from the outlet head bottom of one-level condensate cooler 2,
Enter refined liquid sulfur pit 11 through the gravity flow of molten sulfur sealing groove 10, it is cooled after Process Gas be warming up to 220 DEG C of entrance through primary heater 3
First order reaction converter 4, the inlet temperature of first-stage reactor 4 is 210 DEG C, and catalytic reaction is carried out at a temperature of 350 DEG C.Wherein
Primary heater 3 is connected with one turn of water distributing can 5, realizes steam-water separation.In the presence of catalyst, hydrogen sulfide is sent out with sulfur dioxide
Raw reaction, generates sulphur.After the completion of reaction, temperature enters B-grade condensation cooler 2 for 300 DEG C of course of reaction gas, and by-product goes out
0.3Mpa steam, Process Gas is cooled to 160 DEG C, and the molten sulfur condensed out is sealed from the bottom of B-grade condensation cooler 2 through molten sulfur
The gravity flow of groove 10 enters refined liquid sulfur pit 11, it is cooled after Process Gas be warming up to 220 DEG C through secondary heater 6 and enter second order reaction
Device, the inlet temperature of second reactor is 210 DEG C, and reaction temperature is 220 DEG C.Heater 6 is connected with two turns of water distributing cans 7, is realized
Steam-water separation.In the presence of catalyst, hydrogen sulfide continues to react with sulfur dioxide, generates sulphur.230 DEG C of reaction
Journey gas is cooled to 130 DEG C into three-level condensate cooler 9, and the molten sulfur condensed out is from three-level condensate cooler bottom, through molten sulfur
The gravity flow of sealing groove 10 enters refined liquid sulfur pit 11.Process Gas after cooling again after the further trap sulfur mist of trap 12, into
Line heating furnace 13.Enter the burning of places equivalent in natural gas and air on-line heating stove 13 first, there is provided hydrogenation 0.7 for air distribution ratio
Hydrogen needed for reaction, and heating tail gas is to 300 DEG C simultaneously, in feeding hydrogenation reactor 14.In the presence of catalyst, tail gas
In sulfur dioxide, elementary sulfur be hydrogenated and be reduced into hydrogen sulfide, organic sulfur (COS, CS2) then it is hydrolyzed to hydrogen sulfide.Passing through
It is hydrogenated with after the cooling of cooler 15, waste heat recovery by-product 0.3Mpa steam is used for gas utilization unit, is that tail gas is traveled further into
Chilling tower serves the effect of precooling.
H in hydrogenating reduction tail gas2S and part CO2Enter absorption tower after over-quenching again, by the suction of amine liquid selectivity
Receive after desorption, remaining sulfide, by natural gas air calcination, is converted into SO by the tail gas after purification in reclamation tail gas burning stove2,
Now SO2Content is less than 20ppm, and air is drained into via chimney.
Embodiment 3：
A kind of handling process for carbon disulphide production Process Gas, by the processing of Process Gas be divided into oxidation catalysis reclaim and
Hydrogenation catalyst reduction is divided into two stages, the Process Gas containing hydrogen sulfide after voltage stabilizing from upstream process, in acid gas
Burn, burnt completely with hydro carbons and 1/3 hydrogen sulfide generation two at 1000 DEG C with natural gas NG, air CA in combustion furnace 1
Sulfur oxide controls 80% air quantity, further accordance with H in tail gas2S:SO2= 2:1 controls remaining 20% air quantity.Height after burning
Warm Process Gas enters the steam generating system of acid gas combustion furnace, and by-product 2.2MPa middle pressure steam is cooled to 350 DEG C after heat exchange.
Process Gas enters one-level condensate cooler 2,0.35Mpa low-pressure steam is produced in one-level condensate cooler 2, while Process Gas
Itself be cooled to 160 DEG C, the molten sulfur condensed out from the outlet head bottom of one-level condensate cooler 2, through molten sulfur sealing groove 10 from
Stream enters refined liquid sulfur pit 11, it is cooled after Process Gas be warming up to 210 DEG C through primary heater 3 and enter first order reaction converters
4, the inlet temperature of first-stage reactor 4 is 250 DEG C, and catalytic reaction is carried out at a temperature of 300 DEG C.Wherein primary heater 3 with
One turn of water distributing can 5 is connected, and realizes steam-water separation.In the presence of catalyst, hydrogen sulfide reacts with sulfur dioxide, generates sulphur
Sulphur.After the completion of reaction, temperature enters B-grade condensation cooler 2 for 300 DEG C of course of reaction gas, and by-product goes out 0.3Mpa steam, mistake
Journey gas is cooled to 160 DEG C, and the molten sulfur condensed out flows automatically through molten sulfur sealing groove 10 and entered from the bottom of B-grade condensation cooler 2
Refined liquid sulfur pit 11, it is cooled after Process Gas be warming up to 220 DEG C through secondary heater 6 and enter second reactor, second order reaction
The inlet temperature of device is 220 DEG C, and reaction temperature is 240 DEG C.Heater 6 is connected with two turns of water distributing cans 7, realizes steam-water separation.
