CN104910986A - Device and process for preparing natural gas by virtue of double-fluidization bed gasification of biomass - Google Patents
Device and process for preparing natural gas by virtue of double-fluidization bed gasification of biomass Download PDFInfo
- Publication number
- CN104910986A CN104910986A CN201510346119.9A CN201510346119A CN104910986A CN 104910986 A CN104910986 A CN 104910986A CN 201510346119 A CN201510346119 A CN 201510346119A CN 104910986 A CN104910986 A CN 104910986A
- Authority
- CN
- China
- Prior art keywords
- gas
- charcoal
- carrier
- biomass
- bed
- 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
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
-
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention provides a device and a process for preparing natural gas by virtue of double-fluidization bed gasification of a biomass. The device comprises a burning carrier heating unit, a pyrolysis gasification unit, a biological carbon/carrier separation and conveying unit and a methane synthesis and tar returning unit, wherein the pyrolysis gasification unit is connected with the burning carrier heating unit, the biological carbon/carrier separation and conveying unit and the methane synthesis and tar returning unit. The other components are converted into methane gas as much as possible while the biological carbon is obtained, the content of methane in a pyrolysis product is about 10%, the pressure for subsequent synthesis is reduced, the tar in hydrolysis gas is used as a fuel for a double-fluidization bed, and the problems that combustion cannot be stabilized at a low temperature and alkali metals causes scorification in a high-temperature state when other double-fluidization beds adopt biological carbon combustion can be avoided to ensure that the temperature of a combustion furnace can be controlled very flexibly. The device and the process provided by the invention fully use different pyrolysis products of the biomass, can realize treatment of various biomasses, and are wide in raw material application range.
Description
Technical field
The present invention relates to biogas technicalization field, be specially a kind of biomass double fluidized-bed vaporizing system gas plant and technique.
Background technology
China has the huge agricultural-forestry biomass resource of reserves, utilizes chemical effects analysis of biomass gasification for liquid fuel synthesis to substitute day by day exhausted fossil oil and has market outlook widely.Gasifying biomass is the transformation technology of a high-efficiency cleaning, effect by means of the vaporized chemical conversion of biomass is obtained combustion gas that principal combustible components is CO, H2, CO2 and CH4 or synthetic gas, gasification technology and subsequent technique coupling can be used for generating electricity, heat supply or synthesis of chemicals.Gasifying biomass can by bulky, energy density is low, nonflammable or that efficiency of combustion is low biomass material be converted into energy density higher, be suitable for storing, transport and the Sweet natural gas used or other gas or liquid fuel, improve energy utilization quality and utilising efficiency, that has widened biomass energy utilizes scope simultaneously.
Gasifying biomass Poly-generation technology is by volatile matter and fixed carbon feature dimerous based on biomass combustibleconstituents, adopt decoupling zero reactive mode, fixed carbon transforms into high-quality biological charcoal, volatile matter transforms into combustion gas or synthetic gas, and then generates heat energy, electric energy or comprise the chemicals of Sweet natural gas.The wooden class raw material of bamboo obtains bamboo charcoal and deep processing becomes gac; Rice husk class raw material to obtain after rice hull carbon for steel mill's lagging material or carries out deep processing and obtain gac and nano-scale silicon crystals; Stalk raw materials obtains straw charcoal and then makes high added value charcoal base composite fertilizer, and after Different treatments, charcoal all can realize high value applications.
The present situation of China's natural gas resource growing tension and environmental stress active demand utilize biomass to develop the green natural gas of sustainable supply in interior renewable energy source, economic benefit is good simultaneously, adapts to this demand and obtain development based on biomass double fluidized-bed gasifying biomass synthetic natural gas technology.Biomass double fluidized-bed vapourizing furnace is made up of burning bed and gasifier bed two portions, is coupled by two beds by high-temp solid thermal barrier.Owing to not adding air in gasifier bed, avoid the dilution of a large amount of nitrogen to combustion gas, thus obtain high-quality synthetic gas, simultaneously co-producing bio charcoal.Because pyrolytic reaction is principal reaction, in synthetic gas, methane content is up to more than 10%, is conducive to follow-up synthesizing section.The mode of being conducted heat to pyrolytic gasification stove by thermal barrier owing to adopting roasting kiln in double-fluidized-bed gasification technology, the temperature of roasting kiln needs higher than pyrolytic gasification stove, and current double fluidized bed combustion stove burning adopts charcoal (semicoke) as roasting kiln fuel, and charcoal kindling temperature is at about 700 DEG C, this just requires that the temperature of roasting kiln can not lower than 700 DEG C, and a lot of high alkalinity biomass material (straw, straw etc.) ash fusion point also at about 700 DEG C, when therefore adopting high alkalinity biomass material, traditional double-fluidized-bed mode cannot be run, raw material can only be limited to wooden, the high ash melting point biomass such as rice husk, therefore the double-fluidized-bed technology that exploitation adaptability to raw material is wide is badly in need of, make it to be widely used in grain husk, wood working offal, the utilization of waste material of papermaking waste material and various agricultural crop straw and process, as save energy, protection of the environment, reduce production cost, the effective means of increasing the benefit.
