CN107875977A - A kind of high-pressure spiral fast pyrogenation reaction unit - Google Patents
A kind of high-pressure spiral fast pyrogenation reaction unit Download PDFInfo
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- CN107875977A CN107875977A CN201711142660.3A CN201711142660A CN107875977A CN 107875977 A CN107875977 A CN 107875977A CN 201711142660 A CN201711142660 A CN 201711142660A CN 107875977 A CN107875977 A CN 107875977A
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 28
- 238000000197 pyrolysis Methods 0.000 claims description 45
- 239000000463 material Substances 0.000 claims description 29
- 239000000571 coke Substances 0.000 claims description 15
- 229910000831 Steel Inorganic materials 0.000 claims description 6
- 239000010959 steel Substances 0.000 claims description 6
- 239000011449 brick Substances 0.000 claims description 4
- 239000012774 insulation material Substances 0.000 claims description 4
- 238000004519 manufacturing process Methods 0.000 abstract description 13
- 239000000203 mixture Substances 0.000 abstract description 3
- 238000005979 thermal decomposition reaction Methods 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 29
- 239000003245 coal Substances 0.000 description 10
- 238000000034 method Methods 0.000 description 8
- 238000010438 heat treatment Methods 0.000 description 6
- 238000012546 transfer Methods 0.000 description 6
- 239000004744 fabric Substances 0.000 description 5
- 238000009434 installation Methods 0.000 description 5
- 230000008569 process Effects 0.000 description 5
- 230000008901 benefit Effects 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000009825 accumulation Methods 0.000 description 2
- 239000002817 coal dust Substances 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 239000008187 granular material Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000005855 radiation Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 241000208340 Araliaceae Species 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 229910001208 Crucible steel Inorganic materials 0.000 description 1
- 206010030973 Oral discomfort Diseases 0.000 description 1
- 235000005035 Panax pseudoginseng ssp. pseudoginseng Nutrition 0.000 description 1
- 235000003140 Panax quinquefolius Nutrition 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000012876 carrier material Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011143 downstream manufacturing Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 235000008434 ginseng Nutrition 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 229910000679 solder Inorganic materials 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
- B01J6/008—Pyrolysis reactions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/2425—Tubular reactors in parallel
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
- B01J19/243—Tubular reactors spirally, concentrically or zigzag wound
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/18—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge
- C10B47/20—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion with moving charge according to the moving bed type
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
- C10B53/04—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of powdered coal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00051—Controlling the temperature
- B01J2219/00157—Controlling the temperature by means of a burner
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/00049—Controlling or regulating processes
- B01J2219/00162—Controlling or regulating processes controlling the pressure
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4012—Pressure
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Materials Engineering (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- General Chemical & Material Sciences (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of high-pressure spiral fast pyrogenation reaction unit, including body of heater, spiral reactor and burner, wherein spiral reactor is arranged in body of heater；Burner is uniformly distributed on the wall of body of heater, is heated for jetting out flames to spiral reactor.The device of the present invention disclosure satisfy that the working condition of HTHP, and can adjust the production composition of thermal decomposition product as requested, improve the thermal efficiency, reduce environmental pollution and production cost.
Description
Technical field
The present invention relates to a kind of down-flow fluidized bed using ECT fast pyrolysis reactor for coal chemical industry, to prepare high heating value combustion
The high value added products such as gas, high-quality semicoke and high quality oils, and it is anti-to relate more specifically to a kind of high-pressure spiral fast pyrogenation
Answer device.
Background technology
The energy resource structure feature in China is rich coal, oil-poor, few gas, as coal production maximum in the world and country of consumption,
Within one considerably long period, coal resources are unshakable as the status that China dominates the energy.According to statistics, China has been
Coal reserves is verified as 114,500,000,000 tons, wherein, middle low-order coal (lignite, lower-grade metamorphic bituminous) accounts for national reserves
55.15% or so.Because low-order coal has, moisture is high, easy-weathering is natural, is difficult to sort, should not transport for long-distance and store
Feature so that its comprehensive utilization is very limited.Widely used as modernization coal mining is polytechnic, pyrolysis of coal technology quilt
It is considered the maximally efficient approach of coal high-efficiency clean utilization, but in pyrolysis art, particularly fast pyrogenation becomes one kind
New and effective method for pyrolysis.
