CN108913208A - A kind of cold grey formula high efficient heat recovery gasification system of wet process and technique - Google Patents
A kind of cold grey formula high efficient heat recovery gasification system of wet process and technique Download PDFInfo
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- 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
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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
- C10J2300/12—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
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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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- 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
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Abstract
This application provides a kind of cold grey formula high efficient heat recovery gasification systems of wet process, including gasification furnace, it is provided with injection apparatus on the indoor heat-transfer surface of radiation heat transfer of gasification furnace, forms the core high-temperature region close to the low-temperature space of heat-transfer surface and positioned at the low-temperature space far from the heat-transfer surface side；Gas solid separation and the cold apparatus for ash of wet process, are connected to setting with the syngas outlet of the gasification furnace；Convective heat transfer device, for recycling the sensible heat of synthesis gas and generating power steam；Gas scrubbing system, including the Venturi scrubber and scrubbing tower being arranged in series；Black water treatment system, including the primary flash device and two-stage flash device being 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, that is, can guarantee the safety of heat exchanger tube, ensure that heat recovery efficiency is higher under high radiance, saturated vapor yield is high, and equipment volume is smaller.
Description
Technical field
The invention belongs to synthesis gas technical fields, and in particular to using chemical products, fuel gas and IGCC as target, use
The cold grey method of wet process can high efficiente callback thermal energy gasification system and technique.
Background technique
Producing synthesis gas using carbonaceous materials such as coal, petroleum, 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.The recycling and utilization efficiency for how improving this part sensible heat, to chemical industry
Device production and it is energy-saving significant.
Currently, one is by quick there are mainly two types of the heat recovery techniques of the high-temperature synthesis gas generated to gasification furnace
Sensible heat in high-temperature synthesis gas is transferred in Heisui River by cooling means, then the recycling and 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 company water-coal-slurry it is water-water chilling technology, in the process, gasification furnace produce
Raw high-temperature synthesis gas (being lower than 1400 DEG C) is cooled to rapidly 230~250 DEG C, the synthesis gas after cooling after a large amount of water are cooling
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,
The sensible heat in referred to as Heisui River, 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 is 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
Lower, cooling water consumption is big, and since lime-ash fully enters in water, water system internal circulating load is big, and power consumption is higher.
Second of technique is mainly the following：First is that the technology is by synthesis gas in gas using shell gasification technology as representative
Change furnace roof portion to mix with low-temperature circulating gas, temperature enters useless pot 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
It produces and requires.In addition to shell gasification technology, the prior art passes through setting radiation waste there are also using GE pot destroying process as the technology of representative
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 guarantee that long period is steady
Determine service requirement.
Chinese patent document CN104017606B proposes a kind of coal water slurry gasification on the basis of circulating air Quench thinking
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 is in tedge and after low-temperature circulating gas hybrid cooling, into heat exchanger (overheat
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, second 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 there is heat exchanger abrasion blocking
Situation.Scraping slag cooling component is dynamic 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 circulation synthesis gas temperature for Quench is higher compared with Shell technology, leads to recycle gas compressor pressure
Contracting amount is much larger than Shell technology, and compressor operating temperature is more increased, energy consumption is 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 washing water.To high temperature
The cooling of gas synthesis gas refers to a) water Quench and directly contacts cooling and b) two kinds of indirect heat exchange (radiation and/or convection current are 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 it is difficult to will lead to device long-period stable operation.The Heisui River that high-temperature synthesis gas generates can pass through
Three stages of flashing is de-gassed, specially：Primary flash steam is by indirect heat exchange buck, and two-stage flash steam is in oxygen-eliminating device
In the oxygen that dissolves in removal buck is directly contacted with buck, the steam of three stages of flashing is all cooled down with cooling water.It is answered in industry
In, since synthesis gas high temperature sensible heat largely enters in Heisui River, black water discharge amount is big, and system often will be using 3-4 grades of flash distillation systems
Low-temperature heat quantity in system recycling Heisui River, system configuration are complicated.Simultaneously as containing a large amount of sour gas (H in primary flash vapour2S
And CO2Deng) and buck in concentration of suspension, basicity and hardness it is all very high, grey water heater corrosion and scaling outstanding problem, equipment
Master Cost is expensive and it is difficult to ensure that long-period stable operation, operating cost are high.Final stage flash-off steam amount is big, all using cooling
Water is cooling, and 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 preparation 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 initially enter useless pot and carry out heat recovery down to the fly ash granule solidification that can make melting, gaseous mixture entrainment fly ash granule, 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 product gas required for 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 circulation
Gas Quench+useless pot recycling heat method, can convert power steam, useful work efficiency for synthesis gas high temperature position thermal energy
Height, but had the following problems in industrial application：1) it to make high-temperature synthesis gas temperature be down to preference temperature, requires supplementation with a large amount of
Circulating air, recycle gas compressor valuableness high failure rate, and power consumption are high；2) synthesis gas needs Quench to entering useless pots after 900 DEG C or less,
Based on heat convection, because granule content is higher in gas, useless pot is easily caused to block and denude；3) solid separation is in industry is answered
Ceramic filter is generallyd use, easy to damage and cost is 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.
Summary of the invention
The invention solves the recycling and utilization efficiency of the sensible heat of synthesis gas gasification process in the prior art and system
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
Significantly reduce synthesis that the sensible heat for entering Heisui River, the useless pot service efficiency of raising, flying dust removing system are simplified, using the cold ash of wet process
Gas gasification system and technique.
The present invention solve the technical solution that uses of above-mentioned technical problem for：
A kind of cold grey formula high efficient heat recovery gasification system of wet process, including：It is used to prepare synthesis gas and carries out radiation heat transfer
Gasification furnace, the gasification furnace includes vaporizer and positioned at the radiation heat transfer room in the vaporizer downstream, in the radiation heat transfer
It is provided with injection apparatus on indoor heat-transfer surface, formed close to the low-temperature space of heat-transfer surface and is changed positioned at the low-temperature space far from described
The core high-temperature region of hot face side is provided with Quench collection slag device, institute in the downstream of the low-temperature space and core high-temperature region
It states and has Quench liquid in Quench collection slag device, the Quench collection slag device is provided with black water discharge mouth；Gas solid separation and wet process are cold
Apparatus for ash is connected to setting with the syngas outlet of the gasification furnace, using the cold grey equipment of wet process to the dry ash after gas solid separation into
Row cooling, the cold grey equipment of the wet process are provided with black water discharge mouth；Convective heat transfer device, with the gas solid separation and cooling equipment
Gas vent connection, for recycling the sensible heat of synthesis gas and generating steam；Gas scrubbing system, with the convective heat transfer device
Gas vent be connected to setting, including the Venturi scrubber and scrubbing tower being arranged in series, the scrubbing tower be provided with Heisui River row
Put mouth；Black water treatment system, including the primary flash device and two-stage flash device being arranged in series, the Quench collection slag device,
The black water discharge mouth of the cold grey equipment of the wet process and the scrubbing tower connect setting with the primary flash device.
The gas solid separation and the cold apparatus for ash of wet process include the dry ash outlet company of cyclone separator and the cyclone separator
The cold grey equipment of the wet process of logical setting.
The convective heat transfer device includes superheater, is provided with water cooling on the heat-transfer surface of the vaporizer and radiation heat transfer room
Heat-exchanger rig, the steam (vapor) outlet of the water cooling heat-exchanger rig are 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 sequentially enters the multistage saturated steam generator and boiler water preheater by the synthesis gas that the superheater comes out.
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, is connected with filter device with the solids outlet port of the subsider.
A kind of cold grey formula high efficient heat recovery gasification process of wet process, including：(1) vaporizing system is for synthesis gas, by the synthesis
Pneumatic transmission enters radiation heat transfer room and exchanges heat, and injection apparatus, the injection apparatus are provided on the heat-transfer surface of the radiation heat transfer room
Fluid is sprayed, the core high temperature close to the low-temperature space of heat-transfer surface and positioned at the low-temperature space far from the heat-transfer surface side is formed
Area, 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 in synthesis gas
High-temperature ash carry out Quench, formed Heisui River discharge；(2) gas-solid point is carried out to the synthesis gas after the heat exchange of the radiation heat transfer room
From, using wet process to the high temperature dry ash spraying cooling liquid isolated, the high temperature dry ash is cooled down and formed Heisui River discharge；
(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) right
Treated that synthesis gas is washed for heat convection in step (3), and cleaning solution forms Heisui River discharge；(5) to step (1) and step
(2) and in step (4) Heisui River being discharged carries out double flash evaporation processing.
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.
Gas solid separation is carried out to the synthesis gas in step (2), the grain diameter control in the synthesis gas is being less than
Or it is equal in the range of 5 μm.
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,.
The gas generated in double flash evaporation treatment process in step (5) is condensed and separated, the sour gas isolated
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 cold grey formula high efficient heat recovery gasification system of wet process and technique, advantage in the application are：
(1) the gasification furnace in the application mode can guarantee heat exchanger tube using the radiation heat transfer room of border area temperature control technique
Safety, ensures that heat recovery efficiency is higher under high radiance, and saturated vapor yield is high, and equipment volume is smaller；Compared to
Using the heat recovery apparatus 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.
Using the high-temperature residual heat in useless pot recycling synthesis gas, reduce the sensible heat entered in the system of Heisui River, with water Quench stream
Journey is compared, and the sensible heat being transferred in Heisui River reduces about 15%, and black water flash system loading significantly reduces, it is only necessary to configure two-stage sudden strain of a muscle
Steaming system.Primary flash removes the sour gas dissolved in Heisui River, and two-stage flash reduces Heisui River temperature.With water chilling process
It compares, the gasification system that the application uses wet process cooling, gasification installation circulating cooling water consumption can reduce about 30%.
(2) by setting 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 second level.It is such as configured using one cyclonic, flying dust in controllable preparing synthetic gas
Partial size≤5 μm can effectively solve the problems, such as the useless pot abrasion of convection current and blocking in traditional process, guarantee that the long period of device stablizes fortune
Row；It is such as configured using second level whirlwind, 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 Heisui River concentration, improves water quality, reduces wastewater discharge.
The application further limits the cooling of the dry ash after carrying out gas solid separation using wet process mode, utilizes wet process cooling device
Cooling dry ash forms the Heisui River after Heisui River is discharged with gasification furnace, scrubbing tower and carries out flash distillation process jointly.
(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, every 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, every 1000Nm3(CO+H2) 0.7-0.8 tons of superheated steams can be sent outside.
In order to make the technical solution of the cold grey formula high efficient heat recovery gasification system of wet process of the present invention and technique more
Clear, below in conjunction with specific drawings and examples, the present invention will be described in further detail.
Detailed description of the invention
It is the cold grey formula high efficient heat recovery gas of the wet process of the present invention for being used to prepare downstream chemical products as shown in Figure 1
The flow diagram of change system；
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 the cold grey formula High Efficiency Thermal of the wet process for being used to prepare downstream fuel gas or IGCC product of the present invention as shown in Figure 5
The flow diagram of gasification system can be recycled.
Wherein, appended drawing reference is：
1- gasification furnace；11- vaporizer；The feed(raw material)inlet 111-；112- laryngeal inlet；The second injection apparatus of 113-；
12- radiation heat transfer room；
The first injection apparatus of 121-；122- third injection apparatus；124- outer cylinder；The outlet of 125- radiation heat transfer room；In 126-
Cylinder；
13- slag bath；14- slag breaker；15- dreg-locking hopper；
2- gas solid separation and cold grey equipment；21- cyclone separator；22- wet process cooling tank；3- convective heat transfer device；31- mistake
Hot device；32- multistage saturated steam generator；33- boiler water preheater；41- Venturi scrubber；42- scrubbing tower；51- level-one
Flash distillation plant；52- two-stage flash device；61- is connected to the condensation separating unit after primary flash device；62- oxygen-eliminating device；63-
Condensation separating unit after being connected to two-stage flash device；64- subsider；65- ash water tank；66- filter device.
