CN106839808A - Raw coke oven gas waste heat high/low temperature comprehensive recovery system and method - Google Patents
Raw coke oven gas waste heat high/low temperature comprehensive recovery system and method Download PDFInfo
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- CN106839808A CN106839808A CN201710150815.1A CN201710150815A CN106839808A CN 106839808 A CN106839808 A CN 106839808A CN 201710150815 A CN201710150815 A CN 201710150815A CN 106839808 A CN106839808 A CN 106839808A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28C—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA COME INTO DIRECT CONTACT WITHOUT CHEMICAL INTERACTION
- F28C1/00—Direct-contact trickle coolers, e.g. cooling towers
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/06—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits having a single U-bend
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F25/00—Component parts of trickle coolers
- F28F25/02—Component parts of trickle coolers for distributing, circulating, and accumulating liquid
- F28F25/06—Spray nozzles or spray pipes
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Abstract
The present invention discloses a kind of raw coke oven gas waste heat high/low temperature comprehensive recovery system and method, mainly for the less problem of the heat reclaimed in existing raw coke oven gas waste heat recovery, 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 the waste heat of more than 470 ± 10 DEG C of raw coke oven gas is reclaimed using high-temperature heat-exchanging, using raw coke oven gas being cooled into 260 ± 10 DEG C of most of organic matters of removal, the residual heat resources using cryogenic heat exchanger 120 ± 10~260 ± 10 DEG C of raw coke oven gas of recovery and raw coke oven gas is cooled into 80 ± 10 DEG C using subcolling condenser.In raw coke oven gas waste heat high/low temperature comprehensive recovery system method of the present invention, raw coke oven gas waste heat recovery temperature range is expanded, extend the service life of equipment.
Description
Technical field
The present invention relates 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 drop
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 recovery.
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, with raw coke oven gas directly contact, 80~85 DEG C is rapidly decreased to by the temperature of raw coke oven gas；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 is used.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 the production cost to increase, while residual heat resources are also failed 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》
Propose that a kind of use heat exchange of heat pipe absorbs the device of raw coke oven gas waste heat, but it is to avoid 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 into bridge tube carry out spray ammonia cooling.Application number
200810201705.4th, patent name《Coke oven coke oven uprising tube waste heat recovery couples the process for utilizing with dry quenching system》Propose
A kind of method for combining dry coke quenching technique and raw coke oven gas residual neat recovering system, but it is to avoid coking, also only reclaims waste coal
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 is returned
Receive the system and method for superheated steam》, reclaimed by setting the method for setting evaporator in heat exchanger, bridge tube in tedge
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 blocking bridge can occur
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：＞ is light for pitch ＞ carbolineum ＞ washing oil ＞ naphtalene oil ＞ carbolic oil
Oil, pitch adiabatic condensation temperature highest, start at 450 DEG C or so condense, secondly for carbolineum about start at 360 DEG C condense, washing oil coagulate
Junction temperature is near 320 DEG C, and the adiabatic condensation temperature such as naphtalene oil, carbolic oil continues to reduce, and its when being condensed into liquid viscosity it is not high, because
This condenses also be difficult to produce wall built-up phenomenon on heat exchangers.
Waste heat of coke oven crude gas reclaims problems faced：One is that recovered temperature interval is narrow, generally reclaims more than more than 500 DEG C
Heat；Two is complicated component in raw coke oven gas, and coking influence heat exchange efficiency easily occurs.The present invention can very well solve raw coke oven gas waste heat
The interval narrow and heat exchanger coking problem of recovered temperature.
The content of the invention
Regarding to the issue above, the present invention provides a kind of raw coke oven gas waste heat high/low temperature of synthetical recovery raw coke oven gas waste heat and comprehensively returns
Receipts system.
To reach above-mentioned purpose, raw coke oven gas waste heat high/low temperature comprehensive recovery system of the present invention, including along raw coke oven gas flowing side
To the high-temperature heat-exchanging of more than 470 ± 10 DEG C of waste heat of the recovery raw coke oven gas for setting gradually, raw coke oven gas is cooled to 260 ± 10 DEG C
Middle temperature cooler, reclaim the cryogenic heat exchanger of residual heat resources of 120 ± 10~260 ± 10 DEG C of raw coke oven gas and raw coke oven gas is cold
But to 80 ± 10 DEG C of subcolling condenser.
Further, the high-temperature heat-exchanging includes shell and inner casing, sets Packed between the shell and inner casing
Dielectric cavity, the dielectric cavity is provided with heat transferring medium import and export；Heat-insulation layer is provided with the outside of the shell.
Further, the middle temperature cooler includes a container, bottom level the entering less than the container of the container
Highly, the entrance and exit of the container is respectively arranged with least one is used to spray the spray of ammoniacal liquor for mouth and the lower edge of outlet
Mouth, the bottom of the container is 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 heat transferring medium of the outlet of the heat transferring medium pipeline of the cryogenic heat exchanger and 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, middle 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, but the outlet of device raw coke oven gas sets thermometer to low-temp. spraying, connects and set on the cooling medium pipeline of nozzle
There are flowmeter and magnetic valve, the thermometer and flowmeter are connected with a controller communication, the controller controls the electromagnetism
Valve.
In raw coke oven gas waste heat high/low temperature comprehensive recovery system of the present invention, raw coke oven gas waste heat recovery temperature range expands, not only
More than 470 DEG C waste heats can be reclaimed, moreover it is possible to reclaim 120~260 DEG C of part of waste heat；Solve raw coke oven gas waste heat recovery low-temperature zone (low
In 450 DEG C) problem of coking can occur, improve the heat exchanger life-span；Precise control cyclic ammonia water amount, than conventional recycle ammonia volume
Decline 50%, reduce enterprise operation cost.
Regarding to the issue above, the present invention provides a kind of raw coke oven gas waste heat high/low temperature of synthetical recovery raw coke oven gas waste heat and comprehensively returns
Receiving method.
To reach above-mentioned purpose, raw coke oven gas waste heat high/low temperature comprehensive recovering process of the present invention comprises 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 lowered the temperature using middle temperature cooler to raw coke oven gas, control the temperature of exit gas of middle temperature cooler for 260 ±
10℃；
S3 proceeds heat exchange to raw coke oven gas using cryogenic heat exchanger, and the temperature of exit gas for controlling cryogenic heat exchanger is
120±10℃；
S4 proceeds cooling to raw coke oven gas using subcolling condenser, and the temperature of exit gas for controlling cryogenic heat exchanger is 80
±10℃。
Further, in S2, at the entrance and exit of middle temperature cooler to raw coke oven gas in spray ammoniacal liquor cooled down,
Control the porch of middle temperature cooler to spray drop SMD scopes at 5~10 μm, control the exit sprinkling drop of middle temperature cooler
SMD is 1 ± 0.3mm.
Further, in S1, the initial temperature of the heat transferring medium in control high-temperature heat-exchanging is not less than 100 DEG C.
Further, in the S4, cooled down to water smoke is sprayed in raw coke oven gas.
In raw coke oven gas waste heat high/low temperature comprehensive recovering process of the present invention, raw coke oven gas waste heat recovery temperature range expands, not only
More than 470 DEG C waste heats can be reclaimed, moreover it is possible to reclaim 120~260 DEG C of part of waste heat；Solve raw coke oven gas waste heat recovery low-temperature zone (low
In 450 DEG C) problem of coking can occur, improve the heat exchanger life-span；Precise control cyclic ammonia water amount, than conventional recycle ammonia volume
Decline 50%, reduce enterprise operation cost.
Brief description of the drawings
Fig. 1 is the process chart of the embodiment 1 of raw coke oven gas waste heat high/low temperature comprehensive recovery system of the present invention；
Fig. 2 is the nozzle of the middle temperature cooler of the embodiment 1 of raw coke oven gas waste heat high/low temperature comprehensive recovery system of the present invention
Layout viewing.
Specific embodiment
With reference to Figure of description, the present invention will be further described.
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, middle temperature spray cooler 2, cryogenic heat exchanger 3 and low temperature spray cooler 4.
From the high temperature raw coke oven gas of more than 650 DEG C out of cooking camber heat exchange, high temperature heat exchange are carried out into high-temperature heat-exchanging 1
Device outlet raw gas temperature is down to 470 DEG C or so, reclaims Part I high-temperature residual heat.Heat transferring medium is then used according to liquid
Following current heat exchange form, heat transferring medium enters heat exchanger, is left from working medium side outlet 1.2 from the working medium side-entrance 1.1 of high-temperature heat-exchanging 1
Heat exchanger；If heat transferring medium uses gas medium, using countercurrent flow form, heat-exchange working medium enters heat exchange from inlet side 1.2
Device, outlet side 1.1 leaves heat exchanger.
The thermocouple T1 real-time monitoring high-temperature heat-exchanging outlet temperatures exported by high-temperature heat-exchanging, 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.
Enter middle temperature spray cooler 2, middle temperature spray cooler 2 from the raw coke oven gas of about 470 DEG C out of high-temperature heat-exchanging 1
It is rectangular box, the top of the middle entrance of temperature spray cooler 2 sets 3 high pressure fan nozzles 2.1, its sprinkling drop SMD scope
In 5~10 μm of ammoniacal liquor, raw coke oven gas is lowered the temperature rapidly；In 3 fan-shaped spray spouts 2.2 of its tail end top layout, its flushing liquor
SMD is near 1mm for drop, and droplet is settled for coalescence；Lower seal tank is dropped down onto under oil droplet and ammoniacal liquor, liquid level is provided with tank
Meter, mixed liquor periodically enters tar ammonia and separates link by mudhole 2.3, is condensed by preliminary cooling, higher boiling in coal gas,
High-viscosity larger molecular organicses are most of to be condensed, for follow-up low-temperature heat exchange link provides condition.Middle temperature spray cooler water
Plain cloth is put, and multiple fan nozzles are arranged in inducer, according to the Aspect Ratio of cooler, in 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 be sprayed into middle temperature
The raw coke oven gas of cooler is rapid to be cooled to 280 DEG C, and further raw coke oven gas collects the liquid core for condensing, 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, asphalt component now in raw coke oven gas, most anthracenes
Oil, part washing oil, and part H2S is removed from raw coke oven gas.From spray cooler raw coke oven gas out through electrostatic precipitator
Absorb the condensation water core do not collected by spray cooler.
In the thermocouple T2 of the different radial depths of middle temperature spray cooler 2 outlet arrangement, 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 need to reduce the spray ammonia vol of high pressure fan nozzle 2.1 less than 250 DEG C.
Enter cryogenic heat exchanger 3 by the raw coke oven gas of preliminary tar removing, heat-exchange working medium enters from tube side import 3.1.1 manages
Formula heat exchanger 3.1, heat exchanger is left from the outlet of pipe heat exchanger 3.1 3.1.2, and the raw coke oven gas by heat exchanger is further lowered the temperature,
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 controlled at 120 ± 10 DEG C
System strategy is identical with high-temperature heat-exchanging, will not be repeated here.
From the raw coke oven gas out of cryogenic heat exchanger 3 enter low temperature spray cooler 4, low temperature spray cooler construction be with often
Rule raw coke oven gas bridge tube is similar to, and by the misting cooling of mist-generating nozzle 4.1, the synthesis gas for being down to 80 DEG C enters conventional raw coke oven gas treatment
Primary cooler further cool down；Spray water droplet is collected into tar ammonia with the organic matter in the raw coke oven gas for condensing 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, middle 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
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；Solve raw coke oven gas waste heat recovery low-temperature zone
(being less than 450 DEG C) can occur the problem of coking, improve the heat exchanger life-span；Precise control cyclic ammonia water amount, than conventional recycle ammoniacal liquor
Consumption declines 50%, reduces enterprise operation cost.
Embodiment 2
The present embodiment is with the difference of above-described embodiment：Cryogenic heat exchanger and high-temperature heat-exchanging are adopted in the present embodiment
Identical working medium is used, therefore, the two to be connected in the present embodiment, heat-exchange working medium carries out tentatively adding first by cryogenic heat exchanger
Heat, enters back into high-temperature heat-exchanging and further improves the hot quality of heat-exchange working medium.
In the above-described embodiments, middle temperature cooler uses rectangular box, and the casing can not also use rectangular box,
It is the pipeline of circular or other shapes to use section.
In the above-described embodiments, the nozzles spray of middle temperature cooler is ammoniacal liquor, it will be appreciated that using ammoniacal liquor be one at this
Preferred embodiment mode is planted, rather than unique, 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 be using water smoke at this
A kind of preferred embodiment mode, rather than unique, can also use other cooling ways of this area.
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, it is to avoid form the larger temperature difference and cause heat exchanger
It is too low near 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 done 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, raw coke oven gas waste heat high/low temperature comprehensive recovering process of the present invention comprises 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 lowered the temperature using middle temperature cooler to raw coke oven gas, control the temperature of exit gas of middle temperature cooler for 260 ±
10℃；Middle 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 that the raw coke oven gas of middle temperature spray cooler is rapid to be cooled to 280 DEG C in order to enter, further raw coke oven gas passes through spraying cooling
Device collects the liquid core for condensing, 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 is 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 carbolineum, part washing oil, and part H2S is removed from raw coke oven gas.From spray cooler out
Raw coke oven gas through electrostatic precipitator absorb not by spray cooler collect condensation water core.
S3 proceeds heat exchange to raw coke oven gas using cryogenic heat exchanger, and the temperature of exit gas for controlling cryogenic heat exchanger is
120±10℃；
S4 proceeds cooling to raw coke oven gas using subcolling condenser, and the temperature of exit gas for controlling cryogenic heat exchanger is 80
±10℃.In this step, cooled down to water smoke is sprayed in raw coke oven gas.By the misting cooling of mist-generating nozzle 4.1,80 DEG C are down to
Synthesis gas enter the primary cooler of conventional raw coke oven gas treatment and further cool down；Organic matter in spray water droplet and the raw coke oven gas for condensing
Collect and enter tar ammonia separation link.
In S2, at the entrance and exit of middle temperature cooler to raw coke oven gas in spray ammoniacal liquor and cooled down, control middle temperature
Drop SMD scopes are sprayed at 5~10 μm in the porch of cooler, control middle temperature cooler exit spray drop SMD for 1 ±
0.3mm。
In S1, the initial temperature of the heat transferring medium in control high-temperature heat-exchanging is 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；Solve raw coke oven gas waste heat recovery low-temperature zone
(being less than 450 DEG C) can occur the problem of coking, improve the heat exchanger life-span；Precise control cyclic ammonia water amount, than conventional recycle ammoniacal liquor
Consumption declines 50%, reduces enterprise operation cost.
More than, only presently preferred embodiments of the present invention, but protection scope of the present invention is not limited thereto, any to be familiar with sheet
Those skilled in the art the invention discloses technical scope in, the change or replacement that can be readily occurred in should all be covered
Within protection scope of the present invention.Therefore, the protection domain that protection scope of the present invention should be defined by claim is defined.
Claims (9)
1. a kind of 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 of the waste heat that more than 470 ± 10 DEG C of the recovery raw coke oven gas put, the middle Wen Leng that raw coke oven gas is cooled to 260 ± 10 DEG C
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 middle temperature cooler bag
Include a container, the bottom level of the container less than the entrance and exit of the container lower edge highly, the container enters
Mouth and outlet are respectively arranged with least one is used to spray the nozzle of 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
Include a housing, the height of the bottom less than the entrance and exit lower edge of the housing 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. a kind of raw coke oven gas waste heat high/low temperature comprehensive recovering process, it is characterised in that：Comprise the following steps：
S1 is exchanged heat using high-temperature heat-exchanging to raw coke oven gas, and the temperature of exit gas for controlling high-temperature heat-exchanging is 470 ± 10 DEG C；
S2 is lowered the temperature using middle temperature cooler to raw coke oven gas, and the temperature of exit gas for controlling middle temperature cooler is 260 ± 10 DEG C；
S3 using cryogenic heat exchanger to raw coke oven gas proceed heat exchange, control cryogenic heat exchanger temperature of exit gas be 120 ±
10℃；
S4 proceeds cooling to raw coke oven gas using subcolling condenser, and the temperature of exit gas for controlling cryogenic heat exchanger is 80 ± 10
℃。
7. raw coke oven gas waste heat high/low temperature comprehensive recovering process as claimed in claim 6, it is characterised in that：In S2, in middle Wen Leng
But cooled down to sprinkling ammoniacal liquor in raw coke oven gas at the entrance and exit of device, controlled the porch sprinkling Suo Taier of middle temperature cooler
Average diameter (SMD) scope controls the exit of middle temperature cooler to spray drop SMD for 1 ± 0.3mm at 5~10 μm.
8. raw coke oven gas waste heat high/low temperature comprehensive recovering process as claimed in claim 6, it is characterised in that：In S1, high temperature is controlled
The initial temperature of the heat transferring medium in heat exchanger is not less than 100 DEG C.
9. raw coke oven gas waste heat high/low temperature comprehensive recovering process as claimed in claim 6, it is characterised in that：In the S4, Xiang Huangmei
Water smoke is sprayed in gas to be cooled down.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111521037A (en) * | 2020-03-20 | 2020-08-11 | 北京国利衡清洁能源科技(集团)有限公司 | Pipeline type raw gas precooling system and precooling method thereof |
| CN113091481A (en) * | 2021-04-15 | 2021-07-09 | 唐山市宝凯科技有限公司 | Device and method for recovering waste heat of crude gas of bridge pipe |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111521037A (en) * | 2020-03-20 | 2020-08-11 | 北京国利衡清洁能源科技(集团)有限公司 | Pipeline type raw gas precooling system and precooling method thereof |
| CN113091481A (en) * | 2021-04-15 | 2021-07-09 | 唐山市宝凯科技有限公司 | Device and method for recovering waste heat of crude gas of bridge pipe |
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