CN210560258U - Ethylene device burnt gas resource utilization and deep purification device - Google Patents
Ethylene device burnt gas resource utilization and deep purification device Download PDFInfo
- Publication number
- CN210560258U CN210560258U CN201921245235.1U CN201921245235U CN210560258U CN 210560258 U CN210560258 U CN 210560258U CN 201921245235 U CN201921245235 U CN 201921245235U CN 210560258 U CN210560258 U CN 210560258U
- Authority
- CN
- China
- Prior art keywords
- coke
- main pipe
- pipe
- conveying main
- pipeline
- 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
Landscapes
- Treating Waste Gases (AREA)
Abstract
The utility model discloses an ethylene device burnt gas resource utilization and deep purification device, which comprises a conveying main pipe, wherein the conveying main pipe is divided into a front-section conveying main pipe and a rear-section conveying main pipe, one end of the front-section conveying main pipe is communicated with a plurality of pyrolysis furnaces, the other end of the front-section conveying main pipe is communicated with one end of the rear-section conveying pipe, the other end of the rear-section conveying main pipe is communicated with a boiler, and the outlet of the boiler is communicated with a desulfurizing tower; the inlet of the coke catching pipeline is communicated with the joint of the front-section conveying main pipe and the rear-section conveying main pipe, and the inlet of the coke catching pipeline is higher than the outlet of the coke catching pipeline; and the inlet of the dust-removing and coke-catching device is communicated with the outlet of the coke-catching pipeline.
Description
Technical Field
The utility model belongs to ethylene device burnt gas purification field, concretely relates to ethylene device burnt gas resource utilization and deep purification device.
Background
Ethylene is an important basic raw material of modern petrochemical industry, and at present, 90 percent of industrial ethylene is obtained by cracking light hydrocarbon and petroleum fraction in an ethylene cracking furnace through a steam cracking technology, and the ethylene cracking furnace is core equipment of an ethylene production device.
In the cracking process, the light hydrocarbon and petroleum fraction not only undergo cracking reaction to produce main reactions such as ethylene and propylene, but also undergo secondary reaction to produce polymerized coke. Coke is conglomerated and adhered to the inner wall of the furnace tube, which not only affects the heat transfer effect and the product yield, but also increases the temperature of the tube wall, increases the pressure drop and improves the reaction energy consumption. Therefore, the ethylene cracking must be carried out with periodical decoking measures. Current ethylene cracking operations therefore include both cracking and decoking operations.
In the decoking process of the ethylene cracking furnace, a large amount of high-temperature coke-burning gas can be discharged, the temperature of the high-temperature coke-burning gas reaches over 500 ℃, and a large amount of energy is carried. The main components of the coke-burning gas are water vapor and air, and besides the main components, the coke-burning gas also contains almost all gas pollutant types such as particulate matters, sulfur, CO, NOx, VOC (benzene, heterocycle and organic sulfur), malodorous gas and the like. Wherein, the main component of the solid particles is semicoke, and the solid particles have high calorific value.
At present, the ethylene cracking device generally adopts a coke burning tank method, and after a part of solid particles and organic matters are removed, the ethylene cracking device is directly emptied.
The treatment method consumes a large amount of water resources, generates a large amount of slurry wastewater, cannot thoroughly eliminate stink, and cannot remove water-insoluble organic matters such as CO, NOx and the like. Although, the discharge is intermittent, the pollution is serious.
Patent CN104117264 provides a method for controlling the depth of pollutants in a coke-burning gas on the basis of a coke-burning tank, which comprises the following steps:
(1) and (4) removing solid particles in the coke-burning gas by rotary separation.
(2) And (4) washing, absorbing and cooling the odor pollutants carried in the coke-burning gas.
(3) Spraying, cyclone absorbing and cooling.
(4) And (4) regenerating the rich solution.
The patented technology does provide more effective removal of solid particles and a portion of malodorous contaminants than conventional coke drums. However, this patent suffers from the following drawbacks:
1) the patent adopts water quenching cooling (cooling by water evaporation), consumes a large amount of water resources, wastes a large amount of heat energy contained in the burnt gas
2) The particulate matter removal is not thorough: only can remove particles with large particle size but can not remove particles with particle size less than 2.5 mu m
3) The process is long, the absorption liquid needs to be recycled, the energy consumption is high, and no specific absorption liquid regeneration scheme is provided in the patent.
4) The composition of the components of the absorption liquid and the method of regeneration of the absorption liquid are not described in the scheme.
5) CO, NOx, and insoluble VOCs that cannot be removed.
SUMMERY OF THE UTILITY MODEL
The utility model aims at present burning burnt gas purification treatment's technical bottleneck and defect, provide an ethylene device burns burnt gas changing waste into valuables's utilization and deep purification device, under the condition that does not increase water resource consumption promptly, rely on the heat energy that present facility fully retrieved burnt gas, realize the deep purification of burning burnt gas simultaneously, reach the purifier that all pollutants all up to standard or even ultra-clean discharged.
The utility model provides a technical scheme as follows:
the utility model provides an ethylene unit burnt gas resource utilization and deep purification device, includes:
the conveying main pipe is divided into a front-section conveying main pipe and a rear-section conveying main pipe, one end of the front-section conveying main pipe is communicated with a plurality of pyrolysis furnaces, the other end of the front-section conveying main pipe is communicated with one end of the rear-section conveying pipe, the other end of the rear-section conveying main pipe is communicated with a boiler, a pin removal reactor is arranged in the boiler, and an outlet of the boiler is communicated with a desulfurizing tower;
the inlet of the coke catching pipeline is communicated with the joint of the front-section conveying main pipe and the rear-section conveying main pipe, and the inlet of the coke catching pipeline is higher than the outlet of the coke catching pipeline;
and the inlet of the dust-removing and coke-catching device is communicated with the outlet of the coke-catching pipeline.
In the technical scheme, the burnt gas generated by the pyrolysis furnace is sent into the burnt gas conveying main pipe at a high speed, part of the burnt gas enters the coke catching pipeline after passing through the front-section conveying main pipe under the action of inertia, and the burnt gas contains solid semi-coke particles and large-particle solid semi-coke particles with large inertia, so the large-particle semi-coke particles can more easily enter the coke catching pipeline and enter the dust removal coke catcher through the coke catching pipeline, and the small-particle solid semi-coke particles are carried by the burnt gas and sent into the boiler to be combusted as air distribution. In the process, semicoke solid particles, VOC organic matters and the like contained in the coke-burning gas release heat through combustion and are simultaneously converted into CO2And H2O, in which organic sulfur is converted to SO by combustion2，SO2The desulfurization tower of the boiler is used for removing NOx organic matters, and the denitration reactor of the boiler is used for removing NOx organic matters, so that all pollutants in the burnt gas are thoroughly purified.
Preferably, the dust and coke catcher comprises:
the coke particle discharging device comprises a shell, wherein the bottom of the shell is provided with a coke particle discharging port, and the coke particle discharging port is provided with an ash storage discharging valve;
the porous interlayer surrounds the bottom of the shell and divides the shell into two parts, namely an upper ash storage space and a lower condensate space;
the condensate conveying pump is communicated with the lower condensate space through a condensate discharging pipe, and a condensate discharging valve is arranged on the condensate discharging pipe.
Further, preferably, the shell is a shell with a conical bottom, the included angle of the conical bottom of the shell is 30-90 degrees, the porosity of the porous interlayer is 50-80%, and the pore size of the porous interlayer is 20-200 μm.
In the technical scheme, the collected dust of the dust and coke removing and catching device is discharged and recycled periodically through an ash storage discharge valve; and the possible condensate is sent into the rear-section conveying main pipe again through the condensate discharge valve and the condensate conveying pump to be vaporized at high temperature and then sent into the boiler to be combusted.
Preferably, a primary air distribution pipe and a tertiary air distribution pipe are arranged at the inlet of the boiler;
the rear section conveying main pipe is respectively communicated with the primary air distribution pipe and the tertiary air distribution pipe, a primary air distribution valve is arranged at the primary air distribution pipe, and a tertiary air distribution valve is arranged at the tertiary air distribution pipe.
In the technical scheme, the burnt gas enters a hearth in two paths, and one part of the burnt gas is mixed with primary air through a primary air distribution pipe and enters the hearth as primary air; the other part of the air enters the hearth as tertiary air distribution through a tertiary air distribution pipe. The primary air distribution quantity of the coke-burning gas is based on that under the condition of keeping the total primary air quantity basically unchanged, the primary air distribution temperature is increased to 300-350 ℃, the ignition heat of coal fuel is reduced, and the ignition position is advanced, so that the effects of increasing the ignition speed and the ignition stability of pulverized coal are achieved, the operation condition of a boiler is improved, and simultaneously, the air distribution quantity can be reduced, and the load of a fan is reduced.
A small amount of residual burnt gas after primary air distribution is used as tertiary air distribution high-speed jet flow to enter the boiler, so that the fluidization effect of the pulverized coal in the boiler and the complete combustion of the residual pulverized coal are improved.
Preferably, the front-section conveying main pipe is a horizontal conveying pipeline, and an included angle between the front-section conveying main pipe and the rear-section conveying main pipe is 90 degrees;
the coke catching pipeline is communicated with the front section conveying main pipe through a horizontal connecting pipe extending out of the front section conveying main pipe;
the coke capturing pipeline is communicated with the dust and coke collecting device through a vertical connecting pipe, and the vertical connecting pipe is perpendicular to the horizontal connecting pipe.
Preferably, the coke catching pipeline is an arc pipeline or a straight pipeline;
the central angle of the arc-shaped pipeline is 45-90 degrees;
the inner diameter of the coke catching pipeline is 1-2 times of the inner diameter of the conveying main pipe;
the diameter of the vertical connecting pipe is the same as the inner diameter of the coke capturing pipeline;
the curvature radius of the arc-shaped pipeline is 2-10 times of the inner diameter of the arc-shaped pipeline;
the length of horizontal connecting pipe and the length of vertical connecting pipe are 0 ~ 500 mm.
Preferably, a plurality of pyrolysis furnaces are respectively communicated with the front-section conveying main pipe through corresponding conveying branch pipes, and branch pipe stop valves are arranged on the conveying branch pipes.
The utility model provides a pair of ethylene device burnt gas utilization and deep purification device can bring following beneficial effect:
1) the utility model discloses a utilization of ethylene device burnt gas changing waste into valuables and deep purification device possess burnt gas pipeline and the arc of specific trend and catch the bend, through hierarchical high temperature air distribution, reduce the air distribution energy consumption of boiler, improve the combustion performance of boiler, realized the utilization of the resource of burning burnt gas, can retrieve the heat energy more than 70% in the burnt gas.
2) The utility model discloses an ethylene unit burnt gas resource utilization and deep purification device have adopted the high temperature decoking ware that gathers dust of special construction, can reach the purpose of collecting dry dust and the dry powder semicoke granule after retrieving can regard as the fuel to use.
3) The utility model discloses ethylene unit burnt gas resource utilization and deep purification device are one set of purifier of many pyrolysis furnaces sharing, and the pollutant can reach the ultra-clean emission in the purification back burnt gas, realizes the thorough purification to all pollutants in the burnt gas.
Drawings
The features and advantages of the present invention and the manner of attaining them will be further described in the following detailed description of the preferred embodiments of the invention when considered in conjunction with the accompanying drawings.
FIG. 1 is a schematic view of the process of recycling and purifying the coke-burning gas in the ethylene plant and the deep purification plant of the present invention,
FIG. 2 is a schematic view of a flow of recycling of coke-burning gas in an ethylene plant and energy recovery and purification of coke-burning gas in a deep purification plant using a straight pipeline;
the reference numbers illustrate:
1-dust removal coke catcher, 1.1-upper ash storage space, 1.2-lower condensate space, 1.3-porous interlayer, 1.4-ash storage discharge valve, 1.5-condensate discharge valve, 2-arc pipeline, 21-straight pipeline, 31-front section conveying main pipe, 32-rear section conveying main pipe, 4-conveying branch pipe, 5-branch pipe cut-off valve, 6-condensate conveying pump, 7-horizontal connecting pipe, 8-vertical connecting pipe, 9-pyrolysis furnace, 10-pin removal reactor, 11-boiler, 12-tertiary air distribution pipe, 13-primary air distribution pipe, 14-desulfurizing tower, 15-tertiary air distribution valve and 16-primary air distribution valve.
Detailed Description
In order to more clearly illustrate embodiments of the present invention or technical solutions in the prior art, specific embodiments of the present invention will be described below with reference to the accompanying drawings. It is obvious that the drawings in the following description are only examples of the invention, and that for a person skilled in the art, other drawings and embodiments can be obtained from these drawings without inventive effort.
For the sake of simplicity, the drawings only schematically show the parts relevant to the present invention, and they do not represent the actual structure of the product.
The utility model provides a resource utilization and deep purification device and technology with an ethylene device burnt gas changing waste into valuables rely on the heat energy of the present facility abundant recovery burnt gas promptly not increasing water resource consumption, realize the deep purification of burnt gas simultaneously, reach all pollutants and all reach standard or even ultra-clean emission.
[ example 1 ]
As shown in fig. 1, the ethylene plant burnt gas resource utilization and deep purification device comprises: the conveying main pipe is divided into a front-section conveying main pipe 31 and a rear-section conveying main pipe 32, one end of the front-section conveying main pipe 31 is communicated with the plurality of pyrolysis furnaces 9, the other end of the front-section conveying main pipe 31 is communicated with one end of the rear-section conveying pipe, the other end of the rear-section conveying main pipe 32 is communicated with the boiler 11, the outlet of the boiler 11 is communicated with a desulfurizing tower 14, and a pin removal reactor 10 is arranged in the boiler 11;
ethylene device burnt gas resource utilization and deep purification device still include: the inlet of the coke catching pipeline is communicated with the joint of the front-section conveying main pipe 31 and the rear-section conveying main pipe 32, and the inlet of the coke catching pipeline is higher than the outlet of the coke catching pipeline;
ethylene device burnt gas resource utilization and deep purification device still include: and the inlet of the dust-removing and coke-catching device 1 is communicated with the outlet of the coke-catching pipeline.
As shown in FIG. 1, the coke-burning gas of the pyrolysis furnace 9 with 20Kpag to 50Kpag is sent into a coke-burning gas delivery main pipe at a high speed, part of the coke-burning gas enters a coke-catching pipeline after passing through a front-segment delivery main pipe 31 under the action of inertia, and as the coke-burning gas contains solid semi-coke particles and large-particle solid semi-coke particles have large inertia, the large-particle semi-coke particles can more easily enter the coke-catching pipeline and enter a dust-removing coke catcher 1 through the coke-catching pipeline for dust removal, and the small-particle solid semi-coke particles are entrained by the coke-burning gas and sent into a boiler 11 for air distribution and combustion. In the process, semicoke solid particles, VOC organic matters and the like contained in the coke-burning gas release heat through combustion and are simultaneously converted into CO2And H2O, in which organic sulfur is converted to SO by combustion2，SO2NOx organic matters are removed through a desulfurizing tower 14 arranged in the boiler, and the denitration reactor 10 arranged in the boiler is used for removing the NOx organic matters, so that all pollutants in the burnt gas are thoroughly purified.
The VOC in the purified coke-burning gas is 0mg/Nm3CO is 0mg/Nm3Dust: less than 5mg/Nm3If the desulfurization and denitrification system of the boiler 11 itself is an ultra-clean exhaust system, NOx in the purified coke-burning gas: less than 50mg/Nm3SOx is less than 35mg/Nm3。
[ example 2 ]
As shown in fig. 1, the present embodiment further discloses, on the basis of embodiment 1, a dust-removing and coke-collecting device 1, which specifically includes:
the coke particle discharging device comprises a shell, wherein the shell is a shell with a conical bottom, the conical bottom included angle of the conical bottom of the shell is 30-90 degrees, the bottom of the shell is provided with a coke particle discharging port, and an ash storage discharging valve 1.4 is arranged at the coke particle discharging port;
the shell comprises a porous interlayer 1.3, the porous interlayer 1.3 surrounds the conical bottom of the shell, the shell is divided into two parts by the porous interlayer 1.3, namely an upper ash storage space 1.1 and a lower condensate space 1.2, the void ratio of the porous interlayer 1.3 is 50% -80%, and the pore size of the porous interlayer 1.3 is 20-200 mu m.
The condensate conveying pump 6 is communicated with the lower condensate space 1.2 through a condensate discharging pipe, and a condensate discharging valve 1.5 is arranged on the condensate discharging pipe.
In the embodiment, the collected dust of the dust and coke collector 1 is discharged and recycled periodically through the dust storage discharge valve 1.4; and the possible condensate is sent to the rear-section conveying main pipe 32 again through the condensate discharging valve 1.5 and the condensate conveying pump 6 to be vaporized at high temperature and then sent to the boiler 11 to be combusted.
[ example 3 ]
As shown in fig. 1, in this embodiment, on the basis of embodiment 2, embodiment 2 further includes:
a plurality of pyrolysis furnaces 9 communicate with the front section conveying main pipe 31 through the conveying branch pipes 4 corresponding to the pyrolysis furnaces respectively, the conveying branch pipes 4 are provided with branch pipe shut-off valves 5, and conveying switching between different pyrolysis furnaces 9 burning gas is realized through the branch pipe shut-off valves 5.
Specifically, a primary air distribution pipe 13 and a tertiary air distribution pipe 12 are arranged at the inlet of the boiler 11, and a denitration reactor is also arranged in the boiler 11;
the rear section conveying main pipe 32 is respectively communicated with the primary air distribution pipe 13 and the tertiary air distribution pipe 12, a primary air distribution valve 16 is arranged at the primary air distribution pipe 13, and a tertiary air distribution valve 15 is arranged at the tertiary air distribution pipe 12.
In the embodiment, the burnt gas enters the hearth in two paths, and one part of the burnt gas is mixed with primary air through the primary air distribution pipe 13 and enters the hearth as primary air; the other part of the air enters the hearth as tertiary air distribution through a tertiary air distribution pipe 12. The primary air distribution quantity of the coke-burning gas is based on that under the condition of keeping the total primary air quantity basically unchanged, the primary air distribution temperature is increased to 300-350 ℃, the ignition heat of coal fuel is reduced, and the ignition position is advanced, so that the effects of increasing the ignition speed and the ignition stability of pulverized coal are achieved, the operation condition of the boiler 11 is improved, and meanwhile, the primary air distribution quantity can be reduced, and the load of a fan is reduced.
A small amount of residual burnt gas after primary air distribution is used as tertiary air distribution high-speed jet flow to enter the boiler 11, so that the fluidization effect of the pulverized coal in the boiler 11 and the complete combustion of the residual pulverized coal are improved.
Semicoke, VOCs organic matters and the like contained in the burnt gas release heat through combustion and are simultaneously converted into CO2And H2O, organic sulfur is converted into SO by combustion2，SO2The flue gas is removed by a desulfurization facility of the boiler 11; NOx contained in the flue gas is removed by a flue gas denitration facility of the boiler 11, and the process realizes the thorough purification of all pollutants in the coke-burning gas.
[ example 4 ]
As shown in fig. 1, in this embodiment, on the basis of embodiment 3, the front-stage conveying main pipe 31 is a horizontal conveying pipe and forms an angle of 90 ° with the rear-stage conveying main pipe 32;
the coke catching pipeline is communicated with the front-section conveying main pipe 31 through a horizontal connecting pipe 7 extending out of the front-section conveying main pipe 31;
the coke-catching pipeline is communicated with the dust-removing coke catcher 1 through a vertical connecting pipe 8, and the vertical connecting pipe 8 is vertical to the horizontal connecting pipe 7.
Specifically, the coke catching pipeline is an arc-shaped pipeline 2;
the central angle α of the arc-shaped pipeline 2 is 45-90 degrees;
the inner diameter D of the coke catching pipeline is 1-2 times of the inner diameter D of the conveying main pipe;
the diameter of the vertical connecting pipe 8 is the same as the inner diameter d of the coke-catching pipeline;
the curvature radius R of the arc-shaped pipeline 2 is 2-10 times of the inner diameter of the arc-shaped pipeline 2;
the length L1 of the horizontal connecting pipe 7 and the length L2 of the vertical connecting pipe 8 are both 0-500 mm.
in the embodiment, the optimal range of the central angle α of the arc-shaped pipeline 2 is 60-90 degrees, the angle is too small to be beneficial to rubber powder sedimentation, the central angle is too large to ensure that not only is the sedimentation resistance large, but also the bridge is easy to be built, and the coke catching effect is influenced, the inner diameter D of the coke catching pipe cannot be lower than that of the conveying main pipe, otherwise, the coke catching is not beneficial, the inner diameter D of the coke catching pipe is too large and the cost is too high, and the optimal range of the curvature radius R of the arc-shaped pipeline 2 is 6-8 times of the inner diameter of the arc-shaped pipeline 2 to be beneficial.
[ example 5 ]
As shown in fig. 2, in this embodiment, on the basis of embodiment 3, this embodiment further includes:
the front-section conveying main pipe 31 is a horizontal conveying pipeline and forms an included angle of 90 degrees with the rear-section conveying main pipe 32;
the coke catching pipeline is communicated with the front-section conveying main pipe 31 through a horizontal connecting pipe 7 extending out of the front-section conveying main pipe 31;
the coke-catching pipeline is communicated with the dust-removing coke catcher 1 through a vertical connecting pipe 8, and the vertical connecting pipe 8 is vertical to the horizontal connecting pipe 7.
Specifically, the coke capturing pipeline is a straight pipeline 21;
the inner diameter of the straight pipeline 21 is 1-2 times of the inner diameter d of the conveying main pipe;
the diameter of the vertical connecting pipe is the same as the inner diameter of the straight pipeline 21;
the length L1 of the horizontal connecting pipe 7 and the length L2 of the vertical connecting pipe are both 0-500 mm.
The utility model discloses according to characteristics such as burnt gas high temperature, high pressure head, pollutant kind are complicated, adopt special design's high temperature decoking ware that gathers dust, retrieve the great solid burnt grain of particle diameter in the burnt gas after, with the residual air as once air distribution and cubic air distribution respectively and replace part air distribution air to send into 11 furnace combustions of boiler, CO, organic matter, the semicoke solid particle that smugglies secretly in the burnt gas can turn into the harmless CO of environment after burning in the furnace chamber2With water, with simultaneous release of energy, organic sulfurConversion to SO2And water. NOx and SO2Through the SOx/NOx control system of 11 flue gases in boiler, the purification back is up to standard, ultra-clean discharges even, need not to establish purifier in addition.
The technical scheme can purify all pollutants in the coke-burning gas and realize the standard emission in the true sense. Meanwhile, the coke gas can recover at least 1000Kcal of heat per standard square, and no investment on new purifying equipment is needed. Meanwhile, the air distribution energy consumption of the existing boiler 11 can be reduced, and the combustion performance of the existing boiler 11 is improved.
[ Experimental examples ]
Based on the above examples 1-6, the applicant performed specific test procedures as shown in table 1 by changing the parameters of the arc coke-catching curve, the dust-removing coke-catcher 1 and the air distribution of the boiler 11 after the coke-burning gas passes through the reaction zone for different contents of pollutants in the coke-burning gas:
TABLE 1 test examples for different content of burnt gas pollutants
wherein L1 is the length of the horizontal connecting pipe 7, L2 is the length of the vertical connecting pipe 8, α represents the central angle of the arc-shaped coke-catching curve, β represents the inner diameter of the arc-shaped coke-catching curve, β represents the inner diameters of the conveying main pipe and the horizontal connecting pipe 7, R represents the curvature radius of the arc-shaped coke-catching curve, beta represents the included angle of the conical bottom of the shell of the dust-removing coke catcher 1, the void ratio of the partition layer and the pore diameter of the micropores are both the partition layer and the pore diameter on the porous partition layer 1.3, VOCs is the English abbreviation of volatile organic compounds (VOLATE organic compounds), and NOx is nitrogen oxide.
Table 2 shows the results of the purification effect achieved by using the corresponding process according to the content of the coke-burning gas pollutants in Table 1.
Table 2: energy recovery and purification effects achieved by the process of the test examples in Table 1
As can be seen from tables 1 and 2, in the above test examples, the burnt gas was mixed with the low-temperature air from a high temperature of about 500 ℃ and then burned in the boiler, and then the temperature was lowered to 180 ℃ by heat removal, and 60% of the heat energy contained therein was recovered and utilized, and the combustion heat of the contained VOCs was all recovered and utilized. And dust, NOx and Sox are purified by a desulfurization and denitrification device arranged in the boiler and then discharged after reaching the standard. The CO and VOC are deeply purified.
The recovered energy consists of two parts: 1) high temperature gas temperature drop, 2) combustion of VOCs. In example 1, the temperature drop of the high-temperature gas is the main factor in recovering energy due to the low content of VOCs. In example 2, the combustion contribution energy of VOCs increases due to the higher content of VOCs. And the rest of the experimental examples are analogized in turn.
It should be noted that the above embodiments can be freely combined as necessary. The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (7)
1. The utility model provides an ethylene unit burnt gas resource utilization and deep purification device which characterized in that includes:
the conveying main pipe is divided into a front-section conveying main pipe and a rear-section conveying main pipe, one end of the front-section conveying main pipe is communicated with a plurality of pyrolysis furnaces, the other end of the front-section conveying main pipe is communicated with one end of the rear-section conveying main pipe, the other end of the rear-section conveying main pipe is communicated with a boiler, and an outlet of the boiler is communicated with a desulfurizing tower;
the inlet of the coke catching pipeline is communicated with the joint of the front-section conveying main pipe and the rear-section conveying main pipe, and the inlet of the coke catching pipeline is higher than the outlet of the coke catching pipeline;
and the inlet of the dust-removing and coke-catching device is communicated with the outlet of the coke-catching pipeline.
2. The ethylene plant burnt gas resource utilization and deep purification device of claim 1, wherein the dust removal coke catcher comprises:
the coke particle discharging device comprises a shell, wherein the bottom of the shell is provided with a coke particle discharging port, and the coke particle discharging port is provided with an ash storage discharging valve;
the porous interlayer surrounds the bottom of the shell and divides the shell into two parts, namely an upper ash storage space and a lower condensate space;
the condensate conveying pump is communicated with the lower condensate space through a condensate discharging pipe, and a condensate discharging valve is arranged on the condensate discharging pipe.
3. The ethylene plant burnt gas resource utilization and deep purification device of claim 2, which is characterized in that:
the shell is provided with a conical bottom, the included angle of the conical bottom of the shell is 30-90 degrees, the porosity of the porous interlayer is 50-80%, and the pore size of the porous interlayer is 20-200 mu m.
4. The ethylene plant burnt gas resource utilization and deep purification device of claim 1, which is characterized in that:
a primary air distribution pipe and a tertiary air distribution pipe are arranged at the inlet of the boiler;
the rear section conveying main pipe is respectively communicated with the primary air distribution pipe and the tertiary air distribution pipe, a primary air distribution valve is arranged at the primary air distribution pipe, and a tertiary air distribution valve is arranged at the tertiary air distribution pipe.
5. The ethylene plant burnt gas resource utilization and deep purification device of claim 1, which is characterized in that:
the front-section conveying main pipe is a horizontal conveying pipeline, and an included angle between the front-section conveying main pipe and the rear-section conveying main pipe is 90 degrees;
the coke catching pipeline is communicated with the front section conveying main pipe through a horizontal connecting pipe extending out of the front section conveying main pipe;
the coke capturing pipeline is communicated with the dust and coke collecting device through a vertical connecting pipe, and the vertical connecting pipe is perpendicular to the horizontal connecting pipe.
6. The ethylene plant burnt gas resource utilization and deep purification device of claim 5, which is characterized in that:
the coke catching pipeline is an arc pipeline or a straight pipeline;
the central angle of the arc-shaped pipeline is 45-90 degrees;
the inner diameter of the coke catching pipeline is 1-2 times of the inner diameter of the conveying main pipe;
the diameter of the vertical connecting pipe is the same as the inner diameter of the coke capturing pipeline;
the curvature radius of the arc-shaped pipeline is 2-10 times of the inner diameter of the arc-shaped pipeline;
the length of horizontal connecting pipe and the length of vertical connecting pipe are 0 ~ 500 mm.
7. The ethylene plant burnt gas resource utilization and deep purification device of claim 1, which is characterized in that:
a plurality of pyrolysis furnaces are respectively communicated with the front-section conveying main pipe through corresponding conveying branch pipes, and branch pipe stop valves are arranged on the conveying branch pipes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921245235.1U CN210560258U (en) | 2019-08-02 | 2019-08-02 | Ethylene device burnt gas resource utilization and deep purification device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921245235.1U CN210560258U (en) | 2019-08-02 | 2019-08-02 | Ethylene device burnt gas resource utilization and deep purification device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN210560258U true CN210560258U (en) | 2020-05-19 |
Family
ID=70632974
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921245235.1U Active CN210560258U (en) | 2019-08-02 | 2019-08-02 | Ethylene device burnt gas resource utilization and deep purification device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN210560258U (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110317619A (en) * | 2019-08-02 | 2019-10-11 | 上海蓝科石化环保科技股份有限公司 | A kind of ethylene unit burns gas resource utilization and device for deep cleaning and technique |
| CN115193166A (en) * | 2021-04-09 | 2022-10-18 | 中国石化工程建设有限公司 | Comprehensive treatment system and method for coke-burning tail gas of cracking furnace |
-
2019
- 2019-08-02 CN CN201921245235.1U patent/CN210560258U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110317619A (en) * | 2019-08-02 | 2019-10-11 | 上海蓝科石化环保科技股份有限公司 | A kind of ethylene unit burns gas resource utilization and device for deep cleaning and technique |
| CN115193166A (en) * | 2021-04-09 | 2022-10-18 | 中国石化工程建设有限公司 | Comprehensive treatment system and method for coke-burning tail gas of cracking furnace |
| CN115193166B (en) * | 2021-04-09 | 2024-04-16 | 中国石化工程建设有限公司 | Comprehensive treatment system and method for pyrolysis furnace burnt tail gas |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101112669A (en) | Multilevel purifier for disacidifying using dry and wet method and for removing dust by using cloth bag | |
| CN100563783C (en) | A kind of bitumen flue gas purifying method | |
| WO2018032806A1 (en) | Multi-stage purification treatment system for tail gas from manufacturing ceramic by carbonization of sludge from bottom of river or lake | |
| CN104906876A (en) | Tail gas purification method and device for thermal desorption of organic contaminated soil | |
| CN105214478A (en) | The integral process of a kind of coke oven flue exhuast gas desulfurization denitration and waste heat recovery | |
| CN101628201A (en) | Clearing device for smoke pollutants of glass kiln and clearing method thereof | |
| CN106439843B (en) | Petrochemical industry not recovering discarded material harmless treatment process | |
| CN210560258U (en) | Ethylene device burnt gas resource utilization and deep purification device | |
| CN102585918A (en) | Process and system for deeply removing tar through biomass gas coupling adsorption | |
| CN111530441B (en) | Powdered activated carbon regeneration system and regeneration method thereof | |
| CN109945211B (en) | Burning treatment method and system for semi-coke pyrolysis waste gas and waste liquid | |
| CN112657330A (en) | Volatile organic waste gas treatment process and device in tire industry | |
| CN205774358U (en) | A kind of carbonaceous organic material continuous pyrolysis purifies the system of CO fuel gas | |
| CN103028303A (en) | Method and device for purifying asphalt smoke | |
| CN106352364A (en) | Integrated method and integrated device for catalytic cracking, flue gas incineration and heat exchange separation | |
| CN109157961A (en) | A kind of multi-pollutant joint removing means, method and the purposes of electrolytic aluminium carbon anode roasting flue gas | |
| CN104107602A (en) | On-line regeneration method of deduster filter core used in high-temperature inflammable dust environment | |
| CN101310832B (en) | Purification method and device dioxins in solid waste incineration fume | |
| CN201304313Y (en) | Dry bag-type dust exhaust device for gas gasification burner | |
| CN105318342B (en) | A kind for the treatment of process of industrial smoke | |
| CN110317619A (en) | A kind of ethylene unit burns gas resource utilization and device for deep cleaning and technique | |
| CN214693828U (en) | Oily sludge treatment system | |
| CN213433606U (en) | Coke and asphalt smoke tail gas treatment device | |
| CN212651583U (en) | Dual cycle formula active carbon separation is analytic msw incineration flue gas processing system | |
| CN211562491U (en) | Asphalt smoke waste gas treatment system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |