CN105462619A - Gasification process system for urban household garbage and industrial organic solid waste - Google Patents
Gasification process system for urban household garbage and industrial organic solid waste Download PDFInfo
- Publication number
- CN105462619A CN105462619A CN201511012851.9A CN201511012851A CN105462619A CN 105462619 A CN105462619 A CN 105462619A CN 201511012851 A CN201511012851 A CN 201511012851A CN 105462619 A CN105462619 A CN 105462619A
- Authority
- CN
- China
- Prior art keywords
- fluidized bed
- ash
- gasification
- coal gas
- bed gasification
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/026—Dust removal by centrifugal forces
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/75—Multi-step processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
- C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
- C10K3/003—Reducing the tar content
- C10K3/006—Reducing the tar content by steam reforming
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0946—Waste, e.g. MSW, tires, glass, tar sand, peat, paper, lignite, oil shale
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0956—Air or oxygen enriched air
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0953—Gasifying agents
- C10J2300/0973—Water
- C10J2300/0976—Water as steam
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0983—Additives
- C10J2300/0986—Catalysts
-
- 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
-
- 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
- C10J2300/1625—Integration of gasification processes with another plant or parts within the plant with solids treatment
- C10J2300/1628—Ash post-treatment
- C10J2300/1631—Ash recycling
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1687—Integration of gasification processes with another plant or parts within the plant with steam generation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/169—Integration of gasification processes with another plant or parts within the plant with water treatments
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
-
- 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
- C10J2300/1838—Autothermal gasification by injection of oxygen or steam
-
- 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
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Environmental & Geological Engineering (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Analytical Chemistry (AREA)
- Gasification And Melting Of Waste (AREA)
Abstract
The invention relates to a gasification process system for urban household garbage and industrial organic solid waste. A circulating fluidized bed gasification system is communicated with a coal gas quality reforming system and a waste heat utilization system, respectively; the circulating fluidized bed gasification system and the waste heat utilization system are connected with an ash residue collection system; a coal gas purification system is communicated with the waste heat utilization system and a water treatment system, respectively; a gasification medium preheating system is communicated with the waste heat utilization system and the water treatment system, respectively and is used for supplying heat for the incomplete combustion of the circulating fluidized bed gasification system; a catalyst is provided for the gasification reaction of the circulating fluidized bed gasification system by overheated high-temperature steam produced by the waste heat utilization system; the coal gas quality reforming system is used for supplying heat for gasification reaction products of the circulating fluidized bed gasification system; the waste heat utilization system is used for recycling the waste heat of the coal gas quality reforming system. According to the gasification process system, resources of the system are adequately utilized for reaction, so that the energy consumption is reduced, the cost is lowered, and the problems that gas products are impure and low in heat value are solved.
Description
Technical field
The present invention relates to domestic refuse and organic solid waste processing technology field, particularly relate to a kind of domestic waste and industrial organic solid waste gasifying process system.
Background technology
As long as the place of someone activity, will produce rubbish, that is domestic refuse all will produce in people's activity every day.Because current Domestic Environment is polluted, destroyed acutely, the requirement of Environmental protection is more strict, therefore requires to carry out appropriate process to domestic waste and industrial organic solid waste.The domestic waste that current China commonly uses and a kind of mode for burning of industrial organic solid waste processing mode, but a large amount of pollutents can be produced in burning process, thermal pollution environment, and can mass energy be consumed.Another mode is the mode of gasification, but in conventional gasifying process system: the Effiency of whirlwind Separator is low, causes coal gas to carry away a large amount of circulating ash, impact gasification, scission reaction, and causes more serious corrosion and wearing and tearing to follow-up equipment; The high-temperature steam of gasification takes from other process systems, waste self energy; Lime-ash directly discharges, contaminate environment; The scavenging process of coal gas does not thoroughly cause coal gas to contain corrosive gases and dust on the one hand, and long-time perishable pipeline endangers safety, and causes coal gas moisture higher on the other hand, affects gas quality; Needed for water treatment device and gasifying medium primary heater unit, the energy takes from other process systems, waste self energy.By literature search, China Patent No. is that the patent of invention of ZL200810024077.7 proposes domestic waste and industrial organic solid waste fluidized bed gasification combustion facture, China Patent No. is that the patent of invention of ZL03147866.2 proposes a kind of rotary kiln refuse gasification, the multistage incinerating method of carbon ash cosmelting and system thereof, China Patent No. is that the patent of invention of ZL200710070193.8 proposes domestic garbage pyrolysis gasification oven, the patent No. is a kind of gasification installation and the method that the patent of invention of ZL201010574948.X proposes domestic waste and industrial organic solid waste, it is short all to there is the gasification residence time in above-mentioned several device and system, gasification efficiency is low, energy expenditure is huge, contaminate environment, the problems such as aerogenesis calorific value is low.
