CN204803273U - Be used for making pneumatolytic equipment of carbon containing solid - Google Patents

Be used for making pneumatolytic equipment of carbon containing solid Download PDF

Info

Publication number
CN204803273U
CN204803273U CN201390000581.8U CN201390000581U CN204803273U CN 204803273 U CN204803273 U CN 204803273U CN 201390000581 U CN201390000581 U CN 201390000581U CN 204803273 U CN204803273 U CN 204803273U
Authority
CN
China
Prior art keywords
stream
water
reactor
pipeline
equipment
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.)
Expired - Lifetime
Application number
CN201390000581.8U
Other languages
Chinese (zh)
Inventor
F·茹达斯
G·阿鲁穆加姆
M·绍尔
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Application granted granted Critical
Publication of CN204803273U publication Critical patent/CN204803273U/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/06—Continuous processes
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F2001/007—Processes including a sedimentation step
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/0916—Biomass
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/1687—Integration of gasification processes with another plant or parts within the plant with steam generation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/16—Integration of gasification processes with another plant or parts within the plant
    • C10J2300/169—Integration of gasification processes with another plant or parts within the plant with water treatments
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Abstract

Be used for making pneumatolytic equipment of carbon containing solid, this equipment have gasification reaction ware, separator and a water purification installation in the gasification reaction ware the solid turns into CO and H2 at least in part from passing through among the separator the moisture liquid flow of thick synthetic gas separation that the gasification obtained the water purification installation medium cleaning moisture stream, wherein, water purification installation designs into feasiblely contain the three stream that the flow separation becomes to have different purity, and water purification installation is connected via pipeline and steam purification device, and/or via pipeline and solid pulp device, preferred other ashes processing apparatus or access to the pipe connection that is used for the soup compound in the reactor, and/or via the pipeline with the gasification reaction ware is connected.

Description

The equipment gasified for making carbonaceous solids
Technical field
The present invention relates to a kind of method and apparatus for making carbonaceous solids gasify, wherein in the first method steps, solid is converted into CO and H at least in part between pneumatolytic stage 2, in the second method steps, be separated aqueous stream, and the aqueous stream experience Water warfare will obtained in the second method steps in third method step.
Background technology
Gasification is called chemical-physical process, and in this chemical-physical process, solid matter is transferred in gaseous state final product at least partially.The final product of gaseous state is primarily of carbon monoxide (CO) and hydrogen (H 2) mixture that forms.Many reactions only understood by halves are up to now carried out simultaneously.Actual gasification is burnt by the heat release of solid and is realized.The product of this reaction can react further with solid and the steam guided in addition or react each other.Except combustion reactions, all primitive reactions are balanced reaction, make transform also can with counter movement.At temperature (600 to 1600 DEG C) higher in coal gasification reaction, the component of product gas closely balances usually.
In principle, known three kinds of dissimilar methods for solids gasification: the gasification in fluidized-bed, by the gasification in the fixed bed that solid is formed and last gasification in entrained-flow reactor.
Realize gasification reaction howsoever, all must purify synthesis gas CO and H obtained in described method subsequently 2.Owing to during reaction needing steam as educt and water is one of possible reaction product, so especially must from gas stream except anhydrating.
Containing other impurity such as such as solid, ammonia, phenolic compounds in the current be separated, current must be cleaned.
Such as known this method from DE4107109C1.Make solid fuel gasification to produce raw gas (rawgas) under using the pressure of the gasifying medium containing aerobic and steam in the scopes of 10 to 100 bar.Raw gas from gasifier is cooled to the temperature of 20 to 200 DEG C, obtains the condensation product being rich in water thus.Make condensate separation and evaporate at least in part, wherein taking out the bittern of condensate stream and saliferous respectively.The bittern of burning saliferous, is partly added to the raw gas through purification by condensate stream.
DE3515484 describes and cool the acquisition condensation product when the progressively cooling of product gas in the washer-water cooler being filled with recirculated water, is washed out by most of halogen thus.Have and be expanded to lower pressure the temperature of 120 to 220 DEG C with the washing water crossed, obtain flash-off steam and liquid phase thus.Discharge the flash-off steam almost not having halogen, make most of liquid phase again enter washer-water cooler, and residual liquid phase is supplied to disposal plant.
DE3207779A1 describes the condensation product making to obtain from synthesis gas and expands and be supplied to isolation base members, takes out the condensation phase primarily of water composition from this isolation base members.In condensation for before cooling rough coal air-flow, condensation phase directly contacts with colder gas and cools.That be heated, containing steam cooling gas is supplied to burner and such as reactor heating.
DD147679 describes the recirculation of the stream be substantially made up of water, and described stream comes from current swirler, from the low flow point of solids content from the high stream of solids content in this current swirler.The overflow stream (overflowstream) that solids content is low mixes with the segregation logistics of gasifier and the source of steam required in being used as to react.The underflow stream (underflowstream) that solids content is high distills to purify further at atmosheric pressure.
Finally, GB2198744A describes the gasification in fixed bed, and in described fixed bed, after gas delivery, wastewater streams guides in evaporation parts.Gaseous composition is recycled to the reactor as gasifying medium from described evaporation parts.
In addition, from diverse method, contain to known portions the recirculation of the current of most of solid.Such as, US5,586,510 are described in rotary kiln and produce cement, and the mud obtained when manufacture of cement in rotary kiln is recycled in rotary kiln, atomization/atomize in rotary kiln and burning.
The something in common of all described methods is that a large amount of waste water can not utilize further in method.Therefore, need the waste water after-treatment device of costliness and high cost to process one or more stream, make to observe environmental standard during disposing.
Summary of the invention
Therefore, the object of the invention is the waste water produced when reducing solids gasification.
According to the present invention, realize this object by the method for the feature with claim 1.There is the situation gasified of oxygen and steam and be converted into carbon monoxide and hydrogen at least in part in carbonaceous solids material.Then, the gaseous mixture produced is supplied to tripping device, from gaseous parts separation of liquid part in tripping device, obtains so-called rough coal air-flow and aqueous stream thus.Last aqueous liquid stream experience Water warfare.
According to the present invention, realize Water warfare to obtain three streams of different purity.First purity is the highest, is almost only made up of water, and has following component:
Table 1: the material comprised in first-class
Therefore, this stream is suitable for steam generation.When this stream does not reach these ultimate values, the first-class water coolant that can be used as device interior.
Second has medium purity.
Table 2: the material comprised in second
3rd stream has minimum purity and with the highest solids content:
Table 3: the material comprised in the 3rd stream
Organic compound wt-％ 5-80
Compound containing nitrogen and/or phosphorus wt-％ 1-5
Metal hydroxides wt-％ 5-15
According to the recirculation of each stream that The inventive process provides in these three stream.The current with highest purity are supplied to the water-in of vapour generator; The current with medium purity are supplied to the other treatment unit of the ashes obtained in gasifying reactor; And/or there is lowest purity and the current that solids content is high lead back in gasifying reactor.
Particularly advantageously, all three streams are in the interior recirculation of gasification unit itself.The amount of waste water obtained in the method not only can reduce greatly, but in fact fully can be down to zero.
Meanwhile, the stream with medium purity and lowest purity also can jointly be recycled in gasification zone, can realize the extra high utilization ratio of comprised organic composition thus.
To a certain extent, first purity does not reach the purity needed for steam generation.When pH value is identical, its component is compared with the concentration shown in table 1, and the concentration of each composition is three times, is even six times individually.The stream with this component can be used as cooling-water flowing and described water coolant can not evaporate the cooling tower that maybe can be added to equipment for gasification in the optional position of technique.
Of the present invention one favourable in, be separated by decant by the stream in a first step with lowest purity.Such as can reduce water content further by evaporation.In the second step, residual stream is supplied to reverse osmosis unit subsequently.Reverse osmosis is the physical process for concentrated dissolving material in a liquid, utilizes pressure by reverse for naturally osmotic process in reverse osmosis.The medium that the medium that the concentration of predetermined substance should reduce should be improved by semipermeable partition and described concentration is separated.In the case of this example, in the current entered, the concentration of solid should reduce and should improve having leaving in stream of lowest purity.The medium that concentration should improve is exposed to the high pressure of the pressure that must obtain than the infiltration needed for equalization of concentration.This causes particle and propagation direction to be moved on the contrary.In the method for the invention, the first-class second time of the experience again reverse osmosis through purification preferably obtained, has the stream of highest purity to obtain and has the stream of medium purity.
Also the ion-exchanger by being positioned at reverse osmosis unit upstream obtains a part for the stream with medium purity.Subsequently two parts with medium purity from ion-exchanger and reverse osmosis unit are flowed mixing.
Separation three stream before and/or be separated have lowest purity stream---its water content is lower than 89wt-%, preferably lower than 50wt-% and particularly preferably lower than 30wt-%---and between reverse osmosis unit, more purifying step can be provided, the removing of such as denitrogenation, nitrated and/or organic compound.
Denitrogenation is interpreted as specific non-autotrophic bacteria by adhering to film and some autotrophic bacterias by nitrate (NO 3 -) in nitrogen transformation be nitrogen molecule (N 2).Come, in this process energy-producing, to there is not oxygen molecule (O utilizing bacterium 2) when (anoxic conditions) use nitrate to make such as organic substance, hydrogen sulfide (H as oxygenant (oxygenant) 2and hydrogen molecule (H S) 2) various an oxidisable substances (electron donor) oxidation.
Nitrated expression ammonia (NH 3) bacterial oxidation is nitrate (NO 3).It is made up of the local process that two link: in the first local process, make ammonia oxidation be nitrite, this nitrite is oxidized to nitrate in the second local process.
Preferably by the anaerobic treatment using bacterium to carry out in oxygen-free environment to realize the removing of organic compound.
In addition, find advantageously such as to be used for by the steam that intrasystem for the steam supply being used for gasification vapour generator produces educt in preheating such as still-process and/or by steam for generation of the electric energy being such as used for operate turbines machine.Thus, the demand of described method to water can be reduced.Advantageously, vapour generator is connected to downstream turbine via the pipeline produced steam being guided to downstream turbine.
Especially, when realizing gasification in fixed-bed reactor, the ashes obtained in fixed-bed reactor should be washed out.For this reason, according to a scheme of the present invention, use the current with medium purity.
In fixed bed gasification, these ashes pass through the reaction acquisition of the carbonaceous solids of such as coal or biomass and so on and the grid in the bottom section being arranged on fixed bed falls.In order to carry ashes further, introducing water and therefore washing out ashes.
Be in the gasification performed in fluidized-bed, find particularly advantageously also to make the stream of medium purity be recycled in reactor.
In entrained flow gasification, it is recommended that make the stream with medium purity with the educt guided in reactor mixes and/or mixes with slag/wastewater streams after chilling as soup compound.
In addition, the current of highest purity may be necessary to make to have and/or the current of medium purity experienced purification further before being recycled in vapour generator or another ash treatment device.Even if this further purification is provided for still can making wastewater streams recirculation in large quantities when a large amount of dirt is guided in this process by used solid starting material.
Possible process for purifying further can be such as Fenton's reaction (use and by the hydrogen peroxide in the acidic medium of molysite catalysis, organic substrate is oxidized), ozonize (by being inducted into ozonization), use gac (as sorbent material) and/or the chemical process of adding calcium hydroxide (for reducing the water hardness by ion-exchange).Also can imagine and use other precipitation agent or condensing agent.In addition, also separator and/or sewage disposal device can be used.
In addition, a favourable aspect of the present invention provides solid and gasifies in fixed bed.
In fixed bed gasification, find advantageously to guide to above fixed bed by the current with lowest purity, wherein fine distribution ground sprays this stream as far as possible.
When using entrained-flow reactor, can imagine and the current with lowest purity are directly fed in burner flame via service.In a fluidized bed reactor, the atomization above fluidized-bed should also be considered.When fuel supplies as soup compound in entrained flow gasification, it is recommended that stream mixed with this soup compound before entering reactor area.
As solid matter, coal can be used on the one hand.Coal gasification course implements many decades.On the other hand, biomass also can be used as starting materials, reproducible starting material can be converted into synthesis gas thus.Especially, when gasifying biomass, said process is very important, because most of incombustible material is discharged by current.
The present invention also comprises a kind of equipment for making carbonaceous solids material gasify with the feature of claim 9.Correspondingly, this equipment comprises gasifying reactor, tripping device and water-purification plant, in described gasifying reactor, solid is converted into carbon monoxide and hydrogen at least in part, in described tripping device, be separated raw gas from liquid water stream, in described water-purification plant, purify the liquid water stream obtained in tripping device.When Water warfare, water is separated into three streams with different purity.The current with highest purity are supplied to the water-in of vapour generator via the first pipeline; The current with medium purity are supplied to the device of the further process for the ashes from gasifying reactor via second pipe; And/or the current with lowest purity are led back in gasifying reactor via the 3rd pipeline.
Advantageously, for from liquid flow point from the apparatus design of gaseous parts be condenser or droplet separator (dropletseparator).The advantage being designed to condenser is air-flow cooling further simultaneously.When using droplet separator, air-flow the heat energy that obtains can be used for other position in cooling before and when cooling.
Advantageously, also comprise the gas quench system between gasifying reactor and tripping device according to equipment of the present invention, this gas-liquid separator to be formed as droplet separator and thus must other position in method realize cooling time be recommendable especially.In addition, equipment according to the present invention preferably includes the ammonia recovery unit between tripping device and other ash treatment device.
When gas-liquid separation, be separated the comprised liquid stream from gas quench system further by decant, it is coal-tar middle oil, oily, phenolic compound and ammonia (NH 3) be separated substantially.
By downstream the further purification of process implementation water.? in process, according to mixing tank-separator principles make water containing phenolic compound in multistage extraction tower with close mixing.In being separated subsequently, in solvent, there is the phenolic compound of largest portion.This process repeated several times, the water wherein containing phenolic compound and solvent guide with adverse current.Solvent to be separated with phenolic compound by distillation and to flow back in extraction tower again to wash phenolic compound off.
In process after process, CLL process (ChemieLinz-can be carried out ).In this process, by selectivity stripping come from the condensation product of process and remove sour gas and ammonia.
Due to this design of equipment, particularly along with more and more stricter environmental protection requirement, can obviously reduce cost of investment and operation cost, because the purification of the costliness of waste water to be disposed can be saved wholly or in part.By the stream of the major portion with solid is led back in gasification installation, the drying operation utilizing cost of energy high can be saved solid is separated with water.
When the current with medium purity are for washing out ashes, additional fresh water cost can be saved and there is the further processing cost of water of medium purity.
Accompanying drawing explanation
Further feature of the present invention, advantage and possible application also can from hereafter obtaining the description of exemplary embodiment and accompanying drawing.Described and/or shown all features or formed theme of the present invention itself with arbitrary combination, it is independent of the content in quoting in claim or they follow-up.
In the accompanying drawings:
Fig. 1 illustrates the schema with the traditional gasification method of waste water aftertreatment according to prior art;
Fig. 2 schematically shows the schema according to method of the present invention.
Embodiment
In ordinary method as shown in Figure 1, solid to guide in gasifying reactor 10 via pipeline 1 and oxygen guides via pipeline 2.Steam is fed in reactor 10 via another pipeline identical or unshowned.Gas cooler 20 is supplied to from reactor 10 via pipeline 14 by reacting the gaseous mixture formed.Take out the crude synthetic gas obtained via pipeline 21 from this gas cooler.The liquid stream obtained is supplied to gas/liquid tripping device 23 via pipeline 22.This liquid stream guides to ammonia recovery unit 25 from gas/liquid tripping device via pipeline 24.Can arrange between gas/liquid tripping device 23 and ammonia recovery unit 25 process (not shown in figure 1).
Aqueous liquid stream is transferred to water treatment device 30 from ammonia recovery unit 25 via pipeline 26.On the one hand, moisture waste water is discharged from described water treatment device via pipeline 31 and may be processed into and waste water can be disposed.Take out stream via pipeline 32, this stream comprises most of solid particulate and is therefore also called slag stream.The stream comprising solid is supplied to moisture eliminator 33, and the water comprised in this moisture eliminator is evaporated by supply energy and spilt in air.Then the slag of drying such as can be transported to disposal site.
Ashes via pipeline 11 from gasifying reactor 10 (particularly when it is fixed bed gasification reactor) discharge and be supplied to other ash treatment device 12.In order to conveying solid substance ashes, by so-called supplementary feed, ashes stream can be flowed.Supplementary feed is fed to other ash treatment device 12 from source via pipeline 40.Then flowable ashes take out via pipeline 13.
In this process, the water obtained from waste water after-treatment device is disposed as waste water, but can not be recycled in process.As an alternative, at other position feeding fresh waters of this process.
Fig. 2 illustrates the configuration according to method of the present invention with schema, and solid wherein to be gasified is supplied to gasifying reactor 10 via pipeline 1 equally and oxygen supplies via pipeline 2.Ashes to take out via pipeline 11 from gasifying reactor 10 and are supplied to another ash treatment device 12.Then ashes take out from this other ash treatment device via pipeline 13.
In illustrated embodiment, gasifier 10 is designed to fixed-bed reactor and comprises the rectilinear reactor of the general cylindrical with outer water jacket.Coal or biomass guide to through chute (sluice) from top and are present in the solid dispenser of inside reactor, form fixed bed thus, this fixed bed is installed on the rotary grate (rotarygrate) of the lower region being arranged in reactor 10.Oxygen and steam also spray from this lower region.Due to the hot gas risen, the desorb of the gas of the coal adopted or the drying of biomass and institute's physical adsorption occurs in the top of gasifier 10.Reaction zone is positioned at below drying zone, and the degassed of coal or biomass occurs in the top of reaction zone.In reaction zone, there is actual gasification according to Boudouard reaction in coal or biomass after degassing.In foot district subsequently, there is the burning of coal or biomass and water-gas reaction and water gas shift reaction.The ashes obtained fall through grid and discharge further from that.Take out via the venting hole be arranged on above fixed bed with the hot gas guided with the coal fallen from top or the reverse adverse current of biomass.
The gaseous mixture obtained by gasification reaction to be taken out from reactor 10 via pipeline 14 and is supplied to water cooler 20.Obtain crude synthetic gas due to cooling, this crude synthetic gas takes out via pipeline 21.Aqueous liquid stream flow in gas-liquid separator (tripping device) 23 via pipeline 22.Certainly it is also envisaged that, only being realized by the condensation in gas cooler 20 of gas and liquid.
The liquid obtained is recycled to ammonia recovery unit 25 from the gas-liquid separator 23 that can be formed with condenser or droplet separator via pipeline 24.Can arrange between gas/liquid tripping device 23 and ammonia recovery unit 25 process (not shown in Fig. 2).Then pipeline 26 is introduced into water treatment device 30 from ammonia recovery unit 25.The current obtained in water treatment device 30 are divided into three streams.There is flowing through of highest purity and be supplied to unshowned vapour generator by pipeline 31.Then the steam produced in water treatment device 30 be used as such as heating the thermal barrier of educt in actual gasification, or produce for the energy in downstream turbine.In principle, also can imagine current are fed in cooling loop as refrigerant.The other unshowned refining plant of this stream may be necessary.
Flowing through of medium purity guides to other ash treatment device 12 by pipeline 37 and be used as liquid agent in ash treatment device 12.Therefore the introducing of supplementary feed can fully be saved.It is possible that the stream that also can be the medium purity in pipeline 37 arranges other water-purification plant 38.
Stream with most of solid is finally transmitted back in gasifier via pipeline 36.When reactor 10 is designed to fixed-bed reactor, it is recommended that the stream with solid is sprayed onto fixed bed from top.Thus, can save power consumption and therefore expensive solid drying.In addition, therefore the valuable product still comprised can be supplied to gasifier.
Utilize the method, can solids gasification be provided, can not waste water be obtained in the method.
List of numerals
1,2 pipelines
10 gasifying reactors
11 pipelines
12 other ash treatment devices
13,14 pipelines
20 water coolers
21,22 pipelines
23 tripping devices
24 pipelines
25 ammonia recovery units
26 pipelines
30 water after-treatment devices
31,32 pipelines
33 solid drying devices
34-37 pipeline
38 water after-treatment devices
40 pipelines.

Claims (6)

1. the equipment for making carbonaceous solids gasify, this equipment has gasifying reactor (10), tripping device (23) and water-purification plant (30), and described in described gasifying reactor, solid is converted into CO and H at least in part 2, aqueous liquid stream is separated from the crude synthesis gas obtained by described gasification in described tripping device (23), described aqueous stream is purified in described water-purification plant, the feature of described equipment is, described water-purification plant (30) is designed so that described aqueous stream is separated into three streams with different purity, and described water-purification plant (30) is connected with steam purifier via pipeline (31), and/or via pipeline (37) and solids slurry gasifying device, preferably other ash treatment device (12) or the pipeline for soup compound led in described reactor (10) connect, and/or be connected with described gasifying reactor (10) via pipeline (36).
2. equipment according to claim 1, is characterized in that, described tripping device (23) is condenser or droplet separator.
3. equipment according to claim 1, is characterized in that, described gasifying reactor (10) is fixed-bed reactor.
4. equipment according to claim 1, is characterized in that, described steam purifier comprises vapour generator.
5. equipment according to claim 4, is characterized in that, described vapour generator is connected with gasifying reactor (10) via the pipeline guided to by produced steam in gasifying reactor (10).
6. equipment according to claim 4, is characterized in that, described vapour generator is connected to downstream turbine via the pipeline produced steam being guided to downstream turbine.
CN201390000581.8U 2012-07-03 2013-04-23 Be used for making pneumatolytic equipment of carbon containing solid Expired - Lifetime CN204803273U (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102012013139.9A DE102012013139B4 (en) 2012-07-03 2012-07-03 Process and device for the gasification of solids
DE102012013139.9 2012-07-03
PCT/EP2013/058337 WO2014005738A1 (en) 2012-07-03 2013-04-23 Process and apparatus for the gasification of solids

Publications (1)

Publication Number Publication Date
CN204803273U true CN204803273U (en) 2015-11-25

Family

ID=48236894

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201390000581.8U Expired - Lifetime CN204803273U (en) 2012-07-03 2013-04-23 Be used for making pneumatolytic equipment of carbon containing solid

Country Status (9)

Country Link
KR (1) KR102038725B1 (en)
CN (1) CN204803273U (en)
AU (1) AU2013286304B2 (en)
DE (1) DE102012013139B4 (en)
EA (1) EA029238B1 (en)
IN (1) IN2014MN01869A (en)
UA (1) UA114198C2 (en)
WO (1) WO2014005738A1 (en)
ZA (1) ZA201406985B (en)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN114702987A (en) * 2022-04-18 2022-07-05 李冶 Pure oxygen gasification device and method

Family Cites Families (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4222847A (en) 1978-12-15 1980-09-16 Gulf Oil Corporation Coal liquefaction process with improved slurry recycle system
DE3207779A1 (en) 1982-03-04 1983-09-08 Metallgesellschaft Ag, 6000 Frankfurt Process for the treatment of water-containing condensate from the cooling of the crude gas of coal pressure gasification
DD224611A5 (en) 1984-09-06 1985-07-10 British Gas Corp COAL GASIFICATION PROCESS
DE3515484A1 (en) 1985-04-30 1986-10-30 Metallgesellschaft Ag, 6000 Frankfurt METHOD FOR TREATING CONDENSATE FROM THE PRODUCT GAS OF GASIFYING SOLID FUELS
GB8630047D0 (en) 1986-12-16 1987-01-28 British Gas Plc Purification of effluent liquors
DE4107109C1 (en) 1991-03-06 1992-10-08 Metallgesellschaft Ag, 6000 Frankfurt, De Environmentally friendly purificn. of crude gas - by cooling to contain condensate, sepg. condensate and evaporating to obtain saline soln. which is combusted and condensate stream which is added to pure gas
US5586510A (en) 1994-03-16 1996-12-24 Cement Industry Environment Consortium Method and system for controlling pollutant emissions in combustion operations
US6610112B1 (en) * 1999-12-07 2003-08-26 Texaco Inc. Method for oil gasification
DE102007035301B4 (en) * 2007-07-27 2009-04-30 Lurgi Gmbh Process and device for the utilization of brine obtained in the biological treatment of gas condensate
US8992641B2 (en) * 2007-10-26 2015-03-31 General Electric Company Fuel feed system for a gasifier
US20090188867A1 (en) * 2008-01-30 2009-07-30 Dinh-Cuong Vuong Methods and systems for processing waste water
US8048311B2 (en) * 2009-01-06 2011-11-01 General Electric Company Methods and systems for zero discharge water treatment
US20110259014A1 (en) * 2010-04-23 2011-10-27 General Electric Company Refinery residuals processing for integrated power, water, and chemical products

Also Published As

Publication number Publication date
AU2013286304A1 (en) 2014-11-06
IN2014MN01869A (en) 2015-07-03
KR20150027062A (en) 2015-03-11
KR102038725B1 (en) 2019-10-30
ZA201406985B (en) 2015-11-25
EA029238B1 (en) 2018-02-28
EA201401126A1 (en) 2015-01-30
UA114198C2 (en) 2017-05-10
DE102012013139A1 (en) 2014-01-09
AU2013286304B2 (en) 2018-02-22
DE102012013139B4 (en) 2022-05-05
WO2014005738A1 (en) 2014-01-09

Similar Documents

Publication Publication Date Title
RU2516533C2 (en) Method and device for obtaining synthesis-gas with low content of resins from biomass
JP2010024448A (en) Systems and methods for producing substitute natural gas
KR101668549B1 (en) Wastewater treatment system and combined power generation equipment
AU2008207372B2 (en) Method and installation for the purification of gas
CZ285404B6 (en) Process of partial oxidation of hydrocarbon fuel, connected with generation of electric power
KR20160018484A (en) Solid fuel staged gasification-combustion dual-bed polygeneration system and method
US9381446B2 (en) System for deaeration in a flash vessel
US20200190613A1 (en) Plant and method for the thermal treatment of solids
KR101401472B1 (en) Two-stage biomass gasifier having nickel distributor plate and biomass gasifier apparatus having the same
CN106318417A (en) Method and system for the manufacture of bio-methane and eco-methane
CN104428401A (en) Two stage gasification with dual quench
WO2014070420A1 (en) Systems and methods for producing substitute natural gas
CN104711025A (en) Gasifier cooling system
CN115321630B (en) Method and system for producing hydrogen by coal grading utilization and wastewater zero discharge coupling
CN107474859B (en) Coal pyrolysis gasification process coupling device and method thereof
CN204803273U (en) Be used for making pneumatolytic equipment of carbon containing solid
CN103237874A (en) Soot water cleaning by means of pressure filtration
JP2001354975A (en) Coal gasification and ash fusion furnace, and composite electricity generation system
US8506765B2 (en) Device and method for thermal decomposition of organic materials
JP2020055946A (en) Gasification gas production apparatus, and production method of gasification gas
CN102264874A (en) Tar-free gasification system and process
JP5332367B2 (en) Tar removal device
KR101753046B1 (en) Recycling organic compounds from gasifier syngas condensate
CN105820844A (en) Process and plant for the production and further treatment of fuel gas
CN204918509U (en) Desorption and recovery unit of macromolecule organic matter among coal -to -synthesis gas

Legal Events

Date Code Title Description
C14 Grant of patent or utility model
GR01 Patent grant
CX01 Expiry of patent term
CX01 Expiry of patent term

Granted publication date: 20151125