CN102864674B - Device and method for recycling gasified and burned alkali for straw pulp papermaking black liquor circulating fluidized bed - Google Patents
Device and method for recycling gasified and burned alkali for straw pulp papermaking black liquor circulating fluidized bed Download PDFInfo
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- CN102864674B CN102864674B CN201210344221.1A CN201210344221A CN102864674B CN 102864674 B CN102864674 B CN 102864674B CN 201210344221 A CN201210344221 A CN 201210344221A CN 102864674 B CN102864674 B CN 102864674B
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Abstract
The invention provides a device and a method for recycling gasified and burned alkali for a straw pulp papermaking black liquor circulating fluidized bed and relates to the device and the method for recycling the alkali of papermaking black liquor. The device and the method are used for solving the problems that the prior art is difficult to be used for recycling the straw pulp papermaking black liquor, the auxiliary fuels are added to a recycling process and the running cost is increased. The device comprises a multi-effect evaporator, a disc evaporator, a thick black liquor tank, a pump, a spraying gun, a gasifying chamber, a feedback valve, a waste heat boiler, an air pre-heater, a bag-type dust collector, a draught fan, a cone valve, a heat exchange chamber, a dissolving tank, a causticizer, a chain plate type slag conveyor, a drier, a secondary air fan, a second gas-solid separator, a tar condensing tower, a spraying dehydrating tower, a sewage treatment plant, a water annular compressor, an air storage tank, a circulating ash distributing chamber and a circulating fluidized bed, wherein the dissolving tank is respectively communicated with the causticizer and the chain plate type slag conveyor and the chain plate type slag conveyor is communicated with the drier. The device provided by the invention is used for recycling the alkali of the straw pulp papermaking black liquor.
Description
Technical field
The present invention relates to a kind of alkali recycling and processing device and method of black liquid, be specifically related to a kind of recirculating fluidized bed gasification, burning alkali recycling and processing device and method of black liquid of straw pulp paper-making.
Background technology
In recent years, paper industry has become that investment is large, energy consumption is high, one of industry that environmental pollution is serious.Alkali recovery technology is the effective method of current improvement wood pulp papermaking black liquor, and the high load capacity that Silvola recovery can significantly reduce black liquor pollutes, and can also reclaim heat energy, chemicals etc.The straw paper making raw material of China is contained very abundant, straw fiber raw material is the traditional Main Paper raw material of China, it is high that black liquid of straw pulp paper-making has silicon content, easily there is the stifled phenomenon of silicon, and silicon is dissolved in black liquor, in the time that reclaiming evaporation, alkali separates out, stop up evaporimeter, easily cause the accident, so the poor effect of current Silvola recovery to black liquid of straw pulp paper-making processing.What most of black liquid of straw pulp paper-making that therefore, China's paper industry produces caused pollutes so far also not fine solution.
By literature search, China Patent No. is that the patent of invention of ZL20031016916.7 has proposed a kind of alkali recovery device for straw pulp papermaking, this device equipment needed thereby quantity is few, the high-temperature flue gas obtaining with coal combustion is thermal source, although, in black liquid combusting furnace, arrange ash fall district, but still can be mixed with coal ash in bed course, had the problem of coking and separation difficulty; China Patent No. is that the patent of invention of ZL200610030429.0 has proposed a kind of method for recovering alkali of straw pulp papermaking, and the method can maintain the smooth combustion of alkali stove, but due to replace oil with coal, can make to be mixed with coal ash in alkali stove, has the problem of coking and separation difficulty; China Patent No. is that the utility model patent of ZL201020185445.9 has proposed a kind of gasifying pulping black liquor and direct causticization soda recovery unit, required caloric requirement fuel oil (as diesel oil, the heavy oil etc.) burning of this device black liquor gasification provides, and has increased the cost of processing black liquor; Chinese Patent Application No. is the method and apparatus that 201010549609.6 application for a patent for invention has proposed a kind of pulp treatment factory black liquor, although this patent has been avoided expensive gasifier, but separator used is difficult to sand grains to separate with other solids, pyrolytic reaction actuator temperature is higher, black liquor and sand grains easily bonding are agglomerating, and pyrolytic reaction is difficult to normally carry out; And need extra fuel normally to move for fluidized-bed combustion boiler, increase operating cost.
