CN101608137A - Primary cooling process for coal gas - Google Patents
Primary cooling process for coal gas Download PDFInfo
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- CN101608137A CN101608137A CNA2008100393166A CN200810039316A CN101608137A CN 101608137 A CN101608137 A CN 101608137A CN A2008100393166 A CNA2008100393166 A CN A2008100393166A CN 200810039316 A CN200810039316 A CN 200810039316A CN 101608137 A CN101608137 A CN 101608137A
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Abstract
The invention discloses a kind of primary cooling process for coal gas.By having the transverse pipe initial cooler of recirculated water section and low-temperature cooling water section, raw gas is cooled to 20～30 ℃, simultaneously spray the tar proportioning in 2～10% gas liquor in the low-temperature cooling water section of transverse pipe initial cooler, remove the naphthalene that coal gas is separated out; Directly spraying with direct-cooled circulation fluid in the cooling tower, coal gas is washed then, remove suspension tar and the dust carried secretly in the coal gas.The present invention makes full use of transverse pipe initial cooler cooling efficiency height, remove the good characteristics of the effective and direct cooling tower washing effect of naphthalene carries out effective process combination, can more effectively carry out coal gas cooling, remove naphthalene and dedusting, reduce the obstruction of coal gas after device, improve equipment operating environment, realize energy-saving and cost-reducing.
Description
Technical field
The present invention relates to primary cooling process for coal gas and relate to fine purification technique for coke oven gas, refer to that more specifically a kind of coal gas that helps removes naphthalene and coal gas cooling, and go out to greatest extent except that tar in the coal gas and dust, when guaranteeing coal gas cooling and washing, optimize primary cooling process for coal gas, reduced one-time investment.
Background technology
In fine purification technique for coke oven gas, raw gas temperature height, volume that coke oven produces are big, must just can enter gas blower and follow-up gas cleaning device through after the preliminary cooling of coal gas.Primary cooling process for coal gas commonly used has: transverse tube primary cooling process, transverse tube are just cold or standpipe is just cold+and direct process for cooling.
In the transverse tube primary cooling process, 80～85 ℃ of the raw gas that coke oven comes, after recirculated water cooling and the cooling of low-temperature cooling water adverse current, satisfy the coal gas set temperature (generally at 20～30 ℃) of user's needs, it is laggard to the gas purification after-treatment device to boost through gas blower again.As shown in Figure 1.
Coke-oven gas is from 82 ℃ of about 293g/m of phlegma that are cooled to 25 ℃ of generations
3, the coal gas treatment capacity of separate unit transverse pipe initial cooler is pressed 25000m
3/ h meter, gas liquor amount 7.3m
3/ h, phlegma magnitude of recruitment 25～30m of every
3/ h.The phlegma specific liquid rate 2.6～2.9m of low-temperature cooling water section
3/ m
2, liquid-gas ratio 0.4L/m
3Coal gas.At this moment, because contain a spot of tar in the phlegma, the naphthalene that the coal gas cooling separates out at first is condensed, and liquid washs and dissolving, because the phlegma of transverse pipe initial cooler has from washing action tube wall, the naphthalene that part sticks to tube wall also is rinsed.Therefore, transverse pipe initial cooler has favorable cooling effect, and the suspension naphthalene removes naphthalene efficient more than 90% in the coal gas.
But, because the phlegma specific liquid rate of transverse pipe initial cooler is low, the non-constant of washing effect to dust such as the tar in the coal gas and coal dust, burnt parts, cooling coal gas carries a large amount of tar secretly and dust enters into follow-up gas cleaning device, cause that equipment, pipeline, filler stop up, and cause the rising of the energy consumption and the cost of overhaul.
Transverse tube is just cold or standpipe is just cold+directly in the process for cooling (accompanying drawing 2 be standpipe just cold+direct process for cooling synoptic diagram), about 80～85 ℃ of the raw gas temperature that coke oven comes, be cooled to 40～45 ℃ through cold at the beginning of the transverse tube or the first cold clear recirculated water of standpipe, the total naphthalene of coal gas is not also separated out, and just cold or standpipe substantially removes naphthalene in just cold to coal gas at single transverse tube.Then, coal gas enters into direct cooling tower, utilizes circulating cooling liquid directly to contact with coal gas, and coal gas is cooled to 20～30 ℃ again.Simultaneously, in circulating cooling liquid, add 2～10% tar and remove suspension naphthalene in the coal gas, and at specific liquid rate 28～30 m
3/ m
2Condition under, tar more than 90% and dust in the coal gas are removed.Circulating cooling liquid is by the cooling that circulates of ammoniacal liquor shower nozzle, direct-cooled tower recycle pump and spiral-plate heat exchanger.
But directly the cooling of coal gas cooling tower needs outer cooling amount that coal gas is cooled to the set temperature of needs, and the cooling apparatus of configuration is also many.If the coal gas amount is at 100000m
3/ h needs configuration 146m
29～11 of spiral-plate heat exchangers, investment cost is high relatively; Behind the suspension naphthalene, interchanger stops up easily in the circulating cooling liquid washing coal gas, and management expectancy is also high.
Summary of the invention
The object of the invention is at above shortcomings in the common process, a kind of rational primary cooling process for coal gas configuration is provided, makes full use of transverse pipe initial cooler cooling efficiency height, remove the good characteristics of the effective and direct cooling tower washing effect of naphthalene and carry out effective process combination.
For achieving the above object, the present invention has adopted following technical scheme:
(1) by having the transverse pipe initial cooler of recirculated water section and low-temperature cooling water section, raw gas is cooled to 20～30 ℃, simultaneously sprays the tar proportioning in 2～10% gas liquor, remove the naphthalene that coal gas is separated out in the low-temperature cooling water section of transverse pipe initial cooler.
More specifically, the inlet water temperature of recirculated water section is controlled at is no more than 33 ℃, be generally 30～33 ℃, come 80～85 ℃ raw gas of coke oven is cooled to 40～45 ℃ through transverse pipe initial cooler recirculated water section earlier; Be cooled to 20～30 ℃ through the low-temperature cooling water section again, spray the tar proportioning in 2～10% gas liquor in the low-temperature cooling water section of transverse pipe initial cooler simultaneously, the naphthalene more than 90% that coal gas is separated out about 25 ℃ removes.The inlet water temperature of low-temperature cooling water section is controlled at and is no more than 18 ℃, is generally 16～18 ℃.
With 80000～100000m
3/ h gas meter, tar proportioning at 2～10% gas liquor magnitude of recruitment at 1～2m
3/ h.
(2) 20～30 ℃ coal gas enters into direct cooling tower, with direct-cooled circulation fluid spray, coal gas is washed, and removes suspension tar and the dust more than 90% carried secretly in the coal gas.
With 80000～100000m
3/ h gas meter, the specific liquid rate of direct-cooled circulation fluid is at 28～30m
3/ m
2
Direct-cooled circulation fluid cools off with interchanger and cool circulation water, and the temperature of cool circulation water is controlled at and is no more than 18 ℃, is generally 16～18 ℃.Interchanger can adopt spiral-plate heat exchanger.Used direct-cooled circulation fluid can be an ammoniacal liquor.
80～85 ℃ raw gas is cooled to 20～30 ℃ (claim coal gas set temperature again, the user selects according to the requirement of self) through transverse pipe initial cooler with coal gas earlier.When 25 ℃ of left and right sides, naphthalene in the coal gas is separated out, be suspended in the coal gas, part sticks to the tube wall of transverse pipe initial cooler, because transverse pipe initial cooler produces a certain amount of gas liquor with coal oven dithio-gas when 80～85 ℃ are cooled to 20～30 ℃, from top to bottom, have good in rinse capability, with the outer adherent naphthalene washes clean of tube wall.The tar proportioning of Bu Chonging can be removed the naphthalene of coal gas suspension in 2～10% gas liquor simultaneously.
The recirculated water section routinely of transverse pipe initial cooler and the configuration of low-temperature cooling water section, clear recirculated water cooling just cold with single transverse tube or that standpipe is just cold is compared, investment need increase by 20～30% on the basis of single clear recirculated water cooling, but when recirculated water section and the configuration of low-temperature cooling water section, coal gas to remove naphthalene effective, avoid the obstruction of heat exchanging device in the working cycle of direct cooling tower circulation fluid.The cooling efficiency height of transverse pipe initial cooler, after the recirculated water cooling and subcooling water cooling of 80～85 ℃ raw gas through transverse pipe initial cooler, coal gas can cool off the coal gas set temperature (20～30 ℃) that the user needs rapidly.
Directly cooling tower only washs coal gas and removes suspension tar and the dust of carrying secretly in the coal gas, guarantees the cleaning of coal gas, does not bear except that naphthalene, refrigerating function.The configuration of the cooling apparatus of circulation fluid only needs to consider coal gas caloric requirement when the temperature variation of washing process and weather seasonal variation, has avoided the but shortcoming of equipment of a large amount of configuration cycles liquid cooling of traditional technology.Therefore, the configuration of circulation fluid cooling apparatus only needs to consider the caloric requirement of coal gas in the temperature variation and the weather seasonal variation of washing process.If 9～11 spiral-plate heat exchangers of normal set-up so, only consider that the spiral-plate heat exchanger of circulation fluid washing tar and dust only needs 3 (2 open 1 is equipped with), the gross investment of direct-cooled Tower System reduces more than 50%.To be direct cooling tower contain the naphthalene amount when low at coal gas to key, and washing tar and coal dust are effective, and the system operation condition improves significantly, and go out to greatest extent except that tar in the coal gas and dust, when guaranteeing coal gas cooling and washing, optimized primary cooling process for coal gas, reduce one-time investment.
Therefore, the present invention makes full use of transverse pipe initial cooler cooling efficiency height, removes the good characteristics of the effective and direct cooling tower washing effect of naphthalene, carry out effective process combination, can more effectively carry out coal gas cooling, remove naphthalene and dedusting, reduce the obstruction of coal gas after device, improve equipment operating environment, realize energy-saving and cost-reducing.
Description of drawings
Fig. 1 is a transverse tube primary cooling process for coal gas schema.
Fig. 2 is standpipe gas primary cool+direct cooling process figure.
Fig. 3 is a novel gas primary cooling process schema.
Wherein, 1-transverse pipe initial cooler, 11-recirculated water section, 12-low-temperature cooling water section, 13-recirculated water heat transfer tube, 14-low-temperature cooling water heat transfer tube, the direct cooling tower of 2-, 21-ammoniacal liquor shower nozzle, the direct-cooled tower recycle pump of 22-, 23-spiral-plate heat exchanger, the 24-gas distributor, the 25-gas line, 26-bypass duct, the single standpipe primary cooler of 3-
Embodiment
Equipment as shown in Figure 3, transverse pipe initial cooler 1 is connected to coke oven, and transverse pipe initial cooler is divided into recirculated water section 11 and low-temperature cooling water section 12; In the recirculated water section, cool off by recirculated water heat transfer tube 13; In the low-temperature cooling water section, cool off by low-temperature cooling water heat transfer tube 14.
The transverse pipe initial cooler bottom links to each other with the bottom of direct cooling tower.
Directly be provided with one or more ammoniacal liquor shower nozzles 21 in the cooling tower, cyclic ammonia water is sprayed in the direct cooling tower by the ammoniacal liquor shower nozzle, by direct-cooled tower recycle pump 22, again via ammoniacal liquor shower nozzle is sprayed into direct cooling tower after 23 coolings of process spiral-plate heat exchanger in the bottom.In the spiral-plate heat exchanger, by the temperature of cool circulation water Control Circulation ammoniacal liquor.
Directly also be provided with gas distributor 24 in the cooling tower.Directly cooling tower top is connected with gas blower by gas line 25.Gas blower also can be connected to the bottom of transverse pipe initial cooler 1 by by-pass channel 26, and when directly cooling tower overhauled, coal gas can enter gas blower by bypass duct from the transverse pipe initial cooler bottom, normally carried to guarantee coal gas.
The inlet water temperature of recirculated water section is controlled at 30～33 ℃, and come 80～85 ℃ raw gas of coke oven is cooled to 40～45 ℃ through transverse pipe initial cooler recirculated water section earlier;
The inlet water temperature of low-temperature cooling water section is controlled at 16～18 ℃, and cooling is cooled to 20～30 ℃ with coal gas to 40～45 ℃ raw gas through the low-temperature cooling water section again;
Recirculated water and low-temperature cooling water direction are all opposite with the raw gas direction, are the adverse current cooling.
The gas liquor that produces when collecting the coal gas cooling, and after its quality of coke tar ratio is controlled at 8% is replenished and is joined the low-temperature cooling water section and spray, and removes the naphthalene in the coal gas.The coal gas amount is 80000m
3/ h, gas liquor magnitude of recruitment are 1.2m
3/ h.In this step, can remove at least 90% naphthalene of separating out because of coal gas cooling.Gas liquor can reclaim and reuse.
Through transverse pipe initial cooler cooling with after removing naphthalene, temperature enters direct cooling tower at 20～30 ℃ coal gas, the coal gas amount is 80000m
3/ h is 28m with specific liquid rate
3/ m
2Cyclic ammonia water spray, remove suspension tar and dust in the coal gas.By the direct-cooled tower recycle pump of ammoniacal liquor process of ammoniacal liquor shower nozzle spray, after being cooled off by spiral-plate heat exchanger and cool circulation water, circulation enters direct cooling tower once more again.The temperature of cool circulation water is controlled at 16～18 ℃.
Coal gas through first cold-peace purifying treatment enters gas blower through gas line 25.
Equipment is with embodiment 1.
The inlet water temperature of recirculated water section is controlled at 30～33 ℃, and come 80～85 ℃ raw gas of coke oven is cooled to 40～45 ℃ through transverse pipe initial cooler recirculated water section with coal gas earlier;
At 16～18 ℃, 40～45 ℃ raw gas is cooled to 20～30 ℃ through the low-temperature cooling water section again with the inlet water temperature of low-temperature cooling water section.
Recirculated water and low-temperature cooling water direction are all opposite with the raw gas direction, are the adverse current cooling.
The phlegma that produces when collecting the coal gas cooling, and after its quality of coke tar ratio is controlled at 3% replenishes and joins the low-temperature cooling water section and spray, and removes the naphthalene in the coal gas.The coal gas amount is 100000m
3/ h, gas liquor magnitude of recruitment are 1.8m
3/ h.In this step, can remove at least 90% naphthalene of separating out because of coal gas cooling.Gas liquor can reclaim and reuse.
Through transverse pipe initial cooler cooling with after removing naphthalene, temperature enters direct cooling tower at 20～30 ℃ coal gas, with 100000m
3/ h gas meter is 30m with specific liquid rate
3/ m
2Cyclic ammonia water spray, remove suspension tar and dust in the coal gas.
By the direct-cooled tower recycle pump of ammoniacal liquor process of ammoniacal liquor shower nozzle spray, after being cooled off by spiral-plate heat exchanger and cool circulation water, circulation enters direct cooling tower once more again.The temperature of cool circulation water is controlled at 16～18 ℃.
Coal gas through first cold-peace purifying treatment enters gas blower through gas line 25.
Claims (9)
1, a kind of primary cooling process for coal gas is characterized in that, comprises the steps:
(1) by having the transverse pipe initial cooler of recirculated water section and low-temperature cooling water section, raw gas is cooled to 20～30 ℃, simultaneously sprays the tar proportioning in 2～10% gas liquor, remove the naphthalene that coal gas is separated out in the low-temperature cooling water section of transverse pipe initial cooler;
(2) 20～30 ℃ coal gas enters into direct cooling tower, with direct-cooled circulation fluid spray, coal gas is washed, and removes suspension tar and the dust carried secretly in the coal gas.
2, the described a kind of primary cooling process for coal gas of claim 1 is characterized in that, in the step (1), raw gas is cooled to 40～45 ℃ through transverse pipe initial cooler recirculated water section earlier, is cooled to 20～30 ℃ through the low-temperature cooling water section again.
3, claim 1 or 2 described a kind of primary cooling process for coal gas is characterized in that, in the step (1), with 80000～100000m
3/ h gas meter, described tar proportioning is 1～2m at 2～10% gas liquor magnitude of recruitment
3/ h.
4, claim 1 or 2 described a kind of primary cooling process for coal gas is characterized in that, in the step (1), recirculated water section inlet water temperature is no more than 33 ℃.
5, claim 1 or 2 described a kind of primary cooling process for coal gas is characterized in that, in the step (1), subcooling recirculated water section inlet water temperature is no more than 18 ℃.
6, the described a kind of primary cooling process for coal gas of claim 1 is characterized in that, in the step (2), described direct-cooled circulation fluid is an ammoniacal liquor.
7, claim 1 or 6 described a kind of primary cooling process for coal gas is characterized in that, in the step (2), with 80000～100000m
3/ h gas meter, the specific liquid rate of described direct-cooled circulation fluid are 28～30m
3/ m
2
8, claim 1 or 6 described a kind of primary cooling process for coal gas is characterized in that, in the step (2), described direct-cooled circulation fluid cools off with interchanger and cool circulation water, and the temperature of cool circulation water is no more than 18 ℃.
9, the described a kind of primary cooling process for coal gas of claim 8 is characterized in that, described interchanger is a spiral-plate heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100393166A CN101608137A (en) | 2008-06-20 | 2008-06-20 | Primary cooling process for coal gas |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNA2008100393166A CN101608137A (en) | 2008-06-20 | 2008-06-20 | Primary cooling process for coal gas |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN101608137A true CN101608137A (en) | 2009-12-23 |
Family
ID=41482047
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|---|---|---|---|
| CNA2008100393166A Pending CN101608137A (en) | 2008-06-20 | 2008-06-20 | Primary cooling process for coal gas |
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Cited By (19)
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|---|---|---|---|---|
| CN101760250A (en) * | 2009-12-29 | 2010-06-30 | 中冶焦耐(大连)工程技术有限公司 | Novel technique for cooling of coke-oven gas |
| CN101857810A (en) * | 2010-07-07 | 2010-10-13 | 沈文奎 | Novel full negative pressure coke oven gas purifying combination process |
| CN102587884A (en) * | 2011-12-28 | 2012-07-18 | 新奥气化采煤有限公司 | Utilizing process for underground gasified gas condensate |
| CN102732327A (en) * | 2012-06-26 | 2012-10-17 | 窦伟星 | Method for recovering benzene hydrocarbon from coal gas |
| CN103031159A (en) * | 2013-01-07 | 2013-04-10 | 唐山中润煤化工有限公司 | Coal gas purifying and cooling technology and system |
| CN103122261A (en) * | 2013-02-25 | 2013-05-29 | 襄阳双利环保设备有限公司 | Method for eliminating naphthaline in high-temperature coke-oven gas |
| CN103146439A (en) * | 2012-12-18 | 2013-06-12 | 柳州钢铁股份有限公司 | Coke oven gas negative pressure naphthalene washing method and equipment |
| CN103254943A (en) * | 2013-05-21 | 2013-08-21 | 中冶焦耐工程技术有限公司 | Pre-cooling process and device of low-section replenishing liquor of transverse pipe pre-cooler |
| CN103307925A (en) * | 2013-05-22 | 2013-09-18 | 济钢集团有限公司 | Transverse tube-type cooling tower with leakage testing and overhauling function and overhauling and leakage testing method |
| CN103805292A (en) * | 2012-11-13 | 2014-05-21 | 山东汉菱电气有限公司 | Weak base source self-cleaning heat exchanger for purification, desulfurization, degreasing and dehydration of gas |
| CN103897713A (en) * | 2012-12-26 | 2014-07-02 | 山东汉菱电气有限公司 | Comprehensive processing system and processing method for organic materials |
| CN104194841A (en) * | 2014-07-28 | 2014-12-10 | 洛阳龙泽焦化有限公司 | Cooling system used in primary cooler |
| CN104327884A (en) * | 2014-11-15 | 2015-02-04 | 马钢(集团)控股有限公司 | Coal gas dust removal system for low-moisture coal coking |
| CN104403703A (en) * | 2014-11-28 | 2015-03-11 | 中冶焦耐工程技术有限公司 | Spiral plate type coal gas primary cooler |
| CN104830352A (en) * | 2015-04-29 | 2015-08-12 | 济南冶金化工设备有限公司 | Direct-cooling primary-cooling device in coke oven raw gas chamber and cooling method |
| CN106590764A (en) * | 2017-01-23 | 2017-04-26 | 中冶焦耐(大连)工程技术有限公司 | Coke oven gas cooling apparatus and process |
| 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 |
| CN111662753A (en) * | 2020-05-08 | 2020-09-15 | 广东韶钢松山股份有限公司 | Tandem type coke oven gas final cooling purification equipment and process thereof |
| CN112521983A (en) * | 2020-09-28 | 2021-03-19 | 福建省气柜设备安装有限公司 | Automatic water replenishing device of gas purification system and control method thereof |
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2008
- 2008-06-20 CN CNA2008100393166A patent/CN101608137A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101760250A (en) * | 2009-12-29 | 2010-06-30 | 中冶焦耐(大连)工程技术有限公司 | Novel technique for cooling of coke-oven gas |
| CN101857810A (en) * | 2010-07-07 | 2010-10-13 | 沈文奎 | Novel full negative pressure coke oven gas purifying combination process |
| CN102587884A (en) * | 2011-12-28 | 2012-07-18 | 新奥气化采煤有限公司 | Utilizing process for underground gasified gas condensate |
| CN102587884B (en) * | 2011-12-28 | 2014-11-26 | 新奥气化采煤有限公司 | Utilizing process for underground gasified gas condensate |
| CN102732327B (en) * | 2012-06-26 | 2014-04-09 | 窦伟星 | Method for recovering benzene hydrocarbon from coal gas |
| CN102732327A (en) * | 2012-06-26 | 2012-10-17 | 窦伟星 | Method for recovering benzene hydrocarbon from coal gas |
| CN103805292B (en) * | 2012-11-13 | 2016-01-13 | 山东汉菱电气有限公司 | Weak base for gas purification desulfurization oil removing dehydration is derived from clean interchanger |
| CN103805292A (en) * | 2012-11-13 | 2014-05-21 | 山东汉菱电气有限公司 | Weak base source self-cleaning heat exchanger for purification, desulfurization, degreasing and dehydration of gas |
| CN103146439A (en) * | 2012-12-18 | 2013-06-12 | 柳州钢铁股份有限公司 | Coke oven gas negative pressure naphthalene washing method and equipment |
| CN103897713A (en) * | 2012-12-26 | 2014-07-02 | 山东汉菱电气有限公司 | Comprehensive processing system and processing method for organic materials |
| CN103897713B (en) * | 2012-12-26 | 2015-12-23 | 山东汉菱电气有限公司 | A kind of organic materials total system and treatment process |
| CN103031159A (en) * | 2013-01-07 | 2013-04-10 | 唐山中润煤化工有限公司 | Coal gas purifying and cooling technology and system |
| CN103122261A (en) * | 2013-02-25 | 2013-05-29 | 襄阳双利环保设备有限公司 | Method for eliminating naphthaline in high-temperature coke-oven gas |
| CN103122261B (en) * | 2013-02-25 | 2014-02-19 | 襄阳双利环保设备有限公司 | Method for eliminating naphthaline in high-temperature coke-oven gas |
| CN103254943A (en) * | 2013-05-21 | 2013-08-21 | 中冶焦耐工程技术有限公司 | Pre-cooling process and device of low-section replenishing liquor of transverse pipe pre-cooler |
| CN103307925A (en) * | 2013-05-22 | 2013-09-18 | 济钢集团有限公司 | Transverse tube-type cooling tower with leakage testing and overhauling function and overhauling and leakage testing method |
| CN104194841A (en) * | 2014-07-28 | 2014-12-10 | 洛阳龙泽焦化有限公司 | Cooling system used in primary cooler |
| CN104327884A (en) * | 2014-11-15 | 2015-02-04 | 马钢(集团)控股有限公司 | Coal gas dust removal system for low-moisture coal coking |
| CN104403703A (en) * | 2014-11-28 | 2015-03-11 | 中冶焦耐工程技术有限公司 | Spiral plate type coal gas primary cooler |
| CN104830352A (en) * | 2015-04-29 | 2015-08-12 | 济南冶金化工设备有限公司 | Direct-cooling primary-cooling device in coke oven raw gas chamber and cooling method |
| CN106590764A (en) * | 2017-01-23 | 2017-04-26 | 中冶焦耐(大连)工程技术有限公司 | Coke oven gas cooling apparatus and process |
| 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 |
| CN111662753A (en) * | 2020-05-08 | 2020-09-15 | 广东韶钢松山股份有限公司 | Tandem type coke oven gas final cooling purification equipment and process thereof |
| CN112521983A (en) * | 2020-09-28 | 2021-03-19 | 福建省气柜设备安装有限公司 | Automatic water replenishing device of gas purification system and control method thereof |
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Application publication date: 20091223 |