CN203998946U - Carbonated gas returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas - Google Patents
Carbonated gas returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas Download PDFInfo
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- CN203998946U CN203998946U CN201420159745.8U CN201420159745U CN203998946U CN 203998946 U CN203998946 U CN 203998946U CN 201420159745 U CN201420159745 U CN 201420159745U CN 203998946 U CN203998946 U CN 203998946U
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- catalytic converter
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- pipes
- carbonated
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- 239000007789 gas Substances 0.000 claims abstract description 300
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 92
- 238000002407 reforming Methods 0.000 claims abstract description 37
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000006243 chemical reaction Methods 0.000 claims abstract description 23
- 235000009508 confectionery Nutrition 0.000 claims abstract description 15
- 239000003345 natural gas Substances 0.000 claims abstract description 15
- 239000000571 coke Substances 0.000 claims abstract description 14
- 238000000034 method Methods 0.000 claims description 30
- 238000001816 cooling Methods 0.000 claims description 19
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 16
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 8
- 239000001569 carbon dioxide Substances 0.000 claims description 8
- 239000007800 oxidant agent Substances 0.000 claims description 8
- 230000001590 oxidative effect Effects 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 6
- 238000010791 quenching Methods 0.000 claims description 5
- 238000011084 recovery Methods 0.000 claims description 2
- 230000003197 catalytic effect Effects 0.000 abstract description 12
- 238000004519 manufacturing process Methods 0.000 abstract description 10
- 239000000446 fuel Substances 0.000 abstract description 9
- 239000005431 greenhouse gas Substances 0.000 abstract description 6
- 229930195733 hydrocarbon Natural products 0.000 description 14
- 150000002430 hydrocarbons Chemical class 0.000 description 14
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 10
- 235000011941 Tilia x europaea Nutrition 0.000 description 10
- 239000004571 lime Substances 0.000 description 10
- 239000004215 Carbon black (E152) Substances 0.000 description 8
- 229910002091 carbon monoxide Inorganic materials 0.000 description 8
- 238000005516 engineering process Methods 0.000 description 8
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 7
- 239000012528 membrane Substances 0.000 description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 230000009466 transformation Effects 0.000 description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 5
- 230000008901 benefit Effects 0.000 description 4
- 230000015572 biosynthetic process Effects 0.000 description 4
- 239000006229 carbon black Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- 238000002156 mixing Methods 0.000 description 4
- 230000003647 oxidation Effects 0.000 description 4
- 238000007254 oxidation reaction Methods 0.000 description 4
- 238000003786 synthesis reaction Methods 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 235000019628 coolness Nutrition 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 230000001131 transforming effect Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The disclosed carbonated gas of the utility model returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas, it at least comprises on-catalytic conversion system and CO 2 enriched gas line of pipes, methane-rich gas line of pipes, the input terminus of its CO 2 enriched gas line of pipes connects CO 2 enriched gas and reclaims source, and the output terminal of CO 2 enriched gas line of pipes is connected with methane-rich gas line of pipes.The utility model is synthetic by Fischer-Tropsch, PSA etc. is rich in CO
2tail gas be back to after the methane rich unstripped gass such as conversion section and Sweet natural gas or coke(oven)gas mix and enter pure oxygen non-catalytic Partial Conversion stove (POX), its synthetic gas is delivered to the synthetic HuoPSADeng of Fischer-Tropsch workshop section again.Adopt the utility model, can increase production the available gas CO in synthetic gas, regulate H in synthetic gas
2the mol ratio of/CO; Meanwhile, reduced greenhouse gases CO
2discharge.Make the former CO that contains that should discharge or be used as fuel
2gas reforming becomes the available gas of synthetic gas, and the recycle of resource is more reasonable.
Description
Technical field
The utility model relates to the comprehensive utilization technique field of carbon dioxide containing gas, and particularly the conversion unstripped gas such as the carbonated gas such as Fischer-Tropsch process exhaust and Sweet natural gas mixes and by on-catalytic Partial Conversion preparing synthetic gas, with the carbon dioxide containing gas of carbon monoxide in volume increase synthetic gas, returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas.
Background technology
Take the methane-rich gas such as Sweet natural gas or coke(oven)gas, be unstripped gas, transform and prepare that synthetic gas is synthetic for Fischer-Tropsch, methyl alcohol is synthetic or hydrogen manufacturing carbon monoxide processed, reforming gas H
2/ CO mol ratio is generally higher, shows as Fu Qing and lacks carbon.
Various process tail gas, if Fischer-Tropsch process exhaust is after preliminary treatment, produce containing CO
2gas, this part gas is generally speeded to put or as fuel combustion, is had the problems such as the wasting of resources and environmental pollution.Take Fischer-Tropsch process exhaust as example, and Fischer-Tropsch process exhaust is mainly by CO
2, N
2, unreacted synthesis gas, a small amount of lower carbon number hydrocarbons (be mainly C
6below) and other components form.General tail gas partly circulates and returns to Fischer-Tropsch synthesis device entrance to improve total hydrocarbon conversion rate and yield, and the Fischer-Tropsch process exhaust of narrow sense often refers to the partial tail gas of sending Fischer-Tropsch synthesizer.Because wherein containing H
2, the higher component of economic worth such as CO or lower carbon number hydrocarbons, Fischer-Tropsch tail gas, through processing, reclaims one or more component, but final tail gas is still as fuel or is rich in CO
2gas qualified discharge, H in tail gas
2, CO and lower carbon number hydrocarbons etc. are uneconomical as fuel when tail gas amount is very large.Also having patented technology is that synthetic gas returns to Fischer-Tropsch synthesis device by modes such as conversions by the hydrocarbon conversion in tail gas, but H in tail gas
2high with CO content, if deliver to Fischer-Tropsch synthesis device, there is the reactor volume of major part to be wasted.
And synthetic gas reclaims H through PSA
2after active principle, in PSA tail gas, also contain a large amount of CO
2gas.PSA tail gas is generally as fuel, due to CO
2belong to non-combustible gas, enter fuel gas system and discharge process and all need to consume a large amount of heats, also have the serious situation of energy dissipation.Therefore, improving tail gas comprehensive utilization value can produce material impact to production process, and has important meaning to reducing greenhouse gas emission and improving efficiency of energy utilization aspect.
Consider that take the high methane gass such as Sweet natural gas or coke(oven)gas is raw material, the general rich hydrogen of synthetic gas obtaining by conversion reaction lacks carbon, utilizes advanced non-catalytic transforming technology, will be containing CO in factory
2tail gas with transform unstripped gas and mix after, enter on-catalytic converter and react, CO
2can with unstripped gas in hydro carbons react and generate CO and H
2, can increase CO content in reforming gas, avoided the wasting of resources, reduced again greenhouse gases CO
2discharge, there is good economy and environment benefit.
Pure oxygen non-catalytic transformation technology is a kind of safe, reliable, simple directly synthetic gas technology of preparing, the application experience of existing many these technology of cover of applicant, and respectively there are many cover POX pure oxygen non-catalytic converters in Hebei, Ningxia at safety, stable, long-term operation.Compare with other transformation technologies, on-catalytic transform have steam consumption seldom, carbon monoxide output is high, converter temperature out is high, while normally producing without carbon black and to features such as the requirement of unstripped gas foreign matter content are low.Therefore, utilize advanced pure oxygen non-catalytic transformation technology (POX), containing CO
2the methane-rich gas such as gas and Sweet natural gas or coke(oven)gas transform unstripped gas to be mixed and transforms preparing synthetic gas, to increase production CO, and reduces and contains CO
2the discharge of tail gas has realistic feasibility.
Utility model content
Technical problem to be solved in the utility model is that the tail gas recycle of the processes such as, PSA synthetic for current Fischer-Tropsch is utilized insufficient or recycles that energy consumption is large, flow process is complicated, invest high present situation, a kind of tail gas comprehensive utilization process of low-carbon emission is proposed, the carbonated gas of the problems such as the environment bringing when solving the exhaust emissions of the processes such as Fischer-Tropsch is synthetic, PSA or being used as fuel and the wasting of resources returns to the device that on-catalytic converter is prepared synthetic gas, this device can increase production the CO in transformation of synthetic gas, has reduced again greenhouse gases CO
2discharge, there is good economy and environment benefit.