Summary of the invention
The object of the invention is to, when solving existing domestic waste and industrial organic solid waste process, make full use of that own resource carries out gasifying, scission reaction, solve energy consumption, the problem reduced costs and coal gas product impure, the problem that calorific value is low.And then a kind of domestic waste and industrial organic solid waste gasifying process system are provided.
For realizing above object, by the following technical solutions: a kind of domestic waste and industrial organic solid waste gasifying process system, by ciculation fluidized bed gasification system, coal gas makings reforming system, bootstrap system, ash collection system, gas cleaning system, water treatment system and gasification media preheating system composition, ciculation fluidized bed gasification system is communicated with bootstrap system with coal gas makings reforming system respectively, ciculation fluidized bed gasification system and bootstrap system are all connected with ash collection system, gas cleaning system is communicated with water treatment system with bootstrap system respectively, gasifying medium preheating system is communicated with water treatment system with bootstrap system respectively, gasifying medium pre-heating system provides warm air and heat for ciculation fluidized bed gasification system incomplete combustion, the high temperature super heated steam that bootstrap system produces provides catalyzer for the gasification reaction of ciculation fluidized bed gasification system, coal gas makings reforming system provides heat for ciculation fluidized bed gasification system gasification reaction resultant, bootstrap system reclaims the waste heat of the high-temperature gasification resultant of reaction after the heating of coal gas makings reforming system.
Described ciculation fluidized bed gasification system comprises: air compartment, flat blast cap, burner, screw feeder, fuel warehouse, bed material warehouse, circulating fluidized bed burner hearth, primary cyclone, secondary cyclone, material returning device, loosen and returning charge wind air compartment, returning charge pipeline, slaked lime warehouse between material returning device and returning charge pipeline.Burner arrangement is at circulating fluidized bed burner hearth emulsion zone, screw feeder is connected with circulating fluidized bed burner hearth, bed material warehouse is connected with circulating fluidized bed burner hearth, and be communicated with by star-shaped discharge valve between screw feeder with fuel warehouse, described flat blast cap is made up of heat-resistance stainless steel.
Described coal gas makings reforming system comprises coal gas makings reformer chamber, plasma heating gun, and coal gas makings reformer chamber is communicated with the secondary cyclone of ciculation fluidized bed gasification system.
Described bootstrap system comprises: steam distributor, superheater, vaporizer I, drum, air preheater, vaporizer II, economizer; Superheater and coal gas makings reformer chamber are by pipeline communication, and the air compartment of air preheater and described ciculation fluidized bed gasification system is by pipeline communication, and steam distributor is communicated with by the air compartment of pipeline with ciculation fluidized bed gasification system.
Described ash collection system comprises: lime-ash warehouse, lime-ash manifold trunk and ash silo; The secondary cyclone of described ciculation fluidized bed gasification system and the superheater of described bootstrap system, vaporizer I, air preheater, vaporizer II, economizer are all provided with lime-ash warehouse by star-shaped discharge valve, all lime-ash warehouses are all connected to ash silo by lime-ash manifold trunk, and are provided with unloading valve between each lime-ash warehouse and lime-ash manifold trunk.
Described gas cleaning system comprises washing extracting tower, dehydration tower, first grade subsides room, secondary settling pocket, liming recycle pond; The economizer of washing extracting tower and described bootstrap system passes through pipeline communication, the bottom sewage outlet of washing extracting tower, first grade subsides room, secondary settling pocket, liming recycle pond are communicated with successively by pipeline, the washings jet pipe of washing extracting tower and liming recycle pond, by pipeline communication, are provided with steam separator, condensing heat exchanger in dehydration tower.
Described water treatment system comprises cold water storage cistern, water softening device, deoxygenator and connect logical successively, and cold water storage cistern is communicated with the dehydration tower of described gas cleaning system, and the economizer in deoxygenator and described bootstrap system passes through pipeline communication.
