CN107420868A - A kind of coal oven dithio-gas high temperature section heat high efficiente callback technique - Google Patents
A kind of coal oven dithio-gas high temperature section heat high efficiente callback technique Download PDFInfo
- Publication number
- CN107420868A CN107420868A CN201710598509.4A CN201710598509A CN107420868A CN 107420868 A CN107420868 A CN 107420868A CN 201710598509 A CN201710598509 A CN 201710598509A CN 107420868 A CN107420868 A CN 107420868A
- Authority
- CN
- China
- Prior art keywords
- heat exchanger
- heat
- gas
- bushing type
- vapor
- 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.)
- Pending
Links
- 238000000034 method Methods 0.000 title claims abstract description 24
- 239000003245 coal Substances 0.000 title claims abstract description 23
- 239000007789 gas Substances 0.000 claims abstract description 53
- 239000000571 coke Substances 0.000 claims abstract description 44
- 239000002918 waste heat Substances 0.000 claims abstract description 25
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000010791 quenching Methods 0.000 claims abstract description 22
- 230000000171 quenching effect Effects 0.000 claims abstract description 22
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 22
- 238000004140 cleaning Methods 0.000 claims abstract description 20
- 238000004939 coking Methods 0.000 claims abstract description 15
- 238000006392 deoxygenation reaction Methods 0.000 claims abstract description 6
- 238000010612 desalination reaction Methods 0.000 claims abstract description 5
- 239000000779 smoke Substances 0.000 claims description 10
- 238000009413 insulation Methods 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 4
- 239000003153 chemical reaction reagent Substances 0.000 claims description 3
- 238000007664 blowing Methods 0.000 claims description 2
- 235000019504 cigarettes Nutrition 0.000 claims 1
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 claims 1
- 239000010931 gold Substances 0.000 claims 1
- 229910052737 gold Inorganic materials 0.000 claims 1
- 238000005345 coagulation Methods 0.000 abstract description 2
- 230000015271 coagulation Effects 0.000 abstract description 2
- 229920002521 macromolecule Polymers 0.000 abstract description 2
- 229920000642 polymer Polymers 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 description 6
- 238000011084 recovery Methods 0.000 description 5
- 235000011114 ammonium hydroxide Nutrition 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 238000001816 cooling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000012544 monitoring process Methods 0.000 description 2
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000003763 carbonization Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003500 flue dust Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000012716 precipitator Substances 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
- C10K1/046—Reducing the tar content
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Life Sciences & Earth Sciences (AREA)
- Sustainable Development (AREA)
- Sustainable Energy (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a kind of coal oven dithio-gas high temperature section heat high efficiente callback technique, the bushing type vapor heat exchanger that coal oven dithio-gas enters in standpipe bushing type quenching waste heat boiler exchanges heat with water, and temperature is reduced to less than 350 DEG C after heat exchange；Boiler feedwater is through desalination, deoxygenation, then enters after cryogenic heat exchanger exchanges heat to more than 210 DEG C and HTHP saturated vapor is produced in vertical pipe sleeve tubular type quenching waste heat boiler；HTHP saturated vapor is delivered to high-voltage power user after overheat or used after pressure and temperature reducing for low-pressure steam user；Because heat exchanger tube tube wall temperature is more than tar dew-point temperature when raw coke oven gas and water exchange heat, the heat exchanger tube coking cycles length of bushing type vapor heat exchanger；The present invention is capable of the high temperature section heat of high efficiente callback coal oven dithio-gas and produces HTHP saturated vapor, and then produces high pressure superheated steam or low-pressure saturated steam；Meanwhile, it is capable to reduce equipment inner macromolecule polymer coagulation, extend coking cycles, improve coke cleaning efficiency, safeguards system stable operation.
Description
Technical field
The present invention relates to residual heat utilizing technology of coke oven crude gas field, more particularly to a kind of coal oven dithio-gas high temperature section heat
High efficiente callback technique.
Background technology
The raw gas temperature of coke furnace carbonization chamber outlet is about 650~750 DEG C, has very high heat, the high efficiente callback portion
Point heat is to coking industry energy conservation, increasing economic efficiency is significant, meanwhile, high efficiente callback raw coke oven gas high temperature section heat is
Improve the committed step of raw coke oven gas waste heat recovery efficiency.At present, it has been disclosed that waste heat of coke oven crude gas recovery process mainly have with
Lower three kinds：1) using rising heat exchange of heat pipe recovery crude-gas sensible heat and production 0.4~0.6MPa low-pressure saturated steams；2) by dedusting
Raw coke oven gas afterwards imports waste heat boiler, and sprinkling ammoniacal liquor continues to cool after raw gas temperature is down to 150 DEG C, treats that temperature reaches 70~90
After DEG C, raw coke oven gas is sent to follow-up workshop section through gas cooler；3) ammoniacal liquor is sprayed into raw coke oven gas, after being cooled to 70~90 DEG C
Low temperature exhaust heat is reclaimed using gas cooler.
More deficiency be present in three of the above process route：The first technique is steamed, and category is single, steam production is few and easily makes
Coking even leak in tedge, influence coke oven operation；The coking easily in heat exchanger tube of second of technique, causes heat exchange efficiency
It is low, or even phenomena such as generation plugging, booster, influence to keep the safety in production；The heat grade of the third technique recovery is low, and the thermal efficiency is low,
Ammoniacal liquor consumption is big, and sewage discharge is more.
The content of the invention
, being capable of high efficiente callback coke oven famine coal the invention provides a kind of coal oven dithio-gas high temperature section heat high efficiente callback technique
The high temperature section heat of gas simultaneously produces HTHP saturated vapor, and then produces high pressure superheated steam or low-pressure saturated steam；Meanwhile
Equipment inner macromolecule polymer coagulation can be reduced, extends coking cycles, improves coke cleaning efficiency, safeguards system stable operation.
In order to achieve the above object, the present invention is realized using following technical scheme：
A kind of coal oven dithio-gas high temperature section heat high efficiente callback technique, produced using standpipe bushing type quenching waste heat boiler high
Warm high-pressure saturated steam, and then produce high pressure superheated steam or low-pressure saturated steam；Meanwhile heat exchanger tube tube wall temperature is controlled in Jiao
It is more than oily dew-point temperature；Comprise the following steps that：
1) raw gas system：The coal oven dithio-gas that more than 600 DEG C of temperature enters in standpipe bushing type quenching waste heat boiler
Bushing type vapor heat exchanger exchanges heat with water, and temperature is reduced to less than 350 DEG C after heat exchange；Raw coke oven gas enters standpipe bushing type chilling used heat
The mean flow rate of boiler is 25~40m/s, and the heat exchanger tube tube wall temperature of bushing type vapor heat exchanger is not less than 320 DEG C；
2) boiler circuit：Boiler feedwater is through desalination, deoxygenation, then enters after cryogenic heat exchanger exchanges heat to more than 210 DEG C and stand
Drum in pipe sleeve tubular type quenching waste heat boiler, then from down-comer sleeve pipe formula vapor heat exchanger, changed in bushing type steam
It is heated to be in hot device by raw coke oven gas after steam water interface and returns to drum through tedge, steam-water separation is carried out in drum, produces pressure
10~13MPa of power, the HTHP saturated vapor of 311~331 DEG C of temperature；HTHP saturated vapor delivers to high pressure after overheat
Generating user uses after pressure and temperature reducing for low-pressure steam user, and boiler feedwater is again by down-comer sleeve pipe formula steam heat-exchanging
Device continues the circulation for being heated, being gone round and begun again；
3) heat exchanger tube coke cleaning：Because heat exchanger tube tube wall temperature is more than tar dew-point temperature when raw coke oven gas and water exchange heat, set
The heat exchanger tube coking cycles length of pipes type steaming heat exchanger, by monitoring coking situation on-line, it is necessary to use online steam during coke cleaning
Purging, waterpower cleaning, chemical reagent cleaning or mechanical cleaning mode remove tar in heat exchanger tube.
The heat transferring medium to be exchanged heat in the cryogenic heat exchanger with boiler feedwater is high temperature tar.
The standpipe bushing type quenching waste heat boiler is made up of bushing type vapor heat exchanger and drum, bushing type steam heat-exchanging
Device includes upper smoke box, lower smoke box, sleeve pipe, oblate pipe tube sheet, heat exchanger tube, upper header and lower collector pipe, wherein on the outside of oblate pipe tube sheet
It is connected with heat exchanger tube, sleeve pipe bag is outside heat exchanger tube, and sleeve pipe on the inside of oblate pipe tube sheet with being connected, oblate pipe tube sheet and upper and lower collector
Connection, upper and lower collector connected by tedge and down-comer with drum respectively, and the side of drum is provided with water inlet, drum it is upper
Side is provided with steam (vapor) outlet.
Thermal insulation layer is provided with the upper smoke box.
The oblate pipe tube sheet of described sleeve pipe formula vapor heat exchanger uses circular arc or Long Circle.
The heat exchanger tube of described sleeve pipe formula vapor heat exchanger is 41, and is cased with sleeve pipe outside every heat exchanger tube.
Compared with prior art, the beneficial effects of the invention are as follows：
1) present invention leads to coal oven dithio-gas in standpipe bushing type quenching waste heat boiler, to coal oven dithio-gas high temperature section
Heat is recycled, and heat-exchange system and coke oven independent operating, is independent of each other；
2) present invention can produce HTHP saturated vapor, while heat exchanger tube tube wall temperature is not less than 320 DEG C, reduce knot
It is burnt and extend coking cycles；
3) present invention can both produce high pressure superheated steam and used for high-voltage power user, can produce low-pressure saturated steam confession again
Low-pressure steam user uses, and utilization of steam is extensive, strong applicability；
4) present invention is tentatively exchanged heat using cryogenic heat exchanger to the boiler feedwater after desalination, deoxygenation, is improved to water temperature
Degree rationally make use of other high-temperature mediums (such as high temperature tar) of plant area to 210 DEG C or so；Under identical output, with pot
The process system that stove feedwater is not exchanged heat tentatively is compared, steam production increase by 40%；
5) present invention uses standpipe bushing type quenching waste heat boiler, improves the pressure-resistant performance of system, and steam pressure is up to 10
~13MPa；High temperature tar moves in the presence of self gravitation to heat exchange tube bottom, and tar graphitized area is concentrated mainly on pipe
Bottom, it is easy to coke cleaning operation；Coking situation in heat exchanger tube can be monitored on-line simultaneously, be easy to coordinate manufacturing schedule, carry out coke cleaning in advance
Prepare, safeguards system stable operation.
Brief description of the drawings
Fig. 1 is a kind of flow chart of coal oven dithio-gas high temperature section heat high efficiente callback technique of the present invention.
Fig. 2 is the structural representation of standpipe bushing type quenching waste heat boiler of the present invention.
Fig. 3 is the main view profile of bushing type vapor heat exchanger of the present invention.
In figure：1. the boiler feedwater of 5. oxygen-eliminating device of coke oven 2. hot precipitator, 3. sweet-water tank, 4. deaerated feedwater pump 6.
The ash silo 13. of 11. sewage well of pump 7. cryogenic heat exchanger, 8. coke oven coke oven uprising tube, 9. discharge, 10. periodical blowdown expander 12.
Standpipe bushing type quenching waste heat boiler 13-1. bushing type vapor heat exchanger 13-2. tedge 13-3. down-comer 13-4. vapour
Wrap 13-5. upper header 13-6. lower collector pipe 13-7. thermal insulation layer 13-8. oblate pipe tube sheet 13-9. sleeve pipe 13-10. heat exchanger tubes
The steam superheater of 14. reducing-and-cooling plant of 13-11. upper smoke box 13-12. lower smoke box 13-13. steam (vapor) outlets 15.
Embodiment
The embodiment of the present invention is described further below in conjunction with the accompanying drawings：
As shown in Figure 1-Figure 3, a kind of coal oven dithio-gas high temperature section heat high efficiente callback technique of the present invention, using standpipe
Bushing type quenching waste heat boiler produces HTHP saturated vapor, and then produces high pressure superheated steam or low-pressure saturated steam；Together
When, control heat exchanger tube tube wall temperature is more than tar dew-point temperature；Comprise the following steps that：
1) raw gas system：The coal oven dithio-gas that more than 600 DEG C of temperature enters in standpipe bushing type quenching waste heat boiler 13
Bushing type vapor heat exchanger 13-1 and water exchange heat, temperature is reduced to less than 350 DEG C after heat exchange；It is anxious that raw coke oven gas enters standpipe bushing type
The mean flow rate of cold waste heat boiler 13 is 25~40m/s, and bushing type vapor heat exchanger 13-1 heat exchanger tube 13-10 tube wall temperatures are not
Less than 320 DEG C；
2) boiler circuit：Boiler feedwater is through desalination, deoxygenation, then enters after cryogenic heat exchanger 7 exchanges heat to more than 210 DEG C and stand
Drum 13-4 in pipe sleeve tubular type quenching waste heat boiler 13, then from down-comer 13-3 sleeve pipe formula vapor heat exchanger 13-1,
It is heated to be in bushing type vapor heat exchanger 13-1 by raw coke oven gas after steam water interface and returns to drum 13-4 through tedge 13-2,
Steam-water separation is carried out in drum 13-4, produces 10~13MPa of pressure, the HTHP saturated vapor of 311~331 DEG C of temperature；It is high
Warm high-pressure saturated steam is delivered to high-voltage power user after overheat or used after pressure and temperature reducing for low-pressure steam user, and boiler is given
Water continues the circulation for being heated, being gone round and begun again by down-comer 13-3 sleeve pipe formula vapor heat exchangers 13-1 again；
3) heat exchanger tube coke cleaning：Due to when raw coke oven gas and water exchange heat heat exchanger tube 13-10 tube wall temperatures tar dew-point temperature with
On, bushing type vapor heat exchanger 13-1 heat exchanger tube 13-10 coking cycles length, by monitoring coking situation on-line, it is necessary to coke cleaning
The online steam blowings of Shi Caiyong, waterpower cleaning, chemical reagent cleaning or mechanical cleaning mode remove tar in heat exchanger tube 13-10.
The heat transferring medium to be exchanged heat in the cryogenic heat exchanger 7 with boiler feedwater is high temperature tar.
As shown in Figure 2 and Figure 3, the standpipe bushing type quenching waste heat boiler 13 is by bushing type vapor heat exchanger 13-1 and vapour
13-4 compositions are wrapped, bushing type vapor heat exchanger 13-1 includes upper smoke box 13-11, lower smoke box 13-12, sleeve pipe 13-9, oblate pipe pipe
Plate 13-8, heat exchanger tube 13-10, upper header 13-5 and lower collector pipe 13-6, wherein oblate pipe tube sheet 13-8 outside and heat exchanger tube 13-10
Connection, sleeve pipe 13-9 bags are outside heat exchanger tube 13-10, and sleeve pipe 13-9 on the inside of oblate pipe tube sheet 13-8 with being connected, oblate pipe tube sheet 13-
8 connect with upper and lower collector 13-5,13-6, upper and lower collector 13-5,13-6 respectively by tedge 13-2 and down-comer 13-3 with
Drum 13-4 is connected, and drum 13-4 side is provided with water inlet, and drum 13-4 top is provided with steam (vapor) outlet 13-13.
Thermal insulation layer 13-7 is provided with the upper smoke box 13-11.
Described sleeve pipe formula vapor heat exchanger 13-1 oblate pipe tube sheet 13-8 uses circular arc or Long Circle.
Described sleeve pipe formula vapor heat exchanger 13-1 heat exchanger tube 13-10 is 41, and is cased with outside every heat exchanger tube 13-10
Sleeve pipe 13-9.
Following examples are implemented under premised on technical solution of the present invention, give detailed embodiment and tool
The operating process of body, but protection scope of the present invention is not limited to following embodiments.Method therefor is such as without spy in following embodiments
It is conventional method not mentionlet alone bright.
【Embodiment】
In the present embodiment, a kind of described coal oven dithio-gas high temperature section heat high efficiente callback technique, step is as follows：
650~750 DEG C of raw coke oven gas from coke oven 1 enter discharge 9 by coke oven coke oven uprising tube 8, enter height after flue dust aggregation
Warm deduster 2 carries out dedusting, and the raw coke oven gas after dedusting is exchanged heat into standpipe bushing type quenching waste heat boiler 13, after dedusting
Lime-ash enters outer row after ash silo 12；
The bushing type vapor heat exchanger 13-1 that raw coke oven gas enters in standpipe bushing type quenching waste heat boiler 13 is exchanged heat, and is protected
Hold raw coke oven gas inlet temperature be about 600 DEG C, 25~40m/s of mean flow rate, 330 DEG C of heat exchanger tube 13-10 tube wall temperatures, it is low after heat exchange
Warm raw coke oven gas enters other workshop sections and carries out low-temperature zone heat recovery；Meanwhile the normal temperature demineralized water in sweet-water tank 3 is successively through deoxygenation
Temperature reaches 160 DEG C after feed pump 4, oxygen-eliminating device 5,160 DEG C of deaerated feedwater through boiler feed pump 6 enter cryogenic heat exchanger 7 with
Temperature reaches 210 DEG C after high temperature tar heat exchange.
210 DEG C of boiler feedwater enters after drum 13-4 through down-comer 13-3 sleeve pipe formula vapor heat exchanger 13-1, leads to
Heat exchange is crossed, becomes through tedge 13-2 to enter in drum 13-4 after steam water interface and carries out vapor-liquid separation, it is high to produce high temperature
Saturated vapor (10~13MPa of steam pressure, 311~331 DEG C of vapor (steam) temperature) is pressed, can be entered as needed into steam superheater 15
High-voltage power user is delivered to after row overheat or delivers to each low-pressure steam after carrying out desuperheat, decompression into reducing-and-cooling plant 14 and is used
Family.
Caused waste water is discharged into standpipe bushing type quenching waste heat boiler 13 through periodical blowdown expander 10 in process of production
Sewage well 11.
The present invention replaces conventional shell-and-tube heat exchanger using bushing type vapor heat exchanger 13-1, substantially increases heat exchange effect
Rate；Combined using oblate pipe tube sheet 13-8 and replace conventional flat tube plate structure, oblate pipe tube sheet 13-8 is applied to high pressure occasion, and can
Alleviate thermal expansion influence.
Boiler feedwater temperature after cryogenic heat exchanger 7 reaches 210 DEG C, can significantly shorten boiler feedwater in bushing type steam
Heat-exchange time in heat exchanger 13-1, improve operating efficiency.
25~40m/s of mean flow rate that raw coke oven gas enters in standpipe bushing type quenching boiler 13；Sleeve pipe 13-9 and heat exchanger tube
13-10 annular spaces medium temperature is higher than 324 DEG C, and heat exchanger tube 13-10 tube wall temperatures are higher than 320 DEG C (being higher than tar dew-point temperature), energy
Equipment coking amount is enough reduced, extends coke cleaning period.
The foregoing is only a preferred embodiment of the present invention, but protection scope of the present invention be not limited thereto,
Any one skilled in the art the invention discloses technical scope in, technique according to the invention scheme and its
Inventive concept is subject to equivalent substitution or change, should all be included within the scope of the present invention.
Claims (6)
1. a kind of coal oven dithio-gas high temperature section heat high efficiente callback technique, it is characterised in that using standpipe bushing type chilling used heat
Boiler for producing HTHP saturated vapor, and then produce high pressure superheated steam or low-pressure saturated steam；Meanwhile control heat exchanger tube gold
Belong to wall temperature more than tar dew-point temperature；Comprise the following steps that：
1) raw gas system：The sleeve pipe that the coal oven dithio-gas that more than 600 DEG C of temperature enters in standpipe bushing type quenching waste heat boiler
Formula vapor heat exchanger exchanges heat with water, and temperature is reduced to less than 350 DEG C after heat exchange；Raw coke oven gas enters standpipe bushing type quenching waste heat boiler
Mean flow rate be 25~40m/s, the heat exchanger tube tube wall temperature of bushing type vapor heat exchanger is not less than 320 DEG C；
2) boiler circuit：Boiler feedwater enters vertical pipe sleeve through desalination, deoxygenation, then after cryogenic heat exchanger exchanges heat to more than 210 DEG C
Drum in tubular type quenching waste heat boiler, then from down-comer sleeve pipe formula vapor heat exchanger, in bushing type vapor heat exchanger
It is interior to be heated to be by raw coke oven gas after steam water interface through tedge return drum, steam-water separation is carried out in drum, produces pressure 10
~13MPa, the HTHP saturated vapor of 311~331 DEG C of temperature；HTHP saturated vapor delivers to high-voltage power after overheat
User or after pressure and temperature reducing for low-pressure steam user use, boiler feedwater again by down-comer sleeve pipe formula vapor heat exchanger after
It is continuous to be heated, the circulation to be gone round and begun again；
3) heat exchanger tube coke cleaning：Because heat exchanger tube tube wall temperature is more than tar dew-point temperature when raw coke oven gas and water exchange heat, bushing type
The heat exchanger tube coking cycles length of vapor heat exchanger, by monitor coking situation on-line, it is necessary to during coke cleaning using online steam blowing,
Waterpower cleaning, chemical reagent cleaning or mechanical cleaning mode remove tar in heat exchanger tube.
2. a kind of coal oven dithio-gas high temperature section heat high efficiente callback technique according to claim 1, it is characterised in that described
The heat transferring medium to be exchanged heat in cryogenic heat exchanger with boiler feedwater is high temperature tar.
3. a kind of coal oven dithio-gas high temperature section heat high efficiente callback technique according to claim 1, it is characterised in that described
Standpipe bushing type quenching waste heat boiler is made up of bushing type vapor heat exchanger and drum, and bushing type vapor heat exchanger includes upper cigarette
Connect on the outside of case, lower smoke box, sleeve pipe, oblate pipe tube sheet, heat exchanger tube, upper header and lower collector pipe, wherein oblate pipe tube sheet with heat exchanger tube
Connect, sleeve pipe bag is outside heat exchanger tube, and sleeve pipe on the inside of oblate pipe tube sheet with being connected, and oblate pipe tube sheet and upper and lower header in communication are upper and lower
Collector is connected by tedge and down-comer with drum respectively, and the side of drum is provided with water inlet, and the top of drum is provided with steam
Outlet.
4. a kind of coal oven dithio-gas high temperature section heat high efficiente callback technique according to claim 3, it is characterised in that described
Thermal insulation layer is provided with upper smoke box.
5. a kind of coal oven dithio-gas high temperature section heat high efficiente callback technique according to claim 3, it is characterised in that described
The oblate pipe tube sheet of bushing type vapor heat exchanger uses circular arc or Long Circle.
6. a kind of coal oven dithio-gas high temperature section heat high efficiente callback technique according to claim 3, it is characterised in that described
The heat exchanger tube of bushing type vapor heat exchanger is 41, and is cased with sleeve pipe outside every heat exchanger tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710598509.4A CN107420868A (en) | 2017-07-21 | 2017-07-21 | A kind of coal oven dithio-gas high temperature section heat high efficiente callback technique |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710598509.4A CN107420868A (en) | 2017-07-21 | 2017-07-21 | A kind of coal oven dithio-gas high temperature section heat high efficiente callback technique |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN107420868A true CN107420868A (en) | 2017-12-01 |
Family
ID=60430890
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201710598509.4A Pending CN107420868A (en) | 2017-07-21 | 2017-07-21 | A kind of coal oven dithio-gas high temperature section heat high efficiente callback technique |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107420868A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108036290A (en) * | 2017-12-22 | 2018-05-15 | 中冶焦耐(大连)工程技术有限公司 | A kind of coal oven dithio-gas heat recovery process free of discontinuities |
| CN108342199A (en) * | 2018-04-16 | 2018-07-31 | 福建省东锅节能科技有限公司 | Annular membrane water-cooled jacket, crude-gas sensible heat recycling power generator and its working method |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003329201A (en) * | 2002-05-07 | 2003-11-19 | Babcock Hitachi Kk | Exhaust heat recovery boiler, combined power generation method and device |
| CN101725954A (en) * | 2008-10-24 | 2010-06-09 | 同济大学 | Novel process for coupling utilization of waste heat recovery of riser of coke oven and coke dry quenching system |
| CN102796537A (en) * | 2012-08-31 | 2012-11-28 | 上海宝钢节能技术有限公司 | System and method for recovering superheated steam of waste heat of raw gas of combined coke oven |
| CN103436271A (en) * | 2013-08-30 | 2013-12-11 | 常州江南电力节能科技有限公司 | System for recycling raw gas afterheat of coke oven |
| CN103952162A (en) * | 2014-04-16 | 2014-07-30 | 上海交通大学 | Coke oven sensile heat recovery process |
| CN104266159A (en) * | 2014-09-29 | 2015-01-07 | 南京竣业过程机械设备有限公司 | Waste heat recovery technology for crude gas of novel coke oven |
-
2017
- 2017-07-21 CN CN201710598509.4A patent/CN107420868A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003329201A (en) * | 2002-05-07 | 2003-11-19 | Babcock Hitachi Kk | Exhaust heat recovery boiler, combined power generation method and device |
| CN101725954A (en) * | 2008-10-24 | 2010-06-09 | 同济大学 | Novel process for coupling utilization of waste heat recovery of riser of coke oven and coke dry quenching system |
| CN102796537A (en) * | 2012-08-31 | 2012-11-28 | 上海宝钢节能技术有限公司 | System and method for recovering superheated steam of waste heat of raw gas of combined coke oven |
| CN103436271A (en) * | 2013-08-30 | 2013-12-11 | 常州江南电力节能科技有限公司 | System for recycling raw gas afterheat of coke oven |
| CN103952162A (en) * | 2014-04-16 | 2014-07-30 | 上海交通大学 | Coke oven sensile heat recovery process |
| CN104266159A (en) * | 2014-09-29 | 2015-01-07 | 南京竣业过程机械设备有限公司 | Waste heat recovery technology for crude gas of novel coke oven |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108036290A (en) * | 2017-12-22 | 2018-05-15 | 中冶焦耐(大连)工程技术有限公司 | A kind of coal oven dithio-gas heat recovery process free of discontinuities |
| CN108342199A (en) * | 2018-04-16 | 2018-07-31 | 福建省东锅节能科技有限公司 | Annular membrane water-cooled jacket, crude-gas sensible heat recycling power generator and its working method |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107286961A (en) | A kind of coal oven dithio-gas high temperature section heat high efficiente callback device | |
| CN103131432B (en) | Method for recovering waste heat from coke oven raw gas | |
| CN102796537B (en) | System and method for recovering superheated steam of waste heat of raw gas of combined coke oven | |
| CN104048284B (en) | The method of high-temp solid heat recovery waste heat boiler and recovery waste heat | |
| CN201942519U (en) | Thermal energy recovery and utilization device in production of thermal phosphoric acid and production system of thermal energy recovery and utilization device | |
| CN206875995U (en) | Heat power generating system based on coke-oven plant's residual heat and energy integrated utilization | |
| CN107420868A (en) | A kind of coal oven dithio-gas high temperature section heat high efficiente callback technique | |
| CN208594234U (en) | A kind of residual heat heat-exchanging device recycling raw coke over gas riser | |
| CN109282260B (en) | Raw coke oven gas waste heat recovery device and system | |
| CN201772424U (en) | Coke oven gas primary-cooling waste-heat boiler | |
| CN102519285B (en) | Integrated technique and special equipment for raw gas waste heat recovery and steam replacement with heat transfer soil | |
| CN207047150U (en) | A kind of coal oven dithio-gas high temperature section heat high efficiente callback device | |
| CN209540847U (en) | A kind of Low Pressure Gas Network superhigh temperature steam generator | |
| CN205382137U (en) | Double -boiler stove coarse coal gas cooling dust collector | |
| CN208545368U (en) | A kind of coal gasification apparatus | |
| CN111336487A (en) | Coke oven raw gas and waste gas waste heat recycling system | |
| CN201289318Y (en) | Waste heat recovery from smelting reduction ironmaking in heat pipe type rotary hearth furnace and steam production apparatus | |
| CN207262396U (en) | A kind of dry coke quenching superpressure boiler therrmodynamic system | |
| CN104728821A (en) | Ascending pipe raw gas waste heat utilizing boiler system | |
| CN108036290A (en) | A kind of coal oven dithio-gas heat recovery process free of discontinuities | |
| CN205740915U (en) | A kind of coal gasification apparatus with useless pot | |
| CN108504392A (en) | A kind of coal gasification apparatus and technique | |
| CN106370028A (en) | Coking raw gas waste heat recovery method and apparatus | |
| CN110500567A (en) | A kind of efficient nuclear energy uses system and method | |
| CN204786295U (en) | Tedge raw coke oven gas waste heat utilization boiler system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20171201 |