Summary of the invention
The object of the invention is to adopt prior art recycling black liquid of straw pulp paper-making difficulty for solving, and recovery processing technique need to add auxiliary fuel, increase the problem of operating cost, and then a kind of black liquid of straw pulp paper-making recirculating fluidized bed gasification, burning alkali recycling and processing device and method are provided.
The present invention addresses the above problem the technical scheme of taking to be:
Black liquid of straw pulp paper-making recirculating fluidized bed gasification of the present invention, burning alkali recycling and processing device comprises multi-effect evaporator, cascade evaporator, concentrated black liquid groove, pump, spray gun, vaporizer, returning charge valve, waste heat boiler, air preheater, sack cleaner, air-introduced machine, the first cone valve, heat-exchanging chamber, dissolving tank, causticizer, chain-plate type dragveyer, drier, overfire air fan, the second gas-solid separator, tar condensing tower, spray dehydrating tower, sewage treatment plant, water ring compressor, air accumulator, the second cone valve, circulating ash distributor chamber and recirculating fluidized bed, described recirculating fluidized bed comprises burner hearth, the first gas-solid separator, air compartment, air distribution plate, burner, feed bin, conveying worm and primary air fan, the top of burner hearth is provided with the first gas-solid separator and the two connection, the bottom of burner hearth is disposed with Secondary Air entrance and gasification gas entrance from top to bottom, the bottom of burner hearth is provided with air distribution plate, and the below of air distribution plate is provided with air compartment, and air compartment is communicated with burner, burner is communicated with primary air fan, gasification gas entrance is arranged between air distribution plate and Secondary Air entrance, and feed bin is arranged on the top of the feeding mouth of conveying worm, and the outlet of conveying worm is communicated with burner hearth,
The liquid outlet of multi-effect evaporator is communicated with the inlet of cascade evaporator, the liquid outlet of cascade evaporator is communicated with the inlet of concentrated black liquid groove, concentrated black liquid groove is communicated with the spray gun at the top that is arranged in vaporizer by pump, vaporizer is communicated with burner hearth by returning charge valve, the top of vaporizer is provided with the outlet of gasification gas, the outlet of gasification gas is communicated with the second gas-solid separator, the gas vent of the second gas-solid separator is communicated with tar condensing tower, the gas vent of tar condensing tower is communicated with spray dehydrating tower, the tar sewage mouth of the tar sewage mouth of tar condensing tower and spray dehydrating tower is respectively used to be communicated with sewage treatment plant, the gas vent of spray dehydrating tower is communicated with air accumulator by water ring compressor, the gas vent of air accumulator is communicated with gasification gas entrance,
The smoke gas port of the first gas-solid separator is communicated with waste heat boiler, the gas outlet of waste heat boiler is communicated with air preheater, the bottom of air preheater is provided with ash discharging hole, primary air fan is communicated with air preheater, air preheater is communicated with air compartment, the exhanst gas outlet of the bottom of air preheater is communicated with cascade evaporator, and cascade evaporator is communicated with sack cleaner, and sack cleaner is communicated with air-introduced machine;
The bottom of the first gas-solid separator is communicated with circulating ash distributor chamber, circulating ash distributor chamber is communicated with burner hearth, circulating ash distributor chamber is connected with vaporizer by the second cone valve, the bottom of burner hearth is connected with heat-exchanging chamber by the first cone valve, heat-exchanging chamber is communicated with dissolving tank, Secondary Air entrance and overfire air fan respectively, dissolving tank is communicated with causticizer and chain-plate type dragveyer respectively, and the cinder notch that removes of chain-plate type dragveyer is communicated with drier, and the discharging opening of drier is communicated with feed bin.
The concrete steps of black liquid of straw pulp paper-making recirculating fluidized bed gasification of the present invention, burning alkali recovery and treatment method are:
Step 1, the rare black liquor that is 8%～10% containing the percentage by weight of solid content is concentrated to the black liquor that the percentage by weight of solid content is 25%～30% through multi-effect evaporator;
Step 2, the black liquor that is 25%～30% by the percentage by weight of the concentrated multi-effect evaporator solid content obtaining are concentrated to through cascade evaporator the concentrated black liquid that the percentage by weight of solid content is 40%～45%, then, concentrated black liquid are stored in concentrated black liquid groove;
Step 3, will squeeze into spray gun through the concentrated concentrated black liquid obtaining of step 2 with pump, the concentrated black liquid after steam granulation is sent in vaporizer, and this concentrated black liquid gasifies in vaporizer;
Step 4, concentrated black liquid enter successively the second gas-solid separator, tar condensing tower and spray dehydrating tower through the outlet of gasification gas and carry out purified treatment through the gasify gasification gas that obtains of step 3, the solid separating through the second gas-solid separator is sent into burner hearth again, the sewage that contains tar obtaining after tar condensing tower and spray dehydrating tower purify is sent into sewage treatment plant and is processed, and the gasification gas obtaining after tar condensing tower and spray dehydrating tower purify is stored in air accumulator by water ring compressor;
Step 5, first bed material is thrown in to feed bin, the bed material in feed bin is sent in burner hearth through conveying worm, and the carbon containing semicoke that concentrated black liquid obtains after step 3 gasification is sent into hearth combustion by returning charge valve, and Control for Kiln Temperature is at 650 DEG C～900 DEG C; When furnace temperature is less than 650 DEG C, the part that part concentrated black liquid in concentrated black liquid groove in step 2 directly enters through concentrated black liquid entrance the gasification gas that in combustion-supporting in burner hearth and/or step 4, air accumulator stores directly enters in burner hearth combustion-supporting by gasification gas entrance, realize energy-autarchic, provide burner hearth required heat, the carbon containing semicoke obtaining after step 3 gasification can fully be burnt;
Step 6, remaining inorganic sodium and bed material after step 5 burning enter heat-exchanging chamber by the adjusting of the first cone valve, and the air of sending into overfire air fan in heat-exchanging chamber carries out heat exchange; The temperature obtaining after heat exchange is that the hot-air of 200 DEG C～400 DEG C is sent in burner hearth through Secondary Air entrance as Secondary Air;
Step 7, remaining inorganic sodium after step 6 is carried out heat exchange and bed material are sent in dissolving tank and are carried out precipitate and separate, and the solution after separation is sent into causticizer and carried out the recovery of causticization alkali, and it is dry that the sediment after separation is sent into drier by chain-plate type dragveyer; Dried drying device hybrid solid material is sent into feed bin and conveying worm successively, then send into burner hearth and recycle as bed material;
Step 8, enter the first gas-solid separator and carry out gas-solid separation through the burn flue gas that obtains of step 5, separating through the first gas-solid separator the temperature obtaining is the flue gas of 650 DEG C～900 DEG C, enter successively waste heat boiler, the gas obtaining after residual heat boiler for exchanging heat enters the air that air preheater and primary air fan send in air preheater and carries out heat exchange, reclaim heat, flue gas after air preheater heat exchange passes through cascade evaporator successively, after sack cleaner and air-introduced machine, enter atmosphere, temperature after air preheater heat exchange is at least the hot-air of 300 DEG C and sends into air compartment as a wind, separate through the first gas-solid separator the circulating ash obtaining and enter circulating ash distributor chamber, a circulating ash part that enters circulating ash distributor chamber is sent in burner hearth by pipeline, another part is sent in vaporizer by the adjusting of the second cone valve, provides black liquor gasification required heat.
The invention has the beneficial effects as follows: the present invention has effectively solved black liquid of straw pulp paper-making and processed a difficult problem, bed material reusable edible, after device operation, do not need to add auxiliary fuel, as required can be by concentrated black liquid and/or gasification pneumatic transmission to combustion-supporting in burner hearth, the burner hearth institute calorific requirement of recirculating fluidized bed is effectively provided, the self-sufficiency of implement device self-energy, has reduced operating cost, and operating cost has reduced more than 20%; When processing black liquid, also can produce gasification gas, can be used for other purposes, improve value-added content of product, economic benefit increases more than 25%; Utilize recirculating fluidized bed advantage, carry out fractional combustion, can effectively reduce NO
xdischarge, reduce environmental pollution, NOx discharge can reduce more than 50%, NO
xdischarge capacity meet national respective standard, there is good environmental benefit and economic benefit.
Brief description of the drawings
Fig. 1 is the overall structure schematic diagram of apparatus of the present invention and recovery processing technique.
Detailed description of the invention
Detailed description of the invention one: in conjunction with Fig. 1, present embodiment is described, the black liquid of straw pulp paper-making recirculating fluidized bed gasification of present embodiment, burning alkali recycling and processing device comprises multi-effect evaporator 1, cascade evaporator 2, concentrated black liquid groove 3, pump 4, spray gun 5, vaporizer 6, returning charge valve 7, waste heat boiler 10, air preheater 11, sack cleaner 13, air-introduced machine 14, the first cone valve 19, heat-exchanging chamber 20, dissolving tank 22, causticizer 23, chain-plate type dragveyer 24, drier 25, overfire air fan 28, the second gas-solid separator 30, tar condensing tower 31, spray dehydrating tower 32, sewage treatment plant 33, water ring compressor 34, air accumulator 35, the second cone valve 36, circulating ash distributor chamber 38 and recirculating fluidized bed, described recirculating fluidized bed comprises burner hearth 8, the first gas-solid separator 9, air compartment 17, air distribution plate 18, burner 16, feed bin 26, conveying worm 27 and primary air fan 15, the top of burner hearth 8 is provided with the first gas-solid separator 9 and the two connection, the bottom of burner hearth 8 is disposed with Secondary Air entrance 21 and gasification gas entrance 29 from top to bottom, the bottom of burner hearth 8 is provided with air distribution plate 18, the below of air distribution plate 18 is provided with air compartment 17, air compartment 17 is communicated with burner 16, burner 16 is communicated with primary air fan 15, gasification gas entrance 29 is arranged between air distribution plate 18 and Secondary Air entrance 21, feed bin 26 is arranged on the top of the feeding mouth of conveying worm 27, and the outlet of conveying worm 27 is communicated with burner hearth 8,
The liquid outlet of multi-effect evaporator 1 is communicated with the inlet of cascade evaporator 2, the liquid outlet of cascade evaporator 2 is communicated with the inlet of concentrated black liquid groove 3, concentrated black liquid groove 3 is communicated with the spray gun 5 at the top that is arranged in vaporizer 6 by pump 4, vaporizer 6 is communicated with burner hearth 8 by returning charge valve 7, the top of vaporizer 6 is provided with gasification gas outlet 37, gasification gas outlet 37 is communicated with the second gas-solid separator 30, the gas vent of the second gas-solid separator 30 is communicated with tar condensing tower 31, the gas vent of tar condensing tower 31 is communicated with spray dehydrating tower 32, the tar sewage mouth of the tar sewage mouth of tar condensing tower 31 and spray dehydrating tower 32 is respectively used to be communicated with sewage treatment plant 33, the gas vent of spray dehydrating tower 32 is communicated with air accumulator 35 by water ring compressor 34, the gas vent of air accumulator 35 is communicated with gasification gas entrance 29,
The smoke gas port of the first gas-solid separator 9 is communicated with waste heat boiler 10, the gas outlet of waste heat boiler 10 is communicated with air preheater 11, the bottom of air preheater 11 is provided with ash discharging hole 12, primary air fan 15 is communicated with air preheater 11, air preheater 11 is communicated with air compartment 17, the exhanst gas outlet of the bottom of air preheater 11 is communicated with cascade evaporator 2, and cascade evaporator 2 is communicated with sack cleaner 13, and sack cleaner 13 is communicated with air-introduced machine 14;
The bottom of the first gas-solid separator 9 is communicated with circulating ash distributor chamber 38, circulating ash distributor chamber 38 is communicated with burner hearth 8, circulating ash distributor chamber 38 is connected with vaporizer 6 by the second cone valve 36, the bottom of burner hearth 8 is connected with heat-exchanging chamber 20 by the first cone valve 19, heat-exchanging chamber 20 is communicated with dissolving tank 22, Secondary Air entrance 21 and overfire air fan 28 respectively, dissolving tank 22 is communicated with causticizer 23 and chain-plate type dragveyer 24 respectively, the cinder notch that removes of chain-plate type dragveyer 24 is communicated with drier 25, and the discharging opening of drier 25 is communicated with feed bin 26.
Acting as of the returning charge valve 7 of present embodiment, the one, the carbon containing semicoke after black liquor gasification and bed material are sent in the burner hearth 8 of recirculating fluidized bed smoothly, it two is to prevent that the gas anti-channeling in the burner hearth 8 of recirculating fluidized bed from entering in vaporizer 6, to ensure that black liquor gasifies and carries out smoothly in vaporizer 6.
The air accumulator 35 of present embodiment has two outlets, one of them for generation of gasification gas discharge and recycle, another is communicated with (air accumulator 35 is connected with the gas entrance 29 that gasifies by valve) with gasification gas entrance 29.
Detailed description of the invention two: in conjunction with Fig. 1, present embodiment is described, vaporizer 6 is bubbling bed described in present embodiment.So arrange, operate steadily, meet actual needs.Other is identical with detailed description of the invention one.
Detailed description of the invention three: in conjunction with Fig. 1, present embodiment is described, is provided with concentrated black liquid entrance 39 on the burner hearth 8 that is positioned at Secondary Air entrance 21 tops of present embodiment, the liquid outlet of concentrated black liquid groove 3 is communicated with concentrated black liquid entrance 39.So arrange, the burner hearth institute calorific requirement of recirculating fluidized bed can be effectively provided according to actual needs, the self-sufficiency of implement device self-energy, does not need to add other auxiliary fuel.The liquid outlet of present embodiment concentrated black liquid groove 3 is communicated with concentrated black liquid entrance 39 by valve.Other is identical with detailed description of the invention one or two.
Detailed description of the invention four: in conjunction with Fig. 1, present embodiment is described, the spray gun 5 of present embodiment is provided with steam inlet and concentrated black liquid import, concentrated black liquid groove 3 is communicated with the concentrated black liquid import being arranged on the spray gun 5 at top of vaporizer 6 by pump 4.So arrange, by the steam that passes into steam inlet, concentrated black liquid is carried out to granulating, make concentrated black liquid evenly be sprayed onto bed material upper, be conducive to concentrated black liquid gasification, can come from waste heat boiler 10 or other steam generator for the steam of granulation.
Detailed description of the invention five: in conjunction with Fig. 1, present embodiment is described, the black liquid of straw pulp paper-making recirculating fluidized bed gasification of present embodiment, the concrete steps of burning alkali recovery and treatment method are:
Step 1, the rare black liquor that is 8%～10% containing the percentage by weight of solid content is concentrated to the black liquor that the percentage by weight of solid content is 25%～30% through multi-effect evaporator 1;
Step 2, the black liquor that is 25%～30% by the percentage by weight of the concentrated solid content obtaining of multi-effect evaporator 1 are concentrated to through cascade evaporator 2 concentrated black liquid that the percentage by weight of solid content is 40%～45%, then, concentrated black liquid are stored in concentrated black liquid groove 3;
Step 3, will squeeze into spray gun 5 through the concentrated concentrated black liquid obtaining of step 2 with pump 4, the concentrated black liquid after steam granulation is sent in vaporizer 6, and this concentrated black liquid gasifies in vaporizer 6;
Step 4, concentrated black liquid enter successively the second gas-solid separator 30, tar condensing tower 31 and spray dehydrating tower 32 through gasification gas outlet 37 and carry out purified treatment through the gasify gasification gas that obtains of step 3, the solid separating through the second gas-solid separator 30 is sent into burner hearth 8 again, the sewage that contains tar obtaining after tar condensing tower 31 and spray dehydrating tower 32 purify is sent into sewage treatment plant 33 and is processed, and the gasification gas obtaining after tar condensing tower 31 and spray dehydrating tower 32 purify is stored in air accumulator 35 by water ring compressor 34;
Step 5, first bed material is thrown in to feed bin 26, the bed material in feed bin 26 is sent in burner hearth 8 through conveying worm 27, and the carbon containing semicoke that concentrated black liquid obtains after step 3 gasification is sent into burner hearth 8 by returning charge valve 7 and burnt, and Control for Kiln Temperature is at 650 DEG C～900 DEG C; When furnace temperature is less than 650 DEG C, it is interior combustion-supporting that the part that part concentrated black liquid in concentrated black liquid groove 3 in step 2 directly enters through concentrated black liquid entrance 39 the gasification gas that in the interior combustion-supporting and/or step 4 of burner hearth 8, air accumulator 35 stores directly enters burner hearth 8 by gasification gas entrance 29, realize energy-autarchic, provide burner hearth required heat, the carbon containing semicoke obtaining after step 3 gasification can fully be burnt;
Step 6, remaining inorganic sodium and bed material after step 5 burning enter heat-exchanging chamber 20 by the adjusting of the first cone valve 19, heat-exchanging chamber 20 in and the air sent into of overfire air fan 28 carry out heat exchange; The temperature obtaining after heat exchange be the hot-air of 200 DEG C～400 DEG C as Secondary Air in Secondary Air entrance 21 is sent into burner hearth 8;
Step 7, remaining inorganic sodium after step 6 is carried out heat exchange and bed material are sent into and in dissolving tank 22, are carried out precipitate and separate, solution after separation is sent into causticizer 23 and is carried out the recovery of causticization alkali, and it is dry that the sediment after separation is sent into drier 25 by chain-plate type dragveyer 24; Dried drying device 25 hybrid solid material is sent into feed bin 26 and conveying worm 27 successively, then send into burner hearth 8 and recycle as bed material;
Step 8, enter the first gas-solid separator 9 and carry out gas-solid separation through the burn flue gas that obtains of step 5, separating through the first gas-solid separator 9 temperature obtaining is the flue gas of 650 DEG C～900 DEG C, enter successively waste heat boiler 10, the gas obtaining after waste heat boiler 10 heat exchange enters the air that air preheater 11 and primary air fan 15 send in air preheater 11 and carries out heat exchange, reclaim heat, flue gas after air preheater 11 heat exchange passes through cascade evaporator 2 successively, after sack cleaner 13 and air-introduced machine 14, enter atmosphere, temperature after air preheater 11 heat exchange is at least the hot-air of 300 DEG C and sends into air compartment 17 as a wind, separate through the first gas-solid separator 9 circulating ash obtaining and enter circulating ash distributor chamber 38, a circulating ash part that enters circulating ash distributor chamber 38 is sent in burner hearth 8 by pipeline, another part is sent in vaporizer 6 by the adjusting of the second cone valve 36, provides black liquor gasification required heat.
In present embodiment in the time that the temperature of vaporizer 6 is less than 200 DEG C, moisture in black liquor evaporates in vaporizer 6, and do not carry out cracking or gasification reaction, the steam being evaporated directly enters spray dehydrating tower 32 by pipeline and removes moisture, spray dehydrating tower 32 sewage out enters sewage treatment plant 33 and processes, in order to avoid contaminated environment, the gas after dewatering enters atmosphere, and does not enter in air accumulator 35.The burner hearth 8 that black liquor after super-dry is concentrated is directly sent into recirculating fluidized bed burns, and carries out alkali recovery.
The air channel that the primary air fan 15 of present embodiment connects is divided into three tunnels: the first via is for starting fluidized wind, and air is sent in burner 16 by pipeline, and burn required air add hot-air of burner 16 is provided; The second tunnel is the secondary mixing wind that starts fluidized wind, and object is to reduce the wind-warm syndrome that starts fluidized wind, and the first via and the second tunnel are sent in air compartment 17 after mixing, and first and second transportation work style is used in the time of burner hearth 8 cold start of recirculating fluidized bed, while normally operation, closes; Third Road wind is sent in air preheater 11 by pipeline, and normal temperature air is sent into air compartment 17 as a wind by pipeline after air preheater 11 preheatings.
It is interior combustion-supporting that the part of the gasification gas that in the step 5 of present embodiment, air accumulator 35 stores directly enters burner hearth 8 by the valve on adjusting pipeline by gasification gas entrance 29; It is interior combustion-supporting that part concentrated black liquid in concentrated black liquid groove 3 directly enters burner hearth 8 by the valve on adjusting pipeline through concentrated black liquid entrance 39.
Detailed description of the invention six: the bed material of present embodiment is Na
2cO
3or zeolite.So arranging, is because black-liquor combustion product main component is Na
2cO
3particle; When present embodiment mesolite is bed material, furnace temperature can reach 900 DEG C, is conducive to improve vaporizer gasification temperature.Other is identical with detailed description of the invention five.
Detailed description of the invention seven: in the step 3 of present embodiment, the gasification temperature of vaporizer 6 is 200 DEG C～800 DEG C.The fluidizing agent of the vaporizer 6 of present embodiment can be steam or gasification gas, and steam comes from waste heat boiler 10 or other steam, and gasification gas comes from air accumulator 35.So arrange, be conducive to improve the calorific value of gasification gas, meet later use needs.Other is identical with detailed description of the invention five.
Detailed description of the invention eight: in the step 5 of present embodiment, Control for Kiln Temperature is at 660 DEG C～900 DEG C.So arrange, meet actual needs.Other is identical with detailed description of the invention five, six or seven.
Detailed description of the invention nine: the fluidizing agent that the circulating ash distributor chamber 38 of the step 8 of present embodiment adopts is steam, steam comes from waste heat boiler 10 or other steam.So arrange, in order to prevent that air from entering vaporizer and causing blast.Other is identical with detailed description of the invention five.
Claims (5)
1. black liquid of straw pulp paper-making recirculating fluidized bed gasification, a burning alkali recovery and treatment method, is characterized in that: the concrete steps of described method are:
Step 1, the rare black liquor that is 8%～10% containing the percentage by weight of solid content is concentrated to the black liquor that the percentage by weight of solid content is 25%～30% through multi-effect evaporator (1);
Step 2, the black liquor that is 25%～30% by the percentage by weight of the concentrated solid content obtaining of multi-effect evaporator 1 are concentrated to through cascade evaporator (2) concentrated black liquid that the percentage by weight of solid content is 40%～45%, then, concentrated black liquid is stored in concentrated black liquid groove (3);
Step 3, will squeeze into spray gun (5) through the concentrated concentrated black liquid obtaining of step 2 with pump (4), the concentrated black liquid after steam granulation is sent in vaporizer (6), and this concentrated black liquid gasifies in vaporizer (6);
Step 4, concentrated black liquid enters the second gas-solid separator (30) through the gasify gasification gas that obtains of step 3 successively through gasification gas outlet (37), tar condensing tower (31) and spray dehydrating tower (32) carry out purified treatment, the solid separating through the second gas-solid separator (30) is sent into burner hearth (8) again, the sewage that contains tar obtaining after tar condensing tower (31) and spray dehydrating tower (32) purify is sent into sewage treatment plant (33) and is processed, the gasification gas obtaining after tar condensing tower (31) and spray dehydrating tower (32) purify is stored in air accumulator (35) by water ring compressor (34),
Step 5, first bed material is thrown in to feed bin (26), bed material in feed bin (26) is sent in burner hearth (8) through conveying worm (27), the carbon containing semicoke that concentrated black liquid obtains after step 3 gasification is sent into burner hearth (8) burning by returning charge valve (7), and Control for Kiln Temperature is at 650 DEG C～900 DEG C; When furnace temperature is less than 650 DEG C, the part of the gasification gas that in combustion-supporting and/or step 4, air accumulator (35) stores in concentrated black liquid entrance (39) directly enters burner hearth (8) of the part concentrated black liquid in the concentrated black liquid groove (3) in step 2 directly enters in burner hearth (8) combustion-supporting by the gas entrance (29) that gasifies, realize energy-autarchic, provide burner hearth required heat, the carbon containing semicoke obtaining after step 3 gasification can fully be burnt;
Step 6, remaining inorganic sodium and bed material after step 5 burning enter heat-exchanging chamber (20) by the adjusting of the first cone valve (19), in heat-exchanging chamber (20) and the air sent into of overfire air fan (28) carry out heat exchange; The temperature obtaining after heat exchange be the hot-air of 200 DEG C～400 DEG C as Secondary Air in Secondary Air entrance (21) is sent into burner hearth (8);
Step 7, remaining inorganic sodium after step 6 is carried out heat exchange and bed material are sent in dissolving tank (22) and are carried out precipitate and separate, solution after separation is sent into causticizer (23) and is carried out the recovery of causticization alkali, and it is dry that the sediment after separation is sent into drier (25) by chain-plate type dragveyer (24); Dried drying device (25) hybrid solid material is sent into feed bin (26) and conveying worm (27) successively, then send into burner hearth (8) and recycle as bed material;
Step 8, enter the first gas-solid separator (9) and carry out gas-solid separation through the burn flue gas that obtains of step 5, separating through the first gas-solid separator (9) temperature obtaining is the flue gas of 650 DEG C～900 DEG C, enter successively waste heat boiler (10), the gas obtaining after waste heat boiler (10) heat exchange enters the air that air preheater (11) and primary air fan (15) send in air preheater (11) and carries out heat exchange, reclaim heat, flue gas after air preheater (11) heat exchange passes through cascade evaporator (2) successively, after sack cleaner (13) and air-introduced machine (14), enter atmosphere, temperature after air preheater (11) heat exchange is at least the hot-air of 300 DEG C and sends into air compartment (17) as a wind, separate through the first gas-solid separator (9) circulating ash obtaining and enter circulating ash distributor chamber (38), a circulating ash part that enters circulating ash distributor chamber (38) is sent in burner hearth (8) by pipeline, another part is sent in vaporizer (6) by the adjusting of the second cone valve (36), provides black liquor gasification required heat.