Summary of the invention
Technical problem solved by the invention is to provide a kind of biomass double fluidized-bed vaporizing system gas plant and technique, to solve the problem in above-mentioned background technology.
Technical problem solved by the invention realizes by the following technical solutions: a kind of biomass double fluidized-bed vaporizing system gas plant, comprise: combustion carrier heating unit, pyrolytic gasification unit, charcoal/carrier is separated and supply unit, methane synthesis and tar loopback cell, shown pyrolytic gasification unit connects combustion carrier heating unit, charcoal/carrier is separated and supply unit, methane synthesis and tar loopback cell, described combustion carrier heating unit comprises fluid-bed combustion furnace, flue gas whirlwind, material returning device one, vapour generator, air preheater and gas blower, described pyrolytic gasification unit comprises fluidized bed pyrolysis vapourizing furnace, gas cyclone, biomass feeding device and material returning device two, described charcoal/carrier is separated and supply unit comprises charcoal refrigerated separation stove, charcoal whirlwind and carrier vent pipe and carrier e Foerderanlage, the synthesis of described methane and tar loopback cell comprise gas-purification purifying plant and methane synthesis device and tar transferpump.
Described fluidized-bed combustion furnace upper end side connects flue gas whirlwind, flue gas whirlwind lower end connects material returning device one, upper end is connected to vapour generator, air preheater is provided with on the downside of vapour generator, air preheater is connected to the bottom of fluid-bed combustion furnace, material returning device one is connected to fluidized bed pyrolysis vapourizing furnace, fluidized bed pyrolysis vapourizing furnace side is provided with biomass feeding device, side, fluidized bed pyrolysis vapourizing furnace upper end is provided with gas cyclone, gas cyclone upper end is connected to gas-purification purifying plant, lower end is connected to material returning device two, material returning device two is connected to charcoal refrigerated separation stove, charcoal refrigerated separation furnace upper end side is provided with charcoal whirlwind, charcoal refrigerated separation stove lower end is provided with carrier vent pipe, carrier vent pipe side is connected to fluid-bed combustion furnace by carrier e Foerderanlage, described gas-purification purifying plant is connected to fluid-bed combustion furnace by pipeline, carrier e Foerderanlage, gas-purification purifying plant is connected with methane synthesis device.
Described air preheater side is provided with gas blower.
A kind of biomass double fluidized-bed vaporizing system natural gas process, comprises the following steps:
Step (1) adds biomass material by biomass feeding device in fluidized bed pyrolysis vapourizing furnace, biomass material carried by fluid-bed combustion furnace the high-temperature heat carrier heating state of coming issue raw pyrolytic gasification reaction, the high-temperature hot generated containing tar is vented one's spleen and charcoal, charcoal and thermal barrier are carried by pyrolysis gas and enter gas cyclone and realize gas solid separation, pyrolysis gas enters gas-purification purifying plant, and charcoal and thermal barrier enter charcoal refrigerated separation stove by material returning device two;
Step (2) is vented one's spleen containing the high-temperature hot of tar and remove tar, moisture, dust and carbonic acid gas in gas-purification purifying plant, synthetic gas is obtained after pyrolysis gas purification, synthetic gas main component is carbon monoxide, hydrogen, methane and polymer hydro carbons, and synthetic gas enters methane synthesis device and synthesizes Sweet natural gas;
The tar that step (3) gas-purification purifying plant obtains sends into efficient burning in fluid-bed combustion furnace through tar transferpump, the heat produced is mainly used in heat hot carrier, the high-temperature flue gas produced carries high-temperature heat carrier and enters flue gas whirlwind, after gas solid separation, flue gas is discharged after vapour generator and air preheater, and high-temperature heat carrier enters fluidized bed pyrolysis vapourizing furnace through material returning device one;
The steam that step (4) steam evaporator produces is sent to fluidized bed pyrolysis vapourizing furnace as fluidizing medium and participates in gasification reaction, air through air preheater laggard enter fluid-bed combustion furnace realize the high velocity fluidization of thermal barrier as tar combustion air;
The carbonic acid gas that step (5) gas-purification purifying plant obtains sends into the cooling realizing charcoal in charcoal refrigerated separation stove, density difference is utilized to realize being separated of thermal barrier and charcoal, cooled charcoal is carried by carbon dioxide and enters charcoal whirlwind, obtains charcoal after gas solid separation;
Step (6) thermal barrier flows into carrier e Foerderanlage through carrier vent pipe, under the air conveying effect of carbon dioxide, enter fluid-bed combustion furnace.
The water content of described biomass material is 0-50%, and biomass are of a size of 0-10cm.
Described fluid-bed combustion furnace in-furnace temperature is 600 ~ 1000 DEG C, and fluidized bed pyrolysis gasification in-furnace temperature is 500 ~ 950 DEG C, and charcoal refrigerated separation furnace temperature is 200 ~ 400 DEG C.
Described thermal barrier is that abrasion resistant particles comprises river sand, quartz sand, alumina balls, Ceramic Balls, and particle diameter is 0.2 ~ 2mm.
Compared with public technology, there is following advantage in the present invention: the present invention obtains charcoal and realizes all the other compositions simultaneously and transform into methane gas as far as possible, in pyrolysis product, methane content is about 10%, decrease the pressure of follow-up synthesis, use as double-fluidized-bed fuel after the tar in pyrolysis gas is collected, can avoid occurring during other double-fluidized-bed employing charcoal burning low temperature cannot stable burning and under the condition of high temperature basic metal cause clogging problems, furnace temperature is controlled very flexible, the present invention takes full advantage of the different pyrolysis products of biomass, multiple biomass processes can be achieved, raw material wide accommodation.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
In figure: 1, fluid-bed combustion furnace, 2, flue gas whirlwind, 3, material returning device one, 4, gas cyclone, 5, fluidized bed pyrolysis vapourizing furnace, 6, biomass feeding device, 7, gas-purification purifying plant, 8, methane synthesis device, 9, charcoal whirlwind, 10, charcoal refrigerated separation stove, 11, tar transferpump, 12, carrier vent pipe, 13, carrier e Foerderanlage, 14, material returning device two, 15, gas blower, 16, air preheater, 17, vapour generator.
Embodiment
Object is reached and effect is easy to understand in order to make technique means of the present invention, creation characteristic, workflow, using method, below in conjunction with the embodiment of the present invention, technical scheme in the embodiment of the present invention is clearly and completely described, obviously, described embodiment is only the present invention's part embodiment, instead of whole embodiments.Based on the embodiment in the present invention, those of ordinary skill in the art, not making the every other embodiment obtained under creative work prerequisite, belong to the scope of protection of the invention.
As shown in Figure 1, a kind of biomass double fluidized-bed vaporizing system gas plant, comprise: combustion carrier heating unit, pyrolytic gasification unit, charcoal/carrier is separated and supply unit, methane synthesis and tar loopback cell, shown pyrolytic gasification unit connects combustion carrier heating unit, charcoal/carrier is separated and supply unit, methane synthesis and tar loopback cell, described combustion carrier heating unit comprises fluid-bed combustion furnace 1, flue gas whirlwind 2, material returning device 1, vapour generator 17, air preheater 16 and gas blower 15, described pyrolytic gasification unit comprises fluidized bed pyrolysis vapourizing furnace 5, gas cyclone 4, biomass feeding device 6 and material returning device 2 14, described charcoal/carrier is separated and supply unit comprises charcoal refrigerated separation stove 10, charcoal whirlwind 9 and carrier vent pipe 12 and carrier e Foerderanlage 13, the synthesis of described methane and tar loopback cell comprise gas-purification purifying plant 7 and methane synthesis device 8 and tar transferpump 11.
Side, described fluid-bed combustion furnace 1 upper end connects flue gas whirlwind 2, flue gas whirlwind 2 lower end connects material returning device 1, upper end is connected to vapour generator 17, air preheater 16 is provided with on the downside of vapour generator 17, air preheater 16 is connected to the bottom of fluid-bed combustion furnace 1, material returning device 1 is connected to fluidized bed pyrolysis vapourizing furnace 5, fluidized bed pyrolysis vapourizing furnace 5 side is provided with biomass feeding device 6, side, fluidized bed pyrolysis vapourizing furnace 5 upper end is provided with gas cyclone 4, gas cyclone 4 upper end is connected to gas-purification purifying plant 7, lower end is connected to material returning device 2 14, material returning device 2 14 is connected to charcoal refrigerated separation stove 10, side, charcoal refrigerated separation stove 10 upper end is provided with charcoal whirlwind 9, charcoal refrigerated separation stove 10 lower end is provided with carrier vent pipe 12, carrier vent pipe 12 side is connected to fluid-bed combustion furnace 1 by carrier e Foerderanlage 13.
Described gas-purification purifying plant 7 is connected to fluid-bed combustion furnace 1, carrier e Foerderanlage 13 by pipeline, gas-purification purifying plant 7 is connected with methane synthesis device 8.
Described air preheater 16 side is provided with gas blower 15.
A kind of biomass double fluidized-bed vaporizing system natural gas process, comprises the following steps:
Step (1) adds biomass material by biomass feeding device 6 in fluidized bed pyrolysis vapourizing furnace 5, biomass material carried by fluid-bed combustion furnace 1 the high-temperature heat carrier heating state of coming issue raw pyrolytic gasification reaction, the high-temperature hot generated containing certain tar content is vented one's spleen and charcoal, charcoal and thermal barrier are carried by pyrolysis gas and enter gas cyclone 4 and realize gas solid separation, pyrolysis gas enters gas-purification purifying plant 7, and charcoal and thermal barrier enter charcoal refrigerated separation stove 10 by material returning device 2 14;
Step (2) is vented one's spleen containing the high-temperature hot of tar and remove tar, moisture, dust and carbonic acid gas in gas-purification purifying plant 7, synthetic gas is obtained after pyrolysis gas purification, synthetic gas main component is carbon monoxide, hydrogen, methane and a small amount of polymer hydro carbons, and synthetic gas enters methane synthesis device 8 and synthesizes Sweet natural gas;
The tar that step (3) gas-purification purifying plant 7 obtains sends into efficient burning in fluid-bed combustion furnace 1 through tar transferpump 11, the heat produced is mainly used in heat hot carrier, the high-temperature flue gas produced carries high-temperature heat carrier and enters flue gas whirlwind 2, after gas solid separation, flue gas is discharged after vapour generator 17 and air preheater 16, and high-temperature heat carrier enters fluidized bed pyrolysis vapourizing furnace 5 through material returning device 1;
The steam that step (4) steam evaporator 17 produces is sent to fluidized bed pyrolysis vapourizing furnace 5 as fluidizing medium and participates in gasification reaction, air through air preheater 16 laggard enter fluid-bed combustion furnace 1 realize the high velocity fluidization of thermal barrier as tar combustion air;
The carbonic acid gas that step (5) gas-purification purifying plant 7 obtains sends into the cooling realizing charcoal in charcoal refrigerated separation stove 10, density difference is utilized to realize being separated of thermal barrier and charcoal, cooled charcoal is carried by carbon dioxide and enters charcoal whirlwind 9, obtains charcoal after gas solid separation.
Step (6) thermal barrier flows into carrier e Foerderanlage 13 through carrier vent pipe 12, under the air conveying effect of carbon dioxide, enter fluid-bed combustion furnace 1.
The water content of described biomass material is not higher than 50%, and biomass size is not more than 10cm.
Described fluid-bed combustion furnace in-furnace temperature is 600 ~ 1000 DEG C, and in fluidized bed pyrolysis vapourizing furnace 5, temperature is 500 ~ 950 DEG C, and charcoal refrigerated separation stove 10 temperature is 200 ~ 400 DEG C.
Described thermal barrier is abrasion resistant particles, comprises river sand, quartz sand, alumina balls, Ceramic Balls, and particle diameter is 0.2 ~ 2mm.
Embodiment 1
By water ratio 18%, particle diameter is that 5mm wood chip adds in fluidized bed pyrolysis vapourizing furnace 5 by feeding device 6, raw material carried by fluid-bed combustion furnace 1 893 DEG C of high-temperature heat carrier 0.5mm quartz sand heating states of coming issue raw pyrolytic gasification reaction, temperature 835 DEG C in fluidized bed pyrolysis vapourizing furnace 5, the high-temperature hot generating tar content 7% is vented one's spleen and charcoal, charcoal and thermal barrier are carried by pyrolysis gas and enter gas cyclone 4 and realize gas solid separation, pyrolysis gas enters gas-purification purifying plant 7, charcoal and thermal barrier enter charcoal refrigerated separation stove 10 by material returning device 2 14, charcoal refrigerated separation stove 10 temperature is 350 DEG C, high-temperature hot containing tar is vented one's spleen and remove tar, moisture, dust and carbonic acid gas in gas-purification purifying plant 7, and obtain synthetic gas after pyrolysis gas purification, synthetic gas enters methane synthesis device 8 and synthesizes Sweet natural gas, methane content 95%, the tar that gas purification device 7 obtains sends into efficient burning in fluid-bed combustion furnace 1 through tar transferpump 11, burning in-furnace temperature 950 DEG C, the heat produced is mainly used in heat hot carrier, the high-temperature flue gas produced carries high-temperature heat carrier and enters flue gas whirlwind 2, after gas solid separation, flue gas is discharged after vapour generator 17 and air preheater 16, and high-temperature heat carrier enters fluidized bed pyrolysis vapourizing furnace 5 through material returning device 1, the steam 450 DEG C that steam evaporator 17 produces is sent to fluidized bed pyrolysis vapourizing furnace 5 as fluidizing medium and participates in gasification reaction, air through air preheater 16 be preheating to 433 DEG C laggard enter fluid-bed combustion furnace 1 realize the high velocity fluidization of thermal barrier as tar combustion air, the carbonic acid gas that gas-purification purifying plant 7 obtains sends into the cooling realizing charcoal in charcoal refrigerated separation stove 10, density difference is utilized to realize being separated of thermal barrier and charcoal, the charcoal being cooled to 75 DEG C is carried by carbon dioxide and enters charcoal whirlwind 9, charcoal is obtained, biomass charcoal carbon content 81% after gas solid separation.