In the presence of catalyst, hydrogen sulfide continues to react with sulfur dioxide, generates sulphur.230 DEG C of course of reaction gas enters three
Level condensate cooler 9 is cooled to 130 DEG C, and the molten sulfur condensed out flows automatically from three-level condensate cooler bottom through molten sulfur sealing groove 10
Into refined liquid sulfur pit 11.Process Gas after cooling is again after the further trap sulfur mist of trap 12, into on-line heating stove 13.
Enter the burning of places equivalent in natural gas and air on-line heating stove 13 first, air distribution is than there is provided the hydrogen needed for hydrogenation reaction 0.7
Gas, and heating tail gas is to 280 DEG C simultaneously, in feeding hydrogenation reactor 14.In the presence of catalyst, the titanium dioxide in tail gas
Sulphur, elementary sulfur, which are hydrogenated, is reduced into hydrogen sulfide, organic sulfur (COS, CS2) then it is hydrolyzed to hydrogen sulfide.By being hydrogenated with cooler
After 15 coolings, waste heat recovery by-product 0.35Mpa steam is used for gas utilization unit, is that tail gas travels further into chilling tower and played
The effect precooled.
H in hydrogenating reduction tail gas2S and part CO2Enter absorption tower after over-quenching again, by the suction of amine liquid selectivity
Receive after desorption, remaining sulfide, by natural gas air calcination, is converted into SO by the tail gas after purification in reclamation tail gas burning stove2,
Now SO2Content is less than 25ppm, and air is drained into via chimney.
Claims (8)
1. a kind of processing equipment for carbon disulphide production Process Gas, it is characterised in that including along the flowing side of Process Gas
To the acid gas combustion furnace set gradually, one-level condensate cooler, primary heater, one-level conversion reactor, B-grade condensation cooling
Device, trap, hydrogenation reactor and hydrogenation cooler.
2. a kind of processing equipment for carbon disulphide production Process Gas according to claim 1, it is characterised in that described
It is cold provided with secondary heater, two grades of conversion reactors and the three-level set gradually between B-grade condensation cooler and the trap
Solidifying cooler.
3. a kind of processing equipment for carbon disulphide production Process Gas according to claim 1, it is characterised in that described to catch
Heating furnace is provided between storage and the hydrogenation reactor.
4. a kind of processing equipment for carbon disulphide production Process Gas according to claim 1, it is characterised in that described one
Level condensate cooler and B-grade condensation cooler are same condensate cooler.
5. a kind of processing equipment for carbon disulphide production Process Gas according to claim 1, it is characterised in that described one
Level condensate cooler, B-grade condensation cooler and three-level condensate cooler are connected with refined liquid sulfur pit by molten sulfur sealed cans.
6. a kind of processing equipment for carbon disulphide production Process Gas according to claim 1, it is characterised in that described one
Level conversion reactor and two grades of conversion reactors use heat-insulating fixed-bed conversion device.
7. a kind of processing equipment for carbon disulphide production Process Gas according to claim 1, it is characterised in that described one
Level heater is connected with one-level water distributing can.
8. a kind of processing equipment for carbon disulphide production Process Gas according to claim 2, it is characterised in that described two
Level heater is connected with two grades of water distributing cans.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108799644A (en) * | 2018-07-27 | 2018-11-13 | 四川大学 | Overheat sulfur vapor preparation facilities |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108799644A (en) * | 2018-07-27 | 2018-11-13 | 四川大学 | Overheat sulfur vapor preparation facilities |
| CN108799644B (en) * | 2018-07-27 | 2023-07-21 | 四川大学 | Superheated sulfur vapor preparation device |
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