CN206930181U - Raw coke oven gas waste heat high/low temperature comprehensive recovery system - Google Patents
Raw coke oven gas waste heat high/low temperature comprehensive recovery system Download PDFInfo
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- CN206930181U CN206930181U CN201720246179.8U CN201720246179U CN206930181U CN 206930181 U CN206930181 U CN 206930181U CN 201720246179 U CN201720246179 U CN 201720246179U CN 206930181 U CN206930181 U CN 206930181U
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Abstract
The utility model discloses a kind of raw coke oven gas waste heat high/low temperature comprehensive recovery system, mainly for the heat reclaimed in existing raw coke oven gas waste heat recovery it is less the problem of, propose a kind of raw coke oven gas waste heat high/low temperature comprehensive recovery system of synthetical recovery raw coke oven gas waste heat, including remove most of organic matter using the waste heat of more than 470 ± 10 DEG C of high-temperature heat-exchanging recovery raw coke oven gas, using raw coke oven gas is cooled into 260 ± 10 DEG C, the residual heat resources of 120 ± 10~260 ± 10 DEG C of raw coke oven gas are reclaimed using cryogenic heat exchanger and use subcolling condenser that raw coke oven gas is cooled into 80 ± 10 DEG C.In the utility model raw coke oven gas waste heat high/low temperature comprehensive recovery system method, raw coke oven gas waste heat recovery temperature range is expanded, extends the service life of equipment.
Description
Technical field
It the utility model is related to a kind of raw coke oven gas waste heat high/low temperature comprehensive recovery system and method.
Background technology
With the continuous propulsion of international community's energy-saving and emission-reduction policy, high energy-consuming enterprises's production pressure is continuously increased, and how to be dropped
Low enterprise energy consumption turns into the major issue that numerous high energy-consuming enterprises face.Coking is steel industry important component,
It is energy consumption upper section, 650~750 DEG C of coal oven dithio-gas outlet temperature, its heat loss accounts for 33% or so of coke oven energy consumption, the portion
Heat energy is divided but to fail effectively to reclaim.
Due to raw coke oven gas complicated component, especially containing tar etc., easily coking composition causes its waste heat recovery difficult,
During less than 450 DEG C, tar, asphalt component in raw coke oven gas can rapid cokings.Common practice is：Sprayed in bridge tube and discharge
Cyclic ammonia water, is directly contacted with raw coke oven gas, and the temperature of raw coke oven gas is rapidly decreased into 80~85 DEG C；Raw coke oven gas after cooling enters just
Cooler is cooled further to 25 DEG C, and cyclic ammonia water cooling tar removing Posterior circle uses.Heat of raw coke oven gas is circulated during this
The latent heat of vaporization of ammoniacal liquor absorbs, and consumes substantial amounts of cyclic ammonia water and causes production cost to increase, while residual heat resources also fail to effectively
Utilize.Therefore, some researchers propose the scheme of raw coke oven gas waste heat recovery.
Retrieval discovery, application number 200810122711.0, patent name《Raw coke over gas riser residual heat recovery device》
A kind of device that raw coke oven gas waste heat is absorbed using heat exchange of heat pipe is proposed, but it is avoids coking risk, only reclaims raw coke oven gas
In be higher than 500 DEG C of above section waste heats, the raw coke oven gas that 500 DEG C of heat exchanger exit carries out spraying ammonia cooling into bridge tube.Application number
200810201705.4, patent name《Coke oven coke oven uprising tube waste heat recovery couples the process utilized with dry quenching system》It is proposed
A kind of method for combining dry coke quenching technique and raw coke oven gas residual neat recovering system, but it also only reclaims waste coal to avoid coking
More than 500 DEG C of waste heat in gas.Application number 201210317957.X, patent name《A kind of combined type waste heat of coke oven crude gas returns
Receive the system and method for superheated steam》, by setting heat exchanger in tedge, the method for evaporator being set in bridge tube to reclaim
Waste heat in raw coke oven gas, although the waste heat in raw coke oven gas can be reclaimed to greatest extent, bridge tube space is limited, burnt in raw coke oven gas
Oil component when less than 450 DEG C can rapid coking, and then influence heat exchange efficiency, meanwhile, the limited inconvenient evaporator in bridge tube space
The cleaning of heat exchanger surface tar, long-play, bridge tube evaporator heat exchange effect is very low, or even tar can occur and block bridge
Manage-style danger.
By analysis, the composition that can be condensed in raw coke oven gas including pitch, carbolineum, washing oil, naphtalene oil, carbolic oil and
Light oil etc., each component in the liquid state, each component viscosity at identical temperature：Pitch ＞ carbolineum ＞ washing oil ＞ naphtalene oil ＞ carbolic oil ＞ is light
Oil, pitch adiabatic condensation temperature highest, starts to condense at 450 DEG C or so, secondly about starts to condense at 360 DEG C for carbolineum, and washing oil coagulates
Junction temperature is near 320 DEG C, and the adiabatic condensation temperature such as naphtalene oil, carbolic oil continues to reduce, and viscosity is not high when it is condensed into liquid, because
This condenses on heat exchangers also is difficult to produce wall built-up phenomenon.
Waste heat of coke oven crude gas reclaims problems faced：First, recovered temperature section is narrow, generally more than more than 500 DEG C of recovery
Heat；Second, complicated component in raw coke oven gas, coking, which easily occurs, influences heat exchange efficiency.The utility model can solve raw coke oven gas very well
Waste heat recovery temperature range is narrow and heat exchanger coking problem.
Utility model content
In view of the above-mentioned problems, a kind of raw coke oven gas waste heat high/low temperature of synthetical recovery raw coke oven gas waste heat of the utility model offer is comprehensive
Close recovery system.
To reach above-mentioned purpose, the utility model raw coke oven gas waste heat high/low temperature comprehensive recovery system, including along raw coke oven gas stream
The high-temperature heat-exchanging for the waste heat that more than 470 ± 10 DEG C of the recovery raw coke oven gas that sets gradually of dynamic direction, raw coke oven gas is cooled to 260 ±
10 DEG C of medium temperature cooler, reclaim 120 ± 10~260 ± 10 DEG C of raw coke oven gas residual heat resources cryogenic heat exchanger and by waste coal
The subcolling condenser of air cooling to 80 ± 10 DEG C.
Further, the high-temperature heat-exchanging includes shell and inner casing, is set between the shell and inner casing Packed
Dielectric cavity, the dielectric cavity are provided with heat transferring medium import and export；Heat-insulation layer is provided with the outside of the shell.
Further, the medium temperature cooler includes a container, bottom level the entering less than the container of the container
Mouth and the lower edge of outlet height, the entrance and exit of the container are respectively arranged with least one spray for being used to spray ammoniacal liquor
Mouth, the bottom of the container are provided with sewage draining exit.
Further, the cryogenic heat exchanger includes a housing, the bottom of the housing less than the housing entrance and
Export the height of lower edge；
Heat exchange pipeline or heat exchanging interlayer are provided with the housing or on the outer wall of housing, the bottom of the housing is set
There is sewage draining exit.
Further, the subcolling condenser includes a pipeline and the hydraulic spray nozzle being arranged in pipeline.
Further, the outlet of the heat transferring medium pipeline of the cryogenic heat exchanger and the heat transferring medium of the high-temperature heat-exchanging
The entrance connection of pipeline.
Further, the high-temperature heat-exchanging raw coke oven gas outlet is provided with temperature sensor, and heat transferring medium import is provided with flow
Meter and magnetic valve, the temperature sensor and the flowmeter are connected with a controller communication, and the controller controls the electricity
Magnet valve.
Further, medium temperature cooler raw coke oven gas outlet is provided with thermometer, connects the cooling medium pipeline of the nozzle
On be provided with flowmeter and magnetic valve, the thermometer and flowmeter are connected with a controller communication, and the controller controls institute
State magnetic valve.
Further, the cryogenic heat exchanger raw coke oven gas outlet is provided with temperature sensor, and heat transferring medium import is provided with flow
Meter and magnetic valve, the thermometer and flowmeter are connected with a controller communication, and the controller controls the magnetic valve.
Further, low-temp. spraying but sets thermometer in the outlet of device raw coke oven gas, connects and is set on the cooling medium pipeline of nozzle
There are flowmeter and magnetic valve, the thermometer and flowmeter are connected with a controller communication, and the controller controls the electromagnetism
Valve.
In the utility model raw coke oven gas waste heat high/low temperature comprehensive recovery system, raw coke oven gas waste heat recovery temperature range expands,
More than 470 DEG C waste heats can not only be reclaimed, moreover it is possible to reclaim 120~260 DEG C of part of waste heat；Solves raw coke oven gas waste heat recovery low-temperature zone
The problem of coking can occur for (being less than 450 DEG C), improve the heat exchanger life-span；Accurate control cyclic ammonia water amount, than conventional recycle ammoniacal liquor
Dosage declines 50%, reduces enterprise operation cost.
In view of the above-mentioned problems, a kind of raw coke oven gas waste heat high/low temperature of synthetical recovery raw coke oven gas waste heat of the utility model offer is comprehensive
Close recovery method.
To reach above-mentioned purpose, the utility model raw coke oven gas waste heat high/low temperature comprehensive recovering process, comprise the following steps：
S1 is exchanged heat using high-temperature heat-exchanging to raw coke oven gas, control the temperature of exit gas of high-temperature heat-exchanging for 470 ±
10℃；
S2 is cooled using medium temperature cooler to raw coke oven gas, control the temperature of exit gas of medium temperature cooler for 260 ±
10℃；
S3 continues to exchange heat using cryogenic heat exchanger to raw coke oven gas, and the temperature of exit gas for controlling cryogenic heat exchanger is
120±10℃；
S4 continues to cool down using subcolling condenser to raw coke oven gas, and the temperature of exit gas for controlling cryogenic heat exchanger is 80
±10℃。
Further, in S2, into raw coke oven gas, sprinkling ammoniacal liquor is cooled down at the entrance and exit of medium temperature cooler,
The porch of medium temperature cooler is controlled to spray drop SMD scopes at 5~10 μm, the exit sprinkling drop of control medium temperature cooler
SMD is 1 ± 0.3mm.
Further, in S1, the initial temperature of the heat transferring medium in high-temperature heat-exchanging is controlled to be not less than 100 DEG C.
Further, in the S4, into raw coke oven gas, sprinkling water smoke is cooled down.
In the utility model raw coke oven gas waste heat high/low temperature comprehensive recovering process, raw coke oven gas waste heat recovery temperature range expands,
More than 470 DEG C waste heats can not only be reclaimed, moreover it is possible to reclaim 120~260 DEG C of part of waste heat；Solves raw coke oven gas waste heat recovery low-temperature zone
The problem of coking can occur for (being less than 450 DEG C), improve the heat exchanger life-span；Accurate control cyclic ammonia water amount, than conventional recycle ammoniacal liquor
Dosage declines 50%, reduces enterprise operation cost.
Brief description of the drawings
Fig. 1 is the process chart of the embodiment 1 of the utility model raw coke oven gas waste heat high/low temperature comprehensive recovery system；
Fig. 2 is the spray of the medium temperature cooler of the embodiment 1 of the utility model raw coke oven gas waste heat high/low temperature comprehensive recovery system
The layout viewing of mouth.
Embodiment
The utility model is further described with reference to Figure of description.
Embodiment 1
As shown in Figure 1-2, the present embodiment provides a kind of raw coke oven gas waste heat high/low temperature comprehensive recovering process, and the system includes height
Warm heat exchanger 1, medium temperature spray cooler 2, cryogenic heat exchanger 3 and low temperature spray cooler 4.
