CN207193218U - A kind of biomass char vaporizing system for synthesis gas system - Google Patents
A kind of biomass char vaporizing system for synthesis gas system Download PDFInfo
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- CN207193218U CN207193218U CN201720951597.7U CN201720951597U CN207193218U CN 207193218 U CN207193218 U CN 207193218U CN 201720951597 U CN201720951597 U CN 201720951597U CN 207193218 U CN207193218 U CN 207193218U
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Abstract
It the utility model is related to a kind of system of biomass char vaporizing system for synthesis gas.Within the system, biomass char issues raw gasification reaction in gasification reactor in the synergy of oxygen carrier granule and vapor, generation is using hydrogen and carbon monoxide as the oxygen carrier granule after the crude synthesis gas and oxygen release of key component, crude synthesis gas removes vapor and ash content in crude synthesis gas by the second-order separation equipment, form synthesis gas, oxygen carrier granule after oxygen release carries out oxidation reaction with oxygen-containing gas in oxidation reactor, the oxidized oxygen carrier granule of generation, the oxygen carrier granule after being oxidized are sent into gasification reactor and reused.Thus oxygen carrier granule circulates between gasification reactor and oxidation reactor, realizes continuous gasification.This gasification cost is low, energy consumption is low.Also, because in synthesis gas without nitrogen, so combustable gas concentration is high in the synthesis gas of generation, flow rate is high.
Description
Technical field
It the utility model is related to a kind of system of biomass char vaporizing system for synthesis gas.
Background technology
Biomass energy is as renewable resource, and yield is huge, and according to statistics, China about produces 6.87 hundred million tons of biomass moneys every year
Source (calorific value is roughly equal to 3.4 hundred million tons of standard coals).Compared with fossil fuel, biomass sulfur content and content of ashes are relatively low, if it is replaced
Fossil fuel can effectively reduce the environmental pollution that sulfur dioxide and nitrogen oxides are brought.In addition, because biomass is uniquely may be used
Regenerated carbon source, therefore the carbon dioxide in air can be solidified, not Additional discharges carbon dioxide.
The process of the thermochemical study change synthesis gas of biomass includes two stages：Biomass pyrolytic and biomass char gas
Change, biomass char gasification is the process that gaseous fuel is converted biomass into by thermal chemical reaction, the gas production for the gained that gasifies
If owner's hydrogen, methane, carbon monoxide, carbon dioxide and other hydro carbons.At present, the gasifying agent used in gasification of biomass leads to
It is often pure oxygen, its gasification result is good, caused combustable gas concentration is high, aerogenesis calorific value is high.But there is system in existing oxygenerating technology
Oxygen high energy consumption, the problem of cost is high, this will substantially reduce its economy.
Utility model content
(1) technical problems to be solved
The purpose of this utility model, which is to provide, a kind of can obtain the aerogenesis that combustable gas concentration is high, calorific value is high, and can
The biomass char vaporizing system of cost and energy consumption is reduced for the system of synthesis gas.
(2) technical scheme
In order to achieve the above object, the main technical schemes that the utility model uses include：
The utility model provides a kind of system of biomass char vaporizing system for synthesis gas, including gasification reactor, a fraction
From equipment, the second-order separation equipment and oxidation reactor；Gasification reactor has oxygen carrier entrance, steam entry, biomass char
Entrance and mixture outlet；There is one-level separation equipment mixture inlet, oxygen carrier outlet and crude synthesis gas outlet, mixture to enter
Mouth connects with the mixture outlet of gasification reactor；The second-order separation equipment has crude synthesis gas entrance and syngas outlet, thick to close
Into gas entrance and the crude synthesis gas outlet of one-level separation equipment；Oxidation reactor, which has, to be constructed as below：Oxidation reaction utensil
There are oxygen carrier entrance, oxygen-containing gas entrance, oxygen carrier outlet and Poor oxygen gas outlet, the oxygen carrier entrance of oxidation reactor and one
The oxygen carrier outlet of level separation equipment, the oxygen carrier outlet of oxidation reactor and the oxygen carrier entrance of gasification reactor connect
It is logical；Or oxidation reactor has oxygen carrier entrance, oxygen-containing gas entrance, gas-solid mixture outlet, the oxygen carrier of oxidation reactor
The oxygen carrier outlet of body entrance and one-level separation equipment, the gas-solid mixture outlet of oxidation reactor and the gas of a separator
Solid mixture entrance connects, and the oxygen carrier outlet of separator connects with the oxygen carrier entrance of gasification reactor, and separator also has
Poor oxygen gas export.
According to the utility model, the second-order separation equipment includes cyclone separator and condenser；Cyclone separator has thick close
Into gas entrance, crude synthesis gas outlet and ash outlet, the crude synthesis gas entrance of cyclone separator is as the thick of the second-order separation equipment
Synthesis gas entrance；Condenser has crude synthesis gas entrance, condensing medium inlet, condensing medium outlet, liquid water out and synthesis
Gas exports, the crude synthesis gas entrance of condenser and the crude synthesis gas outlet of cyclone separator, the syngas outlet of condenser
Respectively as the syngas outlet of the second-order separation equipment.
According to the utility model, the second-order separation equipment includes condenser and deduster：Condenser have crude synthesis gas entrance,
Crude synthesis gas outlet, condensing medium inlet, condensing medium outlet and liquid water out, the crude synthesis gas entrance of condenser is as two
The crude synthesis gas entrance of level separation equipment；Deduster has the crude synthesis gas entrance with the crude synthesis gas outlet of condenser,
Also there is syngas outlet, the syngas outlet of the syngas outlet of deduster as the second-order separation equipment.
According to the utility model, deduster is sack cleaner.