Specific embodiment
Embodiment 1
A kind of cold grey formula high efficient heat recovery gasification system of wet process is present embodiments provided, can be used for preparing the chemical industry in downstream
Product, as shown in Figure 1, the gasification system includes：It is used to prepare synthesis gas and carries out the gasification furnace 1 of radiation heat transfer, the gas
Changing furnace 1 includes vaporizer 11 and radiation heat transfer room 12, and gasification furnace 1 described in the present embodiment uses vaporizer 11 and radiation heat transfer room
12 structures being wholely set, as shown in Figure 2.
The lower section of the vaporizer 11 is arranged in radiation heat transfer room 12 described in the present embodiment, at the top of vaporizer 11
It is provided with feed(raw material)inlet 111, the radiation heat transfer room 12 includes setting in the intracorporal inner cylinder 126 of shell and outer cylinder 124；The inner cylinder
126 inner side and outer side wall surface and the interior sidewall surface of outer cylinder 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, 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 cylinder 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 cylinder 124.In the inner cylinder 126
Top is provided with radiation heat transfer chamber inlet, and the radiation heat transfer chamber inlet and 11 outlet of vaporizer are arranged；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 heat-transfer surface side i.e. core high-temperature region of inside, the heat exchange of inner cylinder 126 as described in present embodiment
Face is cylinder, therefore the core high-temperature region formed is located at the intracorporal middle position of 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 flow 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 nozzle1Equivalent radius greater than 0 and less than inner cylinder at nozzle place, as excellent
The embodiment of choosing, the radius of spray d of each nozzle1Greater than 0 and it is 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 nozzle1Equivalent radius greater than 0 and less than inner cylinder 126 at nozzle place
30%, thus be conducive to improve core high-temperature region volume；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 it1Locate and fluid stream that the adjacent nozzle that is located on the same floor sprays converges, described the
One vertical range d1Radius of spray rs greater 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, thus 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 the total heat exchange amount in radiation heat transfer room 12
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 mentioned 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 set in the spoke
The inlet of Heat Room 12 is penetrated, also can be set 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 group2Greater 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, the settable single layer of the second nozzle group or multilayer, each nozzle of each layer of nozzle
The fluid stream of ejection is in the second vertical range of heat-transfer surface d where it2Locate and stream that the adjacent nozzle that is located on the same floor sprays
The convergence of body stream, 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 cylinder 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 inner wall 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 inner wall of the corresponding outer cylinder 124, described
4th nozzle sets are arranged close to the bottom end of the inner cylinder 126 and outer cylinder 124；In the outer cylinder for being located 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,
Synthesis gas after cooling, vapor, the combination of any one or more in 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, thus 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 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 cylinder 124 by inner cylinder 126,
High-temperature ash enters slag bath 13 under the effect of gravity, is quickly quenched liquid cooling but, and 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 the cold apparatus for ash 2 of wet process, the gas solid separation and the cold apparatus for ash 2 of wet process include cyclone separator 21 with
The cold grey equipment of the wet process of the dry ash outlet setting of the cyclone separator.As selectable embodiment, in addition to whirlwind
Separator 21, gas-solid separating device are also possible to other separation dresses such as ceramic filter, sintered metal filter, electrostatic precipitator
It sets.As selectable embodiment, the cold grey equipment of wet process described in the present embodiment is wet process cooling tank 22, cold in the wet process
But be provided with spray equipment in tank 22, be used for spraying cooling liquid, cool down to the high temperature dry ash, the coolant liquid sprayed out with
Heisui River is formed after dry ash mixing, is provided with black water discharge mouth on the wet process cooling tank 22.