More than 650 DEG C of the high temperature raw coke oven gas come out from cooking camber enters high-temperature heat-exchanging 1 and carries out heat exchange, high temperature heat exchange
Device outlet raw gas temperature is down to 470 DEG C or so, reclaims Part I high-temperature residual heat.Heat transferring medium then uses according to liquid
Downstream heat transfer form, heat transferring medium enter heat exchanger from the working medium side-entrance 1.1 of high-temperature heat-exchanging 1, left from working medium side outlet 1.2
Heat exchanger；If heat transferring medium uses gas medium, using countercurrent flow form, heat-exchange working medium enters from inlet side 1.2 to exchange heat
Device, outlet side 1.1 leave heat exchanger.
The thermocouple T1 exported by high-temperature heat-exchanging monitors high-temperature heat-exchanging outlet temperature in real time, when high-temperature heat-exchanging goes out
During mouth temperature TGH ＞ 470+10 DEG C, increase cooling medium consumption；As high-temperature heat-exchanging outlet temperature TGH ＜ 470-10 DEG C, subtract
Few cooling medium consumption.
About 470 DEG C of the raw coke oven gas come out from high-temperature heat-exchanging 1 enters medium temperature spray cooler 2, medium temperature spray cooler 2
For rectangular box, the top of the entrance of medium temperature spray cooler 2 sets 3 high pressure fan nozzles 2.1, and it sprays drop SMD scopes
In 5~10 μm of ammoniacal liquor, raw coke oven gas is cooled rapidly；In 3 fan-shaped spray spouts 2.2 of its tail end top layout, its flushing liquor
SMD is dripped near 1mm, and droplet is settled for coalescence；Oil droplet is provided with liquid level with dropping down onto lower seal tank under ammoniacal liquor in tank
Meter, mixed liquor periodically enters tar ammonia separation link by mudhole 2.3, by the condensation that tentatively cools, higher boiling in coal gas,
Highly viscous larger molecular organicses are largely condensed, and condition is provided for follow-up low-temperature heat exchange link.Medium temperature spray cooler water
Plain cloth is put, and multiple fan nozzles are arranged in inducer, according to the Aspect Ratio of cooler, on cooler top and side distribution cloth
Put 1-3 branch nozzles.Cycle of higher pressure ammoniacal liquor sprays through nozzle, and drop SMD is 5~10 μm, in order to will enter medium temperature and spray
The raw coke oven gas of cooler is cooled to rapidly 280 DEG C, and further raw coke oven gas collects the liquid core condensed, spray fan by spray cooler
The ammoniacal liquor drop SMD of the outlet of shape nozzle is about 1mm, primarily to condensing droplet so that drop rapid subsidence to spray
Cooler lower seal tank, now raw gas temperature be down to 260 DEG C, the now asphalt component in raw coke oven gas, most anthracenes
Oil, part washing oil, and part H2S is removed from raw coke oven gas.The raw coke oven gas come out from spray cooler is through electrostatic precipitator
Absorb the condensation water core do not collected by spray cooler.
The thermocouple T2 of different radial depths is arranged in the outlet of medium temperature spray cooler 2, when mean temperature is at 260 ± 10 DEG C
When, keep the injection flow rate of high pressure fan nozzle 2.1 constant；If temperature need to increase the spray of high pressure fan nozzle 2.1 more than 270 DEG C
Ammonia vol；If temperature is less than 250 DEG C of spray ammonia vols that need to reduce high pressure fan nozzle 2.1.
Enter cryogenic heat exchanger 3 by the raw coke oven gas of preliminary tar removing, heat-exchange working medium enters from pipe side-entrance 3.1.1 manages
Formula heat exchanger 3.1, export 3.1.2 from pipe heat exchanger 3.1 and leave heat exchanger, further cool by the raw coke oven gas of heat exchanger,
Which part organic matter can be condensed further, and the liquid state organics of condensation are discharged by mudhole 3.2, into subsequent handling.
By adjusting heat transferring medium flow, the control raw coke oven gas outlet temperature scope of cryogenic heat exchanger 3 is at 120 ± 10 DEG C, control
System strategy is identical with high-temperature heat-exchanging, will not be repeated here.
The raw coke oven gas come out from cryogenic heat exchanger 3 enters low temperature spray cooler 4, low temperature spray cooler construction for it is normal
It is similar to advise raw coke oven gas bridge tube, by the misting cooling of mist-generating nozzle 4.1, is down to 80 DEG C of synthesis gas and is handled into conventional raw coke oven gas
Primary cooler further cool down；Spray water droplet is collected into tar ammonia with the organic matter in the raw coke oven gas condensed and separates link.
In the present embodiment, raw coke oven gas waste heat high/low temperature comprehensive recovering process passes through high-temperature heat-exchanging, medium temperature spraying cooling system
System, cryogenic heat exchanger and low temperature spray cooling system reclaim the segmentation of raw coke oven gas waste heat, cooling, not only reclaim raw coke oven gas waste heat also
It can realize that cyclic ammonia water amount declines 50%, save operating cost.
In the present embodiment raw coke oven gas waste heat high/low temperature comprehensive recovery system, raw coke oven gas waste heat recovery temperature range expands, no
More than 470 DEG C waste heats can only be reclaimed, moreover it is possible to reclaim 120~260 DEG C of part of waste heat；Solves raw coke oven gas waste heat recovery low-temperature zone
The problem of coking can occur for (being less than 450 DEG C), improve the heat exchanger life-span；Accurate control cyclic ammonia water amount, than conventional recycle ammoniacal liquor
Dosage declines 50%, reduces enterprise operation cost.
Embodiment 2
The difference of the present embodiment and above-described embodiment is：Cryogenic heat exchanger and high-temperature heat-exchanging are adopted in the present embodiment
With identical working medium, therefore, the two is connected in the present embodiment, heat-exchange working medium by cryogenic heat exchanger tentatively add first
Heat, enter back into high-temperature heat-exchanging and further improve the hot quality of heat-exchange working medium.
In the above-described embodiments, medium temperature cooler can not also use rectangular box using rectangular box, the casing,
Section is used as circular or other shapes pipeline.
In the above-described embodiments, the nozzles spray of medium temperature cooler is ammoniacal liquor, it will be appreciated that it is one that ammoniacal liquor is used at this
Kind preferred embodiment mode, rather than uniquely, other cooling ways of this area can also be used.
In the above-described embodiments, the nozzles spray in subcolling condenser is water smoke, it will be appreciated that is using water smoke at this
A kind of preferred embodiment mode, rather than uniquely, other cooling ways of this area can also be used.
In the above-described embodiments, described high-temperature heat-exchanging can use jacket type formula or coiled structure, with raw coke oven gas
Contact side wall should ensure that smooth enough, for the raw gas temperature exported from carbonization chamber to be down into 470 DEG C or so, heat-conducting medium
Can be water, conduction oil or fused salt, heat-conducting medium inlet temperature should be higher than that 100 DEG C, avoid the formation of the larger temperature difference and cause heat exchanger
It is too low close to raw coke oven gas side temperature.
It will be appreciated by those skilled in the art that the heat exchange mode of the high-temperature heat-exchanging and cryogenic heat exchanger in above-described embodiment
A kind of preferred embodiment mode is merely possible to, rather than the restriction made by exchange hot mode, in high-temperature heat-exchanging and low
Other heat exchange modes well-known to those skilled in the art can also be used in warm heat exchanger.
Embodiment 3
The present embodiment provides a kind of raw coke oven gas waste heat high/low temperature comprehensive recovering process of synthetical recovery raw coke oven gas waste heat.
To reach above-mentioned purpose, the utility model raw coke oven gas waste heat high/low temperature comprehensive recovering process, comprise the following steps：
S1 is exchanged heat using high-temperature heat-exchanging to raw coke oven gas, control the temperature of exit gas of high-temperature heat-exchanging for 470 ±
10℃；
S2 is cooled using medium temperature cooler to raw coke oven gas, control the temperature of exit gas of medium temperature cooler for 260 ±
10℃；Medium temperature spray cooler is horizontally disposed, and multiple fan nozzles are arranged in inducer, according to the Aspect Ratio of cooler,
Cooler top and side distribution arrangement 1-3 branch nozzles.Cycle of higher pressure ammoniacal liquor sprays through nozzle, and drop SMD is 5~10 μm, mesh
Be in order to by enter medium temperature spray cooler raw coke oven gas be cooled to 280 DEG C rapidly, further raw coke oven gas passes through spraying cooling
Device collects the liquid core condensed, and the ammoniacal liquor drop SMD for spraying the outlet of fan nozzle is about 1mm, primarily to droplet is condensed,
So that drop rapid subsidence, to spray cooler lower seal tank, now raw gas temperature is down to 260 DEG C, now in raw coke oven gas
Asphalt component, most carbolineums, part washing oil, and part H2S is removed from raw coke oven gas.Come out from spray cooler
Raw coke oven gas through electrostatic precipitator absorb not by spray cooler collect condensation water core.
S3 continues to exchange heat using cryogenic heat exchanger to raw coke oven gas, and the temperature of exit gas for controlling cryogenic heat exchanger is
120±10℃；
S4 continues to cool down using subcolling condenser to raw coke oven gas, and the temperature of exit gas for controlling cryogenic heat exchanger is 80
±10℃.In this step, into raw coke oven gas, sprinkling water smoke is cooled down.By the misting cooling of mist-generating nozzle 4.1,80 DEG C are down to
Synthesis gas enter conventional raw coke oven gas processing primary cooler further cool down；Spray the organic matter in water droplet and the raw coke oven gas condensed
Collect and enter tar ammonia separation link.
In S2, into raw coke oven gas, sprinkling ammoniacal liquor is cooled down at the entrance and exit of medium temperature cooler, controls medium temperature
Drop SMD scopes are sprayed at 5~10 μm in the porch of cooler, control medium temperature cooler exit spray drop SMD for 1 ±
0.3mm。
In S1, the initial temperature of the heat transferring medium in high-temperature heat-exchanging is controlled to be not less than 100 DEG C.So as to avoid due to changing
The wall surface temperature of hot device is too low and causes coking.
In the present embodiment raw coke oven gas waste heat high/low temperature comprehensive recovering process, raw coke oven gas waste heat recovery temperature range expands, no
More than 470 DEG C waste heats can only be reclaimed, moreover it is possible to reclaim 120~260 DEG C of part of waste heat；Solves raw coke oven gas waste heat recovery low-temperature zone
The problem of coking can occur for (being less than 450 DEG C), improve the heat exchanger life-span；Accurate control cyclic ammonia water amount, than conventional recycle ammoniacal liquor
Dosage declines 50%, reduces enterprise operation cost.
More than, preferred embodiment only of the present utility model, but the scope of protection of the utility model is not limited thereto, and is appointed
What those familiar with the art the change that can readily occur in or replaces in the technical scope that the utility model discloses
Change, should all cover within the scope of protection of the utility model.Therefore, the scope of protection of the utility model should be with claim
The protection domain defined is defined.
Claims (7)
- A kind of 1. raw coke oven gas waste heat high/low temperature comprehensive recovery system, it is characterised in that：Including being set successively along raw coke oven gas flow direction The high-temperature heat-exchanging for the waste heat that more than 470 ± 10 DEG C of the recovery raw coke oven gas put, the medium temperature that raw coke oven gas is cooled to 260 ± 10 DEG C are cold But device, reclaim 120 ± 10~260 ± 10 DEG C of raw coke oven gas residual heat resources cryogenic heat exchanger and raw coke oven gas is cooled to 80 ± 10 DEG C of subcolling condenser.
- 2. raw coke oven gas waste heat high/low temperature comprehensive recovery system as claimed in claim 1, it is characterised in that：The high-temperature heat-exchanging bag Include shell and inner casing, Packed dielectric cavity be set between the shell and inner casing, the dielectric cavity be provided with heat transferring medium enter, Outlet；Heat-insulation layer is provided with the outside of the shell.
- 3. raw coke oven gas waste heat high/low temperature comprehensive recovery system as claimed in claim 1, it is characterised in that：The medium temperature cooler bag A container is included, the bottom level of the container is less than the lower edge height of the entrance and exit of the container, and the container enters Mouth and outlet are respectively arranged with least one nozzle for being used to spray ammoniacal liquor, and the bottom of the container is provided with sewage draining exit.
- 4. raw coke oven gas waste heat high/low temperature comprehensive recovery system as claimed in claim 1, it is characterised in that：The cryogenic heat exchanger bag A housing is included, the bottom of the housing is less than the height of the entrance and exit lower edge of the housing；Heat exchange pipeline or heat exchanging interlayer are provided with the housing or on the outer wall of housing, the bottom of the housing is provided with row Dirty mouth.
- 5. raw coke oven gas waste heat high/low temperature comprehensive recovery system as claimed in claim 1, it is characterised in that：The subcolling condenser bag Include a pipeline and the hydraulic spray nozzle being arranged in pipeline.
- 6. raw coke oven gas waste heat high/low temperature comprehensive recovery system as claimed in claim 1, it is characterised in that：The cryogenic heat exchanger The outlet of heat transferring medium pipeline connects with the entrance of the heat transferring medium pipeline of the high-temperature heat-exchanging.
- 7. raw coke oven gas waste heat high/low temperature comprehensive recovery system as claimed in claim 1, it is characterised in that：The high-temperature heat-exchanging is waste Gas exit is provided with temperature sensor, and heat transferring medium import is provided with flowmeter and magnetic valve, the temperature sensor and the stream Gauge is connected with a controller communication, and the controller controls the magnetic valve；The outlet of medium temperature cooler raw coke oven gas is provided with thermometer, connects and is provided with flowmeter and electricity on the cooling medium pipeline of nozzle Magnet valve, the thermometer and flowmeter are connected with a controller communication, and the controller controls the magnetic valve；The cryogenic heat exchanger raw coke oven gas outlet is provided with temperature sensor, and heat transferring medium import is provided with flowmeter and magnetic valve, institute State thermometer and flowmeter to be connected with a controller communication, the controller controls the magnetic valve；The outlet of subcolling condenser raw coke oven gas sets thermometer, connects and is provided with flowmeter and electromagnetism on the cooling medium pipeline of nozzle Valve, the thermometer and flowmeter are connected with a controller communication, and the controller controls the magnetic valve.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106839808A (en) * | 2017-03-14 | 2017-06-13 | 中冶华天工程技术有限公司 | Raw coke oven gas waste heat high/low temperature comprehensive recovery system and method |
| WO2021097905A1 (en) * | 2019-11-19 | 2021-05-27 | 南京华电节能环保设备有限公司 | Recycling device for high-temperature sensible heat of raw coke oven gas in coke oven ascension pipe |
-
2017
- 2017-03-14 CN CN201720246179.8U patent/CN206930181U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106839808A (en) * | 2017-03-14 | 2017-06-13 | 中冶华天工程技术有限公司 | Raw coke oven gas waste heat high/low temperature comprehensive recovery system and method |
| CN106839808B (en) * | 2017-03-14 | 2022-12-06 | 中冶华天工程技术有限公司 | High-low temperature comprehensive recovery system and method for waste heat of raw gas |
| WO2021097905A1 (en) * | 2019-11-19 | 2021-05-27 | 南京华电节能环保设备有限公司 | Recycling device for high-temperature sensible heat of raw coke oven gas in coke oven ascension pipe |
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Effective date of registration: 20220608 Address after: 243000 Fu Chang Industrial Park, 259 HSI Nan Road, Ma'anshan economic and Technological Development Zone, Anhui Patentee after: HUATIAN ENGINEERING & TECHNOLOGY CORPORATION, MCC Patentee after: HUATIAN NANJING ENGINEERING & TECHNOLOGY CORPORATION, MCC Address before: 243005 Hunan West Road, Ma'anshan, Ma'anshan, Anhui Patentee before: HUATIAN ENGINEERING & TECHNOLOGY CORPORATION, MCC Patentee before: MCC Huatian (Anhui) energy conservation and Environmental Protection Research Institute Co., Ltd |
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