Described gasifying medium pre-heating system is superheated vapour-air heat exchanger, superheated vapour-air heat exchanger, be connected respectively by pipeline with air preheater with the steam distributor of described bootstrap system, superheated vapour-air heat exchanger is connected by pipeline with the deoxygenator of described water treatment system.
beneficial effect of the present invention:
1, ciculation fluidized bed gasification system have employed anaerobism combustion system, utilizes part waste incineration liberated heat to provide energy for gasification;
2, after efficient cyclone separator, be provided with coal gas makings reforming system, gas temperature is raised, in abundant decomposition gasification process, produce dioxin;
3, after coal gas is separated by separator, be provided with residual heat using device, residual heat using device is superheater, vaporizer I, air preheater, vaporizer II, economizer, the heat recuperation of being carried by coal gas is also transformed in high-temperature steam, and high-temperature steam is transmitted back to ciculation fluidized bed gasification system carries out gasifying, scission reaction, utilize self energy cost-saving;
4, take star-shaped discharge valve, combination ash collection system that lime-ash warehouse adds unloading valve, without gas leakage when ensureing to collect lime-ash;
5, be provided with condensing heat exchanger in dehydration tower, reduce flue-gas temperature, tentatively make the hydrogenesis in flue gas, after carry out second time through steam separator again and be separated, the water vapor fully carried in minimizing coal gas.And the water in condensing heat exchanger carrys out self-cooling water tank, and circulates with cold water storage cistern, the water temp into deoxygenator can be improved, reduce steam consumption;
7, high temperature super heated steam divides three parts to carry, and first part sends in ciculation fluidized bed gasification system and participates in gasification, scission reaction; Carry out steaming out in superheater in second section feeding bootstrap system, vaporizer I, air preheater, vaporizer II, economizer, improve heat-transfer effect, reclaim heat energy efficiently; Part III sends into superheated vapour-air heat exchanger, preheating freezing air.Make full use of the self-energy in this process system, save energy.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
As shown in the figure: 1, air compartment, 2, flat blast cap, 3, burner, 4, screw feeder, 5, fuel warehouse, 6, star-shaped discharge valve VII, 7, bed material warehouse, 8, circulating fluidized bed burner hearth, 9, primary cyclone, 10, secondary cyclone, 11, material returning device, 12, loosen and returning charge wind air compartment, 13, returning charge pipeline, 14, slaked lime warehouse, 15, coal gas makings reformer chamber, 16, plasma heating gun, 17, steam distributor, 18, superheater, 19, vaporizer I, 20, drum, 21, air preheater, 22, vaporizer II, 23, economizer, 24, star-shaped discharge valve I, 25, lime-ash warehouse I, 26, unloading valve I, 27, star-shaped discharge valve II, 28, lime-ash warehouse II, 29, unloading valve II, 30, star-shaped discharge valve III, 31, lime-ash warehouse III, 32, unloading valve III, 33, star-shaped discharge valve IV, 34, lime-ash warehouse IV, 35, unloading valve IV, 36, star-shaped discharge valve V, 37, lime-ash warehouse V, 38, unloading valve V, 39, star-shaped discharge valve VI, 40, lime-ash warehouse VI, 41, unloading valve VI, 42, lime-ash manifold trunk, 43, ash silo, 44, washing extracting tower, 45, dehydration tower, 46, steam separator, 47, condensing heat exchanger, 48, first grade subsides room, 49, secondary settling pocket, 50, liming recycle pond, 51, washings jet pipe, 52, cold water storage cistern, 53, water softening device, 54, deoxygenator, 55, superheated vapour-air heat exchanger.
Embodiment
Embodiment
Below in conjunction with accompanying drawing to the present invention to further illustrating; This example is made up of ciculation fluidized bed gasification system, coal gas makings reforming system, bootstrap system, ash collection system, gas cleaning system, water treatment system and gasification media preheating system, ciculation fluidized bed gasification system is communicated with bootstrap system with coal gas makings reforming system respectively, ciculation fluidized bed gasification system and bootstrap system are all connected with ash collection system, gas cleaning system is communicated with that with bootstrap system with water treatment system respectively, and gasifying medium preheating system is communicated with water treatment system with bootstrap system respectively.
Ciculation fluidized bed gasification system comprises: air compartment (1), flat blast cap (2), burner (3), screw feeder (4), fuel warehouse (5), be positioned at the star-shaped discharge valve VII (6) between screw feeder (4) and fuel warehouse (5), bed material warehouse (7), circulating fluidized bed burner hearth (8), primary cyclone (9), secondary cyclone (10), material returning device (11), be positioned at loosening and returning charge wind air compartment (12) of material returning device (11) bottom, returning charge pipeline (13), be positioned at the slaked lime warehouse (14) between material returning device (11) and returning charge pipeline (13).Under burner (1) is arranged in bed, air compartment is provided with startup heating unit in (1), and hot blast derives from the air preheater (21) in bootstrap system.Cloth elegance is with flat blast cap (2), the flow velocity of fuel air and vaporized chemical (gasification wind) is 0.5 ~ 1m/s, bed material is mixed with wind, realize rubbish low velocity fluidization anaerobism to burn, gasify and rationally get rid of large granular materials, this flat blast cap (2) is made up of heat-resistance stainless steel.The mode that feed adopts screw feeder (4) and star-shaped discharge valve VII (6) to combine, ensures continuity, stopping property, the reliability of feed.This system has two-stage efficient cyclone separator altogether, i.e. primary cyclone (9), secondary cyclone (10), this efficient cyclone separator adopts jacket structured, chuck is made up of heat-resistance stainless steel, coal gas (850 DEG C) to enter after efficient cyclone separator high speed rotating in chuck, by centrifugal force by the dust separation in flue gas out, this efficient cyclone separator separation efficiency can reach more than 98%.Between material returning device (11) and returning charge pipeline (13), be provided with slaked lime warehouse (14), be mixed with returning charge ash feeding burner hearth in returning charge pipeline (13), carries out preliminary desulfurization process.
Gas cleaning system comprises coal gas makings reformer chamber (15), plasma heating gun (16).Coal gas makings reformer chamber (15) is communicated with the secondary cyclone (10) of ciculation fluidized bed gasification system.The coal gas (850 DEG C) separated via ciculation fluidized bed gasification system secondary cyclone (10) enters coal gas makings reformer chamber (15), is heated to the dioxin produced in (900 DEG C ~ 1000 DEG C) next thorough decomposition gasification process in coal gas makings reformer chamber (15) by plasma heating gun (16).
Bootstrap system comprises: steam distributor (17), superheater (18), vaporizer I (19), drum (20), air preheater (21), vaporizer II (22), economizer (23); Superheater (18) and vaporizer I (19) pass through pipeline communication, vaporizer I (19) and air preheater (21) pass through pipeline communication, air preheater (21) and vaporizer II (22) are by pipeline communication, and vaporizer II (22) and economizer (23) pass through pipeline communication.Superheater (18) and coal gas makings reformer chamber (15) pass through pipeline communication, air preheater (21) passes through pipeline communication with the air compartment (1) of described ciculation fluidized bed gasification system, bootstrap system is provided with steam distributor (17), and steam distributor (17) is communicated with the air compartment (1) of ciculation fluidized bed gasification system by pipeline.
There are in drum (20) four high efficiency cyclonic separators flash liberation is carried out to steam water interface (temperature of saturation 195 DEG C), steam (temperature of saturation 195 DEG C) after separation carries out secondary separation by screen separator again, to ensure to enter superheater (18) after steam contains lower moisture, prevent superheater (18) body generation pipe explosion accident; Be provided with feeding apparatus, chemicals dosing plant, continuous blow off equipment, liquid-level monitoring device, drum pressure watching device and overpressure protection apparatus in drum (20), ensure in drum higher water quality and ensure security of system, reliable, stable operation.
Steam distributor (17) and superheater (18) pass through pipeline communication, superheated vapour (1.25Mpa in steam distributor (17), 500 DEG C) points three strands send outside: first strand is the air compartment (1) sent into as gasification wind in ciculation fluidized bed gasification system, and being mixed with fuel air enters circulating fluidized bed burner hearth (8) by the flat blast cap of ciculation fluidized bed gasification system (2) and carry out gasification reaction; Second strand is send into superheater (18), vaporizer I, vaporizer II (22) and economizer (23) as sootblowing dielectric; 3rd strand is send into gasifying medium pre-heating system preheating freezing air as thermal source;
Coal gas of high temperature (900 DEG C ~ 1000 DEG C) after coal gas makings reforming system enters superheater (18), and superheater (18) housing adopts flanging technology, reduces weld seam and guarantees sealing; Superheater (18) body have employed sinuous coil convection heating surface, is made by high-temperature alloy steel; Sinuous coil the top two array of pipes is furnished with wearing-resistant tile, effectively protects convection heating surface; Pitch (120mm ~ 180mm) reasonable in design between sinuous coil ensures the unimpeded and suitable gas speed of gas flue; Arrange steam soot-blower to guarantee heat-transfer effect in rational position between sinuous coil, steam is from steam distributor (17).In the middle part of superheater (18) body, being provided with convection-type desuperheater regulating final high-temperature steam outlet temperature by regulating spray water flux.After saturation steam (195 DEG C) overheated one-tenth high-temperature steam (500 DEG C) by Cemented filling to steam distributor (17);
Coal gas of high temperature (710 DEG C) after superheater (18) cooling enters vaporizer I (19), and the housing of vaporizer I (19) adopts flanging technology, reduces weld seam and guarantees sealing.Vaporizer I (19) body employing angle of inclination is the convection tubes group of 10 °, avoids pipe internal memory gas explosion pipe phenomenon to occur; Pitch (120mm ~ 180mm) reasonable in design between convection tubes group ensures the unimpeded and suitable flue gas flow rate of exhaust gases passes; Arrange steam soot-blower to guarantee heat-transfer effect in rational position between convection tubes group, steam is from steam distributor (17).Every three tubule groups are communicated with composition bassoon group by header, the top two array of pipes of each tubule group is furnished with wearing-resistant tile, effectively protects convection heating surface;
Through vaporizer I (19) lower the temperature after coal gas (510 DEG C) first through air preheater (21), then through evaporator II (22).Vaporizer II (22) body employing angle of inclination is the convection tubes group of 10 °, avoids pipe internal memory gas explosion pipe phenomenon to occur; Pitch (120mm ~ 180mm) reasonable in design between convection tubes group ensures the unimpeded and suitable flue gas flow rate of exhaust gases passes; Arrange steam soot-blower to guarantee heat-transfer effect in rational position between convection tubes group, steam is from steam distributor (17).Every three tubule groups are communicated with composition bassoon group by header, the top two array of pipes of each tubule group is furnished with wearing-resistant tile, effectively protects convection heating surface.Air preheater (21) housing adopts flanging technology, reduces weld seam and guarantees sealing.Air preheater (21) body adopts medium in pipe to be air, manages outer medium is the structure of high-temperature flue gas, body is arranged by reasonable computation, ensure that pipe surface temperature is higher than 160 DEG C, avoid the generation of acid dew piont corrosion phenomenon, and make heat transfer reach optimum regime by pitch reasonable in design and pipe sizes, quantity.120 DEG C of warm airs to be heated to after 500 DEG C of warm airs by Cemented filling to the air compartment (1) in ciculation fluidized bed gasification system, be mixed with gasification wind and enter circulating fluidized bed burner hearth (8) by the flat blast cap of ciculation fluidized bed gasification system (2) and carry out gasification reaction, 120 DEG C of warm airs are from gasifying medium pre-heating system;
Coal gas (250 DEG C) after air preheater (21) cooling enters economizer (23).Economizer (23) housing adopts flanging technology, reduces weld seam and guarantees sealing.Economizer (23) have employed sinuous coil convection heating surface; Arrange steam soot-blower to guarantee heat-transfer effect in rational position between sinuous coil, steam is from steam distributor (17).Sinuous coil the top two array of pipes is furnished with wearing-resistant tile, effectively protects convection heating surface; Pitch (120mm ~ 180mm) reasonable in design between sinuous coil ensures the unimpeded and suitable gas speed of gas flue.
Ash collection system comprises lime-ash warehouse, lime-ash manifold trunk (42) and ash silo (43), the secondary cyclone (10) of ciculation fluidized bed gasification system is provided with lime-ash warehouse I (25) by star-shaped discharge valve I (24), the superheater (18) of bootstrap system is provided with lime-ash warehouse II (28) by star-shaped discharge valve II (27), vaporizer I (19) is provided with lime-ash warehouse III (31) by star-shaped discharge valve III (30), air preheater (21) is provided with lime-ash warehouse IV (34) by star-shaped discharge valve IV (33), vaporizer II (22) is provided with lime-ash warehouse V (37) by star-shaped discharge valve V (36), economizer (23) is crossed star-shaped discharge valve VI (39) and is provided with lime-ash warehouse VI (40), lime-ash warehouse I (25), lime-ash warehouse II (28), lime-ash warehouse III (31), lime-ash warehouse IV (34), lime-ash warehouse V (37), lime-ash warehouse VI (40) all passes through lime-ash manifold trunk (42) and is connected to ash silo (43), and be provided with corresponding unloading valve I (26) between each lime-ash warehouse with lime-ash manifold trunk (42), unloading valve II (29), unloading valve III (32), unloading valve IV (35), unloading valve V (38), unloading valve VI (41).First open star-shaped discharge valve when unloading ash, be disposed to by lime-ash in lime-ash warehouse, then close star-shaped discharge valve, then open unloading valve, so operation can avoid gas leakage.
Gas purification system comprises washing extracting tower (44), dehydration tower (45), settling pocket, liming recycle pond (50); Washing extracting tower (44) passes through pipeline communication with the economizer (23) of described bootstrap system, the bottom sewage outlet of washing extracting tower (44), first grade subsides room (48), secondary settling pocket (49), liming recycle pond (50) are communicated with successively by pipeline, the washings jet pipe (51) of washing extracting tower (44) by pipeline communication, is provided with steam separator (46), condensing heat exchanger (47) with liming recycle pond (50) in dehydration tower (45).Coal gas (250 DEG C) enters gas cleaning system, first the washings jet pipe (51) in washing extracting tower (44) carries out washing depickling dedusting, then condensing heat exchanger (47) heat exchange in dehydration tower (45), gas temperature after heat exchange is down to 80 DEG C by 110 DEG C, major part steam coagulation Cheng Shui, eventually pass steam separator (46) and carry out carbonated drink separation, effectively decrease the water vapor that coal gas carries, to ensure that coal gas has high heating value, improve gas quality.
Water treatment system comprises cold water storage cistern (52), water softening device (53), deoxygenator (54) and connect logical successively, cold water storage cistern (52) is communicated with the dehydration tower (45) of described gas cleaning system, and deoxygenator (54) passes through pipeline communication with the economizer (23) in described bootstrap system.Tap water (20 DEG C) is sent in cold water storage cistern (52) after water softening device (53) process, in cold water storage cistern (52) be arranged in the condensing heat exchanger (47) of gas cleaning system dehydration tower (45) by pipeline communication, and form the recycle system.After condensing heat exchanger (47) heat exchange being arranged in gas cleaning system dehydration tower (45), water temperature sends into deoxygenator (54) by pipe connecting after rising to 50 DEG C by 20 DEG C.The pipeline that deaerated water (104 DEG C) after deoxygenation is connected with the economizer (23) in bootstrap system by deoxygenator (54) is sent in the economizer (23) in bootstrap system, carries out waste heat recovery.Needed for deoxygenator (54) deoxygenation, steam is from gasifying medium pre-heating system.
Gasifying medium pre-heating system is superheated vapour-air heat exchanger (55); Superheated vapour-air heat exchanger (55) is connected respectively by pipeline with air preheater (21) with the steam distributor (17) of described bootstrap system, and superheated vapour-air heat exchanger (55) is connected by pipeline with the deoxygenator (54) of described water treatment system.Superheated vapour (1.25Mpa, 500 DEG C) pipeline that is connected with the steam distributor (17) being arranged in bootstrap system by superheated vapour-air heat exchanger (55) sends into superheated vapour-air heat exchanger (55), be heated to the warm air of 120 DEG C at this freezing air by 20 DEG C, warm air (120 DEG C) is sent into by the pipeline that superheated vapour-air heat exchanger (55) is connected with the air preheater (21) being arranged in bootstrap system the air preheater (21) being arranged in bootstrap system and is carried out waste heat recovery.Superheated vapour after cooling is sent into the deoxygenator (54) being arranged in water treatment system and is carried out deoxygenation to oiler feed.
Claims (8)
1. domestic waste and an industrial organic solid waste gasifying process system, is characterized in that; Be made up of ciculation fluidized bed gasification system, coal gas makings reforming system, bootstrap system, ash collection system, gas cleaning system, water treatment system and gasification media preheating system, ciculation fluidized bed gasification system is communicated with bootstrap system with coal gas makings reforming system respectively, ciculation fluidized bed gasification system and bootstrap system are all connected with ash collection system, gas cleaning system is communicated with water treatment system with bootstrap system respectively, and gasifying medium preheating system is communicated with water treatment system with bootstrap system respectively; Gasifying medium pre-heating system provides warm air and heat for ciculation fluidized bed gasification system incomplete combustion, the high temperature super heated steam that bootstrap system produces provides catalyzer for the gasification reaction of ciculation fluidized bed gasification system, coal gas makings reforming system provides heat for ciculation fluidized bed gasification system gasification reaction resultant, and bootstrap system reclaims the waste heat of the high-temperature gasification resultant of reaction after the heating of coal gas makings reforming system.
2. a kind of domestic waste according to claim 1 and industrial organic solid waste gasifying process system, it is characterized in that, described ciculation fluidized bed gasification system is provided with air compartment (1), screw feeder (4), fuel warehouse (5), bed material warehouse (7), cyclonic separator; Burner (3) is arranged in circulating fluidized bed burner hearth (2) emulsion zone, screw feeder (4) is connected with circulating fluidized bed burner hearth (8), bed material warehouse (7) is connected with circulating fluidized bed burner hearth (8), is communicated with between screw feeder (4) with fuel warehouse (5) by star-shaped discharge valve.
3. a kind of domestic waste according to claim 2 and industrial organic solid waste gasifying process system, it is characterized in that, described coal gas makings reforming system comprises coal gas makings reformer chamber (15), plasma heating gun (16), and coal gas makings reformer chamber (15) is communicated with the secondary cyclone (10) of ciculation fluidized bed gasification system.
4. a kind of domestic waste according to claim 3 and industrial organic solid waste gasifying process system, is characterized in that, described bootstrap system comprises superheater (18), vaporizer, air preheater (21), economizer (23); Superheater (18) and coal gas makings reformer chamber (15) pass through pipeline communication, air preheater (21) passes through pipeline communication with the air compartment (1) of described ciculation fluidized bed gasification system, bootstrap system is provided with steam distributor (17), and steam distributor (17) is communicated with the air compartment (1) of ciculation fluidized bed gasification system by pipeline.
5. a kind of domestic waste according to claim 4 and industrial organic solid waste gasifying process system, is characterized in that, described ash collection system comprises lime-ash warehouse, lime-ash manifold trunk (42) and ash silo (43); The secondary cyclone (10) of described ciculation fluidized bed gasification system and the superheater (18) of described bootstrap system, vaporizer I (19), air preheater (21), vaporizer II (22), economizer (23) are all provided with lime-ash warehouse by star-shaped discharge valve, all lime-ash warehouses all pass through lime-ash manifold trunk (42) and are connected to ash silo (43), and are provided with unloading valve between each lime-ash warehouse and lime-ash manifold trunk (42).
6. a kind of domestic waste according to claim 4 and industrial organic solid waste gasifying process system, it is characterized in that, described gas cleaning system comprises washing extracting tower (44), dehydration tower (45), settling pocket, liming recycle pond (50); Washing extracting tower (44) passes through pipeline communication with the economizer (23) of described bootstrap system, the bottom sewage outlet of washing extracting tower (44), first grade subsides room (48), secondary settling pocket (49), liming recycle pond (50) are communicated with successively by pipeline, the washings jet pipe (51) of washing extracting tower (44) by pipeline communication, is provided with steam separator (46), condensing heat exchanger (47) with liming recycle pond (50) in dehydration tower (42).
7. a kind of domestic waste according to claim 6 and industrial organic solid waste gasifying process system, it is characterized in that, described water treatment system comprises cold water storage cistern (52), water softening device (53), deoxygenator (54) and connect logical successively, cold water storage cistern (52) is communicated with the dehydration tower (45) of described gas cleaning system, and deoxygenator (54) passes through pipeline communication with the economizer (23) in described bootstrap system.
8. a kind of domestic waste according to claim 7 and industrial organic solid waste gasifying process system, is characterized in that, described gasifying medium pre-heating system is superheated vapour-air heat exchanger (55); Superheated vapour-air heat exchanger (55) is connected respectively by pipeline with air preheater (21) with the steam distributor (17) of described bootstrap system, and superheated vapour-air heat exchanger (55) is connected by pipeline with the deoxygenator (54) of described water treatment system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201511012851.9A CN105462619A (en) | 2015-12-31 | 2015-12-31 | Gasification process system for urban household garbage and industrial organic solid waste |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201511012851.9A CN105462619A (en) | 2015-12-31 | 2015-12-31 | Gasification process system for urban household garbage and industrial organic solid waste |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105462619A true CN105462619A (en) | 2016-04-06 |
Family
ID=55600787
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201511012851.9A Pending CN105462619A (en) | 2015-12-31 | 2015-12-31 | Gasification process system for urban household garbage and industrial organic solid waste |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105462619A (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012039751A2 (en) * | 2010-09-24 | 2012-03-29 | James Charles Juranitch | Renewable combined cycle low turbine boost |
| CN103205281A (en) * | 2013-03-29 | 2013-07-17 | 合肥德博生物能源科技有限公司 | Gasification system of oxygen-enriched biomass circulating fluidized-bed |
| CN103484164A (en) * | 2013-09-13 | 2014-01-01 | 广州迪森热能技术股份有限公司 | Biomass waste heat steam gasification heating system |
| CN204325282U (en) * | 2014-12-09 | 2015-05-13 | 中国东方电气集团有限公司 | Plasma asistance rubbish fluidized bed gasification system |
| CN104804774A (en) * | 2015-04-21 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and device for preparing fuel gas by utilizing ash coal as raw material |
| CN204589098U (en) * | 2014-12-26 | 2015-08-26 | 北京雷浩环保能源技术有限公司 | Utilize the pyrolysis of coal system of spouted bed bioreactor |
| CN204607939U (en) * | 2015-05-07 | 2015-09-02 | 合肥德博生物能源科技有限公司 | The combustion and segmented inverting biological charcoal/steam co-producing device of biomass pyrogenation gasification |
| CN205653413U (en) * | 2015-12-31 | 2016-10-19 | 大连科林能源工程技术开发有限公司 | City domestic waste and industry is gasification system useless admittedly organically |
-
2015
- 2015-12-31 CN CN201511012851.9A patent/CN105462619A/en active Pending
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012039751A2 (en) * | 2010-09-24 | 2012-03-29 | James Charles Juranitch | Renewable combined cycle low turbine boost |
| CN103205281A (en) * | 2013-03-29 | 2013-07-17 | 合肥德博生物能源科技有限公司 | Gasification system of oxygen-enriched biomass circulating fluidized-bed |
| CN103484164A (en) * | 2013-09-13 | 2014-01-01 | 广州迪森热能技术股份有限公司 | Biomass waste heat steam gasification heating system |
| CN204325282U (en) * | 2014-12-09 | 2015-05-13 | 中国东方电气集团有限公司 | Plasma asistance rubbish fluidized bed gasification system |
| CN204589098U (en) * | 2014-12-26 | 2015-08-26 | 北京雷浩环保能源技术有限公司 | Utilize the pyrolysis of coal system of spouted bed bioreactor |
| CN104804774A (en) * | 2015-04-21 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and device for preparing fuel gas by utilizing ash coal as raw material |
| CN204607939U (en) * | 2015-05-07 | 2015-09-02 | 合肥德博生物能源科技有限公司 | The combustion and segmented inverting biological charcoal/steam co-producing device of biomass pyrogenation gasification |
| CN205653413U (en) * | 2015-12-31 | 2016-10-19 | 大连科林能源工程技术开发有限公司 | City domestic waste and industry is gasification system useless admittedly organically |
Non-Patent Citations (2)
| Title |
|---|
| 《火电厂生产岗位技术问答》编委会: "《热工仪表及自动装置》", 31 January 2012 * |
| 贺永德等: "《现代煤化工技术手册》", 31 March 2011 * |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102433160B (en) | Control method for biomass gasification equipment | |
| CN100582197C (en) | Circulating fluidized bed heat-power-gas-tar multi-joint-production apparatus and method | |
| CN102618330B (en) | High temperature normal pressure biomass gasification island process | |
| CN102358841B (en) | Multistage pulverized coal multiple-tube rotary low temperature dry distillation technology and system | |
| CN105314812A (en) | Sludge treatment system and treatment method thereof | |
| CN102864674B (en) | Device and method for recycling gasified and burned alkali for straw pulp papermaking black liquor circulating fluidized bed | |
| CN104449872A (en) | Gasification process system for fine particle biomass or solid fossil fuel | |
| CN104017594B (en) | Coal low-temperature cracking process | |
| CN110818220A (en) | Sludge low-temperature drying coupling pyrolysis system | |
| CN101984018B (en) | External heating internal coal decomposing equipment | |
| CN111621315A (en) | Pyrolysis process system for recycling waste plastics | |
| CN101024782A (en) | Dense-phase conveying-bed coal pressurizing gasifying apparatus and method | |
| CN103591591A (en) | Saponification waste liquid combustion and alkali recovery boiler | |
| CN211367382U (en) | Sludge low-temperature drying coupling pyrolysis system | |
| CN211394370U (en) | System for pyrolysis of junked tire of boiler flue gas of thermal power plant | |
| CN104629814A (en) | Fluidized-bed gasified gas afterheat recycling and purifying system and application thereof | |
| CN205653413U (en) | City domestic waste and industry is gasification system useless admittedly organically | |
| CN106635174B (en) | Heat accumulating type high-calorific-value synthesis gas gasification device and gasification production method based on same | |
| CN107057768B (en) | Dry coal powder gasification furnace with air preheating and steam generation functions and method thereof | |
| CN105219443A (en) | The technique of plasma fluidized-bed gasification furnace and process biomass thereof | |
| CN205170639U (en) | Sludge treatment system | |
| CN203571761U (en) | Saponification waste liquid burning and alkali recovery boiler | |
| CN204356293U (en) | The gasifying process system of a kind of fine particle biomass or solid fossil fuel | |
| CN101974351B (en) | Scale fixed bed biomass gasification power generation production technology and suite of equipment | |
| CN105331380A (en) | Power generation system and power generation method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20160406 |
|
| RJ01 | Rejection of invention patent application after publication |