CN106753491A - A kind of solid thermal carriers activation coal gas flashing speed oven coal produces the system and method for coal tar, coal gas and semicoke - Google Patents
A kind of solid thermal carriers activation coal gas flashing speed oven coal produces the system and method for coal tar, coal gas and semicoke Download PDFInfo
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- CN106753491A CN106753491A CN201710040944.5A CN201710040944A CN106753491A CN 106753491 A CN106753491 A CN 106753491A CN 201710040944 A CN201710040944 A CN 201710040944A CN 106753491 A CN106753491 A CN 106753491A
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- coke
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- 239000003245 coal Substances 0.000 title claims abstract description 121
- 239000003034 coal gas Substances 0.000 title claims abstract description 117
- 239000011280 coal tar Substances 0.000 title claims abstract description 63
- 239000007787 solid Substances 0.000 title claims abstract description 63
- 230000004913 activation Effects 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000000969 carrier Substances 0.000 title claims abstract description 21
- 239000007789 gas Substances 0.000 claims abstract description 205
- 238000000197 pyrolysis Methods 0.000 claims abstract description 133
- 239000000571 coke Substances 0.000 claims abstract description 126
- 239000003546 flue gas Substances 0.000 claims abstract description 68
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 65
- 238000006243 chemical reaction Methods 0.000 claims abstract description 46
- 238000001816 cooling Methods 0.000 claims abstract description 25
- 238000004064 recycling Methods 0.000 claims abstract description 16
- 239000003921 oil Substances 0.000 claims description 61
- 239000011269 tar Substances 0.000 claims description 39
- 239000012530 fluid Substances 0.000 claims description 23
- 239000002817 coal dust Substances 0.000 claims description 19
- 238000004062 sedimentation Methods 0.000 claims description 16
- 230000008676 import Effects 0.000 claims description 14
- 239000012716 precipitator Substances 0.000 claims description 14
- 238000002485 combustion reaction Methods 0.000 claims description 12
- 238000006477 desulfuration reaction Methods 0.000 claims description 12
- 230000023556 desulfurization Effects 0.000 claims description 12
- 238000010992 reflux Methods 0.000 claims description 12
- 238000000926 separation method Methods 0.000 claims description 12
- 239000000428 dust Substances 0.000 claims description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 11
- 238000001035 drying Methods 0.000 claims description 8
- 239000000843 powder Substances 0.000 claims description 8
- 239000002245 particle Substances 0.000 claims description 6
- 239000002994 raw material Substances 0.000 claims description 6
- 230000005484 gravity Effects 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 239000007921 spray Substances 0.000 claims description 4
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 238000011084 recovery Methods 0.000 claims description 3
- 238000003786 synthesis reaction Methods 0.000 claims description 3
- 238000005406 washing Methods 0.000 claims description 3
- 230000008859 change Effects 0.000 claims description 2
- 238000012958 reprocessing Methods 0.000 claims description 2
- 239000002199 base oil Substances 0.000 claims 1
- 238000010304 firing Methods 0.000 claims 1
- 238000000227 grinding Methods 0.000 claims 1
- 238000005265 energy consumption Methods 0.000 abstract description 7
- 238000005457 optimization Methods 0.000 abstract description 4
- 238000002360 preparation method Methods 0.000 abstract description 2
- 241000196324 Embryophyta Species 0.000 description 29
- 241000273930 Brevoortia tyrannus Species 0.000 description 27
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 229910052799 carbon Inorganic materials 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000005299 abrasion Methods 0.000 description 3
- 238000004939 coking Methods 0.000 description 3
- 238000009795 derivation Methods 0.000 description 3
- 238000002309 gasification Methods 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- 230000003213 activating effect Effects 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000008878 coupling Effects 0.000 description 2
- 238000010168 coupling process Methods 0.000 description 2
- 238000005859 coupling reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003517 fume Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 238000005453 pelletization Methods 0.000 description 2
- 150000003254 radicals Chemical class 0.000 description 2
- 241001672694 Citrus reticulata Species 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 239000012159 carrier gas Substances 0.000 description 1
- 238000007233 catalytic pyrolysis Methods 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000001934 delay Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000004321 preservation Methods 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 239000004449 solid propellant Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
-
- 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
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/005—After-treatment of coke, e.g. calcination desulfurization
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/18—Modifying the properties of the distillation gases in the oven
-
- 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
- C10K1/024—Dust removal by filtration
-
- 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
- C10K1/16—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids
- C10K1/18—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with non-aqueous liquids hydrocarbon oils
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Materials Engineering (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Industrial Gases (AREA)
Abstract
The present invention relates to the system and method that a kind of solid thermal carriers activation coal gas flashing speed oven coal produces coal tar, coal gas and semicoke, including raw coal Preliminary working device, pyrolytic reaction separator, semicoke heated separator, circulation recycling device, coal tar recovering device and Semi-coke cooling device；Pyrolytic reaction separator a part of semi-coke powder out enters semicoke heated separator, high-temperature flue gas from semicoke heated separator out enter circulation recycling device, the coal tar recovering device produces coal tar oil and gas, the Semi-coke cooling device to produce semicoke；Pyrolysis of coal optimization is bad in existing coal tar preparation method, cause that oil productivity is low, investment high energy consumption technical problem, solid thermal carriers of the present invention activation coal gas flashing speed oven coal produce coal tar, coal gas and semicoke system hold fast pyrogenation, it is quick derive, quick cooling.
Description
Technical field
The invention belongs to technical field of coal chemical industry, and in particular to a kind of solid thermal carriers activation coal gas flashing speed oven coal is produced
The system and method for coal tar, coal gas and semicoke.
Background technology
, using an important channel for being clean Coal Chemical Industry, pyrolysis of coal is coal for high-volatile bituminous coal and lignite step sub-prime
The key technology that step sub-prime is utilized, pyrolysis of coal plant investment is few, and energy consumption is low, and the thermal efficiency is high, and water consume is small, carbon emission is low, has
Extensive market prospects and preferable economic benefit.
From the mechanism of pyrolysis and facts have proved fast pyrogenation and it is quick derive, quick cooling is to improve pyrolytic tar yield
Effective way.The speed being pyrolyzed under the smaller similarity condition of particle diameter of coal is faster, less than 0.1mm pulverized coal pyrolysis, belongs to flashing speed oven；
Tar gas after pyrolysis can quickly be derived and can quickly cooled down, it is to avoid second pyrolysis, liquid yield is high；Powder is defeated using air-flow
Send controllability good, process is simple, small investment is praised highly.Because the dust pelletizing system of the too small each link of coal particle size is difficult to ensure that spy
It is not dedusting under raw coke oven gas high temperature, thoroughly solution is failed so far, governs the development of the technique.Cyclone dust collectors are used as ash-laden gas
Body rough dedusting, small investment is reliable；The incising control of whirlwind and the diameter of Whirlwind cyclone have larger relation, industrially for
Compared with small particle dedusting more use whirlwind sub-portfolio, but whirlwind sub-portfolio dust pelletizing system is mutually collaborated efficiency of dust collection due to lower dipleg
Decline, macromolecular coal tar is polymerized, tar precipitation and coal dust combination carbon deposit during thermograde occurs raw coke oven gas at high temperature in addition,
Block the lower dipleg of Whirlwind cyclone, device cannot run.Using the measures such as traditional external whirlwind or jacket heat-preservation or Whirlwind cyclone
Plus the mode of flutter valve cannot ensure that blanking is unobstructed and does not collaborate mutually, it is impossible to ensure high-effective dust-removing and stabilization in raw gas system
Operation.
Methane produces free radical after activation of catalyst in saturable pyrolytic process in coal gas, it is to avoid produce substantial amounts of gas
Body, can greatly improve the tar yield of pyrolysis.Methane activation has activation of catalyst method, has oxidation activation method, and catalytic activation is easy
Carbon distribution is formed in catalyst surface, it is impossible to which long-term operation, oxidized activating can overcome the weakness of catalytic activation under high temperature.
The method that the A fine coal comprehensive utilizations of patent CN 101955799 prepare coal tar, coal gas, vapor, using being less than
The fine coal solid thermal carriers riser pyrolysis of 0.1mm, though accomplish drying, one-level pyrolysis, two grades of pyrolysis, systems of high-temperature semi-coke
Work, gasification, steam, have carried out cascade utilization, and pyrolysis falls within flashing speed oven, but just the dust removal problem of pyrolysis is not recorded,
Quick derivation and quick cooling, the gasification of the A semi-coke powders of patent CN 102250646 and reformation gas pyrolysis coupling coal tar is not considered
It is riser gas-solid heat carrier pyrolysis with the device and method of coal gas, raw materials used is the fine coal of 200 mesh (less than 0.1mm), is
Gasification and the coupling of pyrolysis, semicoke all gasify, while activating coal gas with high-temperature gas, tar yield is high, but limiting of being gasified
System, has certain restriction, the thermal source being pyrolyzed in addition substantially gas heat carrier, follow-up dedusting pressure in large-scale promotion
It is too big.The low temperature pyrogenation method of solid fuel in the A counter-current downer pyrolysis reactors of patent CN 102127460.The patent is
It is reverse-flow, material from top to bottom, gas from bottom to top, the method that heat is heated by gas and side wall, the method due to fine coal at
In suspended state, and gas heat carrier and indirect heat exchange are used, gas heat carrier amount is big, and a large amount of fine breezes are taken out of with gas, make
It is difficult into follow-up raw coke oven gas dedusting.The riser pulverized coal pyrolysis method of patent 201410673063.3 and patent 201410673070.3
Hot carrier gas lifts the pulverized coal pyrolysis method of fast reaction, and using the hot 0.1mm-5mm fine coal of feed coal, pyrolysis temperature is 400-800
DEG C, pressure is 0.1-3MPa, reaction time 1-10s, due to that cannot accomplish flashing speed oven using raw material is larger, it is impossible in riser
Be pyrolyzed during lifting, certainly will be pyrolyzed in expansion chamber, rough dedusting has used built-in whirlwind, but the specification of undeclared whirlwind and
Arrangement, it is impossible to reach efficient dedusting, carries substantial amounts of dust in coal tar after cooling, cannot subsequently utilize, using interior
The oil gas residence time put after the expansion chamber pyrolysis of whirlwind is long, causes coal tar second pyrolysis, reduces the yield of tar, together
When pyrolysis temperature not in rational scope, 400 DEG C cannot be pyrolyzed, and 800 DEG C of pyrolysis are excessive, and tar yield is extremely low.Patent
A kind of 201410625795.5 following current downstriker coal gas semicoke activation pulverized coal pyrolysis system and method, raw materials used is 200 purposes
(being less than 0.1mm) fine coal, is flashing speed oven in solid thermal carriers down pipe, and coal gas is activated in conveying solid substance heat carrier, is separated
Crude separation is carried out using gravitational settling and built-in two grades of whirlwind groups, it is to avoid tar separates out and collection is combined with coal dust when there is thermograde
Block is blocked, and also improves the yield of the tar of pyrolysis, and down-flow fluidized bed using ECT energy consumption is relatively low, but expansion chamber after pyrolysis is big, and pyrolysis oil gas stops
Stay the time more long, the yield of a certain degree of cracking influence tar.On the whole using higher, the one-time investment of descending bed apparatus
It is larger.Patent CN 101935539A carrying out catalytic pyrolysis on pulverized pyrolysis prepares the method and its device and patent of coal tar
A kind of methods for improving pyrolysis of coal tar yield as reaction gas with methane of CN1664069A, are metal supported catalyst methane activation
It is pyrolyzed in atmosphere, the yield of coal tar can be greatly improved, but due to the easy coking inactivation of catalyst, it is impossible to ensure device long period
Stable operation.
