CN101619243A - Gas naphthalene washing process in primary-cooling working procedure of coke oven gas purification unit - Google Patents
Gas naphthalene washing process in primary-cooling working procedure of coke oven gas purification unit Download PDFInfo
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Abstract
The invention discloses a gas naphthalene washing process in a primary-cooling working procedure of a coke oven gas purification unit. In the naphthalene washing process, a separating system is arranged and comprises an upper condensate separating tank positioned near to a cooler, wherein the condensate on the upper stage of the cooler flows to the upper condensate separating tank in a form of gravity flow and stands in the tank for at least more than 30 min, and the separated tar flows to a lower circulating naphthalene washing liquid tank. Compared with the prior art, the invention has the advantages: firstly, the condensate continuously produced during the coke oven gas condensation process is used for washing naphthalene, the naphthalene content in the purified gas is 350-100 mg/m<3>, the dew-point temperature of naphthalene in the gas is lower than the gas temperature, a naphthalene removal device is not required to be arranged in the follow-up gas purification working procedure and the multi-step naphthalene washing process is changed into a one-step naphthalene washing process; secondly, the number of the process equipment is reduced to be minimum than that of the prior known naphthalene washing process, therefore, the land occupied by the equipment is also correspondingly reduced; and thirdly, the energy consumption of the working procedure is reduced.
Description
Technical field:
The invention belongs to the coke oven gas purification unit of coke-oven plant, belong to the coal gas naphthalene washing process in the coke oven gas purification unit primary-cooling working procedure especially.
Background technology:
Coke-oven gas is in scavenging process, and the naphthalene in the coal gas can be separated out the gas purification equipment that stops up with the reduction of temperature, is conceived to just the naphthalene in the coal gas is removed to below the dew-point temperature in coke oven gas purification unit primary-cooling working procedure in the industry at present.Corresponding naphthalene washing process mainly contains :-direct-cooled placed in-line just cold first cold naphthalene (being called for short technology 2) and the just cold and whole cold process intermediary oil wash naphthalene (being called for short technology 3) of removing that removes naphthalene (being called for short technology 1), indirect transverse tube type primary cooler.In the technology 1, coal gas at first is cooled to about 50 ℃ at the indirect type primary cooler, be cooled to specified temperature at the direct type primary cooler then, in the direct type primary cooler, coal gas is contained a large amount of ammoniacal liquor circulation sprinkling coolings of a small amount of tar, the naphthalene of condensation is dissolved by tar, and gas exit contains the naphthalene amount and approaches the saturated naphthalene amount that contains under the temperature out, and the shortcoming that this kind technology (comparing with the present invention) exists is: (1) gas exit contains the naphthalene amount and approaches the saturated naphthalene amount that contains under the temperature out; (2) number of devices many (ammoniacal liquor water coolers); (3) need in cooling ammoniacal liquor system, to replenish tar; (4) ammoniacal liquor water cooler material is a stainless steel.In the technology 2, coal gas and phlegma all are mobile from top to bottom in the transverse tube type primary cooler, the moisture tar (or claiming emulsion) that utilizes the tar ammonia separation circuit in the middle and lower part of primary cooler is washing away the water-cooled tube outer wall, the naphthalene that condensation in the coal gas is separated out is dissolved fully by tar and can not stop up primary cooler, the shortcoming that this kind technology exists is: (1) needs the next moisture tar of hypomere cooling tar ammonia separation circuit at primary cooler, energy consumption height; (2) to wash naphthalene liquid storage tank volume big for oily water separating equipment and circulation, and number of devices is many.Technology 3 adopts tar washing oil or solar oil etc. to make absorption agent, and the shortcoming that this kind technology exists is: (1) number of devices many (washing naphthalene tower, washing oil pump or solar oil pump, washing oil groove or solar oil groove, washing oil circulation groove or solar oil circulation groove); (2) tar washing oil or solar oil need outsourcing.In addition, Chinese patent 88103450 provides a kind of coke-oven gas primary cooling technology, and the described naphthalene method of washing use tar light oil to contact with coal gas following current in two (descending) section water cooler, and the tar light oil sprinkler discharge density is greater than 1m in two sections water coolers
3/ h.m
2The described naphthalene method of washing comprises the two-part naphthalene washing process of cold wash naphthalene and whole cold wash naphthalene just, employed tar is the resulting tar light oil of epimere phlegma process separation system, described separation system comprises: condensate pit, 2 pumps, tar separator, medial launder, water cooler, the technical process complexity, equipment is many, the energy consumption height.
