CN210215271U - Energy recovery and purification system for crude gas containing high-concentration coke powder particles - Google Patents
Energy recovery and purification system for crude gas containing high-concentration coke powder particles Download PDFInfo
- Publication number
- CN210215271U CN210215271U CN201921939653.0U CN201921939653U CN210215271U CN 210215271 U CN210215271 U CN 210215271U CN 201921939653 U CN201921939653 U CN 201921939653U CN 210215271 U CN210215271 U CN 210215271U
- Authority
- CN
- China
- Prior art keywords
- coal gas
- section
- evaporator
- energy recovery
- purification system
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Coke Industry (AREA)
Abstract
The application discloses contain high enriched fine coke granule coal gas energy recuperation and clean system includes: the system comprises a first evaporator section, a superheating section, a second evaporator section, a cyclone separator, a high-efficiency dust remover and an economizer, wherein the first evaporator section, the superheating section and the second evaporator section are sequentially connected in an upper position, a middle position and a lower position to form a waste heat boiler; the outlet of the second evaporator section is connected with a cyclone separator through a pipeline, and the coal gas centrifugally separated by the cyclone separator passes through the second evaporator section and then enters a high-efficiency dust remover and an economizer; the arrangement positions of the high-efficiency dust remover and the coal economizer can be interchanged. The application solves the problems of abrasion, corrosion, blockage and the like of the heat exchange tube at the low-temperature section in the coal gas cooling process, greatly prolongs the service life of the waste heat boiler and the economizer, and is suitable for cooling and purifying high-temperature raw coal gas produced in the fluidized bed gasification field and the air flow bed gasification field.
Description
Technical Field
The application belongs to the technical field of high-temperature dust-containing coal gas heat recovery and purification, and particularly relates to a system for recovering and purifying energy of coarse coal gas containing high-concentration coke powder particles.
Background
The energy structure of China is that more coal is used and less oil is used, so that the coal-based chemical products are produced by adopting the coal as the raw material, the dependence of China on petroleum is reduced, the energy safety is improved, and the coal gas production is an important technical support for realizing the coal-based chemical industry. At present, the coal gas is mainly produced by a fluidized bed gasification furnace and a fluidized bed gasification furnace, and the clean low-temperature coal gas obtained by dedusting and cooling energy recovery can enter a downstream working section for transformation or desulfurization and decarburization to produce qualified purified coal gas.
Cooling and purifying high-temperature crude gas rich in high-concentration dust, and performing a cooling process of a gas-divided gas ascending waste heat boiler and a gas descending chilling cooling process of an entrained flow gasifier; the fluidized bed gasification furnace is limited by a gasification principle and only has a flow of coal gas ascending waste heat boiler.
Most of the upstream waste heat boilers of the existing entrained flow gasifier adopt a circulating gas chilling and coiled pipe type and straight pipe type water-cooled wall waste heat boiler, and the circulating gas chilling and coiled pipe type and straight pipe type water-cooled wall waste heat boilers are sent to a ceramic dry dust remover after being cooled to 340 ℃. In the process configuration, because a large amount of molten slag and coke powder are carried into the coil pipe type or straight pipe type water-cooled wall waste heat boiler, the waste heat boiler is often blocked, and the heat exchange effect is influenced.
The cooling process of the upstream waste heat boiler of the existing fluidized bed gasification furnace generally passes through a high-temperature cyclone dust collector firstlyPrimarily dedusting high-temperature coal gas at 850-1050 ℃, sending the high-temperature coal gas subjected to cyclone dedusting to an air preheater and a waste heat boiler to cool to 165-280 ℃, wherein the dust concentration of the coal gas is still as high as 30-150 g/Nm3. And (3) the coal gas after the temperature of the waste boiler is cooled is sent to a downstream transformation or desulfurization and decarburization working section after being subjected to dry dedusting and water washing. The high-temperature coal gas entering the waste heat boiler contains high coal ash and high coke powder (30-150 g/Nm)3) The coal ash and coke powder particles quickly scour the fire tubes and the shell parts of the evaporation section, the overheating section and the economizer section of the waste heat boiler, so that the parts are abraded to cause the breakage of the heat exchange tube; in addition, as the temperature of the coal gas is continuously reduced along with the passing of the coal gas through the waste heat boiler, the gas speed of the coal gas is gradually reduced, and coke powder particles in the coal gas have the tendency of depositing on the surface of the heat exchanger; particularly, in the water pipe type economizer section, as the temperature of the wall of the water pipe is close to the dew point of the coal gas, dew point corrosion is caused in partial dead zones, the surface of the water pipe is corroded to be unsmooth, coal ash and coke powder in the coal gas are more easily adhered, the water pipe shell is formed into large scale dirt after a long time, the scale corrosion is further caused, and in a more serious situation, the shutdown overhaul of the waste heat boiler can be possibly caused.
In the prior art, a cooling process of a coal gas ascending waste heat boiler for a fluidized bed gasification furnace comprises a high-temperature evaporator, a superheater, a low-temperature evaporator and an economizer. Chinese utility model patent CN 208871582U discloses a novel waste heat boiler, and it adopts the novel waste heat boiler design that a necking down section of thick bamboo and a center section of thick bamboo combined together, and the fine coke mainly concentrates on a center section of thick bamboo department for dust content reduces in the waste heat boiler heat exchanger, has reduced the wearing and tearing of fine coke to heat exchanger and tube sheet. The gas temperature at the central cylinder is still higher, the efficiency of collecting coke powder at the central cylinder is still lower, and a large amount of dust still enters the heat exchanger, so that the problem that the waste heat boiler is worn by the coke powder cannot be thoroughly solved.
The chinese invention patent CN 102047038B discloses a waste heat boiler for fluidized bed coal gasification process, which comprises a high temperature evaporator, a superheater, a low temperature evaporator and an economizer, wherein the superheater, the low temperature evaporator and the economizer adopt water tube type structures, and the high temperature evaporator adopts a fire tube type structure. The heat exchanger of the integrated combined waste heat boiler still has the problems of abrasion and corrosion on the actually operated industrialized demonstration device, which shows that the fire tube at the coal gas inlet of the high-temperature evaporation section is seriously abraded; especially, the shell of the water pipe of the economizer is seriously scaled, the dew point corrosion is serious, and the parking accidents are most frequent. The above illustrates that entrained coal ash and dust in the coal gas has a significant impact on the equipment.
SUMMERY OF THE UTILITY MODEL
In view of the above disadvantages, the present application provides a system for recovering and purifying energy of raw gas containing high concentration coke powder particles.
In order to solve the technical problem, the application is realized by the following technical scheme:
a coal gas energy recovery and purification system containing high-concentration coke powder particles comprises: a first evaporator section, a superheating section, a second evaporator section, a cyclone separator, a high-efficiency dust remover and an economizer,
the first evaporator section, the overheating section and the second evaporator section are sequentially connected according to the upper position, the middle position and the lower position to form a waste heat boiler;
the high-temperature coal gas enters the first stage of the evaporator for primary cooling, then passes through the hot stage for secondary cooling, then passes through the second stage of the evaporator for tertiary cooling, and is discharged from an outlet of the evaporator;
the outlet of the second evaporator section is connected with the cyclone separator through a pipeline, and the coal gas centrifugally separated by the cyclone separator is discharged from the central pipe at the upper part of the cyclone separator, passes through the second evaporator section and then enters the high-efficiency dust remover and the economizer;
wherein the arrangement positions of the high-efficiency dust remover and the coal economizer can be interchanged.
Further, in the energy recovery and purification system for the coal gas containing the high-concentration coke powder particles, the evaporator section and the superheating section are separated by a flexible tube plate.
Further, in the energy recovery and purification system for coal gas containing high concentration coke powder particles, a fire tube for coal gas to pass through is arranged in the evaporator section, a first water flow channel for conveying boiler water is arranged between the fire tube and the shell of the evaporator section, and the water flow direction of the boiler water is opposite to the coal gas flow direction.
Further, in the energy recovery and purification system for coal gas containing high-concentration coke breeze particles, the fire tube is obliquely arranged, and a wear-resistant sleeve is arranged at the inlet of the fire tube.
Further, in the energy recovery and purification system for coal gas containing high-concentration coke powder particles, at least one section of water pipe is arranged in the superheating section, high-temperature saturated steam is introduced into the water pipe, and a flow channel between the outside of the water pipe and the shell of the superheating section is used for allowing high-temperature coal gas to pass through.
Further, in the energy recovery and purification system for the coal gas containing the high-concentration coke powder particles, an inspection hole and a manhole are further arranged on the shell of the overheating section.
Further, in the energy recovery and purification system for the coal gas containing the high-concentration coke powder particles, the evaporator second section is provided with a first tube pass and a second tube pass,
further, in the energy recovery and purification system for the coal gas containing the high-concentration coke powder particles, the upper part of the first tube pass is connected with the overheating section, and the outlet of the first tube pass is connected with the cyclone separator through a pipeline;
further, in the energy recovery and purification system for coal gas containing high-concentration coke powder particles, the lower part of the second tube pass is connected with the upper central tube of the cyclone separator, and the outlet of the second tube pass is connected with the high-efficiency dust remover or the economizer.
Further, in the energy recovery and purification system for coal gas containing high-concentration coke powder particles, a second water flow channel for conveying boiler water is further arranged between the first tube pass and the shell of the second evaporator section, wherein the water flow direction of the boiler water is opposite to the flowing direction of the coal gas.
Further, in the energy recovery and purification system for coal gas containing high-concentration coke powder particles, the second evaporator section adopts a fire tube structure.
Further, in the energy recovery and purification system for the coal gas containing the high-concentration coke powder particles, a plurality of straight-cutting double-inlet centrifugal tubes are adopted in the cyclone separator.
Further, in the energy recovery and purification system for the coal gas containing the high-concentration coke powder particles, the high-efficiency dust remover adopts a high-efficiency ceramic dust remover or a metal fiber dust remover.
Further, in the energy recovery and purification system for coal gas containing high-concentration coke powder particles, the dust content of the coal gas filtered by the high-efficiency dust remover is reduced to 10mg/Nm3The following.
Further, in the energy recovery and purification system for coal gas containing high-concentration coke powder particles, the economizer adopts a one-way fire tube structure, a third water flow channel for passing deoxygenated water is further arranged between the one-way fire tube structure and the shell of the economizer, and the flow direction of the deoxygenated water is opposite to the flow direction of the coal gas.
Further, in the energy recovery and purification system for the coal gas containing the high-concentration coke powder particles, the temperature of the coal gas at the outlet of the economizer is reduced to 160-210 ℃.
Compared with the prior art, the method has the following technical effects:
the high-efficiency multi-pipe cyclone separator and the high-efficiency dust remover are introduced in the middle link of the coal gas cooling process, so that the high-temperature dust-containing coal gas cooling and the dust removing purification are organically integrated, the coal gas cooling and the dust removing purification are not isolated, the problems of abrasion, corrosion, blockage and the like of a low-temperature section heat exchange tube in the coal gas cooling process are solved, the service lives of a waste heat boiler and an economizer are greatly prolonged, and the high-temperature multi-pipe cyclone separator and the high-efficiency dust remover are suitable for cooling and purifying high-temperature crude coal gas produced in the fluidized bed gasification. The dust concentration at the outlet of the high-efficiency dust remover can be reduced to 10mg/Nm3And the temperature of the coal gas at the outlet of the economizer can be reduced to 160-210 ℃.
Drawings
Other features, objects and advantages of the present application will become more apparent upon reading of the following detailed description of non-limiting embodiments thereof, made with reference to the accompanying drawings in which:
FIG. 1: the application discloses a structural schematic diagram of a first embodiment of a high-concentration coke powder particle-containing coal gas energy recovery and purification system;
FIG. 2: the second embodiment of the energy recovery and purification system for coal gas containing high-concentration coke powder particles is schematically shown in the structure.
Detailed Description
The conception, specific structure and technical effects of the present application will be further described in conjunction with the accompanying drawings to fully understand the purpose, characteristics and effects of the present application.