Above patent not with regard to holding fast pyrogenation, quick derivation, quick cooling during pyrolysis of coal well, satisfy by free radical
The mechanism of sum, and high-temperature oil gas are easily condensed coking and blocking, energy consumption, one-time investment aspect optimization, otherwise cause oil productivity
It is low, otherwise investment, energy consumption it is higher.On the premise of tar yield is improved, optimization high-temperature oil gas are easily condensed coking and block up the present invention
Plug, abrasion, once comprehensive energy consumption, the factor such as investment, propose targetedly firm scheme.
The content of the invention
In existing coal tar preparation method pyrolysis of coal optimization it is bad, cause oil productivity it is low, investment high energy consumption technical problem,
A kind of solid thermal carriers activation coal gas flashing speed oven coal preparing coal is to provide in order to solve one of the technical problem, the object of the invention
The system of tar, coal gas and semicoke.The two of the object of the invention are to provide a kind of solid thermal carriers activation coal gas flashing speed oven coal system
The method for taking coal tar, coal gas and semicoke.
To achieve these goals, a kind of solid thermal carriers activation coal gas flashing speed oven coal preparing coal of the present invention
The system of tar, coal gas and semicoke is：
The system that a kind of solid thermal carriers activation coal gas flashing speed oven coal produces coal tar, coal gas and semicoke, its it is special it
Place is to include raw coal Preliminary working device, pyrolytic reaction separator, semicoke heated separator, circulation recycling device, coal tar
Retracting device and Semi-coke cooling device；Pyrolytic reaction separator a part of semi-coke powder out enters semicoke heated separator
10, the high-temperature flue gas from semicoke heated separator 10 out enter circulation recycling device, and the coal tar recovering device is produced
Soft coal Jiao's oil and gas, the Semi-coke cooling device produces semicoke；
The raw coal Preliminary working device includes Vertical Mill 14, dries cyclone separator 3, sack cleaner 2, flue gas recirculation blower fan
1st, dry coal surge bunker 4, dry coal intermediate bin 5 and dry coal conveying storehouse 6 a, entrance of the Vertical Mill 14 connects raw coal, and another enters
Mouth connects 300~350 DEG C of high-temperature flue gas, and the outlet of the Vertical Mill 14 connects the entrance for drying cyclone separator 3, dries cyclonic separation
The one outlet of device 3 connects sack cleaner 2, and another outlet connects an entrance of dry coal surge bunker 4, the sack cleaner
One outlet connects another entrance of dry coal surge bunker 4, and the outlet of dry coal surge bunker 4 is connected with the entrance of dry coal intermediate bin 5, does
The outlet of coal intermediate bin 5 is connected with an entrance in dry coal conveying storehouse 6, and another entrance in dry coal conveying storehouse 6 connects coal gas, dry coal
The outlet for conveying storehouse 6 is connected with pyrolytic reaction separator；
The pyrolytic reaction separator includes activation fast bed 8-17, semicoke surge bunker 8-7, pyrolysis riser 8-9, sedimentation
Room and the gas-solid separator in expansion chamber and and pyrolysis cyclone unit, the top of the expansion chamber is set
There is collection chamber 8-1；
Coal feed point, the coal gas of high temperature import for being exported with dry coal conveying storehouse 6 and being connected are provided with the activation fast bed 8-17
The upper end of 8-19 and high-temperature semi-coke charging aperture 8-18, the activation fast bed 8-17 connects with the arrival end of pyrolysis riser 8-9
Connect, the outlet of the pyrolysis riser 8-9 is connected with the entrance of gas-solid separator, and the gas that the gas-solid separator is isolated leads to
Cross the entrance that gas vent enters pyrolysis cyclone unit；The semicoke that the gas-solid separator is isolated stays in gas-solid
Enter expansion chamber in separator and along gas-solid separator；By being pyrolyzed secondary semicoke that cyclone unit is separate along heavy
Drop room moves down, and the gas for by being pyrolyzed cyclone unit separate enters collection chamber 8-1 by exporting；The semicoke surge bunker
Product semicoke discharge gate 8-8 and circulation semicoke discharge gate 8-16, the product semicoke discharge gate 8-8 and semicoke are provided with 8-7
Cooling device is connected, and the circulation semicoke discharge gate 8-16 is connected with semicoke heated separator；The semicoke surge bunker 8-7 with it is heavy
The lower end connection of room is dropped；Raw coke oven gas export mouth 8-11, the raw coke oven gas export mouth 8-11 and coal are provided with the collection chamber 8-1
Tar recovery system is connected.
The housing of above-mentioned expansion chamber 8-13 include successively from the bottom up first straight line section, the first flared section, second straight line section,
Second flared section, the 3rd straightway and gas collecting segment, the collection chamber 8-1 are located at gas collecting segment；
The gas-solid separator includes expansion chamber inner housing 8-14, is pyrolyzed fast parted hair 8-4, one-level stripper plant and two grades of vapour
Device is carried, one end of the expansion chamber inner housing 8-14 is located at the second flared section, the other end of the expansion chamber inner housing 8-14
Positioned at the 3rd straightway, the one-level stripper plant is located in interior expansion chamber inner housing 8-14, and two grades of stripper plants are located at
At the second straight line section of expansion chamber 8-13；The one-level stripper plant includes the one-level taper drainage cone being sequentially placed from top to bottom
The big footpath section of 8-5, one-level cone bucket 8-6 and one-level stripping gas endless tube 8-21, the one-level cone bucket 8-6 and one-level taper drainage cone
The big footpath section of 8-5 is relative, and air-vent is offered on the one-level taper drainage cone 8-5 and one-level cone bucket 8-6, and one-level taper is drawn
The cone angle of flow cone 8-5 is 55~75 °, and the cone angle of one-level cone bucket 8-6 is 125~105 °；
Two grades of stripper plants include the two grades of taper drainages cone 8-22, the two grades of cone bucket 8-23 that are sequentially placed from top to bottom
And two grades of stripping gas endless tube 8-24；The big footpath section of two grades of cone bucket 8-23 and two grades of big footpath section phases of taper drainage tube 8-22
It is right, offer air-vent on two grades of taper drainage tube 8-22 and two grades of cone bucket 8-23, two grades of taper drainage tube 8-22's
Cone angle is 55~75 °, and two grades of cone angles of cone bucket 8-23 are 125~105 °；
The port of export of the pyrolysis riser 8-9 is located in expansion chamber inner housing 8-14 through semicoke surge bunker 8-7；It is described
Sedimentation passage in being formed between expansion chamber inner housing 8-14 and pyrolysis riser 8-9, the fast parted hair 8-4 of pyrolysis is arranged on pyrolysis
The port of export of riser 8-9, the semicoke separated by being pyrolyzed fast parted hair 8-4 is gathered in interior sedimentation passage and along expansion chamber
Inner housing 8-14 is moved down, and into the second straight line section of expansion chamber 8-13, is entered by the gas for separating for being pyrolyzed fast parted hair 8-4
It is pyrolyzed the entrance of cyclone unit；
Circumferential weld is provided between the expansion chamber inner housing 8-14 and the housing of expansion chamber 8-13.
The housing of above-mentioned expansion chamber 8-13 include successively from the bottom up first straight line section, the first flared section, second straight line section,
Second flared section, the 3rd straightway and gas collecting segment, the collection chamber 8-1 are located at gas collecting segment；
The gas-solid separator includes center cyclone separator 8-20, one-level stripper plant and two grades of stripper plants, described
The solid outlet of center cyclone separator 8-20 is located at the second flared section, and the gas of the center cyclone separator 8-20 goes out
Mouthful it is located at the 3rd straightway, the one-level stripper plant is located in center cyclone separator 8-20, the one-level cone bucket 8-6's
Big footpath section is relative with the big footpath section of one-level taper drainage cone 8-5, on the one-level taper drainage cone 8-5 and one-level cone bucket 8-6
Air-vent is offered, the cone angle of one-level taper drainage cone 8-5 is 55~75 °, the cone angle of one-level cone bucket 8-6 is 125~105 °；
Two grades of stripper plants are located at the second straight line of expansion chamber 8-13 section；The one-level stripper plant is included from upper
One-level taper drainage cone 8-5, the one-level cone bucket 8-6 and one-level stripping gas endless tube 8-21 being sequentially placed under,
Two grades of stripper plants include the two grades of taper drainages cone 8-22, the two grades of cone bucket 8-23 that are sequentially placed from top to bottom
And two grades of stripping gas endless tube 8-24；The big footpath section of two grades of cone bucket 8-23 and two grades of big footpath section phases of taper drainage tube 8-22
It is right, offer air-vent on two grades of taper drainage tube 8-22 and two grades of cone bucket 8-23, two grades of taper drainage tube 8-22's
Cone angle is 55~75 °, and two grades of cone angles of cone bucket 8-23 are 125~105 °；
The pyrolysis riser 8-9 outside expansion chamber 8-13, the outlet of pyrolysis riser 8-9 and center cyclone separator
8-20 entrances are connected.
