CN116146987B

CN116146987B - Device and method for incinerating and disposing oil residue gasified filter cake

Info

Publication number: CN116146987B
Application number: CN202310423005.4A
Authority: CN
Inventors: 常涛; 雷祖磊; 赵琛杰; 张相; 何春晓
Original assignee: Pyneo Co ltd
Current assignee: Pyneo Co ltd
Priority date: 2023-04-20
Filing date: 2023-04-20
Publication date: 2023-08-01
Anticipated expiration: 2043-04-20
Also published as: CN116146987A

Abstract

The utility model relates to a chemical industry mud burns and handles technical field, concretely relates to burn device and method of handling gasification filter cake, the device is including the drying unit that connects gradually and carry the separation unit, carry the separation unit again respectively with lean carbon burn the unit and rich carbon burn the unit and be connected, gasification filter cake is the desiccation filter cake through the drying unit drying, later is carried the separation unit and is selected separately into rich carbon sediment and lean carbon sediment, rich carbon sediment send into rich carbon and burn the unit and burn the high temperature, lean carbon sediment then send into lean carbon and burn the unit and burn the flameless combustion. According to the method, the multi-hearth furnace is coupled with the sectional combustion, the dried filter cake is subjected to preliminary screening through the gravity separator, so that different incineration conditions of carbon deficiency and carbon enrichment are met, and reduction, harmlessness and recycling of the gasified filter cake are realized.

Description

Device and method for incinerating and disposing oil residue gasified filter cake

Technical Field

The application relates to the technical field of chemical sludge incineration disposal, in particular to a device and a method for incinerating and disposing oil residue gasification filter cakes.

Background

In the petrochemical industry, oil residue gasification is an important process device, and a Shell gasifier developed by Holland Shell is generally adopted for oil residue gasification. The process can be used for treating waste oil residue, liquid hydrocarbon, phenol tar and other wastes in a refinery, and hydrogen and carbon monoxide are generated through non-catalytic partial oxidation. The gasification of the oil residue generates a large amount of gasification filter cakes, and the components of the gasification filter cakes are as follows: 70-80wt% of water; the content of the received base carbon is 10-20%; 2-5% of base ash is received; 2-5% of base molybdenum is received; 0-2% of base nickel is received; and 0-2% of vanadium is received. It is known that the filter cake is chemical sludge with high water content and contains a certain amount of carbon-containing organic matters and trace amounts of metallic elements such as molybdenum, nickel, vanadium and the like.

According to the national hazardous waste directory, the gasified filter cake belongs to hazardous waste, and the classification number is HW08 code 251-011-08. The common disposal method of the gasification filter cake is to use a multi-hearth furnace for incineration to make harmless and reduce, and meanwhile, the molybdenum, the nickel and the vanadium are calcined and recovered in the form of metal oxides. However, firing temperature is an important parameter in the operation of a multiple hearth furnace. The melting points of metal oxides, such as molybdenum trioxide (melting point 795 ℃) and vanadium pentoxide (melting point 690 ℃) are relatively low, and because the multi-hearth furnace is a moving bed, mass transfer is poor, temperature distribution in the furnace is uneven and difficult to control, the temperature of a local area in the furnace easily exceeds the melting point of the metal oxides, so that furnace burden is hardened, rapid abrasion of parts of the multi-hearth furnace is further caused, and the roasting effect and stable operation of the system are finally influenced.

Disclosure of Invention

Aiming at the characteristics of high water content of the gasified filter cake, low melting point of incineration residual metal oxide and high added value, the application provides a device and a method for incinerating and disposing the gasified filter cake, and the device and the method can realize reduction, harmlessness and recycling of the gasified filter cake.

In one aspect, the application discloses a device for incinerating and disposing a gasified filter cake, which comprises a drying unit 100 and a conveying and sorting unit 200 which are sequentially connected, wherein the conveying and sorting unit 200 is further respectively connected with a carbon-lean incineration unit 300 and a carbon-rich incineration unit 400, and the conveying and sorting unit 200 comprises a first material returning device 21, an ash conveying device 22 and a gravity separator 23 which are sequentially connected; the ash conveying device 22 comprises a gas inlet 222, a contraction section 223, a throat section 224, a diffusion section 225 and an ash discharge hole 226 from left to right, and an ash feed inlet 221 is formed in the side wall of the throat section 224 and is connected with the first material returning device 21; the gravity separator 23 comprises a separator separation section 232 which is transversely arranged, a carbon-poor ash bucket 234 is arranged at the bottom of the gravity separator and near the feed inlet of the gravity separator, and a carbon-rich ash bucket 235 is arranged at the bottom of the gravity separator and near the air outlet of the gravity separator; the carbon-rich incineration unit 400 comprises a cyclone incinerator 4, an incineration chamber 41 and a cooling chamber 42, wherein the cyclone incinerator 4 is connected by a connecting section 416, an ash conveying device 22 is further arranged between the carbon-rich ash hopper 235 and the incineration chamber 41, the incineration chamber 41 comprises an incineration chamber feeding section 413, a cyclone furnace conveying section 411 and a cyclone furnace combustion section 412 from top to bottom, and the incineration chamber feeding section 413 comprises a carbon-rich slag conveying channel 4131 and a residual flue gas conveying channel 4132 which are coaxially arranged; the carbon-lean incineration unit 300 comprises a fluidized bed flameless combustion furnace 3, and an ash conveying device 22 is also arranged between the carbon-lean ash bucket 234 and the fluidized bed flameless combustion furnace 3.

In particular, the bottoms of the incineration chamber 41 and the cooling chamber 42 are protruded downwards from the edge to the center, the connecting section 416 is respectively communicated with the lower parts of the side walls of the incineration chamber 41 and the cooling chamber 42, and the slag catching pipe 417 is arranged in the connecting section 416.

In particular, the lower ends of the carbon-rich slag conveying channel 4131 and the residual flue gas conveying channel 4132 are provided with swirl plates 4133, an incineration chamber air inlet 414 is further formed in the upper portion of the side wall of the incineration chamber 41, the upper space of the incineration chamber air inlet 414 is a cyclone furnace conveying section 411, and the lower space is a cyclone furnace combustion section 412.

Specifically, the cooling chamber 42 includes a cooling chamber cylinder 422, an ash capturing tube 426, and a cyclone flue gas outlet 427, the cyclone flue gas outlet 427 is located at the top of the cooling chamber 42, the ash capturing tube 426 is disposed at the upper portion of the cooling chamber cylinder 422 and near the bottom end of the cyclone flue gas outlet 427, the cooling chamber cylinder 422 is in a square structure, a flame folding angle 424 is disposed at the lower portion of the side wall opposite to the connecting section 416, a cooling chamber air inlet 423 is disposed above the corner of the flame folding angle 424, and a cooling chamber wet slag inlet 425 is disposed at the upper portion of the cooling chamber cylinder 422 and below the ash capturing tube 426.

Specifically, the bottom of the incineration chamber 41 and the cooling chamber 42 have an inclination angle of 2 ° -10 ° with respect to the horizontal plane, and the central low points of the bottom of the incineration chamber 41 and the cooling chamber 42 are respectively provided with a slag discharge port 415 and a cooling chamber ash discharge port 421, the slag discharge port 415 is connected with the slag cooler 43, and the cooling chamber ash discharge port 421 is connected with the ash cooler 5.

Specifically, the fluidized bed flameless combustion furnace 3 is connected with two stages of cyclone separators, an ash discharge port of each cyclone separator is connected with an ash cooler, the fluidized bed flameless combustion furnace 3 comprises an air chamber 31, an air distribution plate 32, a fluidized bed combustion chamber 33 and a combustion chamber flue gas outlet 34 from bottom to top, the combustion chamber flue gas outlet 34 is connected with a first cyclone separator 301, an air discharge port of the first cyclone separator 301 is connected with a second cyclone separator 302, an ash discharge port of the first cyclone separator 301 is sequentially connected with the ash cooler 5 and the second material return device 6, a second material return pipe 62 of the second material return device 6 is connected with the lower part of the side wall of the fluidized bed combustion chamber 33, an ash discharge port 226 of an ash conveying device 22 arranged between the lean carbon ash hopper 234 and the fluidized bed flameless combustion furnace 3 is also connected with the lower part of the side wall of the fluidized bed combustion chamber 33, the connection position of the ash discharge port 226 and the fluidized bed combustion chamber 33 is higher than the connection position of the second material return pipe 62 and the fluidized bed combustion chamber 33, the high temperature wind generating device 7 is connected with the temperature equalizer 8 and the temperature equalizer 31, and the temperature equalizer 8 is connected with the temperature equalizer 3.

Specifically, the ash cooler 5 is cylindrical, and has two tapered ends, and includes a feeding zone 51, an upper cooling zone 52, an intermediate zone 53, a lower cooling zone 54, and a discharging zone 55 from top to bottom, wherein the inner spaces of the upper cooling zone 52 and the lower cooling zone 54 are respectively provided with a water-cooled wall heat exchanger 57, the intermediate zone 53 is hollow, and the outer side of the outer shell of the intermediate zone 53 is provided with a communicating pipe 575 connected with the upper water-cooled wall heat exchanger 57 and the lower water-cooled wall heat exchanger 57; the water wall heat exchanger 57 comprises a film water wall 573 which is vertically arranged, and the vertical projections of the film water wall 573 of the upper water wall heat exchanger 57 and the lower water wall heat exchanger 57 are not overlapped.

In particular, the water-cooled wall heat exchanger 57 comprises a lower header 572, a membrane water-cooled wall 573 and an upper header 574 which are connected in sequence from bottom to top; the membrane wall 573 of the upper and lower water wall heat exchangers 57 is vertically angled by 10 ° -40 °.