2. black liquid of straw pulp paper-making recirculating fluidized bed gasification according to claim 1, burning alkali recovery and treatment method, is characterized in that: described bed material is Na
2cO
3or zeolite.
3. black liquid of straw pulp paper-making recirculating fluidized bed gasification according to claim 1, burning alkali recovery and treatment method, is characterized in that: the gasification temperature of vaporizer in step 3 (6) is 200 DEG C～800 DEG C.
4. according to the black liquid of straw pulp paper-making recirculating fluidized bed gasification described in claim 1,2 or 3, burning alkali recovery and treatment method, it is characterized in that: in step 5, Control for Kiln Temperature is at 660 DEG C～900 DEG C.
5. black liquid of straw pulp paper-making recirculating fluidized bed gasification according to claim 1, burning alkali recovery and treatment method, it is characterized in that: the fluidizing agent that the circulating ash distributor chamber (38) of step 8 adopts is steam, and steam comes from waste heat boiler (10) or other steam.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210344221.1A CN102864674B (en) | 2012-09-17 | 2012-09-17 | Device and method for recycling gasified and burned alkali for straw pulp papermaking black liquor circulating fluidized bed |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210344221.1A CN102864674B (en) | 2012-09-17 | 2012-09-17 | Device and method for recycling gasified and burned alkali for straw pulp papermaking black liquor circulating fluidized bed |
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| CN102864674A CN102864674A (en) | 2013-01-09 |
| CN102864674B true CN102864674B (en) | 2014-08-27 |
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| CN103396839B (en) * | 2013-08-20 | 2015-04-08 | 中国科学院广州能源研究所 | Gasification alkali-recovering method of straw soda-process pulping black-liquor solid and apparatus |
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| CN110669541A (en) * | 2019-11-08 | 2020-01-10 | 重庆科技学院 | Process and device for preparing oil by pyrolyzing waste plastics |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4808264A (en) * | 1985-06-03 | 1989-02-28 | Kignell Jean Erik | Process for chemicals and energy recovery from waste liquors |
| CN1086865A (en) * | 1992-06-18 | 1994-05-18 | 燃烧工程有限公司 | The technology of CFB black liquor gasification system operation at low pressures and design |
| CN101210396A (en) * | 2007-12-25 | 2008-07-02 | 哈尔滨工业大学 | Paper-making black liquor fluidized bed alkali reclaiming device and method |
| CN101831827A (en) * | 2010-04-30 | 2010-09-15 | 中国科学院广州能源研究所 | Preparation method of paper making black liquid semi-coke |
| CN102086605A (en) * | 2009-10-05 | 2011-06-08 | 美卓动力有限公司 | Method and apparatus for processing black liquor of pulp mill |
-
2012
- 2012-09-17 CN CN201210344221.1A patent/CN102864674B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4808264A (en) * | 1985-06-03 | 1989-02-28 | Kignell Jean Erik | Process for chemicals and energy recovery from waste liquors |
| CN1086865A (en) * | 1992-06-18 | 1994-05-18 | 燃烧工程有限公司 | The technology of CFB black liquor gasification system operation at low pressures and design |
| CN101210396A (en) * | 2007-12-25 | 2008-07-02 | 哈尔滨工业大学 | Paper-making black liquor fluidized bed alkali reclaiming device and method |
| CN102086605A (en) * | 2009-10-05 | 2011-06-08 | 美卓动力有限公司 | Method and apparatus for processing black liquor of pulp mill |
| CN101831827A (en) * | 2010-04-30 | 2010-09-15 | 中国科学院广州能源研究所 | Preparation method of paper making black liquid semi-coke |
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