Above-mentioned semicoke heated separator includes fluid bed combustion-supporting chamber 10-6, second-time burning air inlet pipe 10-13, heater riser tube
10-5, high-temperature semi-coke expansion chamber 10-3 and the outdoor semicoke cyclone unit with flutter valve of high-temperature semi-coke sedimentation, institute
State and circulation semicoke charging aperture 10-7, fluidizer air inlet 10-14 and second-time burning are provided with fluid bed combustion-supporting chamber 10-6 enter
Gas port 10-8, is provided with second-time burning air inlet pipe 10-13, the fluid bed combustion-supporting chamber 10-6 in the fluid bed combustion-supporting chamber 10-6
Upper end connected with one end of heater riser tube 10-5, it is fast to be provided with high-temperature semi-coke on the other end of the heater riser tube 10-5
Parted hair 10-12, the high-temperature semi-coke expansion chamber 10-3 cover on the upper end of heater riser tube 10-5, the high-temperature semi-coke expansion chamber
The lower end of 10-3 is fixed on heater riser tube 10-5, and the bottom of the high-temperature semi-coke expansion chamber 10-3 is provided with high-temperature semi-coke and goes out
Mouth 10-4, the high-temperature semi-coke exports 10-4 and is connected with high-temperature semi-coke charging aperture 8-18, the high-temperature semi-coke expansion chamber 10-3's
Upper end is provided with flue gas export mouth 10-11, and the flue gas export mouth is connected with the entrance of semicoke cyclone unit, and described half
The outlet of burnt cyclone unit is connected with circulation recycling device.
Above-mentioned circulation recycling device includes afterburning chamber 11, high-temperature gas heat exchanger 12 and desulfurization and denitrification reaction device 13, institute
The outlet for stating cyclone separator group is connected with the entrance of afterburning chamber 11, outlet and the high-temperature gas heat exchanger 12 of the afterburning chamber 11
Connection, while what is be connected with high-temperature gas heat exchanger 12 also has outlet, the coal gas of coal tar generation device of flue gas recirculation blower fan 1
Air outlet slit after outlet and pressurization, the entrance of the flue gas recirculation blower fan 1 connects another outlet of sack cleaner 2；It is described
The outlet of high-temperature gas heat exchanger 12 is connected with the entrance of desulfurization and denitrification reaction device 13, while the outlet of high-temperature gas heat exchanger 12
Also it is connected with coal gas of high temperature import 8-19, fluidizer air inlet 10-14 and secondary combustion air inlets 10-8, the desulphurization denitration
The outlet of reactor 13 is connected with Vertical Mill 14；
The Semi-coke cooling device includes high-temperature semi-coke cooler 7, and the entrance of the high-temperature semi-coke cooler practices midwifery product partly
Burnt discharge gate 8-8, another entrance of high-temperature semi-coke cooler 7 connects desalted water, and the one outlet of high-temperature semi-coke cooler 7 connects steaming
Vapour；
The coal tar recovering device includes quencher 9, filter collector 15, oil scrubber 16, bottom of towe oil circulating pump 17, tower
Top reflux pump 18, horizontal water-tube cooler 19, electric coke booster oil device 20 and coal gas circulating fan 21；The entrance and coal of the quencher 9
Conductance outlet 8-11 connections, the outlet of the quencher 9 is connected with the entrance of filter collector 15, the filter collector 15
Outlet is connected with the bottom of oil scrubber 16, and the bottom of the oil scrubber 16 is connected with bottom of towe oil circulating pump 17, the top of the oil scrubber 16
Overhead reflux pump 18 is connected with, the bottom of towe oil circulating pump 17 reclaims heavy coal tar, and the overhead reflux pump 18 reclaims lightweight
Coal tar；The top exit of oil scrubber 16 is connected with the entrance of horizontal water-tube cooler 19, the outlet electric fishing of the horizontal water-tube cooler 19
Tar device 20, produces coal gas, a portion coal gas to discharge after electrical tar precipitator 20, and another part coal gas is through coal gas circulated air
Machine 21 enters the gas entry of high-temperature gas heat exchanger 12.
Above-mentioned pyrolysis cyclone unit includes 1-3 pyrolysis cyclone separator group, the pyrolysis cyclone separator group
Including multiple pyrolysis cyclone separators in parallel；
The semicoke cyclone unit includes the semicoke primary cyclone group with flutter valve being sequentially connected
10-1, semicoke secondary cyclone group 10-2 and semicoke three-stage cyclone separator group 10-3.
The above-mentioned fast parted hair 8-4 of pyrolysis is that the fast parted hair of umbrella hat type or three leaf spiral-flow types (VQS) are fast separately, the three leaves spiral-flow type
The lower swing angle of fast parted hair is 20 °, and aperture area is 0.75-0.85 with pyrolysis riser area ratio.
The method for producing coal tar, coal gas and semicoke, it is characterised in that comprise the following steps：
1) raw material preliminary working：
Raw coal feeding Vertical Mill 14 is ground, is 300~350 DEG C of high temperature flue gas drying selection by winnowing, 85%-90% particle diameters through temperature
Below 0.1mm, moisture are reached below 2%, after Vertical Mill flue gas pressures are tiny structure, by dried coal dust by drying whirlwind
After separator 3, dry pulverized coal surge bunker 4 and sack cleaner 2 are fed sequentially into, coal dust is stored in dry pulverized coal surge bunker 4；
2) activation fast bed reaction：
2.1) temperature is 750~850 DEG C of high-temperature semi-coke powder by high-temperature semi-coke charging aperture 8-18 into pyrolytic reaction point
From the activation fast bed 8-17 of device 8；The coal gas of high temperature that temperature is 550~650 DEG C, pressure is 0.01~2MPa passes through coal gas of high temperature
Import 8-19 enters activation fast bed 8-17；The gas velocity of coal gas of high temperature is 0.5~3m/s, and high-temperature semi-coke powder is by coal gas of high temperature in work
Change the bottom activation of fast bed；
2.2) coal dust that temperature in dry pulverized coal surge bunker 4 is 80~120 DEG C will be stored in and is forced into 0.01 through dry coal conveying storehouse 6
Activation fast bed top is entered by coal feed point after~2Mpa；The mixing quality ratio of high-temperature semi-coke powder and coal dust for (2.5~
5):1
2.3) coal dust mixes with coal gas and high-temperature semi-coke powder after activation on activation fast bed top；
3) pyrolytic reaction：
Coal dust carries out pyrolytic reaction with the pyrolysis riser 8-9 that enters of high-temperature semi-coke powder after mixing, in pyrolysis riser 8-9
Pyrolysis temperature is 480~750 DEG C, and synthesis pressure is 0.01~2MPa, and gas velocity is 8-16m/s, is lifted through pyrolysis after pyrolytic reaction
The gas-solid separator 4 of pipe 8-9 outlets is separated；
4) separate：
4.1) after being pyrolyzed 480~750 DEG C of a semi-coke powder in the presence of gravity and inertia force mass settlement in gas-solid
Separator is moved down, while strip coal gas boring stripping distributor 8-5 by semi-coke powder into ring by stripping gas inlet 8-15
Residual oil gas stripping, the temperature of stripping gas is identical with pyrolysis temperature, pressure is 0.01~2MPa, and section gas velocity is not more than 0.1m/
s；
4.2) raw coke oven gas of 480~750 DEG C after pyrolysis sequentially enters pyrolysis one by the gas vent of gas-solid separator
After level cyclone separator group 8-3, pyrolysis secondary cyclone group 8-2, pyrolysis three-stage cyclone separator group 8-12 are separated, in collection
Air chamber 8-1 is used to prepare coal gas and coal tar after being derived through raw coke oven gas export mouth 8-11 after collecting；
Expansion chamber 8-13 is entered through being pyrolyzed the secondary semi-coke powder after cyclone unit is separated, and in gas-solid separator
One time semi-coke powder is moved downwardly together, into semicoke surge bunker 8-7, low temperature semicoke to be prepared；
5) high-temperature semi-coke reprocessing：
A part of 480~750 DEG C of semi-coke powders enter through circulating semicoke discharge gate 8-16 and circulation semicoke in semicoke surge bunker 8-7
Material mouth 10-7 enters the fluid bed combustion-supporting chamber 10-6 of semicoke heated separator 10, enters to become a mandarin with by fluidizer air inlet 10-14
After 450~550 DEG C of Air Fluidizeds of temperature burning of Hua Chuan combustion-supporting chamber, and with pass sequentially through secondary combustion air inlets 10-8 and secondary
After the temperature of burning charge pipe 10-13 is burnt again for 450~550 DEG C of high-temperature flue gas；The fluidizing gas velocity of fluid bed be 0.2~
1m/s。
Heated riser 10-5 is lifted into high-temperature semi-coke expansion chamber 10-3, the semi-coke powder and high-temperature gas after burning
Temperature is 750~850 DEG C, and pressure is 0.01~2MPa, and the lifting gas velocity of heater riser tube 10-5 is 8~16m/s, semi-coke powder warp
After the fast parted hair 10-12 of high-temperature semi-coke at the top of heater riser tube 10-8 separates sedimentation；
High-temperature flue gas sequentially enter external semicoke one cyclonic and separate through semicoke heated separator flue gas export mouth 10-11
Device group 10-2, semicoke secondary cyclone group 10-1, semicoke three-stage cyclone separator group 10-10 are separated, the semicoke after separation
Powder discharges 750~850 after entering high-temperature semi-coke expansion chamber 10-3 through the flutter valve of cyclone separator by high-temperature semi-coke outlet 10-4
DEG C high-temperature semi-coke powder it is stand-by；750~850 DEG C of high-temperature flue gas are treated after the outlet of semicoke three-stage cyclone separator group 10-3
With；
6) coal gas and coal tar are prepared：
Cooled down with 250~300 DEG C of Low Temperature Steam heat exchange in quencher 9 through raw coke oven gas derived from raw coke oven gas export mouth 8-11
By being rapidly cooled between 360~400 DEG C for 480~750 DEG C of raw coke oven gas, subsequently into filter collector dust removal by filtration, dedusting
Raw coke oven gas afterwards enters the bottom of oil scrubber 16 and reclaims heavy coal tar by the spray washing of bottom of towe oil circulating pump 17, by overhead reflux pump
Light tar is reclaimed in 18 coolings；
The tower overhead gas of oil scrubber 16 cools down laggard electrical tar precipitator 20 and reclaims light oil and pyrolysis water into horizontal water-tube cooler 19,
Coal gas is generated after electric fishing；A part of coal gas discharge, another part is recycled into high-temperature gas and exchanges heat through coal gas circulating fan 21
The gas entry of device 12；
7) low temperature semicoke is prepared：
480~750 DEG C of semi-coke powders part in semicoke surge bunker 8-7 enters high temperature half through product semicoke discharge gate 8-8
Burnt cooler 7, semi-coke powder is cooled to less than 80 DEG C by desalted water and steam heat-exchanging in the high-temperature semi-coke cooler 7 stores in a warehouse；
Wherein step 5), 6), 7) while carrying out or being carried out according to timing requirements.
