CN109385286B - Continuous pyrolysis device and method suitable for direct coal liquefaction residues - Google Patents
Continuous pyrolysis device and method suitable for direct coal liquefaction residues Download PDFInfo
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- CN109385286B CN109385286B CN201710659224.7A CN201710659224A CN109385286B CN 109385286 B CN109385286 B CN 109385286B CN 201710659224 A CN201710659224 A CN 201710659224A CN 109385286 B CN109385286 B CN 109385286B
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 107
- 239000003245 coal Substances 0.000 title claims abstract description 78
- 238000000034 method Methods 0.000 title claims abstract description 37
- 239000002184 metal Substances 0.000 claims abstract description 36
- 238000006243 chemical reaction Methods 0.000 claims abstract description 31
- 238000007599 discharging Methods 0.000 claims abstract description 14
- 230000008569 process Effects 0.000 claims description 16
- 239000002245 particle Substances 0.000 claims description 8
- 230000014759 maintenance of location Effects 0.000 claims description 4
- 239000007789 gas Substances 0.000 description 19
- 239000002994 raw material Substances 0.000 description 12
- 239000000047 product Substances 0.000 description 11
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 10
- 239000003546 flue gas Substances 0.000 description 10
- 239000000126 substance Substances 0.000 description 10
- 239000007787 solid Substances 0.000 description 9
- 239000003921 oil Substances 0.000 description 6
- 229910052799 carbon Inorganic materials 0.000 description 5
- 239000000571 coke Substances 0.000 description 5
- 238000000926 separation method Methods 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 239000010426 asphalt Substances 0.000 description 4
- 238000004939 coking Methods 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- 230000005540 biological transmission Effects 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 239000000295 fuel oil Substances 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
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- 238000004458 analytical method Methods 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
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- 230000008676 import Effects 0.000 description 2
- 229910052500 inorganic mineral Inorganic materials 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000005096 rolling process Methods 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000007605 air drying Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
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- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000007769 metal material Substances 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
Abstract
The invention relates to the field of continuous pyrolysis of direct coal liquefaction residues, in particular to a continuous pyrolysis device and method suitable for direct coal liquefaction residues. The device includes: the coal direct liquefaction pyrolysis device comprises a feeding unit, a pyrolysis unit and a discharging unit, wherein the pyrolysis unit comprises a rotary pyrolysis reactor (3) suitable for pyrolyzing coal direct liquefaction residues, and a metal rod capable of freely moving is arranged in a reaction cavity (302) of the rotary pyrolysis reactor (3). According to the continuous pyrolysis device, the metal rod capable of freely moving is ingeniously arranged in the reaction cavity, so that semicoke generated by pyrolysis of the direct coal liquefaction residues can be crushed on line under the impact of the metal rod capable of freely moving, and continuous pyrolysis of the direct coal liquefaction residues is facilitated.
Description
Technical Field
The invention relates to the field of continuous pyrolysis of direct coal liquefaction residues, in particular to a continuous pyrolysis device and method suitable for direct coal liquefaction residues.
Background
In the existing direct coal liquefaction process, the conversion rate of coal is less than 100%, and unreacted coal, inorganic mineral substances carried in the unreacted coal and part of catalyst exist in a solid state. They are mixed with liquefied oil and various liquefaction processes separate them from the liquefied oil by different solid-liquid separation methods. The unseparated liquefied oil and remaining solid matter, collectively referred to as liquefaction residue, are one of the by-products of the liquefaction process. The yield of liquefaction residue accounts for about 30% of the raw coal feed. Taking the demonstration project of direct liquefaction of Shenhua coal as an example, 5Mt oil products are produced annually, the first production line of the prior project is 1.08Mt oil products annually, wherein the coal for liquefaction is 2Mt/a, and the yield of the liquefaction residue is about 0.61 Mt/a.
The liquefaction residue contains no moisture, and has high fixed carbon content, high ash content and volatile matter content, and high sulfur content. The results of the extraction analysis show: the solid content of the residue is about 45 percent, the oil and asphalt content is relatively high, and the recovery value is certain. If the liquefied petroleum gas is not effectively and reasonably utilized, the economy of the liquefaction project is reduced, and the local environment is influenced to a certain extent.
Since the residue contains about half of the heavy oil and bitumen and is high in carbon content, thermal processing is the most common way to use. However, the semi-coke is melted into a liquid-solid mixed state in the pyrolysis process and has fluidity and adhesiveness, and the semi-coke is converted into a solid state along with the separation of volatile matters, so that the semi-coke finally obtained is solidified into a large block and cannot be smoothly discharged from the pyrolysis furnace. Thus, conventional pyrolysis methods such as fixed bed pyrolysis cannot be applied, and although there are documents that can be mixed with coal for pyrolysis to solve the problem of caking, the blending ratio is low. Continuous pyrolysis technology with residue as raw material has not yet emerged. At present, more extraction processes are researched, and the general process is complex, long in flow, large in investment and small in treatment capacity, and cannot meet all requirements.
CN201713483U discloses a continuous coking plant for coal liquefaction residues. The coke and pyrolysis gas outlet of the device are respectively communicated with the vacuum generating device, so that the coking furnace is in a vacuum state, coal liquefaction residues are heated and coked under vacuum, and a differential double-screw conveying device is arranged in the coking furnace in a matched mode, and the pyrolysis gas and the semicoke are convenient to discharge. However, the liquefied residues have strong adhesion in a molten state, the differential double-screw conveying device still has difficulty in achieving the purpose of crushing semicoke, the negative pressure operation cost is high, the requirement on the sealing property is high, and serious accidents are easily caused by gas leakage of the coking furnace.
Disclosure of Invention
The invention aims to provide a continuous pyrolysis device and a method thereof, which can crush semicoke on line and are suitable for direct coal liquefaction residues.
In order to accomplish the above objects, the present invention provides, in one aspect, a continuous pyrolysis apparatus for direct coal liquefaction residues, the apparatus comprising: the coal direct liquefaction pyrolysis device comprises a feeding unit, a pyrolysis unit and a discharging unit, wherein the pyrolysis unit comprises a rotary pyrolysis reactor suitable for pyrolyzing coal direct liquefaction residues, and a metal rod capable of freely moving is arranged in a reaction cavity of the rotary pyrolysis reactor.
The invention provides a continuous pyrolysis method of direct coal liquefaction residues, wherein the method adopts the device to carry out continuous pyrolysis on the direct coal liquefaction residues; the method comprises the following steps:
and continuously conveying the direct coal liquefaction residues into the rotary pyrolysis reactor through a feeding unit, pyrolyzing the direct coal liquefaction residues under the rotation of the reaction cavity and the free movement of a metal rod in the reaction cavity, and continuously discharging the obtained pyrolysis gas and semicoke from the discharging unit.
According to the continuous pyrolysis device, the metal rod capable of freely moving is ingeniously arranged in the reaction cavity, so that semicoke generated by pyrolysis of the direct coal liquefaction residues can be crushed on line under the impact of the metal rod capable of freely moving, and continuous pyrolysis of the direct coal liquefaction residues is facilitated.
Drawings
FIG. 1 is a schematic view of a continuous pyrolysis apparatus according to one embodiment of the present invention.
Fig. 2 is a schematic view of a continuous pyrolysis apparatus according to another embodiment of the present invention.
Fig. 3 is a schematic view of a feed port of direct coal liquefaction residue according to another embodiment of the present invention.
Description of the reference numerals
1-raw material bin; 2-feeder; 3-rotary pyrolysis reactor; 301-feed inlet; 302-reaction chamber; 303-heating the hearth; 304-outlet for pyrolysis gas; 305-semicoke outlet; 306-support means; 307-transmission; 4-feeding pump.
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
A first aspect of the present invention provides a continuous pyrolysis apparatus suitable for direct coal liquefaction residues, the apparatus comprising: the coal direct liquefaction pyrolysis device comprises a feeding unit, a pyrolysis unit and a discharging unit, wherein the pyrolysis unit comprises a rotary pyrolysis reactor 3 suitable for pyrolyzing coal direct liquefaction residues, and a metal rod capable of freely moving is arranged in a reaction cavity 302 of the rotary pyrolysis reactor 3.
According to the continuous pyrolysis device, the metal rods capable of moving freely are skillfully arranged in the reaction cavity, so that the metal rods can be driven to move freely when the reaction cavity rotates, collision and friction among the metal rods, the raw materials and products can be prevented from caking in the pyrolysis process, and large semi-coke can be crushed.
According to the invention, the size and number of the metal rods are preferably chosen such that the particle size of the resulting semicoke is below 30mm, for example from 2 to 25 mm. Thus, in a preferred embodiment of the invention, the diameter of the metal rod is 50 to 140mm, preferably 60 to 120 mm. Preferably, the length of the metal rod is shorter than the effective length of the reaction cavity 302 by 100-500mm, preferably 150-300mm, and more preferably 180-200 mm. Preferably, the metal rod occupies 10 to 35% of the volume of the reaction chamber 302, preferably 15 to 28%.
Wherein, the size of the reaction chamber 302 can be properly designed and adjusted according to the need, for example, the inner diameter of the reaction chamber 302 is 1-5m, preferably 1.5-4.5 m; the effective length of the reaction chamber 302 is in the range of 3-15m, preferably 4-10 m.
According to the present invention, the metal rod may be a rod material made of various metal materials capable of exhibiting the effects of the present invention, and a heat-resistant steel rod having a temperature of more than 850 ℃ is preferably used. The grade of steel material is 022Cr19Ni10, 42Cr9Si2, ZG40Cr17Si2, etc.
According to the present invention, the feeding unit may be appropriately adjusted according to the state of the raw material, such as the continuous pyrolysis apparatus shown in fig. 1, wherein the feeding unit comprises a raw material bin 1, a feeder 2 and a feeding port 301, and such an arrangement is more suitable for cold coal direct liquefaction residues, i.e. solid coal direct liquefaction residues, to enter the rotary pyrolysis reactor 3 through the raw material bin 1, the feeder 2 and the head feeding port 301 of the rotary pyrolysis reactor 3. The feeder 2 may be any feeder conventionally used in the art, such as a star feeder, a screw conveyor, etc.
As further shown in fig. 2, wherein the feeding unit comprises a feeding pump 4 and a feeding port 301, the arrangement is more suitable for the hot coal direct liquefaction residue, i.e. the fluid coal direct liquefaction residue, and the feeding pump 4 can be directly integrated with the coal direct liquefaction process.
According to the present invention, the discharging unit is used for discharging pyrolysis gas and semicoke, and the configuration thereof may be conventional in the art, for example, the discharging unit comprises a pyrolysis gas outlet 304 and a semicoke outlet 305 which are arranged at the tail end of the rotary pyrolysis reactor 3, the pyrolysis gas outlet 304 is arranged at the top of the tail end or the top of the head of the rotary pyrolysis reactor 3 (when the high-temperature flue gas is used as a heat carrier to provide a heat source and the raw material is required to be in countercurrent contact with the high-temperature flue gas), and the semicoke outlet 305 is arranged at the bottom of the tail end of the rotary pyrolysis reactor 3.
According to the invention, in order to facilitate raw material mixing and semicoke discharging, the reaction chamber 302 is preferably arranged obliquely, the included angle between the central line and the horizontal plane is 0-3 degrees, and the preferred rotating speed is 0.3-5 r/min.
In a preferred embodiment of the invention, the rotary pyrolysis reactor 3 is a rotary cylinder calciner or a rotary kiln.
Fig. 1 and 2 show the construction of a continuous pyrolysis apparatus in which the rotary pyrolysis reactor 3 is a rotary cylinder roasting furnace, and it can be seen that the rotary cylinder roasting furnace may include a heating furnace 303, a supporting device 306, a transmission device 307, and the like, in addition to the above-described components. Wherein, the heating hearth 303 is used for providing heat preservation and heating for the reaction cavity 302, the supporting device 306 is used for supporting the rotary cylinder roasting furnace, and the transmission device 307 is used for transmitting materials to the tail end of the reactor. Such a rotary drum roasting furnace may be electrically heated.
According to the present invention, the rotary pyrolysis reactor 3 may also be a rotary kiln, and the rotary kiln may also have all or part of the above components, and may also include the above components which are not described but are necessary for the rotary kiln, and the description of the present invention is omitted here.
Among them, it is worth mentioning that the rotary kiln generally heats the coal direct liquefaction residue using a solid heat carrier (e.g., hot semicoke products) or high-temperature flue gas (e.g., pyrolysis gas) to cause pyrolysis thereof. The components of the feed unit can be adjusted for the case of a solid heat carrier. As shown in fig. 3, two feed inlets may be provided at the head of the rotary pyrolysis reactor 3, one is a feed inlet for direct coal liquefaction residue, i.e., a raw material inlet shown in fig. 3, and the other is a solid heat carrier inlet, i.e., a semicoke inlet shown in fig. 3. As seen in the view A-A from the side A-A and the view B-B from the side B-B of FIG. 3, it can be seen that the raw material inlet end portion may be provided with a V-shaped distribution pipe, and a plurality of small holes (not shown) are uniformly arranged at the bottom of the distribution pipe. The inlet end of the char is provided with a V-shaped distributor like a bifurcated scoop as seen in a-a view from side a-a and C-C view from side C-C of fig. 3. Wherein, the direct liquefaction residue of coal gets into its distributing pipe by the raw materials import to from the vertical stream of a plurality of apertures in V-arrangement distributing pipe bottom to the semicoke import distributor on, be taken away by the semicoke and fall into the rotary kiln, make direct liquefaction residue of coal and semicoke homogeneous mixing. If high-temperature flue gas is used as a heat carrier, the pyrolysis raw material is preferably in countercurrent contact with the high-temperature flue gas. The high-temperature flue gas enters from the top of the tail end of the reactor, and the pyrolysis gas outlet is arranged at the top of the head of the reactor.
The invention provides a continuous pyrolysis method of direct coal liquefaction residues, wherein the method adopts the device to carry out continuous pyrolysis on the direct coal liquefaction residues; the method comprises the following steps:
the coal direct liquefaction residues are continuously sent to the rotary pyrolysis reactor 3 through a feeding unit, the coal direct liquefaction residues are pyrolyzed under the rotation of the reaction cavity 302 and the free movement of the metal rod in the reaction cavity, and the obtained pyrolysis gas and the semicoke are continuously discharged from the discharging unit.
The continuous pyrolysis apparatus is as described above and the present invention is not described herein in detail.
According to the invention, the coal direct liquefaction residue is a high-carbon, high-ash, high-sulfur substance, mainly composed of two parts, namely inorganic substances and organic substances, wherein the organic substances comprise liquefied heavy oil, asphalt substances and unconverted coal (referring to organic substances insoluble in tetrahydrofuran in the residue), and the inorganic substances (generally called ash) comprise minerals in the coal and additional catalysts. Wherein the liquefied heavy oil and asphalt substances in the organic substances account for about 40-60 wt% of the total amount of the liquefied residues, the unconverted coal accounts for about 20-40 wt% of the total amount of the liquefied residues, and the ash accounts for about 10-30 wt% of the total amount of the liquefied residues.
In the present invention, the direct coal liquefaction residue may be a liquefaction residue as a whole, or may be a mixture of a liquefaction residue and carbonaceous materials such as coal, pitch, and vacuum residue.
Wherein, when the coal direct liquefaction residue is a cold feed, the particle size thereof is preferably 30mm or less, for example, 2 to 25 mm. When the coal direct liquefaction residue is a hot feed, the temperature is preferably 280-320 ℃.
According to the invention, the direct coal liquefaction residues enter the reaction cavity 302 from the feeding hole 301 through the feeding unit, and the metal rods arranged in the reaction cavity 302 are driven to move freely (such as free rolling and collision) through the rotation of the reaction cavity 302, so that the direct coal liquefaction residues and the products thereof collide with the metal rods, and the purposes of preventing the residues from being aggregated and crushing large blocks of semicoke are achieved. Wherein the arrangement of the metal rod and the control of pyrolysis conditions enable the particle size of the semicoke obtained by pyrolysis to be less than or equal to 30 mm.
Preferably, the pyrolysis conditions include: the temperature is 550-680 ℃, and the retention time is 10-100 min. More preferably, the pyrolysis conditions include: the temperature is 600-650 ℃, and the retention time is 40-60 min.
According to the invention, the pyrolysis gas is continuously discharged from the outlet 304 and then can enter the oil-gas separation unit to be separated into tar and flue gas. After being continuously discharged from the outlet 305, the semicoke can enter a cooling unit to obtain a semicoke product. However, in the case of the rotary kiln, a part of the hot pyrolysis gas or the hot semicoke may be used as a heat source for the coal direct liquefaction residue, as described above, which is a conventional operation in the art, and the present invention is not particularly limited thereto.
The invention can realize the continuous feeding of the liquefaction residues and the continuous discharging of the semicoke, has the advantages of simple process, short flow, large treatment capacity, convenient implementation, small investment and the like, can be independently constructed and implemented, and can also realize the combination with the direct coal liquefaction process to remove the residue forming flow.
The present invention will be described in detail below by way of examples.
In the following examples:
the continuous pyrolysis apparatus shown in fig. 2 is used, that is, the continuous pyrolysis apparatus includes: a feed pump 4 and a rotary pyrolysis reactor 3, wherein the rotary pyrolysis reactor 3 is an electrically heated rotary drum roasting furnace comprising a feed inlet 301, a reaction chamber 302 (drum), a heated hearth 303 outside the drum, a pyrolysis gas outlet 304 at the tail and a semicoke outlet 305, wherein the rotary drum roasting furnace is supported by a support 306 and is provided with a transmission 307 to transmit material. Wherein, the inner diameter of the reaction cavity 302 is 1.8m, the length is 4m, the reaction cavity is arranged in an inclined way, and the included angle between the central line and the horizontal plane is 0.5 degree. The rotary cylinder roasting furnace is provided with metal rods capable of freely moving (such as freely rolling and colliding) in the furnace cylinder, wherein the metal rods are made of ZG40Cr17Si2, the diameter of the metal rods is 85mm, the length of the metal rods is 3.8m, and the number of the metal rods is 120.
The analysis of the coal direct liquefaction residue samples is shown in table 1 below:
TABLE 1
Note: the unit of the content of each component in the table is weight%; madRepresents: moisture; a. theadRepresents: ash content; vadRepresents: volatilizing; FCadRepresents: fixing carbon; cdRepresents: carbon; hdRepresents: hydrogen; n is a radical ofdRepresents: nitrogen; sdRepresents: sulfur; o isdRepresents: oxygen; subscript ad represents an air drying base and subscript d represents a drying base, as follows.
Example 1
This example is for explaining the continuous pyrolysis apparatus for direct coal liquefaction residue and the method thereof according to the present invention.
The continuous pyrolysis device shown in FIG. 2 is adopted, coal direct liquefaction residues (with the temperature of 310 ℃) are pumped to a feed port 301 through a feed pump 4 at the flow rate of 1000kg/h and enter a rotary cylinder roasting furnace, the coal direct liquefaction residues are continuously pyrolyzed (the furnace body rotation speed is 0.9r/min and the retention time is 60min) at the temperature of 650 ℃ under the rotation of a furnace cylinder of the rotary cylinder roasting furnace and the free movement of a metal rod in the rotary cylinder roasting furnace, pyrolysis gas and hot semicoke are obtained, the pyrolysis gas is discharged through a pyrolysis gas outlet 304 and enters an oil-gas separation unit for separation, tar and smoke are obtained, and the hot semicoke enters a cooling unit from a semicoke outlet for cooling, so that a semicoke product is obtained.
After continuous operation for 10 hours, the total coal direct liquefaction residue is 10000kg, the yield of the obtained semicoke product is 8020kg, the total yield of tar and water is 1150kg, the yield of flue gas is 830kg, and the particle size of the semicoke obtained in the process is 0-30 mm.
Example 2
This example is for explaining the continuous pyrolysis apparatus for direct coal liquefaction residue and the method thereof according to the present invention.
The process of example 1 was followed, except that the rotary drum roaster was operated at a speed of 1.4r/min and a residence time of 39min, and the process was otherwise the same as in example 1.
After continuous operation for 10 hours, the total coal direct liquefaction residue is 10000kg, the yield of the obtained semicoke product is 8124kg, the total yield of tar and water is 1064kg, the yield of flue gas is 812kg, and the particle size of the semicoke obtained in the process is 0-30 mm.
Comparative example 1
According to the method of example 1, except that no freely movable metal bars were placed in the shaft of the rotary drum roasting furnace, the operation had to be stopped after 2h of operation due to caking of the semicoke.
2000kg of total coal direct liquefaction residues, 1732kg of obtained semicoke product yield, 127kg of total yield of tar and water and 141kg of smoke yield, wherein the semicoke obtained in the process is large and larger than 150 mm.
Comparative example 2
According to the method described in example 1, except that freely movable metal balls with a diameter of 85mm were placed in the shaft of the rotary cylinder roasting furnace, the charging volume was 30% of the furnace volume. Because the residue has strong adhesion in the pyrolysis process, a plurality of metal balls are adhered together to form a large cluster, normal discharge cannot be realized, and the shutdown treatment has to be carried out after the operation for 3 hours.
3000kg of total coal direct liquefaction residues are obtained, the yield of the obtained semicoke product is 2546kg, the total yield of tar and water is 235kg, the yield of flue gas is 219kg, and the size of the semicoke obtained in the process is larger than 150 mm.
The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.
Claims (9)
1. A continuous pyrolysis apparatus for direct coal liquefaction residues, the apparatus comprising: the coal direct liquefaction pyrolysis device comprises a feeding unit, a pyrolysis unit and a discharging unit, wherein the pyrolysis unit comprises a rotary pyrolysis reactor (3) suitable for pyrolyzing coal direct liquefaction residues, and a metal rod capable of freely moving is arranged in a reaction cavity (302) of the rotary pyrolysis reactor (3);
the metal rod accounts for 15-28% of the volume of the reaction cavity (302); the length of the metal rod is shorter than the effective length of the reaction cavity (302) by 180-200 mm.
2. The device of claim 1, wherein the diameter of the metal rod is 50-140 mm.
3. The device according to claim 1 or 2, wherein the diameter of the metal rod is 60-120 mm.
4. The apparatus according to claim 1 or 2, wherein the discharge unit comprises a pyrolysis gas outlet (304) and a char outlet (305) arranged at the tail end of the rotary pyrolysis reactor (3), the pyrolysis gas outlet (304) being arranged at the top of the tail end or the top of the head of the rotary pyrolysis reactor (3), and the char outlet (305) being arranged at the bottom of the tail end of the rotary pyrolysis reactor (3).
5. The apparatus according to claim 1 or 2, wherein the size and number of the metal rods are selected such that the particle size of the char obtained from pyrolysis is below 30 mm.
6. A continuous pyrolysis method of direct coal liquefaction residues, wherein the method employs the apparatus of any one of claims 1 to 5 to perform continuous pyrolysis of direct coal liquefaction residues; the method comprises the following steps:
and continuously conveying the direct coal liquefaction residues into the rotary pyrolysis reactor (3) through a feeding unit, pyrolyzing the direct coal liquefaction residues under the rotation of the reaction cavity (302) and the free movement of a metal rod in the reaction cavity, and continuously discharging the obtained pyrolysis gas and semicoke from the discharging unit.
7. The method of claim 6, wherein the coal direct liquefaction residue has a particle size of 30mm or less when the coal direct liquefaction residue is a cold feed;
when the coal direct liquefaction residue is a hot feed, the temperature is 280-320 ℃.
8. The method of claim 6, wherein the pyrolysis conditions comprise: the temperature is 550-680 ℃, and the retention time is 10-100 min.
9. The process according to any one of claims 6 to 8, wherein the semicoke obtained by pyrolysis has a particle size of 30mm or less.
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| CN102757805A (en) * | 2012-06-08 | 2012-10-31 | 北京国电龙源环保工程有限公司 | Low-temperature dry distillation equipment and method of low-rank coal and oil shale and petroleum residue |
| CN205740885U (en) * | 2016-05-19 | 2016-11-30 | 湖南万容科技股份有限公司 | A kind of rotary kiln heat conduction coke cleaning pearl circulating device |
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| US4526679A (en) * | 1983-09-02 | 1985-07-02 | Texaco Inc. | Removal of low melting particles from unground coal liquefaction residue |
| CN101760220A (en) * | 2010-01-12 | 2010-06-30 | 肇庆市顺鑫煤化工科技有限公司 | Method for continuously coking coal liquefaction residuals and equipment thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102757805A (en) * | 2012-06-08 | 2012-10-31 | 北京国电龙源环保工程有限公司 | Low-temperature dry distillation equipment and method of low-rank coal and oil shale and petroleum residue |
| CN205740885U (en) * | 2016-05-19 | 2016-11-30 | 湖南万容科技股份有限公司 | A kind of rotary kiln heat conduction coke cleaning pearl circulating device |
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Address after: 100011 Beijing Dongcheng District, West Binhe Road, No. 22 Patentee after: CHINA ENERGY INVESTMENT Corp.,Ltd. Patentee after: Beijing low carbon clean energy research institute Address before: 100011 Shenhua building, 22 West Binhe Road, Dongcheng District, Beijing Patentee before: SHENHUA GROUP Corp.,Ltd. Patentee before: Beijing low carbon clean energy research institute |