CN111377625A - Comprehensive utilization process and device for reducing roasting of phosphogypsum circulating fluidized bed - Google Patents
Comprehensive utilization process and device for reducing roasting of phosphogypsum circulating fluidized bed Download PDFInfo
- Publication number
- CN111377625A CN111377625A CN201910898514.6A CN201910898514A CN111377625A CN 111377625 A CN111377625 A CN 111377625A CN 201910898514 A CN201910898514 A CN 201910898514A CN 111377625 A CN111377625 A CN 111377625A
- Authority
- CN
- China
- Prior art keywords
- fluidized bed
- cyclone separator
- phosphogypsum
- flue gas
- stage
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- PASHVRUKOFIRIK-UHFFFAOYSA-L calcium sulfate dihydrate Chemical compound O.O.[Ca+2].[O-]S([O-])(=O)=O PASHVRUKOFIRIK-UHFFFAOYSA-L 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 18
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 53
- 239000003546 flue gas Substances 0.000 claims abstract description 53
- 238000001816 cooling Methods 0.000 claims abstract description 44
- 239000000463 material Substances 0.000 claims abstract description 39
- 239000003245 coal Substances 0.000 claims abstract description 32
- 229910052602 gypsum Inorganic materials 0.000 claims abstract description 32
- 239000010440 gypsum Substances 0.000 claims abstract description 32
- 239000002994 raw material Substances 0.000 claims abstract description 27
- 239000000203 mixture Substances 0.000 claims abstract description 8
- 239000002893 slag Substances 0.000 claims abstract description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 6
- ZOMBKNNSYQHRCA-UHFFFAOYSA-J calcium sulfate hemihydrate Chemical compound O.[Ca+2].[Ca+2].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O ZOMBKNNSYQHRCA-UHFFFAOYSA-J 0.000 claims abstract description 5
- 229910052500 inorganic mineral Inorganic materials 0.000 claims abstract description 5
- 239000011707 mineral Substances 0.000 claims abstract description 5
- 239000002245 particle Substances 0.000 claims description 33
- 239000000428 dust Substances 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 7
- 230000001590 oxidative effect Effects 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 7
- 238000002485 combustion reaction Methods 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 239000000725 suspension Substances 0.000 claims description 5
- 239000003077 lignite Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- 239000000779 smoke Substances 0.000 claims 4
- 238000002156 mixing Methods 0.000 abstract description 3
- 230000004913 activation Effects 0.000 abstract description 2
- 239000004566 building material Substances 0.000 abstract description 2
- 238000001035 drying Methods 0.000 abstract description 2
- 238000005516 engineering process Methods 0.000 abstract description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000002689 soil Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- -1 bark Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000007789 gas Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 239000004058 oil shale Substances 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B11/00—Calcium sulfate cements
- C04B11/02—Methods and apparatus for dehydrating gypsum
- C04B11/028—Devices therefor characterised by the type of calcining devices used therefor or by the type of hemihydrate obtained
- C04B11/0283—Fluidised beds
-
- C—CHEMISTRY; METALLURGY
- C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
- C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
- C04B11/00—Calcium sulfate cements
- C04B11/26—Calcium sulfate cements strating from chemical gypsum; starting from phosphogypsum or from waste, e.g. purification products of smoke
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Ceramic Engineering (AREA)
- Materials Engineering (AREA)
- Structural Engineering (AREA)
- Organic Chemistry (AREA)
- Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
- Crucibles And Fluidized-Bed Furnaces (AREA)
Abstract
The invention discloses a comprehensive utilization process and a device for reducing roasting of a phosphogypsum circulating fluidized bed, which comprises a circulating fluidized bed reactor provided with a slag discharge port, wherein the bottom of the circulating fluidized bed reactor is provided with an air inlet, the lower part of the dense phase area is respectively provided with a coal feeding inlet, a phosphogypsum/mineral mixture inlet, a circulating material inlet and a secondary air inlet, the top of the circulating fluidized bed reactor is provided with a flue gas outlet which is connected with the circulating material inlet and a first-stage fluidized bed cooling device through a first-stage cyclone separator, the flue gas outlet of the first-stage cyclone separator is connected with a second-stage cyclone separator, the lower part of the second-stage separator is connected with the first-stage fluidized bed cooling device, the flue gas outlet of the second-stage cyclone separator is connected with a third-stage cyclone separator, the lower part of the third-stage cyclone separator is connected with the second-stage fluidized bed cooling device. The invention aims to realize activation of the phosphogypsum/tailing mixed material under the condition of reduction roasting at the temperature of about 850 ℃ by blending the components of the phosphogypsum/tailing mixed raw material. Therefore, the efficient roasting technology and device are the key for realizing the efficient clean utilization of the phosphogypsum/tailing mixed raw material. On the other hand, the hemihydrate gypsum is a better building material and has a better application market at present. Therefore, the application value of the phosphogypsum can be improved by preparing the existing water-containing gypsum into the hemihydrate gypsum through the processes of drying and the like.
Description
Technical Field
The invention relates to the field of phosphogypsum resource utilization, in particular to a reduction roasting process and a reduction roasting device for a phosphogypsum circulating fluidized bed.
Background
The phosphogypsum is solid waste residue generated in the production process of phosphoric acid, the emission amount is huge every year, and the discharged phosphogypsum occupies a large amount of land to form slag hills and seriously pollute the environment, so how to carry out resource utilization on the phosphogypsum is a problem to be solved urgently. According to research, the phosphogypsum/tailing mixed raw material contains various mineral components and can be used as a soil improvement fertilizer after being activated. By blending the components of the phosphogypsum/tailings mixed raw material, the phosphogypsum/tailings mixed material can be activated under the condition of reduction roasting at the temperature of about 850 ℃. Therefore, the efficient roasting technology and device are the key for realizing the efficient clean utilization of the phosphogypsum/tailing mixed raw material.
On the other hand, the hemihydrate gypsum is a better building material and has a better application market at present. Therefore, the application value of the phosphogypsum can be improved by preparing the existing water-containing gypsum into the hemihydrate gypsum through the processes of drying and the like.
Disclosure of Invention
In order to solve the problem of resource utilization of the phosphogypsum, the invention provides a comprehensive reduction roasting utilization process and a comprehensive reduction roasting utilization device of a phosphogypsum circulating fluidized bed, which comprise a circulating fluidized bed reactor with a slag discharge port.
The circulating fluidized bed reactor is characterized in that an air inlet is formed in the bottom of the circulating fluidized bed reactor, a coal feeding inlet, a phosphogypsum/mineral mixture inlet, a circulating material inlet and a secondary air inlet are formed in the lower portion of a dense-phase region respectively, a flue gas outlet is formed in the top of the circulating fluidized bed reactor and is connected with the circulating material inlet and a primary fluidized bed cooling device through a primary cyclone separator, the flue gas outlet of the primary cyclone separator is connected with a secondary cyclone separator, the lower portion of the secondary cyclone separator is connected with the primary fluidized bed cooling device, the flue gas outlet of the secondary cyclone separator is connected with a tertiary cyclone separator, the lower portion of the tertiary cyclone separator is connected with the secondary fluidized bed cooling device, and meanwhile.
In the invention, the semi-hydrated gypsum production device is connected with a flue gas outlet of a third-stage cyclone separator, a phosphogypsum feeder is arranged at the top of the left side of the device, a flue gas outlet is arranged at the top of the right side of the device and is connected with a fourth-stage cyclone separator, the flue gas outlet of the fourth-stage cyclone separator is connected with a bag-type dust collector, the lower part of the bag-type dust collector is connected with a draught fan and a chimney, and the outlet of the bag.