Convective heat transfer device 3 is connected to, for recycling the sensible heat of synthesis gas simultaneously with the gas vent of the cyclone separator 21
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 being arranged in series, the gasification furnace 1
Setting is connect with the primary flash device 51 with the black water discharge mouth of the wet process cooling tank 22 and the scrubbing tower 42.With
The gas vent of the primary flash device 51 and two-stage flash device 52 is provided with and respectively communicated with condensation separating unit 61,63,
The sour gas outlet of the condensation separating unit is connect with burner；The cold of setting is connected to the primary flash device 51
The liquid outlet of solidifying separator is connected to oxygen-eliminating device 62；The two-stage flash device 52 and with the two-stage flash device 52
The liquid outlet of condensation separating unit for being connected to setting is connected to subsider 64, the liquid outlet of the subsider 64 with it is described
The connection setting of oxygen-eliminating device 62, as preferred embodiment, is arranged useful between the subsider 64 and the oxygen-eliminating device 62
In the ash water tank 65 worked as a buffer, filter device 66, the mistake are connected with the solids outlet port of the subsider 64
The liquid outlet of filter device 66 is connected to setting with the subsider 64, the reflux for partially liq.
As preferred embodiment, the liquid outlet of the oxygen-eliminating device 62 in the present embodiment is provided with and communicated with three road pipelines,
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；All the way with wet process cooling tank 22
Connection, for the cooling for being used for high temperature dry ash that flows back；Another way is connected to slag bath 13, is sent into the Quench collection slag after pump boosting
Device keeps the Quench liquid in slag bath 13 to maintain a certain amount for supplementing the Quench liquid in slag bath 13.
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 in the radiation heat transfer room 12 by laryngeal inlet 112
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 lower than 900 DEG C, and the temperature of core high-temperature region is 900
DEG C or more, to guarantee efficient heat exchange efficiency.Wherein the equivalent radius of the 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 touching when entering outer cylinder 124 by the turning of inner cylinder 126 with wall surface
Bonding is hit, further sprays cooling into after between the inner cylinder and outer cylinder 124, then by the 4th nozzle sets, is made not sufficiently
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,
As the gas temperature of synthesis gas declines, the melt cinder in synthesis gas solidifies 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 using 21 pairs of the cyclone separator synthesis gas after the heat exchange of the radiation heat transfer room 12, it will
Grain diameter control in the synthesis gas is in the range of being less than or equal to 5 μm；In the way of wet process cooling, to separation
Spraying cooling liquid in high temperature dry ash out, high temperature dry ash carry out cooling treatment, and coolant liquid and dry ash are mixed to form Heisui River discharge.
(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, can be used for downstream preparation by the synthesis gas that superheater 31 comes out
Chemical products.
(4) successively using Venturi scrubber 41 and scrubbing tower 42 to treated the synthesis gas of heat convection in step (4)
It is washed, synthesis gas washing to granule content is less than or equal to 1mg/Nm3, washing water then formed Heisui River discharge；
(5) double flash evaporation processing is carried out to the Heisui River generated in step (1) and step (2) and step (4), utilizes condensation
Separator condenses and separates the gas generated in double flash evaporation treatment process, burns to the sour gas isolated
Processing, by after primary flash condensation and separation of liquid be sent into oxygen-eliminating device 62 carry out deoxygenation processing；It is condensed and separated after two-stage flash
The remaining liq after liquid and two-stage flash out is then introduced into subsider 64, and the supernatant liquor after settlement treatment is re-fed into institute
It states oxygen-eliminating device 62 and carries out deoxygenation processing, the sedimentation solid portion that settlement treatment generates then is sent into filter device 66 and is filtered, mistake
The filtrate that filter generates is back to subsider 64 again；The liquid reflux that oxygen-eliminating device 62 comes out in the present embodiment is to scrubbing tower 42 and slag bath
13 and the cold ash can of wet process, realize recycling for water；The liquid of subsider discharge, a part are sent into oxygen-eliminating device, and a part is sent
Locked slag bucket is returned, for promoting deslagging, a part forms waste water discharge to balance the salinity dissolved in ash water system.