On the other hand, the method for incinerating and disposing the gasified filter cake is that the gasified filter cake is dried to be a dried filter cake with the temperature of 150-350 ℃ and simultaneously generates smoke with the temperature of 150-350 ℃, and the dried filter cake is gravity separated into carbon-rich slag and carbon-lean slag under the transportation of the smoke; the carbon-rich slag enters from the top of the incineration chamber of the cyclone incinerator under the transportation of the flue gas, the carbon-rich slag and the transportation flue gas are spirally downward and are mixed with the introduced air for combustion, liquid slag generated by combustion is discharged from the bottom of the incineration chamber, the liquid slag is changed into water-containing wet slag through direct contact cooling, the flue gas generated by the incineration chamber enters into a cooling chamber after slag capturing, the cooling chamber exchanges heat with the introduced air and the water-containing wet slag in sequence, high-temperature ash slag falling after the flue gas exchanges heat is discharged from the bottom of the cooling chamber, and the low-temperature dry slag product G2 is obtained after heat exchange cooling; the lean carbon slag enters the fluidized bed flameless combustion furnace through the delivery of the flue gas, the lean carbon slag and high-temperature low-oxygen wind are burnt in the fluidized bed flameless combustion furnace, the burnt flue gas sequentially enters the two-stage cyclone separator, the large-grain-size product T1 is separated under the action of the first-stage cyclone separator, and the product T1 is returned to the lower part of the fluidized bed flameless combustion furnace after heat exchange and temperature reduction and is mixed with the lean carbon slag.

Specifically, the combustion temperature of the carbon-rich slag is controlled to be 850-1300 ℃, the smoke passing through the slag capturing enters the folding flame angle of the cooling chamber to be turned, and then is cooled by the air and the water-containing wet slag which are sequentially introduced, the temperature of the high-temperature ash falling after the smoke exchanges heat is 500-650 ℃, and then enters the ash cooler to exchange heat and cool into a low-temperature dry slag product with the temperature of 50-80 ℃. .

On the basis of the common sense in the art, the above preferred conditions can be arbitrarily combined to obtain the preferred examples of the application.

The technical scheme has the following advantages or beneficial effects: the reduction, harmlessness and recycling of the gasification filter cake are realized by coupling the multi-hearth furnace and the sectional combustion; through the special structural design of the ash cooler, the dry slag product is ensured to be cooled to the required temperature; primarily screening the dried filter cake through a gravity separator to meet different incineration conditions; the ash conveying device solves the problem of high-speed uniform conveying of the smoke-slag mixture; the safe operation of the feeding channel is protected through reasonable arrangement of the cyclone furnace conveying section and the cyclone furnace combustion section; the cooling chamber is used for solving the problems of energy utilization of the liquid slag carrying smoke and collection of metal oxide products; the optimal utilization of energy and substances is realized through the deep coupling linkage among the system devices.

Drawings

FIG. 1 is a schematic and simplified flow chart of the incineration disposal of the gasified filter cake of the present application.

Fig. 2 is a schematic diagram of the structure of the drying unit of the present application.

Fig. 3 is a schematic flow diagram of a transport sorting unit of the present application.

Fig. 4 is a schematic structural view of the ash conveyor of the present application.

Fig. 5 is a schematic view of the gravity separator structure of the present application.

Fig. 6 is a schematic structural diagram of the carbon-rich incineration unit of the present application.

FIG. 7 is a schematic top view of the incinerator feed section of the present application.

FIG. 8 is a schematic cross-sectional view of the feed section of the incineration chamber of the present application.

FIG. 9 is a schematic view of the structure of the bottom of the cyclone incinerator of the present application.

FIG. 10 is a schematic diagram of the structure and flow of the carbon-lean burn unit of the present application.

Fig. 11 is a schematic diagram of the connection of the drying unit, the transport sorting unit and the carbon-lean burn unit of the present application.

Fig. 12 is a schematic diagram of the connection of the drying unit, the transport sorting unit and the carbon-rich incineration unit of the present application.

FIG. 13 is a schematic view of the construction of the ash cooler of the present application.

FIG. 14 is a schematic top view of an upper cooling zone of the ash cooler of the present application.

FIG. 15 is a schematic bottom view of a lower cooling zone of the ash cooler of this application.

FIG. 16 is a schematic view of a long section membrane wall structure of an ash cooler of the present application.

FIG. 17 is a schematic view of a short section membrane wall structure of an ash cooler of the present application.

FIG. 18 is a schematic top view of a long section membrane water wall of the ash cooler of the present application.

FIG. 19 is a schematic top view of a short section membrane water wall of the ash cooler of the present application.

FIG. 20 is a schematic top view of a long section membrane water wall in the upper and lower cooling zones of the ash cooler of this application.

Detailed Description

The technical solutions in the embodiments of the present application are clearly and completely described below with reference to the drawings of the present application. It is apparent that the described embodiments are only some of the embodiments of the present application and are intended to be used to explain the inventive concept. All other embodiments, which can be made by those skilled in the art based on the embodiments of the present application without making any inventive effort, are intended to be within the scope of the present application.

Referring to fig. 1, one embodiment of the present application proposes an apparatus for incinerating a gasification cake, which includes a drying unit 100, a transport sorting unit 200, a carbon-lean incineration unit 300, and a carbon-rich incineration unit 400, wherein the drying unit 100 is connected to the transport sorting unit 200, and further, the transport sorting unit 200 is connected to the carbon-lean incineration unit 300 and the carbon-rich incineration unit 400, respectively.

Referring to fig. 2, one embodiment of the present application proposes an apparatus for incinerating a gasification cake, a drying unit 100 of which includes a multi-hearth furnace dryer 1, a high temperature wind generating device 7, and a temperature equalizer 8. The multi-hearth furnace dryer 1 is characterized in that the body of the multi-hearth furnace dryer 1 is cylindrical, a multi-hearth furnace feed inlet 11 and a multi-hearth furnace flue gas outlet 12 are formed in the top of the multi-hearth furnace dryer 1, a multi-hearth furnace ash outlet 15 is formed in the bottom of the multi-hearth furnace dryer, a multi-hearth furnace center shaft 13 is arranged in the center of the multi-hearth furnace dryer, multi-hearth furnace rake arm rake teeth 14 are connected to the multi-hearth furnace center shaft 13 in a self-supporting mode, and the multi-hearth furnace rake arm rake teeth 14 are arranged in 3-6 layers, preferably 4 layers. A plurality of heating smoke ports 16 are arranged on the side wall of the cylinder of the multi-hearth furnace dryer 1. The heating flue gas interface 16 is sequentially connected with the temperature equalizer 8 and the high-temperature wind generating device 7, the high-temperature wind generating device 7 is a flue burner, and the honeycomb ceramic heat accumulator is arranged in the temperature equalizer 8.

Referring to fig. 3 to 5, one embodiment of the present application proposes an apparatus for incinerating a gasification cake, a transport sorting unit 200 of which includes a first return 21, an ash transporting device 22 and a gravity separator 23 connected in this order.

The first material returning device 21 comprises a first material returning riser 211 and a first material returning device return pipe 212, wherein the first material returning riser 211 is connected with the ash outlet 15 of the multi-hearth furnace, and the first material returning device return pipe 212 is connected with the ash conveying device 22.

The ash conveyor 22 is arranged laterally and includes, from left to right, a gas inlet 222, a constriction 223, a throat 224, a diffuser 225, and an ash discharge port 226. The sidewall of the throat section 224 is provided with an ash feeding port 221, and the first return pipe 212 of the return feeder is connected with the ash feeding port 221.

The gravity separator 23 comprises a separator feed inlet 231, a separator separation section 232 and a separator air outlet 233 which are transversely arranged from left to right, a carbon-lean ash bucket 234 is arranged at the bottom of the separator separation section 232 and near the separator feed inlet 231, and a carbon-rich ash bucket 235 is arranged at the bottom of the separator separation section 232 and near the separator air outlet 233. The ash discharge port 226 is connected to the classifier feed port 231.

The ash conveyor 22 is also connected to the outlets of the carbon-lean hopper 234 and the carbon-rich hopper 235, respectively, in a similar manner to the connection of the first return 21 and the ash conveyor 22.

Referring to fig. 6 to 9, one embodiment of the present application proposes an apparatus for incinerating a gasification cake, the carbon-rich incineration unit 400 of which mainly includes a cyclone incinerator 4, an ash cooler 5, and a waste heat boiler 9.

The cyclone incinerator 4 mainly comprises an incineration chamber 41 and a cooling chamber 42 connected by a connecting section 416. The main body of the incineration chamber 41 is in a circular structure, and comprises a cyclone furnace conveying section 411, a cyclone furnace combustion section 412 and a slag discharge port 415 from top to bottom. An incineration chamber feeding section 413 is arranged at the top of the incineration chamber 41, the incineration chamber feeding section 413 comprises a carbon-rich slag conveying channel 4131 and a residual flue gas conveying channel 4132 which are coaxially arranged, the carbon-rich slag conveying channel 4131 is of a hollow cylinder structure, the residual flue gas conveying channel 4132 is of a hollow cylinder structure, and the carbon-rich slag conveying channel 4131 is arranged inside the residual flue gas conveying channel 4132. Further, the carbon-rich slag conveying passage 4131 and the part of the bottom of the residual flue gas conveying passage 4132 near the cyclone incinerator 4 are provided with swirl vanes 4133. An incineration chamber air inlet 414 is also formed at the upper position of the side wall of the incineration chamber 41. The upper space of the air inlet 414 of the incineration chamber is a cyclone furnace conveying section 411, and the lower space is a cyclone furnace combustion section 412. The slag discharging port 415 is positioned at the center of the bottom of the incineration chamber 41, and the slag discharging port 415 is connected with the slag cooler 43.