Further, also including recycling step, specially：
8.1) 750~850 DEG C of the temperature of semicoke heated separator discharge, the high-temperature flue gas that pressure is 0.01~2MPa enter
Afterburning chamber 11, obtains the high-temperature flue gas that temperature is raised to 850~950 DEG C after burning, afterwards into high-temperature gas heat exchanger 12；
8.2) high-temperature gas heat exchanger 12 is received：It is later 80 from flue gas recirculation blower fan temperature through the dedusting of sack cleaner 2
~120 DEG C, the circulating flue gas that pressure is 0.01~2Mpa；The temperature exported through coal gas circulating fan 21 is discharged from electrical tar precipitator 20
Spend for circulating gas that 25~50 DEG C, pressure are 0.01~2Mpa；And the sky that temperature is 25 DEG C, pressure is 0.01~2Mpa
Gas；
850~950 DEG C of high-temperature flue gas obtain temperature 450 with after circulating flue gas, circulating gas and air heat-exchange respectively
~550 DEG C, the circulating flue gas that pressure is 0.01~2Mpa；The circulation coal that temperature is 600~650 DEG C, pressure is 0.01~2Mpa
Gas；And the air that temperature is 450~550 DEG C, pressure is 0.01~2Mpa；
8.3) 300~350 DEG C of temperature, the flue gas that pressure is 0.01~2Mpa are sent to and are depressurized after desulfurization and denitrification reaction device 13
For normal pressure is dried selection by winnowing into Vertical Mill 14 to raw coal；
The circulating gas input coal gas of high temperature import 8-19 that temperature is 550~650 DEG C, pressure is 0.01~2Mpa；
The air that temperature is 450~550 DEG C, pressure is 0.01~2Mpa enters fluidisation by fluidizer air inlet 10-14
Bed combustion-supporting chamber 10-6；
450~550 DEG C of temperature, the circulating flue gas that pressure is 0.01~2Mpa feeding secondary combustion air inlets 10-8.
Further, step 4) it is specially：
4.1) after being pyrolyzed 480~750 DEG C of a semi-coke powder in the presence of gravity and inertia force mass settlement in sedimentation
The second straight line section of indoor housing 8-14 and expansion chamber is moved down, while strip coal gas enters one-level by stripping gas inlet 8-15
Stripping endless tube and two grades of stripping endless tubes, by the residual oil gas stripping in semi-coke powder, the temperature of stripping gas is identical with pyrolysis temperature, press
Power is 0.01~2MPa, and section gas velocity is not more than 0.1m/s；
4.2) top exit that the raw coke oven gas of 480~750 DEG C after pyrolysis passes through expansion chamber inner housing 8-14, sequentially enters
Pyrolysis primary cyclone group 8-3, pyrolysis secondary cyclone group 8-2, pyrolysis three-stage cyclone separator group 8-12 are separated
Afterwards, coal gas and coal tar are prepared after being derived through raw coke oven gas export mouth 8-11 after collection chamber 8-1 collects；
Expansion chamber 8-13 is entered through being pyrolyzed the secondary semi-coke powder after cyclone unit is separated, by expansion chamber inner housing
Circumferential weld on 8-14 is simultaneously moved downwardly together with a semi-coke powder in expansion chamber inner housing 8-14, into semicoke surge bunker 8-7,
Low temperature semicoke to be prepared.
Advantage for present invention：
1st, the system that solid thermal carriers activation coal gas flashing speed oven coal of the present invention produces coal tar, coal gas and semicoke is held fast
Speed heat solution, quick derivation, quick cooling.Using less than 0.1mm materials during lifting flashing speed oven, top is adopted separately soon
The mode of materials dnockout reduces the abrasion of equipment and realizes quick separating sedimentation, and gas phase is introduced directly into multistage cyclone group and removes
Dirt, the gas residence time before cooling greatly shortens, it is to avoid the second pyrolysis of tar gas, and multistage cyclone group is built in inside and outside
Between chuck, it is to avoid whirlwind ties carbon due to thermograde, high temperature raw coke oven gas and Low Temperature Steam are exchanged heat cooling in quencher
Rapidly cooling dew point more than, it is ensured that do not separate out tar while preventing the second pyrolysis of oil gas.The sedimentation of pyrolytic reaction separator
Room is designed to baffling cone sample, increases the flowing time of semi-coke powder, to improve Srteam Stripping effect, increases the yield of coal tar.
2nd, system design of the invention rationally, will be pyrolyzed the part high-temperature semi-coke powder that obtains as semicoke heated separator
Raw material, and be set to fluid bed and increased the burning residence time in heater base make hot semicoke in bottom conflagration, burning
Afterburning hoisting way is carried out by intermediate gas pipe again afterwards, not only firm high-temperature semi-coke is bottom is compared with the problem of difficult to burn but also reduces
The volume of fluid bed, top solves solid material to equipment by the way of point expansion chamber soon and external how sub multigroup whirlwind
Abrasion and efficiency of dust collection it is low bottleneck, turn avoid built-in high-temp. vortex difficulty, will be produced by semicoke heated separator again
High-temperature flue gas are circulated utilization as the energy of pyrolysis, and energy is rationally utilized, it is not necessary to individually heating, energy-saving, investment
It is small.
3rd, the present invention activates coal gas in fast bed, participates in the yield that pyrolysis improves tar.
Brief description of the drawings
Fig. 1 is the process chart of embodiment 1.
Fig. 2 is a kind of structural representation of the pyrolytic reaction separator of Fig. 1.
Fig. 3 is another structural representation of the pyrolytic reaction separator of Fig. 1
Fig. 4 is the structural representation of the semicoke heated separator of Fig. 1.
Wherein reference is：1- flue gas recirculation blower fans, 2- sack cleaners, 3- dries cyclone separator, and 4- dry coals delay
Rush storehouse, 5- dry coal intermediate bins, 6- dry coals conveying storehouse, 7- high-temperature semi-coke coolers, 8- pyrolytic reaction separators, 9- quenchers, 10-
Semicoke heated separator, 11- afterburning chambers, 12- high-temperature gas heat exchangers, 13- desulfurization and denitrification reaction devices, 14- Vertical Mills, 15- filterings
Deduster, 16- oil scrubbers, 17- bottom of towe oil circulating pumps, 18- overhead reflux pumps, 19- horizontal water-tube coolers, 20- electrical tar precipitators,
21- coal gas circulating fans, 8-1 collection chambers, 8-2 is pyrolyzed two grades of rotation packets, and 8-3 pyrolysis one cyclonic groups, 8-4- pyrolysis is fast separately,
8-5 one-level tapers drainage is bored, 8-6 one-level cone buckets, 8-7 semicoke surge bunkers, 8-8 product semicoke discharge gates, 8-9 pyrolysis risers,
8-10 coal feed points, 8-11 raw coke oven gas export mouths, 8-12 pyrolysis three-level whirlwind groups, 8-13 expansion chambers, 8-14 expansion chamber inner housings, 8-
15 stripping gas imports, 8-16 circulation semicoke discharge gates, 8-17 activation fast beds, 8-18 high-temperature semi-coke charging apertures, 8-19 high-temperature coals
Gas import, 8-20 centers cyclone separator, 8-21 one-level stripping gas endless tubes, bis- grades of taper drainage cones of 8-22, bis- grades of cone buckets of 8-23,
Bis- grades of stripping gas endless tubes of 8-24, two grades of whirlwind groups of 10-1 semicokes heated separator, 10-2 semicoke heated separator one cyclonic groups,
10-3 high-temperature semi-coke expansion chambers, the outlet of 10-4 high-temperature semi-cokes, 10-5 heater riser tubes, 10-6 fluid beds combustion-supporting chamber；10-7 is circulated
Semicoke charging aperture, 10-8 secondary combustion air inlets, 10-9 semicokes heating cyclone separator exhanst gas outlet, the heating point of 10-10 semicokes
From device three-level whirlwind group, 10-11 semicoke heated separator flue gas export mouths, the fast parted hair of 10-12 high-temperature semi-cokes, bis- combustions of 10-13
Burn into tracheae, 10-14 fluidizer air inlets.
Specific embodiment
Technical scheme is further described with embodiment in conjunction with accompanying drawing, but the present invention is not limited only to
Following implementation situations.
Embodiment 1：As shown in figure 1, a kind of solid thermal carriers activation coal gas flashing speed oven coal produces coal tar, coal gas and half
Burnt system, including raw coal Preliminary working device, pyrolytic reaction separator, semicoke heated separator, circulation recycling device, coal tar
Oil recovery apparatus and Semi-coke cooling device；Pyrolytic reaction separator a part of semi-coke powder out enters semicoke heated separator
10, pyrolytic reaction separator is used to for dry coal pyrolysis to produce raw coke oven gas and middle temperature semicoke；Semicoke heated separator is used for middle temperature
Semicoke further heats separation and produces high-temperature semi-coke and high-temperature flue gas；High-temperature flue gas from semicoke heated separator 10 out enter
Enter circulation recycling device, coal tar recovering device produces coal tar oil and gas using raw coke oven gas；During Semi-coke cooling device is utilized
Warm semicoke produces low temperature semicoke；
Raw coal Preliminary working device includes Vertical Mill 14, dries cyclone separator 3, sack cleaner 2, flue gas recirculation blower fan 1, dry
Coal surge bunker 4, dry coal intermediate bin 5 and dry coal conveying storehouse 6, an entrance of Vertical Mill 14 connects raw coal, and another entrance connects 300~
350 DEG C of high-temperature flue gas, the outlet of Vertical Mill 14 connects the entrance for drying cyclone separator 3, dries the one outlet of cyclone separator 3
Sack cleaner 2 is connect, another outlet connects an entrance of dry coal surge bunker 4, the one outlet of sack cleaner connects dry coal and delays
Another entrance in storehouse 4 is rushed, the outlet of dry coal surge bunker 4 is connected with the entrance of dry coal intermediate bin 5, the outlet of dry coal intermediate bin 5
An entrance with dry coal conveying storehouse 6 be connected, and another entrance in dry coal conveying storehouse 6 connects coal gas, the outlet in dry coal conveying storehouse 6 and
Pyrolytic reaction separator is connected.
