CN102247743B - Dehydration method for desorption gas used in desulphurization of flue gas - Google Patents
Dehydration method for desorption gas used in desulphurization of flue gas Download PDFInfo
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Abstract
The invention provides a dehydration method for desorption gas used in desulphurization of flue gas. The method comprises the following steps: carrying out primary condensation and secondary condensation on desorption gas which has been desorbed from a desorption system so as to obtain first condensate liquid, second condensate liquid and desorption gas containing vapor, sulfur dioxide gas and a desulfurizer; delivering the resultant desorption gas into a gas-liquid separation device for gas-liquid separation so as to generate liquid and acidic gas containing sulfur dioxide; delivering the resultant second condensate liquid and liquid generated in gas-liquid separation into a suspension filter for filtration so as to remove impurities in the liquid and obtain a desulphurization solution containing saturated sulfurous acid and a small amount of desulfurizer; supplying the desorption system with the desulphurization solution. The method provided in the invention can effectively maintain water balance of the desorption system, utmostly reduces loss of sulfur dioxide, and further reduces energy consumption and the like of the desorption system.
Description
Technical field
The present invention relates to a kind of dehydration method for desorption gas used in desulphurization of flue gas, relate to particularly a kind of by the method for dewatering desorption gas for flue gas desulfurization.
Background technology
Sulfur dioxide serious environment pollution, need to carry out sulfur dioxide absorption with the desulfuration solution that contains desulfurizing agent, then need the desulfuration solution to being rich in sulfur dioxide to carry out desorb, so that desorb the desulfuration solution of sulfur dioxide reuse, in desorb, give off the sinter fume that mainly contains steam and sulfur dioxide and a part of desulfurizing agent.Traditionally, in desorption gas, contain a large amount of steam, make the desorption gas giving off through condensation, obtain on the one hand the desorption gas that mainly contains sulfur dioxide, be again provided in desorption apparatus through the condensate liquid that contains large water gaging of condensation on the other hand.In addition, in sinter fume, also contain a large amount of dust, SO
3, SO
2, Cl
-, NO
xdeng highly acid gas componant and oxygen composition etc.Specifically, sintering contains about 10% the wet moisture content that contains.
But, in the desulfuration solution of separating sucking-off sulfur dioxide, contain strong acid radical ion, when the desulfuration solution that has removed sulfur dioxide is in the solution of trapping sulfur dioxide is supplied to absorption tower again, need to remove strong acid radical ion.Current employing ion exchange resin removes strong acid radical ion, and the first washing desulphurization liquid water of resin, will directly return in desulfuration solution, and the desulfuration solution of every processing 1 volume will be introduced the industrial soft water of about 0.5 volume.Then, the solution of having removed strong acid radical ion is supplied to absorption tower and catches sulfur dioxide, and the solution of having caught sulfur dioxide is supplied to from absorption tower and desorption system, carries out desulfurization.Cyclic process is known thus, if the condensate liquid that contains water obtaining after desorption gas condensation is provided in desorption apparatus as desulfuration solution, there is the problem of solution dilution in desulfuration solution after long-term operation, thereby reduce the valid density of desulfuration solution, condensate liquid directly outer row, by sulfurous acid a large amount of loss, brings secondary environmental pollution simultaneously.
Publication number be CN200920078566.0 Patent Application Publication a kind of multifunctional absorption tower for flue gas desulfurization, it is separated to form pretreating zone, uptake zone and middle flue by division board by absorption tower tower body.Wherein, pretreating zone is for washing and wash rear demist to flue gas, and uptake zone is used for absorbing flue gas SO
2with the foam removal of desulfurization fume, middle flue is for guiding the Rational flow of flue gas from pretreating zone to uptake zone.In addition, the Patent Application Publication that publication number is CN200920078791.4 a kind of multifunctional absorption tower for flue gas desulfurization.In above-mentioned patent application, the temperature that flue gas enters absorber portion after washing is at 40～60 DEG C, and after desulfuration solution absorbs, discharged gas fume temperature is at 50～70 DEG C.Therefore, in flue gas washing absorption process, can cause the dilution problem of desulfuration solution.
Publication number be CN200920350778.X Patent Application Publication one make desorption system, it mainly carries out twice regeneration by desulfuration solution, (the condensate liquid of regeneration high-temp gas returns to desorption system, desorption system), adopt the gas that contains sulfur dioxide after rich solution desorb to heat, sulfur removing pregnant solution desorb energy consumption have reduce, but in cyclic process, still can there is dilution problem in desulfuration solution.In addition, existing amine process desulfur technology is to carry out one section of absorption and one section of desorb, the condensate liquid of desorption gas directly returns to desorption system, condensate liquid rises to desorption temperature from 50 DEG C of left and right need a lot of heats, therefore, virtually having reduced the desorb degree of rich solution, increase energy of desorption consumption.
In above-mentioned patent application, in flue gas washing process, desulphurization system, because flue gas is containing demist and the rear flue gas efflux gas of washing moist, washing section upper strata, so be difficult to keep water balance, can cause solution to become dilution.Meanwhile, the condensed water in desorb high-temperature gas returns to desorption system, does not effectively reduce the water yield in desorption gas, thereby has increased desulfurization energy consumption.
In order to overcome, the water yield in existing flue gas desulfurization solution increases, desulfurization desorb condensate liquid returns to desorption system and has the shortcomings such as desorb energy consumption height, need a kind of gas-condensate liquid to desorption system to process separately, thereby can the resolution system water yield increase and the problem such as energy consumption is large.
Summary of the invention
For the desulfurizing agent in not loss desulfuration solution and the further sulfur dioxide that reclaims, and in order to reduce energy consumption, the invention provides a kind of dehydration method for desorption gas used in desulphurization of flue gas, said method comprising the steps of: will carry out one-level condensation and B-grade condensation from the desorption gas of desorption system solution sucking-off, thereby produce the first condensate liquid, the second condensate liquid and contain steam, the desorption gas of sulfur dioxide gas and desulfurizing agent, wherein, described the first condensate liquid contains water with a small amount of sulfurous acid and by outer row, described the second condensate liquid is saturated sulfurous acid solution and contains a small amount of desulfurizing agent and impurity, the desorption gas of generation is supplied to and in gas-liquid separation device, carries out gas-liquid separation, thus the sour gas that produces liquid and contain sulfur dioxide, the liquid supply of described the second condensate liquid and gas-liquid separation generation is filtered in suspended filter, to remove the impurity wherein containing, thereby obtain the desulfuration solution containing saturated sulfurous acid and a small amount of desulfurizing agent, described desulfuration solution is supplied in described desorption system.
Described method can also comprise the following steps: before in described desulfuration solution is supplied to described desorption system, make described desulfuration solution carry out heat exchange in heat-exchange system Yu from a part of desorption gas of described desorption system solution sucking-off, then the desulfuration solution after heat exchange is supplied in described desorption system, and makes the described a part of desorption gas after heat exchange carry out again one-level condensation.
Described method can also comprise the following steps: make another part desorption gas from the sucking-off of described desorption system solution another heat-exchange system with heat exchange after rich solution carry out heat exchange, then the rich solution after further heat exchange is supplied in described desorption system, and make the described another part desorption gas after heat exchange carry out again one-level condensation, the rich solution after wherein said heat exchange be from the absorption after absorption tower and high-temperature barren liquor heat exchange from desorption system the rich solution of sulfur dioxide.
Described suspended filter can be sulphur filter.
Described desulfurizing agent can be By Amine Solutions or ionic liquid.
Brief description of the drawings
Fig. 1 shows the flow chart of dehydration method for desorption gas used in desulphurization of flue gas according to an embodiment of the invention;
Fig. 2 shows the flow chart of dehydration method for desorption gas used in desulphurization of flue gas according to another embodiment of the present invention;
Fig. 3 shows according to the flow chart of a kind of dehydration method for desorption gas used in desulphurization of flue gas of further embodiment of this invention.
Detailed description of the invention
Below in conjunction with accompanying drawing, embodiments of the invention are elaborated.
Dehydration method for desorption gas used in desulphurization of flue gas according to the present invention comprises the following steps: will carry out one-level condensation and B-grade condensation from the desorption gas of desorption system solution sucking-off, thereby the desorption gas that produces the first condensate liquid, the second condensate liquid and contain steam, sulfur dioxide gas and desulfurizing agent, wherein, described the first condensate liquid contains water, a small amount of sulfurous acid and by outer row, described the second condensate liquid is saturated sulfurous acid solution and contains a small amount of desulfurizing agent and impurity; The desorption gas of generation is supplied to and in gas-liquid separation device, carries out gas-liquid separation, thus the sour gas that produces liquid and contain sulfur dioxide; The liquid supply of described the second condensate liquid and gas-liquid separation generation is filtered in suspended filter, to remove the impurity wherein containing, thereby obtain the desulfuration solution containing saturated sulfurous acid and a small amount of desulfurizing agent; Described desulfuration solution is supplied in described desorption system.It should be noted that above-mentioned steps can be carried out simultaneously or suitably sequentially carry out with other, instead of being only confined to the order providing above.
The object of multi-stage condensing is that the steam-laden sulfur dioxide desorption gas of high temperature is lowered the temperature, after moisture content cooling in desorption gas, major part transfers liquid state to and condensation, the desulfuration solution of carrying secretly in desorption gas and impurity thereof are because of cooling condensation, sulfur dioxide gas in desorption gas is partially dissolved in condensed water, form in condensed fluid and contain desulfuration solution, foreign ion and sulfurous acid, simultaneously to the condensation under different temperatures of the steam-laden sulfur dioxide desorption gas of high temperature, in condensate liquid, sulfurous acid concentration difference is carried out the condensed water containing a small amount of sulfurous acid outer row and is not returned to desorption system.Suspension in condensate liquid, as sulphur, filters by filter, has overcome condensed fluid in condenser and the ducted obstruction that is connected thereof; Gas-liquid separation device further carries out gas-liquid separation to the acid sulfur dioxide gas containing partial condensation liquid, obtains the sulfur dioxide gas of higher degree, is the solution containing saturated sulfurous acid through the separating liquid of gas-liquid separation.
To carry out gas-liquid separation and be a large amount of steam in order making to contain in condensate liquid, desorption gas and a small amount of desulfurizing agent and to become liquid and separate with acid sulfur dioxide gas, but inevitably can contain a large amount of sulfurous acid.Adopt industrial colling or cryogenic liquid and desorption gas in condenser, to carry out indirect heat exchange, general condenser is more than or equal to secondary; Connect successively, be connected with gas-liquid separator through afterbody condenser.Be 80～95 DEG C through the condensed acid gas temperature of one-level, condensate temperature is 80～95 DEG C; Acid gas temperature after B-grade condensation is 55～65 DEG C, and condensate temperature is 50～65 DEG C; High-purity sulfur dioxide gas temperature through gas-liquid separator separates is 45～55 DEG C, and gas-liquid separator separates liquid temp is 40～55 DEG C
In one embodiment, method of the present invention can also comprise the following steps: before in described desulfuration solution is supplied to described desorption system, make described desulfuration solution carry out heat exchange in heat-exchange system Yu from a part of desorption gas of described desorption system solution sucking-off, then the desulfuration solution after heat exchange is supplied in described desorption system, and makes the described a part of desorption gas after heat exchange carry out again one-level condensation.
Method of the present invention can also comprise the following steps: make another part desorption gas from the sucking-off of described desorption system solution another heat-exchange system with heat exchange after rich solution carry out heat exchange, then the rich solution after further heat exchange is supplied in described desorption system, and make the described another part desorption gas after heat exchange carry out again one-level condensation, the rich solution after wherein said heat exchange be from the absorption after absorption tower and high-temperature barren liquor heat exchange from desorption system the rich solution of sulfur dioxide.The rich solution temperature that has absorbed sulfur dioxide on absorption tower is 45～55 DEG C, the high-temperature barren liquor temperature of discharging from desorption system bottom is 100～115 DEG C, absorb the rich solution of sulfur dioxide with from the high-temperature barren liquor heat exchange of desorption system bottom discharge, rich solution temperature is elevated to 75～85 DEG C, rich solution (75～85 DEG C) after heat exchange further carries out heat exchange with a part of desorption under high temperature gas (105～115 DEG C) again, and rich solution temperature is elevated to 85～95 DEG C.
Described suspended filter can be sulphur filter.
Described desulfurizing agent can be By Amine Solutions or ionic liquid.
Dehydration method for desorption gas used in desulphurization of flue gas according to the embodiment of the present invention is described with reference to the accompanying drawings in more detail.
Embodiment 1
With reference to Fig. 1, in the present embodiment, will carry out condensed in two stages from the desorption under high temperature gas of desorption system solution sucking-off.The first condensate liquid that one-level condensation is produced is outer row directly, and the first condensate liquid mainly contains water and a small amount of sulfurous acid.Then the desorption gas that mainly contains desulfurizing agent, water and impurity one-level condensation being produced carries out B-grade condensation, thereby produce the second condensate liquid and desorption gas, the second condensate liquid is saturated sulfurous acid solution and contains a small amount of desulfurizing agent and impurity (such as sulphur etc.).
Subsequently, desorption gas is supplied to and in gas-liquid separation device, carries out gas-liquid separation, thereby produce sour gas and the liquid containing sulfur dioxide.In the liquid that gas-liquid separation produces, mainly contain water, and contain a large amount of sulfur dioxide and impurity.
Then, the sour gas containing sulfur dioxide producing is supplied to acid making system or is stored, and the second condensate liquid producing after the liquid producing after gas-liquid separation and B-grade condensation is supplied to suspended filter filters, thereby removal impurity, obtains the desulfuration solution containing saturated sulfurous acid and a small amount of desulfurizing agent thus.Then the sweetening liq after filtering is provided in desorption system.
In addition, outer row's cooling lean solution can be supplied to wash-water system or for other purposes.
Embodiment 2
With reference to Fig. 2, in the present embodiment, except comprising the step in embodiment 1, the method of the present embodiment also comprises step below: before in the sweetening liq after filtering is provided to desorption system, make desulfuration solution carry out heat exchange in the first heat-exchange system Yu from a part of desorption gas of desorption system solution sucking-off, then the desulfuration solution after heat exchange is supplied in desorption system, and makes the part desorption gas after heat exchange carry out again the steps such as one-level condensation.
Embodiment 3
With reference to Fig. 3, in the present embodiment, except comprising the step in embodiment 2, the method of the present embodiment also comprises step below: make another part desorption gas from the sucking-off of desorption system solution the second heat-exchange system with heat exchange after rich solution carry out heat exchange, then the rich solution after heat exchange is supplied in desorption system, and makes this another part desorption gas after heat exchange carry out again the steps such as one-level condensation.In the present embodiment, the rich solution after heat exchange be from the absorption after absorption tower and high-temperature barren liquor heat exchange from desorption system the rich solution of sulfur dioxide.Specifically, the rich solution temperature that has absorbed sulfur dioxide on absorption tower is 45～55 DEG C, the high-temperature barren liquor temperature of discharging from desorption system bottom is 100～115 DEG C, absorb the rich solution of sulfur dioxide with from the high-temperature barren liquor heat exchange of desorption system bottom discharge, rich solution temperature is elevated to 75～85 DEG C, rich solution (75～85 DEG C) after heat exchange further carries out heat exchange with a part of desorption under high temperature gas (105～115 DEG C) again, and rich solution temperature is elevated to 85～95 DEG C.
It may be noted that the processing step in processing step or the embodiment in above-mentioned different embodiment can exchange or combine.In the above-described embodiments, the desulfurizing agent of use can be By Amine Solutions or ionic liquid.It may be noted that in addition in the liquid after condensate liquid and gas-liquid separation and also can inevitably contain other highly acid gas componant, such as Cl, NO
x, SO
3, SO
2deng.
In the present invention, high-temperature acidic gas and a large amount of steam carry out condensation in first order condensation, are essentially the aqueous solution in condensate liquid, there is no desulfuration solution solution, and containing few a small amount of inorganic anion.By the condensation of desorption under high temperature gas classification and classification processing, reduce backflow and the treating capacity of condensate liquid.
Second level condensed fluid is collected separately, and mix as desulfuration solution with the liquid of gas-liquid separator separates, then the suspension that adopts suspension filter to filter wherein (is mainly sulphur, other impurity), condensed fluid after filtering and high temperature are resolved gas and are carried out returning to resolution system after heat exchange, thereby filter suspension, and reduce the obstruction of pipeline and pump, further the condensate liquid of classification is processed simultaneously, reduce the condensate liquid scale of construction of retrieval system, carry out in addition heat exchange, reduce the energy consumption of condensed fluid in the needs heating of resolution system, simultaneously also having reduced high temperature resolution gas needs the energy consumption of the cryogenic substance of condensation.
The first heat-exchange system adopts the rich solution of 75～85 DEG C after rich or poor liquid heat exchange, further with the high temperature resolution gas heat exchange of 100～115 DEG C, rich solution is elevated to 85～95 DEG C, high temperature resolution gas is reduced to 90～100 DEG C, this process only has a small amount of water condensation out, then enter condenser, general condenser is more than or equal to secondary; Connect successively, be connected with gas-liquid separator through afterbody condenser., for condensed in two stages device, be for example 80～95 DEG C through the condensed acid gas temperature of one-level, condensate temperature is 80～95 DEG C; Acid gas temperature after B-grade condensation is 55～65 DEG C, and condensate temperature is 50～65 DEG C; High-purity sulfur dioxide gas temperature through gas-liquid separator separates is 45～55 DEG C, and the parting liquid temperature of gas-liquid separator is 40～55 DEG C.B-grade condensation liquid and gas-liquid separation liquid, after suspended filter filters, more further carry out heat exchange with high temperature resolution gas, and the temperature of resolution gas is 85～100 DEG C, and the temperature of condensed fluid after heat exchange is 75～85 DEG C.
In an embodiment according to the present invention, due to process B-grade condensation, what one-level condensation produced mainly contains the condensate liquid of water by direct outer row, the condensate liquid that B-grade condensation produces mainly contains desulfurizing agent and a part of water, saturated sulfurous acid and impurity, the moisture content containing in desorption under high temperature gas after B-grade condensation is present in desorption gas with the form of steam, and impurity is removed after through filtration.Like this, mainly contain liquid that the B-grade condensation liquid of desulfurizing agent, water, saturated sulfurous acid and impurity and gas-liquid separation produce being supplied in desorption system as desulfuration solution after filtering, or before being supplied to desorption system, be heated to 85 DEG C～95 DEG C, then being supplied in desorption system.Because the condensate liquid that desorption under high temperature gas produces after one-level condensation is directly arranged outward, so can overcome because condensate liquid all returns to desorption system increases the desulphurization system water yield, and the deficiency that causes desulfuration solution to dilute, also reduced the deficiency of the further condensations of first order condensation needs, reduced the energy consumption of desorption system simultaneously.
In addition, the desorption under high temperature gas of desorption system solution sucking-off can carry out indirect heat exchange with condensate liquid, also can with desorption system in the sulfur removing pregnant solution that heats of needs carry out heat exchange, thereby for sulfur removing pregnant solution carries out preheating, thereby needed other indirect energy consumption of rich solution preheating.In addition, directly in outer row's lean solution, contain a large amount of water, thereby can be further used for washing process, thereby reduced the consumption of industry water.Simultaneously, also can make the condensate liquid and the desorption gas that return to desulfurization desorption system carry out heat exchange, realize the inner utilization of heat exchange between high-temperature gas, cryogenic liquid, greatly reduce desulfurization regeneration energy consumption, simultaneously by only containing the B-grade condensation liquid of saturated sulfurous acid and liquid that gas-liquid parting liquid obtains (, they the two be mainly saturated sulfurous acid solution, wherein, in solution containing a small amount of suspension such as desulfurizing agent, sulphur) carry out desorb.Therefore, this process modification has been saved system energy consumption greatly.
Therefore, the invention has the advantages that, can carry out multi-stage condensing to desorption under high temperature gas, utilize sulfurous acid in every grade of condensate liquid, the different feature of desulfurizing agent content, every section of condensate liquid is carried out to segmentation to be collected separately, can reduce secondary pollution that sulfurous acid in the condensate liquid of mixed collection brings because of outer row and the loss of sulfur dioxide resource, meanwhile, also overcome the deficiency that increases desorb energy consumption and systematic water balance increase containing the sulfurous acid condensate liquid of low content returns to desorption system.Specifically, the first condensate liquid mainly contains water, and the desorption gas that mainly contains desulfurizing agent, water and impurity that one-level condensation produces carries out B-grade condensation, thereby produces the second condensate liquid and the desorption gas that contain a small amount of desulfurizing agent, water, sulfurous acid and impurity.Isolated condensate liquid or carry out part recycling through the liquid of gas-liquid separation, the condensate liquid of recycling or liquid, desorption under high temperature gas and need the rich solution of preheating on heat, to carry out step heat exchange, thus utilize fully the conversion of system thermal inside.In addition, the balance that this has kept the desulphurization system water yield effectively, has also further reduced the problems such as the energy consumption of desorption system.
Claims (5)
1. a dehydration method for desorption gas used in desulphurization of flue gas, is characterized in that, said method comprising the steps of:
To carry out one-level condensation and B-grade condensation from the desorption gas of desorption system solution sucking-off, thereby the desorption gas that produces the first condensate liquid, the second condensate liquid and contain steam, sulfur dioxide gas and desulfurizing agent, wherein, described the first condensate liquid contains water with a small amount of sulfurous acid and by outer row, described the second condensate liquid is saturated sulfurous acid solution and contains a small amount of desulfurizing agent and impurity;
The desorption gas of generation is supplied to and in gas-liquid separation device, carries out gas-liquid separation, thus the sour gas that produces liquid and contain sulfur dioxide;
The liquid supply of described the second condensate liquid and gas-liquid separation generation is filtered in suspended filter, to remove the impurity wherein containing, thereby obtain the desulfuration solution containing saturated sulfurous acid and a small amount of desulfurizing agent;
Described desulfuration solution is supplied in described desorption system.
2. method according to claim 1, is characterized in that, described method is further comprising the steps of:
Before in described desulfuration solution is supplied to described desorption system, make described desulfuration solution carry out heat exchange in heat-exchange system Yu from a part of desorption gas of described desorption system solution sucking-off, then the desulfuration solution after heat exchange is supplied in described desorption system, and makes the described a part of desorption gas after heat exchange carry out again one-level condensation.
3. method according to claim 2, is characterized in that, described method is further comprising the steps of:
Make another part desorption gas from the sucking-off of described desorption system solution another heat-exchange system with heat exchange after rich solution carry out heat exchange, then the rich solution after further heat exchange is supplied in described desorption system, and make the described another part desorption gas after heat exchange carry out again one-level condensation, the rich solution after wherein said heat exchange be from the absorption after absorption tower and high-temperature barren liquor heat exchange from desorption system the rich solution of sulfur dioxide.
4. method according to claim 1, is characterized in that, described suspended filter is sulphur filter.
5. method according to claim 1, is characterized in that, described desulfurizing agent is By Amine Solutions or ionic liquid.
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| CN103801173B (en) * | 2012-11-08 | 2016-08-31 | 中国石油化工股份有限公司 | The processing method of NOx waste gas in a kind of copper zinc catalyst preparation technology |
| CN103708427A (en) * | 2013-12-19 | 2014-04-09 | 中国平煤神马集团开封兴化精细化工有限公司 | Method for recycling sulfur dioxide tail gas in saccharin production process |
| CN108079751B (en) * | 2018-01-16 | 2023-07-28 | 鲍满腔 | High-efficiency energy-saving flue gas dust removal desulfurization system |
| CN108774751A (en) * | 2018-08-09 | 2018-11-09 | 宜宾丝丽雅股份有限公司 | Viscose deaeration system |
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|---|---|---|---|---|
| CN1214953A (en) * | 1997-10-21 | 1999-04-28 | 三菱重工业株式会社 | Waste gas desulfurization device |
| CN101698806A (en) * | 2009-05-25 | 2010-04-28 | 莱芜钢铁股份有限公司 | Gravity-flow type efflux technology of condensate of coal gas primary cooler |
| CN101708414A (en) * | 2009-12-31 | 2010-05-19 | 攀钢集团研究院有限公司 | System and method for desulphurizing waste gas by cyclic absorption and application thereof |
| CN101721894A (en) * | 2008-10-17 | 2010-06-09 | 山东省冶金设计院有限责任公司 | De-sulfur method with reproducible desulfurizer for preparing sulfuric acid as final product |
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2011
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1214953A (en) * | 1997-10-21 | 1999-04-28 | 三菱重工业株式会社 | Waste gas desulfurization device |
| CN101721894A (en) * | 2008-10-17 | 2010-06-09 | 山东省冶金设计院有限责任公司 | De-sulfur method with reproducible desulfurizer for preparing sulfuric acid as final product |
| CN101698806A (en) * | 2009-05-25 | 2010-04-28 | 莱芜钢铁股份有限公司 | Gravity-flow type efflux technology of condensate of coal gas primary cooler |
| CN101708414A (en) * | 2009-12-31 | 2010-05-19 | 攀钢集团研究院有限公司 | System and method for desulphurizing waste gas by cyclic absorption and application thereof |
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