CN108795500A - A kind of gasification system and technique of high efficient heat recovery - Google Patents
A kind of gasification system and technique of high efficient heat recovery Download PDFInfo
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- CN108795500A CN108795500A CN201810952011.8A CN201810952011A CN108795500A CN 108795500 A CN108795500 A CN 108795500A CN 201810952011 A CN201810952011 A CN 201810952011A CN 108795500 A CN108795500 A CN 108795500A
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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
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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
- C10J3/72—Other features
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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
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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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
- C10J3/72—Other features
- C10J3/86—Other features combined with waste-heat boilers
-
- 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
- C10J2300/12—Heating the gasifier
- C10J2300/1269—Heating the gasifier by radiating device, e.g. radiant tubes
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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
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
- C10J2300/1615—Stripping
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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
- C10J2300/1687—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
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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
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
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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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
This application provides a kind of gasification systems of high efficient heat recovery, including gasification furnace, it is provided with injection apparatus on the indoor heat-transfer surface of radiation heat transfer of gasification furnace, is formed close to the low-temperature space of heat-transfer surface and positioned at core high-temperature region of the low-temperature space far from the heat-transfer surface side；Gas solid separation and cold grey equipment, setting is connected to the syngas outlet of the gasification furnace；Convective heat transfer device, sensible heat for recycling synthesis gas simultaneously generate power steam；Gas scrubbing system, including the Venturi scrubber and scrubbing tower that are arranged in series；Black water treatment system, including the primary flash device and two-stage flash device that are arranged in series.The application additionally provides the gasification process of high efficient heat recovery simultaneously, application scheme uses the radiation heat transfer room of border area temperature control technique, you can the safety for ensureing heat exchanger tube ensures that heat recovery efficiency higher under high radiance, saturated vapor yield is high, equipment volume smaller.
Description
Technical field
The invention belongs to synthesis gas technical fields, and in particular to, can be high using chemical products, fuel gas and IGCC as target
The gasification system and technique of effect recycling thermal energy.
Background technology
Producing synthesis gas using carbonaceous materials such as coal, oil, coal tars as raw material, (main component is CO and H2) gasification technology,
As the important means of fossil feedstock clean utilization, it is widely used to the fields such as combustion gas, synthesis gas, IGCC.In gasification reaction
In the process, the chemical energy of carbon raw material is largely converted into the chemical energy of synthesis gas, but still has about 20% chemical energy to be converted into
The sensible heat of synthesis gas and lime-ash, so as to cause thermal loss.Recycling and the utilization ratio for how improving this part sensible heat, to chemical industry
Device produce and it is energy-saving significant.
Currently, to gasification furnace generate high-temperature synthesis gas heat recovery technique there are mainly two types of, one is by quick
Sensible heat in high-temperature synthesis gas is transferred in Heisui River by cooling means, then recycling and the synthesis of heat are carried out to the Heisui River compared with low temperature
It utilizes, one is utilize the high-temperature position thermal energy in waste heat boiler recycling synthesis gas.
The first technique be represented as GE companies water-coal-slurry it is water-water chilling technology, in the process, gasification furnace production
Raw high-temperature synthesis gas (being less than 1400 DEG C) is cooled to rapidly 230~250 DEG C, the synthesis gas after cooling after a large amount of water coolings
Washed dedusting (temperature is further reduced to 210~240 DEG C) is sent out afterwards.Solid content in cooling water and cleaning dust water is higher,
It is referred to as Heisui River, the sensible heat of synthesis gas largely enters in Heisui River.Heisui River enters flash distillation plant and carries out multistage flash distillation, flashes off
For directly or indirectly being heated to Heisui River, residual steam then recycles after cooling water cooling some vapor.This water Quench
Technique has the advantages that easy to operate, but the high-temperature position thermal energy in technique is largely converted to low temperature heat energy, energy utilization efficiency
Relatively low, cooling water consumption is big, and since lime-ash fully enters in water, and water system internal circulating load is big, and power consumption is higher.
Second of technique is mainly the following：First, using shell gasification technology as representative, the technology is by synthesis gas in gas
Change furnace roof portion to mix with low-temperature circulating gas, temperature enters the pot that gives up and exchanges heat after being down to 900 DEG C or less, heat exchange is with heat convection
It is main, but because in gas entrained with granule content it is higher, useless pot easily occurs blocking and wear phenomena, and synthesis gas goes out after useless pot using flying
Grey filter carries out gas solid separation, and the dry ash isolated carries out air lift and cooling using high pressure nitrogen, and the gasification technology is because using
Dry method ash disposal has the advantages that high pressure usage on black water is simple, internal circulating load is small, but the flying dust removing system that dry method ash disposal uses is more
Complexity, operation difficulty is high, and the consumption of high pressure nitrogen is big, and simultaneously synthesizing gas water-gas ratio is low, it is more difficult to reach the life of chemical products
Production requires.In addition to shell gasification technology, the prior art also has using GE pot destroying process as the technology of representative, by the way that radiation waste is arranged
Heat in pot section and the useless pot section recycling synthesis gas of convection current, but the useless pot of convection current is also easy to produce fouling phenomenon, it is difficult to ensure that long period is steady
Determine service requirement.
Chinese patent document CN104017606B is on the basis of circulating air Quench thinking, it is proposed that a kind of coal water slurry gasification
Process system, it is intended to solve the problems, such as that a large amount of thermal energy of synthesis gas in coal-water slurry gasification system are irretrievable.Gasification furnace is
Uplink structure, the high-temperature gas of combustor exit, with after low-temperature circulating gas hybrid cooling, (overheat in tedge into heat exchanger
Device) saturated vapor from drum is overheated.Subsequent synthesis gas enters the second cyclone dust collectors, carries out first gas-solid point
From.Then, synthesis gas enters cooling device (containing superheater and two saturated steam generators), continues to recycle the heat in synthesis gas
Amount.Low temperature synthesis gas after cooling enters the first cyclone dust collectors, carries out secondary gas solid separation, then remove and close through ceramic filter
At the solid particle of the overwhelming majority in gas.The low temperature synthesis gas come out from ceramic filter, a part are passed through as Quench gas
Compressor returns to gasification furnace, and a part is sent out after washing.The dry ash that two stage cyclone is collected is sent into ash can and cools down and drop through buck
It is discharged into dragveyer after pressure.Multiple dross cooling components are set inside aforesaid heat exchangers and cooling device, it can be by table in heat exchanging chamber
The lime-ash in face scrapes, and the obstruction of heat exchanger is caused to avoid lime-ash accumulation.But in the technique, two level whirlwind is set to heat exchanger
It is very high into the granule density in the synthesis gas of heat exchanger after (superheater), it is possible to occurring what heat exchanger abrasion blocked
Situation.It is dynamic component to scrape slag cooling component, and working environment is severe, high failure rate.In addition, being swashed using cooling syngas pressurized circulation
Cold method, because there are a large amount of CO in coal water slurry gasification synthesis gas2And vapor, combustor exit tolerance are that shell vaporizer goes out
About 1.2 times of implication amount, while the cycle synthesis gas temperature for Quench leads to recycle gas compressor pressure compared with Shell technology higher
Contracting amount is much larger than Shell technology, and compressor operating temperature more increases, energy consumption higher.
The patent CN1037503C of Texaco Development Corporation discloses a kind of prepare and cools down and clean synthesis gas to remove
The method of the particulate material of entrainment, this method include flash distillation, deaerate, the energy efficient filtration of gas cooling and washings.To high temperature
The cooling of gas synthesis gas refers to a) water Quench and is in direct contact cooling and b) two kinds of indirect heat exchange (radiation and/or convection current cooling)
Method, wherein high-temperature synthesis gas is cooled down using a) method, the sensible heat of high-temperature synthesis gas largely enters water at low temperature
In, energy dissipation is serious.High-temperature synthesis gas is cooled down using b) method, because granule content is high in synthesis gas, convection current is given up pot
Abrasion and dust stratification problem are serious, then device long-period stable operation can be caused difficult.The Heisui River that high-temperature synthesis gas generates can pass through
Three stages of flashing is de-gassed, specially：Primary flash steam is steamed by grey water heater indirect heat exchange buck, two-stage flash
Vapour is in direct contact the oxygen dissolved in removal buck in oxygen-eliminating device with buck, and the steam of three stages of flashing is all with cooling water cooling
But.In commercial Application, since synthesis gas high temperature sensible heat largely enters in Heisui River, black water discharge amount is big, and system will often use
Low-temperature heat quantity in 3-4 grades of flash system recycling Heisui River, system configuration are complicated.Simultaneously as containing a large amount of in primary flash vapour
Sour gas (H2S and CO2Deng) and buck in concentration of suspension, basicity and hardness it is all very high, grey water heater corrosion and scaling is asked
Topic protrudes, equipment and materials somewhat expensive and it is difficult to ensure that long-period stable operation, operating cost height.Final stage flash-off steam amount is big,
All using cooling water cooling, cooling water consumption is big.
In addition to above-mentioned cooling means, United States Patent (USP) US4859213 also discloses a kind of related synthesis gas and prepares and purification work
Process system, the high-temperature synthesis gas in the system are mixed with the low temperature synthesis gas from recycle gas compressor first, mixed temperature
Degree should be down to that can be such that the fly ash granule of melting cures, and gaseous mixture entrainment fly ash granule initially enters useless pot and carries out heat recovery, so
Enter in dry ash separation equipment (such as cyclone separator) afterwards and isolate most of fine ash particle, last gas enter the system that washes into
The washing cooling of one step, most obtains the required product gas of downstream user after cooling heat transferring and sour gas remove afterwards.Cooling lime-ash
After removing the sour gas wherein dissolved using gas stripping process with the Heisui River washed, it can be recycled.The system is using cycle
The method of gas Quench+useless pot recycling heat, can convert synthesis gas high temperature position thermal energy to power steam, useful work efficiency
Height, but had the following problems in commercial Application：1) it is that high-temperature synthesis gas temperature is made to be down to preference temperature, requires supplementation with a large amount of
Circulating air, recycle gas compressor costliness high failure rate, and power consumption are high；2) synthesis gas needs Quench to entering the pots that give up after 900 DEG C or less,
Based on heat convection, because granule content is higher in gas, easily causes useless pot and block and denude；3) solid separation is in industry is answered
Generally use ceramic filter, fragile and cost are high.Flying dust after separation need to consume a large amount of high pressure nitrogens carry out air lifts and
It is cooling.Entire flying dust removes system complex, and operation difficulty is high, and high pressure nitrogen consumption is big.
Invention content
What the present invention solved is recycling and the utilization ratio of the sensible heat of synthesis gas gasification process and system in the prior art
Low, useless pot abrasion situation seriously leads to the technical issues of short service life, flying dust removing system complex, and then providing one kind can
It significantly reduces the sensible heat into Heisui River, improve pot service efficiency of giving up, the synthesis gas gasification system that flying dust removing system is simplified and work
Skill.
The present invention solve the technical solution that uses of above-mentioned technical problem for：
A kind of gasification system of high efficient heat recovery, including：It is used to prepare synthesis gas and carries out the gasification furnace of radiation heat transfer,
The gasification furnace includes vaporizer and the radiation heat transfer room positioned at the vaporizer downstream, in the indoor heat exchange of the radiation heat transfer
It is provided with injection apparatus on face, is formed close to the low-temperature space of heat-transfer surface and positioned at the low-temperature space far from the heat-transfer surface side
Core high-temperature region is provided with Quench collection slag device, the Quench collection slag device in the downstream of the low-temperature space and core high-temperature region
Inside there is Quench liquid, the Quench collection slag device is provided with black water discharge mouth；Gas solid separation and cold grey equipment, with the gasification furnace
Syngas outlet connection setting；Convective heat transfer device is connected to the gas vent of the gas solid separation and cooling equipment, is used for
It recycles the sensible heat of synthesis gas and generates steam；Gas scrubbing system is connected to setting with the gas vent of the convective heat transfer device,
Including the Venturi scrubber and scrubbing tower being arranged in series, the scrubbing tower is provided with black water discharge mouth；Black water treatment system, packet
Include the primary flash device being arranged in series and two-stage flash device, the black water discharge of the Quench collection slag device and the scrubbing tower
Mouth connect setting with the primary flash device.
The gas solid separation and cooling equipment include cyclone separator.
The convective heat transfer device includes superheater, and water cooling is provided on the heat-transfer surface of the vaporizer and radiation heat transfer room
The steam (vapor) outlet of heat-exchanger rig, the water cooling heat-exchanger rig is connected to setting with the superheater, and the synthesis gas enters the mistake
Hot device exchanges heat with the steam, and the steam that the water cooling heat-exchanger rig comes out is heated to be superheated steam.
The convective heat transfer device includes the superheater being arranged in series, multistage saturated steam generator and boiler water preheating
Device, the synthesis gas come out by the superheater sequentially enter the multistage saturated steam generator and boiler water preheater.
It is provided with and respectively communicated with condensation separating unit with the gas vent of the primary flash device and two-stage flash device,
The sour gas outlet of the condensation separating unit is connect with Sour gas disposal device；It is connected to and sets with the primary flash device
The liquid outlet for the condensation separating unit set is connected to oxygen-eliminating device；The two-stage flash device and with the two-stage flash device
The liquid outlet for being connected to the condensation separating unit of setting is connected to subsider, the liquid outlet of the subsider and the deoxygenation
Device connection setting and the solids outlet port of the subsider are connected with filter device.
A kind of gasification process of high efficient heat recovery, including：(1) synthesis gas is sent into spoke by vaporizing system for synthesis gas
It penetrates Heat Room to exchange heat, injection apparatus is provided on the heat-transfer surface of the radiation heat transfer room, the injection apparatus sprays fluid,
It is formed close to the low-temperature space of heat-transfer surface and positioned at core high-temperature region of the low-temperature space far from the heat-transfer surface side, the synthesis
Gas temperature after the radiation heat transfer room exchanges heat is down to 700 DEG C or more and is discharged, using Quench liquid to the high-temperature ash in synthesis gas
Quench is carried out, Heisui River discharge is formed；(2) gas solid separation is carried out to the synthesis gas after the radiation heat transfer room exchanges heat, to separation
The fine ash gone out carries out cooling treatment；(3) heat convection processing is carried out to the synthesis gas isolated in step (2), recycles synthesis gas
Sensible heat and generate steam；(4) to heat convection in step (3), treated that synthesis gas washs, and cleaning solution forms Heisui River
Discharge；(5) double flash evaporation processing is carried out to the Heisui River being discharged in step (1) and step (4).
Synthesis gas washing to granule content is less than or equal to 1mg/Nm in step (4)3。
The temperature of low-temperature space described in step (1) is less than 900 DEG C, and the temperature of the core high-temperature region is at 900 DEG C or more.
In step (2) to the synthesis gas carry out gas solid separation, by the synthesis gas grain diameter control less than
Or it is equal in the range of 5 μm.
The cooling treatment to the fine ash is realized using dry method mode in step (2).
The heat of heat and radiation heat transfer indoor synthesis gas that synthesis gas generation is prepared in step (1) is by heat-transfer surface to water
Cooling medium carries out heating and generates steam；The synthesis gas and the steam are subjected to heat convection in step (3), by the steaming
It is 4.0-12MPa, the superheated steam that temperature is 320-540 DEG C that vapour, which is heated into pressure,.
Condensation separation, the sour gas isolated are carried out to the gas generated in double flash evaporation processing procedure in step (5)
The Sour gas disposal device for sending downstream, to after primary flash condensation and separation of liquid carry out deoxygenation processing；After two-stage flash
Condensation and separation of liquid and two-stage flash after remaining liq after settlement treatment, then deoxygenation processing is carried out, to settlement treatment
The solid of generation is filtered.
The gasification system and its technique of high efficient heat recovery in the application, advantage are：
(1) gasification furnace in the application mode, using the radiation heat transfer room of border area temperature control technique, you can ensure heat exchanger tube
Safety ensures that heat recovery efficiency higher under high radiance, and saturated vapor yield is high, equipment volume smaller；Compared to
Using the heat reclamation device of whole spray cooling mode, the recuperation of heat of the radiation heat transfer room of border area temperature control technique is used in the application
10-50% can be improved in rate.
The application further makes to enter Heisui River system using the high-temperature residual heat in radiation+convective heat transfer device recycling synthesis gas
Sensible heat in system is reduced, and compared with water chilling process, the sensible heat being transferred in Heisui River reduces about 49%, and black water flash system is negative
Lotus significantly reduces, it is only necessary to configure double flash evaporation system.Primary flash removes the sour gas dissolved in Heisui River, two-stage flash
Reduce Heisui River temperature.The application is entered because 90% fine ash is recycled in the form of dry ash in Heisui River using the cold grey flow of dry method
Total ash quantity is only the 45% of water chilling process, then Heisui River internal circulating load is only the 50% of water chilling process, and Heisui River takes away sensible heat and is about
The 51% of water chilling process, circulating cooling water consumption reduce about 50%.
(2) by be arranged cyclonic separation cooling device, it can be achieved that in grading control synthesis gas particle size of fly ash and reduce particle
The purpose of concentration.Whirlwind can be level-one, or two level.Such as one cyclonic is used to configure, flying dust in controllable preparing synthetic gas
Grain size≤5 μm can effectively solve the problems, such as the useless pot abrasion of convection current in traditional process and block, ensure that the long period of device stablizes fortune
Row；Such as two level whirlwind is used to configure, then particle size of fly ash≤1 μm in controllable preparing synthetic gas, it is dense to further decrease particle in synthesis gas
Degree reduces scrubbing tower ash disposal load and Heisui River concentration, improves water quality, reduces wastewater discharge.As selectable embodiment,
Gas-solid separating device can also be other separation methods such as ceramic filter, sintered metal filter, electrostatic precipitator.
The application is further limited carries out gas solid separation and cooling using dry method mode, system configuration and easy to operate, if
Standby investment is small, and it is low to share engineering consumption.Cyclone separator inner wall sets water cooling coil pipe, you can protects whirlwind outer wall not overtemperature, and can
Waste heat in output saturated vapor recovery section synthesis gas.
(3) when the convective heat transfer device in the application only configures superheater, it may make synthesis gas that there is certain water
Gas ratio, the requirement for meeting downstream to do chemical products as target；The convective heat transfer device is configured to superheater+multistage saturation and steams
When vapour generator+boiler water heater, then the waste heat in high-temperature synthesis gas can be recycled to greatest extent, under the synthesis gas of output meets
Trip is to be fuel gas or IGCC as the requirement of target.
(4) system and technique described herein have high power steam output.When the convective heat transfer device only configures
When superheater, per 1000Nm3(CO+H2) 0.5-0.65 tons of superheated steams can be sent outside；When the convective heat transfer device is configured to overheat
When device+multistage saturated steam generator+boiler water heater, per 1000Nm3(CO+H2) 0.7-0.8 tons of superheated steams can be sent outside.
In order to make the gasification system of high efficient heat recovery of the present invention and the technical solution of technique be more clearly understood,
Below in conjunction with specific drawings and examples, the present invention will be described in further detail.
Description of the drawings
It is the flow diagram of the gasification system of the present invention for being used to prepare downstream chemical products as shown in Figure 1；
It is the structural schematic diagram of the gasification furnace in gasification system of the present invention as shown in Figure 2；
It is illustrated in figure 3 the structural schematic diagram in the section at the inner cylinder of radiation heat transfer room of the present invention；
It is illustrated in figure 4 the structural schematic diagram in the section at the laryngeal inlet of heat-exchanger rig of the present invention；
It is that the flow of the gasification system of the present invention for being used to prepare downstream fuel gas or IGCC products is shown as shown in Figure 5
It is intended to.
Wherein, reference numeral is：
1- gasification furnaces；11- vaporizers；The feed(raw material)inlets 111-；112- laryngeal inlets；The second injection apparatus of 113-；
12- radiation heat transfers room；
The first injection apparatus of 121-；122- third injection apparatus；124- outer barrels；125- radiation heat transfers room exports；In 126-
Cylinder；
13- slag baths；14- slag breakers；15- dreg-locking hoppers；
2- gas solid separations and cold grey equipment；21- cyclone separators；3- convective heat transfer devices；31- superheaters；32- multistages are full
And steam generator；33- boiler water preheaters；41- Venturi scrubbers；42- scrubbing towers；51- primary flash devices；52- bis-
Grade flash distillation plant；61- is connected to the condensation separating unit after primary flash device；62- oxygen-eliminating devices；63- is connected to two-stage flash
Condensation separating unit after device；64- subsiders；65- ash water tanks；66- filter devices.
Specific implementation mode
Embodiment 1
A kind of gasification system of high efficient heat recovery is present embodiments provided, can be used for preparing the chemical products in downstream, such as
Shown in Fig. 1, the gasification system includes：It is used to prepare synthesis gas and carries out the gasification furnace 1 of radiation heat transfer, the gasification furnace 1 wraps
Vaporizer 11 and radiation heat transfer room 12 are included, gasification furnace 1 described in the present embodiment is using 12 one of vaporizer 11 and radiation heat transfer room
The structure of setting, as shown in Figure 2.
Radiation heat transfer room 12 described in the present embodiment is arranged in the lower section of the vaporizer 11, at the top of vaporizer 11
It is provided with feed(raw material)inlet 111, the radiation heat transfer room 12 includes the inner cylinder 126 being arranged in shell and outer barrel 124；The inner cylinder
126 inner side and outer side wall surface and the interior sidewall surface of outer barrel 124 are heat-transfer surface, in the vaporizer 11 and radiation heat transfer room 12
Heat-transfer surface on be provided with water cooling heat-exchanger rig, the water cooling heat-exchanger rig described in present embodiment be water cooling tube, the gasification
Heat in room 11 and radiation heat transfer room 12 is exchanged heat by heat-transfer surface and the water cooling medium in water cooling tube, the water cooling tube
Interior water cooling medium evaporates to form steam, and the water cooling medium is using boiler water.
The inner cylinder 126 in the present embodiment and outer barrel 124 are cylindrical tube, as selectable embodiment,
The inner cylinder 126 may be alternatively provided as the cylinder that section is rectangular or other arbitrary shapes with outer barrel 124.In the inner cylinder 126
Top is provided with radiation heat transfer chamber inlet, and the radiation heat transfer chamber inlet is arranged with 11 outlet of the vaporizer；Described
Be provided with the first injection apparatus 121 on the heat-transfer surface of the upstream of inner cylinder 126, formed close to the heat-transfer surface low-temperature space and be located at
Low-temperature space is far from the core high-temperature region that the heat-transfer surface side is inside, due to the heat exchange of inner cylinder 126 described in present embodiment
Face is cylinder, therefore the core high-temperature region formed is located at the centre position in cylinder.First injection apparatus 121 preferably the
One nozzle sets, what the first jet group surround the heat-transfer surface of the upstream of the inner cylinder 126 is arranged for one week, and can be flowed along fluid
Multilayer or single layer is arranged in direction, and the fluid flow direction in present embodiment is from top to bottom.First is stated in present embodiment
Nozzle sets setting haves three layers, and adjacent 2 layers of nozzle is using being staggered, as shown in figure 3, multiple nozzles in every layer of nozzle are uniformly set
It sets, the radius of spray d of each nozzle in every layer of nozzle1More than 0 and less than the equivalent radius of inner cylinder at nozzle place, as excellent
The embodiment of choosing, the radius of spray d of each nozzle1More than 0 and less than the equivalent radius of inner cylinder 126 at nozzle place
60%, it is highly preferred that the radius of spray d of each nozzle1More than 0 and less than the equivalent radius of inner cylinder 126 at nozzle place
30%, to be conducive to improve the volume of core high-temperature region；The fluid stream that each nozzle in every layer of nozzle sprays is in distance
Heat-transfer surface position the first vertical range d where it1The fluid stream that place is sprayed with the adjacent nozzle positioned at same layer converges, and described the
One vertical range d1Radius of spray rs more than 0 and less than nozzle1.As selectable embodiment, between layers described
Noninterlace arrangement mode can also be used in nozzle；Non-homogeneous setting can also be used in multiple nozzles in every layer of nozzle, between layers
The fluid stream that ejects of the nozzle can converge, can also not converge mutually.In present embodiment, what distributed nozzle sprayed
Fluid forms one and is effectively isolated, to close to forming low-temperature space at heat-transfer surface.Into low-temperature space grey solid impurity particle through cooling
After lose viscosity, the grit that is difficult to clean off will not be formed in wall surface；Meanwhile core high-temperature region still keeps 900 DEG C or more of high temperature,
To keep higher radiation heat transfer ability.Because the Radiant exothermicity of core high-temperature region accounts for 12 total heat exchange amount of radiation heat transfer room
Most of, relative to synthesis gas entirety cool-down method, the method for border area cooling, core high temperature in the present invention can be carried effectively
Shoot high heat exchange amount.