Pyrolytic reaction separator include activation fast bed 8-17, semicoke surge bunker 8-7, pyrolysis riser 8-9, expansion chamber,
And gas-solid separator in expansion chamber and and pyrolysis cyclone unit, the top of expansion chamber is provided with collection chamber
8-1；Be provided with activation fast bed 8-17 exported with dry coal conveying storehouse 6 be connected coal feed point, coal gas of high temperature import 8-19 and
The upper end of high-temperature semi-coke charging aperture 8-18, activation fast bed 8-17 is connected with the arrival end of pyrolysis riser 8-9, is pyrolyzed riser
The outlet of 8-9 is connected with the entrance of gas-solid separator, and the gas that gas-solid separator is isolated enters pyrolysis and revolves by gas vent
The entrance of wind separator unit；The semicoke that gas-solid separator is isolated is stayed in gas-solid separator and along gas-solid separator
Into expansion chamber；The secondary solid semicoke for by being pyrolyzed cyclone unit separate is moved down along expansion chamber, by being pyrolyzed whirlwind
The gas that separator unit is separate enters collection chamber 8-1 by exporting；Product semicoke discharge gate is provided with semicoke surge bunker 8-7
8-8 is connected with circulation semicoke discharge gate 8-16, product semicoke discharge gate 8-8 with Semi-coke cooling device, circulation semicoke discharge gate 8-
16 are connected with semicoke heated separator；Semicoke surge bunker 8-7 is connected with the lower end of expansion chamber；Waste coal is provided with collection chamber 8-1
Conductance exports 8-11, and raw coke oven gas export mouth 8-11 is connected with coal tar recovering device.By being pyrolyzed the product that riser 8-9 is pyrolyzed
Separated by gas-solid separator, gas enters pyrolysis cyclone unit carries out secondary separation, and semi-coke powder is gathered in gas
Expansion chamber into semicoke surge bunker 8-7 is moved downwards through in solid separator.The housing of expansion chamber 8-13 is wrapped successively from the bottom up
Include first straight line section, the first flared section, second straight line section, the second flared section, the 3rd straightway and gas collecting segment, collection chamber 8-1
In gas collecting segment.
Semi-coke cooling device includes high-temperature semi-coke cooler 7, and the entrance of high-temperature semi-coke cooler is practiced midwifery product semicoke discharge gate
8-8, another entrance of high-temperature semi-coke cooler 7 connects desalted water, and the one outlet of high-temperature semi-coke cooler 7 connects steam；
Coal tar recovering device includes that quencher 9, filter collector 15, oil scrubber 16, bottom of towe oil circulating pump 17, tower top are returned
Stream pump 18, horizontal water-tube cooler 19, electric coke booster oil device 20 and coal gas circulating fan 21；The entrance of quencher 9 and coal gas export mouth
8-11 is connected, and the outlet of quencher 9 is connected with the entrance of filter collector 15, outlet and the bottom of oil scrubber 16 of filter collector 15
Portion connects, and the bottom of oil scrubber 16 is connected with bottom of towe oil circulating pump 17, and the top of oil scrubber 16 is connected with overhead reflux pump 18, bottom of towe oil
Circulating pump 17 reclaims heavy coal tar, and overhead reflux pump 18 reclaims light tar；The top exit of oil scrubber 16 is cold with transverse tube
But the entrance connection of device 19, the outlet electrical tar precipitator 20 of horizontal water-tube cooler 19 produces coal gas after electrical tar precipitator 20, wherein
A part of coal gas discharge, another part coal gas enters the gas entry of high-temperature gas heat exchanger 12 through coal gas circulating fan 21.Oil wash
Tower middle part mouth spray and heavy oil outlet are connected with bottom of towe oil circulating pump；Overhead reflux pump and light tar are arranged at oil scrubber top
Outlet, oil scrubber top gas outlet is connected with horizontal water-tube cooler entrance, and horizontal water-tube cooler is exported and electrical tar precipitator entrance
It is connected, electrical tar precipitator outlet is connected with coal gas circulating fan, electrical tar precipitator is connected with light oil and water with cooler is traversed
Outlet.
Embodiment 2：For energy-saving and emission-reduction, energy recycling.Circulation recycling device of the present invention includes afterburning chamber 11, height
Warm gas heat exchanger 12 and desulfurization and denitrification reaction device 13, the outlet of cyclone separator group are connected with the entrance of afterburning chamber 11, afterburning
The outlet of room 11 is connected with high-temperature gas heat exchanger 12, while the flue gas that also has being connected with the entrance of high-temperature gas heat exchanger 12 is followed
The outlet of ring blower fan 1, the import of the gas exit and forced air of coal tar generation device, the entrance of flue gas recirculation blower fan 1
Connect another outlet of sack cleaner 2；The outlet of high-temperature gas heat exchanger 12 is connected with the entrance of desulfurization and denitrification reaction device 13,
Simultaneously high-temperature gas heat exchanger 12 outlet also with coal gas of high temperature import 8-19, fluidizer air inlet 10-14 and second-time burning
Air inlet 10-8 is connected, and the outlet of desulfurization and denitrification reaction device 13 is connected with Vertical Mill 14.
Embodiment 3：In order to optimize pyrolytic process, as shown in Fig. 2 gas-solid separator in pyrolytic reaction separator of the invention
Including expansion chamber inner housing 8-14, it is pyrolyzed fast parted hair 8-4, one-level stripper plant and two grades of stripper plants, expansion chamber inner housing 8-
14 one end is located at the second flared section, and the other end of expansion chamber inner housing 8-14 is located at the 3rd straightway, one-level stripper plant position
In in interior expansion chamber inner housing 8-14, two grades of stripper plants are located at the second straight line of expansion chamber 8-13 section；One-level stripper plant
Including the one-level taper drainage cone 8-5, the one-level cone bucket 8-6 and one-level stripping gas endless tube 8-21, one that are sequentially placed from top to bottom
The big footpath section of level cone bucket 8-6 is relative with the big footpath section of one-level taper drainage cone 8-5, one-level taper drainage cone 8-5 and one-level cone bucket
Air-vent is offered on 8-6, the cone angle of one-level taper drainage cone 8-5 and one-level cone bucket 8-6 is 55~75 ° and 125~105 °；
Two grades of stripper plants include the two grades of taper drainages cone 8-22, the two grades of cone bucket 8-23 that are sequentially placed from top to bottom and
Two grades of stripping gas endless tube 8-24；Two grades of big footpath sections of cone bucket 8-23 are relative with the big footpath section of two grades of taper drainage tube 8-22, two grades
Air-vent, two grades of taper drainage tube 8-22 and two grades of cone bucket 8-23 are offered on taper drainage tube 8-22 and two grades of cone bucket 8-23
Cone angle be 55~75 ° and 125~105 °；
The port of export of pyrolysis riser 8-9 is located in expansion chamber inner housing 8-14 through semicoke surge bunker 8-7；The sedimentation
Sedimentation passage in being formed between indoor housing 8-14 and pyrolysis riser 8-9, the fast parted hair 8-4 of pyrolysis is arranged on pyrolysis lifting
The port of export of pipe 8-9, the semicoke separated by being pyrolyzed fast parted hair 8-4 is gathered in interior sedimentation passage and along expansion chamber inner casing
Body 8-14 is moved down, and into the second straight line section of expansion chamber 8-13, pyrolysis is entered by the gas for separating for being pyrolyzed fast parted hair 8-4
The entrance of cyclone unit；Circumferential weld is provided between the housing of expansion chamber inner housing 8-14 and expansion chamber 8-13.Pyrolysis is fast
Parted hair 8-4 is that the fast parted hair of umbrella hat type or three leaf spiral-flow types (VQS) are fast separately, and the lower swing angle of three leaf vortex sepatation system heads is 20 °, is opened
Open area is 0.75-0.85 with pyrolysis riser area ratio.
Embodiment 4：In order to prevent gas rapid condensation, as shown in figure 3, gas-solid point in pyrolytic reaction separator of the invention
Structure from device is：Gas-solid separator includes center cyclone separator 8-20, one-level stripper plant and two grades of stripper plants,
The solid outlet of center cyclone separator 8-20 is located at the second flared section, the gas vent position of center cyclone separator 8-20
At the 3rd straightway, the one-level stripper plant is located in center cyclone separator 8-20, and one-level stripper plant is located at center
In cyclone separator 8-20, two grades of stripper plants are located at the second straight line of expansion chamber 8-13 section；One-level stripper plant include from
One-level taper drainage cone 8-5, one-level cone bucket 8-6 and one-level stripping gas endless tube 8-21 that top to bottm is sequentially placed, two grades of strippings
Device includes the two grades of taper drainages cone 8-22, the two grades of cone bucket 8-23 and two grades of stripping gas endless tube 8- that are sequentially placed from top to bottom
24；Pyrolysis riser 8-9 outside expansion chamber 8-13, the outlet of pyrolysis riser 8-9 and center cyclone separator 8-20 entrances
It is connected.
Stripper plant settling section in the cyclone separator of center sets one, and one is set outside the cyclone separator of center
It is individual.Stripping coal gas is divided by stripping gas inlet 8-15 into one-level stripping gas endless tube 8-21 and two grades of stripping gas endless tube 8-24
Do not stripped by one-level stripper plant, two grades of stripper plants.
Embodiment 5：As shown in figure 4, semicoke heated separator includes fluid bed combustion-supporting chamber 10-6, second-time burning air inlet pipe
The outdoor rotation of the semicoke with flutter valve of 10-13, heater riser tube 10-5, high-temperature semi-coke expansion chamber 10-3 and high-temperature semi-coke sedimentation
Wind separator unit, be provided with fluid bed combustion-supporting chamber 10-6 circulation semicoke charging aperture 10-7, fluidizer air inlet 10-14 and
Secondary combustion air inlets 10-8, is provided with second-time burning air inlet pipe 10-13, fluid bed combustion-supporting chamber in fluid bed combustion-supporting chamber 10-6
The upper end of 10-6 connects with one end of heater riser tube 10-5, and it is fast to be provided with high-temperature semi-coke on the other end of heater riser tube 10-5
Parted hair 10-12, high-temperature semi-coke expansion chamber 10-3 cover on the upper end of heater riser tube 10-5, the lower end of high-temperature semi-coke expansion chamber 10-3
It is fixed on heater riser tube 10-5, the bottom of high-temperature semi-coke expansion chamber 10-3 is provided with high-temperature semi-coke outlet 10-4, high temperature half
Jiao's outlet 10-4 is connected with high-temperature semi-coke charging aperture 8-18, and the upper end of high-temperature semi-coke expansion chamber 10-3 is provided with flue gas export mouth
10-11, flue gas export mouth is connected with the entrance of semicoke cyclone unit, the exhanst gas outlet of semicoke cyclone unit
10-9 is connected with circulation recycling device.