The invention further provides a phosphogypsum circulating fluidized bed reduction roasting process and a device based on the device, and the process comprises the following steps:
(1) granular coal materials are fed into the middle part of a dense-phase region of a circulating fluidized bed reactor through a coal hopper, the particle size of the coal is 0-5mm, primary air enters a hearth from an air chamber at the bottom of the hearth and reacts with the coal particles, the reaction temperature is between 800 and 900 ℃, secondary air enters the hearth from the upper part of the dense-phase region and is distributed by primary air and secondary air in a grading manner, the region at the lower part of the hearth is a reducing atmosphere, and the upper part of the hearth is an oxidizing atmosphere. The phosphogypsum/tailing mixture is directly fed into the lower part of a hearth through a feeding device, so that high-temperature roasting is realized.
(2) The outlet at the upper part of the circulating fluidized bed reactor is provided with a first-stage cyclone separator, most of the separated high-temperature particles are directly returned to the roasting furnace through a loopseal material returning device to realize circulating roasting so as to improve the combustion efficiency of the coal particles and the roasting effect of the raw materials, and the smaller part of the separated high-temperature particles is used as a roasted finished product and is fed into a fluidized bed cooling device. The high-temperature flue gas after the first-stage separation enters a second-stage cyclone separator to separate the contained roasted finished product particles, and the separated particles are sent to a first-stage air fluidized bed cooling device. The hot air heated by the first-stage fluidized bed cooling device is directly sent into the circulating fluidized bed roasting furnace to be used as secondary air. And feeding the material particles after the first-stage cooling into a second-stage fluidized bed cooling device for cooling, and then sending out as a product. The heated hot air is mixed with the high-temperature flue gas from the secondary cyclone separator before being sent into the tertiary cyclone separator, and the temperature of the flue gas entering the tertiary cyclone separator is controlled to be about 625 ℃.
(3) The mixed flue gas enters a three-stage cyclone separator for further separating the contained roasted products, and the separated materials are sent to a two-stage fluidized bed cooling device. And (3) the separated high-temperature flue gas enters a suspension bed semi-hydrated gypsum reaction device to be mixed with the fed phosphogypsum raw material, and the phosphogypsum raw material is heated to dry most of water contained in the phosphogypsum raw material to be separated out in the process of carrying phosphogypsum raw material particles to flow so as to form the semi-hydrated gypsum.
(4) The cooled flue gas carries the semi-hydrated gypsum particles to enter a four-stage cyclone separator, most of the produced semi-hydrated gypsum particles are separated, and the separated flue gas (lower than 190 ℃) carries a small amount of semi-hydrated gypsum particles to enter a bag-type dust collector for further separation. And (4) discharging the dedusted flue gas from a chimney.
Description of the invention
The interior of the circulating fluidized bed reactor is respectively a reducing atmosphere region and an oxidizing atmosphere region from bottom to top, phosphogypsum is subjected to reducing roasting in the reducing atmosphere region at the lower part of a hearth, secondary air is supplemented in the oxidizing atmosphere region at the upper part of the hearth for oxidizing roasting, most of phosphogypsum solid particles are separated from gas by a cyclone separator, and are returned to the hearth for roasting through a material returning device to be mixed with newly charged phosphogypsum and coal, so that a main loop of the circulating fluidized bed reactor is formed. The invention aims to reduce and roast phosphogypsum/tailings through a circulating fluidized bed reactor so as to achieve the purpose of full activation, and finally the phosphogypsum/tailings are used for a soil improvement fertilizer.
Compared with the prior art, the invention has the following beneficial effects:
the roasting reaction atmosphere and the temperature distribution are convenient to adjust and control. The gas-solid two phases are mixed violently in the reduction roasting process of the circulating fluidized bed, and the heat transfer and mass transfer process is fast. The material is returned by the cyclone separator and the material returning device, so that the retention time of the material in the reactor can be prolonged; by means of graded air distribution, the reaction atmosphere in different areas of the reactor can be controlled, and the roasting effect is ensured.
The fuel adaptability is wide, the circulating fluidized bed reactor can burn high-quality coal, various inferior fuels such as high-ash coal, high-sulfur coal, high-ash high-sulfur coal, high-moisture coal, coal gangue, coal slime and the like, and oil shale, petroleum coke, tailings, furnace slag, bark, waste wood, garbage and the like.
The low-temperature combustion characteristic of the circulating fluidized bed reactor can realize in-furnace desulfurization.
The semi-hydrated gypsum is produced by using high-temperature flue gas generated by roasting of the circulating fluidized bed, the waste heat is fully utilized, and the comprehensive utilization of the phosphogypsum is realized while the high heat efficiency of the system is realized.
Drawings
Fig. 1 is a schematic diagram of an implementation of the device according to the invention.
In the figure: the system comprises a coal feeding device 1, a phosphogypsum/ore feeding device 2, a circulating fluidized bed reactor 3, a Loopseal returning device 4, a primary cyclone separator 5, a secondary cyclone separator 6, an air chamber 7, a primary fan 8, a primary fluidized bed cooler 9, a secondary fan 10, a secondary fluidized bed cooler 11, a product collector 12, a tertiary cyclone separator 13, a suspended bed semi-hydrated gypsum reaction device 14, a phosphogypsum feeding device 15, a quaternary cyclone separator 16, a semi-hydrated gypsum collector 17, a bag-type dust remover 18, an induced draft fan 19 and a chimney 20
The specific implementation mode is as follows:
the following describes an implementation form of the present invention with reference to the accompanying drawings.
The solution of the invention is to provide a reduction roasting process and a device of a phosphogypsum circulating fluidized bed, which mainly comprise a circulating fluidized bed reactor 3 with a slag discharge port.
An air chamber 7 is arranged at the bottom of the circulating fluidized bed reactor 3, a coal feeding device 1 and a phosphogypsum/mineral feeding device 2 are respectively arranged at the lower part of a dense-phase region, the top of the circulating fluidized bed reactor 3 is connected with a primary cyclone separator 5, a Loopseal returning device 4 is connected with the circulating fluidized bed reactor 3 and the primary fluidized bed cooling device 9, a flue gas outlet of the primary cyclone separator 5 is connected with a secondary cyclone separator 6, the lower part of the secondary cyclone separator 6 is connected with the primary fluidized bed cooling device 9, a flue gas outlet of the secondary cyclone separator 6 is connected with a tertiary cyclone separator 13, the lower part of the tertiary cyclone separator 13 is connected with a secondary fluidized bed cooling device 11, meanwhile, the primary fluidized bed cooling device 9 is connected with the secondary fluidized bed cooling device 11, and materials from the outlet of the secondary fluidized bed cooling device.
In the invention, the semi-hydrated gypsum production device 14 is connected with a flue gas outlet of a third-stage cyclone separator 13, a phosphogypsum feeder 15 is arranged at the top of the left side of the device, a flue gas outlet is arranged at the top of the right side of the device and is connected with a fourth-stage cyclone separator 16, the flue gas outlet of the fourth-stage cyclone separator 16 is connected with a bag-type dust collector 18, the lower part of the fourth-stage cyclone separator 16 is connected with a semi-hydrated gypsum collector 17, and the outlet of the bag-type.
The phosphogypsum circulating fluidized bed reduction roasting process and device based on the device comprise the following steps:
(1) granular coal materials are sent into the middle part of a dense-phase region of a circulating fluidized bed reactor 3 through a coal feeding device 1, the particle size of the coal is 0-5mm, primary air enters a hearth from an air chamber 7 at the bottom of the hearth and reacts with the coal materials, the reaction temperature is between 800 ℃ and 900 ℃, secondary air enters the hearth from the upper part of the dense-phase region through a secondary fan 10 and is distributed in a grading manner through the primary air and the secondary air, the lower region of the hearth is a reducing atmosphere, and the upper part of the hearth is an oxidizing atmosphere. The phosphogypsum/tailing mixture is directly fed into the lower part of the hearth through the feeding device 2, and high-temperature reduction roasting is realized.
(2) The outlet at the upper part of the circulating fluidized bed reactor 3 is provided with a primary cyclone separator 5, and the separated high-temperature particles are directly returned to the hearth through a loopseal return feeder 4 to realize circulating roasting so as to improve the combustion efficiency of the lignite and the roasting effect of the raw materials. The high-temperature flue gas after the first-stage separation enters a second-stage cyclone separator 6 to separate the contained roasted finished product raw materials, and the separated particles are sent to a first-stage air fluidized bed cooling device 9. The hot air heated by the first fluidized bed cooling device 9 is directly sent into the circulating fluidized bed reactor 3 to be used as secondary air. The cooled material is sent to a secondary fluidized bed cooling device 11 to be cooled and then sent out as a product. The heated hot air is mixed with the high-temperature flue gas from the secondary cyclone separator 6 for temperature reduction before being sent to the tertiary cyclone separator 13.
(3) The mixed flue gas enters a third-stage cyclone separator 13 to further separate the contained roasted products, and the separated materials are sent to a second-stage fluidized bed cooling device 11. The separated high-temperature flue gas enters a suspension bed semi-hydrated gypsum reaction device 17 to be mixed with the fed phosphogypsum raw material, and the phosphogypsum raw material is heated to dry most of water contained in the phosphogypsum raw material to be separated out in the process of carrying phosphogypsum raw material particles to flow so as to form semi-hydrated gypsum.
(4) The cooled flue gas carries the semi-hydrated gypsum particles to enter a four-stage cyclone separator 16, most of the produced semi-hydrated gypsum particles are separated, the separated flue gas carries a small amount of semi-hydrated gypsum particles to enter a bag-type dust remover 18 for further separation, and the flue gas is discharged through an induced draft fan 19 and a flue gas barrel chimney 20 after dust removal.
Examples of specific applications
Granular coal materials are fed into the middle of a dense-phase region of a circulating fluidized bed reactor through a coal hopper, the coal feeding amount is 12600kg/h, the particle size of the coal is 0-5mm, primary air enters a hearth from an air chamber at the bottom of the hearth and reacts with the coal materials, the reaction temperature is about 850 ℃, secondary air enters the hearth from the upper part of the dense-phase region, and the lower region of the hearth is controlled to be in a reducing atmosphere and the upper part of the hearth is controlled to be in an oxidizing atmosphere through graded air distribution of the primary air and the secondary air.
The phosphogypsum/tailing mixture is directly fed into the lower part of a hearth through a feeding device, the feeding amount is 40000kg/h, and high-temperature reduction roasting is realized. The outlet at the upper part of the circulating fluidized bed reactor is provided with a primary cyclone separator, the separated high-temperature particles are directly returned to the roasting furnace through a loopseal material returning device to realize circulating roasting so as to improve the combustion efficiency of lignite and the roasting effect of raw materials, and part of the materials are sent to a primary fluidized bed cooling device. The high-temperature flue gas after the first-stage separation enters a second-stage cyclone separator to separate the contained roasted finished product raw materials, and the separated particles are sent to a first-stage air fluidized bed cooling device. The hot air at about 465 ℃ heated by the first-stage fluidized bed cooling device is directly sent into the circulating fluidized bed roasting furnace to be used as secondary air. The cooled material is sent into a secondary fluidized bed cooling device to be cooled to 170 ℃ and then sent out as a product, and the amount of the roasted finished product is 32900 kg/h. The heated hot air is mixed with the high-temperature flue gas from the secondary cyclone separator for cooling before being sent to the tertiary cyclone separator, and the temperature of the mixed flue gas is about 625 ℃.
The mixed flue gas enters a three-stage cyclone separator for further separating the contained roasted products, and the separated materials are sent to a two-stage fluidized bed cooling device. And (3) feeding the separated high-temperature flue gas into a descending suspension bed semi-hydrated gypsum reaction device, mixing the separated high-temperature flue gas with the fed phosphogypsum raw material, wherein the feeding amount of the phosphogypsum is 41000kg/h, heating the phosphogypsum raw material to dry and separate out most of water in the flowing process of carrying phosphogypsum raw material particles to form semi-hydrated gypsum, and the yield of the semi-hydrated gypsum is 28400 kg/h.
Claims (10)
1. A reducing roasting process and a device of a phosphogypsum circulating fluidized bed mainly comprise a circulating fluidized bed reactor with a slag discharge port.
The circulating fluidized bed reactor is characterized in that an air inlet is formed in the bottom of the circulating fluidized bed reactor, a coal material inlet, a phosphogypsum/mineral mixture inlet, a circulating material inlet and a secondary air inlet are formed in the lower portion of a dense-phase region respectively, a flue gas outlet is formed in the top of the circulating fluidized bed reactor and is connected with the circulating material inlet and a primary fluidized bed cooling device through a primary cyclone separator, the flue gas outlet of the primary cyclone separator is connected with a secondary cyclone separator, the lower portion of the secondary cyclone separator is connected with the primary fluidized bed cooling device, the flue gas outlet of the secondary cyclone separator is connected with a tertiary cyclone separator, the lower portion of the tertiary cyclone separator is connected with the secondary fluidized bed cooling device, and meanwhile.
The suspension bed semi-hydrated gypsum production device is connected with a smoke outlet of a third-stage cyclone separator, a phosphogypsum feeder is arranged at the top of the left side of the device, a smoke outlet is arranged at the top of the right side of the device and is connected with a fourth-stage cyclone separator, the smoke outlet of the fourth-stage cyclone separator is connected with a bag-type dust collector, and the lower part of the smoke outlet is connected with a semi-hydrated gypsum collector.
And the outlet of the bag-type dust collector is connected with an induced draft fan and a chimney.
2. The apparatus of claim 1, wherein:
the interior of the circulating fluidized bed reactor is divided into an air chamber, a dense-phase area and a dilute-phase area from bottom to top, a primary air inlet is connected with the air chamber, a coal and phosphogypsum/ore mixture inlet is positioned in the middle of the dense-phase area, and a flue gas outlet is positioned at the top of the dilute-phase area.
The interior of the circulating fluidized bed reactor is divided into an air chamber, a dense-phase area and a dilute-phase area from bottom to top; the secondary air inlet is positioned at the upper part of the dense-phase area, and the circulating material inlet is positioned at the upper part of the dense-phase area.
3. The apparatus of claim 1, wherein the circulating fluidized bed reactor is provided with a lock hopper having a slag discharge port at the bottom thereof.
4. The apparatus as claimed in claim 1, wherein the first cyclone has a flue gas outlet connected to the second cyclone, and the lower return feeder is connected to the circulating material inlet of the circulating fluidized bed reactor and the material inlet of the first fluidized bed cooling device.
5. The apparatus as claimed in claim 1, wherein the primary fluidized bed cooling apparatus has a bottom provided with an air chamber, the air chamber is connected to the secondary air blower, and the material outlet is connected to the secondary fluidized bed cooling apparatus.
6. The apparatus of claim 1, wherein the flue gas outlet of the secondary cyclone is connected to the tertiary cyclone, and the material outlet is connected to the primary fluidized bed cooling unit.
7. The apparatus of claim 1, wherein the flue gas outlet of the tertiary cyclone is connected to a hemihydrate gypsum production plant and the material outlet is connected to a secondary fluidized bed cooling unit.
8. The device of claim 1, wherein a phosphogypsum feeding port is arranged at the top of the left side of the semi-hydrated gypsum production device, a four-stage cyclone separator is arranged at the top of the right side of the semi-hydrated gypsum production device, a flue gas outlet of the four-stage cyclone separator is connected with a bag-type dust collector, and a material outlet is connected with a semi-hydrated gypsum collector.
9. The device of claim 1, wherein the flue gas outlet of the bag-type dust collector is connected with an induced draft fan, and the material outlet is connected with the semi-hydrated gypsum collector.
10. The apparatus according to claim 1, comprising the steps of:
(1) coal particles are fed into the middle part of a dense-phase region of a circulating fluidized bed reactor through a coal hopper, the particle size of the coal is 0-5mm, primary air enters a hearth from an air chamber at the bottom of the hearth and reacts with the coal, the reaction temperature is between 800 ℃ and 900 ℃, secondary air enters the hearth from the upper part of the dense-phase region, and the lower region of the hearth is controlled to be a reducing atmosphere and the upper part of the hearth is controlled to be an oxidizing atmosphere through graded air distribution of the primary air and the secondary air. The phosphogypsum/tailing mixture is directly fed into the lower part of a hearth through a feeding device, and high-temperature reduction roasting is realized.
(2) The outlet at the upper part of the circulating fluidized bed reactor is provided with a primary cyclone separator, the separated high-temperature particles are directly returned to the roasting furnace through a loopseal material returning device to realize circulating roasting so as to improve the combustion efficiency of lignite and the roasting effect of raw materials, and part of particles are directly sent to a primary fluidized bed cooling device as finished products. The high-temperature flue gas after the first-stage separation enters a second-stage cyclone separator to separate the contained roasted finished product raw materials, and the separated particles are sent to a first-stage air fluidized bed cooling device. The hot air heated by the first-stage fluidized bed cooling device is directly sent into the circulating fluidized bed roasting furnace to be used as secondary air. And sending the cooled material into a secondary fluidized bed cooling device for cooling and then sending out as a product. The heated hot air is mixed with the high-temperature flue gas from the secondary cyclone separator for cooling before being sent to the tertiary cyclone separator.
(3) The mixed flue gas enters a three-stage cyclone separator for further separating the contained roasted products, and the separated materials are sent to a two-stage fluidized bed cooling device. And (3) the separated high-temperature flue gas enters a suspension bed semi-hydrated gypsum reaction device to be mixed with the fed phosphogypsum raw material, and the phosphogypsum raw material is heated to dry most of water contained in the phosphogypsum raw material to be separated out in the process of carrying phosphogypsum raw material particles to flow so as to form the semi-hydrated gypsum.
(4) The cooled flue gas carries the semi-hydrated gypsum particles to enter a four-stage cyclone separator, most of the produced semi-hydrated gypsum particles are separated, and the separated flue gas carries a small amount of semi-hydrated gypsum particles to enter a bag-type dust collector for further separation. And (4) discharging the dedusted flue gas from a chimney.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910898514.6A CN111377625A (en) | 2019-09-28 | 2019-09-28 | Comprehensive utilization process and device for reducing roasting of phosphogypsum circulating fluidized bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201910898514.6A CN111377625A (en) | 2019-09-28 | 2019-09-28 | Comprehensive utilization process and device for reducing roasting of phosphogypsum circulating fluidized bed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111377625A true CN111377625A (en) | 2020-07-07 |
Family
ID=71213460
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201910898514.6A Pending CN111377625A (en) | 2019-09-28 | 2019-09-28 | Comprehensive utilization process and device for reducing roasting of phosphogypsum circulating fluidized bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111377625A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113105130A (en) * | 2021-04-19 | 2021-07-13 | 河南省新思源电力科学研究院有限公司 | Circulating fluidized bed boiler structure |
| CN115180853A (en) * | 2022-06-24 | 2022-10-14 | 云南磷化集团有限公司 | Method for producing high-quality building gypsum through in-situ deep purification of phosphogypsum |
| CN115594155A (en) * | 2022-10-24 | 2023-01-13 | 中石化南京工程有限公司（Cn） | Device and method for producing sulfur dioxide-containing gas by decomposing phosphogypsum circulating fluidized bed |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201161187Y (en) * | 2008-01-08 | 2008-12-10 | 上海大学 | A compound circulating fluidized bed device for decomposing phosphogypsum |
| CN201261720Y (en) * | 2008-07-07 | 2009-06-24 | 昆明理工大学 | An integrated device for phosphogypsum decomposition circulating fluidized bed waste heat utilization |
| CN102442650A (en) * | 2011-10-18 | 2012-05-09 | 中国石油化工集团公司 | Method for producing sulfuric acid and co-producing calcium carbide by using phosphogypsum |
-
2019
- 2019-09-28 CN CN201910898514.6A patent/CN111377625A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201161187Y (en) * | 2008-01-08 | 2008-12-10 | 上海大学 | A compound circulating fluidized bed device for decomposing phosphogypsum |
| CN201261720Y (en) * | 2008-07-07 | 2009-06-24 | 昆明理工大学 | An integrated device for phosphogypsum decomposition circulating fluidized bed waste heat utilization |
| CN102442650A (en) * | 2011-10-18 | 2012-05-09 | 中国石油化工集团公司 | Method for producing sulfuric acid and co-producing calcium carbide by using phosphogypsum |
Non-Patent Citations (2)
| Title |
|---|
| 朱锡锋: "《生物质热解原理与技术》", 30 September 2006, 中国科学技术大学出版社 * |
| 李显海: "《工业锅炉节能改造技术与工程实例》", 31 May 2012, 金盾出版社 * |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113105130A (en) * | 2021-04-19 | 2021-07-13 | 河南省新思源电力科学研究院有限公司 | Circulating fluidized bed boiler structure |
| CN115180853A (en) * | 2022-06-24 | 2022-10-14 | 云南磷化集团有限公司 | Method for producing high-quality building gypsum through in-situ deep purification of phosphogypsum |
| CN115180853B (en) * | 2022-06-24 | 2023-09-08 | 云南磷化集团有限公司 | A method for in-situ deep purification of phosphogypsum to produce high-quality building gypsum |
| CN115594155A (en) * | 2022-10-24 | 2023-01-13 | 中石化南京工程有限公司（Cn） | Device and method for producing sulfur dioxide-containing gas by decomposing phosphogypsum circulating fluidized bed |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108753368B (en) | Circulating fluidized bed coal gasification system and method | |
| CN101294765B (en) | Low rank coal high temperature flue gas drying method and device | |
| CN102010728B (en) | Method for preparing semicoke, empyreumatic oil and coal gas by pyrolyzing coal | |
| CN103468930B (en) | Method and device for preparing nickel iron roasted ore by utilizing lateritic nickel ore | |
| CN103911179B (en) | Coal gasification method and device | |
| CN108239700B (en) | Coal-based fluidization reduction roasting system and roasting method thereof | |
| CN111377625A (en) | Comprehensive utilization process and device for reducing roasting of phosphogypsum circulating fluidized bed | |
| CN102585913A (en) | Coal gas, tar, semi-coke and steam poly-generation method based on fluidized bed pyrolysis technology | |
| CN102453489B (en) | Poly-generation process for pyrolyzing solid thermal carrier via low-rank coal vibration bed | |
| CN108130105B (en) | Metallurgical reduction coupling type coking and carbonization co-terminal coal pyrolysis process and system | |
| CN207552251U (en) | A kind of powdery semi-coke preparation facilities | |
| CN108164161B (en) | High-activity magnesium oxide suspension state calcination system and magnesium oxide preparation method | |
| CN204874405U (en) | Biological oily preparation system | |
| CN107652997B (en) | A kind of powdery semi-coke preparation device and process | |
| CN107686099A (en) | A kind of device and method that yellow phosphorus is produced using mid low grade phosphate rock stone | |
| CN102676193A (en) | Humidifying process for high-moisture charged coking coal | |
| CN108624751B (en) | Refractory iron ore fluidization heating low-temperature hydrogen reduction device | |
| CN105001895A (en) | Bio-oil preparation system | |
| CN107557039A (en) | A kind of hierarchical segmented formula coke breeze preparation system and technique | |
| CN201381333Y (en) | Iron-bearing material suspension two-stage fast reducing furnace | |
| CN117144078A (en) | System and method for reducing red mud to extract iron by biomass pyrolysis | |
| CN111453728B (en) | Raw coal carbonization and activation co-production process and system thereof | |
| CN203403141U (en) | Device for preparing ferronickel roasted ores by means of nickel laterite ores | |
| CN101215631A (en) | An iron ore fluidized bed magnetization roasting device | |
| CN115682732A (en) | Flexible and adjustable coal gangue suspension calcining production system and production method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20200707 |
|
| WD01 | Invention patent application deemed withdrawn after publication |