Embodiment 2
By water ratio 35%, particle diameter is that 2mm bamboo bits add in fluidized bed pyrolysis vapourizing furnace 5 by feeding device 6, raw material carried by fluid-bed combustion furnace 1 845 DEG C of high-temperature heat carrier 2mm Ceramic Balls heating states of coming issue raw pyrolytic gasification reaction, temperature 775 DEG C in fluidized bed pyrolysis vapourizing furnace 5, the high-temperature hot generating tar content 5% is vented one's spleen and charcoal, charcoal and thermal barrier are carried by pyrolysis gas and enter gas cyclone 4 and realize gas solid separation, pyrolysis gas enters gas-purification purifying plant 7, charcoal and thermal barrier enter charcoal refrigerated separation stove 10 by material returning device 2 14, charcoal refrigerated separation stove 10 temperature is 310 DEG C, high-temperature hot containing tar is vented one's spleen and remove tar, moisture, dust and carbonic acid gas in gas-purification purifying plant 7, and obtain synthetic gas after pyrolysis gas purification, synthetic gas enters methane synthesis device 8 and synthesizes Sweet natural gas, methane content 95%, the tar that gas purification device 7 obtains sends into efficient burning in fluid-bed combustion furnace 1 through tar transferpump 11, burning in-furnace temperature 894 DEG C, the heat produced is mainly used in heat hot carrier, the high-temperature flue gas produced carries high-temperature heat carrier and enters flue gas whirlwind 2, after gas solid separation, flue gas is discharged after vapour generator 17 and air preheater 16, and high-temperature heat carrier enters fluidized bed pyrolysis vapourizing furnace 5 through material returning device 1, the steam 450 DEG C that steam evaporator 17 produces is sent to fluidized bed pyrolysis vapourizing furnace 5 as fluidizing medium and participates in gasification reaction, air through air preheater 16 be preheating to 370 DEG C laggard enter fluid-bed combustion furnace 1 realize the high velocity fluidization of thermal barrier as tar combustion air, the carbonic acid gas that gas-purification purifying plant 7 obtains sends into the cooling realizing charcoal in charcoal refrigerated separation stove 10, density difference is utilized to realize being separated of thermal barrier and charcoal, the charcoal being cooled to 73 DEG C is carried by carbon dioxide and enters charcoal whirlwind 9, charcoal is obtained, biomass charcoal carbon content 80.3% after gas solid separation.
Embodiment 3
By water ratio 42%, particle length is that 10mm stalk adds in fluidized bed pyrolysis vapourizing furnace 5 by feeding device 6, raw material carried by fluid-bed combustion furnace 1 591 DEG C of high-temperature heat carrier 1mm alumina balls heating states of coming issue raw pyrolytic gasification reaction, temperature 540 DEG C in fluidized bed pyrolysis vapourizing furnace 5, the high-temperature hot generating tar content 6% is vented one's spleen and charcoal, charcoal and thermal barrier are carried by pyrolysis gas and enter gas cyclone 4 and realize gas solid separation, pyrolysis gas enters gas-purification purifying plant 7, charcoal and thermal barrier enter charcoal refrigerated separation stove 10 by material returning device 2 14, charcoal refrigerated separation stove 10 temperature is 240 DEG C, high-temperature hot containing tar is vented one's spleen and remove tar, moisture, dust and carbonic acid gas in gas-purification purifying plant 7, and obtain synthetic gas after pyrolysis gas purification, synthetic gas enters methane synthesis device 8 and synthesizes Sweet natural gas, methane content 95%, the tar that gas purification device 7 obtains sends into efficient burning in fluid-bed combustion furnace 1 through tar transferpump 11, burning in-furnace temperature 665 DEG C, the heat produced is mainly used in heat hot carrier, the high-temperature flue gas produced carries high-temperature heat carrier and enters flue gas whirlwind 2, after gas solid separation, flue gas is discharged after vapour generator 17 and air preheater 16, and high-temperature heat carrier enters fluidized bed pyrolysis vapourizing furnace 5 through material returning device 1, the steam 450 DEG C that steam evaporator 17 produces is sent to fluidized bed pyrolysis vapourizing furnace 5 as fluidizing medium and participates in gasification reaction, air through air preheater 16 be preheating to 310 DEG C laggard enter fluid-bed combustion furnace 1 realize the high velocity fluidization of thermal barrier as tar combustion air, the carbonic acid gas that gas-purification purifying plant 7 obtains sends into the cooling realizing charcoal in charcoal refrigerated separation stove 10, density difference is utilized to realize being separated of thermal barrier and charcoal, the charcoal being cooled to 68 DEG C is carried by carbon dioxide and enters charcoal whirlwind 9, charcoal is obtained, biomass charcoal carbon content 45% after gas solid separation.
Principle of work of the present invention is:
Biomass issue raw pyrolytic reaction at heating state, and its reaction equation is: biomass=CO
2+ CO+CH
4+ C
2above gas+H
2+ charcoal+tar
The present invention obtains charcoal and realizes all the other compositions simultaneously and transform into methane gas as far as possible, and in pyrolysis product, methane content is about 10%, decreases the pressure of follow-up synthesis, CO and H
2as the unstripped gas of synthesizing methane, C
2above gas volume seldom and can improve the calorific value of Sweet natural gas, therefore CO, CH
4, C
2above gas and H
2be available gas and can be used for follow-up synthesis.The calorific value of the tar in pyrolysis product is very high and be difficult to use as chemical products when a small amount of generation, therefore this part is used as double-fluidized-bed fuel, can avoid occurring during other double-fluidized-bed employing charcoal burning low temperature cannot stable burning and under the condition of high temperature basic metal cause clogging problems, furnace temperature is controlled very flexible.Carbonic acid gas in pyrolysis gas is in temperature lower than when 1000 DEG C being rare gas element, and the cooling for charcoal can realize the resume combustion that temperature reduces and avoids charcoal.The present invention takes full advantage of the different pyrolysis products of biomass, can achieve multiple biomass (comprising high bases) process, raw material wide accommodation.
More than show and describe ultimate principle of the present invention, principal character and advantage of the present invention.The technician of the industry should understand; the present invention is not restricted to the described embodiments; what describe in above-described embodiment and specification sheets just illustrates principle of the present invention; without departing from the spirit and scope of the present invention; the present invention also has various changes and modifications, and these changes and improvements all fall in the claimed scope of the invention.Claimed scope of the present invention is defined by appending claims and equivalent thereof.
Claims (7)
1. a biomass double fluidized-bed vaporizing system gas plant, it is characterized in that: comprising: combustion carrier heating unit, pyrolytic gasification unit, charcoal/carrier is separated and supply unit, methane synthesis and tar loopback cell, shown pyrolytic gasification unit connects combustion carrier heating unit, charcoal/carrier is separated and supply unit, methane synthesis and tar loopback cell, described combustion carrier heating unit comprises fluid-bed combustion furnace, flue gas whirlwind, material returning device one, vapour generator, air preheater and gas blower, described pyrolytic gasification unit comprises fluidized bed pyrolysis vapourizing furnace, gas cyclone, biomass feeding device and material returning device two, described charcoal/carrier is separated and supply unit comprises charcoal refrigerated separation stove, charcoal whirlwind and carrier vent pipe and carrier e Foerderanlage, the synthesis of described methane and tar loopback cell comprise gas-purification purifying plant and methane synthesis device and tar transferpump.
2. the biomass double fluidized-bed vaporizing system gas plant of one according to claim 1, it is characterized in that: described fluidized-bed combustion furnace upper end side connects flue gas whirlwind, flue gas whirlwind lower end connects material returning device one, upper end is connected to vapour generator, air preheater is provided with on the downside of vapour generator, air preheater is connected to the bottom of fluid-bed combustion furnace, material returning device one is connected to fluidized bed pyrolysis vapourizing furnace, fluidized bed pyrolysis vapourizing furnace side is provided with biomass feeding device, side, fluidized bed pyrolysis vapourizing furnace upper end is provided with gas cyclone, gas cyclone upper end is connected to gas-purification purifying plant, lower end is connected to material returning device two, material returning device two is connected to charcoal refrigerated separation stove, charcoal refrigerated separation furnace upper end side is provided with charcoal whirlwind, charcoal refrigerated separation stove lower end is provided with carrier vent pipe, carrier vent pipe side is connected to fluid-bed combustion furnace by carrier e Foerderanlage, described gas-purification purifying plant is connected to fluid-bed combustion furnace by pipeline, carrier e Foerderanlage, gas-purification purifying plant is connected with methane synthesis device.
3. the biomass double fluidized-bed vaporizing system gas plant of one according to claim 2, is characterized in that: described air preheater side is provided with gas blower.
4. a biomass double fluidized-bed vaporizing system natural gas process, comprises the following steps:
Step (1) adds biomass material by biomass feeding device in fluidized bed pyrolysis vapourizing furnace, biomass material carried by fluid-bed combustion furnace the high-temperature heat carrier heating state of coming issue raw pyrolytic gasification reaction, the high-temperature hot generated containing tar is vented one's spleen and charcoal, charcoal and thermal barrier are carried by pyrolysis gas and enter gas cyclone and realize gas solid separation, pyrolysis gas enters gas-purification purifying plant, and charcoal and thermal barrier enter charcoal refrigerated separation stove by material returning device two;
Step (2) is vented one's spleen containing the high-temperature hot of tar and remove tar, moisture, dust and carbonic acid gas in gas-purification purifying plant, synthetic gas is obtained after pyrolysis gas purification, synthetic gas main component is carbon monoxide, hydrogen, methane and polymer hydro carbons, and synthetic gas enters methane synthesis device and synthesizes Sweet natural gas;
The tar that step (3) gas-purification purifying plant obtains sends into efficient burning in fluid-bed combustion furnace through tar transferpump, the heat produced is mainly used in heat hot carrier, the high-temperature flue gas produced carries high-temperature heat carrier and enters flue gas whirlwind, after gas solid separation, flue gas is discharged after vapour generator and air preheater, and high-temperature heat carrier enters fluidized bed pyrolysis vapourizing furnace through material returning device one;
The steam that step (4) steam evaporator produces is sent to fluidized bed pyrolysis vapourizing furnace as fluidizing medium and participates in gasification reaction, air through air preheater laggard enter fluid-bed combustion furnace realize the high velocity fluidization of thermal barrier as tar combustion air;
The carbonic acid gas that step (5) gas-purification purifying plant obtains sends into the cooling realizing charcoal in charcoal refrigerated separation stove, density difference is utilized to realize being separated of thermal barrier and charcoal, cooled charcoal is carried by carbon dioxide and enters charcoal whirlwind, obtains charcoal after gas solid separation;
Step (6) thermal barrier flows into carrier e Foerderanlage through carrier vent pipe, under the air conveying effect of carbon dioxide, enter fluid-bed combustion furnace.
5. the biomass double fluidized-bed vaporizing system natural gas process of one according to claim 4, is characterized in that: the water content of described biomass material is 0-50%, and biomass are of a size of 0-10cm.
6. the biomass double fluidized-bed vaporizing system natural gas process of one according to claim 4, it is characterized in that: described fluid-bed combustion furnace in-furnace temperature is 600 ~ 1000 DEG C, fluidized bed pyrolysis gasification in-furnace temperature is 500 ~ 950 DEG C, and charcoal refrigerated separation furnace temperature is 200 ~ 400 DEG C.
7. the biomass double fluidized-bed vaporizing system natural gas process of one according to claim 4, is characterized in that: described thermal barrier is that abrasion resistant particles comprises river sand, quartz sand, alumina balls, Ceramic Balls, and particle diameter is 0.2 ~ 2mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510346119.9A CN104910986B (en) | 2015-06-19 | 2015-06-19 | A kind of biomass double fluidized-bed vaporizing system gas plant and technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510346119.9A CN104910986B (en) | 2015-06-19 | 2015-06-19 | A kind of biomass double fluidized-bed vaporizing system gas plant and technique |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN104910986A true CN104910986A (en) | 2015-09-16 |
| CN104910986B CN104910986B (en) | 2017-01-04 |
Family
ID=54080437
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510346119.9A Active CN104910986B (en) | 2015-06-19 | 2015-06-19 | A kind of biomass double fluidized-bed vaporizing system gas plant and technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104910986B (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106675573A (en) * | 2017-01-10 | 2017-05-17 | 刘继强 | Waterproof and breathable powdered carbon and preparation method thereof |
| CN108264937A (en) * | 2017-12-21 | 2018-07-10 | 北京交通大学 | A kind of double-fluidized-bed reaction system |
| CN109456802A (en) * | 2018-11-29 | 2019-03-12 | 长沙凯天工研院环保服务有限公司 | Biomass double fluidized-bed gas making device |
| CN109652151A (en) * | 2017-10-12 | 2019-04-19 | 中国石油化工股份有限公司 | The device and method of double bubbling bed catalytic coal gasifaction methane |
| TWI659096B (en) * | 2018-06-05 | 2019-05-11 | 國立成功大學 | Dual fluidized-bed gasification system |
| CN109945557A (en) * | 2019-03-23 | 2019-06-28 | 安徽晋煤中能化工股份有限公司 | A kind of refrigeration system and technique based on biomass energy |
| CN115261037A (en) * | 2022-07-12 | 2022-11-01 | 江苏爱园健康科技有限公司 | Heating production equipment and processing method of mineral-based biochar |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4084545A (en) * | 1975-10-21 | 1978-04-18 | Battelle Development Corporation | Operating method |
| EP2302016A2 (en) * | 2000-12-21 | 2011-03-30 | Rentech, Inc. | Biomass gasification system and method |
| CN204874433U (en) * | 2015-06-19 | 2015-12-16 | 合肥德博生物能源科技有限公司 | Two fluidized bed gasifica tion system natural gas devices of living beings |
-
2015
- 2015-06-19 CN CN201510346119.9A patent/CN104910986B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4084545A (en) * | 1975-10-21 | 1978-04-18 | Battelle Development Corporation | Operating method |
| EP2302016A2 (en) * | 2000-12-21 | 2011-03-30 | Rentech, Inc. | Biomass gasification system and method |
| CN204874433U (en) * | 2015-06-19 | 2015-12-16 | 合肥德博生物能源科技有限公司 | Two fluidized bed gasifica tion system natural gas devices of living beings |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106675573A (en) * | 2017-01-10 | 2017-05-17 | 刘继强 | Waterproof and breathable powdered carbon and preparation method thereof |
| CN109652151A (en) * | 2017-10-12 | 2019-04-19 | 中国石油化工股份有限公司 | The device and method of double bubbling bed catalytic coal gasifaction methane |
| CN109652151B (en) * | 2017-10-12 | 2020-07-03 | 中国石油化工股份有限公司 | Device and method for preparing methane by catalytic gasification of coal with double bubbling beds |
| CN108264937A (en) * | 2017-12-21 | 2018-07-10 | 北京交通大学 | A kind of double-fluidized-bed reaction system |
| TWI659096B (en) * | 2018-06-05 | 2019-05-11 | 國立成功大學 | Dual fluidized-bed gasification system |
| CN109456802A (en) * | 2018-11-29 | 2019-03-12 | 长沙凯天工研院环保服务有限公司 | Biomass double fluidized-bed gas making device |
| CN109945557A (en) * | 2019-03-23 | 2019-06-28 | 安徽晋煤中能化工股份有限公司 | A kind of refrigeration system and technique based on biomass energy |
| CN109945557B (en) * | 2019-03-23 | 2020-11-20 | 安徽晋煤中能化工股份有限公司 | Biomass energy-based refrigeration system and process |
| CN115261037A (en) * | 2022-07-12 | 2022-11-01 | 江苏爱园健康科技有限公司 | Heating production equipment and processing method of mineral-based biochar |
| CN115261037B (en) * | 2022-07-12 | 2023-09-12 | 江苏爱园健康科技有限公司 | Heating production equipment and processing method of mineral-based biochar |
Also Published As
| Publication number | Publication date |
|---|---|
| CN104910986B (en) | 2017-01-04 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN104910986B (en) | A kind of biomass double fluidized-bed vaporizing system gas plant and technique | |
| EP2551332B1 (en) | Process and system for producing synthesis gas from biomass by carbonization | |
| JP5753253B2 (en) | Method and system for producing synthesis gas from biomass by pyrolysis | |
| US8328887B2 (en) | Method and system for producing synthetic gas from biomass by high temperature gasification | |
| AU2011282097B2 (en) | Method and apparatus for biomass pyrolysis gasification via two interconnected furnaces | |
| US8361348B2 (en) | Method and system for producing synthetic gas from biomass by high temperature gasification | |
| CN104830377B (en) | The combustion and segmented inverting biological charcoal/steam co-producing technology of biomass pyrogenation gasification | |
| US20110035990A1 (en) | Method and device for converting carbonaceous raw materials | |
| CN101100621A (en) | Method and device for preparing biomass hydrogen-rich combustion gas | |
| CN102786994A (en) | Method for preparing methane-rich gas through autocatalytic gasification of biomass | |
| CN103930523A (en) | Process for the thermochemical conversion of a carbon-based feedstock to synthesis gas containing predominantly H2 and CO | |
| US8431044B2 (en) | Method and system for producing synthetic gas from biomass by high temperature gasification | |
| US8632615B2 (en) | Method and system for producing synthetic gas from biomass by high temperature gasification | |
| CN204874433U (en) | Two fluidized bed gasifica tion system natural gas devices of living beings | |
| Meng et al. | Influence of higher equivalence ratio on the biomass oxygen gasification in a pilot scale fixed bed gasifier | |
| CN204607939U (en) | The combustion and segmented inverting biological charcoal/steam co-producing device of biomass pyrogenation gasification | |
| CN110848665B (en) | Steam/carbon combined production process based on biomass pyrolysis gasification and combustion and application thereof | |
| CN203096004U (en) | Power generation system based on classification and transformation of hydrocarbon components of coal | |
| WO2007143653A2 (en) | Power or fuel production using photosynthesis | |
| CN204509231U (en) | A kind of biomass double fluidized-bed vaporizing system methane device | |
| Feng et al. | Simulation of Biomass-to-SNG Process via Pressurized Interconnected Fluidized Beds |
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 | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20180208 Address after: 230088 Hefei hi tech Zone, Hefei, Anhui Province, Wangjiang West Road, Wantong Industrial Park, No. 2, 801-809 Patentee after: Hefei Deborah Power Co. Ltd. Address before: 230088 Wantong Industrial Park, No. 520, Wangjiang West Road, Hefei hi tech Zone, Anhui Province, No. 2 Patentee before: Hefei Debo Bioenergy Science & Technology Co., Ltd. |
|
| TR01 | Transfer of patent right |