Embodiment 6：In order to further improve yield, slowly moved down through baffling cone baffling, realize fully stripping.The present invention is heavy
The housing for dropping room 8-13 includes first straight line section, the first flared section, second straight line section, the second flared section, the successively from the bottom up
Three straightways and gas collecting segment, collection chamber 8-1 are located at gas collecting segment.
Embodiment 7：In order to submit to separating effect, pyrolysis cyclone unit of the invention to include being sequentially connected pyrolysis one
Level cyclone separator group 8-3, pyrolysis secondary cyclone group 8-2, pyrolysis three-stage cyclone separator group 8-12, each pyrolysis rotation
Wind separator group includes multiple pyrolysis cyclone separators in parallel, is distributed in a ring.
Semicoke cyclone unit include be sequentially connected the semicoke primary cyclone group 10-1 with flutter valve,
Semicoke secondary cyclone group 10-2 and semicoke three-stage cyclone separator group 10-3.
Embodiment 8：Coal tar, coal gas are produced present invention also offers a kind of solid thermal carriers activation coal gas flashing speed oven coal
Method with semicoke is：
(1) raw coal feeding Vertical Mill 14 is ground, is 300~350 DEG C of high temperature cigarettes through the temperature after desulfurization and denitrification reaction device 13
Gas, dries selection by winnowing, and 85%~90% particle diameter reaches below 0.1mm, moisture below 2%, and Vertical Mill flue gas pressures are tiny structure, and
Dried coal dust is fed sequentially into dry coal cyclone dust collectors and sack cleaner 2, coal dust is stored in dry pulverized coal surge bunker 4；
Except the partial fume after coal dust is circulated by flue gas recirculation blower fan 1, partial fume emptying.
(2) high-temperature semi-coke of semicoke heated separator 10 outlet 10-4 temperature be 750~850 DEG C high-temperature semi-coke by height
Warm semicoke charging aperture 8-18 enters the activation fast bed 8-17 of pyrolytic reaction separator 8, the temperature heated by high-temperature gas heat exchanger
Spend for the coal gas of high temperature that 550~650 DEG C, pressure are 0.01~2MPa enters activation fast bed 8- by coal gas of high temperature import 8-19
17, the gas velocity of coal gas of high temperature is 0.5~3m/s, and high-temperature semi-coke is activated by coal gas of high temperature in the bottom of activation fast bed, through dry coal
Temperature is that 80~120 DEG C of coal dusts are forced into 0.01~2MPa by inflating feed cone feeding activation fast bed top by conveying storehouse 6
Coal feed point 8-10, the high-temperature semi-coke after coal dust and activation is mixed and fed into pyrolysis riser 8-9 and enters on activation fast bed top
The mixed proportion of row pyrolytic reaction, semi-coke powder and coal dust is 2.5~5:1, pyrolysis temperature is 480~750 DEG C, and synthesis pressure is
0.01~2MPa, the gas velocity for being pyrolyzed riser is 8-16m/s, pyrolysis of the reacted semi-coke powder through being pyrolyzed at the top of riser 8-9
Fast parted hair 8-4 is separated, and most of semi-coke powder mass settlement in the presence of gravity and inertia force, in expansion chamber inner housing 8-14, is passed through
Baffling cone baffling is slowly moved down, while stripping coal gas by stripping gas inlet 8-15 into one-level stripping gas endless tube 8-21 and two
Level stripping gas endless tube 8-24, is stripped the oil residues in semi-coke powder by one-level stripper plant, two grades of stripper plants respectively
Gas is stripped, and the temperature of stripping gas is identical with pyrolysis temperature, pressure is 0.01~2MPa, and section gas velocity is not more than 0.1m/s, pyrolysis
Raw coke oven gas sequentially enters primary cyclone group 8-3, two grades of rotations quickly through the top exit of expansion chamber inner housing 8-14 afterwards
Wind separator group 8-2, three-stage cyclone separator group 8-12, enter anxious after collection chamber 8-1 collects through raw coke oven gas export mouth 8-11
Cooler 9 is cooled down.Semi-coke powder after separation enters expansion chamber 8-13 and expansion chamber inner housing 8- through the dipleg flutter valve of cyclone separator
The circumferential weld and the semicoke with expansion chamber inner housing 8-14 of 14 centres are moved downwardly together, into semicoke surge bunker 8-7.In quencher
Being rapidly cooled to 480~750 DEG C of raw coke oven gas between 360~400 DEG C is cooled down with 250~300 DEG C of Low Temperature Steam heat exchange in 9,
More than dew point, prevent the second pyrolysis of oil gas from not separating out tar.Subsequently into filter collector dust removal by filtration, the famine after dedusting
Coal gas is cooled down into the bottom of oil scrubber 16 by the spray washing of bottom of towe oil circulating pump 17, and overhead reflux pump 18, is separately recovered heavy
Coal tar and light tar, tower overhead gas cool down laggard electrical tar precipitator 20 and reclaim light oil and pyrolysis into horizontal water-tube cooler 19
Water.Through the coal gas part discharge after electric fishing, another part is recycled into high-temperature gas heat exchanger 12 through coal gas circulating fan 21
Gas entry.
(3) 480~750 DEG C of semi-coke powders part after being pyrolyzed enters high through semicoke surge bunker product semicoke discharge gate 8-8
Warm semicoke cooler 7 and desalted water heat exchange produce steam, semi-coke powder is cooled into less than 80 DEG C and is stored in a warehouse.Another part semi-coke powder is passed through
Circulation semicoke discharge gate 8-16 enters semicoke heated separator 10 by regulating slide valve on pipeline and circulation semicoke charging aperture 10-7
Fluid bed combustion-supporting chamber 10-6, with 450~550 DEG C of skies of temperature for entering fluidized bed combustion-supporting chamber by fluidizer air inlet 10-14
Gas fluidized bed combustion, the fluidizing gas velocity of fluid bed is 0.2~1m/s, and be 450 by the temperature of second-time burning air inlet pipe 10-13
~550 DEG C of oxygen-enriched flue gases burn again and heated riser 10-5 is lifted into high-temperature semi-coke expansion chamber 10-3, after burning
The temperature of semicoke and high-temperature gas is 750~850 DEG C, and pressure is 0.01~2MPa, and the lifting gas velocity of heater riser tube 10-5 is 8
~16m/s, after the fast parted hair 10-12 of high-temperature semi-coke at the top of the boosted pipe of semicoke separates sedimentation, high-temperature flue gas are through semicoke heating point
External semicoke primary cyclone group 10-1, semicoke secondary cyclone group are sequentially entered from device flue gas export mouth 10-11
10-2, semicoke three-stage cyclone separator group 10-10 are separated, semi-coke powder after separation through the lower dipleg of semicoke cyclone separator the wing
Valve enters high-temperature semi-coke expansion chamber 10-3.Flue gas, into afterburning chamber 11, will give birth to through three-level whirlwind outlet during combustion heating
Into a small amount of fuel gas burn, then high-temperature flue gas enter high-temperature gas heat exchanger 12.
(4) 750~850 DEG C of the temperature of semicoke heated separator discharge, the high-temperature flue gas that pressure is 0.01~2MPa enter
Afterburning chamber, temperature is raised to 850~950 DEG C after burning, into high-temperature gas heat exchanger and temperature be 80~120 DEG C, pressure be
0.01~2MPa circulating flue gas, temperature are 25~50 DEG C, pressure be 0.01~2MPa circulating gas and temperature be 25 DEG C, pressure be
0.01~2MPa air is exchanged heat, and the temperature of high-temperature flue gas is reduced to 300~350 DEG C of temperature, pressure for 0.01~2MPa flue gases
Decompression is normal pressure into Vertical Mill 14 after desulfurization and denitrification reaction device, and heated by gas to 600~650 DEG C, pressure is 0.01~2MPa,
Circulating flue gas be heated to 450~550 DEG C, pressure be 0.01~2MPa, air be heated to 450~550 DEG C, pressure be 0.01~
2MPa。
Claims (10)
1. the system that a kind of solid thermal carriers activation coal gas flashing speed oven coal produces coal tar, coal gas and semicoke, it is characterised in that：
Including raw coal Preliminary working device, pyrolytic reaction separator, semicoke heated separator, circulation recycling device, coal tar recovering dress
Put and Semi-coke cooling device；Pyrolytic reaction separator a part of semi-coke powder out enters semicoke heated separator (10), from
High-temperature flue gas in semicoke heated separator (10) out enter circulation recycling device, and the coal tar recovering device produces coal
Burnt oil and gas, the Semi-coke cooling device produces semicoke；
The raw coal Preliminary working device includes Vertical Mill (14), dries cyclone separator (3), sack cleaner (2), flue gas recirculation wind
Machine (1), dry coal surge bunker (4), dry coal intermediate bin (5) and dry coal conveying storehouse (6), an entrance of the Vertical Mill (14) connect original
Coal, another entrance connects 300~350 DEG C of high-temperature flue gas, and the outlet of the Vertical Mill (14) connects and dries entering for cyclone separator (3)
Mouthful, the one outlet for drying cyclone separator (3) connects sack cleaner (2), and another outlet meets of dry coal surge bunker (4)
Entrance, the one outlet of the sack cleaner connects another entrance of dry coal surge bunker (4), the outlet of dry coal surge bunker (4)
Entrance with dry coal intermediate bin (5) is connected, and the outlet of dry coal intermediate bin (5) is connected with an entrance of dry coal conveying storehouse (6), does
Another entrance of coal conveying storehouse (6) connects coal gas, and the outlet of dry coal conveying storehouse (6) is connected with pyrolytic reaction separator；
The pyrolytic reaction separator includes activation fast bed (8-17), semicoke surge bunker (8-7), is pyrolyzed riser (8-9), sinks
Drop room and the gas-solid separator in expansion chamber and pyrolysis cyclone unit, the top of the expansion chamber is set
There is collection chamber (8-1)；
Coal feed point, the coal gas of high temperature import being connected with dry coal conveying storehouse (6) outlet are provided with activation fast bed (8-17)
(8-19) and high-temperature semi-coke charging aperture (8-18), upper end and pyrolysis riser (8-9) of activation fast bed (8-17)
Arrival end is connected, and the outlet of pyrolysis riser (8-9) is connected with the entrance of gas-solid separator, and the gas-solid separator is separated
The gas for going out enters the entrance of pyrolysis cyclone unit by gas vent；The gas-solid separator isolate once half
Jiao stays in gas-solid separator and enters expansion chamber along gas-solid separator；By being pyrolyzed the secondary of cyclone unit separation
Semicoke is moved down along expansion chamber, and the gas for by being pyrolyzed cyclone unit separate enters collection chamber (8-1) by exporting；Institute
State and product semicoke discharge gate (8-8) and circulation semicoke discharge gate (8-16) are provided with semicoke surge bunker (8-7), the product half
Burnt discharge gate (8-8) is connected with Semi-coke cooling device, and circulation semicoke discharge gate (8-16) is connected with semicoke heated separator；
The semicoke surge bunker (8-7) connects with the lower end of expansion chamber；Raw coke oven gas export mouth (8- is provided with the collection chamber (8-1)
11), the raw coke oven gas export mouth (8-11) is connected with coal tar recovering device.
2. solid thermal carriers activation coal gas flashing speed oven coal according to claim 1 produces coal tar, coal gas and semicoke
System, it is characterised in that：The housing of the expansion chamber (8-13) from the bottom up successively include first straight line section, the first flared section,
Second straight line section, the second flared section, the 3rd straightway and gas collecting segment, the collection chamber (8-1) are located at gas collecting segment；
The gas-solid separator includes expansion chamber inner housing (8-14), pyrolysis fast (8-4), one-level stripper plant and two grades of vapour separately
Carry device, one end of the expansion chamber inner housing (8-14) is located at the second flared section, the expansion chamber inner housing (8-14) it is another
One end is located at the 3rd straightway, and the one-level stripper plant is located in interior expansion chamber inner housing (8-14), two grades of strippings dress
At the second straight line section of expansion chamber (8-13)；The one-level stripper plant includes the one-level cone being sequentially placed from top to bottom
Shape drainage cone (8-5), one-level cone bucket (8-6) and one-level stripping gas endless tube (8-21), the big footpath section of the one-level cone bucket (8-6)
Big footpath section with one-level taper drainage cone (8-5) is relative, is opened in the one-level taper drainage cone 8-5 and one-level cone bucket (8-6)
Air-vent is provided with, the cone angle of one-level taper drainage cone (8-5) is 55~75 °, the cone angle of one-level cone bucket (8-6) is 125~105 °；
Two grades of stripper plants include two grades of taper drainages cone (8-22), the two grades of cone buckets (8-23) that are sequentially placed from top to bottom
And two grades of stripping gas endless tubes (8-24)；The big footpath section of two grades of cone buckets (8-23) is big with two grades of taper drainage tubes (8-22)
Footpath section is relative, and air-vent is offered on two grades of taper drainage tubes (8-22) and two grades of cone buckets (8-23), and two grades of tapers are drawn
The cone angle of flow tube (8-22) is 55~75 °, and two grades of cone angles of cone bucket (8-23) are 125~105 °；
The port of export of pyrolysis riser (8-9) is located in expansion chamber inner housing (8-14) through semicoke surge bunker (8-7)；Institute
Sedimentation passage in formed between expansion chamber inner housing (8-14) and pyrolysis riser (8-9) is stated, the pyrolysis fast (8-4) separately sets
The port of export in pyrolysis riser (8-9) is put, interior sedimentation passage is gathered in by the pyrolysis semicoke that (8-4) is separated fast separately
And moved down along expansion chamber inner housing (8-14), into the second straight line section of expansion chamber (8-13), by the fast (8- separately of pyrolysis
4) the gas for separating enters the entrance of pyrolysis cyclone unit；
Circumferential weld is provided between the expansion chamber inner housing (8-14) and the housing of expansion chamber (8-13).
3. solid thermal carriers activation coal gas flashing speed oven coal according to claim 1 produces coal tar, coal gas and semicoke
System, it is characterised in that：The housing of the expansion chamber (8-13) from the bottom up successively include first straight line section, the first flared section,
Second straight line section, the second flared section, the 3rd straightway and gas collecting segment, the collection chamber (8-1) are located at gas collecting segment；
The gas-solid separator include center cyclone separator (8-20), one-level stripper plant and two grades of stripper plants, it is described in
The solid outlet of heart cyclone separator (8-20) is located at the second flared section, the gas of the center cyclone separator (8-20)
Outlet is located at the 3rd straightway, and the one-level stripper plant is located in center cyclone separator (8-20), the one-level cone bucket
The big footpath section of (8-6) is relative with the big footpath section of one-level taper drainage cone (8-5), and (8-5) and one-level are bored in the one-level taper drainage
Air-vent is offered in cone bucket (8-6), the cone angle of one-level taper drainage cone (8-5) is 55~75 °, one-level cone bucket (8-6)
Cone angle is 125~105 °；
Two grades of stripper plants are located at the second straight line of expansion chamber (8-13) section；The one-level stripper plant include on to
Under one-level taper drainage cone (8-5), one-level cone bucket (8-6) and one-level stripping gas endless tube (8-21) that are sequentially placed,
Two grades of stripper plants include two grades of taper drainages cone (8-22), the two grades of cone buckets (8-23) that are sequentially placed from top to bottom
And two grades of stripping gas endless tubes (8-24)；The big footpath section of two grades of cone buckets (8-23) is big with two grades of taper drainage tubes (8-22)
Footpath section is relative, and air-vent is offered on two grades of taper drainage tubes (8-22) and two grades of cone buckets (8-23), and two grades of tapers are drawn
The cone angle of flow tube (8-22) is 55~75 °, and two grades of cone angles of cone bucket (8-23) are 125~105 °；
Pyrolysis riser (8-9) in expansion chamber (8-13) outward, outlet and the center cyclonic separation of pyrolysis riser (8-9)
Device (8-20) entrance is connected.
4. according to claim 1 or 2 or 3 solid thermal carriers activation coal gas flashing speed oven coal produce coal tar, coal gas and
The system of semicoke, it is characterised in that：The semicoke heated separator includes fluid bed combustion-supporting chamber (10-6), second-time burning air inlet pipe
(10-13), heater riser tube (10-5), high-temperature semi-coke expansion chamber (10-3) and high-temperature semi-coke sedimentation it is outdoor with flutter valve
Semicoke cyclone unit, is provided with circulation semicoke charging aperture (10-7), fluid bed on the fluid bed combustion-supporting chamber (10-6)
Air inlet (10-14) and secondary combustion air inlets (10-8), circulation semicoke discharge gate (8-16) and circulation semicoke charging
Mouth (10-7) connection；Second-time burning air inlet pipe (10-13) is provided with the fluid bed combustion-supporting chamber (10-6), the fluid bed is helped
The upper end for firing room (10-6) connects with one end of heater riser tube (10-5), is set on the other end of the heater riser tube (10-5)
It is equipped with high-temperature semi-coke fast separately (10-12), the high-temperature semi-coke expansion chamber (10-3) covers on the upper end of heater riser tube (10-5),
The lower end of the high-temperature semi-coke expansion chamber (10-3) is fixed on heater riser tube (10-5), the high-temperature semi-coke expansion chamber (10-
3) bottom is provided with high-temperature semi-coke outlet (10-4), high-temperature semi-coke outlet (10-4) and high-temperature semi-coke charging aperture (8-18)
Connection, the upper end of the high-temperature semi-coke expansion chamber (10-3) is provided with flue gas export mouth (10-11), the flue gas export mouth and half
The entrance connection of burnt cyclone unit, the outlet of the semicoke cyclone unit is connected with circulation recycling device.
5. solid thermal carriers activation coal gas flashing speed oven coal according to claim 4 produces coal tar, coal gas and semicoke
System, it is characterised in that：The circulation recycling device includes afterburning chamber (11), high-temperature gas heat exchanger (12) and desulphurization denitration
Reactor (13), the outlet of the semicoke cyclone unit is connected with the entrance of afterburning chamber (11), the afterburning chamber (11)
Outlet be connected with high-temperature gas heat exchanger (12), while be connected with high-temperature gas heat exchanger (12) also have flue gas recirculation blower fan
(1) outlet, the gas exit of coal tar generation device and air outlet slit after pressurization, flue gas recirculation blower fan (1) enters
Mouth connects another outlet of sack cleaner (2)；The outlet of the high-temperature gas heat exchanger (12) and desulfurization and denitrification reaction device
(13) entrance connection, while the outlet of high-temperature gas heat exchanger (12) also with coal gas of high temperature import (8-19), fluid bed air inlet
Mouth (10-14) and secondary combustion air inlets (10-8) connection, outlet and the Vertical Mill (14) of the desulfurization and denitrification reaction device (13)
Connection；
The Semi-coke cooling device includes high-temperature semi-coke cooler (7), and the entrance of the high-temperature semi-coke cooler is practiced midwifery product semicoke
Discharge gate (8-8), another entrance of high-temperature semi-coke cooler (7) connects desalted water, the one outlet of high-temperature semi-coke cooler (7)
Connect steam；
The coal tar recovering device includes quencher (9), filter collector (15), oil scrubber (16), bottom of towe oil circulating pump
(17), overhead reflux pump (18), horizontal water-tube cooler (19), electric coke booster oil device (20) and coal gas circulating fan (21)；The urgency
The entrance of cooler (9) is connected with coal gas export mouth (8-11), the outlet of the quencher (9) and the entrance of filter collector (15)
Connection, the outlet of the filter collector (15) is connected with oil scrubber (16) bottom, and oil scrubber (16) bottom is connected with tower
Base oil circulating pump (17), oil scrubber (16) top is connected with overhead reflux pump (18), and the bottom of towe oil circulating pump (17) is returned
Heavy coal tar is received, the overhead reflux pump (18) reclaims light tar；The top exit of oil scrubber (16) is cooled down with transverse tube
The entrance connection of device (19), the outlet electrical tar precipitator (20) of the horizontal water-tube cooler (19) is produced after electrical tar precipitator (20)
Soft coal gas, a portion coal gas discharge, another part coal gas enters high-temperature gas heat exchanger through coal gas circulating fan (21)
(12) gas entry.
6. solid thermal carriers activation coal gas flashing speed oven coal according to claim 5 produces coal tar, coal gas and semicoke
System, it is characterised in that：The pyrolysis cyclone unit includes 1-3 pyrolysis cyclone separator group, the pyrolysis whirlwind
Separator group includes multiple pyrolysis cyclone separators in parallel；
The semicoke cyclone unit includes the semicoke primary cyclone group (10- with flutter valve being sequentially connected
1), semicoke secondary cyclone group (10-2) and semicoke three-stage cyclone separator group (10-3).
7. solid thermal carriers activation coal gas flashing speed oven coal according to claim 2 produces coal tar, coal gas and semicoke
System, it is characterised in that：The parted hair (8-4) soon that is pyrolyzed is the fast parted hair of umbrella hat type or three leaf spiral-flow types (VQS) parted hair soon, described
The lower swing angle of three leaf vortex sepatation system heads is 20 °, and aperture area is 0.75-0.85 with pyrolysis riser area ratio.