Technical problem to be solved in the utility model can be achieved through the following technical solutions:
Carbonated gas returns to the device that on-catalytic converter is prepared synthetic gas, at least comprise on-catalytic conversion system and CO 2 enriched gas line of pipes, methane-rich gas line of pipes, the top of described on-catalytic conversion system converter has burner, described burner has feed gas passage and oxidant channel, described oxidant channel connects the pure oxygen delivery port of air separation plant by pure oxygen line of pipes, described feed gas passage connects the output terminal of methane-rich gas line of pipes, it is characterized in that, the input terminus of described CO 2 enriched gas line of pipes connects CO 2 enriched gas and reclaims source, the output terminal of CO 2 enriched gas line of pipes is connected with methane-rich gas line of pipes.
In a preferred embodiment of the present utility model, described CO 2 enriched gas recovery source is Fischer-Tropsch process exhaust or PSA tail gas.
In a preferred embodiment of the present utility model, the methane-rich gas that described methane-rich gas line of pipes is carried is Sweet natural gas or coke(oven)gas.
In a preferred embodiment of the present utility model, described Fischer-Tropsch process exhaust is produced by a Fischer-Tropsch synthesizer, described Fischer-Tropsch synthesizer at least has a carbonated tail gas and discharges mouth and a synthetic gas input aperture, and described on-catalytic converter has a reforming gas delivery port; And also comprise an exhaust gas processing device, described exhaust gas processing device at least has a tail gas input aperture, CO 2 enriched gas delivery port, and described tail gas input aperture and carbonated tail gas on described Fischer-Tropsch synthesizer discharge and mouthful by exhaust pipe line, is connected; , between the reforming gas delivery port of described on-catalytic converter and the synthetic gas input aperture of described Fischer-Tropsch synthesizer, technique is connected, and described CO 2 enriched gas delivery port is connected with the input terminus of described CO 2 enriched gas line of pipes.
In a preferred embodiment of the present utility model, between the reforming gas delivery port of described on-catalytic converter and the synthetic gas input aperture of described Fischer-Tropsch synthesizer, by Quench or heat reclamation device, wash cooling device, be connected successively.
In a preferred embodiment of the present utility model, described PSA tail gas is produced by a PSA device, described PSA device at least has one and is rich in that carbon dioxide tail gas discharges mouthful and a synthetic gas input aperture, described on-catalytic converter has a reforming gas delivery port, and between the reforming gas delivery port of described on-catalytic converter and the synthetic gas input aperture of described PSA device, technique is connected; The carbon dioxide tail gas that is rich in described PSA device discharges and mouthful is connected with the input terminus of described CO 2 enriched gas line of pipes.
In a preferred embodiment of the present utility model, between the reforming gas delivery port of described on-catalytic converter and the synthetic gas input aperture of described PSA device, by Quench or heat reclamation device, wash cooling device, be connected successively.
In a preferred embodiment of the present utility model, described heat reclamation device is the combination of useless pot, vapor superheater, feedwater preheater.
Principle of work of the present utility model is: the tail gas of Fischer-Tropsch synthesizer or PSA tail gas etc. is rich in to CO
2gas mixes with methane rich unstripped gass such as Sweet natural gas or coke(oven)gas, enters pure oxygen non-catalytic Partial Conversion stove (POX) and carries out conversion reaction.The pure oxygen of the oxygenant of converter for dividing from sky.By the burner/nozzle mixer of particular design, mixing raw material gas and pure oxygen be fast mixing combustion in on-catalytic Partial Conversion stove (POX), and hydro carbons and oxygen carry out combustion reactions until oxygen depletion is complete, remaining hydro carbons respectively with CO
2, H
2o reacts and generates CO and H
2.Containing CO
2adding of gas, is conducive to increase production CO, reaction below main generation in converter:
CH
4+CO
2=2CO+2H
2
The reforming gas that goes out pure oxygen non-catalytic converter (POX) adopts Quench and/or waste heat boiler to reclaim heat, then through wash cooling, according to need of production, synthetic gas is delivered to Fischer-Tropsch synthesizer HuoPSADeng workshop section.The tail gas producing in technique after treatment be rich in CO
2gas is back to conversion section and unstripped gas is mixed into pure oxygen non-catalytic Partial Conversion stove (POX).
In device of the present utility model, the burner at on-catalytic converter top is a nucleus equipment, can directly have influence on the generation of transformation efficiency and the carbon black of conversion system.Owing to there being more CO
2allocate in converter, the trend that generates carbon black in converter has been increased, therefore applicant of the present utility model faces the unfavourable condition such as higher yielding stress and various corrosion for existing POX burner material under worst hot case, recommend adoption the applicant denomination of invention that 26Xiang China national Department of Intellectual Property submits in May, 2011 is the disclosed burner for preparing syngas by non-catalytic partial oxidation of " burner for preparing syngas by non-catalytic partial oxidation " patent of invention (Granted publication CN102275872B), unstripped gas and oxygenant are mixed, burn more abundant, and can improve unstripped gas transformation efficiency, effectively avoid the generation of carbon black in converter, more be conducive to containing CO
2tail gas returns to the feasibility of conversion section technique.
The utility model is used is rich in CO
2gas is including but not limited to Fischer-Tropsch process exhaust, PSA tail gas, and on-catalytic transforms raw material including but not limited to methane-rich gas such as Sweet natural gas, coke(oven)gas, membrane sepn impermeable gas.Synthetic gas after the utility model is processed, according to need of production, can deliver to that follow-up Fischer-Tropsch is synthetic, PSADeng workshop section.
Adopt device of the present utility model, reclaim the CO that contains of the processes such as Fischer-Tropsch is synthetic, PSA
2gas, produces hydrogeneous and synthetic gas carbon monoxide, can increase production the CO in synthetic gas, has reduced again greenhouse gases CO
2discharge, whole flow process is more simplified, and has good economy and environment benefit.
The effect that specifically can reach is as follows:
1. CO in the waste gas that device of the present utility model is used
2in converter with unstripped gas in hydrocarbon reaction be converted into CO, can increase production CO.The former CO that contains that should discharge or be used as fuel
2gas reforming becomes the available gas of synthetic gas, and the recycle of resource is more reasonable.
2. adopt device of the present utility model, can be by allocating into containing CO in converter
2gas volume, suitably regulates synthetic gas H
2/ CO mol ratio, makes synthetic gas H
2/ CO mol ratio reaches the synthetic requirement that waits workshop section of Fischer-Tropsch, or reduces the load of subsequent adjustment synthetic gas hydrogen-carbon ratio workshop section, has shortened process, the advantages such as saving investment in fixed assets.
3. adopt device of the present utility model, the methane content in its process gas can be reduced to below 0.3%, and concerning producing the device that synthetic ammonia or synthesizing methanol are object, whole technical process is greatly simplified, and available gas utilization ratio rises.
4. adopt device of the present utility model, can Fischer-Tropsch is synthetic, the tail gas of the process such as PSA delivers to on-catalytic conversion unit, reduces the direct discharge of final tail gas or the flue gas that burning produces, reduced containing CO
2the discharge of greenhouse gases.Therefore, be conducive to improve problem of environmental pollution.
Accompanying drawing explanation
Fig. 1 is that the carbonated gas of the utility model embodiment 1 returns to the structural representation that on-catalytic converter is prepared the device of synthetic gas.
Fig. 2 is that the carbonated gas of the utility model embodiment 2 returns to the structural representation that on-catalytic converter is prepared the device of synthetic gas.
Embodiment
Embodiment 1
Referring to Fig. 1, carbonated gas shown in figure returns to the device that on-catalytic converter is prepared synthetic gas, comprises on-catalytic converter 100, chilling device or heat reclamation device 200, wash cooling device 300, exhaust gas processing device 400 and Fischer-Tropsch synthesizer 500.
In on-catalytic converter 100, have a burner (not shown), this burner adopts Granted publication CN102275872B specification sheets and the disclosed burner for preparing syngas by non-catalytic partial oxidation of Figure of description thereof.This on-catalytic converter 100 also has a reforming gas delivery port 110.
Fischer-Tropsch synthesizer 500 has a synthetic gas input aperture 510, wastewater outlet 520, liquid hydrocarbon outlet 530 and one carbonated tail gas and speeds to put mouthfuls 540.
Exhaust gas processing device 400 has tail gas input aperture 410, CO 2 enriched gas delivery port 420 and clean gas outlet 430.
Heat reclamation device is the combination of useless pot, vapor superheater, feedwater preheater.
Feed gas passage in the interior burner of on-catalytic converter 100 connects a methane-rich gas line of pipes 600, methane-rich gas line of pipes 600 is inputted the methane-rich gas such as Sweet natural gas or coke(oven)gas or membrane sepn impermeable gas continually in the feed gas passage of burner, oxidant channel in the interior burner of on-catalytic converter 100 is connected to the pure oxygen delivery port 710 of air separation plant 700 by pure oxygen transfer lime 610, air separation plant 700 is carried pure oxygen endlessly by pure oxygen delivery port 710 and pure oxygen transfer lime 610 in the oxidant channel in burner.
The reforming gas of reforming gas delivery port 110 outputs of on-catalytic converter 100 enters into chilling device by the reforming gas input aperture 210 in reforming gas transfer lime 620, chilling device or heat reclamation device 200 or heat reclamation device 200 carries out heat recuperation, the reforming gas delivery port 220 of reforming gas after heat recuperation in chilling device or heat reclamation device 200 out after, by the reforming gas entrance 310 in reforming gas transfer lime 630, wash cooling device 300, enter and in wash cooling device 300, carry out wash cooling.The syngas outlet 320 of synthetic gas after wash cooling device 300 wash coolings in wash cooling device 300 sent, the synthetic gas of sending is sent in Fischer-Tropsch synthesizer 500 by the synthetic gas input aperture 510 in synthetic gas transfer lime 640, Fischer-Tropsch synthesizer 500, the waste water that Fischer-Tropsch synthesizer 500 produces is discharged by wastewater outlet 520, and liquid hydrocarbon exports 530 by liquid hydrocarbon and sends into next workshop section.And the carbonated tail gas of the richness that Fischer-Tropsch synthesizer 500 produces discharges mouthfuls 540 by carbon dioxide tail gas and sends, the carbonated tail gas of richness of sending enters into exhaust gas processing device 400 by the tail gas input aperture 410 in exhaust pipe line 650, exhaust gas processing device 400 and processes, and the purified gas after processing is sent into next workshop section by the clean gas outlet 430 in exhaust gas processing device 400.And the carbonated gas of richness in exhaust gas processing device 400 is sent by CO 2 enriched gas delivery port 420, the carbonated gas of richness of sending is sent into methane-rich gas line of pipes 600 by CO 2 enriched gas line of pipes 660, mix with methane-rich gas such as Sweet natural gas or coke(oven)gas or membrane sepn impermeable gas, after mixing, by burner, spray in on-catalytic converter 100, be converted into carbon monoxide with the hydrocarbon reaction in the methane-rich gas such as Sweet natural gas or coke(oven)gas or membrane sepn impermeable gas.The former CO that contains that should discharge or be used as fuel
2gas reforming becomes the available gas of synthetic gas, and the recycle of resource is more reasonable.
Embodiment 2
Referring to Fig. 2, the carbonated gas shown in figure returns to the device that on-catalytic converter is prepared synthetic gas, comprises on-catalytic converter 100, chilling device or heat reclamation device 200, wash cooling device 300 and PSA device 800.
In on-catalytic converter 100, have a burner (not shown), this burner adopts Granted publication CN102275872B specification sheets and the disclosed burner for preparing syngas by non-catalytic partial oxidation of Figure of description thereof.This on-catalytic converter 100 also has a reforming gas delivery port 110.
PSA device 800 has the outlets 820 of gas such as a synthetic gas input aperture 810, CO, the outlet 830 of purified gas and a carbonated tail gas speed to put mouth 840.