Summary of the invention:
Technical problem to be solved by this invention is to provide the naphthalene washing process that a kind of energy consumption is low, equipment is few in coke oven gas purification unit primary-cooling working procedure.
The technical scheme of technical solution problem of the present invention is: the coke-oven gas naphthalene washing process in coke oven gas purification unit primary-cooling working procedure, use moisture tar to contact at the gas cooler hypomere with coal gas following current in gas cooler, wash naphthalene, the mixture of the hypomere phlegma that the described moisture tar epimere phlegma that to be coal gas obtain at the gas cooler epimere obtains when the gas cooler hypomere cools off through the resulting tar light oil of separation system and coal gas, it is characterized in that: described separation system comprises near the epimere phlegma separator tank that is positioned at the gas cooler, the epimere phlegma of gas cooler flows into epimere phlegma separator tank in the mode of gravity flow, time of repose in groove is not less than 30 minutes, fully to isolate ammoniacal liquor and tar, isolated tar flows automatically to hypomere circulation and washes in the naphthalene liquid bath, keeps circulation to wash tar content and naphthalene content in the naphthalene liquid with stable.
Flow automatically to epimere phlegma separator tank for the ease of the epimere phlegma, described gas cooler is the segmentation transverse tube type water cooler that is provided with every the liquid dish.
The temperature of described epimere phlegma is 35-50 ℃.
Described epimere phlegma separator tank isolating ammoniacal liquor with the gravity flow mode flow in the storage tank of tar ammonia separation circuit, as tar ammonia separator tank, mechanize tar ammonia clarifying tank, phlegma (underground) groove.
The temperature that naphthalene liquid is washed in described circulation is 18-25 ℃, and wherein tar content is 40-65wt%, and naphthalene content is 6-24wt% in the tar, moisture tar sprinkler discharge density 〉=2m
3/ hm
2
Low excessively in order to prevent that circulation from washing naphthalene liquid tar content, the naphthalene effect is washed in influence, also a spot of benefit of separating from the emulsion of tar ammonia separator tank, from mechanize tar ammonia clarifying tank or mechanize tar clarifying tank of moisture tar can be gone into the hypomere circulation and wash the naphthalene liquid bath.Also can wash the naphthalene liquid bath to the hypomere circulation and replenish a spot of tar washing oil, naphthalene content should be lower than 15wt% in the additional tar washing oil.
In order to prevent that the gas cooler epimere from being stopped up by the naphthalene in the coal gas, also can with epimere phlegma separator tank isolated tar spray through the top that pump is input to gas cooler.
The function of phlegma storage tank, gas liquor sealing groove and water-and-oil separator that epimere phlegma separator tank among the present invention is integrated.
Utilize the potential difference of epimere phlegma separator tank and tar ammonia separator tank, the isolated ammoniacal liquor of epimere phlegma from flowing into the tar ammonia separator tank, is reduced and carries the required power consumption of ammoniacal liquor.
Adopt band to be divided into different heat-eliminating mediums from top to bottom: hot water section, one section water coolant section of technology and two sections water coolant sections of technology every three sections transverse tube type gas coolers of liquid dish, made full use of the heat of thick coke-oven gas and the gas liquor of two sections generations on the water cooler has been discharged, make the required cooling water inflow of primary cooler hypomere the least possible, the required power consumption of water at low temperature is discharged and produced to corresponding the minimizing to atmospheric heat and steam;
Adopt tar conduct self-produced in the coal gas refrigerating work procedure to wash naphthalene liquid, need not use tar washing oil or 10# solar oil etc. outer for washing naphthalene liquid, to consume 2.5t/h tar washing oil, year saving tar washing oil 21900t;
Because the coal-tar middle oil naphthalene amount that contains of naphthalene liquid of washing that recycles is below 24wt%, wash naphthalene liquid naphthalene is had good dissolving ability, be mass transfer force, make in the primary cooler outlet coal gas dew-point temperature of naphthalene be lower than about 2 ℃ of gas temperature (naphthalene content～350mg/m in the coal gas when washing behind the naphthalene 20 ℃
3, be equivalent to 18 ℃ of dew-point temperatures), solved the obstruction of naphthalene at this in-process to follow-up gas purification equipment.
