CN203530252U - Coal gas production device using high-temperature rich oxygen and high-temperature steam as gasifying agents - Google Patents
Coal gas production device using high-temperature rich oxygen and high-temperature steam as gasifying agents Download PDFInfo
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- CN203530252U CN203530252U CN201320629326.1U CN201320629326U CN203530252U CN 203530252 U CN203530252 U CN 203530252U CN 201320629326 U CN201320629326 U CN 201320629326U CN 203530252 U CN203530252 U CN 203530252U
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- 239000001301 oxygen Substances 0.000 title claims abstract description 91
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 91
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 84
- 239000003034 coal gas Substances 0.000 title claims abstract description 36
- 239000003795 chemical substances by application Substances 0.000 title claims abstract description 10
- 238000004519 manufacturing process Methods 0.000 title abstract description 7
- 239000000126 substance Substances 0.000 claims abstract description 41
- 238000000034 method Methods 0.000 claims abstract description 28
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims description 113
- 239000010881 fly ash Substances 0.000 claims description 32
- 238000002156 mixing Methods 0.000 claims description 27
- 239000003245 coal Substances 0.000 claims description 18
- 238000002309 gasification Methods 0.000 claims description 16
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 14
- 230000001105 regulatory effect Effects 0.000 claims description 13
- 229910052757 nitrogen Inorganic materials 0.000 claims description 7
- 150000002926 oxygen Chemical class 0.000 claims description 7
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 claims description 4
- 230000001276 controlling effect Effects 0.000 claims description 3
- 229910052786 argon Inorganic materials 0.000 claims description 2
- 230000013011 mating Effects 0.000 claims description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 abstract description 4
- 230000007547 defect Effects 0.000 abstract 1
- 239000002893 slag Substances 0.000 abstract 1
- 238000005516 engineering process Methods 0.000 description 11
- 238000006243 chemical reaction Methods 0.000 description 6
- 239000002956 ash Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 238000006722 reduction reaction Methods 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000000354 decomposition reaction Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000000571 coke Substances 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 238000007664 blowing Methods 0.000 description 2
- 239000003610 charcoal Substances 0.000 description 2
- 230000007812 deficiency Effects 0.000 description 2
- 230000001590 oxidative effect Effects 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The utility model belongs to the technical field of chemical coal gas production, and in particular discloses a coal gas production method and device using high-temperature rich oxygen and high-temperature steam as gasifying agents. According to the method and device, the coal gas is produced by using rich oxygen air with the oxygen concentration of 25-30% and the oxygen temperature of 120-220 DEG C and high-temperature steam with the temperature of 120-220 DEG C as the gasifying agents, and correspondingly, a rich oxygen air source and relevant heat exchanger and control valves and pipelines are additionally arranged into the original coal gas production device. The technical defects in coal gas production by using the conventional normal-pressure fixed bed coal gas generation furnace are well overcome, the capability of the coal gas furnace and the coal gas thermal value are improved, the ash slag carbon content is reduced, the sensible heat loss is reduced, and the unit consumption of the coal gas is reduced by 10-30%.
Description
Technical field
The utility model belongs to chemical industry gas maked coal technical field, is specifically related to a kind of gas producing device.
Background technology
Atmospheric fixed bed gas-producer (also claiming mixed gas producer) is usingd the mixed gas of air and water vapor conventionally as vaporized chemical producing coal in next life gas, its working process is normally added fuel by producer gas generator top, then from furnace bottom, pass into air or oxygen enrichment and solid fuel ignition, heat is put aside at fuel bed, to fuel bed, pass into steam and carbon water generation reaction coal gas again, produce the process of coal gas mainly at gasification layer, general, the main chemical reactions of gasification layer has following oxidation and reduction reaction:
C+ O2 = CO2 + Q (1)
2C + O2 = 2CO + Q (2)
C+H2O (vapour)=CO+H2 – Q (3)
C+2H2O (vapour)=CO2+2H2-Q (4)
C + CO2 = 2CO – Q (5)
In theory, if the heat that keeps oxidizing reaction release of heat and reduction reaction to absorb, gas-making process is sustainable carrying out, and therefore, the gas-made technology flow process based on above-mentioned mechanism generally has up-downgoing air-flow journey processed and the up air-flow journey processed of continous way:
(1) upward and downward type air-flow journey processed:
Adopt air and steam as vaporized chemical, the heat savings that oxidizing reaction produces is in charcoal layer, the equal aerogenesis of up-downgoing, because this method adopts air, be that the nitrogen content brought into of vaporized chemical is higher, in the coal gas of producing, conventionally also contain too high nitrogen content, the amount of CO+H2 is relatively low, and in 40% left and right, caloric power of gas is lower;
And, in this gas-making process, conventionally, too high nitrogen content is not allowed in a lot of occasions, now, can only the method for part coal gas emptying be improved to makings by adopting, but obviously, sensible heat and latent heat have not only been wasted in this operation, have also reduced gas production rate, and have seriously polluted environment simultaneously.
In addition, this producer gas generator steam decomposition rate is lower, when upper blowing gas, steam decomposition rate is generally 40%～50%, during down blowing gas, steam decomposition rate is generally 30%～35%, cause the waste of a large amount of high-temperature steams, except waste heat boiler can reclaim a small amount of sensible heat, a large amount of steam latent heats is wasted in scrubber tower, has also greatly increased the weight of the load of circulation cleaning water system.
(2) the up air-flow journey processed of continous way
For balance heat release and endothermic process, reach the object of continuous gas processed, adopt oxygen-rich air (hereinafter to be referred as oxygen enrichment) for vaporized chemical be effective means comparatively, this production technique is because of need not emptying, few to topsoil, but because moving towards heat, single air-flow is difficult to savings at charcoal layer, gas outlet temperature is higher, and sensible heat loss is large, and in coal gas, is being mingled with a large amount of dust materials, Dui Hou workshop section processes and has proposed very high requirement, unfavorable to terminal use gas.
Summary of the invention
The purpose of this utility model is to provide that a kind of efficiency is high, quality good, eco-friendly gas producing device.
It is vaporized chemical producing coal in next life gas that the utility model adopts the high-temperature steam of 120～220 ℃ of the oxygen-rich air of 120～220 ℃ of oxygen concentrations 25～30%, oxygen temperature and temperature, overcome preferably the technological deficiency of traditional atmospheric fixed bed gas-producer gas processed, gas furnace output and caloric power of gas have been improved, reduced ash content carbon, reduced sensible heat loss, gas unit consumption has reduced the mark coal that 10～30%(unit calorific value consumes).
The high-temperature oxygen-enriched gazogene that is vaporized chemical with high-temperature steam of employing that the utility model provides, as shown in Figure 1, it comprises:
(1) at least a set of producer gas generator body 02, and as the utility appliance of mating with main body known to known technology, comprising: coal bunker 01, producer gas generator 02, mixing tank 04, chuck drum 05, fly-ash separator 06, electric tar 07, air-cooler 08, scrubber cooler 09;
(2) at least one oxygen-rich air source 03, the oxygen-rich air that oxygen-rich air source 03 provides, its oxygen concentration is 25～30%(v/v, volume percent), all the other components are nitrogen and are less than other minor components such as argon gas of 1%;
(3) at least one First Heat Exchanger, this First Heat Exchanger and fly-ash separator 06 Integrated design, within being arranged on fly-ash separator 06, or after this First Heat Exchanger is sequentially arranged on fly-ash separator 06, before air-cooler 08, producer gas generator 02 self-produced steam carries out a heat exchange with the coal gas from 02 time gas exit of producer gas generator through this First Heat Exchanger, to reclaim the heat energy of this part, and this steam preheating is become to the high-temperature steam of 120～220 ℃ of temperature, as vaporized chemical;
(4) at least one second interchanger, this second interchanger and fly-ash separator 06 Integrated design, within being arranged on fly-ash separator 06, after aforementioned First Heat Exchanger, or air-cooler 08 Integrated design that this second interchanger and gas generator system itself have, within being arranged on air-cooler 08, or before air-cooler 08; This second interchanger is used for the oxygen-rich air from oxygen-rich air source 03, the coal gas from 02 time gas exit of producer gas generator that has carried out a heat exchange with above-mentioned warp and steam gasification agent carries out a heat exchange again, and this oxygen-rich air is promoted to the temperature of 120～220 ℃, as vaporized chemical;
Further, preferably oxygen-rich air is as the heat-exchange working medium of this second interchanger or air-cooler, if underfed, can assist adopt air even water-cooled be that heat-exchange working medium carries out heat exchange compensation;
(5) preferred but non-essential at least one in order to control the by-pass valve control to aforementioned interchanger and necessary process pipeline from chuck drum 05;
(6) preferred but non-essential at least one in order to control the regulated valve to mixing tank 04 and necessary process pipeline from aforementioned interchanger;
(7) preferred but non-essential at least one in order to control the valve to mixing tank 04 and necessary process pipeline from chuck drum 05;
(8) preferred but non-essential at least one in order to control the regulated valve to producer gas generator 02 bottom and necessary process pipeline from mixing tank 04;
(9) preferred but non-essential at least one in order to control the regulated valve to producer gas generator 02 top and necessary process pipeline from mixing tank 04;
(10) as known technology, system also needs to comprise necessary control unit, so that system dynamic equipment can move, by-pass valve control can switch etc. as requested.
Based on above-mentioned gazogene, coal gas method for generation of the present utility model, detailed process is as follows:
Coal is added to producer gas generator 02 by the furnace roof coal bunker 01 with atmospheric fixed bed producer gas generator 02, after coking, enter gasification layer gasification;
It is 25～30% oxygen-rich air that oxygen-rich air source 03 provides oxygen concentration to the gasification layer of producer gas generator 02, together with the steam self-produced with producer gas generator 02, as gasification layer vaporized chemical; Wherein, from the coal gas of 02 time gas exit of producer gas generator and the interior self-produced steam of producer gas generator 02 first at First Heat Exchanger through a heat exchange, to reclaim the heat energy of this part, and this steam preheating is become to the high-temperature steam of 120～220 ℃ of temperature; Oxygen-rich air and the above-mentioned coal gas from lower gas exit that has carried out a heat exchange from oxygen-rich air source 03 carry out a heat exchange again through the second interchanger, and by these oxygen-rich air temperature increase to 120～220 ℃;
Aforementioned high-temperature steam and oxygen-rich air two portions gas enter the mixing tank 04 of furnace bottom, after mixing, as vaporized chemical, enter the bottom (or top of producer gas generator 02) of producer gas generator 02 by regulated valve; In producer gas generator 02, vaporized chemical in stove with the coal reduction reaction that gasifies, produce coal gas;
From the coal gas of lower gas exit, enter fly-ash separator 06 through dedusting, then enter First Heat Exchanger, again through and producer gas generator 02 self-produced steam heat exchange, again through air-cooler 08 with oxygen-rich air or/and other working medium heat exchange and cooling after, and the coke gas after electric tar 07 coming with upper gas exit mixes, then enter and process afterwards for user as the purification Deng Hou workshop section operation of known technology.
The applicable upward and downward type air-flow journey processed of the utility model or the up air-flow journey processed of continous way, preferably applicable upward and downward type air-flow journey processed;
And, at the vaporized chemical in uplink and downlink stage, be that oxygen enrichment is or/and steam;
The oxygen concentration of this oxygen-rich gasifying agent is 25～30%(v/v, volume percent);
Steam in this vaporized chemical has carried out a heat exchange with the coal gas (being typically about the temperature of 600 ℃) from lower gas exit, so that this steam (being generally the temperature of 100～110 ℃) is promoted to the temperature of 120～220 ℃, this heat exchanger can with the integrated design of fly-ash separator, within being arranged on fly-ash separator, also after can being sequentially arranged on fly-ash separator, before air-cooler.
Oxygen enrichment in this vaporized chemical and above-mentioned warp carry out a heat exchange again with the coal gas from lower gas exit that a heat exchange has been carried out in steam gasification agent, and this oxygen enrichment is promoted to the temperature of 120～220 ℃, this heat exchanger can with the integrated design of fly-ash separator, within being arranged on fly-ash separator, after aforementioned interchanger, and, the air-cooler Integrated design that also can have with producer gas generator itself, within being arranged on air-cooler, or before air-cooler.
Through the above-mentioned oxygen enrichment that has carried out heat exchange and steam, form the high-temperature steam vaporized chemical of 120～220 ℃ of the oxygen-rich air of 120～220 ℃ of oxygen concentrations 25～30%, oxygen temperature and temperature, after mixing tank mixes, as vaporized chemical, entered the bottom of producer gas generator.
To adopting the technique of descending system gas, through the oxygen enrichment of above-mentioned heat exchange and steam, form the high-temperature steam vaporized chemical of 120～220 ℃ of the oxygen-rich air of 120～220 ℃ of oxygen concentrations 25～30%, oxygen temperature and temperature, after mixing tank mixes, as vaporized chemical, entered the top of producer gas generator.
The utility model adopts 2 interchanger, successively the steam in vaporized chemical and oxygen-rich air are preheated to the temperature of 120～220 ℃, not only reclaimed the heat energy that descending coal gas is taken out of, alleviated the load of rear class air-cooler, wash cooling tower, what is more important is because the high-temperature steam vaporized chemical of 120～220 ℃ of the oxygen-rich air of 120～220 ℃ of the oxygen concentrations 25～30% that formed, oxygen temperature and temperature, so:
(1) improve the concentration that enters stove oxidation reactant oxygen and the temperature that enters furnace gases, be conducive to improve furnace temperature, strengthened gas processed, and be conducive to gas furnace gasification reaction, be conducive to the generation of CO;
(2) improve the concentration that enters stove oxidation reactant oxygen, reduced N2 content, thereby reduced calorific loss, reduced the ratio of void gas in coal gas simultaneously, increased inflammable gas ratio, increased the calorific value of coal gas;
(3) improve the temperature of steam in the boiler, significantly improved steam decomposition rate, thereby increased caloric power of gas;
(4) more fully and completely, coal burning more fully and completely, has reduced ash content carbon in combustion gasification reaction;
(5) increased inflammable gas in coal gas, corresponding discharge amount of exhaust gas reduces.
The present invention has comparatively comprehensively overcome the technological deficiency of traditional atmospheric fixed bed gas-producer gas processed, gas furnace output and caloric power of gas have been improved, reduce ash content carbon, reduced sensible heat loss, significantly reduced gas unit consumption (the mark Reducing Coal Consumption that unit calorific value consumes reaches 10～30%).
Accompanying drawing explanation
Fig. 1 adopts the high-temperature oxygen-enriched gazogene diagram that is vaporized chemical with high-temperature steam.
Fig. 2 is the gazogene diagram that traditional employing air and steam are vaporized chemical.
Number in the figure: 01 is coal bunker, 02 is producer gas generator, and 03 is oxygen-rich air source, and 04 is mixing tank, and 05 is chuck drum, and 06 except being dirt device, and 07 is electric tar, and 08 is air-cooler, and 09 is scrubber cooler, and 10 is interchanger; 11 is gas blower, V01, V02,, V101, V102A, V102B are variable valve.
Embodiment
Different below in conjunction with accompanying drawing with explanation the utility model and prior art, and further describe the utility model.
Fig. 1 adopts the high-temperature oxygen-enriched gazogene diagram that is vaporized chemical with high-temperature steam, and composition comprises:
Fig. 2 is the gazogene diagram that traditional employing air and steam are vaporized chemical, and as a comparison case, composition comprises:
In the utility model, oxygen-rich air used source 03 can be all oxygen rich source that oxygen concentration 25～30% can be provided, typically, as adopt the oxygen sources such as membrane sepn oxygen generating plant, PSA/VPSA/VSA oxygen generating plant, cryogenic air separation unit oxygen generating plant, bottle oxugen/liquid oxygen that the source of oxygen of this purity is independently provided, or adopt aforementioned device provide more highly purified oxygen again with air mixed after the oxygen-rich air source that forms.
In traditional technology, the coal gas of lower gas exit is typically about the temperature of 600 ℃, and this part heat energy only can obtain limited recovery in follow-up workshop section, and need be in air-cooler, scrubber cooler cooling Hou Gonghou workshop section uses, and heat energy is wasted in a large number.In the utility model, in the coal gas of this lower gas exit and stove, self-produced steam is first through a heat exchange, to reclaim the heat energy of this part and this steam preheating to be become to the high-temperature steam of the temperature of 120～220 ℃, as vaporized chemical, this First Heat Exchanger can with the integrated design of fly-ash separator, within being arranged on fly-ash separator, after also can being sequentially arranged on fly-ash separator, before air-cooler.
What in traditional technology, adopt is air, and this air directly enters mixing tank as vaporized chemical.In the utility model, what adopt is the oxygen-rich air of oxygen concentration 25～30%, and this oxygen enrichment and above-mentioned warp carry out a heat exchange again with the coal gas from lower gas exit that a heat exchange has been carried out in steam gasification agent, and this oxygen enrichment is promoted to the temperature of 120～220 ℃, as vaporized chemical; This second interchanger can with the integrated design of fly-ash separator, within being arranged on fly-ash separator, after aforementioned First Heat Exchanger, and the air-cooler Integrated design that also can have with producer gas generator itself, within being arranged on air-cooler, or before air-cooler.
As shown in accompanying drawing 1,2, air-cooler itself is the equipment that traditional producer gas generator has, and in the utility model, preferably oxygen-rich air is as the heat-exchange working medium of this water cooler, if underfed, can assist adopt air even water-cooled be that heat-exchange working medium carries out heat exchange compensation.
In the present invention, above-mentioned twice heat exchange is linked in sequence, and steam gasification agent heat exchange is front, and oxygen-rich air heat exchange is rear, to optimize echelon energy utilization.
As a preferred gas-made technology flow process, as shown in Figure 1, the steam that vapor heat exchanger 10 receives from chuck drum 05, and after preheating, send into mixing tank 04, wherein, chuck drum 05 is between vapor heat exchanger 10, and vapor heat exchanger 10 is between mixing tank 04, variable valve V102A has all been installed, and V102B, to control, to regulate flow and the temperature of vaporized chemical; And, preferably retain identical with former technology from chuck drum 05 to the variable valve V101 between mixing tank 04, using as standby or adopt aforementioned two paths with the steam flow and the temperature that regulate, control enters mixing tank 04;
Simultaneously, as a preferred gas-made technology flow process, with the unshowned path entering for uplink and downlink vaporized chemical that enters producer gas generator 02 from mixing tank 04 in accompanying drawing 1, variable valve V01 has preferably been installed, V02, in order to control respectively the vaporized chemical flow enter bottom in stove or top.
V01, V02,, V101, V102A, V102B, it is variable valve, these valves can be various forms of valves, the stopping valve of manually, automatically controlling, regulating as various, butterfly valve, gate valve etc., preferably adopt various forms of automatic regulating valves, can be pneumatic, electronic, surge, they can be according to predefined logic, as carried out regulating and controlling according to the temperature of monitoring, flow, gas composition etc.
As shown in Figure 2, conventionally, traditional atmospheric fixed bed gas-producer 02, coal is added and after coking, is entered gasification layer and gasify by furnace roof coal bunker 01, vaporized chemical comes from air and the self-produced steam of gas furnace, wherein, air is delivered to furnace bottom mixing tank 04 through gas blower 11 superchargings, and through mixing tank 04, be mixed into producer gas generator 02 with the self-produced saturation steam of stove chuck drum 05, after ash bed preheating, in stove, gasify after reduction reaction, from lower gas exit to fly-ash separator 06 dedusting, after entering after the coke gas after electric tar 07 coming with upper gas exit after air-cooler 08 is cooling mixes, workshop section is used after purifying.
In the utility model, atmospheric fixed bed gas-producer 02, coal is added and after coking, is entered gasification layer and gasify by furnace roof coal bunker 01, vaporized chemical comes from the oxygen-rich air of oxygen concentration 25～30% and the self-produced steam of gas furnace 02, wherein, the coal gas that self-produced steam and oxygen-rich air successively reach the temperature of 600 ℃ with lower gas exit temperature out carries out the high-temperature steam of the temperature of heat exchange using temperature increase to 120～220 ℃ and high-temperature oxygen-enriched air successively as vaporized chemical, in the coal gas of this lower gas exit and stove self-produced steam first at First Heat Exchanger through a heat exchange, using and reclaim the heat energy of this part and this steam preheating is become the high-temperature steam of temperature of 120～220 ℃ as vaporized chemical, this First Heat Exchanger can with fly-ash separator 06 Integrated design, within being arranged on fly-ash separator, also after can being sequentially arranged on fly-ash separator, before air-cooler 08, in addition, in the present invention, oxygen enrichment and above-mentioned warp carry out a heat exchange again with the coal gas from lower gas exit that a heat exchange has been carried out in steam gasification agent, and this oxygen enrichment are promoted to the temperature of 120～220 ℃, this second interchanger can with fly-ash separator 06 Integrated design, within being arranged on fly-ash separator, after aforesaid First Heat Exchanger, and, air-cooler 08 Integrated design that also can have with producer gas generator itself, within being arranged on air-cooler, or before air-cooler.
As accompanying drawing 1,2, air-cooler 08 itself is the equipment that traditional producer gas generator has, in the utility model, preferably oxygen-rich air is as the heat-exchange working medium of this water cooler, if underfed, can assist adopt air even water-cooled be that heat-exchange working medium carries out heat exchange compensation; Wherein, aforementioned high-temperature oxygen-enriched and high-temperature steam vaporized chemical enter furnace bottom mixing tank 04 mix after, can by valve V01/V02, enter producer gas generator 02 respectively on request, after ash bed preheating, in stove, gasify after reduction reaction, from lower gas exit to fly-ash separator 06 dedusting, interchanger 10 with self-produced steam heat exchange, air-cooler 08 with oxygen-rich air or/and other working medium heat exchange and cooling after the coke gas after electric tar 07 that comes with upper gas exit enter after mixing after use after workshop section's purification.
The utility model priority application is in producing fuel gas, but disclosed fundamental principle can be used for a lot of other occasions.By method of the present invention, can realize with producer gas generator and produce unstripped gas as required in ammonia synthesizing industry, for meeting this synthetic gas needs, this gas has specific requirement to a nitrogen content, can meet the demands by adjusting the ratio of oxygen and nitrogen in oxygen-rich air and uplink and downlink activity time, emptied part gas etc.
Embodiment described above is only set forth key characters more of the present utility model, professional and technical personnel will be appreciated that, although the utility model has carried out partly describing by reference to the accompanying drawings, but this is only an application example of the present utility model, all other variations of not violating the essence of the utility model elaboration also belong to category of the present utility model, and scope of the present utility model is limited by appending claims scope only.
Claims (3)
1. adopt a high-temperature oxygen-enriched gas producing device that is vaporized chemical with high-temperature steam, comprising:
(1) at least a set of producer gas generator body, and the utility appliance of mating with main body, comprising: coal bunker (01), producer gas generator (02), mixing tank (04), chuck drum (05), fly-ash separator (06), electric tar (07), air-cooler (08), scrubber cooler (09); It is characterized in that, also comprise:
(2) at least one oxygen-rich air source (03), the oxygen-rich air that oxygen-rich air source (03) provides, its oxygen concentration is 25～30%, v/v, volume percent; All the other components are the argon gas of nitrogen, trace;
(3) at least one First Heat Exchanger, this First Heat Exchanger and fly-ash separator (06) Integrated design, within being arranged on fly-ash separator (06), or this First Heat Exchanger is sequentially arranged on fly-ash separator (06) afterwards, air-cooler (08) before, producer gas generator (02) self-produced steam carries out a heat exchange with the coal gas from the lower gas exit of producer gas generator (02) through this First Heat Exchanger, to reclaim the heat energy of this part and this steam preheating to be become to the high-temperature steam of 120～220 ℃ of temperature, as vaporized chemical;
(4) at least one second interchanger, this second interchanger and fly-ash separator (06) Integrated design, within being arranged on fly-ash separator (06), after aforementioned First Heat Exchanger, or air-cooler (08) Integrated design that this second interchanger and gas generator system itself have, within being arranged on air-cooler (08), or air-cooler (08) before; This second interchanger is used for will be from the oxygen-rich air of oxygen-rich air source (03), the coal gas from the lower gas exit of producer gas generator (02) that has carried out a heat exchange with above-mentioned warp and steam gasification agent carries out a heat exchange again, and this oxygen-rich air is promoted to the temperature of 120～220 ℃, as vaporized chemical;
(5) at least one is in order to control regulated valve and the process pipeline to aforementioned interchanger from chuck drum (05);
(6) at least one is in order to control from aforementioned interchanger regulated valve and the process pipeline to mixing tank (04);
(7) at least one is in order to control from chuck drum (05) regulated valve and the process pipeline to mixing tank (04);
(8) at least one is in order to control from mixing tank (04) regulated valve and the process pipeline to producer gas generator (02) bottom;
(9) at least one is in order to control from mixing tank (04) regulated valve and the process pipeline to producer gas generator (02) top.
2. gas producing device according to claim 1, it is characterized in that, oxygen-rich air source (03) is connected with air-cooler (08), thereby using the heat-exchange working medium as air-cooler (08) from the oxygen-rich air of oxygen-rich air source (03), and auxiliary to adopt air or water-cooled be the heat-exchange working medium of air-cooler (08), carry out heat exchange compensation.
3. gas producing device according to claim 1, is characterized in that, described variable valve is stopping valve, butterfly valve or the gate valve of regulating and controlling manually or automatically.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320629326.1U CN203530252U (en) | 2013-10-13 | 2013-10-13 | Coal gas production device using high-temperature rich oxygen and high-temperature steam as gasifying agents |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201320629326.1U CN203530252U (en) | 2013-10-13 | 2013-10-13 | Coal gas production device using high-temperature rich oxygen and high-temperature steam as gasifying agents |
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| CN203530252U true CN203530252U (en) | 2014-04-09 |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103525465A (en) * | 2013-10-13 | 2014-01-22 | 上海穗杉实业有限公司 | Coal gas production method and device using high-temperature rich oxygen and high temperature steam as gasification agent |
| CN106336902A (en) * | 2016-11-18 | 2017-01-18 | 北京金泰瑞和工程科技有限公司 | Ammonia or methanol synthesizing system |
| CN108300513A (en) * | 2018-01-18 | 2018-07-20 | 山东京博众诚清洁能源有限公司 | A kind of production method improving bed furnace gas quality |
-
2013
- 2013-10-13 CN CN201320629326.1U patent/CN203530252U/en not_active Expired - Lifetime
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103525465A (en) * | 2013-10-13 | 2014-01-22 | 上海穗杉实业有限公司 | Coal gas production method and device using high-temperature rich oxygen and high temperature steam as gasification agent |
| CN103525465B (en) * | 2013-10-13 | 2015-04-29 | 上海穗杉实业有限公司 | Coal gas production method and device using high-temperature rich oxygen and high temperature steam as gasification agent |
| CN106336902A (en) * | 2016-11-18 | 2017-01-18 | 北京金泰瑞和工程科技有限公司 | Ammonia or methanol synthesizing system |
| CN108300513A (en) * | 2018-01-18 | 2018-07-20 | 山东京博众诚清洁能源有限公司 | A kind of production method improving bed furnace gas quality |
| CN108300513B (en) * | 2018-01-18 | 2020-04-17 | 山东京博众诚清洁能源有限公司 | Production method for improving quality of fixed bed furnace gas |
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