Heat reclamation device is the combination of useless pot, vapor superheater, feedwater preheater.
Feed gas passage in burner in on-catalytic converter 100 connects a methane-rich gas input tube 600, methane-rich gas line of pipes 600 is inputted the methane-rich gas such as Sweet natural gas or coke(oven)gas or membrane sepn impermeable gas endlessly in the feed gas passage of burner, oxidant channel in burner in on-catalytic converter 100 is connected to the pure oxygen delivery port 710 of air separation plant 700 by pure oxygen transfer lime 610, air separation plant 700 is carried pure oxygen endlessly by pure oxygen delivery port 710 and pure oxygen transfer lime 610 in the oxidant channel in burner.
The reforming gas of reforming gas delivery port 110 outputs of on-catalytic converter 100 enters into chilling device by the reforming gas input aperture 210 in reforming gas transfer lime 620, chilling device or heat reclamation device 200 or heat reclamation device 200 carries out heat recuperation, the reforming gas delivery port 220 of reforming gas after heat recuperation in chilling device or heat reclamation device 200 out after, by the reforming gas entrance 310 in reforming gas transfer lime 630, wash cooling device 300, enter and in wash cooling device 300, carry out wash cooling.The syngas outlet 320 of synthetic gas after wash cooling device 300 wash coolings in wash cooling device 300 sent, and the synthetic gas of sending is sent in PSA device 800 by the synthetic gas input aperture 810 in synthetic gas transfer lime 640, PSA device 800.
The gases such as CO that PSA device 800 produces are sent into next workshop section by exporting 820, and the purified gas that PSA device 800 produces is sent into next workshop section by exporting 830; And the carbonated gas of the richness that PSA device 800 produces is speeded to put mouthfuls 840 by carbon dioxide tail gas and is sent, the carbonated gas of richness of sending is sent into methane-rich gas input tube 600 by CO 2 enriched gas line of pipes 660, mix with methane-rich gas such as Sweet natural gas or coke(oven)gas or membrane sepn impermeable gas, after mixing, by burner, spray in on-catalytic converter 100, be converted into carbon monoxide with the hydrocarbon reaction in the methane-rich gas such as Sweet natural gas or coke(oven)gas or membrane sepn impermeable gas.The former CO that contains that should discharge or be used as fuel
2gas reforming becomes the available gas of synthetic gas, and the recycle of resource is more reasonable.
Claims (8)
1. carbonated gas returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas, at least comprise on-catalytic conversion system and CO 2 enriched gas line of pipes, methane-rich gas line of pipes, the top of described on-catalytic conversion system converter has burner, described burner has feed gas passage and oxidant channel, described oxidant channel connects the pure oxygen delivery port of air separation plant by pure oxygen line of pipes, described feed gas passage connects the output terminal of methane-rich gas line of pipes, it is characterized in that, the input terminus of described CO 2 enriched gas line of pipes connects CO 2 enriched gas and reclaims source, the output terminal of CO 2 enriched gas line of pipes is connected with methane-rich gas line of pipes.
2. carbonated gas as claimed in claim 1 returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas, it is characterized in that, described CO 2 enriched gas recovery source is Fischer-Tropsch process exhaust or PSA tail gas.
3. carbonated gas as claimed in claim 1 returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas, it is characterized in that, the methane-rich gas that described methane-rich gas line of pipes is carried is Sweet natural gas or coke(oven)gas.
4. carbonated gas as claimed in claim 2 returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas, it is characterized in that, described Fischer-Tropsch process exhaust is produced by a Fischer-Tropsch synthesizer, described Fischer-Tropsch synthesizer at least has a carbonated tail gas and discharges mouth and a synthetic gas input aperture, and described on-catalytic converter has a reforming gas delivery port; And also comprise an exhaust gas processing device, described exhaust gas processing device at least has a tail gas input aperture, CO 2 enriched gas delivery port, and described tail gas input aperture and carbonated tail gas on described Fischer-Tropsch synthesizer discharge and mouthful by exhaust pipe line, is connected; Between the reforming gas delivery port of described on-catalytic converter and the synthetic gas input aperture of described Fischer-Tropsch synthesizer, technique is connected, and described CO 2 enriched gas delivery port is connected with the input terminus of described CO 2 enriched gas line of pipes.