The cooling chamber 42 comprises a cooling chamber ash discharge port 421, a cooling chamber cylinder 422, an ash catching pipe 426 and a cyclone furnace flue gas outlet 427 from bottom to top. The cooling chamber ash discharge port 421 is positioned at the center of the bottom of the cooling chamber 42, the cyclone furnace flue gas outlet 427 is positioned at the top of the cooling chamber 42, the upper part of the cooling chamber cylinder 422 is provided with an ash catching pipe 426 near the bottom of the cyclone furnace flue gas outlet 427. The cooling chamber cylinder 422 has a square structure and is provided with a folded flame pocket 424 at a lower portion of a side wall opposite to the connection section 416. A cooling chamber air inlet 423 is provided above the corner of the folded flame horn 424. A cooling chamber wet slag inlet 425 is provided at a position above the cooling chamber cylinder 422 and below the ash catching pipe 426. The cyclone furnace flue gas outlet 427 of the cyclone furnace 4 is connected with the waste heat boiler 9, and the cooling chamber ash discharge port 421 of the cyclone furnace 4 is connected with the ash cooler 5.

The connecting section 416 has one end communicating with the lower portion of the side wall of the incineration chamber 41 and the other end communicating with the lower portion of the side wall of the cooling chamber 42. The bottom of the incineration chamber 41 is downwards convex from edge to center, and a preferable slag discharging port 415 is positioned at the central low point of the bottom of the incineration chamber 41; similarly, the bottom of the cooling chamber 42 is also convex downwards from edge to center, and the preferred cooling chamber ash discharge port 421 is located at the central low point of the bottom of the cooling chamber 42; the inclination angles of the bottoms of the incineration chamber 41 and the cooling chamber 42 are 2-10 degrees, and the slag catching pipe 417 is arranged in the connecting section 416.

Preferably, taking fig. 9 as an example, the bottom inclination of the incineration chamber 41 is 6 °, and the bottom inclination of the cooling chamber 42 is 3 °. The arrangement of the inclination angle of the chamber bottom can enable the slag and the ash to flow smoothly, and can avoid the contact between the slag and the solid ash.

Referring to fig. 10, one embodiment of the present application proposes an apparatus for incinerating a gasification cake, a carbon-lean incineration unit 300 of which includes a fluidized-bed flameless combustion furnace 3, a high-temperature wind generating device 7, a temperature equalizer 8, a first cyclone 301, a second cyclone 302, an ash cooler 5, and a second return 6.

The fluidized bed flameless combustion furnace 3 is of a round structure or a square structure, and comprises an air chamber 31, an air distribution plate 32, a fluidized bed combustion chamber 33 and a combustion chamber flue gas outlet 34 from bottom to top. The ash discharge port 226 communicates with the lower portion of the side wall of the fluidized bed combustor 33. The combustion chamber flue gas outlet 34 is connected with a first cyclone separator 301, an ash discharge port of the first cyclone separator 301 is connected with a second return riser 61, and an exhaust port of the first cyclone separator 301 is connected with a second cyclone separator 302. An ash cooler 5 is arranged between an ash discharge port of the first cyclone separator 301 and the second return riser 61, a second return pipe 62 of the second return 6 is connected with the lower part of the fluidized bed combustion chamber 33, and the connection position of the ash discharge port 226 and the fluidized bed combustion chamber 33 is above the connection position of the second return pipe 62 and the fluidized bed combustion chamber 33. The ash discharge port of the second cyclone 302 is connected to the ash cooler 5. The high-temperature wind generating device 7 is connected with the temperature equalizer 8, and the temperature equalizer 8 is connected with the air chamber 31 of the fluidized bed flameless combustion furnace 3. The high-temperature wind generating device 7 is a flue burner, and a honeycomb ceramic heat accumulator is arranged in the temperature equalizer 8.

Referring to fig. 11, the connection mode of the drying unit 100, the conveying and sorting unit 200 and the carbon-lean incineration 300 unit is as follows: the multi-hearth furnace dryer 1, the first returning device 21, the ash conveying device 22, the gravity separator 23, the ash conveying device 22 and the fluidized bed flameless combustion furnace 3 are connected in sequence. Referring to fig. 12, the connection mode of the drying unit 100, the conveying and sorting unit 200 and the carbon-rich incineration unit 400 is as follows: the multi-hearth furnace dryer 1, the first returning charge 21, the ash conveyor 22, the gravity separator 23, the ash conveyor 22, the cyclone incineration chamber 41, the connecting section 416, and the cooling chamber 42 are connected in this order.

Referring to fig. 13 to 20, an embodiment of the present application proposes an incineration disposal gasification filter cake device, in which an ash cooler 5 is cylindrical, and has two tapered ends, and includes a feeding zone 51, an upper cooling zone 52, an intermediate zone 53, a lower cooling zone 54, and a discharging zone 55 from top to bottom. The wall surface of the ash cooler 5 is provided with a water-cooling interlayer 56, a first water inlet 561 is formed in the water-cooling interlayer 56 section of the discharging area 55, and a first water outlet 562 is formed in the water-cooling interlayer 56 section of the feeding area 51. The feeding area 51 is a big end with a small top and a big bottom, the inside of the feeding area 51 is of a hollow structure, and the feeding area 51 is provided with a manhole 58. The water-cooled wall heat exchanger 57 is disposed in the inner space of the upper cooling zone 52. The middle area 53 is hollow, the middle area 53 is provided with a manhole 58, and the outer side of the outer shell of the middle area 53 is also provided with a communicating pipe 575. The inner space of the lower cooling zone 54 is provided with a water-cooled wall heat exchanger 57. The discharging area 55 is a big end with big top and small bottom, the inside of the discharging area 55 is of a hollow structure, and the discharging area 55 is provided with a manhole 58.

The water wall heat exchanger 57 includes a lower header 572, a membrane water wall 573, and an upper header 574, which are connected in this order from bottom to top. The lower header 572 includes a lower line header 5721 and a lower annular header 5722 that are communicated, and the lower line header 5721 is uniformly distributed in the lower annular header 5722 in the circumferential direction. The upper header 574 includes an upper line header 5741 and an upper annular header 5742 that are communicated, and the upper line header 5741 is uniformly distributed in the upper annular header 5742 in the circumferential direction. The water-cooled wall heat exchanger 57 in the lower cooling zone 54 has a second water inlet 571 formed in the side wall of the lower annular header 5722. The water-cooled wall heat exchanger 57 in the upper cooling zone 52 has a second water outlet 576 formed in the sidewall of the upper annular header 5742. The water-cooled wall heat exchangers 57 in the upper and lower cooling areas are communicated by the communicating pipes 575 in the middle area 53, and the communicating pipes 575 can be arranged in a plurality and uniformly distributed along the circumferential direction.

Membrane wall 573 includes a long segment membrane wall 5731 and a short segment membrane wall 5732, the number of water wall tubes disposed in long segment membrane wall 5731 is greater than that of short segment membrane wall 5732, and for example, 6 water wall tubes are disposed in long segment membrane wall 5731 and 4 water wall tubes are disposed in short segment membrane wall 5732 as shown in FIGS. 16 and 18. The long section film water-cooling walls 5731 are 4 fans and are uniformly distributed at an included angle of 90 degrees, the short section film water-cooling walls 5732 are provided with a plurality of fans, the fans are uniformly distributed between two adjacent long section film water-cooling walls 5731, and all water-cooling wall pipes are distributed in the center of the ash cooler. Taking fig. 14 and 15 as an example, the long-section membrane water walls 5731 are 4, and two short-section membrane water walls 5732 are disposed between two adjacent long-section membrane water walls 5731.

The number of long-section film water walls 5731 and short-section film water walls 5732 of upper cooling zone 52 and lower cooling zone 54 are the same, and the film water walls located in upper cooling zone 52 and the film water walls located in lower cooling zone 54 are arranged at an included angle of 10 ° -40 °. Taking fig. 20 as an example, the included angle is preferably 15 °.

The working flow of the incineration disposal method for the gasification filter cake is as follows: the gasification filter cake A is sent into the multi-hearth furnace dryer 1 from the multi-hearth furnace feed inlet 11, and the multi-hearth furnace center shaft 13 drives the multi-hearth furnace rake arm rake teeth 14 to rotate, so that the gasification filter cake A is continuously turned over and falls down layer by layer. The flue gas P1 for heating the multi-hearth furnace dryer is introduced into the multi-hearth furnace dryer 1 through the heating flue gas interface 16 to serve as a heating and drying heat source, and the drying time of the gasified filter cake A is adjusted by adjusting the rotation rate of the rake teeth 14 of the multi-hearth furnace rake arm, so that the sufficient drying of the gasified filter cake A is ensured.

After the drying is finished, the flue gas is discharged from a flue gas outlet 12 of the multi-hearth furnace and is divided into flue gas K1 outside the multi-hearth furnace outlet and flue gas K2 for conveying ash slag from the multi-hearth furnace outlet. The gasified filter cake A after drying is dehydrated and becomes a dried filter cake B, the residue of the dried filter cake B mainly contains carbon and metal simple substances and/or compounds thereof, the dried filter cake B leaves the multi-hearth furnace dryer 1 from the multi-hearth furnace ash outlet 15 and then enters the first material returning riser 211, and enters the ash conveying device 22 through the first material returning pipe 212 under the conveying of the first material returning device 21. The dried filter cake B entering the ash conveying device 22 enters a gravity separator 23 under the pneumatic conveying action of the flue gas K2 for conveying ash at the outlet of the multi-hearth furnace, and is roughly separated into carbon-lean slag C and carbon-rich slag D under the action of gravity sedimentation, and falls into a carbon-lean ash bucket 234 and a carbon-rich ash bucket 235 for temporary storage, wherein the carbon content of the carbon-rich slag D is far higher than that of the carbon-lean slag C. Further, the flue gas sorted by the gravity separator 23 becomes the transport remaining flue gas E.

The carbon-rich slag D in the carbon-rich hopper 235 is conveyed into the cyclone incinerator 4 by the slag conveyor 22. The carbon-rich slag D and the residual flue gas E are respectively conveyed through the carbon-rich slag conveying channel 4131 and the residual flue gas conveying channel 4132, and enter the cyclone furnace conveying section 411 after the cyclone flow of the cyclone sheet 4133 is adjusted. Under the action of the cyclone plate 4133, the carbon-rich slag D and the residual flue gas E form a spiral downward movement track in the cyclone furnace conveying section 411. The spiral downward carbon-rich slag D and the residual flue gas E are conveyed and burnt in contact with air R introduced by an air inlet 414 of the burning chamber, the carbon content of the carbon-rich slag D is high, the burning temperature is high, carbon reacts with oxygen to generate carbon dioxide, metal simple substances and/or compounds in the carbon-rich slag D react with oxygen to generate metal oxides, and molybdenum trioxide and vanadium pentoxide in the carbon-rich slag D become liquid. The liquid slag Q generated by combustion, mainly molybdenum trioxide and vanadium pentoxide in liquid state, enters the slag cooler 43 from the slag discharge port 415, and is cooled by the process water X1 in direct contact to become wet slag F containing water.

The flue gas generated in the incineration chamber 41 carries part of the liquid slag, and the liquid slag is captured by the slag capturing pipe 417 and then enters the cooling chamber 42. Air R is introduced into the cooling chamber 42 to cool the flue gas from the incineration chamber 41, and the wet slag F containing water is also introduced into the cooling chamber 42 from the wet slag inlet 425 of the cooling chamber. A small amount of liquid slag in the slag-captured flue gas becomes solid under the cooling of air R, the moisture of the wet slag F is removed under the heating of the flue gas and becomes high Wen Ganzha product G1, and then the wet slag F is discharged from a cooling chamber ash discharge port 421 and enters an ash cooler 5, and the ash cooler 5 adopts boiler feed water X2 as a cooling medium and becomes high-temperature water Y2 after heat exchange. After cooling, the high Wen Ganzha product G1 becomes a low temperature dry slag product G2. The cooled flue gas enters the ash capturing pipe 426 to further remove carried solid particles, and finally becomes cyclone furnace outlet flue gas H which leaves the cyclone incinerator 4 from the cyclone furnace flue gas outlet 427. The flue gas H at the outlet of the cyclone furnace is changed into low-temperature flue gas J for discharging after being subjected to waste heat recovery by the waste heat boiler 9, and the waste heat boiler 9 heats the boiler feed water X2 into steam Y1.

The carbon-lean slag C in the carbon-lean ash bucket 234 is fed into the fluidized-bed flameless combustion furnace 3 via the ash conveyor 22. The fuel M, such as natural gas, coal gas or fuel oil, is burnt with excessive air R in the high-temperature wind generating device 7 to generate high-temperature low-oxygen smoke, and then becomes high-temperature low-oxygen wind P2 with uniform temperature under the uniform temperature effect of the temperature equalizer 8. The high temperature low oxygen wind P2 enters the fluidized bed combustion chamber 33 through the wind chamber 31 and the wind distribution plate 32. The carbon-lean slag C and the high-temperature low-oxygen wind P2 are incinerated in the fluidized bed combustion chamber 33, carbon in the carbon-lean slag C reacts with oxygen to form carbon dioxide, and metal simple substances and/or compounds in the carbon-lean slag C react with oxygen to form metal oxides, which are in a solid state due to relatively low temperature in the fluidized bed combustion chamber 33.

The flue gas N at the outlet of the fluidized bed incinerator carries a large amount of metal oxides and enters the first cyclone separator 301 from the flue gas outlet 34 of the combustion chamber, a large-grain-size product T1 is separated under the centrifugal action and then exchanges heat with boiler feed water X2 through the ash cooler 5, the cooled large-grain-size product T2 is conveyed by the second material returning device 6, and enters the lower part of the fluidized bed flameless combustion furnace 3 through the material returning pipe 62 of the second material returning device. The flue gas carrying metal oxide and coming out of the exhaust port of the first cyclone separator 301 continuously enters the second cyclone separator 302, the high Wen Ganzha product G1 enters the ash cooler 5 under the centrifugal action to exchange heat with the boiler feed water X2, and the main component of the cooled low-temperature dry slag product G2 is metal oxide, namely the final product. The flue gas V discharged from the fluidized bed incinerator is discharged from the exhaust port of the second cyclone separator 42.

The fuel M is burnt with air R in a high-temperature wind generating device 7 to generate high-temperature smoke, and the high-temperature smoke is changed into smoke P1 for heating the multi-hearth furnace dryer with uniform temperature under the uniform temperature effect of a temperature equalizer 8. The flue gas P1 for heating the dryer enters the multi-hearth furnace through the heating flue gas interface 16 to heat and dry the gasified filter cake.

The high-temperature dry slag product G1 passes through the feeding area 51, the upper cooling area 52, the middle area 53, the lower cooling area 54 and the discharging area 55 of the ash cooler 5 from top to bottom to finish the cooling process, and finally becomes the low-temperature dry slag product G2 to leave the ash cooler 5. The walls of the feeding zone 51, the upper cooling zone 52, the middle zone 53, the lower cooling zone 54 and the discharging zone 55 are provided with a water cooling interlayer 56, boiler feed water X2 enters the water cooling interlayer 56 from a first water inlet 561 positioned at the bottom discharging zone 55, absorbs heat and becomes high temperature water Y2 to leave the ash cooler 5 from a first water outlet 562 positioned at the feeding zone 51. Water wall heat exchangers 57 are disposed in the upper cooling zone 52 and the lower cooling zone 54, and boiler feed water X2 enters the lower annular header 5722 of the lower header 572 of the lower cooling zone 54 from the second water inlet 571, further enters the lower linear header 5721, further enters the upper linear header 5741 of the upper header 574 of the lower cooling zone 54 through the membrane water wall 573, and further enters the upper annular header 5742. The boiler feed water X2 entering the upper annular header 5742 enters the lower annular header 5722 of the lower header 572 of the upper cooling zone 52 through the plurality of communicating pipes 575 located in the intermediate zone 53. The path of the boiler feed water X2 in the upper cooling zone 52 is similar to that in the lower cooling zone 54 and will not be described again. Finally, the heat-absorbed boiler feed water X2 becomes high temperature water Y2 and leaves the ash cooler 5 from the second water outlet 576 of the upper annular header 5742 located in the upper cooling zone 52.

The temperature of the dried filter cake B sent out by the multi-hearth furnace dryer 1 is 150-350 ℃, and the temperature of the flue gas K2 for conveying ash slag at the outlet of the multi-hearth furnace is 150-350 ℃. The fuel M is low-calorific-value fuel, and the temperature of the flue gas P1 for heating the multi-hearth furnace dryer 1 is 400-600 ℃. The incineration temperature of the incineration chamber 41 is 850-1300 ℃. The temperature of the flue gas H at the outlet of the cyclone furnace is 500-650 ℃. The temperature of the high-temperature dry slag product G1 is 500-650 ℃, and the temperature of the low-temperature dry slag product G2 is 50-80 ℃. The high-temperature dry slag product G1 passes through the ash cooler 5 from top to bottom, and boiler feed water X2 passes through the ash cooler 5 from bottom to top, and the two are subjected to countercurrent heat exchange. The boiler feed water X2 is normal temperature demineralized water. The temperature of the high-temperature low-oxygen wind P2 is 400-600 ℃, and the oxygen content is 5-16%. The burning temperature of the fluidized bed combustion chamber 33 is 500-650 ℃. The temperature of the cooled large-grain-size product T2 is 50-200 ℃. The connecting position of the ash discharging hole 226 and the fluidized bed flameless combustion furnace 3 is positioned at the upper end of the connecting position of the second material returning pipe 62 and the fluidized bed flameless combustion furnace 3. The circulation multiplying power of the fluidized bed flameless combustion furnace 3 is 10-30 times. The carbon content in the carbon-rich slag D is more than or equal to 70 percent, and the carbon content in the carbon-lean slag C is less than or equal to 30 percent.

The device and the method for incinerating and disposing the gasified filter cake have the beneficial effects and the corresponding principle that:

First: the reduction, harmlessness and recycling of the gasification filter cake are realized by coupling the multi-hearth furnace and the sectional combustion.

The gasified filter cake has the characteristics of high water content and low melting point of metal oxide of the incineration product. The multi-hearth furnace has the defect that the temperature of a roasting section is difficult to control, the temperature exceeding of a gasified filter cake can occur when the multi-hearth furnace is used for incinerating, the metal oxide is liquefied to further cause hardening of furnace burden, and the roasting effect and the stable operation of a system are affected. The cyclone furnace has the characteristics of high volumetric heat load and high incineration temperature, and the problems that raw materials are difficult to convey into a hearth and liquid slag is entrained in smoke can occur when the cyclone furnace is used for directly incinerating a gasified filter cake. The fluidized bed has the advantage of uniform incineration temperature, but the fluidized bed can not process pasty materials with too high water content, and in order to ensure the incineration efficiency, the incineration temperature of the fluidized bed is higher. The problems that the bed material is adhered, the raw materials are difficult to convey into a hearth and the carbon burnout rate is low can occur when the fluidized bed is adopted to directly burn the gasified filter cake.

The method removes the moisture contained in the gasified filter cake by a multi-hearth furnace dryer, and the dried filter cake with the temperature of 150-350 ℃ is separated by a gravity separator to become carbon-rich slag with high carbon content and high heat value and carbon-lean slag with low carbon content and low heat value. The carbon-rich slag is incinerated by adopting the liquid slag-discharging cyclone furnace, the incineration temperature is 850-1300 ℃, the melting points of molybdenum trioxide and vanadium pentoxide are exceeded, the high-temperature condition is enough to ensure the carbon incineration rate, and the problem of slag blockage is not needed to be worried about in liquid slag discharging. The lean carbon slag is sent into a fluidized bed flameless incinerator for incineration, the incineration temperature is 500-650 ℃, and the incineration temperature is lower than the melting points of molybdenum trioxide and vanadium pentoxide. The method thoroughly solves the problem that the fluidized bed is over-temperature and the carbon burnout rate is not high in a flameless combustion combined bed external cooling mode. For the fluidized bed flameless combustion furnace, the materials entering the combustion chamber are lean carbon slag with the temperature of 150-350 ℃ and large-particle products with the temperature of 50-200 ℃, and high-temperature low-oxygen wind (used as a fluidization medium and combustion air) with the temperature of 400-600 ℃ and the oxygen content of 5-16%. The high temperature low oxygen wind and the higher temperature lean carbon slag provide conditions for flameless combustion in the combustion chamber. Flameless combustion has the characteristics of uniform temperature and high combustion efficiency. The combined mode of the fluidized bed and flameless combustion can solve the problems of uneven burning temperature and low carbon burnout rate of the dried filter cake. In conclusion, the multi-hearth furnace and the sectional combustion are coupled together, and the multi-hearth furnace has the advantages of stable system operation and high carbon burnout rate.

Second,: through special ash cooler structural design, guarantee dry slag product cooling to the temperature of demand.

Gas-solid heat transfer is often inefficient. The application satisfies the cooling demand through water-cooling intermediate layer + water-cooled wall heat exchanger integrated configuration. Firstly, the water and ash in the water-cooling interlayer and water-cooling wall heat exchanger are subjected to countercurrent heat exchange, and the temperature and pressure are high. Secondly, the water-cooled wall heat exchanger is designed into a double-cooling section, and a long-section membrane water-cooled wall and a short-section membrane water-cooled wall which are specially designed are uniformly distributed in a single cooling section according to the circumferential direction, and the membrane water-cooled wall with the structural characteristics can ensure the full contact of ash and water-cooled wall pipes and also consider the flow space of ash.

For the fluidized bed flameless incinerator, the fluidized bed flameless incinerator can adopt a water-cooled wall hearth or an adiabatic hearth, but the heat released by the combustion in the incinerator is mainly absorbed by an ash cooler. If only the water-cooled wall hearth is used for absorbing heat released by combustion, the problem that the temperature of the furnace wall area is low and the temperature of the furnace center area is high is easy to occur. The heat released by combustion in the furnace is mainly absorbed by the ash cooler, the temperature of a large-grain-size product entering the furnace is guaranteed to be reduced to a proper temperature level through the external heat exchanger, and meanwhile, the total heat taken away by the ash cooler is guaranteed to be lower than 690 ℃ through higher circulation rate and lower heat value of the material entering the furnace.

Further, the connecting position of the ash conveying device and the fluidized bed flameless combustion furnace is positioned at the upper end of the connecting position of the return pipe of the second material returning device and the fluidized bed flameless combustion furnace, the high-temperature low-oxygen air is firstly contacted with the cooled large-grain-size product and then contacted with the lean carbon slag, namely the lean carbon slag enters the mixture of the high-temperature low-oxygen air with the temperature reduced and the large-grain-size product with the temperature increased, which is directly contacted with the inside of the furnace, the total mass of the mixture is far higher than the quantity of the lean carbon slag, and the heat generated by burning the lean carbon slag entering the furnace is guaranteed to be timely absorbed by the mixture by virtue of the huge heat storage capacity and dilution capacity of the mixture, so that the overtemperature is prevented. Further, due to the fact that the heat value of the lean carbon slag is small, the heat taken away by the ash cooler is small, the fluidized bed flameless combustion furnace can be low in circulation rate, and the required device is small in scale.

Thirdly, the dried filter cake is subjected to primary screening through a gravity separator so as to meet different incineration conditions.

The dried filter cake mainly contains carbon and metal simple substance or compound, and the bulk density of the carbon is about 800-1000kg/m ³ The bulk density of the metal simple substance or compound is more than 1500kg/m ³ . Drying filterWhen the cake is carried by the air flow and moves to the inside of the gravity separator, the flow speed of the air is reduced, under the action of gravity sedimentation, the metal simple substance or compound with high density is preferentially settled, the path of the carbon with low density carried by the air flow is longer, and the settlement is slower. Thus, the dried filter cake is separated into carbon-rich slag with high carbon content and high heat value and carbon-lean slag with low carbon content and low heat value.

The cyclone incinerator is higher than the melting point of the metal compound, the temperature is high, the heat value of the material needing to be fed into the incinerator is high, the fluidized bed incineration is lower than the melting point of the metal compound, the temperature is low, and the heat value of the material needing to be fed into the incinerator is low. Therefore, the screening effect of the gravity separator enables the incineration working condition to meet the process requirement, and is more beneficial to the stable operation and control of the system.

Fourth, through ash conveying device, solve the even transportation problem of cigarette sediment mixture high speed.

The ash conveying device is used for conveying the ash mixture. The speed of the flue gas for conveying ash at the outlet of the multi-hearth furnace is increased after the ash conveying device passes through the contraction section, negative pressure is generated at the throat section, the mixture of the flue gas and the slag enters the throat section under the suction effect of the negative pressure and is fully mixed with the flue gas, and the mixture of the flue gas and the slag is further mixed through the diffusion section and the ash discharge port and the speed of the mixture of the flue gas and the slag is adjusted to a required value.

Fifthly, through reasonable arrangement of the cyclone furnace conveying section and the cyclone furnace combustion section, safe operation of the feeding channel is protected.

The downward spiral airflow of the gas-solid mixture in the cyclone incinerator plays a crucial role in stable incineration in the cyclone incinerator. The cyclone sheet in the cyclone furnace conveying section is used for providing a reasonable movement track of materials entering the cyclone furnace. Further, the cyclone incinerator is high in temperature, has a strong heat radiation effect on the carbon-rich conveying channel and the residual flue gas conveying channel, and is easy to burn out the material channel. The utility model provides a do not set up combustion air passageway in cyclone incinerator's material conveying passageway, so, the material does not take place the combustion reaction after entering cyclone furnace inside very first time, and cyclone furnace conveying section temperature is low, can not burn out and carry the material passageway.

Sixth, the problem of energy utilization of the carried liquid slag smoke and the problem of collection of metal oxide products are solved through the cooling chamber.

The flue gas from the cyclone furnace incineration chamber carries liquid slag, and if the flue gas directly enters the heat exchange surface, the problem that the liquid slag condenses to block the heat exchange surface can occur. The liquid slag from the slag discharge port of the cyclone furnace incineration chamber enters a slag cooler for cooling, and then contains a large amount of water, so that the final product of the project is the dry low-temperature metal oxide. The present application thus introduces the aqueous wet slag and cooling air into the cooling chamber, cooling the liquid slag below the melting point to become solid, while drying the aqueous wet slag. The energy of the flue gas without liquid slag is further recovered by a waste heat boiler, and the high Wen Ganzha product is further cooled by an ash cooler.

Seventh: the optimal utilization of energy and substances is realized through the deep coupling linkage among the system devices.

The used heating medium of multi-chamber stove dryer of this application is the flue gas of high temperature wind generating device production after the temperature equalizer temperature regulation, when make full use of flue gas energy, has still improved multi-chamber stove dryer's stability. The flue gas is an inert medium, and the oxygen content is low, so that the sensible heat of the flue gas mainly depends on the drying process in the multi-hearth furnace dryer, and the problem that the excessive temperature is caused by the carbon and oxygen reaction of the multi-hearth furnace dryer due to the excessive introduction of oxygen is avoided. The flue gas at the outlet of the multi-hearth furnace dryer is an inert medium, and a part of flue gas is used as a conveying medium for drying the filter cake, and the inert medium can prevent carbon and oxygen in the drying filter cake from reacting during conveying, so that the stable operation of the system is facilitated. The byproduct high temperature water of the ash cooler is also used for heating and the like. The byproduct steam of the waste heat boiler can be used for heating or generating electricity.

Example 1

7.5t/h of gasified filter cake A (containing 18% of carbon, 70% of water and the balance of metal and compound thereof) enters the multi-hearth furnace dryer 1 from the multi-hearth furnace feed inlet 11, and the multi-hearth furnace center shaft 13 drives the multi-hearth furnace rake arm rake teeth 14 to rotate and continuously turn over the gasified filter cake A entering the multi-hearth furnace dryer 1 and enable the gasified filter cake A to fall down layer by layer. Flue gas P1 for heating multi-hearth dryer (temperature 550 ℃, volume 29500 m) ³ And/h) the gasified filter cake A is heated and dried by entering the multi-hearth furnace through the heating flue gas interface 16. Multiple chambers after dryingFurnace outlet smoke (temperature 200 ℃, volume 28300 m) ³ And/h) leaves the multi-hearth furnace dryer 1 from the multi-hearth furnace flue gas outlet 12. Further, the fume at the outlet of the multi-hearth furnace after the drying is finished comprises fume K1 outside the outlet of the multi-hearth furnace and fume K2 (the temperature is 200 ℃) for conveying ash slag at the outlet of the multi-hearth furnace.

The dried filter cake B (2.25 t/h, temperature 200 ℃, mainly containing carbon and metal elements or compounds) after drying leaves the multi-hearth furnace dryer 1 from the multi-hearth furnace ash outlet 15. Further, the dried filter cake B enters the first return riser 211 and enters the ash conveyor 22 through the first return pipe 212 under the conveying action of the first return 21. The dried cake B fed into the ash conveyor 22 was fed with ash flue gas K2 (temperature 200 ℃ C., volume 1125 m) at the outlet of the multi-hearth furnace ³ And/h) enters a gravity separator 23 under the pneumatic conveying action, and the dried filter cake B is separated into carbon-lean slag C (0.99 t/h and carbon content of 27%) and carbon-rich slag D (1.26 t/h and carbon content of 86%) under the gravity sedimentation action, and enters a carbon-lean ash bucket 234 and a carbon-rich ash bucket 235 for temporary storage respectively. Further, the flue gas separated by the gravity separator 23 becomes a transport surplus flue gas E (temperature 200 ℃, volume 1125m ³ /h）。

The carbon-rich slag D exits the gravity separator 23 from the carbon-rich hopper 235 into the ash conveyor 22. The carbon-rich slag D introduced into the slag conveyor 22 was fed with a flue gas K2 (temperature 200 ℃ C., volume 630 m) for slag at the outlet of the multi-hearth furnace ³ And/h) enters the cyclone incinerator 4 under the pneumatic conveying action. The carbon-rich slag D and the residual flue gas E enter a carbon-rich slag conveying channel 4131 and a residual flue gas conveying channel 4132 of the incinerator feeding section 413 respectively, and further enter the cyclone furnace conveying section 411 after the cyclone flow direction of the cyclone plate 4133 is adjusted. Under the action of the cyclone plate 4133, the carbon-rich slag D and the residual flue gas E form a spiral downward movement track in the cyclone furnace conveying section 411.

Further, carbon-rich slag D and air R (temperature 25 ℃, volume 24050m ³ And/h) contact combustion, wherein the burning temperature is 1225 ℃, carbon in the carbon-rich slag D reacts with oxygen to form carbon dioxide, and metal simple substance or chemical substance in the carbon-rich slag DThe compound reacts with oxygen to become a metal oxide, and molybdenum trioxide and vanadium pentoxide become liquid. The liquid slag Q (0.15 t/h) enters the slag cooler 43 from the slag discharge port 415, and is cooled by the process water X1 to become wet slag F (direct contact cooling). The flue gas generated in the incineration chamber 41 carries part of the liquid slag, and the slag content is reduced under the slag supplement of the slag trap 417, and further enters the cooling chamber 42. Air R (temperature 25 ℃ C., volume 17180 m) is introduced into the cooling chamber 42 ³ /h) cooling the flue gas from the incineration chamber 41, further, also an aqueous wet slag F (0.15 t/h of metal oxide and 0.15t/h of water) enters the cooling chamber 42 from the cooling chamber wet slag inlet 425. A small amount of liquid slag in the flue gas from the incineration chamber 41 becomes solid under the cooling of the air R, the moisture of the wet slag F is removed and finally becomes high Wen Ganzha product G1 (0.18 t/h, temperature 640 ℃) under the heating action of the flue gas, the wet slag F is discharged from the cooling chamber ash discharge port 421 into the ash cooler 5, the ash cooler 5 adopts boiler feed water X2 (25 ℃,2.4mpa,0.21 t/h) as a cooling medium, and high temperature water Y2 (106 ℃,2.4mpa,0.21 t/h) is generated. After cooling, the high Wen Ganzha product G1 changed to a low temperature dry slag product G2 (0.18 t/h, temperature 50 ℃ C.). The cooled flue gas enters an ash catching pipe 426 to further remove carried solid particles, and finally becomes cyclone furnace outlet flue gas H (temperature 640 ℃ C., volume 136000 m) ³ And/h) leaves the cyclone incinerator 4 from the cyclone flue gas outlet 427. The flue gas H at the outlet of the cyclone furnace is changed into low-temperature flue gas J (the temperature is 160 ℃ and the volume is 64400 m) after the waste heat of the waste heat boiler 9 is recovered ³ And/h), further, the waste heat boiler 9 heats the boiler feed water X2 (25 ℃,2.4MPa,11 t/h) to steam Y1 (210 ℃,1.3MPa,11 t/h).

Lean carbon slag C (0.99 t/h, 27% carbon content) leaves the gravity separator 23 from the lean carbon hopper 234 into the ash conveyor 22. The carbon-lean slag C introduced into the slag conveyor 22 was fed with flue gas K2 (200 ℃ C., 500m volume) for slag at the outlet of the multi-hearth furnace ³ And/h) is fed into the fluidized-bed flameless combustion furnace 3 through the ash discharge port 226 under the pneumatic conveying action.

The fuel M (natural gas, 50 Kg/h) was mixed with excess air R (3780M in the high temperature wind generating device 7 ³ And/h) generating high-temperature low-oxygen smoke by combustion reaction, and changing the smoke into high-temperature low-oxygen wind P2 (550 ℃ and 10600 m) with uniform temperature under the uniform temperature effect of the temperature equalizer 8 ³ /h, oxygen content 16%). The high temperature low oxygen wind P2 enters the fluidized bed combustion chamber 33 through the wind chamber 31 and the wind distribution plate 32. The carbon-lean slag C and the high-temperature low-oxygen wind P2 are incinerated in the fluidized bed combustion chamber 33, carbon in the carbon-lean slag C reacts with oxygen to become carbon dioxide, and metal simple substances and/or compounds in the carbon-lean slag C react with oxygen to generate metal oxides. The flue gas N at the outlet of the fluidized bed incinerator carries metal oxides (600 ℃ C., 15T/h) and enters the first cyclone 301 from the flue gas outlet 34 of the combustion chamber, large-particle-size products T1 (600 ℃ C., 14.3T/h) enter the second return riser 61 under the centrifugal effect and further enter the ash cooler 5, and the ash cooler 5 adopts boiler feed water X2 (25 ℃ C., 2.4MPa, 15T/h) as a cooling medium and generates high-temperature water Y2 (106 ℃ C., 2.4MPa, 15T/h). The cooled large-particle-size product T2 (100 ℃ C., 14.3T/h) enters the fluidized-bed flameless combustion furnace 3 through a second material returning pipe 62 under the conveying action of a second material returning device 6. The flue gas carrying metal oxide from the exhaust port of the first cyclone 301 enters the second cyclone 302, and under the centrifugal action, the high Wen Ganzha product G1 (600 ℃ C., 0.72 t/h) enters the ash cooler 5, and the ash cooler 5 uses boiler feed water X2 (25 ℃ C., 2.4 MPa., 0.8 t/h) as a cooling medium and generates high-temperature water Y2 (106 ℃ C., 2.4 MPa., 0.8 t/h). The main component of the cooled low-temperature dry slag product G2 (50 ℃ C., 0.72 t/h) is metal oxide as a final product. The flue gas V discharged from the fluidized bed incinerator is discharged from the exhaust port of the second cyclone separator 42.

The fuel M (0.28 t/h, low heating value gas) was mixed with air R (temperature 25 ℃ C., volume 10300M) in a high temperature wind generating device 7 ³ And/h) generating high-temperature smoke by combustion reaction, and changing the smoke into smoke P1 (with the temperature of 550 ℃ and the volume of 29500 m) for heating the multi-hearth furnace dryer with uniform temperature under the uniform temperature effect of the temperature equalizer 8 ³ /h). The flue gas P1 for heating the dryer enters the multi-hearth furnace through the heating flue gas interface 16 to heat and dry the gasified filter cake.

For the ash cooler 5 connected to the ash discharge pipe of the first cyclone 301, boiler feed water X2 (25 ℃,2.4MPa,1.5 t/h) enters the water-cooled interlayer 56 from the first water inlet 561 at the bottom discharge zone 55, absorbs heat and becomes hot water Y2 (106 ℃,2.4MPa,1.5 t/h) which leaves the ash cooler from the first water outlet 562 at the feed zone 51. Boiler feed water X2 (25 ℃,2.4mpa,13.5 t/h) also enters from the second water inlet 571, flows through the lower annular header 5722 and the lower linear header 5721 of the lower cooling zone 54 in sequence, further enters the upper header 574 of the lower cooling zone 54 through the membrane water wall 573, and then enters the lower header 572 of the upper cooling zone 52 through the communicating pipe 575. The path of the boiler feed water X2 in the upper cooling zone 52 is similar to that in the lower cooling zone 54 and will not be described again. Finally, the endothermic boiler feed water X2 is changed to hot water Y2 (106 ℃,2.4MPa,13.5 t/h) and leaves the first ash cooler 5 by the upper annular header 5742 of the upper cooling zone 52. The flow of working medium in the rest ash cooler 5 is similar to the flow, and no description is repeated.

In summary, by adopting the system and the method for disposing and separating the metal oxide by the oil residue gasification filter cake, the gasification filter cake of 7.5t/h is subjected to reduction, harmless and recycling treatment, and finally the metal oxide of 0.9 t/h is obtained by collecting.

Example 2

13t/h gasification filter cake A (containing 12% of carbon, 75% of water and the balance of metal and compound) enters the multi-hearth furnace dryer 1 from the multi-hearth furnace feed inlet 11, and the multi-hearth furnace center shaft 13 drives the multi-hearth furnace rake arm rake teeth 14 to rotate and continuously turn into the gasification filter cake A of the multi-hearth furnace dryer 1 and enable the gasification filter cake A to fall layer by layer. Flue gas P1 for heating multi-hearth furnace dryer (temperature 530 ℃ C., volume 66700 m) ³ And/h) the gasified filter cake A is heated and dried by entering the multi-hearth furnace through the heating flue gas interface 16. The flue gas at the outlet of the multi-chamber furnace after the drying is finished (the temperature is 250 ℃ C., the volume is 67030 m) ³ And/h) leaves the multi-hearth furnace dryer 1 from the multi-hearth furnace flue gas outlet 12. Further, the fume at the outlet of the multi-hearth furnace after the drying is finished comprises fume K1 outside the outlet of the multi-hearth furnace and fume K2 (the temperature is 250 ℃) for conveying ash slag at the outlet of the multi-hearth furnace.

The dried filter cake B (3.25 t/h, temperature 250 ℃ C., mainly containing carbon and metal simple substance or chemical Compound) leaves the multi-hearth furnace dryer 1 from the multi-hearth furnace ash outlet 15. Further, the dried filter cake B enters the first return riser 211 and enters the ash conveyor 22 through the first return pipe 212 under the conveying action of the first return 21. The dried filter cake B fed into the ash conveyor 22 was fed with ash flue gas K2 (temperature 250 ℃ C., volume 1625 m) at the outlet of the multi-hearth furnace ³ And/h) enters a gravity separator 23 under the pneumatic conveying action, and the dried filter cake B is separated into carbon-lean slag C (1.68 t/h and the carbon content of 9.5%) and carbon-rich slag D (1.57 t/h and the carbon content of 90%) under the gravity sedimentation action, and enters a carbon-lean ash bucket 234 and a carbon-rich ash bucket 235 for temporary storage respectively. Further, the flue gas separated by the gravity separator 23 becomes the transport residual flue gas E (temperature 250 ℃ C., volume 1625m ³ /h）。

The carbon-rich slag D exits the gravity separator 23 from the carbon-rich hopper 235 into the ash conveyor 22. The carbon-rich slag D fed into the slag conveyor 22 was fed with flue gas K2 (temperature 250 ℃ C., volume 780 m) for slag at the outlet of the multi-hearth furnace ³ And/h) enters the cyclone incinerator 4 under the pneumatic conveying action. The carbon-rich slag D and the residual flue gas E enter a carbon-rich slag conveying channel 4131 and a residual flue gas conveying channel 4132 of the incinerator feeding section 413 respectively, and further enter the cyclone furnace conveying section 411 after the cyclone flow direction of the cyclone plate 4133 is adjusted. Under the action of the cyclone plate 4133, the carbon-rich slag D and the residual flue gas E form a spiral downward movement track in the cyclone furnace conveying section 411.

Further, carbon-rich slag D and air R (temperature 25 ℃, volume 34700m ³ And/h) contact combustion, wherein the incineration temperature is 1100 ℃, carbon in the carbon-rich slag D reacts with oxygen to form carbon dioxide, a metal simple substance or compound in the carbon-rich slag D reacts with oxygen to form metal oxide, and molybdenum trioxide and vanadium pentoxide are changed into liquid states. The liquid slag Q (0.15 t/h) enters the slag cooler 43 from the slag discharge port 415, and is cooled by the process water X1 to become wet slag F (direct contact cooling). The flue gas generated in the incineration chamber 41 carries part of the liquid slag, and the slag content is reduced under the slag supplement of the slag trap 417, and further enters the cooling chamber 42. Air R (temperature) is introduced into the cooling chamber 4225 ℃, volume 26990m ³ /h) cooling the flue gas from the incineration chamber 41, further, also an aqueous wet slag F (0.15 t/h of metal oxide and 0.15t/h of water) enters the cooling chamber 42 from the cooling chamber wet slag inlet 425. A small amount of liquid slag in the flue gas from the incineration chamber 41 becomes solid under the cooling of the air R, the moisture of the wet slag F is removed and finally becomes high Wen Ganzha product G1 (0.17 t/h, temperature 550 ℃) under the heating action of the flue gas, the water is discharged from the cooling chamber ash discharge port 421 into the ash cooler 5, and the ash cooler 5 adopts boiler feed water X2 (25 ℃,2.4mpa,0.2 t/h) as a cooling medium and generates high temperature water Y2 (106 ℃,2.4mpa,0.2 t/h). After cooling, the high Wen Ganzha product G1 changed to a low temperature dry slag product G2 (0.17 t/h, 60 ℃ C.). The cooled flue gas enters an ash catching pipe 426 to further remove carried solid particles, and finally becomes cyclone furnace outlet flue gas H (the temperature is 550 ℃ and the volume is 186000 m) ³ And/h) leaves the cyclone incinerator 4 from the cyclone flue gas outlet 427. The flue gas H at the outlet of the cyclone furnace is changed into low-temperature flue gas J (the temperature is 160 ℃ and the volume is 98090 m) after the waste heat of the waste heat boiler 9 is recovered ³ And/h), further, the waste heat boiler 9 heats the boiler feed water X2 (25 ℃,2.4MPa,13.5 t/h) to steam Y1 (210 ℃,1.3MPa,13.5 t/h).

Lean carbon slag C (1.68 t/h, 9.5% carbon content) leaves the gravity separator 23 from the lean carbon hopper 234 into the ash conveyor 22. The lean carbon slag C entering the slag conveying device 22 conveys slag flue gas K2 (temperature 250 ℃ C., volume 840 m) at the multi-hearth furnace outlet ³ And/h) is fed into the fluidized-bed flameless combustion furnace 3 through the ash discharge port 226 under the pneumatic conveying action.

The fuel M (low heating value gas, 0.6 t/h) was mixed with excess air R (2460M) in a high temperature wind generating device 7 ³ And/h) generating high-temperature low-oxygen smoke by combustion reaction, and changing the smoke into high-temperature low-oxygen wind P2 (560 ℃ C., 8160 m) with uniform temperature under the uniform temperature effect of the temperature equalizer 8 ³ /h, 12% oxygen content). The high temperature low oxygen wind P2 enters the fluidized bed combustion chamber 33 through the wind chamber 31 and the wind distribution plate 32. The carbon-lean slag C and the high-temperature low-oxygen wind P2 are burnt in the fluidized bed combustion chamber 33, carbon in the carbon-lean slag C reacts with oxygen to become carbon dioxide, and metal simple substances and/or oxygen in the carbon-lean slag C The compound reacts with oxygen to form a metal oxide. The flue gas N at the outlet of the fluidized bed incinerator carries metal oxides (550 ℃, 33T/h) and enters the first cyclone 301 from the flue gas outlet 34 of the combustion chamber, the large-particle-size product T1 (550 ℃, 31.5T/h) enters the second return riser 61 under the centrifugal action and further enters the ash cooler 5, and the ash cooler 5 adopts boiler feed water X2 (25 ℃,2.4MPa, 35T/h) as a cooling medium and generates high-temperature water Y2 (106 ℃,2.4MPa, 35T/h). The cooled large-particle-size product T2 (100 ℃ C., 31.5T/h) enters the fluidized-bed flameless combustion furnace 3 through a second return pipe 62 of the second return feeder 6 under the conveying action. The flue gas carrying metal oxide from the exhaust port of the first cyclone 301 enters the second cyclone 302, and under the centrifugal action, the high Wen Ganzha product G1 (550 ℃ C., 1.52 t/h) enters the ash cooler 5, and the ash cooler 5 uses boiler feed water X2 (25 ℃ C., 2.4 MPa., 1.6 t/h) as a cooling medium and generates high-temperature water Y2 (106 ℃ C., 2.4 MPa., 1.6 t/h). The main component of the cooled low-temperature dry slag product G2 (60 ℃ C., 1.52 t/h) is metal oxide as a final product. The flue gas V discharged from the fluidized bed incinerator is discharged from the exhaust port of the second cyclone separator 42.

The fuel M (0.62 t/h, low heating value gas) was mixed with air R (temperature 25 ℃ C., volume 24050M) in a high temperature wind generating device 7 ³ And/h) generating high-temperature smoke by combustion reaction, and changing the smoke into smoke P1 (with the temperature of 550 ℃ and the volume of 66700 m) for heating the multi-hearth furnace dryer with uniform temperature under the uniform temperature effect of the temperature equalizer 8 ³ /h). The flue gas P1 for heating the dryer enters the multi-hearth furnace through the heating flue gas interface 16 to heat and dry the gasified filter cake.

For the ash cooler 5 connected to the ash discharge pipe of the first cyclone 301, boiler feed water X2 (25 ℃,2.4MPa,3 t/h) enters the water-cooled interlayer 56 from the first water inlet 561 at the bottom discharge zone 55, absorbs heat and becomes hot water Y2 (106 ℃,2.4MPa,3 t/h) which leaves the ash cooler from the first water outlet 562 at the feed zone 51. Boiler feed water X2 (25 ℃,2.4MPa,32 t/h) also enters from the second water inlet 571, flows through the lower annular header 5722 and the lower linear header 5721 of the lower cooling zone 54 in sequence, further enters the upper header 574 of the lower cooling zone 54 through the membrane water wall 573, and then enters the lower header 572 of the upper cooling zone 52 through the communicating pipe 575. The path of the boiler feed water X2 in the upper cooling zone 52 is similar to that in the lower cooling zone 54 and will not be described again. Finally, the endothermic boiler feed water X2 is changed to hot water Y2 (106 ℃,2.4MPa,32 t/h) and leaves the first ash cooler 5 by the upper annular header 5742 of the upper cooling zone 52. The flow of working medium in the rest ash cooler 5 is similar to the flow, and no description is repeated.

In summary, by adopting the system and the method for disposing and separating the metal oxide by the oil residue gasification filter cake, the gasification filter cake of 13t/h is subjected to reduction, harmless and recycling treatment, and finally the metal oxide of 1.69 t/h is obtained by collecting.

While embodiments of the present application have been illustrated and described above, it will be appreciated that the above-described embodiments are exemplary and should not be construed as limiting the present application. Various changes and modifications may be made to the present application without departing from the spirit and scope of the application, and such changes and modifications fall within the scope of the application as hereinafter claimed.

Claims

1. The device for incinerating and disposing the oil residue gasified filter cake comprises a drying unit (100) and a conveying and sorting unit (200) which are sequentially connected, wherein the conveying and sorting unit (200) is respectively connected with a carbon-lean incineration unit (300) and a carbon-rich incineration unit (400), and is characterized in that: the conveying and sorting unit (200) comprises a first material returning device (21), an ash conveying device (22) and a gravity separator (23) which are sequentially connected; the ash conveying device (22) comprises a gas inlet (222), a contraction section (223), a throat section (224), a diffusion section (225) and an ash discharge hole (226) from left to right, and an ash feed hole (221) is formed in the side wall of the throat section (224) and is connected with the first material returning device (21); the gravity separator (23) comprises a separator feed inlet (231), a separator separation section (232) and a separator air outlet (233) which are transversely arranged from left to right, a carbon-lean ash bucket (234) is arranged at the bottom of the separator separation section (232) and near the separator feed inlet (231), and a carbon-rich ash bucket (235) is arranged at the bottom of the separator separation section (232) and near the separator air outlet (233); the carbon-rich incineration unit (400) comprises a cyclone incinerator (4), wherein the cyclone incinerator (4) is connected with an incineration chamber (41) and a cooling chamber (42) through a connecting section (416), an ash conveying device (22) is further arranged between the carbon-rich ash hopper (235) and the incineration chamber (41), the incineration chamber (41) comprises an incineration chamber feeding section (413), a cyclone furnace conveying section (411) and a cyclone furnace combustion section (412) from top to bottom, and the incineration chamber feeding section (413) comprises a carbon-rich slag conveying channel (4131) and a residual flue gas conveying channel (4132) which are coaxially arranged; the carbon-lean incineration unit (300) comprises a fluidized bed flameless combustion furnace (3), and an ash conveying device (22) is also arranged between the carbon-lean ash bucket (234) and the fluidized bed flameless combustion furnace (3).

2. The apparatus for incineration disposal of oil sludge gasification cake according to claim 1, wherein: the bottoms of the incineration chamber (41) and the cooling chamber (42) are downwards convex from edge to center, the connecting section (416) is respectively communicated with the lower parts of the side walls of the incineration chamber (41) and the cooling chamber (42), and a slag catching pipe (417) is arranged in the connecting section (416).

3. The apparatus for incineration disposal of oil sludge gasification cake according to claim 1, wherein: the lower ends of the carbon-rich slag conveying channel (4131) and the residual flue gas conveying channel (4132) are provided with swirl plates (4133), an incineration chamber air inlet (414) is further formed in the upper position of the side wall of the incineration chamber (41), the upper space of the incineration chamber air inlet (414) is a cyclone furnace conveying section (411), and the lower space is a cyclone furnace combustion section (412).

4. The apparatus for incineration disposal of oil sludge gasification cake according to claim 1, wherein: the cooling chamber (42) comprises a cooling chamber cylinder (422), an ash catching pipe (426) and a cyclone furnace flue gas outlet (427), wherein the cyclone furnace flue gas outlet (427) is arranged at the top of the cooling chamber (42), the ash catching pipe (426) is arranged at the bottom end of the cooling chamber cylinder (422) and near the cyclone furnace flue gas outlet (427), the cooling chamber cylinder (422) is of a square structure, a folding flame corner (424) is arranged at the lower part of the side wall opposite to the connecting section (416), a cooling chamber air inlet (423) is arranged above the corner of the folding flame corner (424), and a cooling chamber wet slag inlet (425) is arranged at the upper part of the cooling chamber cylinder (422) and below the ash catching pipe (426).

5. The apparatus for incineration disposal of oil sludge gasification cake according to claim 1, wherein: the bottom of the incineration chamber (41) and the bottom of the cooling chamber (42) are inclined at an angle of 2-10 degrees with the horizontal plane, a slag discharging port (415) and a cooling chamber ash discharging port (421) are respectively formed in the central low points of the bottom of the incineration chamber (41) and the bottom of the cooling chamber (42), the slag discharging port (415) is connected with a slag cooler (43), and the cooling chamber ash discharging port (421) is connected with a slag cooler (5).

6. The apparatus for incineration disposal of oil sludge gasification cake according to claim 1, wherein: the fluidized bed flameless combustion furnace (3) is connected with two stages of cyclone separators, an ash discharge port of each cyclone separator is connected with an ash cooler, the fluidized bed flameless combustion furnace (3) comprises an air chamber (31), an air distribution plate (32), a fluidized bed combustion chamber (33) and a combustion chamber flue gas outlet (34) from bottom to top, the combustion chamber flue gas outlet (34) is connected with a first cyclone separator (301), an exhaust port of the first cyclone separator (301) is connected with a second cyclone separator (302), an ash discharge port of the first cyclone separator (301) is sequentially connected with an ash cooler (5) and a second material return pipe (62) of the second material return device (6) is connected with the lower part of the side wall of the fluidized bed combustion chamber (33), a discharge port (226) of an ash conveying device (22) is arranged between the lean carbon ash hopper (234) and the fluidized bed flameless combustion furnace (3) and is also connected with the lower part of the side wall of the fluidized bed combustion chamber (33), the ash discharge port (226) is connected with the fluidized bed combustion chamber (33) and the ash return pipe (62) is connected with the ash cooler (5) and the second material return pipe (6) in turn, the second material return pipe (62) is connected with the fluidized bed combustion chamber (8) and the temperature equalizer (8) is connected with the temperature equalizer (7).

7. The apparatus for incinerating and disposing of oil sludge gasification cake according to claim 5, wherein: the ash cooler (5) is cylindrical, two ends of the ash cooler are tapered, the ash cooler comprises a feeding zone (51), an upper cooling zone (52), a middle zone (53), a lower cooling zone (54) and a discharging zone (55) from top to bottom, water-cooling interlayers are arranged on the wall surfaces of the ash cooler, water-cooling wall heat exchangers (57) are respectively arranged in the inner spaces of the upper cooling zone (52) and the lower cooling zone (54), the middle zone (53) is hollow, and communicating pipes (575) for connecting the upper water-cooling wall heat exchanger and the lower water-cooling wall heat exchanger (57) are arranged outside the middle zone (53); the water-cooled wall heat exchanger (57) comprises a film water-cooled wall (573) which is vertically arranged, and the vertical projections of the film water-cooled walls (573) of the upper water-cooled wall heat exchanger and the lower water-cooled wall heat exchanger are not overlapped; or the drying unit comprises a cylindrical multi-hearth furnace dryer, a high-temperature wind generating device and a temperature equalizer, wherein a multi-hearth furnace feed inlet and a multi-hearth furnace flue gas outlet are formed in the top of the multi-hearth furnace dryer, a multi-hearth furnace ash outlet is formed in the bottom of the multi-hearth furnace dryer, a multi-hearth furnace center shaft is arranged in the center of the multi-hearth furnace center shaft, rake teeth of a multi-hearth furnace rake arm are connected to the multi-hearth furnace center shaft in a self-supporting mode, the rake teeth of the multi-hearth furnace rake arm are arranged in 3-6 layers, a heating flue gas interface is formed in the cylindrical side wall of the multi-hearth furnace dryer, the heating flue gas interface is sequentially connected with the temperature equalizer and the high-temperature wind generating device, the high-temperature wind generating device is a flue burner, and a honeycomb ceramic heat accumulator is arranged in the temperature equalizer.

8. The apparatus for incinerating and disposing of oil sludge gasification cake according to claim 7, wherein: the water-cooled wall heat exchanger (57) comprises a lower header (572), a membrane-type water-cooled wall (573) and an upper header (574) which are sequentially connected from bottom to top; an included angle of 10-40 degrees exists in the vertical direction of a membrane water wall (573) of the upper water wall heat exchanger and the lower water wall heat exchanger; or the membrane water wall comprises a long-section membrane water wall and a short-section membrane water wall, the number of water wall pipes arranged on the long-section membrane water wall is larger than that of the short-section membrane water wall, the short-section membrane water wall is uniformly distributed between two adjacent long-section membrane water walls, and each water wall pipe is distributed in the center of the ash cooler.

9. The method for incinerating and disposing the oil residue gasification filter cake is characterized in that: drying the oil residue gasification filter cake to obtain a dried filter cake at 150-350 ℃, generating smoke at 150-350 ℃ at the same time, and carrying out gravity separation on the dried filter cake to obtain carbon-rich residue and carbon-poor residue under the transportation of the smoke; the carbon-rich slag enters from the top of the incineration chamber of the cyclone incinerator under the transportation of the flue gas, the carbon-rich slag and the transportation flue gas are spirally downward and are mixed with the introduced air for combustion, liquid slag generated by combustion is discharged from the bottom of the incineration chamber, the liquid slag is changed into water-containing wet slag through direct contact cooling, the flue gas generated by the incineration chamber enters into a cooling chamber after slag capturing, the cooling chamber exchanges heat with the introduced air and the water-containing wet slag in sequence, high-temperature ash slag falling after the flue gas exchanges heat is discharged from the bottom of the cooling chamber, and the low-temperature dry slag product G2 is obtained after heat exchange cooling; the lean carbon slag enters the fluidized bed flameless combustion furnace through the delivery of the flue gas, the lean carbon slag and high-temperature low-oxygen wind are burnt in the fluidized bed flameless combustion furnace, the burnt flue gas sequentially enters the two-stage cyclone separator, the large-grain-size product T1 is separated under the action of the first-stage cyclone separator, and the product T1 is returned to the lower part of the fluidized bed flameless combustion furnace after heat exchange and temperature reduction and is mixed with the lean carbon slag.

10. The method for incineration disposal of oil sludge gasification cake according to claim 9, characterized in that: the burning temperature of the carbon-rich slag is controlled to be 850-1300 ℃, the smoke passing through the slag capturing enters the folding flame angle of the cooling chamber to be turned, and then is cooled by the air and the water-containing wet slag which are sequentially introduced, the temperature of the high-temperature ash slag which falls down after the heat exchange of the smoke is 500-650 ℃, and then enters the ash cooler to exchange heat and cool into a low-temperature dry slag product with the temperature of 50-80 ℃.