CN107001090A - With water process and the gasification system recycled - Google Patents
With water process and the gasification system recycled Download PDFInfo
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- CN107001090A CN107001090A CN201580067771.5A CN201580067771A CN107001090A CN 107001090 A CN107001090 A CN 107001090A CN 201580067771 A CN201580067771 A CN 201580067771A CN 107001090 A CN107001090 A CN 107001090A
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- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
- C02F1/5245—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents using basic salts, e.g. of aluminium and iron
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- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F1/54—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using organic material
- C02F1/56—Macromolecular compounds
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- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
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- 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
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
- C02F1/004—Processes for the treatment of water whereby the filtration technique is of importance using large scale industrial sized filters
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- 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
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/08—Thin film evaporation
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- 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
- C02F1/38—Treatment of water, waste water, or sewage by centrifugal separation
- C02F1/385—Treatment of water, waste water, or sewage by centrifugal separation by centrifuging suspensions
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- 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
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2301/00—General aspects of water treatment
- C02F2301/04—Flow arrangements
- C02F2301/046—Recirculation with an external loop
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- 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
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- 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
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A20/00—Water conservation; Efficient water supply; Efficient water use
- Y02A20/124—Water desalination
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Abstract
In gasification system, desalination unit is used to handle main grey current.Desalination unit is preferably evaporator.Desalination unit removes chloride, and producing, there is total dissolved solidss concentration to be 100ppm or lower main recycled grey water stream.In traditional gasification system, desalination unit replaces buck settler.Gasification system is run with 10% or lower water recirculation circuit blowdown ratio.
Description
Technical field
The application is related to water process and recycling in gasification system.
Background technology
In typical gasification, raw material such as coal is crushed and the reaction zone of gasifier is fed to.Air flow bed gas
Change system (entrained flow gasification system) can feed as dry powder or mix to form slurry with water
Size-reduced raw material.Other gasification systems such as fixed bed or fluidized system generally feed the size-reduced original as dry powder
Material.In the reaction region, raw material is heated with the oxygen of the amount of substoichiometric (sub-stoichiometric).Reaction produces conjunction
Into gas (synthesis gas is mainly made up of carbon monoxide and hydrogen), and clinker, cigarette ash and various pollutants.In typical gasification reaction
In device, reaction product enters the quenching area (quenching zone) of reactor, and they are contacted with water wherein.Reactor is produced
It is quenched water blowdown stream and synthesis gas.Synthesis gas flow to synthesis gas scrubber together with some pollutants from gasifier.Closing
Into in gas washing device, synthesis gas is contacted with washings.Micro-solid and volatile matter in washings entrainment synthesis gas.Synthesize air purge
Wash device and produce product syngas and synthesis gas scrubber blowdown stream.
Some water can be reclaimed from the synthesis gas scrubber blowdown in one or more flash chambers.Synthesis gas scrubber is let out
At least a portion of material, such as flash chamber bottom material, are considered as Heisui River.In the system that gasification reactor is quenched using water
In, some unvaporized raw materials can be extracted to carry solid together with some water from quenching water blowdown.It is quenched water blowdown
At least a portion be also regarded as Heisui River.Heisui River is generally handled to produce effluent in settler, and it can be described as buck.Buck
A part be returned to synthesis gas scrubber or gasifier, so as to form main water recirculation circuit.Another part of buck
Remove, and replaced with supplement water from system as buck blowdown stream, to prevent one or more pollutants in main water again
Excessive concentration in circulation loop.
Buck blowdown stream contains various pollutants, and must be discharged at it, be stored in brine pit or deep well disposal it
It is preceding to be handled, or be processed to produce the discharge of zero liquid.Some typical processing include ammonia stripping, the biology of organic matter and gone
Remove and solid- liquid separation, such as nanofiltration or counter-infiltration.Optionally, one or more of these process steps can produce warp
The water of processing, it can be returned to gasifier or synthesis gas scrubber in one or more supplement water recirculation circuits.Can
Settler bottom material is handled, this more water that can be recovered in supplement water recirculation circuit, or settler bottom material
Gasifier can be returned to as raw material, or both.
The content of the invention
This application describes gasification system and method with desalting steps in main water recirculation circuit.In Jiang Jingchu
The water of reason is recycled to before synthesis gas scrubber or gasifier or both, and processing Heisui River is optional in other pollutants to remove
Chloride and other dissolving solids.The total dissolved solidss for the water that desalting steps in main water recirculation circuit continue are excellent
Elect 100ppm as or less.The chloride concentration for the water that desalting steps in main water recirculation circuit continue is preferably
10ppm or less.In one example, desalting steps are provided by hot vaporizer.
The Heisui River of a) substantially all (for example, at least 80%), or b) the quenching water blowdown or c of most of (at least 50%))
One or more in the synthesis gas scrubber blowdown of most of (at least 50%) are with hot vaporizer or other desalination units
Main water recirculation circuit in handled.Water through desalination, the condensate liquid of Tathagata flash-pot, continuation is followed again in main water
In loop back path.The water handled in desalination unit preferably includes to be quenched water blowdown.
Evaporator or other desalination units are optionally the main usage on black water units of the solid for dissolving.In this meaning
On, desalination unit can be considered as replace traditional gasification system in Heisui River settler aspect, it is allowed to by settler (or other
Solid- liquid separation device) operation is designed primarily to for cigarette ash removal.Optionally, desalination unit may also allow for traditional gasification system
One or more of system flash chamber is omitted.Compared with settler, the construction and operation of evaporator are more expensive.It is probably
In this reason, evaporator is only considering processing buck blowdown before.It can return to even if from some water of buck blowdown processing
To gasification system, buck blowdown processing system is generally also not considered as the part of the main water recirculation circuit of gasification system.
In one embodiment, the Heisui River in desalination unit processing gasification system.
In one approach, chloride is removed in the recycling water from gasification system.For example, can be from desalination list
Chloride is removed in the blowdown stream of member.Chloride removal ratio may be selected, with maintain from the gasifier quenching in gasification system and/
Or the balance chloride level selected in the water of washer recycling.Selected balance chloride concentration can for 500ppm or
It is lower, such as in the range of 150 to 200 or 300ppm.Balance chloride concentration can be selected in the design of system, or
Person can be selected as setting value or other values in the controller or control process related to desalination unit.
When evaporator being added in main water recirculation circuit, main water recirculation circuit blowdown ratio reduction.To the greatest extent
Pipe blowdown ratio is reduced, but the balance chloride concentration in water loop is also reduced, because evaporator, which is produced, has the molten of high concentration
Solve the blowdown salt solution of solid.The chloride concentration reduced in main water recirculation circuit can reduce the fouling in gasification system
(scaling) and corrosion, and synthesis gas dew point is reduced.Supplement water the need for and processing water recirculation circuit blowdown cost
Both of which is reduced.In one embodiment, relative to the comparison system only with settler, the demand drop of gasification system supplement water
It is low more than 25%.
The gasification system described in this application is with the main water recirculation circuit blowdown ratio in 10% or less Heisui River
Operation.However, in main usage on black water stream, by using desalination unit, such as hot vaporizer, by main water recirculation circuit
In total dissolved solidss (TDS) concentration maintain 100ppm or lower.Being recycled to gasification reactor is used to be quenched water or synthesis
At least 1/3rd of the water of gas washing device or both, but optionally whole water of (such as 80% or more), with 100ppm or
Lower TDS concentration, or 10ppm or lower chloride concentration, or both.
Brief description of the drawings
Fig. 1 is the process chart of gasification system.
Embodiment
Fig. 1 shows gasification system 10.The system has the entrained flow gasifiers 12 for receiving oxygen A and slurry B.Oxygen A
Gasifier 12 is supplied to optionally as air with the amount of substoichiometric.Gasifier 12 can be for example at about 1250 DEG C to 1600 DEG C
Under, under the pressure of about 30 to 80 atmospheric pressure, and use the residence time operation of about 0.4 to 2 second.Slurry in shown example
Material B is the coal slurry by the way that coal C and water Q are fed into grinder 14, grinder discharge groove 16 and slurry tank 18 and produced.So
And, gasification system 10 is also configured to gasify any other hydrocarbon material, such as timber, waste plastics or petroleum coke.In addition, gasification
Device 12 can be fed with dry feedstock rather than slurry B.Alternately, fixed bed or fluidized-bed gasifier can be used, relative to gas
Fluidized bed gasification device, fixed bed or fluidized-bed gasifier are generally with dry feedstock and at relatively low temperatures and pressures, but longer
Residence time operation.Gasifier 12 produces synthesis gas E, quenching water blowdown R and gasifier bottom material D.Synthesis gas E is in synthesis
Handled in gas washing device 20, to produce product syngas F, it is generally further processed before as fuel.Synthesis
Gas washing device 20 also produces washer blowdown G.Gasifier bottom material D (or is in lock hopper (lockhopper) 28
Scraper bowl cabinet [bucket locker]) in handled, clinker H is separated with bottom water I.(it still has mixed with it clinker H
Some water closed) thick clinker J and fine slag K are further separated into by drag conveyor 30.In another option, gasifier 12
It can be combined with radiant type syngas cooler (RSC, Radiant Syngas Cooler).In general, leaving gasifier 12
Raw syngas can be cooled down by radiant type and/or convection type heat exchanger and/or by being directly quenched system, wherein by water
Or the recycling gas of cooling is injected into the Raw syngas of heat.Synthesis gas can be used for heat by one or more flash chambers
Reclaim and cooling syngas.
Quenching water blowdown R flows through high pressure flash groove 22 and low-pressure flashing tank 24 together with washer blowdown G.Flash drum bottom
Material S flows through vacuum flashing groove 26 with fine slag K (together with some mixed water), to form Heisui River L.In some feelings
Under condition, the second vacuum flashing groove can be added.Although some water are removed in flash tank 22 and flash tank 24, major part is (at least
50%, usually 80% or more) quenching water blowdown R and most of (at least 50%, usually 80% or more) washing
Device blowdown G is present in the L of Heisui River.Major part (at least 50%, usually 80% or more) water in clinker H exists in Heisui River
In L.In alternative solution, no more than the water (half of the combination i.e. no more than quenching water blowdown R and washer blowdown G of half
Water) in any single processing unit of Heisui River L upstreams remove.Therefore, Heisui River L is considered as in gasification system 10 main water again
The part of circulation loop.In shown gasification system 10, main water is recirculated back to route stream G, R, stream S between flash tank,
L, M, N, O and G, and intermediate treatment unit 20,12,2,24,26,30,34,38 and 40 are constituted.
Optionally, the processing Heisui River L in solid-liquid separator 30 (or referred to as flue-dust separator), to produce solid fraction M
With the Heisui River N of pretreatment, or referred to as buck.Solid-liquid separator 30 (if present) is mainly used in reclaiming cigarette ash or stove
Slag.Solid fraction M contains the little particle of clinker and cigarette ash, and it can add in slurry B to increase the generation of synthesis gas.If used
Solid-liquid separator 30, the then Heisui River N pre-processed preferably includes the Heisui River L of 80% or more, or 90% or more.Continuously exist
In main water recirculation circuit three/it is one or more, or optionally whole Heisui River N or L be fed into desalter 34.Desalination
Device 34 produces effluent O and salt solution P.
Solid-liquid separator 30 be preferably hydrocyclone or centrifuge, but be alternatively filter, gravity separator (or
Referred to as settler or clarifier) or axial separation device or other devices for producing dewatered solid cut M.Such as in hydrocyclone and
Between centrifuge, preferably hydrocyclone.Depending on the type of used solid-liquid separator 30, solid fraction M may
It is difficult to pump.In this case, solid fraction M can be transferred to cigarette ash groove 32 and be diluted with some effluents O.Then it can make
The cigarette ash Q of dilution is transported to grinder 14 to be incorporated into slurry B with shifting pump Q.Some effluents O can also be sent to enclosed type
Hopper 28.Flocculant or coagulating agent, such as 1-10ppm polymer flocculants can be added in solid-liquid separator 30 and located
The Heisui River L of reason.
Most of effluent O is optionally recycled to synthesis gas scrubber 20 after by deaerator 38 and heat exchanger 40
Or in gasifier 12.If all effluent O are by producing degassing effluent O desalter 34 (such as evaporator),
Deaerator 38 is not needed.Some effluents O can arrive gasifier 12 directly through or by synthesis gas scrubber 20, for use as gasification
Device quenching water U.By this way, effluent O replaces at least part material, such as the routine of the non-desalination buck from settler
/ 3rd of recycling are to whole.For the sufficient flow by desalter 34, gasification system 10 can be only needed in sedimentation
One vacuum flashing groove of device upstream.
Optionally, by-pass line V may be present around desalter 34.By-pass line V can have blowdown to export W and do not show
The various valves gone out.In an option, by-pass line 34 generally remains closing, but it is interim when needed open, to be desalination
Device 34 provides service.In another option, by-pass line V is used to provide and one or many in main water recirculation circuit
The parallel path of individual desalination unit 34.If for example, existing gasification system will be in main water recirculation circuit with parallel assembling
Two or three desalination units 34 transformed, then can be continuing with by-pass line V, and the desalination list of final number is only installed
Member 34 in some, i.e., one or two.After all desalination units 34 are installed, by-pass line V can be normally closed,
But it is interim when needed to open, to provide service for desalter 34, instead of the capacity for providing unnecessary desalination unit 34.
In another option, gasification system can normally be run in the case where only part Heisui River L or N is by desalter 34.Herein
In option, at least 1/3rd of Heisui River L or N, preferably at least half passes through desalter 34.Less than 1/3rd threshold values
Certain point, flow through the amount of the water of desalter 34 will not substantially influence recycle water pH or chloride concentration, and
It is not considered as the part of main water recirculation circuit.Heisui River L or N simultaneously flow through one or more desalters 34 and side wherein
In the case of the pipeline V of road or when Heisui River L or N simultaneously flow through one or more desalters 34 and by-pass line V, blowdown outlet
W is preferably remained turned-off so that all blowdowns from main water recirculation circuit are extracted as salt solution P.By this way, come
Still reclaimed from the blowdown of main water recirculation circuit with the chloride concentration higher than chloride concentration in Heisui River L or N, and institute
The supplement water volume needed is accordingly reduced.
In main water recirculation circuit have at least one desalter 34, together with or not together with by-pass line V, it is allowed to
The flowing in ratio or change by-pass line V for example, by changing effluent O and salt solution P, to adjust the chlorination in effluent O
Thing concentration.Desalter 34, especially evaporator, also assist in the ammonia density managed in main water recirculation circuit.In one kind
In method, the chloride level that regulation is flowed into the effluent O of synthesis gas scrubber 20, to provide within the required range, for example
Less than 250 DEG C, or the synthesis gas dew point (or referred to as hydrocarbon dew point) in the range of 230 DEG C to 240 DEG C.Synthesis gas dew point is with chlorine
Compound concentration and increase.Moderately low synthesis gas dew point is maintained for example to allow to make in synthesis gas scrubber 20 or miscellaneous part
With the alloy of lower cost.
Desalter 34 is preferably hot vaporizer.Evaporator can for for example with mechanical vapor compression (MVC,
Mechanical vapor compression) vertical tube falling film formula evaporator, or referred to as mechanical vapor recompression (MVR,
mechanical vapor recompression).Alternately, evaporator can be steam-powered evaporator, optionally employ
The exhaust steam of exhaust steam from gasification system 10, such as chuck around gasifier 12.Evaporator can use inoculation slurry
Technique (seeded slurry process) is operated, to reduce the fouling in evaporator.In an example of inoculation slurry methods
In, promote calcium sulphate crystal to be formed in evaporator.Evaporator can with calcium sulfate crystal seed be inoculated with, although or phrase be expressed as
" inoculation slurry ", even if being added without crystal seed, crystal also can be formed spontaneously by the compound in evaporator feedwater.In some feelings
Under condition, compound such as sodium sulphate or calcium chloride are added in the water in evaporator (such as by the way that compound is added in feedwater or
Add in evaporator pool), to change the relative concentration of calcium ion and sulfate ion to promote Crystallization.Carry out flash-pot
Effluent O is alternatively referred to as condensate liquid or distillate.Effluent O preferably has less than 100ppm total dissolved solidss (TDS) and small
In 10ppm, or the chloride less than 5ppm.Compared with conventional practice, the subchloride concentration in effluent O can allow in gasification
Less corrosion-resistant (and therefore relatively inexpensive) material is used in system 10.Compared with conventional practice, the perchloride in salt solution P is dense
Degree can allow to remove less blowdown (salt solution P) from main water recirculation circuit or allow to add corresponding less supplement water T.
Low TDS concentration can reduce the scale problems in gasification system 10.Including the overhead from flash tank 22,24 and 26
(overhead), despite optional, preferably all washer blowdown water or gasifier quenching water with less than 100ppm TDS and
Less than the recycling of 10ppm chlorides.
Bittern P preferably has for the 10% of Heisui River L, the Heisui River N of pretreatment or one or more flow velocitys in effluent O
Or less flow velocity.Flash tank 22,24 and 26 is individually optional.However, at least one flash tank can not be cold available for removal
Solidifying gas such as H2S.Salt solution P can be optionally dense in crystallizer (such as with forced-circulation evaporator), spray dryer, salt solution
Further handled in contracting device or other reductions or zero liquid discharge system.Alternately, can remove salt solution P is used to locate outside the venue
Put or further handle.Can design or actively control salt solution P flow velocitys or influence from desalter 34 remove chloride other
Parameter, is for example measured with providing in flash drum bottom material S, chloride concentration selected in effluent O or in water
Balance chloride concentration selected in recirculation circuit.Selected balance chloride concentration can be in 500ppm or lower, example
As in the range of 150 to 200 or 300ppm.Selected equilibrium concentration can be in the design and its operating process of gasification system 10
Realize, or selected equilibrium concentration can real-time implementation, such as by the way that chloride concentration sensor is connected to for desalination
The controller of device 34 passes through the otherwise operation of regulation desalter 34 as needed so that salt solution P removes enough
Chloride so that balance chloride concentration keep below the value of selection or in the range of including selected value.
In the modeled example of gasification system as shown in Figure 1, Heisui River has 120m3The flow velocity of/hour.Heisui River is pre-
Processing is to remove cigarette ash, and it removes 10m3The 10% solid cigarette ash mixture of/hour.In vertically moving membrane formula mechanical vapor compression
(MVR) remaining pretreated Heisui River is handled in evaporator.Produce 105m3The distillate of/hour is used to return to synthesis air purge
Wash device or gasifier.Distillate has about 50ppm TDS concentration, and the chloride concentration and pH less than 1ppm are 8.5.Produce
5m3The blowdown of/hour, TDS concentration and pH with about 75,000ppm are about 5.Balance chlorine in low-pressure flashing tank bottom material
Compound concentration is less than 150ppm.The system being modeled is general as shown in fig. 1.
Sample based on the processing Heisui River in laboratory scale centrifuge removes the factor come the cigarette ash of forecast model.Heisui River from
Coal gasification apparatus are obtained, and coal slurry is supplied to entrained flow gasifiers by coal gasification apparatus.Heisui River contain gasifier quenching water blowdown and
The mixture of synthesis gas scrubber blowdown.Centrifuge is run with 500rpm, with 5 minute residence time, without chemical addition agent.
Optionally, coagulating agent or flocculant can be used for reducing the residence time.Polymer flocculants are preferred, without additional
Metal salt coagulating agent or flocculant.For example, in some later experiments, by PAMC compound add from
In Heisui River in scheming.Similarly, when handling Heisui River in another solid- liquid separation device, coagulating agent or flocculation can be added
Agent, preferred polymers flocculant.It is preferred that flocculant be cationic polyacrylamide flocculant agent, for example can be from GE Water＆
The BetzDearborn CP1153 that Process Technologies are obtained.Dosage can be 1 to 10ppm or 3-5ppm polymerization
Thing flocculant.In laboratory scale centrifuge as described above Heisui River test in, without flocculant, in centrifuge with
After 1000rpm is handled 20 minutes, the effluent of clarification has 58NTU turbidity.For 3ppm CP1153, in centrifuge with
After 1000rpm is handled 3 minutes, the effluent of clarification has about 9NTU turbidity.For 5ppm CP1153, in centrifuge with
After 1000rpm is handled 3 minutes, the effluent of clarification has about 4NTU turbidity.For with 3ppm CP1153 and 5ppm CP1153
Total suspended solid (TSS) concentration of the clarified effluent of the Heisui River sample centrifuged together is about 1mg/L.
The performance of evaporator factor of the model is to be based on distilling above-mentioned centrifuge outflow in bench scale distillation unit
Thing, to produce the recovery of 95% distillate.Sodium sulphate is added in centrifuge effluent, fed water with simulating to add in sodium sulphate
In, this slurry hot vaporizer being inoculated with for calcium sulfate will be appropriate.The pH of centrifuge effluent is 7.4.In 95% time
After receipts, the pH of the salt solution in the bottom of cucurbit is about 5.
Based on the ammonium concentration in evaporator feedwater, expected ammonia loss has caused salt after being reclaimed 95% in still-process
The pH of water decreases below 3.This prompting will need expensive resistant material in evaporator, and fouling can make evaporator
Operation is unreliable.However, by being tested with 18 days of inoculation slurry evaporator, the pH of salt solution is kept stable at about 5, and does not see
Observe uncommon incrustation.
It is uncertain that why the pH of salt solution is maintained at about 5.A kind of possibility is that the formic acid in evaporator feedwater is produced in salt solution
Raw ammonium formate (NH4COOH), the amount of volatile ammonia steam and is therefore reduced.Another possibility be initially in feedwater or add
Enter and combined with the sodium for simulating inoculation slurry methods with formates or other compounds, to produce buffer compounds.Because reaction production
Thing is quenched in the range of about 250 to 300 degrees Celsius, thus formates in gasifier by coal (and other possible raw materials)
Gasify and produce.Correspondingly, the present inventor's prediction reduction in pH during distilling change (i.e. it was observed that salt solution pH for 5
The salt solution pH for not being prediction is 3) to be likely to the part that gasifier quenching water at least in is the Heisui River handled in evaporator
It is any during occur.
Salt solution is further boiled, and produces the main loose white solid being made up of calcium sulfate, this prompting salt solution
It is suitable for the inoculation slurry evaporator process in evaporator, and effluent brine can be crystallized in zero liquid discharge system.
In the comparative example, equipment for gasification is modeled, wherein the centrifuge and evaporator in above-mentioned model are replaced
For other vacuum flashing groove and conventional settler.Settler produces the effluent with almost 300ppm chlorides and pH 7.
Buck blowdown speed is 27m3/ hour.Balance chloride concentration in low-pressure flashing tank bottom material is more than 250ppm.Compare and be
System needs about 40% more supplement water.
The written description discloses the present invention, including optimal mode using example, and also causes any technology in this area
Personnel can put into practice the present invention, including prepare and using any device or system and perform any method being incorporated to.The present invention
Patentable scope be defined by the claims, and may include other examples that those skilled in the art expect.If these
Other examples have has no different structural elements from the word language of claims, or if they include wanting with right
The word language of book is asked to have no the equivalent structural elements of essence difference, then they are it is contemplated that in the range of claims.
Claims (23)
1. a kind of method for handling the water in equipment for gasification, methods described comprises the steps：Make the master in the equipment for gasification
Want the synthesis gas scrubber blowdown in water recirculation circuit or be quenched water blowdown or both desalination, and the water through desalination is followed again
The synthesis gas scrubber or gasifier of ring to the equipment for gasification are quenched current.
2. according to the method described in claim 1, it is characterised in that at least half of the quenching water blowdown is desalination.
3. according to the method described in claim 1, it is characterised in that at least half of the synthesis gas scrubber blowdown is desalination
's.
4. according to the method described in claim 1, it is characterised in that be recycled to the synthesis gas scrubber or the gasifier
Being quenched the water through desalination of current has the chloride concentration for being less than 10ppm.
5. according to the method described in claim 1, it is characterised in that be recycled to the synthesis gas scrubber or the gasifier
The water through desalination there is 100ppm or lower total dissolved solidss concentration.
6. according to the method described in claim 1, it is characterised in that 80% or more produced in the equipment for gasification it is black
Water is desalination.
7. according to the method described in claim 1, it is characterised in that the desalination occurs in hot vaporizer.
8. according to the method described in claim 1, it is characterised in that the slurry operation of the hot vaporizer inoculation.
9. according to the method described in claim 1, it is characterised in that the hot vaporizer is run with calcium sulfate slurry.
The cigarette ash before 10. according to the method described in claim 1, methods described is additionally included in the desalting steps removes step
Suddenly, wherein the cigarette ash removal step includes adding polymer flocculants.
11. according to the method described in claim 1, it is characterised in that adjust to the feedwater of the desalting steps to promote sulfuric acid
Calcium Crystallization.
12. according to the method described in claim 1, it is characterised in that the feedwater to the desalting steps is quenched including gasifier
Water blowdown.
13. the step of according to the method described in claim 1, methods described includes adding sodium into the desalting steps.
14. according to the method described in claim 1, it is characterised in that the gasifier is entrained flow gasifiers.
15. according to the method described in claim 1, it is characterised in that the gasifier is supplied to coal.
16. according to the method described in claim 1, it is characterised in that the gasifier is supplied to coal slurry.
17. according to the method described in claim 1, methods described forms ammonium formate during being additionally included in the desalting steps.
18. a kind of gasification system, the gasification system has：
Main water recirculation circuit, its reclaimed water comes from gasifier or synthesis gas scrubber or both, and returns to the gas
Change device quenching water inlet or synthesis gas scrubber or both；And,
Desalination unit in the main water recirculation circuit.
19. gasification system according to claim 18, it is characterised in that the desalination unit includes hot vaporizer.
20. gasification system according to claim 18, it is characterised in that the gasifier is entrained flow gasifiers.
21. gasification system according to claim 20, it is characterised in that the gasifier receives coal, preferably coal slurry.
22. gasification system according to claim 18, it is characterised in that the desalination unit receives gasifier quenching water and let out
Material.
23. gasification system according to claim 18, it is characterised in that from the main water recirculation circuit at least
Most of blowdown is removed by the desalination unit.
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| IN6297/CHE/2014 | 2014-12-12 | ||
| IN6297CH2014 | 2014-12-12 | ||
| PCT/US2015/064897 WO2016094612A1 (en) | 2014-12-12 | 2015-12-10 | Gasification system with water treatment and reuse |
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| CN106946394A (en) * | 2017-05-05 | 2017-07-14 | 北京清创晋华科技有限公司 | The coal gasified black water and grey water treatment system and method for a kind of high heat organic efficiency |
| EP3674383A1 (en) * | 2018-12-28 | 2020-07-01 | Meva Energy AB | A biomass gasification system |
| EP4155260A1 (en) * | 2021-09-28 | 2023-03-29 | Aquafair AB | A hydrogen generation system and a method for generating hydrogen |
| US20230159328A1 (en) * | 2021-11-19 | 2023-05-25 | Air Products And Chemicals, Inc. | Gasification of high-ash feedstock |
| WO2023164077A1 (en) * | 2022-02-25 | 2023-08-31 | Sierra Energy | Syngas cleaning and soot recovery |
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| WO2016094612A1 (en) | 2016-06-16 |
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