According to the utility model, in addition to：There is heat supply gas access, waste gas outlet, connection to supply for heat exchanger, heat exchanger
First fluid passage, liquid water inlet, steam outlet, connection between heater gas inlet port and waste gas outlet is in liquid water inlet
Second fluid passage between steam outlet, heat exchange can be carried out between first fluid passage and second fluid passage,
The aqueous water outlet of liquid water inlet and condenser, steam outlet connect with the steam entry of gasification reactor, its
In, in the case where setting separator, the Poor oxygen gas outlet of heat supply gas access and separator, in oxidation reactor
Oxygen carrier outlet connected with the oxygen carrier entrance of gasification reactor and without separator in the case of, heat supply gas access and oxygen
Change the Poor oxygen gas outlet of reactor.
According to the utility model, in addition to：Steam pipe system, steam pipe system selectively connect with heat exchanger, and steam
Pipe network selectively connects with gasification reactor.
According to the utility model, the steam entry of gasification reactor and the steam outlet of heat exchanger pass through the first pipeline
Connection, steam pipe system are connected by the second pipeline with the first pipeline, control valve are provided with the second pipeline, control valve at least can
Make the second pipeline along from the first pipeline towards the direction one-way conduction of steam pipe system storing state and make the second pipeline along from
Steam pipe system switches towards between the release conditions of the direction one-way conduction of the first pipeline.
According to the utility model, in addition to：The heat supply pipeline connected with the heat supply gas access of heat exchanger, wherein, setting
In the case of putting separator, connected between the heat supply gas access of heat supply pipeline and heat exchanger and the Poor oxygen gas outlet of separator
Pipeline connection or the two be connected in parallel to the heat supply gas access of heat exchanger；Wherein, go out in the oxygen carrier of oxidation reactor
Mouth connected with the oxygen carrier entrance of gasification reactor and without separator in the case of, the heat supply gas of heat supply pipeline and heat exchanger
The pipeline connected between the outlet of the Poor oxygen gas of body entrance and oxidation reactor connects or the two is connected in parallel to heat exchanger
Heat supply gas access.
According to the utility model, the condensing medium outlet of condenser connects with the oxygen-containing gas entrance of oxidation reactor.
According to the utility model, gasification reactor is fluidized bed gasification reactor, and its steam entry is located at its bottom, its
Biomass char entrance and mixture outlet are located at its top, and its oxygen carrier entrance is in its bottom sidewall；One-level separation equipment
For cyclone separator, in its side wall, the outlet of its crude synthesis gas is set its mixture inlet located at its top, the outlet of its oxygen carrier
In its bottom；In the cyclone separator of the second-order separation equipment, its crude synthesis gas entrance and crude synthesis gas outlet are located in its side wall,
Its ash outlet is located at its bottom；Oxidation reactor is moving bed oxidation reactor, and located at its top, it contains its oxygen carrier entrance
Carrier of oxygen entrance is located at its bottom, and the outlet of its Poor oxygen gas is provided thereon portion's side wall, and the outlet of its oxygen carrier is located at its underpart side wall,
The position of the oxygen carrier outlet of oxidation reactor passes through therebetween inclination higher than the position of the oxygen carrier entrance of gasification reactor
Straight tube connects.
According to the utility model, in addition to：Screw(-type) feeder, the discharging opening of screw(-type) feeder and the biology of gasification reactor
Matter Jiao entrance connects.
According to the utility model, in addition to：Caisson, caisson and the syngas outlet of the second-order separation equipment connect
It is logical.
According to the utility model, in addition to：Ash bucket, ash bucket connect with the ash outlet of cyclone separator.
(3) beneficial effect
The beneficial effects of the utility model are：
Biomass char vaporizing system provided by the utility model is in the system of synthesis gas, and biomass char is in gasification reactor
Raw gasification reaction is issued in the synergy of oxygen carrier granule and vapor, is generated using hydrogen and carbon monoxide as key component
Crude synthesis gas, wherein with ash content and vapor, crude synthesis gas mixes after the oxygen carrier granule after oxygen release leaves gasification reactor
Separated by one-level separation equipment and be respectively fed to the second-order separation equipment and oxidation reactor；Crude synthesis gas is set by the second-order separation
It is standby to remove vapor and ash content therein, form synthesis gas；Oxygen carrier granule after oxygen release is with oxygen-containing gas in oxidation reactor
Middle carry out oxidation reaction, the oxygen carrier granule and Poor oxygen gas that generation is oxidized again, the oxygen carrier granule after being oxidized again
Gasification reactor is sent into reuse.Thus, made using the synergy of oxygen carrier granule and vapor in gasification reactor
Gasification reaction occurs for biomass char, is reacted again in oxidation reactor with oxygen-containing gas after oxygen carrier granule oxygen loss, realizes oxidation
Regeneration, thus oxygen carrier granule circulates between gasification reactor and oxidation reactor, realizes continuous gasification.This gasification
Cost is low, energy consumption is low.Also, because in synthesis gas without nitrogen, so combustable gas concentration is high in the synthesis gas of generation, synthesis gas heat
Value is high.
Brief description of the drawings
Fig. 1 is the biomass char vaporizing system of embodiment offer for the structural representation of the system of synthesis gas.
【Reference】
1：Gasification reactor；2：Tilt straight tube；3：Oxidation reactor；4：One-level separation equipment；5：Cyclone separator；6：It is cold
Condenser；7：Caisson；8：Ash bucket；9：Screw(-type) feeder；10：Control valve；11：Second pipeline；12：Steam pipe system；13：Heat exchange
Device；14：First pipeline；15：Heat supply pipeline.
Embodiment
It is below in conjunction with the accompanying drawings, right by embodiment in order to understand in order to preferably explain the utility model
The utility model is described in detail.Wherein, the directional terminology such as " on ", " under " involved by this paper, is orientated with what is shown in Fig. 1
With reference to.
Embodiment one
Reference picture 1, the present embodiment provide a kind of system of biomass char vaporizing system for synthesis gas, and the system includes gasified reverse
Answer device 1, one-level separation equipment 4, the second-order separation equipment, oxidation reactor 3, heat exchanger 13, steam pipe system 12, caisson 7, spiral shell
Revolve batcher 9, ash bucket 8.
Gasification reactor 1 can combine work with vapor in high temperature environments, in oxygen carrier granule for cotton-shaped biomass char
With raw gasification reaction is issued, the crude synthesis gas using hydrogen and carbon monoxide as key component is generated, wherein being steamed with ash content and water
Gas, crude synthesis gas are mingled with the oxygen carrier granule after oxygen release and exported from gasification reactor 1.Specifically, gasification reactor 1, which has, supplies
The oxygen carrier entrance of oxygen carrier granule injection, the steam entry of water supply steam injection, the biology for the injection of cotton-shaped biomass char
Matter Jiao entrance and the mixture outlet for the discharge of the mixture of the oxygen carrier granule after oxygen release and crude synthesis gas.Wherein, spiral is given
The discharging opening of material machine 9 connects with the biomass char entrance of gasification reactor 1, to supply cotton-shaped life automatically into gasification reactor 1
Material is burnt.Set auto spiral batcher 9 to improve the automaticity of total system, ensure cotton-shaped biomass char continuous uniform
Ground adds gasification reactor 1.Key reaction in gasification reactor 1 is：
MexOy+ C=CO (g)+MexOy-1
MexOy+ 0.5C=0.5CO2(g)+MexOy-1
MexOy+H2(g)=H2O(g)+MexOy-1
MexOy+ CO (g)=CO2(g)+MexOy-1
MexOy+CH4(g)=2H2(g)+CO(g)+MexOy-1
4MexOy+CH4(g)=2H2O(g)+CO2(g)+4MexOy-1
2C+O2(g)=2CO (g)
C+O2(g)=CO2(g)
C+CO2(g)=2CO (g)
C+H2O=CO (g)+H2(g)
C+2H2(g)=CH4(g)
CO(g)+H2O (g)=H2(g)+CO2(g)
CH4(g)+H2O (g)=3H2(g)+CO(g)
One-level separation equipment 4 connects with gasification reactor 1, and one-level separation equipment 4 can receive the oxygen carrier after oxygen release
The mixture of grain and crude synthesis gas, and the oxygen carrier granule after crude synthesis gas and oxygen release is separated and exported respectively.Specifically,
One-level separation equipment 4 has the mixture inlet for said mixture injection, the oxygen carrier discharged for the oxygen carrier granule after oxygen release
Body exports and the crude synthesis gas outlet for crude synthesis gas discharge, mixture inlet and the gasification reactor 1 of one-level separation equipment 4
Mixture outlet connects, to receive said mixture.
The second-order separation equipment (in reference picture 1 with label 5 and 6 shown in part) is connected with one-level separation equipment 4 to receive
Crude synthesis gas, and the ash content in crude synthesis gas and vapor (vapor is changed into aqueous water removing) are removed, form synthesis gas.Tool
Body, the second-order separation equipment has for the crude synthesis gas entrance of crude synthesis gas injection and for crude synthesis gas removing ash content and vapor
The syngas outlet of the synthesis gas discharge formed afterwards, the crude synthesis gas outlet of the crude synthesis gas entrance and one-level separation equipment 4 connect
It is logical, to receive the crude synthesis gas separated with the oxygen carrier granule after oxygen release.
Specifically, the second-order separation equipment includes removing the cyclone separator 5 of the ash content in crude synthesis gas and removes thick synthesis
The condenser 6 of vapor in gas.The cyclone separator 5 has the crude synthesis gas entrance for crude synthesis gas injection, for removing ash
The crude synthesis gas outlet of crude synthesis gas injection after point and the ash outlet for ash content discharge, the crude synthesis gas of cyclone separator 5
Crude synthesis gas entrance of the entrance as the second-order separation equipment, the ash outlet of cyclone separator 5 are connected with ash bucket 8, and ash bucket 8 is collected
Ash content and periodic cleaning.Condenser 6 has the crude synthesis gas entrance for the crude synthesis gas injection after removing ash content, for cooling medium
(being air in the present embodiment) injection condensing medium inlet, for after heat exchange cooling medium (hot-air in the present embodiment) discharge
Condensing medium outlet, the liquid water out discharged for the aqueous water that is formed after the water vapor condensation in crude synthesis gas and supply
The syngas outlet of the synthesis gas discharge formed after water vapor removing, crude synthesis gas entrance and the cyclone separator 5 of condenser 6
To receive the crude synthesis gas after removing ash content, the syngas outlet of condenser 6 is set crude synthesis gas outlet as the second-order separation
Standby syngas outlet.Thus, it is appreciated that in the present embodiment, in the second-order separation equipment, first remove ash content, then remove water steaming
Gas.
Certainly, the utility model is not limited to this, in other embodiments, can first water vapor removing, then remove ash content,
Such as the second-order separation equipment includes condenser and sack cleaner, condenser is connected with one-level separation equipment 4 to receive thick synthesis
Gas, sack cleaner are connected with condenser to receive the crude synthesis gas after water vapor removing, and then sack cleaner is taken off again
Except the work of ash content.Specifically, in other embodiments, the second-order separation equipment may include condenser and deduster (optional cloth bag
Deduster), condenser has crude synthesis gas entrance, crude synthesis gas outlet, condensing medium inlet, condensing medium outlet and aqueous water
Outlet, the crude synthesis gas entrance of the crude synthesis gas entrance of condenser as the second-order separation equipment.Deduster has and condenser
The crude synthesis gas entrance of crude synthesis gas outlet, also with syngas outlet, the syngas outlet of deduster is as two fractions
From the syngas outlet of equipment.Thus, the crude synthesis gas of one-level separation equipment is introduced into condenser and removes vapor, enters back into and removes
Dirt device removes ash content.
In addition, the second-order separation equipment can also be one point of any ash content that can be removed in crude synthesis gas and vapor
Removing order from the combination of equipment or multiple separation equipments, and ash content and vapor does not limit.Wherein preferably, two fraction
From equipment by by steam transforming for aqueous water in a manner of vapor removed, to recycle aqueous water, certainly, in other realities
Apply the vapor that can be also removed in example by the way of vapor is adsorbed in crude synthesis gas.
Caisson 7 connects with the syngas outlet of the second-order separation equipment, can receive synthesis gas and store.
Oxidation reactor 3 connects with one-level separation equipment 4, and oxidation reactor 3 is moving bed oxidation reactor, oxidation reaction
Device 3 can receive the oxygen carrier granule after oxygen release, and for the oxygen carrier granule after oxygen release and oxygen-containing gas wherein, at high temperature
Carry out oxidation reaction, generation oxidized oxygen carrier granule and Poor oxygen gas again, oxidation reactor 3 also with gasification reactor 1
Connection is sent into gasification reactor 1 with the oxygen carrier granule after will be reoxidized and reused.Thus, oxygen carrier granule is whole
Recycled in system.Specifically, oxidation reactor 3 has the oxygen carrier entrance of the oxygen carrier granule injection after supplying oxygen release, supplied
The oxygen-containing gas entrance of oxygen-containing gas injection, the Poor oxygen gas for Poor oxygen gas discharge export and for the oxygen carriers after being oxidized again
Body particle oxygen carrier exports, the oxygen carrier entrance of oxidation reactor 3 and the oxygen carrier outlet of one-level separation equipment 4.In oxygen
Changing the oxidation reaction occurred in reactor 3 is：
MexOy-1+0.5O2(g)=MexOy
Certainly, the utility model is not limited to this, and the type of oxidation reactor 3 can be any existing oxidation reactor
3 type, as long as the oxygen carrier granule after oxygen release and oxygen-containing gas oxidation reaction can be carried out wherein.For example, oxygen
It can be fluid bed oxidation reactor to change reactor 3, and the top of the oxidation reactor 3 sets oxygen carrier entrance, the oxygen carrier entrance
With the oxygen carrier outlet of one-level separation equipment 4, enter for the oxygen carrier granule after oxygen release；The bottom of oxidation reactor 3 is set
There is oxygen-containing gas entrance, enter for oxygen-containing gas；The upper portion side wall of oxidation reactor 3 exports provided with gas-solid mixture, for oxygen deprivation
The gas-solid mixture output that oxygen carrier granule after gas and oxidation is formed.Now, the Poor oxygen gas formed in oxidation reactor 3
Oxidation reactor is discharged as a mixture because of the self structure reason of oxidation reactor 3 with the oxygen carrier granule after oxidation
3, now the oxygen carrier granule after Poor oxygen gas and oxidation is separated using a separator.Separator is gas-solid separator,
Preferably cyclone separator.The side wall of separator is provided with gas-solid mixture entrance, the gas-solid mixture entrance and oxidation reaction
The gas-solid mixture outlet of device 3, to receive the gas-solid mixture that the oxygen carrier granule after Poor oxygen gas and oxidation is formed；Point
Top from device exports provided with Poor oxygen gas, the Poor oxygen gas discharge for for isolating；The bottom of separator is provided with oxygen carrier granule
Outlet, oxygen carrier outlet are connected with the oxygen carrier entrance of gasification reactor, and the oxygen carrier granule after oxidation is fed through into gas
Change and continue to participate in oxygen release reaction in reactor 1.Thus, separator connects with oxidation reactor 3, defeated to receive oxidation reactor 3
Poor oxygen gas are separated and divided with the oxygen carrier granule after oxidation by the oxygen carrier granule after the Poor oxygen gas gone out and oxidation, separator
Do not export, wherein, separator connects the oxygen carrier granule to be sent into it after oxidation with gasification reactor 1.
Heat exchanger 13 is connected with the second-order separation equipment and oxidation reactor 3, and heat exchanger 13 can be received and set from the second-order separation
(oxidation reaction in oxidation reactor 3 can release largely for aqueous water for discharge and the Poor oxygen gas from the discharge of oxidation reactor 3
Heat, cause Poor oxygen gas to carry substantial amounts of heat), and exchanged heat wherein for aqueous water and Poor oxygen gas, aqueous water is from poor
Obtain heat in carrier of oxygen to form vapor and export, gasification reactor 1 connects with heat exchanger 13, exports to receive heat exchanger 13
Vapor.Specifically, heat exchanger 13 has the heat supply gas access for Poor oxygen gas injection, arranged for the Poor oxygen gas after cooling
The first fluid passage of waste gas outlet, connection between heat supply gas access and waste gas outlet, the liquid for aqueous water injection gone out
State water inlet, the steam outlet discharged for the vapor formed after heat exchange and connection go out in liquid water inlet and vapor
Second fluid passage between mouthful, can carry out heat exchange, heat supply gas enters between first fluid passage and second fluid passage
Mouthful with the Poor oxygen gas outlet of oxidation reactor 3 (certainly, such as in the case where setting separator, heat supply gas access and
The Poor oxygen gas outlet of separator), to receive aqueous water, water steams the aqueous water outlet of liquid water inlet and condenser
Gas outlet is connected with the steam entry of gasification reactor 1, and vapor is sent into gasification reactor 1 and is continuing with.At this
In embodiment, waste gas outlet and atmosphere, certain waste gas outlet can also connect with the equipment of subsequent technique, or also can be with depositing
Reservoir is connected to store Poor oxygen gas (rationally collect Poor oxygen gas and can be used for the production such as chemical fertilizer).
Steam pipe system 12 is selectively connected with heat exchanger 13 to receive vapor, and steam pipe system 12 selectively with
Gasification reactor 1 is connected can convey vapor into gasification reactor 1 at any time.Thus, the vapor that heat exchanger 13 is formed
Can a part be sent directly into gasification reactor 1 be used for react, another part is stored temporarily in steam pipe system 12, treats that needs carry
Vapor is obtained to now water caused by heat exchanger 13 from steam pipe system 12 during high vapor supply to gasification reactor 1
Steam supplements.
Heat supply pipeline 15 is additionally provided with the present embodiment, and heat supply pipeline 15 connects with heat exchanger 13, for supplying external industry
Flue gas enters heat exchanger 13, and being changed into vapor for aqueous water contributes heat.The heat supply gas of the heat supply pipeline 15 and heat exchanger 13
The pipeline connection or two connected between the Poor oxygen gas outlet of the Poor oxygen gas of entrance and oxidation reactor 3 outlet/separator
Person is connected in parallel to the heat supply gas access of heat exchanger 13, the heat supply gas for heat supply pipeline 15 and heat exchanger 13 shown in Fig. 1
The pipeline connection connected between the outlet of the Poor oxygen gas of body entrance and oxidation reactor 3, after industrial smoke mixes with Poor oxygen gas
Enter the heat supply gas access of heat exchanger 13 together.Certainly, the utility model is not limited to this, heat supply pipeline 15 with to heat exchanger
The pipeline of 4 conveying Poor oxygen gas also can connect to form the two structure in parallel with heat supply gas access respectively.
To sum up, send out cotton-shaped biomass char in gasification reactor 1 using the synergy of oxygen carrier granule and vapor
Gasification reaction is given birth to, is reacted again in oxidation reactor 3 with oxygen-containing gas after oxygen carrier granule oxygen loss, realizes oxidation regeneration, thus
Oxygen carrier granule circulates between gasification reactor 1 and oxidation reactor 3, realizes continuous gasification.This gasification cost is low,
Energy consumption is low.Also, because in synthesis gas without nitrogen, so combustable gas concentration is high in the synthesis gas of generation, flow rate is high.
Also, because the synthesis gas finally obtained is probably for multi-chemicals such as synthesizing alcohol, methanol, therefore face
Different target chemicals, the H in synthesis gas2There may be different requirements with CO ratio, the system can be by first will
The vapor that a part of heat exchanger 13 obtains is stored to be used as the variable of vapor injection rate in regulation gasification reactor 1
Mode, adjust the H in synthesis gas2With CO ratio.Thus, the system can be applied to the preparation of different target chemicals simultaneously
And realize that this applicable method is extremely easy, cost is greatlyd save, improves production efficiency.
Also, the system of the present embodiment realizes transmission of the heat between gasification reactor 1 and oxidation reactor 3, whole
System system energy utilization efficiency is higher.Specifically, the heat that Poor oxygen gas carry is supplied to gasified reverse for generating vapor
Should, heat band is back to oxidation reactor 3 again and is used to generate Poor oxygen gas by the oxygen carrier granule after oxygen release, is followed in oxygen carrier granule
While ring uses, the circulation of energy is also form, reduces energy consumption, capacity usage ratio is high.
Also, caused aqueous water forms original of the vapor as gasification reactor 1 by heat exchange in the second-order separation equipment
Material, whole system realizes the zero-emission of waste water, more environmentally-friendly.In addition, the Poor oxygen gas after cooling are discharged into air, ring is also beneficial to
Protect.
, need not be additional in production process also, oxygen carrier granule recycles in process of production, raw material has been saved, has been carried
Oxysome service efficiency is high.
Summary describes, and the system that the present embodiment provides, technological process is simple, innovative to steam oxygen carrier granule and water
Gas is combined with cotton-shaped biomass char, and preparing the part such as high heating value synthesis gas, each reactor and intercoupling realizes heat and water
Resource recycles, and has important energy-saving and emission-reduction realistic meaning.
Further, in the present embodiment, gasification reactor 1 is fluidized bed gasification reactor, its gasification temperature that can be born
Degree is at least 750-1200 DEG C.Such as Fig. 1, the steam entry of gasification reactor 1 is located at the bottom of gasification reactor 1, gasified reverse
The biomass char entrance of device 1 and mixture outlet is answered to be located at the top of gasification reactor 1, the oxygen carrier entrance of gasification reactor 1
In the bottom sidewall of gasification reactor 1.Certainly, the utility model is not limited to this, in other embodiments, gasification reaction
Device 1 can select existing any types, as long as can react raw wherein for cotton-shaped biomass char, oxygen carrier granule and vapor
Oxygen carrier granule into after crude synthesis gas and oxygen release.Wherein, oxygen carrier granule be preferably deoxidation, oxygen ability it is stronger
Composite oxygen carrier particles, the active component of the composite type oxygen carrier granule can be CuMn2O4、Fe2O3、FeNi2O4Deng inertia load
Body can be Al2O3、ZrO2、SiO2、TiO2、MgAl2O4, quartz sand, refractory cement etc., oxygen carrier uses customary preparation methods system
It is standby.
Further, in the present embodiment, one-level separation equipment 4 is cyclone separator, and the mixture of one-level separation equipment 4 enters
Mouth is in the side wall of one-level separation equipment 4, and the crude synthesis gas outlet of one-level separation equipment 4 is located at the top of one-level separation equipment 4
Portion, the oxygen carrier outlet of one-level separation equipment 4 is located at the bottom of one-level separation equipment 4.In the one-level separation equipment 4, density is most
Oxygen carrier granule after big oxygen release is separated.
Further, in the cyclone separator 5 of the second-order separation equipment, the crude synthesis gas entrance of the cyclone separator 5 and thick conjunction
Into gas outlet in the side wall of the cyclone separator 5, the ash outlet of the cyclone separator 5 is located at the cyclone separator 5
Bottom.
Further, in the condenser 6 of the second-order separation equipment, the crude synthesis gas entrance and syngas outlet of condenser 6 are located at
In the side wall of condenser 6, the condensing medium outlet of condenser 6 is located at the top of condenser 6, the condensing medium inlet of condenser 6
The bottom of condenser 6 is located at liquid water out.
Further, in the present embodiment, the reaction temperature that oxidation reactor 3 can be born is 400-1000 DEG C.Oxygen-containing gas
The volumetric concentration of middle oxygen is 5-21%, preferably air or oxygen containing industrial smoke.The oxygen carrier entrance of oxidation reactor 3 is located at
The top of oxidation reactor 3, the oxygen-containing gas entrance of oxidation reactor 3 are located at the bottom of oxidation reactor 3, oxidation reactor 3
Poor oxygen gas outlet located at oxidation reactor 3 upper portion side wall, oxidation reactor 3 oxygen carrier outlet is located at oxidation reactor
3 lower sides, oxidation reactor 3 oxygen carrier outlet position higher than gasification reactor 1 oxygen carrier entrance position, two
Connected between person by tilting straight tube 2, in order to which the oxygen carrier granule after being reoxidized smoothly enters in gasification reactor 1.
Valve can be set on straight tube 2 is tilted.
Further, in the present embodiment, caisson 7 is gas storage holder, and gas storage holder includes synthesis gas entrance, and the synthesis gas enters
Mouth connects with the syngas outlet of condenser 6, to receive synthesis gas.
Further, in the present embodiment, heat exchanger 13 is waste heat boiler.The steam entry of gasification reactor 1 and heat exchange
The steam outlet of device 13 is connected by the first pipeline 14, and steam pipe system 12 is connected by the second pipeline 11 with the first pipeline 14,
It is provided with control valve 10 on the second pipeline 11, control valve 10 can at least make the second pipeline 11 along from the first pipeline 14 towards steaming
The storing state of the direction one-way conduction of steam pipe net 12 and make the second pipeline 11 along from steam pipe system 12 towards the first pipeline 14
Switch between the release conditions of direction one-way conduction.Thus, when control valve 10 is in storing state, discharged from heat exchanger 13
A part for vapor is directly entered gasification reactor 1 by the first pipeline 14, and another part is by the second pipeline 11 (including warp
Cross adjustment control valve 10) enter steam pipe system 12；When control valve 10 is in release conditions, from the vapor of the discharge of heat exchanger 13
All it is directly entered gasification reactor 1, while the vapor in steam pipe system 12 (including is adjusted control by the second pipeline 11
Valve 10 processed) enter the first pipeline 14 and subsequently into gasification reactor 1.Therefore, can be by adjusting the state of control valve 10, adjustment
Vapor whether is fed into gasification reactor 1 from steam pipe system 12, and then controls the injection rate of vapor.Certainly, realize
Steam pipe system 12 is not limited to the citing of the present embodiment with heat exchanger 13 and the selectable mode connected of gasification reactor 1, this
Art personnel can be realized according to the conventional arrangement of this area by the setting of pipeline, valve or special communication apparatus.
Further, the condensing medium outlet of condenser 6 connects with the oxygen-containing gas entrance of oxidation reactor 3, will be hot empty
Pneumatic transmission enters in oxidation reactor 3 to be aoxidized as oxygen-containing gas to the oxygen carrier granule after oxygen release.Thus, the hot-air of formation
It is sent into oxidation reactor 3 and participates in oxidation reaction, reduce energy consumption, capacity usage ratio is high.
In the system of the present embodiment, above-mentioned " connection " can be two parts be directly connected to and turn on or
Two parts are connected by pipeline, and miscellaneous part can also be set on pipeline, as long as the biography of corresponding material can be realized
It is defeated.Also, separator and separation equipment in the present embodiment etc. exercise the setting of the device of separation function, are all based on it
Whether upstream equipment has the separation function such as gas solid separation function, solid separation, separation of solid and liquid and determines in itself, therefore, is holding
When the equipment (gasification, oxidation furnaces) of row main technological steps selects different type, those skilled in the art can delete above-mentioned
The device of enforcement separation function in embodiment, or the device of separation function is exercised in addition in the above-described embodiments.
The systematic difference method of the present embodiment described below, comprises the following steps：
S1, cotton-shaped biomass char are under the high temperature of gasification reactor 1 under the synergy of oxygen carrier granule and vapor
Generation gasification reaction, generate using hydrogen and carbon monoxide as the oxygen carrier granule after the crude synthesis gas and oxygen release of key component,
Ash content and vapor are carried in crude synthesis gas；
The crude synthesis gas of oxygen carrier granule after S2, entrainment oxygen release passes through one-level separation equipment 4, removes the oxygen carrier after oxygen release
Body particle；
The cyclone separator 5 that S3, crude synthesis gas pass through in the second-order separation equipment, removes ash content, and ash content is collected to ash bucket 8
In；
Crude synthesis gas after S4, removing ash content pass through condenser 6, the vapor in crude synthesis gas and cooling medium (
It is air in embodiment) exchange heat, the vapor in crude synthesis gas is changed into aqueous water and departs from crude synthesis gas, forms synthesis gas, air
It is changed into hot-air；
Oxygen carrier granule after S5, oxygen release is with oxygen-containing gas (can use the hot-air formed in step S4) in oxidation reaction
In device 3, oxidation reaction is carried out at high temperature, and generating oxidized oxygen carrier granule, (" oxidized oxygen carrier granule " refers to oxygen release
After oxygen carrier granule afterwards is oxidized again) and Poor oxygen gas, the oxygen carrier granule after being oxidized, which is sent into gasification reactor 1, to be made
With.
S6, the aqueous water that step S4 is generated and the step S5 Poor oxygen gas generated and external industrial smoke are changed
Heat, vapor is formed, a part for the vapor formed is sent directly into gasification reactor 1 and used, another part storage
Get up and can be sent at any time in gasification reactor 1 to use, to control the amount of the vapor used in gasification reactor 1.It is understood that
Above-mentioned steps not only perform 1 time, but persistently carried out in technical process.
Certainly, method of the present utility model is not limited to using the system shown by embodiment one, as long as can complete
Step S1 is stated to step S6.Although also, it is emphasized that sorted in method with S1-S6, do not form pair
The restriction of step sequencing, except non-post step must utilize first step product or well known to a person skilled in the art needs
The situation that first step first carries out, the order listed by above-described embodiment is otherwise not limited to, and combines foregoing detailed description
Understand, progress is the most beneficial simultaneously for some steps, such as step S2 and step S5.
It is understood that in the system of above-described embodiment, when production just starts, the load injected into gasification reactor 1
Oxysome particle and vapor, the oxygen-containing gas (air) injected into oxidation reactor 3 are that system is external, but when production is steady
After fixed, the oxygen carrier granule and vapor that are injected into gasification reactor 1 and the oxygen-containing gas injected into oxidation reactor 3
(air) recycles in systems.
Above content is only preferred embodiment of the present utility model, for one of ordinary skill in the art, according to this reality
With new thought, there will be changes, this specification content should not be construed as in specific embodiments and applications
To limitation of the present utility model.
Claims (13)
1. a kind of biomass char vaporizing system is for the system of synthesis gas, it is characterised in that is separated including gasification reactor (1), one-level
Equipment (4), the second-order separation equipment and oxidation reactor (3)；
The gasification reactor (1) has oxygen carrier entrance, steam entry, biomass char entrance and mixture outlet；
The one-level separation equipment (4) has mixture inlet, oxygen carrier outlet and crude synthesis gas outlet, the mixture inlet
Connected with the mixture outlet of the gasification reactor (1)；
The second-order separation equipment has crude synthesis gas entrance and syngas outlet, the crude synthesis gas entrance and a fraction
From the crude synthesis gas outlet of equipment (4)；
The oxidation reactor, which has, to be constructed as below：
The oxidation reactor (3) has oxygen carrier entrance, oxygen-containing gas entrance, oxygen carrier outlet and Poor oxygen gas outlet, institute
State the oxygen carrier entrance of oxidation reactor (3) and the oxygen carrier outlet of the one-level separation equipment (4), the oxidation reaction
The oxygen carrier outlet of device (3) connects with the oxygen carrier entrance of the gasification reactor (1)；Or
The oxidation reactor (3) has oxygen carrier entrance, oxygen-containing gas entrance, gas-solid mixture outlet, the oxidation reaction
The oxygen carrier entrance of device (3) and the oxygen carrier outlet of the one-level separation equipment (4), the gas of the oxidation reactor (3)
Solid mixture outlet connects with the gas-solid mixture entrance of a separator, oxygen carrier outlet and the gasified reverse of the separator
The oxygen carrier entrance of device (1) is answered to connect, the separator also has Poor oxygen gas outlet.
2. biomass char vaporizing system according to claim 1 is for the system of synthesis gas, it is characterised in that
The second-order separation equipment includes cyclone separator (5) and condenser (6)；
The cyclone separator (5) has crude synthesis gas entrance, crude synthesis gas outlet and ash outlet, the cyclone separator
(5) crude synthesis gas entrance of the crude synthesis gas entrance as the second-order separation equipment；
The condenser (6) has crude synthesis gas entrance, condensing medium inlet, condensing medium outlet, liquid water out and synthesis
Gas exports, the crude synthesis gas entrance of the condenser (6) and the crude synthesis gas outlet of the cyclone separator (5), described
Syngas outlet of the syngas outlet of condenser (6) as the second-order separation equipment.
3. biomass char vaporizing system according to claim 1 is for the system of synthesis gas, it is characterised in that
The second-order separation equipment includes condenser and deduster：
The condenser has crude synthesis gas entrance, crude synthesis gas outlet, condensing medium inlet, condensing medium outlet and aqueous water
Outlet, the crude synthesis gas entrance of the crude synthesis gas entrance of the condenser as the second-order separation equipment；
The deduster has the crude synthesis gas entrance with the crude synthesis gas outlet of the condenser, also goes out with synthesis gas
Mouthful, the syngas outlet of the syngas outlet of the deduster as the second-order separation equipment.
4. biomass char vaporizing system according to claim 3 is for the system of synthesis gas, it is characterised in that
The deduster is sack cleaner.
5. biomass char vaporizing system according to Claims 2 or 3 is for the system of synthesis gas, it is characterised in that also includes：
Heat exchanger (13), the heat exchanger (13) have heat supply gas access, waste gas outlet, connection in the heat supply gas access
First fluid passage, liquid water inlet, steam outlet, connection between the waste gas outlet in the liquid water inlet and
Second fluid passage between the steam outlet, it can enter between the first fluid passage and the second fluid passage
Row heat exchange, the aqueous water outlet of the liquid water inlet and the condenser, the steam outlet and the gasification
The steam entry connection of reactor (1)；
Wherein, in the case where setting separator, the heat supply gas access and the Poor oxygen gas outlet of the separator,
The oxidation reactor oxygen carrier outlet connected with the oxygen carrier entrance of the gasification reactor and without separator
In the case of, the heat supply gas access and the Poor oxygen gas outlet of the oxidation reactor.
6. biomass char vaporizing system according to claim 5 is for the system of synthesis gas, it is characterised in that also includes：
Steam pipe system (12), the steam pipe system (12) selectively connects with the heat exchanger (13), and the steam pipe
Net (12) selectively connects with the gasification reactor (1).
7. biomass char vaporizing system according to claim 6 is for the system of synthesis gas, it is characterised in that
The steam entry of the gasification reactor (1) passes through the first pipeline (14) with the steam outlet of the heat exchanger (13)
Connection, the steam pipe system (12) is connected by the second pipeline (11) with first pipeline (14), in second pipeline
(11) control valve (10) is provided with, the control valve (10) can at least make the second pipeline (11) edge from the first pipeline
(14) towards the steam pipe system (12) direction one-way conduction storing state and make second pipeline (11) along from described
Steam pipe system (12) switches towards between the release conditions of the direction one-way conduction of first pipeline (14).
8. biomass char vaporizing system according to claim 5 is for the system of synthesis gas, it is characterised in that also includes：
The heat supply pipeline (15) connected with the heat supply gas access of the heat exchanger (13)；
Wherein, in the case where setting separator, the heat supply pipeline (15) and the heat supply gas access of the heat exchanger (13)
The pipeline connected between the Poor oxygen gas outlet of the separator connects or the two is connected in parallel to the heat exchanger (13)
Heat supply gas access；
Wherein, the oxidation reactor oxygen carrier outlet connected with the oxygen carrier entrance of the gasification reactor and without
In the case of separator, heat supply gas access and the oxidation reactor of the heat supply pipeline (15) with the heat exchanger (13)
Poor oxygen gas outlet between connect pipeline connection or the two heat supply gas for being connected in parallel to the heat exchanger (13) enter
Mouthful.
9. biomass char vaporizing system according to Claims 2 or 3 is for the system of synthesis gas, it is characterised in that
The condensing medium outlet of the condenser (6) connects with the oxygen-containing gas entrance of the oxidation reactor (3).
10. biomass char vaporizing system according to claim 2 is for the system of synthesis gas, it is characterised in that
The gasification reactor (1) is fluidized bed gasification reactor, and its steam entry is located at its bottom, its biomass char entrance
Its top is located at mixture outlet, its oxygen carrier entrance is in its bottom sidewall；
The one-level separation equipment (4) is cyclone separator, and in its side wall, the outlet of its crude synthesis gas is set its mixture inlet
In its top, the outlet of its oxygen carrier is located at its bottom；
In the cyclone separator of the second-order separation equipment, its crude synthesis gas entrance and crude synthesis gas outlet are located in its side wall,
Its ash outlet is located at its bottom；
The oxidation reactor (3) is moving bed oxidation reactor, and its oxygen carrier entrance is located at its top, its oxygen-containing gas entrance
Located at its bottom, the outlet of its Poor oxygen gas is provided thereon portion's side wall, and the outlet of its oxygen carrier is located at its underpart side wall, and the oxidation is anti-
The position that the oxygen carrier of device (3) exports is answered to pass through therebetween higher than the position of the oxygen carrier entrance of the gasification reactor (1)
Tilt straight tube (2) connection.
11. biomass char vaporizing system according to claim 1 is for the system of synthesis gas, it is characterised in that also includes：
Screw(-type) feeder (9), the discharging opening of the screw(-type) feeder (9) and the biomass char entrance of the gasification reactor (1)
Connection.
12. biomass char vaporizing system according to claim 1 is for the system of synthesis gas, it is characterised in that also includes：
Caisson (7), the caisson (7) connect with the syngas outlet of the second-order separation equipment.
13. biomass char vaporizing system according to claim 2 is for the system of synthesis gas, it is characterised in that also includes：
Ash bucket (8), the ash bucket (8) connect with the ash outlet of the cyclone separator (5).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720951597.7U CN207193218U (en) | 2017-08-01 | 2017-08-01 | A kind of biomass char vaporizing system for synthesis gas system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720951597.7U CN207193218U (en) | 2017-08-01 | 2017-08-01 | A kind of biomass char vaporizing system for synthesis gas system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109054900A (en) * | 2018-08-17 | 2018-12-21 | 新奥科技发展有限公司 | A kind of coal gasification method and system |
| AT526208A1 (en) * | 2022-06-08 | 2023-12-15 | Gs Gruber Schmidt Gmbh | Process for producing synthesis gas from biochar and biogenic fines using electrical energy |
-
2017
- 2017-08-01 CN CN201720951597.7U patent/CN207193218U/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109054900A (en) * | 2018-08-17 | 2018-12-21 | 新奥科技发展有限公司 | A kind of coal gasification method and system |
| AT526208A1 (en) * | 2022-06-08 | 2023-12-15 | Gs Gruber Schmidt Gmbh | Process for producing synthesis gas from biochar and biogenic fines using electrical energy |
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