Embodiment 2
The gasification system for present embodiments providing a kind of high efficient heat recovery 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 same embodiment of gasification furnace 1 described in the present embodiment
1。
Gas solid separation and the cold apparatus for ash 2 of wet process, the gas solid separation and the cold apparatus for ash 2 of wet process include cyclone separator 21 with
The cold grey equipment of the wet process of the dry ash outlet setting of the cyclone separator.The cold grey equipment of the wet process is wet process cooling tank
22, it is provided with spray equipment in the wet process cooling tank 22, spraying cooling liquid is used for, cools down to the high temperature dry ash,
The coolant liquid sprayed out forms Heisui River after mixing with dry ash, is provided with black water discharge mouth on the wet process cooling tank 22.
Convective heat transfer device 3 is connected to, for recycling the sensible heat of synthesis gas simultaneously with the gas vent of the cyclone separator 21
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 again and steams 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 second 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 being arranged in series, the gasification furnace 1
Setting is connect with the primary flash device 51 with the black water discharge mouth of the cold ash can of wet process and the scrubbing tower 42.With described one
The gas vent of grade flash distillation plant 51 and two-stage flash device 52 is provided with and respectively communicated with condensation separating unit, the condensation separation
The sour gas outlet of device is connect with burner；The condensation separating unit of setting is connected to the primary flash device 51
Liquid outlet is connected to oxygen-eliminating device 62；The two-stage flash device 52 and be connected to the two-stage flash device 52 setting it is cold
The liquid outlet of solidifying separator is connected to subsider 64, and the liquid outlet of the subsider 64 is connected to the oxygen-eliminating device 62
Setting, as preferred embodiment, is provided between the subsider 64 and the oxygen-eliminating device 62 for working as a buffer
Ash water tank 65, be connected with filter device 66, the liquid of the filter device 66 with the solids outlet port of the subsider 64
Body outlet is connected to setting with the subsider 64, the reflux for 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 in the radiation heat transfer room 12 by laryngeal inlet 112
Cylinder is cooled down during entrance using second nozzle group injection fluid in advance, and control enters the interior of 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 temperature of the low-temperature space of the radiation heat transfer room 123 lower than 900 DEG C, the temperature of core high-temperature region at 900 DEG C or more,
To guarantee efficient heat exchange efficiency.Wherein the equivalent radius of the 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 when entering outer cylinder 124 by inner cylinder turning with wall surface, entrance
After between the inner cylinder and outer cylinder 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 solidifies 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 using 21 pairs of the cyclone separator synthesis gas after the heat exchange of the radiation heat transfer room 12, it will
Grain diameter control in the synthesis gas is in the range of being less than or equal to 5 μm；In the way of wet process cooling, to separation
Spraying cooling liquid in high temperature dry ash out, high temperature dry ash carry out cooling treatment, and coolant liquid and dry ash are mixed to form Heisui River discharge.
(3) synthesis gas is sequentially sent to superheater 31, multistage saturated steam generator 32 and boiler water preheater 33,
Synthesis gas is as the heat medium in superheater 31 and steam generator, boiler water preheater 33, for generating power steam, satisfying
And steam, and further boiler water is preheated, to sufficiently recycle the sensible heat of synthesis gas.Superheater 31 in the present embodiment
Overheating Treatment is carried out to the steam that gasification furnace 1 generates, 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) successively using Venturi scrubber 41 and scrubbing tower 42 to treated the synthesis gas of heat convection in step (4)
It is washed, synthesis gas washing to granule content is less than or equal to 1mg/Nm3, washing water then formed Heisui River discharge.
(5) double flash evaporation processing is carried out to the Heisui River generated in step (1) and step (2) and step (4), utilizes condensation
Separator condenses and separates the gas generated in double flash evaporation treatment process, burns to the sour gas isolated
Processing, by after primary flash condensation and separation of liquid be sent into oxygen-eliminating device 62 carry out deoxygenation processing；It is condensed and separated after two-stage flash
The remaining liq after liquid and two-stage flash out is then introduced into subsider 64, and the supernatant liquor after settlement treatment is re-fed into institute
It states oxygen-eliminating device 62 and carries out deoxygenation processing, the sedimentation solid portion that settlement treatment generates then is sent into filter device 66 and is filtered, mistake
The filtrate that filter generates is back to subsider 64 again；The liquid reflux that oxygen-eliminating device 62 comes out in the present embodiment is to scrubbing tower 42 and slag bath
13, realize the recycling of water.
Experimental example
Process system in the application can effectively recycle synthesis gas high temperature position thermal energy, and the quantum of output with (CO+H2) is
11 average reaction temperature is real to estimate based on 1400 DEG C, year operating times 8000 hours in 100,000Nm3/h, vaporizer
The output value in example 1 and embodiment 2 is applied, as a result as shown in the table：
Note：10MPag power steam 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 steam up to 50- as seen from the above table
70%.Use this technique can produce 50-65 tons/h of 10.0MPag grade power steam (fuel gas or IGCC product products scheme for
70-80 tons/h), year increases by ten thousand yuan of output value 4800-6240 (fuel gas or IGCC product products scheme be ten thousand yuan of 6720-7680),
Circulating cooling water consumption simultaneously reduces about 470 tons/h (fuel gas or IGCC products scheme be 410 tons/h), and year can save expense 38
Ten thousand yuan (fuel gas or IGCC products scheme be 330,000 yuan), economic benefit and energy conservation and consumption reduction effects are very significant.
The embodiments described above only express several embodiments of the present invention, and the description thereof is more specific and detailed, but simultaneously
Limitations on the scope of the patent of the present invention therefore cannot 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 guarantor of the invention
Protect range.Therefore, the scope of protection of the patent of the present invention should be subject to the claims.
Claims (11)
1. a kind of cold grey formula high efficient heat recovery gasification system of wet process, 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 core high-temperature region positioned at the low-temperature space far from the heat-transfer surface side, it is high in the low-temperature space and core
The downstream of warm area is provided with Quench collection slag device, has Quench liquid in the Quench collection slag device, and the Quench collection slag device is set
It is equipped with black water discharge mouth；
Gas solid separation and the cold apparatus for ash of wet process, are connected to setting with the syngas outlet of the gasification furnace, utilize the cold grey equipment of wet process
Dry ash after gas solid separation is cooled down, the cold grey equipment of the wet process is provided with black water discharge mouth；
Convective heat transfer device is connected to, for recycling the sensible heat of 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, and the venturi including 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 being arranged in series, the Quench collection slag device, institute
The black water discharge mouth for stating the cold grey equipment of wet process and the scrubbing tower connect setting with the primary flash device.
2. the cold grey formula high efficient heat recovery gasification system of wet process according to claim 1, which is characterized in that the gas-solid point
From and the cold apparatus for ash of wet process include that the cold ash of wet process of dry ash outlet setting of cyclone separator and the cyclone separator is set
It is standby.
3. the cold grey formula high efficient heat recovery gasification system of wet process according to claim 1 or 2, which is characterized in that described right
Flowing heat-exchanger rig includes superheater, and water cooling heat-exchanger rig is provided on the heat-transfer surface of the vaporizer and radiation heat transfer room, described
The steam (vapor) outlet of water cooling heat-exchanger rig is connected to setting with the superheater, and the synthesis gas enters the superheater and the steam
It exchanges heat, the steam that the water cooling heat-exchanger rig comes out is heated to be superheated steam.
