CN109628135B - Coke producing device and using method - Google Patents
Coke producing device and using method Download PDFInfo
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- CN109628135B CN109628135B CN201811504261.1A CN201811504261A CN109628135B CN 109628135 B CN109628135 B CN 109628135B CN 201811504261 A CN201811504261 A CN 201811504261A CN 109628135 B CN109628135 B CN 109628135B
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- 239000000571 coke Substances 0.000 title claims abstract description 199
- 238000000034 method Methods 0.000 title claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims abstract description 53
- 239000006260 foam Substances 0.000 claims abstract description 28
- 238000006482 condensation reaction Methods 0.000 claims abstract description 14
- 238000005336 cracking Methods 0.000 claims abstract description 12
- 238000005235 decoking Methods 0.000 claims description 37
- 238000004939 coking Methods 0.000 claims description 27
- 238000006243 chemical reaction Methods 0.000 claims description 23
- 238000005507 spraying Methods 0.000 claims description 11
- 239000002245 particle Substances 0.000 claims description 10
- 239000000428 dust Substances 0.000 claims description 9
- 230000005611 electricity Effects 0.000 claims description 5
- 239000011148 porous material Substances 0.000 claims description 5
- 230000003068 static effect Effects 0.000 claims description 5
- 239000007921 spray Substances 0.000 claims description 3
- 230000008901 benefit Effects 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 3
- 239000003921 oil Substances 0.000 description 66
- 239000007789 gas Substances 0.000 description 62
- 239000010410 layer Substances 0.000 description 50
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 22
- 238000000197 pyrolysis Methods 0.000 description 18
- 239000011280 coal tar Substances 0.000 description 14
- 238000005755 formation reaction Methods 0.000 description 13
- 230000015572 biosynthetic process Effects 0.000 description 12
- 239000000203 mixture Substances 0.000 description 12
- 238000010438 heat treatment Methods 0.000 description 11
- 239000003245 coal Substances 0.000 description 8
- 150000001875 compounds Chemical class 0.000 description 8
- 238000004458 analytical method Methods 0.000 description 7
- 239000003350 kerosene Substances 0.000 description 7
- 239000011269 tar Substances 0.000 description 7
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 6
- 238000001816 cooling Methods 0.000 description 6
- 239000002737 fuel gas Substances 0.000 description 6
- 238000009413 insulation Methods 0.000 description 6
- YNPNZTXNASCQKK-UHFFFAOYSA-N phenanthrene Chemical compound C1=CC=C2C3=CC=CC=C3C=CC2=C1 YNPNZTXNASCQKK-UHFFFAOYSA-N 0.000 description 6
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 5
- 150000002989 phenols Chemical class 0.000 description 5
- 238000004321 preservation Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 239000002028 Biomass Substances 0.000 description 4
- MWPLVEDNUUSJAV-UHFFFAOYSA-N anthracene Chemical compound C1=CC=CC2=CC3=CC=CC=C3C=C21 MWPLVEDNUUSJAV-UHFFFAOYSA-N 0.000 description 4
- 239000002283 diesel fuel Substances 0.000 description 4
- GVEPBJHOBDJJJI-UHFFFAOYSA-N fluoranthrene Natural products C1=CC(C2=CC=CC=C22)=C3C2=CC=CC3=C1 GVEPBJHOBDJJJI-UHFFFAOYSA-N 0.000 description 4
- 239000003208 petroleum Substances 0.000 description 4
- 239000004033 plastic Substances 0.000 description 4
- 229920003023 plastic Polymers 0.000 description 4
- BBEAQIROQSPTKN-UHFFFAOYSA-N pyrene Chemical compound C1=CC=C2C=CC3=CC=CC4=CC=C1C2=C43 BBEAQIROQSPTKN-UHFFFAOYSA-N 0.000 description 4
- 238000012360 testing method Methods 0.000 description 4
- 150000007513 acids Chemical class 0.000 description 3
- 150000001338 aliphatic hydrocarbons Chemical class 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 3
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 3
- 239000003250 coal slurry Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003502 gasoline Substances 0.000 description 3
- 229910052760 oxygen Inorganic materials 0.000 description 3
- 239000001301 oxygen Substances 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 238000007789 sealing Methods 0.000 description 3
- 239000002002 slurry Substances 0.000 description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 2
- YLQBMQCUIZJEEH-UHFFFAOYSA-N Furan Chemical compound C=1C=COC=1 YLQBMQCUIZJEEH-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
- 125000000217 alkyl group Chemical group 0.000 description 2
- 238000012512 characterization method Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- TXCDCPKCNAJMEE-UHFFFAOYSA-N dibenzofuran Chemical compound C1=CC=C2C3=CC=CC=C3OC2=C1 TXCDCPKCNAJMEE-UHFFFAOYSA-N 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000009826 distribution Methods 0.000 description 2
- 238000005485 electric heating Methods 0.000 description 2
- 238000000921 elemental analysis Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000000295 fuel oil Substances 0.000 description 2
- 238000002290 gas chromatography-mass spectrometry Methods 0.000 description 2
- 239000002010 green coke Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- -1 nitrogen-containing compound Chemical class 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000010791 quenching Methods 0.000 description 2
- 230000000171 quenching effect Effects 0.000 description 2
- 239000010959 steel Substances 0.000 description 2
- 229910052717 sulfur Inorganic materials 0.000 description 2
- 239000011593 sulfur Substances 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- FECNOIODIVNEKI-UHFFFAOYSA-N 2-[(2-aminobenzoyl)amino]benzoic acid Chemical class NC1=CC=CC=C1C(=O)NC1=CC=CC=C1C(O)=O FECNOIODIVNEKI-UHFFFAOYSA-N 0.000 description 1
- 239000004322 Butylated hydroxytoluene Substances 0.000 description 1
- NLZUEZXRPGMBCV-UHFFFAOYSA-N Butylhydroxytoluene Chemical compound CC1=CC(C(C)(C)C)=C(O)C(C(C)(C)C)=C1 NLZUEZXRPGMBCV-UHFFFAOYSA-N 0.000 description 1
- ZATLVVJBZQVOPK-UHFFFAOYSA-N C1=CC=CC2=CC=CC=C12.C=1(C(=CC=CC1)C)C.C1(=CC=CC=C1)C.C1=CC=CC=C1 Chemical compound C1=CC=CC2=CC=CC=C12.C=1(C(=CC=CC1)C)C.C1(=CC=CC=C1)C.C1=CC=CC=C1 ZATLVVJBZQVOPK-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005587 bubbling Effects 0.000 description 1
- 230000009172 bursting Effects 0.000 description 1
- 229940095259 butylated hydroxytoluene Drugs 0.000 description 1
- 235000010354 butylated hydroxytoluene Nutrition 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000004517 catalytic hydrocracking Methods 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000005553 drilling Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 229920006351 engineering plastic Polymers 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000003205 fragrance Substances 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 230000002209 hydrophobic effect Effects 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 150000002790 naphthalenes Chemical class 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000004014 plasticizer Substances 0.000 description 1
- 239000003755 preservative agent Substances 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- 239000011241 protective layer Substances 0.000 description 1
- 238000007790 scraping Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
- 239000012209 synthetic fiber Substances 0.000 description 1
- 229920002994 synthetic fiber Polymers 0.000 description 1
- 239000011800 void material Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
- C10G11/10—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with stationary catalyst bed
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Coke Industry (AREA)
Abstract
A coke producing device and a using method thereof comprise a coke producing tower, wherein the coke producing tower comprises a tower body, a coke removing opening is formed in the top of the tower body, and a hydraulic coke removing device is arranged at the coke removing opening; the bottom of the tower body is provided with a feed inlet and a coke outlet, and an automatic bottom cover machine is arranged at the coke outlet; the inside of the tower body is provided with a gas-phase plate layer for oil gas to pass through and a coke plate layer for separating oil-phase foam and gas-phase foam from top to bottom; a catalyst grid reactor is arranged above the gas-phase plate layer. The device of the utility model is operated intermittently, and has the advantages of low investment, simple process and mature technology. Under the proper temperature and pressure conditions in raw Jiao Dada, heavy residual oil or vacuum residual oil can undergo cracking and condensation reaction to obtain coke and oil gas, wherein the oil gas passing through the catalyst grid reactor is characterized and cooled to obtain oil component, the yield of BTXN is obviously increased, and the problem that the existing heavy residual oil or vacuum residual oil is excessive and can not be treated is solved.
Description
Technical Field
The utility model belongs to the technical field of coal chemical industry, and relates to a coking device and a using method thereof.
Background
The coal tar is a liquid byproduct obtained in the pyrolysis process of coal, and can be divided into high-temperature coal tar and low-temperature coal tar according to different pyrolysis temperatures, wherein the low-temperature coal tar has high utilization value. The low-temperature coal tar mainly contains aromatic hydrocarbon compounds, aliphatic hydrocarbon compounds, phenolic compounds and the like. Wherein the aromatic hydrocarbon compound contains naphthalene, anthracene, phenanthrene, pyrene and other fine chemicals with high added value; the aliphatic hydrocarbon compound is an important component of fuel oil such as gasoline, diesel oil and the like, and is an excellent raw material for preparing high-cetane-number diesel oil by hydrogenation; the phenolic compounds have wide application in the aspects of synthetic fibers, engineering plastics, pesticides, medicines, preservatives, plasticizers, fragrances, dye intermediates and the like. So how to efficiently, economically and environmentally separate coal tar is important at present.
Heavy coal tar is more complex than light oil, and most of heavy oil is discarded, which not only causes a great waste of resources, but also pollutes the environment. How to efficiently treat heavy coal tar is a necessary trend of development of the coal chemical industry nowadays. Heavy coal tar can produce a large amount of residual oil with poorer quality in the treatment process, and the traditional coking process and the hydrocracking process have difficulty in effectively processing and utilizing the residual oil.
Chinese patent CN108148613a describes a coke-oven preheating device, through being equipped with wheel carrier, pneumatic tank, electromagnetic heating case, pneumatic pump, heater wire, elevator pump pole, realized the lift homogeneous preheating of equipment, equipment is gone up and down for electromagnetic heating case through being equipped with pneumatic tank for pneumatic pump supply pressure control elevator pump pole, makes electromagnetic heating case can switch work at different altitudes, electromagnetic heating case is equipped with electromagnetic heating wire and carries out homogeneous preheating for the coke-oven, and equipment still makes equipment remove more convenient through being equipped with the wheel carrier, has made things convenient for the problem of the homogeneous preheating of coke-oven. However, this device is energy-consuming and inconvenient to install. In addition, because the device is operated continuously, the device can face large-scale maintenance operation in the driving process, so that the productivity can be reduced, and the production cost can be increased.
Chinese patent No. CN106190226a describes a coke making tower, which comprises a coke making tower body, an electric heating device, a decoking device, and a lifting device. The electric heating device is used for heating the raw coke tower body and the raw oil; the decoking device comprises a driving device arranged at the upper part of the top surface of the raw coke tower, a decoking end arranged in the raw coke tower and used for scraping coke, and a driving shaft used for driving the decoking end to horizontally rotate; the lifting device comprises a lifting speed reducer arranged at the bottom of the driving device and a guide rail mounting seat sleeved on the outer wall of the driving shaft, and a guide rail is arranged on the outer wall of the guide rail mounting seat. Compared with the prior art, the coke producing tower has the advantages of no pollution, thorough decoking and higher automation degree. However, the device has no heat preservation measure, and the tower body is deformed due to the quenching and the shock heating of the tower body.
Chinese patent application 201320370168.2 describes a coke drum preheating apparatus comprising two green coke drums. The utility model realizes the energy saving and consumption reduction of the coke making device, simultaneously stabilizes the material balance and the heat balance of the device system, reduces the periodic fluctuation of the device, shortens the preheating time of the coke making tower, improves the liquid yield of the device, saves the energy consumption of a pump, and breaks through the technical defects of intermittent production of the coke making device. However, the device has no clear heating mode, and only the fixed heating device is arranged on the tower body for heating, so that the problem of uneven heating easily occurs, and the device is inconvenient to mount and dismount.
Disclosure of Invention
In order to overcome the problems in the prior art, the utility model aims to provide a coke producing device and a using method thereof. The device is operated intermittently, and has the advantages of low investment, simple process and mature technology. Under the proper temperature and pressure conditions in raw Jiao Dada, heavy residual oil or vacuum residual oil (petroleum, plastic oil blend, biomass oil blend, coal tar, kerosene blend, kerosene slurry and the like) can undergo cracking and condensation reaction to obtain coke and oil gas (coked gasoline, coked diesel oil, coked wax oil and the like), wherein the oil gas passing through a catalyst mesh reactor is characterized and cooled to obtain oil component, and the oil component is obviously increased in BTXN yield. The new coke producing apparatus has obvious economic benefit, and is one ideal apparatus for processing heavy residual oil or vacuum residual oil.
In order to achieve the above purpose, the technical scheme adopted by the utility model is as follows:
a coke producing device comprises a coke producing tower, wherein the coke producing tower comprises a tower body, a coke removing opening is formed in the top of the tower body, and a hydraulic coke removing device is arranged at the coke removing opening; the bottom of the tower body is provided with a feed inlet and a coke outlet, and an automatic bottom cover machine is arranged at the coke outlet; the inside of the tower body is provided with a gas-phase plate layer for oil gas to pass through and a coke plate layer for separating oil-phase foam and gas-phase foam from top to bottom; a catalyst grid reactor is arranged above the gas-phase plate layer.
The utility model is further improved in that the catalyst mesh grid reactor comprises a shell, wherein a catalyst layer is arranged in the shell, and a clamping ring is arranged on the outer wall of the shell.
The utility model is further improved in that the top of the tower body is provided with a spraying opening and an oil gas outlet; and the spraying opening is positioned at one side of the hydraulic decoking device, and the oil gas outlet is positioned at the other side of the hydraulic decoking device.
The utility model is further improved in that the outer surface of the tower body is provided with a high-temperature fuel gas insulation sleeve.
The utility model is further improved in that the high-temperature gas heat-insulating sleeve and the tower body are arranged on the outer surface of the tower body through flanges, and the high-temperature gas heat-insulating sleeve adopts corrugated plates.
The utility model is further improved in that the tower body is provided with a skirt seat for supporting the tower body.
The utility model is further improved in that the tower body is a cylindrical pressure vessel which is vertically arranged, the tower body is 25m, and the tower body width is 7m.
The coke slab layer comprises a cylindrical plate body, seven round holes with the same size are formed in the cylindrical plate body, one round hole is formed in the center of the cylindrical plate body, the other six round holes are uniformly distributed around the round hole in the center, the outer walls of the 6 round holes are tangent to the inner wall of the tower body, and the diameter of each round hole is 1m;
the foam board layer comprises a cylindrical board body, fourteen round holes with the same size are formed in the cylindrical board body, the diameter of each round hole is 0.5m, four round holes are formed in the center of the cylindrical board body, every two round holes are arranged side by side, the other ten round holes are uniformly distributed around the four round holes in the center, and the outer walls of the ten round holes are tangent to the inner wall of the tower body;
the gas-phase plate layer comprises a cylindrical plate body, a plurality of round holes are formed in the cylindrical plate body, and the diameter of each round hole is smaller than 0.5m.
A further improvement of the utility model is that each of the coke slab, foam slab, and gas phase slab is fitted with a level gauge.
The application method of the coke producing device adopts a first coke producing tower and a second coke producing tower which are shared, and the two coke producing towers are connected with a feed valve through a four-way valve; spraying small dust particles capable of generating static electricity at a spraying opening at the top of the tower before carrying out coking reaction; the heavy residue or vacuum residue preheated to 550-650 ℃ enters a coking tower through a feed inlet, cracking and condensation reaction are carried out in the tower, coke generated by the condensation reaction stays in the tower and expands from the tower wall to the center, a feed channel is formed in the center, oil gas above a gas plate layer passes through a catalyst layer of a catalyst grid reactor, the active site of the catalyst is reached to react, and the oil gas passing through a pore canal of the catalyst layer is discharged and collected from an oil gas outlet; decoking by adopting a high-pressure hydraulic decoking method; when the first coking tower reacts with coking, the other second coking tower is in a coking removing stage; the first coke producing tower is used in decoking stage and the other second coke producing tower is used in reaction to produce coke.
Compared with the prior art, the utility model has the beneficial effects that: the device is characterized in that small dust particles (the particle size is about 5 mu m) which generate static electricity are sprayed at a spraying opening at the top of the tower before the coke formation reaction is carried out, the small dust particles have the function of increasing the surface tension of the inner plate layer of the coke formation tower, so that the coke generated in the coke formation tower is prevented from being adhered to the wall surface of the coke formation tower to be larger, and the generated coke can be well removed and collected.
In the coking reaction, the oil gas above the gas plate layer passes through the catalyst layer of the catalyst mesh-grid reactor to reach the active site of the catalyst for reaction, and the oil gas passing through the top of the catalyst pore canal is discharged and collected from the oil gas outlet. The oil obtained after the characterization cooling found a significant increase in BTXN yield.
The device of the utility model is operated intermittently, and has the advantages of low investment, simple process and mature technology. Under the proper temperature and pressure conditions in raw Jiao Dada, heavy residual oil or vacuum residual oil (petroleum, plastic oil blend, biomass oil blend, coal tar, kerosene blend, kerosene slurry and the like) can undergo cracking and condensation reaction to obtain coke and oil gas (coked gasoline, coked diesel oil, coked wax oil and the like), wherein the oil gas passing through a catalyst mesh reactor is characterized and cooled to obtain oil component, and the oil component is obviously increased in BTXN yield. The new coke producing apparatus has obvious economic benefit, and is one ideal apparatus for processing heavy residual oil or vacuum residual oil.
Drawings
FIG. 1 is a schematic view of a coke making tower structure;
FIG. 2 is a schematic diagram of a parallel structure of coke drums;
FIG. 3 is a schematic view of a decoking device;
FIG. 4 is a schematic view of the internal components of the coke making tower;
FIG. 5 is a schematic diagram of a catalyst mesh reactor;
FIG. 6 shows the results of the combined analysis of the phase chromatograph and the mass spectrometer of the example 1;
FIG. 7 shows the results of the content of each component in example 1;
FIG. 8 shows the BTXN content distribution under different catalyst conditions in example 1;
FIG. 9 is a result of the combined analysis of the phase chromatograph and the mass spectrometer of the example 2;
FIG. 10 shows the results of the content of each component in example 2;
FIG. 11 shows the BTXN content distribution under different catalyst conditions in example 2.
In the figure, 1, a spraying port; 2. a flange; 3. high-temperature fuel gas insulation sleeve; 4. a hydraulic decoking device; 5. decoking port; 6. an oil gas outlet; 7. a catalyst mesh reactor; 8. a level gauge; 9. a skirt; 10. automatic bottom cover machine; 11. a feed inlet; 12. a first coke drum; 13. a second green coke tower; 14. a four-way valve; 15. a feed valve; 16. a high pressure water pump; 17. high-pressure water gun; 18. a drill frame; 19. a drill rod; 20. a hydraulic coke cutter; 21. a chute; 22. coke; 23. a coke slab layer; 24. a foam board layer; 25. a gas panel layer; 26. a clasp; 27. a catalyst layer.
Detailed Description
The present utility model will be described in detail with reference to the accompanying drawings.
Referring to fig. 1, the novel coke producing device comprises a coke producing tower body, wherein a spraying opening 1, a flange 2, a high-temperature gas insulation sleeve 3, a hydraulic decoking device 4, a decoking device Jiao Kou 5, an oil gas outlet 6, a catalyst grid reactor 7, a level gauge 8, a skirt 9, an automatic bottom cover machine 10 and a feed inlet 11 are sequentially arranged on the coke producing tower body from top to bottom.
The coke producing tower body is a vertical cylindrical shell pressure container, the top of the coke producing tower body is provided with a spherical or elliptic decoking opening 5, and the lower part of the coke producing tower body is a tower made of cone thick boiler steel plates. Because the operation temperature of the raw coke tower is higher and the raw coke tower is under the severe operation conditions of quenching, high-pressure water impact and the like, the corrosion, swelling and deformation of the tower body, even the cracking of welding seams and the inclination of the tower body are easy to occur, and the raw coke tower body is made of 1m thick boiler steel plates. The tower body is set to be about 25m, the tower body is set to be about 7m, and two towers are generally required to be shared for operation, one tower is used for coking, and the other tower is used for coke discharging. One tower is in the decoking stage when the reaction is coking, and the other tower is in the decoking stage. I.e., when coke accumulates in a drum to a certain level (typically about 2/3 of the height of the drum).
Fig. 4 is a schematic view of the internal components of the coke making tower body, see fig. 4, and the interior of the coke making tower body mainly comprises three layers, namely a coke slab layer 23, a foam slab layer 24 and a gas phase slab layer 25 from bottom to top. Wherein coke slab layer 23 includes the cylinder plate body, has seted up seven round holes that the size is the same on the cylinder plate body, and a round hole has been seted up at the plate body center, and 6 other round holes evenly distributed are around the round hole that is located the center, and the outer wall of 6 round holes is tangent with the inner wall of the coke making tower body. (the diameter of the round hole is about 1 m) is a main place for coke generation.
The foam board layer 24 includes the cylinder plate body, has seted up fourteen round holes that the size is the same, (round hole diameter is about 0.5 m), and wherein, four round holes (two by two are square side by side) have been seted up at cylinder plate body center, and 10 other round holes evenly distributed are around four round holes that are located the center, and the outer wall and the coke formation tower body inner wall of 10 round holes are tangent. The coke generated by the condensation reaction stays in the tower and expands from the wall of the tower to the center, a material bursting channel is formed in the center, a main reaction area above the coke slab layer 23 is a foam slab layer 24 area, and the foam slab layer 24 is divided into oil phase foam and gas phase foam.
The gas-phase plate layer 25 comprises a cylindrical plate body, a plurality of round holes are formed in the plate body, the diameter of each round hole is smaller than 0.5m, along with the progress of cracking reaction, coal tar with high viscosity is continuously bubbled to form foam, and the formed bubbling is continuously broken to escape oil gas.
The spraying opening 1 on the coke making tower body is arranged at the left side of the top of the coke making tower body, so as to spray small dust particles (the particle size is about 5 mu m) for generating static electricity before the coke making reaction, and the small dust particles have the function of increasing the surface tension of a plate layer in the coke making tower body, avoiding the coke generated in the coke making tower from being adhered to the wall surface of the coke making tower, and ensuring that the generated coke can be well removed and collected.
The high-temperature gas heat-insulating sleeve 3 and the coking tower are arranged at two sides of the coking tower body through the coking tower flange, so that the high-temperature gas heat-insulating sleeve 3 and the coking tower are connected; before the flange is assembled, the flange is cleaned, sundries such as greasy dirt, dust, rust and the like are removed, and a sealing line is removed.
The high-temperature gas heat preservation sleeve 3 of the coke making tower is arranged on the outer surface of the coke making Jiao Dada body, which is a heat preservation sleeve for heat preservation of the tower body through gas combustion heat release. The high-temperature gas heat preservation sleeve 3 adopts corrugated plates, so that the rigidity of the outer protective layer is increased, and the problem of poor thermal expansion of the circumferential direction of the tower body is solved. The high-temperature gas heat-insulating sleeve has good heat insulation effect, high temperature resistance, low temperature resistance, various chemical corrosion resistance, fire resistance, flame retardance, water resistance, oil resistance and good hydrophobic property.
Referring to fig. 3, the hydraulic decoking device 4 of the coke making tower is installed at the top of the coke making tower body, the hydraulic decoking device 4 is an existing device, and the hydraulic decoking device 4 comprises a high-pressure water pump 16, a high-pressure water gun 17, a drilling frame 18, a drill rod 19, a hydraulic coke cutter 20, a chute 21 and coke 22 from top to bottom.
The high pressure hydraulic decoking process is used to decoke, and the coke producing tower with coalesced coke is first cooled with steam and then hydraulic decoked. The high-pressure water conveyed by the high-pressure water pump 16 passes through the high-pressure water gun 17, the drill frame 18 and the drill rod 19 to the nozzle of the hydraulic coke cutter 20, the high-pressure water sprayed out from the nozzle of the hydraulic coke cutter forms high-pressure jet flow, the coke is cut off by the strong impact force of the high-pressure jet flow, the coke and the water flow out from the tower bottom chute 21, and the drill rod 19 is continuously lifted and rotated until the coke 22 in the coke producing tower is completely removed.
Referring to fig. 5, the catalyst mesh reactor 7 is positioned above the gas plate layer and is connected with a coke tower flange. The catalyst mesh-grid reactor 7 comprises a shell, a catalyst layer 27 is arranged in the shell, a clamping ring 26 is arranged on the outer wall of the shell, the catalyst layer 27 is positioned at the middle part inside the catalyst mesh-grid reactor 7, and in order to enable oil gas above the gas phase plate layer 25 to pass through the catalyst layer 27 of the catalyst mesh-grid reactor 7, to reach the active site of the catalyst for reaction, and the tower top oil gas passing through a catalyst pore canal is discharged and collected from an oil gas outlet; the snap ring 26 is located on the outer wall of the catalyst mesh-grid reactor 7, so as to stably fix the catalyst mesh-grid reactor 7 in the coke-oven tower. The catalyst layer 27 is made of ZSM-5 and Al 2 O 3 USY, HY, etc.
The coke-generating tower decoking port 5 is positioned at the top of the coke-generating tower, the hydraulic decoking device 4 is arranged at the coke-generating tower decoking port 5, and the coke-generating tower decoking port 5 is connected with the hydraulic decoking device 4.
The oil gas outlet 6 of the coking tower is positioned on the right side of the tower top, the medium in the pipeline of the oil gas outlet of the tower top is generally gas phase, the pipe diameter is large, the pipeline is as short as possible, and the pipeline has certain flexibility.
The coke making tower level gauge 8 is arranged on the side face of the coke making tower body, the level gauge 8 is arranged on each of the three layers of the coke slab 23, the foam slab 24 and the gas phase slab 25, the heights of the coke slab 23, the foam slab 24 and the gas phase slab 25 are monitored, the positions of the foam slab 24 and the coke slab 25 in the coke making tower are observed, the coke position can be determined in time, process feeding is stopped, the utilization rate of the coke making tower is improved, the coking process operation is guided, and the energy consumption is saved.
The coke formation tower skirt 9 is positioned in a welding line area of a conical part at 2/3 of the position from top to bottom for connecting the tower body and is used for supporting the tower body.
The automatic bottom cover machine 10 of the coke making tower is positioned at the coke outlet of the tower bottom, the automatic bottom cover machine 10 is of an automatic opening and closing sealing structure, the structure strength is reliable, the sealing performance is good, the safety of operators is ensured, the labor intensity is greatly reduced, and the working efficiency of the device can be improved.
The raw coke tower feeding port 11 is positioned below the conical part of the bottom of the raw coke tower, heavy residual oil or vacuum residual oil petroleum, plastic oil blend, biomass oil blend, coal tar, kerosene blend, kerosene slurry and the like which are preheated to 550-650 ℃ are fed into the raw coke tower through the feeding port 11 to carry out raw coke reaction, and coke generated by the reaction is left in the tower.
Referring to fig. 2, a parallel structure schematic diagram of the coke producing towers includes a first coke producing tower 12, a second coke producing tower 13, a four-way valve 14 and a feed valve 15. It is generally desirable to share two columns, such as a first coke making column 12 for making coke and a second coke making column 13 for discharging coke. The first coke making tower 12 is in the decoking stage while the other second coke making tower 13 is in the reaction coke making. I.e., when coke accumulates in a drum to a certain level (typically about 2/3 of the height of the drum).
Fig. 5 is a schematic view of the catalyst mesh reactor 7, see fig. 5, above the gas panel layer 25, the catalyst mesh reactor 7 being fixed in position below the flange 2 by means of a snap ring 26. The catalyst layer 27 may be ZSM-5 or Al 2 O 3 Catalysts such as USY and HY.
Referring to fig. 2, a novel coke forming apparatus is used, in which a small electrostatic dust particle (particle size of about 5 μm) is sprayed at a spray nozzle at the top of a tower before a coke forming reaction is carried out, two towers are used in common, a four-way valve 14 is connected with a feed valve 15, and one tower is in a decoking stage when the coke is formed by the reaction. The first coke making tower 12 is in the decoking stage while the other second coke making tower 13 is in the reaction coke making. Heavy residual oil or vacuum residual oil (petroleum, plastic oil blend, biomass oil blend, coal tar, kerosene blend, coal slurry and the like) preheated at 550-650 ℃ enters a coke producing tower through a feed inlet 11, water is supplied to the outer surface of the coke producing tower through fuel gas, water vapor is generated and is insulated to the tower body through a high-temperature fuel gas insulation sleeve 3, cracking and condensation reaction are carried out under the condition of proper pressure and residence time in the tower, the cracking is an endothermic reaction, the condensation is an exothermic reaction, part of the cracked heat is provided by the condensation reaction except for the raw residual oil, coke generated by the condensation reaction stays in the tower and expands from the tower wall to the center, a feed channel is formed in the center, a main reaction area is formed above a coke slab layer 23, namely a foam slab layer 24, a gas slab layer 25 is formed above the foam slab layer, oil phase foam and gas phase foam are formed, the gas phase foam is arranged above the coke slab layer, the coking reaction temperature is generally 460-480 ℃, and the coke producing rate is higher, and the higher the reaction temperature is the higher. Coking reactions also occur in the coke layer, and gases resulting from the cracking overflow from the coke layer, with the void fraction of the coke layer being about: 30% -50%. The hot coke layer height is made higher than the cold coke height. As the feedstock continues to enter, the amount of coke produced increases, the coke layer height increases and the foam layer continuously rises. And the oil gas above the gas phase plate layer 25 passes through the catalyst layer 27 of the catalyst mesh grid reactor 7 to reach the active site of the catalyst to react, and the tower top oil gas passing through the catalyst pore canal is discharged and collected from the oil gas outlet 6. So that the yield of benzene-toluene-xylene-naphthalene (BTXN) is increased.
The oil obtained after the characterization cooling found a significant increase in BTXN yield. The coke drum that coalesces coke 22 is first cooled with steam and then subjected to hydraulic decoking by high pressure hydraulic decoking. The high-pressure water conveyed by the high-pressure water pump 16 passes through the high-pressure water gun 17, the drill frame 18 and the drill rod 19 to the nozzle of the hydraulic coke cutter 20, the high-pressure water sprayed out from the nozzle of the hydraulic coke cutter 20 forms high-pressure jet flow, the coke 22 is cut off by the strong impact force of the high-pressure jet flow, the high-pressure water and the water flow out from the chute 21 arranged at the bottom of the tower, and the drill rod 19 is continuously lifted and rotated until the coke in the coke making tower is completely removed.
The industrial analysis and elemental analysis of the coal samples used in examples 1 and 2 are shown in table 1.
TABLE 1 Industrial and elemental analysis of coal samples
* Differential subtraction
Example 1
The method comprises the steps of taking low-rank coal of a chemical plant in the north of Shaanxi as a raw material, carrying out industrial analysis and element analysis on the low-rank coal, preheating heavy residual oil of a certain amount of coal slurry to 550-650 ℃, entering a coking tower through a feed inlet for pyrolysis coking, maintaining the pressure of the coking tower at 0.1-0.15MPa, escaping oil gas from the top of the tower, collecting the oil gas, and remaining coke in the tower. The yields of coke, pyrolysis water and pyrolysis gas cooled tar were measured and calculated as shown in table 2. The tar obtained by cooling the pyrolysis gas after the test is subjected to gas chromatography-mass spectrometry and the content of the BTXN component is analyzed, and the results are shown in fig. 6, 7 and 8, and as can be seen from fig. 6 and 7, the tar obtained by cooling the pyrolysis gas after the test mainly comprises aromatic hydrocarbon, aliphatic hydrocarbon, acid compound, oxygen-containing compound, nitrogen-containing compound, sulfur-containing compound and unknown compound, and the contents are 42.02%, 20.94%, 32.01%, 4.79%, 0%, 0.12% and 0.12% respectively. Wherein the aromatic hydrocarbon mainly contains the alkene, anthracene, phenanthrene, substituted aromatic hydrocarbon and the like, the highest alkene content is 6.72%, and the acidic compound mainly contains phenolic compounds, and the content is 32.01%. As can be seen from fig. 8, by using different catalysts, it was found that the content of BTXN was increased, and the use of ZSM-5 catalyst was the best effect, resulting in a rich product.
TABLE 2 example 1 pyrolysis gas Cooling Tar, pyrolysis semicoke, yield of pyrolysis gas
Example 2
The method is characterized in that low-rank coal of a chemical plant in the north of Shaanxi is used as a raw material, industrial analysis and element analysis are shown in table 1, before coke formation, a dust generating static electricity is added into a coke formation tower, a certain amount of heavy residual oil of coal slurry is preheated to 550-650 ℃, enters the coke formation tower through a feed inlet 11 to carry out pyrolysis coke formation, two towers are used for sharing, a four-way valve is connected with a feed valve, and when one coke formation tower is used for coke formation, the other coke formation tower is used for coke discharge. A catalyst mesh reactor is added in a coke producing tower, water is supplied to the outer surface of the coke producing Jiao Dada by fuel gas, a steam-generating high-temperature fuel gas insulation sleeve is used for insulating the tower body, cracking and condensation reactions are carried out under the conditions of proper pressure and residence time in the tower, part of the cracking heat is provided by the condensation reaction besides raw residual oil, and coke generated by the condensation reaction stays in the tower. The yields of coke, pyrolysis water and pyrolysis gas cooled tar were measured and calculated as shown in table 3. The economic benefit is obvious, and the surplus residual oil is overcome without secondary treatment. The tar obtained by cooling the pyrolysis gas after the test is subjected to gas chromatography-mass spectrometry and the content of the BTXN component is analyzed, and the results are shown in fig. 9, 10 and 11, and as can be seen from fig. 9 and 10, the tar obtained by cooling the pyrolysis gas after the test mainly comprises an aromatic hydrocarbon compound, a fatty hydrocarbon compound, an acidic compound, an oxygen-containing compound, a nitrogen-containing compound, a sulfur-containing compound and an unknown compound, and the contents of the tar are 42.91%, 20.01%, 31.67%, 4.35%, 0%, 0.98% and 0.08%, respectively. The aromatic compounds have the highest content, and are mainly alkene, naphthalene, pyrene, phenanthrene, fluoranthene, alkyl substituted naphthalene and the like. The acidic compounds are mainly phenols, mainly phenol and alkyl substituted phenols thereof. And dibenzofuran, furan, alcohol, etc. in the oxygen-containing compound. A small amount of butylated hydroxytoluene was also found to be 0.12%. As can be seen from fig. 8, by using different catalysts, it was found that the content of BTXN was increased, and the use of ZSM-5 catalyst was the best effect, resulting in a rich product.
TABLE 3 example 2 pyrolysis gas Cooling Tar, pyrolysis semicoke, yield of pyrolysis gas
Claims (10)
1. The coke producing device is characterized by comprising a coke producing tower, wherein the coke producing tower comprises a tower body, a coke removing opening (5) is formed in the top of the tower body, and a hydraulic coke removing device (4) is arranged at the coke removing opening (5); the bottom of the tower body is provided with a feed inlet (11) and a coke outlet, and an automatic bottom cover machine (10) is arranged at the coke outlet; the inside of the tower body is provided with a gas-phase plate layer (25) for oil gas to pass through, a foam plate layer (24) for separating oil phase foam and gas phase foam and a coke plate layer (23) for generating coke from top to bottom; a catalyst grid reactor (7) is arranged above the gas-phase plate layer (25).
2. A coke making apparatus according to claim 1, wherein the catalyst mesh reactor (7) comprises a housing in which a catalyst layer (27) is provided and on the outer wall of which a snap ring (26) is provided.
3. A coke making apparatus according to claim 1, wherein the top of the tower body is provided with a spray opening (1) and an oil gas outlet (6); and the spraying opening (1) is positioned at one side of the hydraulic decoking device (4), and the oil gas outlet (6) is positioned at the other side of the hydraulic decoking device (4).
4. A coke making apparatus according to claim 1, wherein a high temperature gas heat retaining jacket (3) is provided on the outer surface of the tower.
5. The coke making apparatus as claimed in claim 4, wherein the high temperature gas heat-insulating jacket (3) and the tower body are installed on the outer surface of the tower body through flanges (2), and the high temperature gas heat-insulating jacket (3) is corrugated.
6. A coke making apparatus according to claim 1, wherein a skirt (9) for supporting the tower is provided on the tower.
7. A coke making apparatus according to claim 1, wherein the tower body is a vertically arranged cylindrical pressure vessel, the tower body is 25m, and the tower body is 7m wide.
8. A coke making apparatus according to claim 1, wherein the coke slab (23) comprises a cylindrical plate body, seven round holes with the same size are formed in the cylindrical plate body, wherein a round hole is formed in the center of the cylindrical plate body, six other round holes are uniformly distributed around the round hole in the center, the outer walls of the 6 round holes are tangent to the inner wall of the tower body, and the diameter of the round hole is 1m;
the foam board layer (24) comprises a cylindrical board body, fourteen round holes with the same size are formed in the cylindrical board body, the diameter of each round hole is 0.5m, four round holes are formed in the center of the cylindrical board body, every two round holes are arranged side by side, the other ten round holes are uniformly distributed around the four round holes in the center, and the outer walls of the ten round holes are tangent to the inner wall of the tower body;
the gas-phase plate layer (25) comprises a cylindrical plate body, a plurality of round holes are formed in the cylindrical plate body, and the diameter of each round hole is smaller than 0.5m.
9. A coke making apparatus according to claim 1, wherein each of the coke slab (23), the foam slab (24) and the gas phase slab (25) is provided with a level gauge (8).
10. A method of using a coke making apparatus as claimed in claim 3, wherein a first coke making tower is employed in common with a second coke making tower, the two coke making towers being connected to a feed valve (15) via a four-way valve (14); spraying small dust particles capable of generating static electricity on a spraying opening (1) at the top of the tower before carrying out coking reaction; heavy residual oil or vacuum residual oil preheated at 550-650 ℃ enters a coke making tower through a feed inlet (11), cracking and condensation reaction occurs in the tower, coke generated by the condensation reaction stays in the tower and expands from the tower wall to the center, a feed channel is formed in the center, oil gas above a gas plate layer (25) passes through a catalyst layer (27) of a catalyst mesh grid reactor (7) to reach an active site of the catalyst to react, and the oil gas passing through a pore canal of the catalyst layer (27) is discharged and collected from an oil gas outlet (6); decoking by adopting a high-pressure hydraulic decoking method; when the first coking tower reacts with coking, the other second coking tower is in a coking removing stage; the first coke producing tower is used in decoking stage and the other second coke producing tower is used in reaction to produce coke.
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4385980A (en) * | 1981-02-26 | 1983-05-31 | Conoco Inc. | Coal treating process |
| CN102899079A (en) * | 2011-07-27 | 2013-01-30 | 中国石油化工股份有限公司 | Delayed coking method |
| CN103087769A (en) * | 2011-11-02 | 2013-05-08 | 中国石油化工股份有限公司 | Delayed coking method |
| CN209210725U (en) * | 2018-12-10 | 2019-08-06 | 西北大学 | A kind of green coke device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US6919017B2 (en) * | 2002-04-11 | 2005-07-19 | Conocophillips Company | Separation process and apparatus for removal of particulate material from flash zone gas oil |
| CA2885717C (en) * | 2012-09-21 | 2018-10-16 | Lummus Technology Inc. | Coke drum additive injection |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4385980A (en) * | 1981-02-26 | 1983-05-31 | Conoco Inc. | Coal treating process |
| CN102899079A (en) * | 2011-07-27 | 2013-01-30 | 中国石油化工股份有限公司 | Delayed coking method |
| CN103087769A (en) * | 2011-11-02 | 2013-05-08 | 中国石油化工股份有限公司 | Delayed coking method |
| CN209210725U (en) * | 2018-12-10 | 2019-08-06 | 西北大学 | A kind of green coke device |
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| Title |
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| 浅谈焦炭塔设计要点;范京薇;;化工管理(29);237-239 * |
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