CN104804478A - Method for preparing carbon black through coal tar chemical chain pyrolysis - Google Patents
Method for preparing carbon black through coal tar chemical chain pyrolysis Download PDFInfo
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- CN104804478A CN104804478A CN201510134022.1A CN201510134022A CN104804478A CN 104804478 A CN104804478 A CN 104804478A CN 201510134022 A CN201510134022 A CN 201510134022A CN 104804478 A CN104804478 A CN 104804478A
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Abstract
The invention belongs to the technical field of carbon black preparation and relates to a method for preparing carbon black through coal tar chemical chain pyrolysis. An original-state oxygen carrier has an oxidation reaction to produce an oxidation-state oxygen carrier which enters a single-stage cyclone separator for gas-solid separation, and separated oxygen-deficient air is sent to a double-jacket fluidized bed heat exchanger, a fuel reactor and a return valve to be used as fluidization gas after part of heat is recovered by a shell-and-tube waste heat boiler; the separated oxidation-state oxygen carrier enters the double-jacket fluidized bed heat exchanger to preheat coal tar and then is sent to the lower part of the fuel reactor to be mixed with the coal tar in a fluidization gas inlet pipe, and the fluidized oxidation-state oxygen carrier evenly disperses the coal tar, performs catalytic cracking on C-H bonds of the coal tar and releases lattice oxygen which reacts with H to produce carbon black. The process is simple, the principle is scientific, used devices are simple in structure, operation and usage are convenient, the maintenance cost is low, the service life is long, energy consumption is low, reasonable utilization of waste energy is realized, and pollution emission is effectively reduced.
Description
Technical field:
The invention belongs to carbon black preparing technical field, relate to the method that carbon black is prepared in the pyrolysis of a kind of coal-tar chemistry chain, particularly a kind of is raw material with tar, is prepared the technique of carbon black by chemical chain technology.
Background technology:
Along with the quickening of China's modernization, with automobile industry be representative rubber rely on industry develop rapidly, and carbon black is as the important strengthening agent of one of rubber, demand also grows with each passing day, become the second largest elastomeric material being only second to rubber, the consumption in rubber industry accounts for 89.5% of its ultimate production; Research shows, adds appropriate carbon black in rubber, can the physical and mechanical properties (tensile strength, tear strength, wear resistance etc.) of effective strongthener, makes rubber product more reliable, durable; In addition, carbon black, as staining agent, conductive agent and ultraviolet screening agent etc., is widely used in the fields such as coating, drying battery and plastics-production equally.
Up to now, conventional method of producing black pigment mainly comprises contact process, pyrolysis method and oven process, and wherein contact process open type is produced, and technique falls behind, and now except specific function carbon black adopts contact process, contact process is less use, pyrolysis method is due to raw natural gas price increase, factors such as carbon black products poor-performing and develop limited, and be that the furnace treated black technology of representative obtains broad development with Audit For Process, the carbon black produced by Audit For Process accounts for more than 95% of production of carbon black total amount, become the main method of current production of carbon black, its ultimate principle is: preheated air carry oil fuel enter combustion reactions room burning produce high-temperature flue gas (temperature of combustion 1700-1800 DEG C) enter pyrolytic reaction room, stock oil after filtration, being atomized by pressurized air after preheating sprays into wherein, at high temperature gasify rapidly and cracking generation carbon black, at reaction chamber rear portion, cold water is directly sprayed in flue gas and stop carbon black reaction to reduce cigarette temperature, final cooled flue gas collects carbon black through main bag filter.As can be seen from above-mentioned principle, Audit For Process principal feature comprises: high temperature must be kept in stove to improve speed of reaction; Stock oil atomization quality is very crucial, and air stoichiometry controls strict; Temperature of combustion is up to 1800 DEG C, and refractory materials is easily burnt, and cost increases; Adopt combustion air, the wherein nitrogen of 79%, under high temperature, easily generate a large amount of thermal NO
x, and the amount of heat of part coal tar burning generation can be carried, cause power loss; Spray into cold water cooling high temperature flue gas, both caused exhaust gas volumn increase and more sensible heats are pulled away, made again tail gas water capacity increase, reduce tail gas calorific value.Therefore, under the overall background nowadays advocating environmental protection and energy saving, consumption reduction, pollution emission reduction be current production of carbon black institute necessary faced by great difficult problem.
Summary of the invention:
The object of the invention is to the shortcoming overcoming prior art existence, seek to design the method providing the pyrolysis of a kind of coal-tar chemistry chain method to prepare carbon black, reduce production of carbon black energy consumption, decreasing pollution discharges.
To achieve these goals, the present invention prepares in the device of carbon black in the pyrolysis of coal-tar chemistry chain and adopts coal tar raw material to prepare carbon black, and its concrete preparation process is:
(1), on fuel reactor air distribution plate, fill out the paving oxygen carrier granule formation oxygen carrier granule bed of material, the thickness of the oxygen carrier granule bed of material is not less than 150mm;
(2) the revert pipe valve, between closedown fuel reactor and air reactor, blocks oxygen carrier granule circulation between two reactors;
(3), 1000 DEG C of flue gases that in external hotblast stove, combustion gas and air combustion produce are utilized to carry out preheating, flue gas is introduced into fuel reactor and carries out baker, flue gas sprays into from fuel reactor air distribution plate, the oxygen carrier granule bed of material in heating fuel reactor and refractory materials, the oxygen carrier granule bed of material loosens and expands and bubbling fluidization, flue gas is up through cooling water coil, in cooling water coil, low power rate of flow of water is run, flue gas is introduced into the air intlet bottom air reactor after leaving the offgas outlet of fuel reactor, enter air reactor by air reactor air distribution plate and carry out preheating, when in fuel reactor, main body furnace temperature reaches 800 ~ 900 DEG C, in pipeline and air reactor, temperature reaches 700 DEG C, the waste heat flue gas of discharging from air reactor introduces shell-and-tube exhaust-heat boiler from the oxygen-denuded air outlet at single stage cyclone top, thus carries out preheating to shell-and-tube exhaust-heat boiler, then progressively reduce intensity of combustion in hotblast stove, start in fuel reactor, send into coal tar and react, oxygen carrier granule enters air reactor exothermic heat of reaction, and takes heat to fuel reactor by oxygen carrier circulation gradually, in fuel reactor after temperature-stable, stop the operation of hotblast stove,
(4), open the revert pipe valve between air reactor and fuel reactor, open coal tar pan feeding valve simultaneously, coal tar is made to enter fuel reactor by coal tar import, the pan feeding speed of coal tar is increased gradually by 0 flow, until rated flow, what keep 1000 DEG C of flue gases sprays into fluidisation, the fluidisation of oxygen carrier granule carries out fragmentation and heating to the coal tar entering fuel reactor, carbon black reaction starts to carry out, the reduction-state oxygen carrier granule generated enters air reactor with the unreacted oxygen carrier granule of small part, open oxygen carrier material inlet valve supplemental state oxygen carrier simultaneously and enter fuel reactor,
(5) fluidized air blower of air reactor, is started, reduction-state oxygen carrier and oxygen carry out oxidizing reaction and generate oxidation state oxygen carrier in air reactor, in air reactor, temperature raises gradually, along with the flow rate of oxygen carrier granule increases, the air capacity sent into from air intlet coupling increases, fast bed state (vigorous fluidisation is presented in air reactor, major part particle is carried up by gas, leave air reactor enter separator and material returning valve and send into pyrolysis reactor) time, stablize each pipe valve aperture;
(6), oxidation state oxygen carrier sends heat and lattice oxygen back to fuel reactor, wherein oxidation state oxygen carrier is introduced into single stage cyclone and carries out gas solid separation, the oxidation state oxygen carrier separated enters double jacket fluid-bed heat exchanger by single stage cyclone dipleg, under fluidizing agent loosens, the oxidation state oxygen carrier in double jacket fluid-bed heat exchanger is sent into feed-pipe, and to the coal tar heating in double jacket fluid-bed heat exchanger chuck, coal tar after preheating together enters the bottom of fuel reactor after being mixed with the fluidizing agent in fluidisation air intake branch by transition pipeline, oxidation state oxygen carrier enters fuel reactor by feed-pipe, fluidizing agent is passed into by the bottom of fuel reactor, under rheomorphism, coal tar is uniformly dispersed by oxygen carrier, and the c h bond of catalytic pyrolysis coal tar, the lattice oxygen of accelerating oxidation state oxygen carrier and H react and generate carbon black, carry the cooling water coil of flue gas successively by being interconnected of carbon black and a small amount of reduction-state oxygen carrier, the outer jacket for heat exchange cooling of water jacket interchanger and double jacket fluid-bed heat exchanger obtains cooled flue gas, cooled flue gas enters two-stage series connection cyclonic separator, reduction-state oxygen carrier is separated in primary cyclone, revert pipe is entered and after mixing with the reduction-state oxygen carrier entering revert pipe from fuel reactor bottom by primary cyclone dipleg, together return air reactor and complete Matter Transfer, and flue gas continues to enter secondary cyclone, part carbon black is separated to be got off to enter storage tank, residue carbon black carries collection device separated and collected after filtration by flue gas, tail gas is sent to waste heat boiler burning through offgas outlet, realize the preparation of carbon black.
Coal-tar chemistry chain of the present invention transforms the main body preparing the device of carbon black and comprises air reactor, single stage cyclone, double jacket fluid-bed heat exchanger, fuel reactor, water jacket interchanger, two-stage series connection cyclonic separator, device for filtering and collecting, air reactor vapor pipe, single stage cyclone dipleg, feed-pipe, transition pipeline, shell-and-tube exhaust-heat boiler, induced draft fan, fluidisation air intake branch, cooling water coil, primary cyclone dipleg, revert pipe, storage tank, oxidation state oxygen carrier, reduction-state oxygen carrier, fluidisation air inlet is responsible for, fuel reactor air distribution plate, revert pipe valve, air reactor air distribution plate, coal tar pan feeding valve, oxygen carrier material inlet valve, returning charge valve, air intlet, oxygen-denuded air exports, the main import of fluidizing agent, entrance of cooling water, high-temperature water exports, coal tar import, fluidizing agent divides import and offgas outlet, air reactor is communicated with single stage cyclone by the air reactor vapor pipe at top, and the bottom of air reactor is provided with air intlet, and the bottom of air reactor is provided with air reactor air distribution plate, air reactor and air reactor exhaust Bottomhole pressure have oxidation state oxygen carrier, and oxidation state oxygen carrier is generated by the oxygen reaction in reduction-state oxygen carrier and air, the bottom of single stage cyclone is communicated with double jacket fluid-bed heat exchanger by single stage cyclone dipleg, and the top of single stage cyclone is provided with oxygen-denuded air outlet, and N is discharged in oxygen-denuded air outlet
2with a small amount of unreacted O
2, double jacket fluid-bed heat exchanger is communicated with the middle part of fuel reactor by feed-pipe, fuel reactor lower end is provided with fuel reactor air distribution plate, the bottom of fuel reactor air distribution plate is be responsible for fluidisation air inlet the air compartment be communicated with, fluidisation air inlet supervisor and the main inlet communication of fluidizing agent, fuel reactor is connected with the bottom of air reactor with revert pipe by returning charge valve, revert pipe between fuel reactor and returning charge valve is provided with revert pipe valve, returning charge Bottomhole pressure has reduction-state oxygen carrier, the top of fuel reactor is provided with cooling water coil, the top of cooling water coil is entrance of cooling water, cooling water coil is connected with water jacket interchanger, the top of fuel reactor is by the pipeline of water jacket heat exchanger cavity and the inlet communication of two-stage series connection cyclonic separator, two-stage series connection cyclonic separator is composed in series by the venting port of primary cyclone and the inlet mouth of secondary cyclone, primary cyclone dipleg is communicated with revert pipe, and the bottom of secondary cyclone is connected with storage tank, device for filtering and collecting is connected with the venting port of secondary cyclone, and the rear portion of device for filtering and collecting is provided with offgas outlet, the top right side of shell-and-tube exhaust-heat boiler is provided with high-temperature water outlet, the top of shell-and-tube exhaust-heat boiler exports with oxygen-denuded air and communicates, the outer chuck of double jacket fluid-bed heat exchanger is communicated with the bottom of shell-and-tube exhaust-heat boiler respectively with water jacket interchanger, bottom the internal layer chuck of double jacket fluid-bed heat exchanger, right side is connected with transition pipeline, the left side of the internal layer chuck of double jacket fluid-bed heat exchanger is provided with coal tar import, be provided with coal tar pan feeding valve with the pipeline of coal tar inlet communication, the fluidized-bed bottom of double jacket fluid-bed heat exchanger is provided with fluidizing agent and divides import, the bottom of transition pipeline is connected with fluidisation air intake branch, and vertical being connected is responsible for fluidisation air inlet in the one end bottom fluidisation air intake branch, and the other end bottom fluidisation air intake branch is provided with the tipping tube of 30 °, and tipping tube is connected with bottom fuel reactor, the pipeline of fluidisation air intake branch upper end is provided with oxygen carrier material inlet valve, and the import of induced draft fan is connected with the bottom of waste heat boiler, and the outlet of induced draft fan respectively import main with fluidizing agent divides import to be connected with fluidizing agent.
Air reactor of the present invention is circulating fluidized bed, and fuel reactor is bubbling fluidized bed; The internal layer chuck of double jacket fluid-bed heat exchanger is coal tar chuck, and outer chuck is cooling water jecket, the top of the coated fluidized-bed of double jacket and surrounding; Device for filtering and collecting adopts filter cloth bag and exhaust gases passes composition.
The present invention adopts the pyrolysis of coal-tar chemistry chain to prepare carbon black, when chemical chain pyrolytic reaction starts, reduction-state oxygen carrier in air reactor and air carry out oxidizing reaction and generate oxidation state oxygen carrier, oxidation state oxygen carrier is carried by air-flow and enters single stage cyclone and carry out gas solid separation, the oxygen-denuded air separated, through shell-and-tube exhaust-heat boiler recovery part heat, is then sent to double jacket fluid-bed heat exchanger, fuel reactor and returning charge valve as fluidizing agent through induced draft fan, the oxidation state oxygen carrier separated enters double jacket fluid-bed heat exchanger by single stage cyclone dipleg, lower oxidation state oxygen carrier is blown by the coal tar preheating in double jacket fluid-bed heat exchanger internal layer chuck at fluidizing agent, coal tar after preheating is fallen by transition pipeline and is sent in fluidisation air intake branch, fluidizing agent from fluidizing agent supervisor carries the bottom that the oxidation state oxygen carrier fallen by oxygen carrier material inlet valve is together sent to fuel reactor, and mix with coal tar in fluidisation air intake branch, fluidizing agent in fluidizing agent supervisor is passed into by the bottom plenum of fuel reactor, coal tar is uniformly dispersed by the oxidation state oxygen carrier of fluidisation, and the c h bond of catalytic pyrolysis coal tar, oxidation state oxygen carrier release lattice oxygen and H react, then carbon is separated out and is generated carbon black rapidly, oxidation state oxygen carrier generates reduction-state oxygen carrier, macrobead reduction-state oxygen carrier enters revert pipe in fluidisation, air reactor is sent back to through returning charge valve, the water coil of flue gas successively by being interconnected of carbon black and a small amount of reduction-state oxygen carrier is carried in fuel reactor, water jacket interchanger enters two-stage separator and filtration unit, two-stage series connection cyclonic separator, reduction-state oxygen carrier is separated in primary cyclone, revert pipe is entered and after mixing with the reduction-state oxygen carrier entering returning charge valve and revert pipe from fuel reactor bottom by primary cyclone dipleg, together return air reactor and complete Matter Transfer, and flue gas continues to enter secondary cyclone, part carbon black is separated to be got off to enter storage tank, residue carbon black carries collection device separated and collected after filtration by flue gas, tail gas is sent to waste heat boiler afterburning through offgas outlet.
The present invention is in the black process of charcoal processing, and the temperature in air reactor is 1000-1100 DEG C, and the temperature of fuel reactor is 850-950 DEG C; Water coolant after water jacket interchanger first passes into outer chuck in double jacket fluid-bed heat exchanger to regulate oil temperature, pass into shell-and-tube exhaust-heat boiler tube side again, and export with utilizing induced draft fan the oxygen-denuded air heat exchange guiding to shell-and-tube exhaust-heat boiler shell side from oxygen-denuded air, cooled oxygen-denuded air goes to the main import of fluidizing agent respectively and fluidizing agent divides import to do fluidisation air inlet, and the water after heating is exported towards external heat user by high-temperature water.
The present invention compared with prior art, prepare in carbon black process, coal tar does not directly contact with air, but the preparation process of carbon black is realized by the alternating oxidation-reduction reaction of oxygen carrier between air reactor and fuel reactor, have the following advantages, one is oxygen carrier under fluidized state and the even blending of oil plant, plays good fragmentation atomization oil plant and the effect of strengthening transmission of heat by contact, saves the energy needed for mechanical atomizing pressurized air in Audit For Process; Two is adopt the lattice oxygen of oxygen carrier to substitute molecular oxygen in ingress of air, simplifies air stoichiometry and controls, avoid the excess enthalpy of oxygen and the loss of carbon, ensure carbon black productivity; Three be air reactor and fuel reaction actuator temperature all lower than equaling 1100 DEG C, temperature of reaction is low, improves the resistance to material life-span, save running cost, and owing to adopting oxygen carrier catalytic pyrolysis oil plant c h bond, promote the reaction of lattice oxygen and H, carbon black speed of reaction does not reduce; Four is because in fuel reactor, temperature is lower, and oil plant not with O in air
2contact, effectively reduces thermal NO
xwith fuel type NO
xproduce; Five is that fuel reactor top is provided with water coil and water jacket interchanger, cigarette temperature is regulated by water coolant and flue gas wall-type heat exchange, co-controlling/termination carbon black reaction, and the water after heating is sent to waste heat boiler utilization, compare the way causing a large amount of thermosteresis to high-temperature flue gas spray cooling, there is huge power savings advantages, and tail gas water capacity is little, is also sent to waste heat boiler afterburning and utilizes; Six is oil plant preheatings in double jacket interchanger when oxygen carrier refluxes, and mobility increases, and is beneficial to and sends into fuel reactor and oxygen carrier blending, save special oil plant warm, have characteristics of energy saving; Seven is that air reactor exhaust leads back waste heat boiler by induced draft fan, the water heat exchange after oil temperature is regulated with through cooling water jecket, cooling final vacuum is namely as the fluidisation air inlet of fuel reactor etc., and high-temperature water is finally sent to heat user, also has the feature that waste heat residual air energy is recovered utilization; Its simple process, scientific in principle, the apparatus structure of use is simple, and easy for operation, maintenance cost is low, long service life, less energy consumption, realizes the Appropriate application of complementary energy, and effective decreasing pollution discharge, has extensively far-reaching social benefit and industrial application potential value.
Accompanying drawing illustrates:
Fig. 1 is that the coal-tar chemistry chain that the present invention relates to transforms the agent structure principle schematic preparing the device of carbon black, comprising air reactor 1, single stage cyclone 2, double jacket fluid-bed heat exchanger 3, fuel reactor 4, water jacket interchanger 5, two-stage series connection cyclonic separator 6, device for filtering and collecting 7, air reactor vapor pipe 8, single stage cyclone dipleg 9, feed-pipe 10, transition pipeline 11, shell-and-tube exhaust-heat boiler 12, induced draft fan 13, fluidisation air intake branch 14, cooling water coil 15, primary cyclone dipleg 16, revert pipe 17, storage tank 18, oxidation state oxygen carrier 19, reduction-state oxygen carrier 20, fluidisation air inlet supervisor 21, fuel reactor air distribution plate 22, revert pipe valve 23, air reactor air distribution plate 24, coal tar pan feeding valve 25, oxygen carrier material inlet valve 26, air intlet A, oxygen-denuded air outlet B, the main import C of fluidizing agent, entrance of cooling water D, high-temperature water outlet E, coal tar import F, fluidizing agent divides import G and offgas outlet H.
Embodiment
Also by reference to the accompanying drawings the present invention is described further below by specific embodiment.
Embodiment:
The present embodiment is prepared in the device of carbon black in the pyrolysis of coal-tar chemistry chain and is adopted coal tar raw material to prepare carbon black, and its concrete preparation process is:
(1), on fuel reactor air distribution plate 22, fill out the paving oxygen carrier granule formation oxygen carrier granule bed of material, the thickness of the oxygen carrier granule bed of material is not less than 150mm;
(2) the revert pipe valve 23, between closedown fuel reactor 4 and air reactor 1, blocks oxygen carrier granule circulation between two reactors;
(3), 1000 DEG C of flue gases that in external hotblast stove, combustion gas and air combustion produce are utilized to carry out preheating, flue gas is introduced into fuel reactor 4 and carries out baker, flue gas sprays into from fuel reactor air distribution plate 22, the oxygen carrier granule bed of material in heating fuel reactor 4 and refractory materials, the oxygen carrier granule bed of material loosens and expands and bubbling fluidization, flue gas is up through cooling water coil 15, in cooling water coil 15, low power rate of flow of water is run, flue gas is introduced into the air intlet A bottom air reactor 1 after leaving the offgas outlet H of fuel reactor 4, enter air reactor 1 by air reactor air distribution plate 24 and carry out preheating, when in fuel reactor 4, main body furnace temperature reaches 800 ~ 900 DEG C, in pipeline and air reactor 1, temperature reaches 700 DEG C, the waste heat flue gas of discharging from air reactor 1 introduces shell-and-tube exhaust-heat boiler 12 from the oxygen-denuded air outlet B at single stage cyclone 2 top, thus carries out preheating to shell-and-tube exhaust-heat boiler 12, then progressively reduce intensity of combustion in hotblast stove, start to send into coal tar in fuel reactor 4 and react, oxygen carrier granule enters air reactor 1 exothermic heat of reaction, and takes heat to fuel reactor 4 by oxygen carrier circulation gradually, in fuel reactor 4 after temperature-stable, stop the operation of hotblast stove,
(4), open the revert pipe valve 23 between air reactor 1 and fuel reactor 4 on pipeline, open coal tar pan feeding valve 25 simultaneously, coal tar is made to enter fuel reactor 4 by coal tar import F, the pan feeding speed of coal tar is increased gradually by 0 flow, until rated flow, what keep 1000 DEG C of flue gases sprays into fluidisation, the fluidisation of oxygen carrier granule carries out fragmentation and heating to the coal tar entering fuel reactor 4, carbon black reaction starts to carry out, the reduction-state oxygen carrier granule 20 generated enters air reactor 1 with the unreacted oxygen carrier granule of small part, open oxygen carrier material inlet valve 26 supplemental state oxygen carrier granule 20 simultaneously and enter fuel reactor 4,
(5) fluidized air blower of air reactor 1, is started, reduction-state oxygen carrier 19 and oxygen carry out oxidizing reaction and generate oxidation state oxygen carrier 19 in air reactor 1, in air reactor 1, temperature raises gradually, along with the flow rate of oxygen carrier granule increases, mate from air intlet A the air capacity sent into increase, fast bed state (vigorous fluidisation is presented in air reactor 1, major part particle is carried up by gas, leave air reactor enter separator and material returning valve and send into pyrolysis reactor) time, stablize each pipe valve aperture;
(6), oxidation state oxygen carrier 19 sends heat and lattice oxygen back to fuel reactor 4, wherein oxidation state oxygen carrier 19 is introduced into single stage cyclone 2 and carries out gas solid separation, the oxidation state oxygen carrier 19 separated enters double jacket fluid-bed heat exchanger 3 by single stage cyclone dipleg 9, under fluidizing agent loosens, the oxidation state oxygen carrier 19 in double jacket fluid-bed heat exchanger 3 is sent into feed-pipe 10, and to the coal tar heating in double jacket fluid-bed heat exchanger 3 chuck, coal tar after preheating together enters the bottom of fuel reactor 4 after being mixed by the fluidizing agent of transition pipeline 11 and fluidisation air intake branch 14 li, oxidation state oxygen carrier 19 enters fuel reactor 4 by feed-pipe 10, fluidizing agent is passed into by the bottom of fuel reactor 4, under rheomorphism, coal tar is uniformly dispersed by oxygen carrier 19, and the c h bond of catalytic pyrolysis coal tar, the lattice oxygen of accelerating oxidation state oxygen carrier 19 and H react and generate carbon black, carry the cooling water coil 15 of flue gas successively by being interconnected of carbon black and a small amount of reduction-state oxygen carrier 20, the outer jacket for heat exchange cooling of water jacket interchanger 5 and double jacket fluid-bed heat exchanger 3 obtains cooled flue gas, cooled flue gas enters two-stage series connection cyclonic separator 6, reduction-state oxygen carrier 20 is separated in primary cyclone a, revert pipe 17 is entered and after mixing with the reduction-state oxygen carrier 20 entering revert pipe 17 from fuel reactor 4 bottom by primary cyclone dipleg 16, together return air reactor 1 and complete Matter Transfer, and flue gas continues to enter secondary cyclone b, part carbon black is separated gets off to enter storage tank 18, residue carbon black carries collection device 7 separated and collected after filtration by flue gas, tail gas is sent to waste heat boiler burning through offgas outlet H, realize the preparation of carbon black.
Coal-tar chemistry chain described in the present embodiment transforms the main body preparing the device of carbon black and comprises air reactor 1, single stage cyclone 2, double jacket fluid-bed heat exchanger 3, fuel reactor 4, water jacket interchanger 5, two-stage series connection cyclonic separator 6, device for filtering and collecting 7, air reactor vapor pipe 8, single stage cyclone dipleg 9, feed-pipe 10, transition pipeline 11, shell-and-tube exhaust-heat boiler 12, induced draft fan 13, fluidisation air intake branch 14, cooling water coil 15, primary cyclone dipleg 16, revert pipe 17, storage tank 18, oxidation state oxygen carrier 19, reduction-state oxygen carrier 20, fluidisation air inlet supervisor 21, fuel reactor air distribution plate 22, revert pipe valve 23, air reactor air distribution plate 24, coal tar pan feeding valve 25, oxygen carrier material inlet valve 26, returning charge valve 27, air intlet A, oxygen-denuded air outlet B, the main import C of fluidizing agent, entrance of cooling water D, high-temperature water outlet E, coal tar import F, fluidizing agent divides import G and offgas outlet H, air reactor 1 is communicated with single stage cyclone 2 by the air reactor vapor pipe 8 at top, and the bottom of air reactor 1 is provided with air intlet A, and the bottom of air reactor 1 is provided with air reactor air distribution plate 24, air reactor 1 and the interior flowing of air reactor vapor pipe 8 have oxidation state oxygen carrier 19, and oxidation state oxygen carrier 19 is generated by the oxygen reaction in reduction-state oxygen carrier 20 and air, the bottom of single stage cyclone 2 is communicated with double jacket fluid-bed heat exchanger 3 by single stage cyclone dipleg 9, and the top of single stage cyclone 2 is provided with oxygen-denuded air outlet B, and oxygen-denuded air outlet B discharges N
2unreacted O less
2, double jacket fluid-bed heat exchanger 3 is communicated with the middle part of fuel reactor 4 by feed-pipe 10, fuel reactor 4 lower end is provided with fuel reactor air distribution plate 22, the bottom of fuel reactor air distribution plate 22 is be responsible for 21 air compartments be communicated with fluidisation air inlet, fluidisation air inlet supervisor 21 is communicated with the main import C of fluidizing agent, fuel reactor 4 is connected with the bottom of revert pipe 17 with air reactor 1 by returning charge valve 27, revert pipe 17 between fuel reactor 4 and returning charge valve 27 is provided with revert pipe valve 23, and in revert pipe 17, flowing has reduction-state oxygen carrier 20, the top of fuel reactor 4 is provided with cooling water coil 15, the top of cooling water coil 15 is entrance of cooling water D, cooling water coil 15 is connected with water jacket interchanger 5, the top of fuel reactor 4 is by the pipeline of water jacket interchanger 5 inner chamber and the inlet communication of two-stage series connection cyclonic separator 6, two-stage series connection cyclonic separator 6 is composed in series by the venting port of primary cyclone a and the inlet mouth of secondary cyclone b, primary cyclone dipleg 16 is communicated with revert pipe 17, and the bottom of secondary cyclone b is connected with storage tank 18, device for filtering and collecting 7 is connected with the venting port of secondary cyclone b, and the rear portion of device for filtering and collecting 7 is provided with offgas outlet H, the top right side of shell-and-tube exhaust-heat boiler 12 is provided with high-temperature water outlet E, top and the oxygen-denuded air of shell-and-tube exhaust-heat boiler 12 export B and communicate, the outer chuck of double jacket fluid-bed heat exchanger 3 is communicated with the bottom of shell-and-tube exhaust-heat boiler 12 respectively with water jacket interchanger 5, bottom the internal layer chuck of double jacket fluid-bed heat exchanger 3, right side is connected with transition pipeline 11, the left side of the internal layer chuck of double jacket fluid-bed heat exchanger 3 is provided with coal tar import F, the pipeline be communicated with coal tar import F is provided with coal tar pan feeding valve 25, and the fluidized-bed bottom of double jacket fluid-bed heat exchanger 3 is provided with fluidizing agent and divides import G, the bottom of transition pipeline 11 is connected with fluidisation air intake branch 14, and the one end bottom fluidisation air intake branch 14 and fluidisation air inlet are responsible for 21 and are vertically connected, and the other end bottom fluidisation air intake branch 14 is provided with the tipping tube of 30 °, and tipping tube is connected with bottom fuel reactor 4, the pipeline of fluidisation air intake branch 14 upper end is provided with oxygen carrier material inlet valve 26, and the import of induced draft fan 13 is connected with the bottom of waste heat boiler 12, and import C main with fluidizing agent and fluidizing agent divide import G to be connected respectively in the outlet of induced draft fan 13.
Described in the present embodiment, air reactor 1 is circulating fluidized bed, and fuel reactor 4 is bubbling fluidized bed; The internal layer chuck of double jacket fluid-bed heat exchanger 3 is coal tar chuck, and outer chuck is cooling water jecket, the top of the coated fluidized-bed of double jacket and surrounding; Device for filtering and collecting 7 adopts filter cloth bag and exhaust gases passes composition.
The present embodiment adopts the pyrolysis of coal-tar chemistry chain to prepare carbon black, when chemical chain pyrolytic reaction starts, reduction-state oxygen carrier 20 in air reactor 1 carries out oxidizing reaction with air and generates oxidation state oxygen carrier 19, oxidation state oxygen carrier 19 is carried by air-flow and enters single stage cyclone 2 and carry out gas solid separation, the oxygen-denuded air separated, through shell-and-tube exhaust-heat boiler 12 recovery part heat, is then sent to double jacket fluid-bed heat exchanger 3, fuel reactor 4 and returning charge valve 27 as fluidizing agent through induced draft fan 13, the oxidation state oxygen carrier 19 separated enters double jacket fluid-bed heat exchanger 3 by single stage cyclone dipleg 9, lower oxidation state oxygen carrier 19 is blown by the coal tar preheating in double jacket fluid-bed heat exchanger 3 internal layer chuck at fluidizing agent, coal tar after preheating is fallen by transition pipeline and is sent to fluidisation air intake branch 14 li, fluidizing agent from fluidizing agent supervisor 21 carries the bottom that the oxidation state oxygen carrier fallen by oxygen carrier material inlet valve 26 is together sent to fuel reactor 4, and mix with coal tar in fluidisation air intake branch 14, fluidizing agent in fluidizing agent supervisor 21 is passed into by the bottom plenum of fuel reactor 4, coal tar is uniformly dispersed by the oxidation state oxygen carrier of fluidisation, and the c h bond of catalytic pyrolysis coal tar, oxidation state oxygen carrier 19 discharges lattice oxygen and H reacts, then carbon is separated out and is generated carbon black rapidly, oxidation state oxygen carrier generates reduction-state oxygen carrier, macrobead reduction-state oxygen carrier enters revert pipe 17 in fluidisation, air reactor 1 is sent back to through returning charge valve 26, the water coil 15 of flue gas successively by being interconnected of carbon black and a small amount of reduction-state oxygen carrier 20 is carried in fuel reactor 4, water jacket interchanger 5 enters two-stage separator and filtration unit, two-stage series connection cyclonic separator 6, reduction-state oxygen carrier 20 is separated in primary cyclone a, revert pipe 17 is entered and after mixing with the reduction-state oxygen carrier 20 entering returning charge valve 27 and revert pipe 17 from fuel reactor 4 bottom by primary cyclone dipleg 16, together return air reactor 1 and complete Matter Transfer, and flue gas continues to enter secondary cyclone b, part carbon black is separated gets off to enter storage tank 18, residue carbon black carries collection device 7 separated and collected after filtration by flue gas, tail gas is sent to waste heat boiler afterburning through offgas outlet H.