As preferred embodiment, the inlet of the radiation heat transfer room 12 or the upstream of entrance are provided with the second spray
Injection device 113, second injection apparatus 113 are preferably second nozzle group.The second nozzle group can be arranged in the spoke
The inlet of Heat Room 12 is penetrated, can also be arranged in the upstream of the entrance, i.e., the described vaporizer 11 and the radiation heat transfer room
On laryngeal inlet 112 between 12 entrances.Second injection apparatus 113 is preferably second nozzle group, as shown in figure 4, described
The radius of spray rs of nozzle in second nozzle group2More than 50% (i.e. 50%R of the radius at the laryngeal inlet 1122) it is less than institute
State the radius R at laryngeal inlet 1122, single layer or multilayer, each nozzle of each layer of nozzle can be arranged in the second nozzle group
The fluid stream of ejection is in the second vertical range of heat-transfer surface d where it2The stream that place is sprayed with the adjacent nozzle positioned at same layer
Body stream converges, the distance d2Less than the radius of spray of nozzle.To realize the cooling of global sections second nozzle group edge
The circumferential direction of the laryngeal inlet 112 is uniformly arranged.
Fluid channel is formed between inner cylinder 126 described in the present embodiment and outer barrel 124, the fluid is by the inner cylinder 126
Downstream, that is, inner cylinder 126 bottom enter the fluid channel.It is located at first injection apparatus in the inner cylinder 126
Third injection apparatus 122 is additionally provided on the internal face in 121 downstream, the third injection apparatus 122 is third nozzle sets, institute
The radius of spray for stating each nozzle in third nozzle sets is 50%R~90%R, and wherein R is the inner cylinder 126 of nozzle position
Equivalent radius.
The 4th injection apparatus is additionally provided on the fluid channel, the 4th injection apparatus is preferably the 4th nozzle
Group, the 4th nozzle sets are distributed on the outside wall surface of the inner cylinder 126 or the internal face of the corresponding outer barrel 124, described
4th nozzle sets are arranged close to the bottom end of the inner cylinder 126 and outer barrel 124；In the outer barrel positioned at the 4th nozzle sets downstream
Radiation heat transfer room outlet 125 is provided on 124.
The fluid that first jet group, second nozzle group, third nozzle sets and the 4th nozzle sets in the present embodiment spray is adopted
Coolant liquid, specially boiler water, as selectable embodiment, the fluid may be nitrogen, carbon dioxide,
The combination of any one or more in synthesis gas after cooling, vapor, water.
Gasification furnace 1 in the present embodiment is provided with Quench collection on the synthesis gas flow path of the radiation heat transfer room 12
Slag device, the effect of Quench collection slag device are that pairing carries out water Quench at the high-temperature ash in gas, to by it from synthesis gas
Middle removal.The Quench collection slag device is arranged under the low-temperature space and core high-temperature region that first injection apparatus 121 is formed
Trip.The Quench collection slag device described in present embodiment is changed using slag bath 13, the setting of the slag bath 13 in the radiation
The bottom in hot cell 12 has Quench liquid in the slag bath 13, and the synthesis gas is transferred when entering outer barrel 124 by inner cylinder 126,
High-temperature ash enters slag bath 13 under the effect of gravity, is quickly quenched liquid cooling but, the slag bath 13 is provided with black water discharge mouth.
Gasification system described in the present embodiment is additionally provided with：
Gas solid separation and cold grey equipment 2, setting is connected to the syngas outlet of the gasification furnace 1；Described in the present embodiment
Gas solid separation and cooling equipment include cyclone separator 21, as selectable embodiment, in addition to cyclone separator 21, gas-solid
Separator can also be other separators such as ceramic filter, sintered metal filter, electrostatic precipitator.
Convective heat transfer device 3 is connected to the gas vent of the cyclone separator 21, for recycling the sensible heat of synthesis gas simultaneously
Generate power steam；Convective heat transfer device 3 described in the present embodiment is superheater 31, the water cooling heat-exchanger rig of the gasification furnace 1
Steam (vapor) outlet be connected to setting with the superheater 31, the synthesis gas is then changed into the superheater 31 with the steam
The steam that the water cooling heat-exchanger rig comes out is heated to be superheated steam by heat.
Gas scrubbing system is connected to setting with the gas vent of the convective heat transfer device 3, including the literary mound being arranged in series
In washer 41 and scrubbing tower 42；
Black water treatment system, including the primary flash device 51 and two-stage flash device 52 that are arranged in series, the gasification furnace 1
With the black water discharge mouth of the scrubbing tower 42 setting is connect with the primary flash device 51.With the primary flash device 51 and
The gas vent of two-stage flash device 52 is provided with and respectively communicated with condensation separating unit 61,63, the acid of the condensation separating unit
Property gas vent connect with Sour gas disposal device, the Sour gas disposal device to the sour gas outlet discharge
Sour gas is handled, and as selectable embodiment, burning processing can be used；It is connected to the primary flash device 51
The liquid outlet of the condensation separating unit of setting is connected to oxygen-eliminating device 62；The two-stage flash device 52 and with the two level dodge
The liquid outlet for steaming the condensation separating unit of the connection setting of device 52 is connected to subsider 64, the liquid discharge of the subsider 64
Mouth is connected to setting with the oxygen-eliminating device 62, as preferred embodiment, between the subsider 64 and the oxygen-eliminating device 62
It is provided with the ash water tank 65 for working as a buffer, filter device is connected with the solids outlet port of the subsider 64
66, the liquid outlet of the filter device 66 is connected to setting with the subsider 64, is used for the reflux of partially liq.
As preferred embodiment, the liquid outlet of the oxygen-eliminating device 62 in the present embodiment is provided with and communicated with two-way pipeline,
It is wherein connected to all the way with scrubbing tower 42, for liquid reflux to scrubbing tower 42 to be used as cleaning solution；Another way is connected to slag bath 13,
It is sent into the Quench collection slag device after being boosted by pump, for supplementing the Quench liquid in slag bath 13, keeps the Quench in slag bath 13
Liquid maintains a certain amount.
The gasification process of high efficient heat recovery based on gasification system described in the present embodiment, includes the following steps：
(1) gasifying agent and oxidant are sent into vaporizer 11 carry out gasification reaction and generate synthesis gas, wherein gasifying agent be containing
Carbon fuel, the oxidant are oxygen-containing gas and steam；Synthesis gas is entered by laryngeal inlet 112 in the radiation heat transfer room 12
Cylinder 126 is cooled down during entrance using second nozzle group injection fluid in advance, and control enters radiation heat transfer room 12
The temperature of fluid in inner cylinder 126 is not higher than 1500 DEG C；Synthesis gas enters the inner cylinder 126, is sprayed using the first injection apparatus 121
Jet body keeps the temperature of the low-temperature space of the radiation heat transfer room 12 to be less than 900 DEG C, and the temperature of core high-temperature region is 900
DEG C or more, to ensure efficient heat exchange efficiency.The equivalent radius of the wherein described core high-temperature region accounts for the spoke of its position
Penetrate the 30%~95% of the equivalent radius of Heat Room 12, and further preferably 30~60%.It is high by the low-temperature space and core
The fluid that warm area continues traveling downwardly cools down under the further jet-action of third injection apparatus 122, so that fluid is cut
Face temperature integrally reduces, and then reduces viscosity, prevents particle from being touched with wall surface when entering outer barrel 124 by the turning of inner cylinder 126
Bonding is hit, further sprays cooling into after between the inner cylinder and outer barrel 124, then by the 4th nozzle sets, is made not fully
Cooling grey solid impurity particle further cools down before colliding wall surface, is adhered to reducing or preventing.In the radiation heat transfer room 12,
Decline with the gas temperature of synthesis gas, the melt cinder in synthesis gas cures rapidly, and big grey solid impurity particle falls into bottom slag bath 13, passes through
Slag breaker 14, dreg-locking hopper 15, dragveyer discharge, remainder form Heisui River discharge.
(2) gas solid separation is carried out to the synthesis gas after the radiation heat transfer room 12 exchanges heat using cyclone separator 21, it will
Grain diameter in the synthesis gas controls in the range of less than or equal to 5 μm；To whirlwind in the way of dry colling
The high temperature dry ash that separator 21 is isolated carries out cooling treatment, and the dry colling refers to utilizing gas, recirculated water, desalted water etc.
Heat convection is carried out to high temperature dry ash as cooling medium, what this mode can go out cyclonic separation accounts for the thin of fine ash total amount 90%
Ash is recycled in the form of dry ash, while can further recycle the energy in high temperature dry ash, and the energy of recycling can further integrate profit
With such as desalted water of heat can be used as drum moisturizing, heat recirculated water can be as hot water uses, hot gas can be used for powder in factory
Material carries out heating or dry use.
(3) heat convection processing is carried out to the synthesis gas isolated in step (2) using superheater 31, synthesis gas was used as
Heat medium in hot device 31 carries out Overheating Treatment to the steam that gasification furnace 1 generates, and the steam, which is heated into pressure, is
4.0-12MPa, the high-quality superheated steam that temperature is 320-540 DEG C, to recycle the sensible heat of synthesis gas and generate high-quality power
Steam, present embodiment setting superheater 31 carry out heat exchange processing, and the synthesis gas come out by superheater 31 can be used for downstream preparation
Chemical products.
(4) utilize Venturi scrubber 41 and scrubbing tower 42 to treated the synthesis gas of heat convection in step (4) successively
It is washed, synthesis gas washing to granule content is less than or equal to 1mg/Nm3, washings then formed Heisui River discharge；
(5) double flash evaporation processing is carried out to the Heisui River generated in step (1) and step (4), utilizes condensation separating unit pair
The gas generated in double flash evaporation processing procedure carries out condensation separation, burning processing is carried out to the sour gas isolated, by level-one
After flash distillation condensation and separation of liquid be sent into oxygen-eliminating device 62 carry out deoxygenation processing；After two-stage flash condensation and separation of liquid and two
Grade flash distillation after remaining liq be then introduced into subsider 64, the supernatant liquor after settlement treatment be re-fed into the oxygen-eliminating device 62 into
Row deoxygenation is handled, and the sedimentation solid portion that settlement treatment generates then is sent into filter device 66 and is filtered, and the filtrate of generation is filtered
It is back to subsider 64 again；The liquid reflux that oxygen-eliminating device 62 comes out in the present embodiment realizes water to scrubbing tower 42 and slag bath 13
It recycles；The liquid of subsider discharge, a part are sent into oxygen-eliminating device, and a part sends locked slag bucket back to, for promoting deslagging, one
Divide and forms waste water discharge to balance the salinity dissolved in ash water system.
Embodiment 2
A kind of gasification system of high efficient heat recovery is present embodiments provided, can be used for preparing the fuel gas or IGCC in downstream
Product, as shown in figure 5, the gasification system includes：
It is used to prepare synthesis gas and carries out the gasification furnace 1 of radiation heat transfer, the 1 same embodiment of gasification furnace described in the present embodiment
1。
Gas solid separation and cold grey equipment 2, setting is connected to the syngas outlet of the gasification furnace 1；Described in the present embodiment
Gas solid separation and cooling equipment include cyclone separator 21, and the present embodiment is configured using two level whirlwind, is flown in controllable preparing synthetic gas
Grey grain size≤1 μm.
Convective heat transfer device 3 is connected to the gas vent of the cyclone separator 21, for recycling the sensible heat of synthesis gas simultaneously
Generate power steam；Convective heat transfer device 3 described in the present embodiment is the superheater 31 being arranged in series, multistage saturated vapor generation
Device 32 and boiler water preheater 33.The steam (vapor) outlet of the water cooling heat-exchanger rig of gasification furnace 1 described in the present embodiment and the overheat
The connection setting of device 31, the synthesis gas then exchange heat with the steam into the superheater 31, the water cooling are exchanged heat and is filled
The steam for setting out is heated to be superheated steam, and the synthesis gas sequentially enters multistage saturation and steams again after being come out by the superheater 31
Vapour generator 32 and boiler water preheater 33, for generating saturated vapor and being preheated to boiler water, to further recycle
Heat in synthesis gas, wherein preheating after boiler water be used as gasification furnace 1 in water cooling medium and injection apparatus spray it is cold
But liquid；The multistage saturated steam generator 32 is suitable for using two level to any one in level Four saturated steam generator.
Gas scrubbing system is connected to setting with the gas vent of the convective heat transfer device 3, including the literary mound being arranged in series
In washer 41 and scrubbing tower 42, to complete heat convection synthesis gas wash.
Black water treatment system, including the primary flash device 51 and two-stage flash device 52 that are arranged in series, the gasification furnace 1
With the black water discharge mouth of the scrubbing tower 42 setting is connect with the primary flash device 51.With the primary flash device 51 and
The gas vent of two-stage flash device 52 is provided with and respectively communicated with condensation separating unit, the sour gas of the condensation separating unit
Outlet is connect with Sour gas disposal device；The liquid discharge of the condensation separating unit of setting is connected to the primary flash device 51
Mouth is connected to oxygen-eliminating device 62；The two-stage flash device 52 and the condensation separation that setting is connected to the two-stage flash device 52
The liquid outlet of device is connected to subsider 64, and the liquid outlet of the subsider 64 is connected to setting with the oxygen-eliminating device 62,
As preferred embodiment, the buck for working as a buffer is provided between the subsider 64 and the oxygen-eliminating device 62
Slot 65 is connected with filter device 66, the liquid outlet of the filter device 66 with the solids outlet port of the subsider 64
It is connected to setting with the subsider 64, is used for the reflux of partially liq.
The gasification process of high efficient heat recovery based on gasification system described in the present embodiment, includes the following steps：
(1) gasifying agent and oxidant are sent into vaporizer 11 carry out gasification reaction and generate synthesis gas, wherein gasifying agent be containing
Carbon fuel, the oxidant are oxygen-containing gas and steam；Synthesis gas is entered by laryngeal inlet 112 in the radiation heat transfer room 12
Cylinder is cooled down during entrance using second nozzle group injection fluid in advance, and control is interior into radiation heat transfer room 12
The temperature of fluid in cylinder is not higher than 1500 DEG C；Synthesis gas enters the inner cylinder, sprays fluid using the first injection apparatus 121,
Keep the low-temperature space of the radiation heat transfer room 123 temperature be less than 900 DEG C, the temperature of core high-temperature region at 900 DEG C or more,
To ensure efficient heat exchange efficiency.The equivalent radius of the wherein described core high-temperature region accounts for the radiation heat transfer room of its position
The 30%~95% of 12 equivalent radius, and further preferably 30~60%.Continued by the low-temperature space and core high-temperature region
The fluid of downlink cools down under the further jet-action of third injection apparatus 122, so that fluid cross-section temperature is whole
Body reduces, and then reduces viscosity, prevents particle from colliding bonding with wall surface when entering outer barrel 124 by inner cylinder turning, enters
After between the inner cylinder and outer barrel 124, then by the 4th nozzle sets cooling is further sprayed, makes insufficient cooling lime-ash
Grain further cools down before colliding wall surface, is adhered to reducing or preventing.In the radiation heat transfer room 12, with synthesis gas
Gas temperature declines, and the melt cinder in synthesis gas cures rapidly, and big grey solid impurity particle falls into bottom slag bath 13, through slag breaker 14, slag
Lock hopper 15, dragveyer discharge, remainder form Heisui River.
(2) gas solid separation is carried out to the synthesis gas after the radiation heat transfer room 12 exchanges heat using cyclone separator 21, it will
Grain diameter in the synthesis gas controls in the range of less than or equal to 1 μm；It is thin to what is isolated in the way of dry method
Ash carries out cooling treatment, and the fine ash for accounting for fine ash total amount 90% is recycled in the form of dry ash.
(3) heat convection processing is carried out to the synthesis gas isolated in step (2) using superheater 31, by the synthesis gas
It is sequentially sent to superheater 31, multistage saturated steam generator 32 and boiler water preheater 33, synthesis gas is as superheater 31 and steams
Heat medium in vapour generator, boiler water preheater 33, for generating power steam, saturated vapor, and further to boiler
Water is preheated, to fully recycle the sensible heat of synthesis gas.Superheater 31 in the present embodiment steams gasification furnace 1 and multistage saturation
The steam that vapour generator 32 generates carries out Overheating Treatment, and it is 4.0-12MPa that the steam can be heated into pressure, and temperature is
320-540 DEG C of high-quality superheated steam.
(4) utilize Venturi scrubber 41 and scrubbing tower 42 to treated the synthesis gas of heat convection in step (4) successively
It is washed, synthesis gas washing to granule content is less than or equal to 1mg/Nm3, washings then form Heisui River.
(5) double flash evaporation processing is carried out to the Heisui River generated in step (1) and step (4), utilizes condensation separating unit pair
The gas generated in double flash evaporation processing procedure carries out condensation separation, burning processing is carried out to the sour gas isolated, by one
Grade flash distillation after condensation and separation of liquid be sent into oxygen-eliminating device 62 carry out deoxygenation processing；After two-stage flash condensation and separation of liquid with
Remaining liq after two-stage flash is then introduced into subsider 64, and the supernatant liquor after settlement treatment is re-fed into the oxygen-eliminating device 62
Deoxygenation processing is carried out, the sedimentation solid portion that settlement treatment generates then is sent into filter device 66 and is filtered, and the filter of generation is filtered
Liquid is back to subsider 64 again；The liquid reflux that oxygen-eliminating device 62 comes out in the present embodiment realizes water to scrubbing tower 42 and slag bath 13
Recycling.
Experimental example
Process system in the application can effectively recycle synthesis gas high temperature position thermal energy, with (CO+H2) quantum of output be
100,000Nm3Average reaction temperature in/h, vaporizer 11 be 1400 DEG C, year operating times be 8000 hours based on estimate
The output value in embodiment 1 and embodiment 2, the results are shown in table below：
Note：10MPag power steams price is based on 120 yuan/ton, and recirculated cooling water price is based on 0.1 yuan/ton.
Synthesis gas high temperature sensible heat is converted into the ratio of 10.0MPag grade power steams up to 50- as seen from the above table
70%.Use this technique that can produce 50-65 tons/h of 10.0MPag grade power steams (non-chemical products scheme is 70-80 tons/h),
Increase by ten thousand yuan of output value 4862-6302 (non-chemical products scheme is ten thousand yuan of 6778-7738) years, while circulating cooling water consumption is reduced
About 780 tons/h (non-chemical products scheme is 720 tons/h), can saving 620,000 yuan of expense year, (fuel gas or IGCC products schemes are
580000 yuan), economic benefit and energy conservation and consumption reduction effects are very significantly.