5. carbonated gas as claimed in claim 4 returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas, it is characterized in that, between the reforming gas delivery port of described on-catalytic converter and the synthetic gas input aperture of described Fischer-Tropsch synthesizer, by Quench or heat reclamation device, wash cooling device, be connected successively.
6. carbonated gas as claimed in claim 2 returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas, it is characterized in that, described PSA tail gas is produced by a PSA device, described PSA device at least has one and is rich in that carbon dioxide tail gas discharges mouthful and a synthetic gas input aperture, described on-catalytic converter has a reforming gas delivery port, and between the reforming gas delivery port of described on-catalytic converter and the synthetic gas input aperture of described PSA device, technique is connected; The carbon dioxide tail gas that is rich in described PSA device discharges and mouthful is connected with the input terminus of described CO 2 enriched gas line of pipes.
7. carbonated gas as claimed in claim 6 returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas, it is characterized in that, between the reforming gas delivery port of described on-catalytic converter and the synthetic gas input aperture of described PSA device, by Quench or heat reclamation device, wash cooling device, be connected successively.
8. carbonated gas as claimed in claim 7 returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas, it is characterized in that, described heat reclamation device is the combination of useless pot, vapor superheater, feedwater preheater.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420159745.8U CN203998946U (en) | 2014-04-02 | 2014-04-02 | Carbonated gas returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420159745.8U CN203998946U (en) | 2014-04-02 | 2014-04-02 | Carbonated gas returns to the device of on-catalytic converter energy-saving and production-increase synthetic gas |
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| CN203998946U true CN203998946U (en) | 2014-12-10 |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106520178A (en) * | 2015-09-14 | 2017-03-22 | 上海华西化工科技有限公司 | Method for combined production of fuel oil with coke oven gas and small-size coke prepared gas |
| CN106520177A (en) * | 2015-09-14 | 2017-03-22 | 上海华西化工科技有限公司 | Method of directly preparing fuel oil from coke oven gas |
| CN106520179A (en) * | 2015-09-14 | 2017-03-22 | 上海华西化工科技有限公司 | Method for combined production of fuel oil with coke oven gas and carbon dioxide-enriched gas |
| CN113518755A (en) * | 2019-03-06 | 2021-10-19 | 林德有限责任公司 | Method and device for producing synthesis gas by carbon dioxide recycling |
| CN113526465A (en) * | 2021-08-06 | 2021-10-22 | 西南大学 | Method for preparing synthesis gas by combining non-catalytic partial oxidation of natural gas with reforming of carbon dioxide |
-
2014
- 2014-04-02 CN CN201420159745.8U patent/CN203998946U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106520178A (en) * | 2015-09-14 | 2017-03-22 | 上海华西化工科技有限公司 | Method for combined production of fuel oil with coke oven gas and small-size coke prepared gas |
| CN106520177A (en) * | 2015-09-14 | 2017-03-22 | 上海华西化工科技有限公司 | Method of directly preparing fuel oil from coke oven gas |
| CN106520179A (en) * | 2015-09-14 | 2017-03-22 | 上海华西化工科技有限公司 | Method for combined production of fuel oil with coke oven gas and carbon dioxide-enriched gas |
| CN113518755A (en) * | 2019-03-06 | 2021-10-19 | 林德有限责任公司 | Method and device for producing synthesis gas by carbon dioxide recycling |
| CN113526465A (en) * | 2021-08-06 | 2021-10-22 | 西南大学 | Method for preparing synthesis gas by combining non-catalytic partial oxidation of natural gas with reforming of carbon dioxide |
| CN113526465B (en) * | 2021-08-06 | 2022-11-08 | 西南大学 | Method for preparing synthesis gas by combining non-catalytic partial oxidation of natural gas with reforming of carbon dioxide |
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| C14 | Grant of patent or utility model | ||
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