8. the method for coal tar, coal gas and semicoke being produced based on the system described in claim 1, it is characterised in that including following step
Suddenly：
1) raw material preliminary working：
Raw coal is sent into Vertical Mill (14) grinding, is 300~350 DEG C of high temperature flue gas drying selection by winnowing through temperature, 85%-90% particle diameters reach
To below 0.1mm, moisture below 2%, after Vertical Mill flue gas pressures are tiny structure, by dried coal dust by drying whirlwind point
After device (3), dry pulverized coal surge bunker (4) and sack cleaner (2) are fed sequentially into, coal dust is stored in dry pulverized coal surge bunker (4)；
2) activation fast bed reaction：
2.1) temperature be 750~850 DEG C high-temperature semi-coke powder by high-temperature semi-coke charging aperture (8-18) enter pyrolytic reaction separate
The activation fast bed (8-17) of device (8)；The coal gas of high temperature that temperature is 550~650 DEG C, pressure is 0.01~2MPa passes through high-temperature coal
Gas import (8-19) enters activation fast bed (8-17)；The gas velocity of coal gas of high temperature is 0.5~3m/s, and high-temperature semi-coke powder is by high-temperature coal
Bottom activation of the gas in activation fast bed；
2.2) coal dust that temperature in dry pulverized coal surge bunker (4) is 80~120 DEG C will be stored in and is forced into 0.01 through dry coal conveying storehouse (6)
Activation fast bed top is entered by coal feed point after~2Mpa；The mixing quality ratio of high-temperature semi-coke powder and coal dust for (2.5~
5):1；
2.3) coal dust mixes with coal gas and high-temperature semi-coke powder after activation on activation fast bed top；
3) pyrolytic reaction：
Coal dust carries out pyrolytic reaction with pyrolysis riser (8-9) that enters of high-temperature semi-coke powder after mixing, in pyrolysis riser (8-9)
Pyrolysis temperature is 480~750 DEG C, and synthesis pressure is 0.01~2MPa, and gas velocity is 8-16m/s, is lifted through pyrolysis after pyrolytic reaction
The gas-solid separator of pipe (8-9) outlet is separated；
4) separate：
4.1) after being pyrolyzed 480~750 DEG C of a semi-coke powder in the presence of gravity and inertia force mass settlement in gas solid separation
Device is moved down, while strip coal gas being entered while stripping coal gas by stripping gas inlet (8- by stripping gas inlet (8-15)
15) gas-solid separator is entered by the residual oil gas stripping in a semi-coke powder, the temperature of stripping gas is identical with pyrolysis temperature, pressure
It is 0.01~2MPa, section gas velocity is not more than 0.1m/s；
4.2) raw coke oven gas of 480~750 DEG C after pyrolysis sequentially enters pyrolysis one-level and revolves by the gas vent of gas-solid separator
After wind separator group (8-3), pyrolysis secondary cyclone group (8-2), pyrolysis three-stage cyclone separator group (8-12) are separated,
Collection chamber (8-1) is used to prepare coal gas and coal tar after being derived through raw coke oven gas export mouth (8-11) after collecting；
Expansion chamber (8-13) is entered through being pyrolyzed the secondary semi-coke powder after cyclone unit is separated, with gas-solid separator one
Secondary semi-coke powder is moved downwardly together, into semicoke surge bunker (8-7), low temperature semicoke to be prepared；
5) high-temperature semi-coke reprocessing：
A part of 480~750 DEG C of semi-coke powders enter through circulating semicoke discharge gate (8-16) and circulation semicoke in semicoke surge bunker (8-7)
Material mouth (10-7) enters the fluid bed combustion-supporting chamber (10-6) of semicoke heated separator (10), and by fluidizer air inlet (10-
14) after entering 450~550 DEG C of Air Fluidizeds of temperature burning of fluidized bed combustion-supporting chamber, and with pass sequentially through secondary combustion air inlets
After the temperature of (10-8) and second-time burning air inlet pipe (10-13) is burnt again for 450~550 DEG C of high-temperature flue gas；The stream of fluid bed
Change gas velocity is 0.2~1m/s；
Heated riser (10-5) is lifted into high-temperature semi-coke expansion chamber (10-3), the semi-coke powder and high-temperature gas after burning
Temperature is 750~850 DEG C, and pressure is 0.01~2MPa, and the lifting gas velocity of heater riser tube (10-5) is 8~16m/s, semi-coke powder
High-temperature semi-coke fast (10-12) separately at the top of heated riser (10-8) is separated after settling；
High-temperature flue gas sequentially enter external semicoke primary cyclone through semicoke heated separator flue gas export mouth (10-11)
Group (10-2), semicoke secondary cyclone group (10-1), semicoke three-stage cyclone separator group (10-10) are separated, after separation
Semi-coke powder is discharged after entering high-temperature semi-coke expansion chamber (10-3) through the flutter valve of cyclone separator by high-temperature semi-coke outlet (10-4)
750~850 DEG C of high-temperature semi-coke powder is stand-by；750~850 DEG C of high-temperature flue gas are through semicoke three-stage cyclone separator group (10-3)
It is stand-by after outlet；
6) coal gas and coal tar are prepared：
Cooled down with 250~300 DEG C of Low Temperature Steam heat exchange in quencher (9) through raw coke oven gas derived from raw coke oven gas export mouth (8-11)
By being rapidly cooled between 360~400 DEG C for 480~750 DEG C of raw coke oven gas, subsequently into filter collector dust removal by filtration, dedusting
Raw coke oven gas afterwards enters oil scrubber (16) bottom and reclaims heavy coal tar by bottom of towe oil circulating pump (17) spray washing, is returned by tower top
Light tar is reclaimed in stream pump (18) cooling；
The tower overhead gas of oil scrubber (16) enters horizontal water-tube cooler (19) and cools down laggard electrical tar precipitator (20) recovery light oil and pyrolysis
Water, generates coal gas after electric fishing；A part of coal gas discharge, another part is recycled into high-temperature gas through coal gas circulating fan (21)
Heat exchanger (12) gas entry；
7) low temperature semicoke is prepared：
480~750 DEG C of semi-coke powders part in semicoke surge bunker (8-7) enters high temperature half through product semicoke discharge gate (8-8)
Burnt cooler (7), semi-coke powder is cooled to less than 80 DEG C storehouses by desalted water and steam heat-exchanging in high-temperature semi-coke cooler (7)
Storage；
Wherein step 5), 6), 7) while carrying out or being carried out according to timing requirements.
9. the method for producing coal tar, coal gas and semicoke according to claim 8, it is characterised in that：Also include reclaiming again
Using step, specially：
8.1) 750~850 DEG C of the temperature of semicoke heated separator discharge, the high-temperature flue gas that pressure is 0.01~2MPa enter afterburning
Room (11), obtains the high-temperature flue gas that temperature is raised to 850~950 DEG C after burning, afterwards into high-temperature gas heat exchanger (12)；
8.2) high-temperature gas heat exchanger (12) is received：It is later 80 from flue gas recirculation blower fan temperature through sack cleaner (2) dedusting
~120 DEG C, the circulating flue gas that pressure is 0.01~2Mpa；Exported through coal gas circulating fan (21) from electrical tar precipitator (20) discharge
Temperature be 25~50 DEG C, the circulating gas that pressure is 0.01~2Mpa；And temperature be 25 DEG C, pressure be 0.01~2Mpa's
Air；
850~950 DEG C of high-temperature flue gas obtain temperature 450~550 with after circulating flue gas, circulating gas and air heat-exchange respectively
DEG C, the circulating flue gas that pressure is 0.01~2Mpa；The circulating gas that temperature is 600~650 DEG C, pressure is 0.01~2Mpa；With
And the air that temperature is 450~550 DEG C, pressure is 0.01~2Mpa；
8.3) 300~350 DEG C of temperature, the flue gas that pressure is 0.01~2Mpa are sent to be depressurized after desulfurization and denitrification reaction device (13) and are
Normal pressure is dried selection by winnowing into Vertical Mill (14) to raw coal；
The circulating gas that temperature is 550~650 DEG C, pressure is 0.01~2Mpa are input into coal gas of high temperature import (8-19)；
The air that temperature is 450~550 DEG C, pressure is 0.01~2Mpa enters fluidized bed by fluidizer air inlet (10-14)
Combustion-supporting chamber (10-6)；
450~550 DEG C of temperature, the circulating flue gas that pressure is 0.01~2Mpa send into secondary combustion air inlets (10-8).
10. the method for producing coal tar, coal gas and semicoke according to claim 8 or claim 9, it is characterised in that：Step 4) tool
Body is：
4.1) after being pyrolyzed 480~750 DEG C of a semi-coke powder in the presence of gravity and inertia force mass settlement in expansion chamber
The second straight line section of housing (8-14) and expansion chamber is moved down, while strip coal gas enters one-level by stripping gas inlet (8-15)
Stripping endless tube and two grades of stripping endless tubes, by the residual oil gas stripping in a semi-coke powder, temperature and the pyrolysis temperature phase of stripping gas
Same, pressure is 0.01~2MPa, and section gas velocity is not more than 0.1m/s；
4.2) top exit that the raw coke oven gas of 480~750 DEG C after pyrolysis passes through expansion chamber inner housing (8-14), sequentially enters heat
Solution primary cyclone group (8-3), pyrolysis secondary cyclone group (8-2), pyrolysis three-stage cyclone separator group (8-12)
After separation, coal gas and coal tar are prepared after being derived through raw coke oven gas export mouth (8-11) after collection chamber (8-1) collects；
Expansion chamber (8-13) is entered through being pyrolyzed the secondary semi-coke powder after cyclone unit is separated, by expansion chamber inner housing
Circumferential weld on (8-14) is simultaneously moved downwardly together with a semi-coke powder in expansion chamber inner housing (8-14), into semicoke surge bunker
(8-7), low temperature semicoke to be prepared.
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| CN107557029A (en) * | 2017-09-15 | 2018-01-09 | 新疆广汇中化能源技术开发有限公司 | Semicoke cooling body and there is its cooling drying system |
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Effective date of registration: 20211101 Address after: 710061 room 20708, block B, Wangzuo Qujiang, No. 3269, Yanxiang Road, Qujiang New Area, Xi'an, Shaanxi Patentee after: Shaanxi kaideli Energy Technology Co.,Ltd. Address before: 719300 Shenmu Fuyou Energy Technology Co., Ltd., Jinjie Industrial Park, Shenmu county, Yulin City, Shaanxi Province Patentee before: Wang Shukuan |