Fast pyrogenation refers under conditions of anaerobic or limit oxygen, material is rapidly heated to temperature needed for pyrolysis so that contain
Chemical bond rupture reaction promptly occurs for carbon macromolecule, and the working environment of HTHP can be to the generating rate of raising thermal decomposition product
Improve a lot.Fast pyrolysis reactor is generally divided into the reaction units such as fluid bed, moving bed, revolving bed, and profit at present
The requirement of the Temperature Distribution in temperature field and heating rate is realized with having two methods of carrier and carrier-free, but uses heat to carry
The flashing reactor of body be related to carrier and raw material it is uniform, mix and react, and downstream vector and semicoke product later
The a series of complex technique such as separate, preheat again, conveying again, causing fault rate to improve, the overall thermal efficiency reduces.Also have using no-load
Body indirect heat transfer reactor, but heat transfer efficiency is low, large-scale is more difficult, and is more the reaction using square-section
Device, the reactor of this structure type is suitable only under the operating mode of middle low temperature, low pressure and normal pressure, for HTHP without heat
Carrier fast pyrolysis reactor need further to develop at present.
The content of the invention
In view of the shortcomings of the prior art, it is anti-to provide a kind of external no new fast pyrogenation of heat carrier downstriker of flame by the present invention
Device is answered, the shortcomings of overcoming existing equipment, structure and complex process, disclosure satisfy that the working condition of HTHP, and can basis
It is required that the production composition of adjustment thermal decomposition product, improves the thermal efficiency, environmental pollution and production cost are reduced.
Specifically, following purpose can be achieved in the present invention：
1) thermal source is provided using the one-level energy, using energy source is saved from energy resource structure；
2) the pressure-resistant and temperature capacity of reactor is improved, realizes the purpose of high pressure；
3) reactor uses cylinder structure, improves stability, and simplifies structure reduction manufacturing cost；
4) operation without heat carrier, simplify system, reduce fault rate, improve the operational reliability of system, reduce energy consumption, subtract
Few mechanical wear；
5) flame is external greatly reduces the weld seam quantity formed by arrangement radiant tube, improves reactor high temperature high pressure fortune
Security reliability under row operating mode；
6) scope of application is wider, and inside reactor bearing temperature can reach 1000 DEG C, and internal bearing capacity can reach
3MPa。
In order to realize or reach above-mentioned purpose, the present invention adopts the following technical scheme that：
According to the present invention, there is provided a kind of high-pressure spiral fast pyrogenation reaction unit, including body of heater, spiral reactor and burning
Mouth, wherein spiral reactor is arranged in body of heater；Burner is uniformly distributed on the wall of body of heater, for jetting out flames to spiral shell
Rotating reactor heating.
According to one embodiment of present invention, spiral reactor include charging aperture, reactor body, pyrolysis gas outlet and
Coke outlet, its middle charging aperture are arranged on the top of spiral reactor, and reactor body is the main body of spiral reactor, pyrolysis
Gas exports the bottom that spiral reactor is arranged at coke outlet.
According to one embodiment of present invention, the steel plate wall thickness of reactor body is 6-15mm, the diameter of reactor body
For 50-300mm, the central diameter of spiral reactor is 100-3000mm, and the pitch of reactor body is not less than 180mm.
According to one embodiment of present invention, the heat resisting temperature of reactor body is 500-1200 DEG C, and material is in reactor
Residence time in body is 6-9s.
According to one embodiment of present invention, the length of run of spiral reactor is 12-405m, spiral reactor
Highly it is 6-405m, the spiral number of spiral reactor is 1-390.
According to one embodiment of present invention, the absolute pressure that reactor body is born is 1.0-10MPa.
According to one embodiment of present invention, it is 100-9000mm per the spacing of two neighboring spiral reactor.
According to one embodiment of present invention, the structure of body of heater is rectangle, cartridge type or annular.
According to one embodiment of present invention, the wall of body of heater is built by laying bricks or stones using resistant to elevated temperatures insulation material, for preventing heat
Amount is scattered and disappeared.
According to one embodiment of present invention, the wall thickness of body of heater is not less than 300mm.
By using above-mentioned technical proposal, the present invention has the following advantages that compared to prior art：
1) spiral reactor of the invention adds spiral form using heat resisting steel body, and high temperature high voltage resistant ability is stronger.
2) device of the invention is external using flame, greatly reduces the weld seam quantity formed by arrangement radiant tube so that
The globality of reactor body is more preferable, the security reliability under spiral reactor high temperature high-voltage operation operating mode is improved, from root
The danger of blast is reduced in sheet.
3) spiral reactor integral installation of the invention is in full of flame and the uniform body of heater of temperature so that spiral
The distribution of inside reactor is also more uniformly distributed, be so designed that avoid because of larger action of thermal difference and caused by structural damage.
4) compared to existing heat carrier rapid pyrolysis reactor, reactor of the invention simplifies structure, reduces manufacture
Cost, improve stock utilization.
5) the reactor body of the spiral reactor of the present invention not only reduces body of heater height, adds body radiating surface,
And residence time of the material in spiral reactor is also add under same height, so as to improve pyrolysis efficiency and reaction
Completeness.
6) manufacture of whole device of the invention and fairly simple, the short construction period of installation.
7) device of the invention can realize the industrial production of variation and maximization according to production-scale size.
8) device of the invention can make it that pyrolysis is more thorough under high temperature and high pressure environment, and the yield of pyrolysis gas is higher, more
It is important that provide advantage for downstream production technology.
9) reactor inboard wall of tube body can install floor additional, not only increase body intensity and added in unit space
Body radiating surface.
10) present invention uses the heat form of cloth in external heat, and the weld seam amount of reactor body greatly reduces so that peace
Dress and flaw detection workload are reduced, it is often more important that the security of reactor is higher under high temperature and high pressure environment.Using body form pole
The big complexity for simplifying structure, improves stock utilization, reduces manufacturing cost, and disclosure satisfy that more high internal pressure and more
The operating environment requirements of high-temperature.
11) pyrolysis gas outlet of the invention is arranged on the bottom of spiral reactor, the top of discharge zone, and pyrolysis gas passes through
Spiral reactor inside and outside differential pressure quickly exports from outlet.Pyrolysis gas outlet is arranged on bottom, and particle have passed through from top to bottom
Whole spiral reactor, makes its pyrolysis more complete, sets pyrolysis gas outlet relative to top and middle part, reduces in gas
Granule number is carried, improves the quality of pyrolysis gas.
Brief description of the drawings
The above-mentioned and/or additional aspect and advantage of the present invention will more in the description carried out to embodiment is combined with accompanying drawing
Add obvious and be readily appreciated that, wherein：
Fig. 1 is the structural representation of the high-pressure spiral fast pyrogenation reaction unit along A-A directions of the embodiment of the present invention；
Fig. 2 is Fig. 1 sectional view；
Fig. 3 is the structural representation of the spiral reactor of the embodiment of the present invention；
Fig. 4 is sectional views of the Fig. 3 along B-B directions.
Description of reference numerals
1 spiral reactor, 2 bodies of heater, 3 burners, 4 charging apertures, 5 reactor bodys, 6 pyrolysis gas outlets, 7 coke outlets.
Embodiment
It should be appreciated that shown embodiments of the invention are merely illustrative in the exemplary embodiment.Although in this hair
Only a small number of embodiments are described in detail in bright, but those skilled in the art are readily appreciated that and depart from the present invention in not essence
In the case of the teaching of theme, a variety of modifications are feasible.Correspondingly, all such modifications should all be included in the present invention's
In the range of.Without departing from the spirit of the invention, design, operating condition and ginseng that can be to following exemplary embodiment
Number etc. makes others and replaces, changes, changes and delete.
As Figure 1-4, the invention provides a kind of high-pressure spiral fast pyrogenation reaction unit, the pyrolysis installation is using fire
The external sped structure of flame, including body of heater 2, spiral reactor 1 and burner 3, wherein spiral reactor 1 is arranged on body of heater 1
It is interior and including charging aperture 4, reactor body 5, pyrolysis gas outlet 6 and coke outlet 7；Burner 3 is uniformly distributed in the wall of body of heater 2
On wall, heated for jetting out flames to spiral reactor 1.
In the present invention, spiral reactor 1 is placed in body of heater 2, and material is in the spiral internal flow of reactor 1, burner 3
On furnace wall, wherein burner 3 is located on heat accumulation type radiant tube, and vertically adjacent two layers of heat accumulation type radiant tube up and down is adopted
With the mode being interspersed so that reaction mass is more uniformly spread in dropping process, in the horizontal direction along annular with
It is evenly arranged；The ability and quantity of burner 3 can carry out the arrangement of rational and orderly according to actual 2 calorific requirements of body of heater, and burner 3 sprays
The flame gone out greatly reduces the weld seam of spiral reactor 1 in the spiral external heat of reactor 1, the peace under high pressure conditions
Full property is higher.
In an embodiment of the present invention, the wall of body of heater 2 is built by laying bricks or stones using resistant to elevated temperatures insulation material, for preventing heat
Scatter and disappear, wall thickness >=300mm of body of heater 2.
In the present invention, material is entered in reactor body 5 by charging aperture 4, the cloth on the spiral top of reactor 1
Uniform distribution is passed through in area, then passes through high-temperature spiral formula reactor 1, material in dropping process with spiral reactor 1
The tube wall of high-temperature gas and spiral reactor 1 contacts, and forms convection current, three kinds of heat transfer types of heat conduction and radiation are carried out simultaneously
High Efficiency Thermal exchanging form, material is quickly accomplished pyrolytic reaction in 6-9s, generate pyrolysis gas and semicoke, fall into spiral anti-
The discharge zone of the lower end of device 1 is answered, semicoke is discharged by coke outlet 7 caused by final reaction, and the pyrolysis gas of HTHP passes through pyrolysis
The export of gas outlet 6.
In an embodiment of the present invention, the structure of body of heater 2 can be the diversified forms such as rectangle, tubular or annular.
In the present invention, spiral reactor 1 is arranged in inside body of heater 2, is designed using spiral cylinder structure, spirally
Sub-material area, reaction zone and the part of discharge zone three, the charging of spiral reactor 1 are formd in the body of reactor 1 from top to bottom
Mouth 4 is coke outlet 7 in top, bottom, and charging aperture 4 and coke outlet 7 are to be vertically arranged.As shown in figure 3, spiral reactor 1
Charging aperture 4 and furnace roof reactor feed mouth correspond, the coke outlet 7 of spiral reactor 1 with the coke outlet of body of heater 2 one by one
It is corresponding.The tube wall of spiral reactor 1 bears the effect of internal pressure, in order to reach the technological requirement of high pressure, can increase spiral
The steel plate thickness of the outer wall of reactor 1, the material of reactor body 5 uses heat resisting cast steel, to adapt to long term high temperature operating mode, according to pressure
Power and diameter difference pipe thickness can take 6-15mm, and all solder joints are welded using air-tightness, and carry out carrying out flaw detection, enter,
Discharge all high temperature resistants, high pressure resistant equipment；Realized by adjusting the ability of burner 3 to the spiral internal temperature of reactor 1
Control, the temperature in reactor body 5 can be caused to reach：T=500-1200 DEG C, meet the temperature strip needed for fast pyrogenation
Part, the diameter of reactor body 5 according to combined factors such as production capacity, bearing capacity, the efficiency of heating surface and Flow of Goods and Materials situations and
It is fixed, it can be set to：Φ=50-300mm.Height, helical angle, central diameter and the number of total coils of spiral reactor 1 must are fulfilled for thing
Expect the requirement of the speed of the requirement of residence time and whereabouts in body of heater 2, wherein helical angle have to be larger than the angle of repose of material
(angle of repose of such as coal dust is 27-45 °), helixangleθ=30-90 °.
In the present invention, in order to ensure the service life of reactor body 5 and wall heat transfer efficiency, reactor body 5
Steel plate wall thickness can be set as：δ=6-15mm；Smooth in order to ensure the circulation of material, the central diameter of spiral reactor 1 is：D=
(2-10) Φ=100-3000mm；The pitch that the reactor body 5 of spiral reactor is calculated by helixangleθ (refers to one
The distance of origin-to-destination when helix rises a full circle)：P=tan θ * π D=180mm- ∞；Material fast heating ramp rate should
For：100 DEG C/s of C ＞, therefore material will be rapidly heated to 500-1200 DEG C, its run duration in reactor body 5 can be with
It is set to：T=6-9s, coefficient of friction of the coal dust to tube wall：μ=0.3-0.5, can be with according to the residence time of material and coefficient of friction
Calculate the length of run of reactor body 5：L=1/2 (g*sin θ-μ g*cos θ) * t2, it follows that the exhibition of spiral reactor 1
Open length：L=12-405m, the height of spiral reactor 1：H=L*sin θ=6-405m.The spiral shell of single spiral reactor 1
It is 1-390 to revolve number n.
In an embodiment of the present invention, the absolute pressure that can be born in reactor body 5 is P：1.0-10.0MPa；Instead
Answer device body 5 to use helical structure, not only reduce the height of body of heater 2, add body radiating surface, and also add material and exist
Residence time in spiral reactor 1, so as to not only increase the thermal efficiency and also material pyrolysis more fully and thoroughly；Reactor
The inwall of body 5 installs floor additional, not only increases body intensity and body radiating surface is added in unit space.It is spiral anti-
Device 1 is answered to be arranged in body of heater 2 with certain rule, its quantity can be depending on actual production capacity requires, often row can set
2-10 are put, can arrange that 2-10 is arranged in the horizontal direction, or other, the spacing of two neighboring spiral reactor 1：D1=
(1-3) * D=100-9000mm.
In an embodiment of the present invention, burner 3 is used to provide the main heat needed for material pyrolysis in spiral reactor 1
Source, it is uniformly distributed on body of heater 2 along body height direction and horizontal direction so that it is uniform that reaction zone forms one or more
Temperature field to meet the temperature needed for the pyrolysis of material in spiral reactor 1, while the temperature of body of heater 2 can pass through each burning
The ability of mouth 3 is adjusted flexibly, and so as to obtain reliable and stable each temperature field, and then substantially increases the quality of product
And yield.The spacing and the number of plies of burner 3 should be set according to body of heater intensity requirement and height for reactor, can arrange 2- from bottom to top
10 layers, set per layer number according to actually required heat.
In an embodiment of the present invention, pyrolysis gas outlet 6 is arranged on the bottom of spiral reactor 1, the top of discharge zone,
Pyrolysis gas is quickly exported by the spiral inside and outside differential pressure of reactor 1 from outlet.Pyrolysis gas outlet 6 is arranged on bottom, and particle is certainly
Whole spiral reactor 1 is have passed through under above, makes its pyrolysis more complete, pyrolysis gas outlet 6 is set relative to top and middle part,
The carrying granule number in gas is reduced, improves the quality of pyrolysis gas.
In an embodiment of the present invention, discharge zone is located at the bottom of spiral reactor 1, and coke outlet 7 is arranged on discharge zone
Bottom be spiral reactor 1 bottom, semicoke pass through deadweight and the spiral internal pressure of reactor 1 comprehensive function, warp
Cross coke outlet 7 and export spiral reactor 1.
In the present invention, the requirement of downstream process is answered, pyrolysis gas needs to realize the conveying of HTHP, but existing at present
Square-section be suitable only for low-pressure delivery without heat carrier rapid pyrolysis reactor, it is impossible to meet process requirements.The present invention with
Existing square-section, circular cross-section contrast without heat carrier rapid pyrolysis reactor, and its scope of application is wider, and structure is more reliable, peace
Full property is higher.Comparatively bearing capacity is stronger for the structure type of cast first, and evenly, stability is more preferable for structure stress, and
And the present invention is greatly reduced using the heat form of cloth in external heat, the weld seam amount of reactor body so that installation and flaw detection
Workload is reduced, it is often more important that the security of reactor is higher under high temperature and high pressure environment.Greatly simplified using body form
The complexity of structure, to improve stock utilization reduce manufacturing cost, and disclosure satisfy that more high internal pressure and higher temperature
Operating environment requirements.
Embodiment
As Figure 1-4, the present invention devises a kind of fast pyrolysis reactor of down-flow fluidized bed using ECT spiral form, this pyrolysis installation
Using the external sped structure of flame, its agent structure includes：Spiral reactor 1, body of heater 2 and burner 3；It is wherein spiral anti-
Device 1 is answered to include charging aperture 4, reactor body 5, pyrolysis gas outlet 6 and coke outlet 7, spiral reactor 1 is installed in body of heater 2,
Burner 3 is uniformly distributed in body of heater side walls, and burner 3 jets out flames to be heated to spiral reactor 1.
Body of heater 2 is circle, and spiral reactor 1 is placed in circular body of heater 2, material in the spiral internal flow of reactor 1,
Flame greatly reduces the weld seam of spiral reactor 1 in the spiral external heat of reactor 1, the security under high pressure conditions
It is higher；Material is entered in reactor body 5 by charging aperture 4, passes through uniform cloth in the cloth area on the spiral top of reactor 1
Material, then passes through high-temperature spiral formula reactor 1, material in dropping process with the high-temperature gas in spiral reactor 1 and
The tube wall contact of spiral reactor 1, form convection current, the efficient heat exchange type that three kinds of heat transfer types of heat conduction and radiation are carried out simultaneously
Formula, material is quickly accomplished pyrolytic reaction in spiral reactor 1, generate pyrolysis gas and semicoke, drop into spiral anti-
The discharge zone of the lower end of device 1 is answered, semicoke is discharged by coke outlet 7 caused by final reaction, and the pyrolysis gas of HTHP passes through pyrolysis
The export of gas outlet 6.
In this preferred embodiment, the wall of body of heater 2 is built by laying bricks or stones for preventing heat using resistant to elevated temperatures insulation material
Scatter and disappear, furnace wall thickness >=300mm, burner 3 is arranged on the exterior wall of body of heater 2, in order to ensure the service life of reactor body 5 and wall
Face heat transfer efficiency, the steel plate wall thickness of reactor body 5 can be set as：δ=10mm；Smooth, the spiral shell in order to ensure the circulation of material
The central diameter of rotating reactor is：D=500mm, helixangleθ are 45 °；The pitch of reactor body 5 is calculated by helixangleθ：p
=1.72m；Material fast heating ramp rate should be：100 DEG C/s of C ＞, therefore material will be rapidly heated to 1000 DEG C, it is in spiral
Run duration in the pipe of formula reactor 1 can be set to t=6s, and reaction can be calculated according to the residence time of material and coefficient of friction
The length of run of device body 5：L=30m, it follows that the length of run of spiral reactor 1：L=80m, spiral reactor 1
Spiral number of turns be 5, the height of spiral reactor：H=56m；The spacing of adjoining spiral formula reactor 1 is 600mm.
Presently preferred embodiments of the present invention is the foregoing is only, is not used for limiting the practical range of the present invention；If do not take off
From the spirit and scope of the present invention, the present invention is modified or equivalent substitution, all should covered in the claims in the present invention
Among protection domain.
Claims (10)
- A kind of 1. high-pressure spiral fast pyrogenation reaction unit, it is characterised in that including body of heater, spiral reactor and burner, its Described in spiral reactor be arranged in the body of heater；The burner is uniformly distributed on the wall of the body of heater, is used for Jet out flames and heated to the spiral reactor.
- 2. high-pressure spiral fast pyrogenation reaction unit according to claim 1, it is characterised in that the spiral reactor Including charging aperture, reactor body, pyrolysis gas outlet and coke outlet, wherein the charging aperture is arranged on the spiral reactor Top, the reactor body is the main body of the spiral reactor, and the pyrolysis gas outlet and the coke outlet are all provided with Put in the bottom of the spiral reactor.
- 3. high-pressure spiral fast pyrogenation reaction unit according to claim 2, it is characterised in that the reactor body Steel plate wall thickness is 6-15mm, a diameter of 50-300mm of the reactor body, and the central diameter of the spiral reactor is 100- 3000mm, the pitch of the reactor body are not less than 180mm.
- 4. high-pressure spiral fast pyrogenation reaction unit according to claim 3, it is characterised in that the reactor body Heat resisting temperature is 500-1200 DEG C, and residence time of the material in the reactor tube body is 6-9s.
- 5. high-pressure spiral fast pyrogenation reaction unit according to claim 4, it is characterised in that the spiral reactor Length of run be 12-405m, the reactor body of the spiral reactor is highly 6-405m, the spiral reactor Spiral number be 1-390.
- 6. high-pressure spiral fast pyrogenation reaction unit according to claim 5, it is characterised in that the reactor body is held The absolute pressure received is 1.0-10MPa.
- 7. high-pressure spiral fast pyrogenation reaction unit according to claim 6, it is characterised in that per two neighboring spiral The spacing of reactor is 100-9000mm.
- 8. high-pressure spiral fast pyrogenation reaction unit according to claim 1, it is characterised in that the structure of the body of heater is Rectangle, tubular or annular.
- 9. high-pressure spiral fast pyrogenation reaction unit according to claim 1, it is characterised in that the wall of the body of heater is adopted Built by laying bricks or stones with resistant to elevated temperatures insulation material, for preventing scattering and disappearing for heat.
- 10. high-pressure spiral fast pyrogenation reaction unit according to claim 9, it is characterised in that the wall of the body of heater Thickness is not less than 300mm.
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| CN110079347A (en) * | 2019-05-29 | 2019-08-02 | 青岛科技大学 | A kind of biomass moving bed pyrolysis reactor of helix tube |
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