Example one
As shown in fig. 1, the energy recovery and purification system for coal gas containing high concentration coke powder particles of the embodiment includes: the system comprises a first evaporator section 1, a superheating section 2, a second evaporator section, a cyclone separator 5, a high-efficiency dust remover 6 and an economizer 7, wherein the first evaporator section 1, the superheating section 2 and the second evaporator section are sequentially connected in an upper position, a middle position and a lower position to form a waste heat boiler; the high-temperature coal gas is subjected to primary cooling from the first section 1 of the evaporator, then subjected to secondary cooling through the hot section 2, and then subjected to tertiary cooling through the second section of the evaporator and then discharged from an outlet of the evaporator; the outlet of the second evaporator section is connected with the cyclone separator 5 through a pipeline, and the coal gas centrifugally separated by the cyclone separator 5 is discharged from the central pipe at the upper part of the cyclone separator 5, passes through the second evaporator section and then sequentially enters the high-efficiency dust remover 6 and the economizer 7.
A fire tube for coal gas to pass through is arranged in the evaporator section 1, wherein a first water flow channel for conveying boiler water is arranged between the fire tube and the shell of the evaporator section 1, and the water flow direction of the boiler water is opposite to the flowing direction of the coal gas. As the temperature of coal gas at the inlet of the fire tube of the first section 1 of the evaporator reaches 850-1050 ℃, the gas velocity at the coal gas inlet is very high, in order to reduce the abrasion problem of the fire tube inlet caused by high gas velocity, the fire tube is preferably arranged in an inclined mode, and a wear-resistant sleeve is arranged at the inlet of the fire tube.
In the embodiment, the high-temperature raw gas from the fluidized bed gasification furnace or the entrained flow gasification furnace has the temperature of 850-1050 ℃, firstly enters the pipe box of the section 1 of the evaporator at the topmost part of the waste heat boiler, the high-temperature gas is distributed to the fire pipes through the pipe box, the flow velocity of the high-temperature gas entering the fire pipes is controlled to be 15-25 m/s, under the condition of the flow velocity, the wear-resistant sleeve is arranged at the position of the inlet pipe bundle of the fire pipes, and the gas is not easy to wear rapidly after being rectified by the wear-resistant sleeve and then linearly passes through the. The high-temperature coal gas carries out convection heat transfer on boiler water through the fire tube, a steam-water mixture is formed on the shell side, the steam-water mixture is saturated steam, and the pressure grade can be different specifications from 1.0Mpa to 5.0Mpa, the steam temperature from 260 ℃ to 450 ℃ and the like according to user requirements. The high temperature coal gas in the fire tube can be reduced to about 650 ℃ at the outlet of the first section 1 of the evaporator.
In this embodiment, the pressure range of the high-temperature raw gas may be 0.1Mpa to 5.0 Mpa.
Further, since the metal temperature of the tube wall of the fire tube of the evaporator section 1 is high, and the metal wall temperature of the evaporator shell is low, in order to eliminate the problem of inconsistent expansion between the fire tube and the shell and the problem of local enrichment of the top of water vapor, the evaporator section 1 and the superheat section 2 are separated by a flexible tube plate.
Further, the high-temperature coal gas at about 650 ℃ enters the superheating section 2, wherein at least one section of water pipe is arranged in the superheating section 2, high-temperature saturated steam is introduced into the water pipe, and a flow channel between the outside of the water pipe and the shell of the superheating section 2 is used for allowing the high-temperature coal gas to pass through.
The water pipe is preferably of a horizontal coil pipe type structure, and by adopting the coil pipe type structure, high-temperature superheated steam is not enriched at the upper connecting pipe plate, so that local overheating is not easily caused, and the problem of local high-temperature burnout is further caused; in addition, the structure can fully utilize space, and the equipment cost is lower.
The shell of the overheating section 2 is also provided with an inspection hole and a manhole, the dust deposition condition in the shell can be observed, and an ash blowing port or a vibrator is arranged, so that the dust deposition can be timely treated by means when the dust deposition occurs. The temperature of the high-temperature coal gas discharged from the overheating section 2 is reduced to about 550 ℃.
In this embodiment, the evaporator second segment adopts a fire tube structure, when the gas flows to the fire tube structure, the temperature is already reduced to about 550 ℃, and the gas velocity of the gas is reduced by about 40% in the same flow area, so that the coal ash and the coke breeze entrained in the gas are easy to deposit on the wall surface to cause ash deposition. Therefore, in this embodiment, the evaporator second stage preferably adopts a two-pass fire tube structure (the first pass 3 and the second pass 4) as described below, so that the gas velocity in the fire tube can be increased, ash deposition is not easy, and the convection heat transfer effect is better. The outlet of the first tube pass 3 is connected with a cyclone separator 5, and the dedusted semi-high temperature coal gas enters the second tube pass 4 of the second section of the evaporator to further exchange heat with boiler water.
In the embodiment, the evaporator second section is provided with a first tube pass 3 and a second tube pass 4, the upper part of the first tube pass 3 is connected with the superheating section 2, and the outlet of the first tube pass 3 is connected with the cyclone separator 5 through a pipeline; the lower part of the second tube pass 4 is connected with the upper central tube of the cyclone separator 5, and the outlet of the second tube pass 4 is connected with the high-efficiency dust remover 6 or the coal economizer 7.
A second water flow channel for conveying boiler water is further arranged between the first tube pass 3 and the shell of the second evaporator section, wherein the water flow direction of the boiler water is opposite to the flowing direction of the coal gas. And the dedusted semi-high temperature coal gas enters a second tube pass 4 of the second section of the evaporator to further exchange heat with boiler water.
Further, high-temperature coal gas at about 550 ℃ enters the first tube pass 3, wherein the upper part of the first tube pass 3 is directly welded with a tube box at the lower part of the superheat section 2, and the coal gas is distributed into each fire tube in the first tube pass 3 through the tube box. After the coal gas flows through the first tube pass 3 from top to bottom, the temperature is reduced to about 400 ℃ and the coal gas is discharged out of the first tube pass 3. The outlet of the first tube side 3 is connected with a high-efficiency multi-tube cyclone separator 5 through a pipeline. Wherein the pipe preferably assumes a wear-resistant lining construction.
A plurality of straight-cutting double-inlet centrifugal tubes are adopted in the cyclone separator 5, so that the operation elasticity is high and the separation efficiency is high; and the vortex core of the structure has small deformation, and the airflow is not easy to short circuit, so the structure is firstly used in the field of dry dedusting of fluidized beds and airflow beds.
The medium temperature coal gas at about 400 ℃ enters the cyclone separator 5 along the tangential rectangular port, and the coal ash and the coke separated by the cyclone separator 5 are conveyed out of the boundary area through the lower ash bucket and the ash pump. The dust content of the medium-temperature coal gas after centrifugal dust removal by the cyclone separator 5 is greatly reduced, and the coal gas is discharged from the central tube at the upper part of the cyclone separator 5. Because the dust in the coal gas is reduced, the scouring to the equipment is reduced, and the service life of the subsequent equipment is prolonged. The medium temperature coal gas enters a cyclone separator 5 to remove coke powder with larger particles, and the cyclone dust removal efficiency is greatly improved due to the lower temperature of the medium temperature coal gas.
The central pipe of the cyclone separator 5 is connected with the lower pipe box of the second pipe pass 4 through a pipeline, the medium temperature coal gas flows through the second pipe pass 4 of the second section of the evaporator of the waste heat boiler from bottom to top, the heat exchange with the boiler water on the shell side is further carried out in the period, and the temperature of the medium temperature coal gas after the heat exchange is reduced to about 260 ℃ and then is discharged out of the waste heat boiler.
In this embodiment, the gas at about 260 ℃ enters the high-efficiency dust remover 6, and in this embodiment, the high-efficiency dust remover 6 comprises a dust remover cylinder and its accessories (a clean gas chamber, a raw gas chamber, and an ash bucket), a filtering system, a pulse blowing system, a diffusing system, and the like. In view of the high operating temperature of the dust remover, the high-efficiency dust remover 6 is preferably made of a material which is wear-resistant, high-temperature-resistant and not easy to crack, for example, the high-efficiency dust remover 6 is a high-efficiency ceramic dust remover or a metal fiber dust remover. The main gas pipe is distributed into the high-efficiency dust remover 6 and enters the gas chamber, the dust with larger particles naturally settles under the action of gravity and enters the ash bucket, and the dust with smaller particles rises along with the gas. When the coal gas passes through the filter bag, the dust is blocked on the outer surface of the filter bag, and the coal gas is purified.
In this embodiment, the high-efficiency dust collector 6 has a high filtering wind speed and an obvious filtering effect, and the dust content of the coal gas filtered by the high-efficiency dust collector 6 is reduced to 10mg/Nm3The following. Wherein the content of the first and second substances,the coal ash and dust in the coal gas are basically collected.
Furthermore, the dust content is less than or equal to 10mg/Nm3The purified coal gas is connected with the coal economizer 7 through an outlet at the upper part of the high-efficiency dust remover 6. The coal economizer 7 adopts a one-way fire tube structure, and the ash removal effect is more obvious. The existing economizer of the waste heat boiler generally adopts a water pipe structure. Due to the fact that the coal gas temperature is reduced, the coal gas speed is reduced, coal ash and coke powder are easy to deposit on a water pipe shell, and in addition, liquid water is easy to appear at the position where the coal gas is close to a dew point, so that dew point corrosion and scale corrosion are caused.
This application adopts the firetube structure, and intraductal coal gas is in the torrent state, is difficult for the deposition for the heat exchange tube life-span is strengthened greatly.
A third water flow channel for the deoxygenated water at about 150 ℃ to pass through is further arranged between the one-way fire tube structure and the shell of the economizer 7, wherein the flow direction of the deoxygenated water is opposite to the flow direction of the coal gas. Coal gas at the outlet of the economizer 7 can be reduced to about 160-210 ℃, and the cooled synthetic gas enters a downstream transformation or desulfurization and decarburization working section through hot water washing or cold water washing.
The fire tube structure can be made of carbon steel or alloy steel, and the economizer 7 is better in low-temperature corrosion resistance effect if the alloy steel is adopted.
Furthermore, the coal economizer 7 adopts a reversing coal economizer structure, so that the problem of dust accumulation in the coal economizer 7 is further solved, and the possibility of dew point corrosion and under-deposit corrosion is effectively prevented.
Example two
As shown in fig. 2, the present embodiment is different from the first embodiment in that: the coal gas passing through the second tube pass 4 of the second evaporator section firstly enters the economizer 7 and then enters the high-efficiency dust remover 6 for treatment.
And the cooled synthesis gas enters a downstream transformation or desulfurization and decarburization working section through hot water washing or cold water washing.
In this embodiment, about 260 ℃ coal gas of the second tube pass 4 of the second evaporator section may first enter the economizer 7 to exchange heat with about 150 ℃ deoxygenated water, and 160-210 ℃ coal gas after heat exchange enters the high-efficiency dust remover 6. According to the flow configuration, although the coal gas entering the economizer 7 has high dust content and may influence the service life of the economizer 7, the filter element of the high-efficiency dust remover can be made of cheap polymers, so that the manufacturing cost is reduced.
In the practical application process, the flow collocation of the first embodiment or the second embodiment is specifically selected, and the cost and the stability can be comprehensively determined.
The high-efficiency multi-pipe cyclone separator and the high-efficiency dust remover are introduced in the middle link of the coal gas cooling process, so that the dust concentration at the outlet of the high-efficiency dust remover can be reduced to 10mg/Nm3The temperature of the coal gas at the outlet of the economizer can be reduced to 160-210 ℃, so that the problems of abrasion, corrosion, blockage and the like of a heat exchange tube at a low-temperature section in the coal gas cooling process are solved, the service lives of the waste heat boiler and the economizer are greatly prolonged, and the high-temperature coarse coal gas cooling and purifying device is suitable for cooling and purifying high-temperature coarse coal gas produced in the fluidized bed gasification field and the fluidized bed gasification field. Therefore, the application prospect is wide.
It should be understood that although the terms first, second, third, etc. may be used in the embodiments of the present application to describe certain components, these components should not be limited by these terms. These terms are only used to distinguish one component from another. For example, a first certain component may also be referred to as a second certain component, and similarly, a second certain component may also be referred to as a first certain component without departing from the scope of embodiments herein.
It is also noted that the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a good or system that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such good or system. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other like elements in a commodity or system that includes the element.
The above embodiments are merely to illustrate the technical solutions of the present application and are not limitative, and the present application is described in detail with reference to preferred embodiments. It will be understood by those skilled in the art that various modifications and equivalent arrangements may be made in the present invention without departing from the spirit and scope of the present invention and shall be covered by the appended claims.
Claims (14)
1. A coal gas energy recovery and purification system containing high-concentration coke powder particles, which is characterized in that,
the method comprises the following steps: a first evaporator section, a superheating section, a second evaporator section, a cyclone separator, a high-efficiency dust remover and an economizer,
the first evaporator section, the overheating section and the second evaporator section are sequentially connected according to the upper position, the middle position and the lower position to form a waste heat boiler;
the high-temperature coal gas enters the first stage of the evaporator for primary cooling, then passes through the hot stage for secondary cooling, then passes through the second stage of the evaporator for tertiary cooling, and is discharged from an outlet of the evaporator;
the outlet of the second evaporator section is connected with the cyclone separator through a pipeline, and the coal gas centrifugally separated by the cyclone separator is discharged from the central pipe at the upper part of the cyclone separator, passes through the second evaporator section and then enters the high-efficiency dust remover and the economizer;
wherein the arrangement positions of the high-efficiency dust remover and the coal economizer can be interchanged.
2. The energy recovery and purification system for coal gas containing high concentration coke breeze particles as claimed in claim 1, wherein said evaporator section is separated from said superheater section by a flexible tube sheet.
3. The energy recovery and purification system for coal gas containing high concentration coke powder particles as claimed in claim 1, wherein a fire tube for passing coal gas is provided in the evaporator section, wherein a first water flow channel for transporting boiler water is provided between the fire tube and the shell of the evaporator section, wherein the boiler water flows in a direction opposite to the flow direction of coal gas.
4. The energy recovery and purification system for coal gas containing high concentration coke breeze particles as claimed in claim 3, wherein the fire tube is disposed obliquely, wherein a wear-resistant sleeve is disposed at the inlet of the fire tube.
5. The energy recovery and purification system for coal gas containing high concentration coke powder particles as claimed in any one of claims 1 to 4, wherein at least one section of water pipe is arranged in the superheating section, wherein high temperature saturated steam is introduced into the water pipe, and a flow passage between the outside of the water pipe and the shell of the superheating section is passed through by high temperature coal gas.
6. The energy recovery and purification system for coal gas containing high concentration coke powder particles as claimed in claim 5, wherein the shell of the superheating section is further provided with an inspection hole and a manhole.
7. The energy recovery and purification system for coal gas containing high concentration coke breeze particles as claimed in claim 1, 2, 3 or 4, wherein said evaporator two-stage is provided with a first tube side and a second tube side,
wherein the upper part of the first tube pass is connected with the overheating section, and the outlet of the first tube pass is connected with the cyclone separator through a pipeline;
the lower part of the second tube pass is connected with the upper central tube of the cyclone separator, and the outlet of the second tube pass is connected with the high-efficiency dust remover or the coal economizer.
8. The energy recovery and purification system for coal gas containing high concentration coke powder particles as claimed in claim 7, wherein a second water flow channel for conveying boiler water is further provided between the first tube pass and the shell of the evaporator two-stage, wherein the water flow direction of the boiler water is opposite to the coal gas flow direction.
9. The energy recovery and purification system for coal gas containing high concentration coke breeze particles as claimed in claim 7, wherein the evaporator two-stage is of fire tube structure.
10. The energy recovery and purification system for coal gas containing high concentration coke powder particles as claimed in claim 1, 2, 3 or 4, wherein the cyclone separator is internally provided with a plurality of straight-cut double-inlet centrifugal tubes.
11. The energy recovery and purification system for coal gas containing high concentration coke breeze particles as claimed in claim 1, wherein the high efficiency dust collector is a high efficiency ceramic dust collector or a metal fiber dust collector.
12. The energy recovery and purification system for coal gas containing high concentration coke powder particles as claimed in claim 1, 2, 3, 4 or 11, wherein the dust content of the coal gas filtered by the high efficiency dust collector is reduced to 10mg/Nm3The following.
13. The energy recovery and purification system for coal gas containing high concentration coke powder particles as claimed in claim 1, 2, 3, 4 or 11, wherein the economizer adopts a one-way fire tube structure, and a third water flow channel for passing oxygen-removed water is further provided between the one-way fire tube structure and the shell of the economizer, wherein the oxygen-removed water flows in a direction opposite to the flowing direction of the coal gas.
14. The energy recovery and purification system for coal gas containing high-concentration coke breeze particles as claimed in claim 1, 2, 3, 4 or 11, wherein the temperature of the coal gas at the outlet of the economizer is reduced to 160-210 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921939653.0U CN210215271U (en) | 2019-11-08 | 2019-11-08 | Energy recovery and purification system for crude gas containing high-concentration coke powder particles |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921939653.0U CN210215271U (en) | 2019-11-08 | 2019-11-08 | Energy recovery and purification system for crude gas containing high-concentration coke powder particles |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210215271U true CN210215271U (en) | 2020-03-31 |
Family
ID=69921584
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921939653.0U Active CN210215271U (en) | 2019-11-08 | 2019-11-08 | Energy recovery and purification system for crude gas containing high-concentration coke powder particles |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210215271U (en) |
-
2019
- 2019-11-08 CN CN201921939653.0U patent/CN210215271U/en active Active
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| AU2012362082B2 (en) | Biomass syngas purification process under negative pressure for producing oil and system configuration thereof | |
| WO2009143700A1 (en) | Waste heat boiler for coal gasification of fluidized bed | |
| CN101701702A (en) | Waste incineration heat recovery boiler | |
| CN111649314A (en) | Box structure of natural circulation ferrosilicon waste heat boiler | |
| AU2012362081B2 (en) | Biomass syngas purification process under positive pressure for producing oil and system configuration thereof | |
| CN210215271U (en) | Energy recovery and purification system for crude gas containing high-concentration coke powder particles | |
| CN111578723A (en) | Metallurgical high temperature dust-containing waste gas treatment system | |
| CN112779061A (en) | Energy recovery and purification system for crude gas containing high-concentration coke powder particles | |
| CN217358109U (en) | Device for recovering waste heat and dust in high-dust flue gas in metallurgical zinc-containing ash disposal | |
| CN205388305U (en) | Novel low temperature second grade economizer | |
| CN109701323A (en) | The axis stream Combined dust removal system and method for the high ash-laden gas of high temperature | |
| CN202450060U (en) | Novel coke oven gas washing and cooling device | |
| CN212377955U (en) | Box structure of natural circulation ferrosilicon waste heat boiler | |
| CN211713030U (en) | Venturi cooling scrubber | |
| CN114184055A (en) | Cement kiln bypass air discharge waste heat boiler | |
| CN205761846U (en) | A kind of high efficiency cyclonic dust collector for pulverized coal pyrolysis | |
| CN2795210Y (en) | Gas sensible heat recorery device | |
| CN218480602U (en) | Waste heat boiler for fluidized bed gasification process | |
| CN108517227B (en) | Industrial gas preparation system and industrial gas preparation method | |
| CN212566916U (en) | Metallurgical high temperature dust-containing waste gas treatment system | |
| CN114395424A (en) | Waste heat boiler for fluidized bed gasification process | |
| CN214619468U (en) | Waste heat boiler for electric furnace | |
| CN2073082U (en) | Heat exchanger with dust-collection | |
| CN213578801U (en) | Cement kiln tail exhaust-heat boiler | |
| CN215480760U (en) | High-temperature gas purification and recovery equipment |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |