CN103509605A - Method and device using high temperature air and high temperature steam as gasification agents for coal gas production - Google Patents
Method and device using high temperature air and high temperature steam as gasification agents for coal gas production Download PDFInfo
- Publication number
- CN103509605A CN103509605A CN201310475179.1A CN201310475179A CN103509605A CN 103509605 A CN103509605 A CN 103509605A CN 201310475179 A CN201310475179 A CN 201310475179A CN 103509605 A CN103509605 A CN 103509605A
- Authority
- CN
- China
- Prior art keywords
- air
- gas
- coal
- steam
- temperature
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Landscapes
- Industrial Gases (AREA)
Abstract
The invention belongs to the technical field of chemical coal gases, in particular to a method and a device using high temperature air and high temperature steam as gasification agents for coal gas production. According to the invention, coal gases are produced by using the air with a temperature of 120 to 220 DEG C and oxygen content of 20.93 percent (v/v) and the high temperature steam with a temperature of 120 to 220 DEG C as the gasification agents. Correspondingly, a heat exchanger, a control valve and a pipeline are additionally arranged in an original coal gas production device. According to the invention, the technical defects of gas production of a conventional normal-pressure fixed bed gas producer are well overcome; yield of a gas furnace and the calorific value of the coal gases are improved; carbon content in ash is reduced; sensible heat loss is reduced; standard coal consumption under the unit calorific value is reduced to 5 to 15 percent.
Description
Technical field
The invention belongs to chemical industry gas maked coal technical field, be specifically related to a kind of coal gas production method and 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 object of the present invention is to provide that a kind of efficiency is high, quality good, eco-friendly coal gas production method and device.
It is the air (oxygen level 20.93% of 120～220 ℃ that the present invention adopts temperature, v/v, volume percent) be that the high-temperature steam of 120～220 ℃ is vaporized chemical producing coal in next life gas with 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 5～15%(unit calorific value consumes).
The gazogene that employing high temperature air provided by the invention and high-temperature steam are vaporized chemical, as shown in Figure 1, it comprises:
(1) at least a set of producer gas generator 02 body, and as the utility appliance of mating with main body known to known technology, comprise as coal bunker 01, producer gas generator 02, gas blower 03, mixing tank 04, chuck drum 05, fly-ash separator 06, electric tar 07, air-cooler 08, scrubber cooler 09, also has the treatment and finishing section of follow-up necessity;
(2) at least one First Heat Exchanger, this first parallel operation 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, make producer gas generator 02 self-produced steam first carry out a heat exchange 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 the temperature of 120～220 ℃, as vaporized chemical;
(3) at least one second interchanger, this second interchanger can with the integrated design of fly-ash separator, within being arranged on fly-ash separator, after aforementioned interchanger; Air-cooler 08 Integrated design that also can have with producer gas generator itself, within being arranged on air-cooler 08, or before air-cooler 08, this second interchanger carries out a heat exchange again for the coal gas from lower gas exit that air and above-mentioned warp and steam gasification agent have been carried out to a heat exchange, and this air themperature is promoted to 120～220 ℃, as vaporized chemical;
Further, preferably air is as the heat-exchange working medium of this interchanger or water cooler, if underfed, can assist adopt air even water-cooled be that heat-exchange working medium carries out heat exchange compensation;
(4) preferred but non-essential one in order to control the regulated valve to aforementioned vapor heat exchanger (First Heat Exchanger) and necessary process pipeline from chuck drum 05;
(5) preferred but non-essential one in order to control the regulated valve to mixing tank 04 and necessary process pipeline from aforementioned vapor heat exchanger (First Heat Exchanger);
(6) preferred but non-essential one in order to control the regulated valve to mixing tank 04 and necessary process pipeline from chuck drum 05;
(7) preferred but non-essential one in order to control the regulated valve to gas furnace bottom and necessary process pipeline from mixing tank 04;
(8) preferred but non-essential one in order to control the regulated valve to gas furnace top and necessary process pipeline from mixing tank 04;
(9) 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 invention, detailed process is as follows:
Coal adds producer gas generator 02 by the coal bunker 01 at atmospheric fixed bed gas-producer 02 top, enters gasification layer gasification after coking; Gasification comes from air and the self-produced steam of producer gas generator 02 with vaporized chemical; Wherein, self-produced steam and air successively carry out heat exchange successively with the coal gas that lower gas exit temperature out reaches the temperature of 600 ℃, by temperature increase to 120～220 ℃, using high-temperature steam and high temperature air as vaporized chemical.As shown in Figure 1, in the coal gas of this lower gas exit and stove self-produced steam first at First Heat Exchanger 10 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 ℃, this First Heat Exchanger 10 can with fly-ash separator 06 Integrated design, within being arranged on fly-ash separator 06, also after can being sequentially arranged on fly-ash separator 06, before air-cooler 08; In addition, air and above-mentioned warp carry out a heat exchange with the coal gas from lower gas exit that a heat exchange has been carried out in steam gasification agent again through the second interchanger, and by the temperature of this air-lift unit to 120～220 ℃; This second interchanger can with fly-ash separator 06 Integrated design, within being arranged on fly-ash separator 60, after aforementioned First Heat Exchanger 10; Air-cooler 08 Integrated design that this second interchanger also can itself have with producer gas generator 02, within being arranged on air-cooler 08, or before air-cooler 08.
As accompanying drawing 1,2, air-cooler 08 itself is the equipment that traditional producer gas generator has, when employing is of the present invention, preferably adopt air 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.
Aforementioned high temperature air and high-temperature steam enter producer gas generator 02 by the variable valve arranging respectively after entering furnace bottom mixing tank 04 and mix as vaporized chemical on request, and vaporized chemical, in 02 li of producer gas generator and the coal reduction reaction that gasifies, produces 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 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 present invention or the up air-flow journey processed of continous way, preferably applicable upward and downward type air-flow journey processed;
Vaporized chemical in the uplink and downlink stage is that air is or/and steam.
The oxygen concentration of this air gasification agent is 20.93%, 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.
Air 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 by the temperature of this air-lift unit to 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 air that has carried out heat exchange and steam, form the high-temperature steam vaporized chemical of 120～220 ℃ of the air of 120～220 ℃ of 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 air of above-mentioned heat exchange and steam, formed the high-temperature steam vaporized chemical of 120～220 ℃ of the air of 120～220 ℃ of temperature and temperature, after mixing, mixing tank enters the top of producer gas generator as vaporized chemical.
The present invention has adopted 2 interchanger successively by the temperature of steam in vaporized chemical and preheating of air to 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 has been because formed the air of 120～220 ℃ of temperature and the high-temperature steam vaporized chemical of 120～220 ℃ of temperature, so:
(1) improve the temperature that enters stove oxidation reactant gas, 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 temperature of steam in the boiler, significantly improved steam decomposition rate, thereby increased caloric power of gas;
(3) more fully and completely, coal burning more fully and completely, has reduced ash content carbon in combustion gasification reaction;
(4) increase of 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 5～15%).
Adopt the present invention, avoid adopting oxygen-rich air, with succinct technique, minimum equipment investment, obtained significant energy-saving effect, avoided the cost of investment of breathing equipment and produced the required operation of oxygen enrichment itself, maintenance cost.
Accompanying drawing explanation
Fig. 1 is for adopting the coal gas method for generation and device diagram that high temperature air and high-temperature steam are vaporized chemical.
Fig. 2 is the coal gas method for generation and device 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 gas blower, and 04 is mixing tank, and 05 is chuck drum, and 06 is fly-ash separator, and 07 is electric tar, and 08 is air-cooler, and 09 is scrubber cooler, and 10 is interchanger; V01, V02, V101, V102A, V102B are variable valve.
Embodiment
Different below in conjunction with accompanying drawing with explanation the present invention and prior art; And further describe the present invention.
Fig. 1 is a kind of coal gas generating process and device that high temperature air and high-temperature steam are vaporized chemical that adopt, and mainly following processing unit, consists of:
Fig. 2 is coal gas generating process and the device that traditional employing air and steam are vaporized chemical, and comparative example, is mainly comprised of following processing unit:
As accompanying drawing 2, in traditional technology, the coal gas of lower gas exit is typically about the temperature of 600 ℃, 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 present invention, as accompanying drawing 1, in the coal gas of this lower gas exit and stove, self-produced steam is first 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 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.
As accompanying drawing 2, what in traditional technology, adopt is normal temperature air, and this air directly enters mixing tank as vaporized chemical.In the present invention, employing be that the coal gas from lower gas exit that has carried out a heat exchange with above-mentioned warp and steam gasification agent carries out a heat exchange again, and by the temperature of this air-lift unit to 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.
As accompanying drawing 1,2, air-cooler itself is the equipment that traditional producer gas generator has, when employing is of the present invention, preferably 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.
Above-mentioned twice heat exchange is linked in sequence, and steam heat-exchanging is front, and air heat-exchange is rear, to optimize echelon energy utilization.
As a preferred gas-made technology flow process, in accompanying drawing 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, by-pass valve control has all been installed, V102A, 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 by-pass valve control 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 up-downgoing vaporized chemical that enters producer gas generator 02 from mixing tank 04 in accompanying drawing 1, control valve V01 has preferably been installed, V02, in order to control respectively the vaporized chemical flow that enters Lu Nei bottom or top.
Variable valve 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 accompanying drawing 2, conventionally, traditional atmospheric fixed bed gas-producer, 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 02 supercharging, 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.
As accompanying drawing 1, atmospheric fixed bed gas-producer of the present invention, 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 02, wherein, the coal gas that self-produced steam and 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 air successively as vaporized chemical, as accompanying drawing 1, in the coal gas of this lower gas exit and stove self-produced steam first at heat exchanger 10 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 heat exchanger 10 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, air 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 by the temperature of this air-lift unit to 120～220 ℃, this heat exchanger can with fly-ash separator 06 Integrated design, within being arranged on fly-ash separator, after aforementioned interchanger 10, 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, when employing is of the present invention, preferably 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 air 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 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 workshop section purify after for user.
Priority application of the present invention 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 uplink and downlink activity time, emptied part gas etc.
Adopt producing gas method of the present invention, overcome preferably the technological deficiency of traditional atmospheric fixed bed gas-producer gas processed, improved gas furnace output and caloric power of gas, reduced ash content carbon, reduced sensible heat loss, gas unit consumption has reduced the mark coal that 5～15%(unit calorific value consumes).
Implementation method described above is only set forth key characters more of the present invention, professional and technical personnel will be appreciated that, although the present invention has carried out partly describing by reference to the accompanying drawings, but this is only an application example of the present invention or a kind of method, all other variations of not violating the essence of the present invention's elaboration also belong to category of the present invention, and scope of the present invention is limited by appending claims scope only.
Claims (3)
1. adopting high temperature air and high-temperature steam is a coal gas production method for vaporized chemical, it is characterized in that, adopting temperature is that the high-temperature steam that the air of 120～220 ℃ and temperature are 120～220 ℃ is vaporized chemical producing coal in next life gas.
2. adopting high temperature air and high-temperature steam is a gas producing device for vaporized chemical, comprising:
(1) at least a set of producer gas generator body, and the utility appliance of mating with main body, comprise: coal bunker (01), producer gas generator (02), gas blower (03), mixing tank (04), chuck drum (05), fly-ash separator (06), electric tar (07), air-cooler (08), scrubber cooler (09);
(2) at least one First Heat Exchanger, this first parallel operation and the integrated design of fly-ash separator, within being arranged on fly-ash separator, or after order is arranged on fly-ash separator, before air-cooler, make producer gas generator (02) self-produced steam first carry out a heat exchange 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;
(3) at least one second interchanger, this second interchanger and the integrated design of fly-ash separator, within being arranged on fly-ash separator, after aforementioned First Heat Exchanger; Or the air-cooler that the second interchanger and producer gas generator have (08) Integrated design itself, within being arranged on air-cooler (08), or air-cooler (08) before, this second interchanger carries out a heat exchange again for the coal gas from lower gas exit that air and above-mentioned warp and steam gasification agent have been carried out to a heat exchange, and this air themperature is promoted to 120～220 ℃, as vaporized chemical;
(4) at least one is in order to control regulated valve and the process pipeline to aforementioned First Heat Exchanger from chuck drum (05);
(5) at least one is in order to control from aforementioned First Heat Exchanger regulated valve and the process pipeline to mixing tank (04);
(6) at least one is in order to control from chuck drum (05) regulated valve and the process pipeline to mixing tank (04);
(7) at least one is in order to control from mixing tank (04) regulated valve and the process pipeline to gas furnace bottom;
(8) at least one is in order to control from mixing tank (04) regulated valve and the process pipeline to gas furnace top.
3. the coal gas production method based on gas producing device described in claim 2, is characterized in that detailed process is:
Coal adds producer gas generator (02) by the coal bunker (01) at atmospheric fixed bed gas-producer (02) top, enters gasification layer gasification after coking; Gasification comes from air and the self-produced steam of producer gas generator (02) with vaporized chemical; Wherein:
In the coal gas of the lower gas exit of producer gas generator (02) and stove self-produced steam first at First Heat Exchanger 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 ℃;
Air and above-mentioned warp carry out a heat exchange with the coal gas from lower gas exit that a heat exchange has been carried out in steam gasification agent again through the second interchanger, and by the temperature of this air-lift unit to 120～220 ℃;
Aforementioned high temperature air enters furnace bottom mixing tank (04) with high-temperature steam as vaporized chemical to be mixed, then by the variable valve arranging, enter producer gas generator (02) respectively on request, vaporized chemical producer gas generator (02) inner 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) and air or/and other working medium heat exchange and cooling after, the coke gas after electric tar (07) coming with upper gas exit mixes, then enter after the operation processing of rear workshop section, for user.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310475179.1A CN103509605B (en) | 2013-10-13 | 2013-10-13 | Method and device using high temperature air and high temperature steam as gasification agents for coal gas production |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310475179.1A CN103509605B (en) | 2013-10-13 | 2013-10-13 | Method and device using high temperature air and high temperature steam as gasification agents for coal gas production |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN103509605A true CN103509605A (en) | 2014-01-15 |
| CN103509605B CN103509605B (en) | 2015-01-07 |
Family
ID=49893042
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310475179.1A Active CN103509605B (en) | 2013-10-13 | 2013-10-13 | Method and device using high temperature air and high temperature steam as gasification agents for coal gas production |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103509605B (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104164257A (en) * | 2014-07-31 | 2014-11-26 | 汤广斌 | Fischer-Tropsch reactor pure-oxygen continuous gasification apparatus and gasification technology |
| CN104726135A (en) * | 2015-03-02 | 2015-06-24 | 云南燃二化工有限公司 | Method for improving temperature of primary air of gas producer |
| CN105779007A (en) * | 2016-03-25 | 2016-07-20 | 北京澳柯清洁煤气工程技术有限公司 | Method for gasifying fly ash with waste heat utilization into coal gas |
| CN105927957A (en) * | 2016-06-07 | 2016-09-07 | 广东工业大学 | Biologic particle gasification combustion steam generation integrated 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 |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202610195U (en) * | 2012-06-01 | 2012-12-19 | 中国石油和化工勘察设计协会煤化工设计技术中心 | Device for preparing ammonia synthesis gas through pressurization and continuous gasification of anthracite |
| CN203095994U (en) * | 2013-01-25 | 2013-07-31 | 山东义升环保设备有限公司 | Coal gasification system with high air temperature and high air pressure |
-
2013
- 2013-10-13 CN CN201310475179.1A patent/CN103509605B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202610195U (en) * | 2012-06-01 | 2012-12-19 | 中国石油和化工勘察设计协会煤化工设计技术中心 | Device for preparing ammonia synthesis gas through pressurization and continuous gasification of anthracite |
| CN203095994U (en) * | 2013-01-25 | 2013-07-31 | 山东义升环保设备有限公司 | Coal gasification system with high air temperature and high air pressure |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104164257A (en) * | 2014-07-31 | 2014-11-26 | 汤广斌 | Fischer-Tropsch reactor pure-oxygen continuous gasification apparatus and gasification technology |
| CN104726135A (en) * | 2015-03-02 | 2015-06-24 | 云南燃二化工有限公司 | Method for improving temperature of primary air of gas producer |
| CN105779007A (en) * | 2016-03-25 | 2016-07-20 | 北京澳柯清洁煤气工程技术有限公司 | Method for gasifying fly ash with waste heat utilization into coal gas |
| CN105779007B (en) * | 2016-03-25 | 2019-02-01 | 北京澳柯清洁煤气工程技术有限公司 | The method that the flyash utilized that has surplus heat regasifies into coal gas |
| CN105927957A (en) * | 2016-06-07 | 2016-09-07 | 广东工业大学 | Biologic particle gasification combustion steam generation integrated 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN103509605B (en) | 2015-01-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| EP2799520B1 (en) | Biomass gasification island process under high temperature and atmospheric pressure | |
| RU2604624C2 (en) | Method and device for gasification of biomass by recycling carbon dioxide without oxygen | |
| CN103509605B (en) | Method and device using high temperature air and high temperature steam as gasification agents for coal gas production | |
| CN102851426A (en) | Direct reduction process for producing spongy iron from CH4-rich coal gas | |
| CN102010924B (en) | Method for producing directly reduced iron from coal | |
| CN103525465B (en) | Coal gas production method and device using high-temperature rich oxygen and high temperature steam as gasification agent | |
| CN105779683B (en) | Converter gas recovery system and recovery method | |
| CN101250419B (en) | Low-temperature dry distillation process with coal gas internal heat | |
| CN111187632B (en) | Coal gas quality-divided return internal heating type low-temperature oxygen-enriched coal dry distillation process method and system | |
| CN203530252U (en) | Coal gas production device using high-temperature rich oxygen and high-temperature steam as gasifying agents | |
| CN102620569B (en) | Resource cyclic utilization system of industrial kiln | |
| CN105368498A (en) | Method for preparing water gas through pressurization continuous gasification of static beds | |
| CN102732317A (en) | Technological process for preparing synthetic gas by using biomass | |
| CN102391892B (en) | Blast furnace gas enrichment apparatus and method | |
| CN108865284A (en) | A kind of high-effective gasization and energy utilization system and coal gasification and energy utilizing method | |
| CN104178234B (en) | Coke-stove gas prepares natural gas and residual-heat utilization method and system with producer gas | |
| CN203530251U (en) | Coal gas production device adopting high-temperature air and high-temperature steam as gasifying agent | |
| CN102585905B (en) | Bituminous coal fixed bed continuous gasification method | |
| CN215886917U (en) | Carbon-reducing emission-reducing semi-coke production system | |
| CN114752418A (en) | Coal quality-based utilization system and process for realizing zero carbon emission | |
| CN108728139A (en) | A kind of pyrolysis of coal nitrogen-free process and system | |
| CN107164594A (en) | A kind of BGL gasifying gas produces the system and method for DRI through dual turn over metaplasia | |
| CN205099627U (en) | Fixed bed pressurization continuous gasification system water gas system | |
| CN207632750U (en) | A kind of four sections of heat reclamation type efficient gasification furnaces | |
| CN207002777U (en) | A kind of Lurgi gasifying gas converts the device of production DRI through steam |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CP01 | Change in the name or title of a patent holder |
Address after: 201506 Jinshan District, Jinshan Industrial Zone, Shanghai Road, Lane No. 285, No. 5 Patentee after: Shanghai Sui Hua Industrial Limited by Share Ltd Address before: 201506 Jinshan District, Jinshan Industrial Zone, Shanghai Road, Lane No. 285, No. 5 Patentee before: Shanghai Huishan Industrial Co., Ltd. |
|
| CP01 | Change in the name or title of a patent holder |