The present invention compared with prior art has following advantage: 1, utilize in the coke-oven gas condensation process phlegma that produces continuously to be used to wash naphthalene, do not use operation external wash the naphthalene absorption agent; 2, purify naphthalene content 350～100mg/m in the coal gas of back
3, the dew-point temperature of naphthalene is lower than gas temperature in the coal gas; Correspondingly, follow-up coke oven gas purification operation needn't be provided with takes off the naphthalene device, multistep Xian naphthalene is become a step wash naphthalene; 3, processing unit quantity is compared with existing known naphthalene washing process, and number of devices is minimum, so equipment takes up an area of also minimizing accordingly; 4, personnel's operation of need not to carry out the steam soaking primary cooler and switching primary cooler, simple to operate, 5, the process energy consumption that reduces, to cooperate 220 * 10
4Oven battery, the coal gas treatment capacity 13 * 10 in ton coke/year
4m
3/ h meter, annual economize on electricity 2.08 * 10
6KWh, water 1.6 * 10
5m
3, steam 1.1 * 10
4T, recovery heat 5.26 * 10
10Kcal amounts to 12091 tons of standard coals.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
As shown in Figure 1:
1 is that the heat-exchange equipment (as interchanger, heating facility etc.), 2 of other operation is for hot water tank; 3 is hot water pump; 4 is gas cooler; 5 wash the naphthalene liquid pump for epimere; 6 is epimere phlegma separator tank; 7 is the hypomere water sealed tank; 8 wash the naphthalene liquid bath for hypomere; 9 wash the naphthalene liquid pump for hypomere; 10 is the tar ammonia separator tank, 41 be in the gas cooler every the liquid dish.
A is the raw gas (coal gas and tar ammonia mixture, about 80 ℃) of coke oven; B is thick coke-oven gas; C is hot water effluent's (about 77 ℃); D is hot water water inlet (about 67 ℃); E is one section water coolant water outlet of technology (being sent to cooling tower ,～42 ℃); F is one section water coolant water inlet of technology (assisting the recirculated water that operation is sent here, 32～35 ℃ by public affairs); G is two sections water coolant water outlets of technology (being sent to refrigerator or cooling tower ,～23 ℃); H is two sections water coolant water inlets of technology (assisting the water at low temperature that operation is sent here ,～16 ℃ by public affairs); I is thick coke-oven gas (being sent to subsequent handling, 18～25 ℃); J is that epimere is washed naphthalene liquid (40～45 ℃); K is epimere phlegma (40～45 ℃); L is that hypomere is washed naphthalene liquid (18～25 ℃); M is hypomere phlegma (18～25 ℃); N washes naphthalene liquid (40～45 ℃) for replenishing; O is ammoniacal liquor (40～45 ℃); P is the circumscribed naphthalene liquid (18～25 ℃) of washing; Q is moisture tar (or claiming emulsion ,～80 ℃); R is tar ammonia mixture (～80 ℃)
Embodiment
Below in conjunction with embodiment the present invention is done detailed explanation.
As shown in Figure 1:
Embodiment 1: to cooperate 220 * 10
4Oven battery, the coal gas treatment capacity 13 * 10 in ton coke/year
4m
3/ h meter, normal gas flow is about 12 * 10
4m
3/ h,
1, the separation of raw gas:
The raw gas A that coke oven comes, the upwards climbing by pipeline is divided into thick coke-oven gas B and tar ammonia mixture R, and tar ammonia mixture R flows automatically to tar ammonia separator tank 10.
2, producing of epimere phlegma:
Thick coke-oven gas B enters gas cooler 4, contains water 81t/h among the thick coke-oven gas B; Tar 5.48t/h; Naphthalene 1.02t/h, gas cooler 4 are divided into hot water section 42, one section water coolant section 43 of technology and two sections water coolant sections 44 of technology, are located between one section water coolant section 43 of technology and two sections water coolant sections 44 of technology every liquid dish 41.Hot water section 42 hot water effluent C temperature is that 77 ℃, the temperature of hot water water inlet D are 67 ℃; One section water coolant water outlet of technology E of one section water coolant section 43 of technology is 42 ℃ (being sent to cooling tower), and one section water coolant water inlet of technology F is 32～35 ℃ (assisting the recirculated water that operation is sent here by public affairs); Two sections water coolant water outlets of technology G of two sections water coolant sections 44 of technology is 23 ℃ (being sent to refrigerator or cooling tower); Two sections water coolant water inlets of technology H is 16 ℃ (assisting the water at low temperature that operation is sent here by public affairs).
Be provided with every liquid dish 41 in the described gas cooler 4, be located between one section water coolant section 43 of technology and two sections water coolant sections 44 of technology every liquid dish 41, every liquid dish 41 the coal gas runner in the gas cooler 4 is divided into two sections, draws at the epimere phlegma K that produces in the coal gas condensation process every liquid Pan41Chu; In order to prevent naphthalene condensation crystalline growth and then the obstruction primary cooler outside primary cooler epimere heat exchange tube wall in the coal gas, the epimere cooling temperature of control coal gas is between 40 ℃-45 ℃, the coal gas naphthalene that condensation is come out in process of cooling is dissolved in the contained tar of epimere phlegma K, the temperature of epimere phlegma K is 40～45 ℃, wherein contains ammoniacal liquor 73t/h; Tar 4t/h, naphthalene 0.4t/h;
3, replenish and to wash producing of naphthalene liquid:
The epimere phlegma K that draws time of repose in epimere condensation liquid bath 6 is 45 minutes, wherein ammoniacal liquor and tar are carried out standing separation, (40～45 ℃ of the ammoniacal liquor O that separates, 73t/h) continuously from flowing into tar ammonia separator tank 10, the tar of separating promptly replenishes and washes (40～45 ℃ of naphthalene liquid N, tar is 4t/h, contain naphthalene and be about 10%,) wash naphthalene liquid bath 8 from flowing into hypomere continuously, owing to replenish and to wash naphthalene liquid N to contain naphthalene low, can guarantee the naphthalene amount that contains that hypomere washes naphthalene liquid L effectively about 24wt%, and then guarantee that the hypomere that recycles washes the naphthalene liquid L naphthalene that outer condensation is come out to the heat exchange tube wall of gas cooler 4 hypomeres and have good dissolving ability.
4, naphthalene is washed in circulation:
With hypomere wash hypomere in the naphthalene liquid bath 8 wash naphthalene liquid L (temperature is 20 ℃, tar content＞40wt%, naphthalene content is about 20wt% in the tar, internal circulating load is～400m
3/ h), to wash naphthalene liquid pump 9 with hypomere and extract out, the hypomere and the coal gas that are transported to gas cooler 4 (contain ammoniacal liquor 5.91t/h; Tar 1t/h) carries out the following current contact, hypomere phlegma M flows automatically to hypomere water sealed tank 7 from the lower part outlet of gas cooler 4, overflow is gone into hypomere and is washed naphthalene liquid bath 8 again, form circulation and wash naphthalene, wash the level stability of naphthalene liquid bath 8 for keeping hypomere, the outlet stool of washing naphthalene liquid pump 9 by hypomere is circumscribed with unnecessary moisture tar, forms the circumscribed naphthalene liquid P that washes, and sends in the tar ammonia separator tank 10.The circumscribed flow of washing naphthalene liquid is washed gas liquor sum (the ammoniacal liquor 5.91t/h that naphthalene liquid N and gas cooler 4 hypomeres obtain for replenishing; Tar 5.25t/h).
Owing to replenish and to wash the coal-tar middle oil 4t/h of being about of naphthalene liquid N, account for hypomere wash naphthalene liquid L total flux～1%, therefore, do not need special cooling apparatus that it is cooled off, simultaneously, the contained tar of epimere phlegma K all adds to hypomere and washes in the naphthalene liquid, purifies naphthalene content 350mg/m in the coal gas of back
3, the dew-point temperature of naphthalene is lower than the coal gas apparent temperature below 2 ℃ in the coal gas, and follow-up gas purification operation does not need to be provided with whole cold wash naphthalene tower again.Gas outlet temperature is stabilized in 20～22 ℃; Gas cooler 4 resistances are stabilized in below the 1000Pa; Do not use steam soaking gas cooler 4, need not to switch gas cooler 4 yet.
Embodiment 2:
For prevent circulation wash naphthalene liquid tar content cross low or naphthalene content too high, the naphthalene effect is washed in influence, also 10 emulsion Q in the tar ammonia separator tank can be mended into the hypomere circulation in the mode of gravity flow and wash naphthalene liquid bath 8.
Embodiment 3:
Purify in the coal gas of back naphthalene content at 100～350mg/m in order further to reduce
3In the scope, wash a spot of moisture tar of naphthalene liquid bath 8 continuous supplementation or the tar washing oil is washed the coal-tar middle oil naphthalene content of naphthalene liquid with further reduction circulation to hypomere circulation.The moisture tar that the tar that replenishes is separated from tar ammonia separator tank, mechanize tar ammonia clarifying tank or mechanize tar clarifying tank; The tar washing oil that replenishes is a kind of product of tar deep processing.Look different coal gas naphthalene content decontamination index requirement,, come Control Circulation to wash the coal-tar middle oil naphthalene content of naphthalene liquid in 6～24wt% scope by controlling the magnitude of recruitment of moisture tar or tar washing oil.
Embodiment 4:
When the obstruction of separating out the crystalline naphthalene outside the gas cooler 4 epimere heat exchange tube walls during gas cooler 4, also can utilize epimere to wash the top that tar that naphthalene liquid pump 5 separated epimere phlegma K is guided to gas cooler 4, spray, wash naphthalene.
Claims (8)
1, coal gas naphthalene washing process in the coke oven gas purification unit primary-cooling working procedure, use moisture tar to contact at the gas cooler hypomere with coal gas following current in gas cooler, wash naphthalene, the mixture of the hypomere phlegma that the described moisture tar epimere phlegma that to be coal gas obtain at the gas cooler epimere obtains when the gas cooler hypomere cools off through the resulting tar light oil of separation system and coal gas, it is characterized in that: described separation system comprises near the epimere phlegma separator tank that is positioned at the gas cooler, the epimere phlegma of gas cooler flows into epimere phlegma separator tank in the mode of gravity flow, time of repose in groove is not less than 30 minutes, fully to isolate ammoniacal liquor and tar, isolated tar flows automatically to hypomere circulation and washes in the naphthalene liquid bath, keeps circulation to wash tar content and naphthalene content in the naphthalene liquid with stable.
2, the coal gas naphthalene washing process in the coke oven gas purification according to claim 1 unit primary-cooling working procedure, it is characterized in that: described gas cooler is the segmentation transverse tube type water cooler that is provided with every the liquid dish.
3, the coal gas naphthalene washing process in the coke oven gas purification according to claim 1 unit primary-cooling working procedure, it is characterized in that: the temperature of described epimere phlegma is 35-50 ℃.
4, the coal gas naphthalene washing process in the coke oven gas purification according to claim 1 unit primary-cooling working procedure, it is characterized in that: described epimere phlegma separator tank isolating ammoniacal liquor with the gravity flow mode flow in the storage tank of tar ammonia separation circuit, as tar ammonia separator tank, mechanize tar ammonia clarifying tank, phlegma (underground) groove.
5, according to the coal gas naphthalene washing process in the described coke oven gas purification of the claim 1 unit primary-cooling working procedure, it is characterized in that: the temperature that naphthalene liquid is washed in described circulation is 18-25 ℃, tar content 40-65wt% wherein, naphthalene content 6-24wt% in the tar, moisture tar sprinkler discharge density 〉=2m
3/ hm
2
6, the coal gas naphthalene washing process in the coke oven gas purification according to claim 1 unit primary-cooling working procedure is characterized in that: wash the moisture tar that a small amount of moisture tar that the naphthalene liquid bath replenishes is separated from tar ammonia separator tank, mechanize tar ammonia clarifying tank or mechanize tar clarifying tank to the hypomere circulation; The tar washing oil that replenishes, its naphthalene content should be lower than 15wt%.
7, the coal gas naphthalene washing process in the coke oven gas purification according to claim 1 unit primary-cooling working procedure is characterized in that: the emulsion in the tar ammonia separator tank is mended into the hypomere circulation in the mode of gravity flow washed the naphthalene liquid bath.
8, the coal gas naphthalene washing process in the coke oven gas purification according to claim 1 unit primary-cooling working procedure is characterized in that: with epimere phlegma separator tank isolated tar spray through the top that pump is input to water cooler.
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| CN 200910144286 CN101619243B (en) | 2009-07-29 | 2009-07-29 | Gas naphthalene washing process in primary-cooling working procedure of coke oven gas purification unit |
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| CN102796542A (en) * | 2012-08-15 | 2012-11-28 | 四川达兴能源股份有限公司 | Primary cooler cleaning method and cleaning system |
| 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 |
| CN104479915A (en) * | 2014-11-25 | 2015-04-01 | 攀钢集团攀枝花钢钒有限公司 | Naphthalene washing solution and production method thereof |
| CN104629816A (en) * | 2015-01-30 | 2015-05-20 | 济南冶金化工设备有限公司 | Self-made cold type coke oven crude gas primary cooling device |
| CN104726139A (en) * | 2015-03-27 | 2015-06-24 | 山东钢铁股份有限公司 | Coke oven gas final cooling system and method |
| CN105779028A (en) * | 2016-04-07 | 2016-07-20 | 青岛科大隆腾科技发展有限公司 | Raw coke oven gas heat and chemical product simultaneous recovery method based on washing and rectifying |
| CN107106968A (en) * | 2014-10-28 | 2017-08-29 | 蒂森克虏伯工业解决方案股份公司 | The reduction of Naphthalene in Coke Oven Gas |
| CN108148636A (en) * | 2018-02-05 | 2018-06-12 | 陕西冶金设计研究院有限公司 | A kind of raw coke oven gas pneumatic trough |
| CN110484309A (en) * | 2019-08-14 | 2019-11-22 | 昆山市三维换热器有限公司 | Combined type coal gas primary cooler and its system |
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Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1014718B (en) * | 1988-06-04 | 1991-11-13 | 河南省安阳钢铁公司 | Indirect two-stage primary cooling technology of coke-oven gas |
| CN1016182B (en) * | 1988-06-04 | 1992-04-08 | 河南省安阳钢铁公司 | Technology for purifying naphthalene from coke-oven gas |
| CN1036662C (en) * | 1993-12-14 | 1997-12-10 | 唐山钢铁(集团)公司 | Process for separating naphthalene from coke oven gas |
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2009
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| CN102796542A (en) * | 2012-08-15 | 2012-11-28 | 四川达兴能源股份有限公司 | Primary cooler cleaning method and cleaning system |
| 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 |
| CN107106968A (en) * | 2014-10-28 | 2017-08-29 | 蒂森克虏伯工业解决方案股份公司 | The reduction of Naphthalene in Coke Oven Gas |
| CN104479915A (en) * | 2014-11-25 | 2015-04-01 | 攀钢集团攀枝花钢钒有限公司 | Naphthalene washing solution and production method thereof |
| CN104629816A (en) * | 2015-01-30 | 2015-05-20 | 济南冶金化工设备有限公司 | Self-made cold type coke oven crude gas primary cooling device |
| CN104629816B (en) * | 2015-01-30 | 2016-09-28 | 济南冶金化工设备有限公司 | From the preliminary chiller of refrigeration mode coal oven dithio-gas |
| CN104726139A (en) * | 2015-03-27 | 2015-06-24 | 山东钢铁股份有限公司 | Coke oven gas final cooling system and method |
| CN105779028A (en) * | 2016-04-07 | 2016-07-20 | 青岛科大隆腾科技发展有限公司 | Raw coke oven gas heat and chemical product simultaneous recovery method based on washing and rectifying |
| CN105779028B (en) * | 2016-04-07 | 2019-04-19 | 青岛科大隆腾科技发展有限公司 | Raw coke oven gas heat and change based on washing rectifying produce the method recycled simultaneously |
| CN108148636A (en) * | 2018-02-05 | 2018-06-12 | 陕西冶金设计研究院有限公司 | A kind of raw coke oven gas pneumatic trough |
| CN110484309A (en) * | 2019-08-14 | 2019-11-22 | 昆山市三维换热器有限公司 | Combined type coal gas primary cooler and its system |
| CN114317039A (en) * | 2022-01-05 | 2022-04-12 | 新疆八一钢铁股份有限公司 | Condensate oil supplementing method for coking horizontal pipe primary cooler |
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