Several embodiments of the invention above described embodiment only expresses, the description thereof is more specific and detailed, but simultaneously
Cannot the limitation to the scope of the claims of the present invention therefore be interpreted as.It should be pointed out that for those of ordinary skill in the art
For, without departing from the inventive concept of the premise, various modifications and improvements can be made, these belong to the guarantor of the present invention
Protect range.Therefore, the protection domain of patent of the present invention should be subject to claim.
Claims (12)
1. a kind of gasification system of high efficient heat recovery, which is characterized in that including：
Be used to prepare synthesis gas and carry out radiation heat transfer gasification furnace, the gasification furnace include vaporizer and be located at the vaporizer
The radiation heat transfer room in downstream is provided with injection apparatus on the indoor heat-transfer surface of the radiation heat transfer, is formed close to heat-transfer surface
Low-temperature space and positioned at core high-temperature region of the low-temperature space far from the heat-transfer surface side, in the low-temperature space and core high-temperature region
Downstream be provided with Quench collection slag device, have Quench liquid in the Quench collection slag device, the Quench collection slag device is provided with
Black water discharge mouth；
Gas solid separation and cold grey equipment, setting is connected to the syngas outlet of the gasification furnace；
Convective heat transfer device is connected to, the sensible heat for recycling synthesis gas with the gas vent of the gas solid separation and cooling equipment
And generate steam；
Gas scrubbing system is connected to setting with the gas vent of the convective heat transfer device, including the venturi being arranged in series is washed
Device and scrubbing tower are washed, the scrubbing tower is provided with black water discharge mouth；
Black water treatment system, including the primary flash device and two-stage flash device that are arranged in series, the Quench collection slag device and
The black water discharge mouth of the scrubbing tower connect setting with the primary flash device.
2. the gasification system of high efficient heat recovery according to claim 1, which is characterized in that the gas solid separation and cooling
Equipment includes cyclone separator.
3. the gasification system of high efficient heat recovery according to claim 1 or 2, which is characterized in that the heat convection dress
It sets including superheater, water cooling heat-exchanger rig, the water cooling heat exchange is provided on the heat-transfer surface of the vaporizer and radiation heat transfer room
The steam (vapor) outlet of device is connected to setting with the superheater, and the synthesis gas is changed into the superheater with the steam
The steam that the water cooling heat-exchanger rig comes out is heated to be superheated steam by heat.
4. the gasification system of high efficient heat recovery according to claim 3, which is characterized in that the convective heat transfer device packet
Include the superheater being arranged in series, multistage saturated steam generator and boiler water preheater, the synthesis gas come out by the superheater
Sequentially enter the multistage saturated steam generator and boiler water preheater.
5. the gasification system of high efficient heat recovery according to claim 1 or 2 or 3 or 4, which is characterized in that with described one
The gas vent of grade flash distillation plant and two-stage flash device is provided with and respectively communicated with condensation separating unit, the condensation separating unit
Sour gas outlet connect with Sour gas disposal device；The condensation separating unit of setting is connected to the primary flash device
Liquid outlet be connected to oxygen-eliminating device；The two-stage flash device and the condensation point that setting is connected to the two-stage flash device
Liquid outlet from device is connected to subsider, the liquid outlet of the subsider be connected to the oxygen-eliminating device setting with it is described
The solids outlet port of subsider is connected with filter device.
6. a kind of gasification process of high efficient heat recovery, which is characterized in that including：
(1) synthesis gas is sent into radiation heat transfer room and exchanged heat by vaporizing system for synthesis gas, the heat exchange of the radiation heat transfer room
Injection apparatus is provided on face, the injection apparatus sprays fluid, is formed close to the low-temperature space of heat-transfer surface and positioned at the low temperature
Core high-temperature region of the area far from the heat-transfer surface side, synthesis gas temperature after the radiation heat transfer room exchanges heat are down to 700
DEG C or more be discharged, using Quench liquid in synthesis gas high-temperature ash carry out Quench, formed Heisui River discharge；
(2) gas solid separation is carried out to the synthesis gas after the radiation heat transfer room exchanges heat, cooling place is carried out to the fine ash isolated
Reason；
(3) heat convection processing is carried out to the synthesis gas isolated in step (2), recycles the sensible heat of synthesis gas and generates steam；
(4) to heat convection in step (3), treated that synthesis gas washs, and cleaning solution forms Heisui River discharge；
(5) double flash evaporation processing is carried out to the Heisui River being discharged in step (1) and step (4).
7. the gasification process of high efficient heat recovery according to claim 6, which is characterized in that by synthesis gas in step (4)
Washing to granule content is less than or equal to 1mg/Nm3。
8. the gasification process of the high efficient heat recovery described according to claim 6 or 7, which is characterized in that low described in step (1)
The temperature of warm area is less than 900 DEG C, and the temperature of the core high-temperature region is at 900 DEG C or more.
9. the gasification process of high efficient heat recovery according to claim 8, which is characterized in that the conjunction in step (2)
Gas solid separation is carried out at gas, the grain diameter in the synthesis gas is controlled in the range of less than or equal to 5 μm.
10. according to the gasification process of any high efficient heat recoveries of claim 6-9, which is characterized in that step is adopted in (2)
The cooling treatment to the fine ash is realized with dry method mode.
11. according to the gasification process of any high efficient heat recoveries of claim 6-10, which is characterized in that in step (1)
The heat of the heat and radiation heat transfer indoor synthesis gas that prepare synthesis gas generation heats water cooling medium by heat-transfer surface
Generate steam；The synthesis gas and the steam are subjected to heat convection in step (3), the steam, which is heated into pressure, is
4.0-12MPa, the superheated steam that temperature is 320-540 DEG C.
12. according to the gasification process of any high efficient heat recoveries of claim 6-11, which is characterized in that step (5)
The gas generated in middle double flash evaporation processing procedure carries out condensation separation, and the sour gas isolated is sent at the sour gas in downstream
Manage device, to after primary flash condensation and separation of liquid carry out deoxygenation processing；After two-stage flash condensation and separation of liquid with
Remaining liq after two-stage flash is after settlement treatment, then carries out deoxygenation processing, and the solid generated to settlement treatment is filtered.
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| PCT/CN2018/122283 WO2020037905A1 (en) | 2018-08-21 | 2018-12-20 | Gasification system and process for efficient heat energy recovery |
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| CN110345459A (en) * | 2019-07-10 | 2019-10-18 | 中海石油华鹤煤化有限公司 | A kind of coal slurry gasifier and high-pressure boiler coproduction steam enhancing device and method |
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