4. the cold grey formula high efficient heat recovery gasification system of wet process according to claim 3, which is characterized in that the convection current is changed
Thermal includes the superheater being arranged in series, multistage saturated steam generator and boiler water preheater, is come out by the superheater
Synthesis gas sequentially enter the multistage saturated steam generator and boiler water preheater.
5. the cold grey formula high efficient heat recovery gasification system of wet process according to claim 1 or 2 or 3 or 4, which is characterized in that
Condensation separating unit, the condensation are provided with and respectively communicated with the gas vent of the primary flash device and two-stage flash device
The sour gas outlet of separator is connect with Sour gas disposal device；The condensation of setting is connected to the primary flash device
The liquid outlet of separator is connected to oxygen-eliminating device；The two-stage flash device and setting is connected to the two-stage flash device
The liquid outlet of condensation separating unit be connected to subsider, the liquid outlet of the subsider is connected to the oxygen-eliminating device and sets
It sets, is connected with filter device with the solids outlet port of the subsider.
6. a kind of cold grey formula high efficient heat recovery gasification process of wet process, which is characterized in that including：
(1) vaporizing system exchanges heat synthesis gas feeding radiation heat transfer room 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 heat exchange of the radiation heat transfer room, it is dry to the high temperature isolated using wet process
Grey spraying cooling liquid cools down the high temperature dry ash and forms Heisui River discharge；
(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 (2) and step (4).
7. the cold grey formula high efficient heat recovery gasification process of wet process according to claim 6, which is characterized in that in step (4)
Synthesis gas washing to granule content is less than or equal to 1mg/Nm3。
8. the cold grey formula high efficient heat recovery gasification process of wet process according to claim 6 or 7, which is characterized in that step (1)
Described in low-temperature space temperature be less than 900 DEG C, the temperature of the core high-temperature region is at 900 DEG C or more.
9. the cold grey formula high efficient heat recovery gasification process of wet process according to claim 8, which is characterized in that in step (2)
Gas solid separation is carried out to the synthesis gas, the grain diameter control in the synthesis gas is being less than or equal to 5 μm of range
It is interior.
10. the cold grey formula high efficient heat recovery gasification process of wet process according to claim 7, 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.
11. according to the cold grey formula high efficient heat recovery gasification process of any wet process of claim 6-9, which is characterized in that right
The gas generated in double flash evaporation treatment process in step (5) is condensed and separated, and the sour gas isolated send the acid in downstream
Property gas treatment equipment, 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 carry out deoxygenation processing, the solid generated to settlement treatment
It is filtered.
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| CN201810952169.5A CN108913208A (en) | 2018-08-21 | 2018-08-21 | A kind of cold grey formula high efficient heat recovery gasification system of wet process and technique |
| PCT/CN2018/122282 WO2020037904A1 (en) | 2018-08-21 | 2018-12-20 | Wet cold ash high efficiency thermal energy recovery gasification system and process |
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| WO2020037904A1 (en) * | 2018-08-21 | 2020-02-27 | 北京航天迈未科技有限公司 | Wet cold ash high efficiency thermal energy recovery gasification system and process |
| WO2020037905A1 (en) * | 2018-08-21 | 2020-02-27 | 北京航天迈未科技有限公司 | Gasification system and process for efficient heat energy recovery |
| CN110938476A (en) * | 2019-11-29 | 2020-03-31 | 北京航天迈未科技有限公司 | Gas-solid separation equipment, system and method |
| CN111607433A (en) * | 2019-02-25 | 2020-09-01 | 新能能源有限公司 | Cooling and deslagging method for coal ash |
| CN112708470A (en) * | 2020-12-23 | 2021-04-27 | 华阳新材料科技集团有限公司 | Device and method for producing synthesis gas by multi-nozzle gasification furnace |
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| CN112852502A (en) * | 2021-03-24 | 2021-05-28 | 北京航天迈未科技有限公司 | Preheating system of cyclone separator and using method thereof |
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