The present embodiment is in the black process of charcoal processing, and the temperature in air reactor 1 is 1000-1100 DEG C, and the temperature of fuel reactor 4 is 850-950 DEG C; Water coolant after water jacket interchanger 5 first passes into outer chuck in double jacket fluid-bed heat exchanger 3 to regulate oil temperature, pass into shell-and-tube exhaust-heat boiler 12 tube side again, and export from oxygen-denuded air the oxygen-denuded air heat exchange that B guides to shell-and-tube exhaust-heat boiler 12 shell side with utilizing induced draft fan 13, cooled oxygen-denuded air goes to the main import C of fluidizing agent respectively and fluidizing agent divides import G to do fluidisation air inlet, and the water after heating exports E towards external heat user by high-temperature water.
Claims (3)
1. a method for carbon black is prepared in the pyrolysis of coal-tar chemistry chain, it is characterized in that preparing in the device of carbon black in the pyrolysis of coal-tar chemistry chain adopting coal tar raw material to prepare carbon black, and its concrete preparation process is:
(1), on fuel reactor air distribution plate, fill out the paving oxygen carrier granule formation oxygen carrier granule bed of material, the thickness of the oxygen carrier granule bed of material is not less than 150mm;
(2) the revert pipe valve, between closedown fuel reactor and air reactor, blocks oxygen carrier granule circulation between two reactors;
(3), 1000 DEG C of flue gases that in external hotblast stove, combustion gas and air combustion produce are utilized to carry out preheating, flue gas is introduced into fuel reactor and carries out baker, flue gas sprays into from fuel reactor air distribution plate, the oxygen carrier granule bed of material in heating fuel reactor and refractory materials, the oxygen carrier granule bed of material loosens and expands and bubbling fluidization, flue gas is up through cooling water coil, in cooling water coil, low power rate of flow of water is run, flue gas is introduced into the air intlet bottom air reactor after leaving the offgas outlet of fuel reactor, enter air reactor by air reactor air distribution plate and carry out preheating, when in fuel reactor, main body furnace temperature reaches 800 ~ 900 DEG C, in pipeline and air reactor, temperature reaches 700 DEG C, the waste heat flue gas of discharging from air reactor introduces shell-and-tube exhaust-heat boiler from the oxygen-denuded air outlet at single stage cyclone top, thus carries out preheating to shell-and-tube exhaust-heat boiler, then progressively reduce intensity of combustion in hotblast stove, start in fuel reactor, send into coal tar and react, oxygen carrier granule enters air reactor exothermic heat of reaction, and takes heat to fuel reactor by oxygen carrier circulation gradually, in fuel reactor after temperature-stable, stop the operation of hotblast stove,
(4), open the revert pipe valve between air reactor and fuel reactor, open coal tar pan feeding valve simultaneously, coal tar is made to enter fuel reactor by coal tar import, the pan feeding speed of coal tar is increased gradually by 0 flow, until rated flow, what keep 1000 DEG C of flue gases sprays into fluidisation, the fluidisation of oxygen carrier granule carries out fragmentation and heating to the coal tar entering fuel reactor, carbon black reaction starts to carry out, the reduction-state oxygen carrier granule generated enters air reactor with the unreacted oxygen carrier granule of small part, open oxygen carrier material inlet valve supplemental state oxygen carrier simultaneously and enter fuel reactor,
(5) fluidized air blower of air reactor, is started, reduction-state oxygen carrier and oxygen carry out oxidizing reaction and generate oxidation state oxygen carrier in air reactor, in air reactor, temperature raises gradually, along with the flow rate of oxygen carrier granule increases, the air capacity sent into from air intlet coupling increases, when presenting fast bed state in air reactor, stablize each pipe valve aperture;
(6), oxidation state oxygen carrier sends heat and lattice oxygen back to fuel reactor, wherein oxidation state oxygen carrier is introduced into single stage cyclone and carries out gas solid separation, the oxidation state oxygen carrier separated enters double jacket fluid-bed heat exchanger by single stage cyclone dipleg, under fluidizing agent loosens, the oxidation state oxygen carrier in double jacket fluid-bed heat exchanger is sent into feed-pipe, and to the coal tar heating in double jacket fluid-bed heat exchanger chuck, coal tar after preheating together enters the bottom of fuel reactor after being mixed with the fluidizing agent in fluidisation air intake branch by transition pipeline, oxidation state oxygen carrier enters fuel reactor by feed-pipe, fluidizing agent is passed into by the bottom of fuel reactor, under rheomorphism, coal tar is uniformly dispersed by oxygen carrier, and the c h bond of catalytic pyrolysis coal tar, the lattice oxygen of accelerating oxidation state oxygen carrier and H react and generate carbon black, carry the cooling water coil of flue gas successively by being interconnected of carbon black and a small amount of reduction-state oxygen carrier, the outer jacket for heat exchange cooling of water jacket interchanger and double jacket fluid-bed heat exchanger obtains cooled flue gas, cooled flue gas enters two-stage series connection cyclonic separator, reduction-state oxygen carrier is separated in primary cyclone, revert pipe is entered and after mixing with the reduction-state oxygen carrier entering revert pipe from fuel reactor bottom by primary cyclone dipleg, together return air reactor and complete Matter Transfer, and flue gas continues to enter secondary cyclone, part carbon black is separated to be got off to enter storage tank, residue carbon black carries collection device separated and collected after filtration by flue gas, tail gas is sent to waste heat boiler burning through offgas outlet, realize the preparation of carbon black.
2. the method for carbon black is prepared in the pyrolysis of coal-tar chemistry chain according to claim 1, it is characterized in that described coal-tar chemistry chain transforms the agent structure preparing the device of carbon black and comprises air reactor, single stage cyclone, double jacket fluid-bed heat exchanger, fuel reactor, water jacket interchanger, two-stage series connection cyclonic separator, device for filtering and collecting, air reactor vapor pipe, single stage cyclone dipleg, feed-pipe, transition pipeline, shell-and-tube exhaust-heat boiler, induced draft fan, fluidisation air intake branch, cooling water coil, primary cyclone dipleg, revert pipe, storage tank, oxidation state oxygen carrier, reduction-state oxygen carrier, fluidisation air inlet is responsible for, fuel reactor air distribution plate, revert pipe valve, air reactor air distribution plate, coal tar pan feeding valve, oxygen carrier material inlet valve, returning charge valve, air intlet, oxygen-denuded air exports, the main import of fluidizing agent, entrance of cooling water, high-temperature water exports, coal tar import, fluidizing agent divides import and offgas outlet, air reactor is communicated with single stage cyclone by the air reactor vapor pipe at top, and the bottom of air reactor is provided with air intlet, and the bottom of air reactor is provided with air reactor air distribution plate, air reactor and air reactor exhaust Bottomhole pressure have oxidation state oxygen carrier, and oxidation state oxygen carrier is generated by the oxygen reaction in reduction-state oxygen carrier and air, the bottom of single stage cyclone is communicated with double jacket fluid-bed heat exchanger by single stage cyclone dipleg, and the top of single stage cyclone is provided with oxygen-denuded air outlet, double jacket fluid-bed heat exchanger is communicated with the middle part of fuel reactor by feed-pipe, fuel reactor lower end is provided with fuel reactor air distribution plate, the bottom of fuel reactor air distribution plate is be responsible for fluidisation air inlet the air compartment be communicated with, fluidisation air inlet supervisor and the main inlet communication of fluidizing agent, fuel reactor is connected with the bottom of air reactor with revert pipe by returning charge valve, revert pipe between fuel reactor and returning charge valve is provided with revert pipe valve, returning charge Bottomhole pressure has reduction-state oxygen carrier, the top of fuel reactor is provided with cooling water coil, the top of cooling water coil is entrance of cooling water, cooling water coil is connected with water jacket interchanger, the top of fuel reactor is by the pipeline of water jacket heat exchanger cavity and the inlet communication of two-stage series connection cyclonic separator, two-stage series connection cyclonic separator is composed in series by the venting port of primary cyclone and the inlet mouth of secondary cyclone, primary cyclone dipleg is communicated with revert pipe, and the bottom of secondary cyclone is connected with storage tank, device for filtering and collecting is connected with the venting port of secondary cyclone, and the rear portion of device for filtering and collecting is provided with offgas outlet, the top right side of shell-and-tube exhaust-heat boiler is provided with high-temperature water outlet, the top of shell-and-tube exhaust-heat boiler exports with oxygen-denuded air and communicates, the outer chuck of double jacket fluid-bed heat exchanger is communicated with the bottom of shell-and-tube exhaust-heat boiler respectively with water jacket interchanger, bottom the internal layer chuck of double jacket fluid-bed heat exchanger, right side is connected with transition pipeline, the left side of the internal layer chuck of double jacket fluid-bed heat exchanger is provided with coal tar import, be provided with coal tar pan feeding valve with the pipeline of coal tar inlet communication, the fluidized-bed bottom of double jacket fluid-bed heat exchanger is provided with fluidizing agent and divides import, the bottom of transition pipeline is connected with fluidisation air intake branch, and vertical being connected is responsible for fluidisation air inlet in the one end bottom fluidisation air intake branch, and the other end bottom fluidisation air intake branch is provided with the tipping tube of 30 °, and tipping tube is connected with bottom fuel reactor, the pipeline of fluidisation air intake branch upper end is provided with oxygen carrier material inlet valve, and the import of induced draft fan is connected with the bottom of waste heat boiler, and the outlet of induced draft fan respectively import main with fluidizing agent divides import to be connected with fluidizing agent.
3. the method for carbon black is prepared in the pyrolysis of coal-tar chemistry chain according to claim 2, and it is characterized in that described air reactor is circulating fluidized bed, fuel reactor is bubbling fluidized bed; The internal layer chuck of double jacket fluid-bed heat exchanger is coal tar chuck, and outer chuck is cooling water jecket, the top of the coated fluidized-bed of double jacket and surrounding; Device for filtering and collecting adopts filter cloth bag and exhaust gases passes composition.
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