CN1075102A - Gas-liquid contact system - Google Patents

Gas-liquid contact system Download PDF

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Publication number
CN1075102A
CN1075102A CN93101505A CN93101505A CN1075102A CN 1075102 A CN1075102 A CN 1075102A CN 93101505 A CN93101505 A CN 93101505A CN 93101505 A CN93101505 A CN 93101505A CN 1075102 A CN1075102 A CN 1075102A
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gas
tower
liquid
area
contanct equipment
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CN93101505A
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CN1070729C (en
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阿南达P·巴特
丹尼斯W·约翰逊
罗伯特B·迈尔斯
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Babcock and Wilcox Co
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Babcock and Wilcox Co
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/78—Liquid phase processes with gas-liquid contact
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D47/00—Separating dispersed particles from gases, air or vapours by liquid as separating agent
    • B01D47/06—Spray cleaning
    • B01D47/063—Spray cleaning with two or more jets impinging against each other
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/502—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific solution or suspension
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
    • B01D53/504—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound characterised by a specific device
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/62—Carbon oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • B01D53/79—Injecting reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/80—Semi-solid phase processes, i.e. by using slurries
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/402—Alkaline earth metal or magnesium compounds of magnesium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/40—Alkaline earth metal or magnesium compounds
    • B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/606—Carbonates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/70—Organic acids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Environmental & Geological Engineering (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Biomedical Technology (AREA)
  • Analytical Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Gas Separation By Absorption (AREA)
  • Treating Waste Gases (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

A kind of gas-liquid contact system that is used for absorbing with absorbability liquid gas pollutant, wherein contact is to reach by flowing relation between control gas and the liquid, thereby is formed with the liquid substance of the liquefaction that is beneficial to the close contact between gas and the liquid.

Description

Gas-liquid contact system
The present invention relates to a kind of device that is used for improving the contact of spray column gas-liquid, particularly be used for improving the device of the elimination efficiency of removing the contained sulfur oxide of flue gas and other pollutants or contaminant.
The contaminant such as sulfur oxide that adopts scrubbing tower or other wet chemistry absorption techniques to remove in the hot flue gas is well-known.This class chemical absorbing system utilizes the technical process of the material of calcic, magnesium or sodium typically.According to these technical process, normally hot flue gas is washed in the gas liquid contact arrangement at upper reaches one with alkaline aqueous solution or suspension.This allows to be scavenged into a certain controllable degree (clearance rate can up to more than 90%) with the contaminant that a kind of controllable mode is removed desire.
United States Patent (USP) U.S.4,263,021 have disclosed a representative instance of this class scrubbing tower.Although this patent can be considered a standard of business circles, the improvement of this technology is constituted theme of the present invention.Other examples of the relevant technologies that this patent is quoted are respectively the U.S.3 that licenses to high stone people such as (Galstaun), and 489,506, license to the U.S.3 of Te Lanna (Terana), 615,199 and license to Da Lingeer people's such as (Darlinger) U.S.3,834,129.
Such scrubbing tower is referred to as tower disc type scrubbing tower or spray/tower disc type scrubbing tower now at large, because wherein adopted such as the distribution of gas of plate or analogous shape and some device of liquid.This tower tray flows evenly flue gas in tower, make it also to play a kind of effect of mass transfer device from wherein flowing through more with being evenly distributed.
One object of the present invention is to improve existing wet flue gas desulfurization technology by improving the spray column distribution of gas.Another object of the present invention is should improve the reactant utilization rate to improve sulfur oxide and/or the mass transfer rates of other contaminants from the gas phase to the liquid phase again, no matter and whether use additive.A further object of the present invention is to promote by the gas flow section that improves downstream liquid conveying equipment front end place the even mixing of gas and liquid.A further object of the invention is to improve the absorption situation by the quantity that changes the suspended particulate in flowing velocity, fluid flow, pH value, the chemism suspension and the area of opening of tower tray.These and other purposes of the present invention will be more obvious after further understanding.
Among the present invention, flue gas with from entering near cat head and contacting and upwards flow through tower by the liquid countercurrent of discharging at the bottom of the tower.At least one horizontally disposed sieve plate is equipped with at the place in the middle of this tower height degree, and liquid is sprayed on the sieve plate.Sieve plate is provided with a plurality of dividing plates, they is arranged to sieve plate is partitioned into unlimited little compartment on a plurality of independent tops.Hole on the sieve plate is to be made for the first area to have first to open area value and second zone has second to open area value, these first and second open that area value is unequal, the cross section that will accomplish to change tower open area so that sieve plate total open area will the sieve plate gross area about 5% and 60% between change.
By doing suitably to adjust to the layout of sieve plate through hole and the size of space and to the liquids and gases flow, gas and liquid will form the liquid substance of gasification in each compartment, impel and form stable liquid holdup, it makes between the two media can reach close contact, having again can be for enough time of contact of carrying out sufficient Chemical Exchange, to reach the purpose of absorption.Flow and size between correlation depend on multiple factor, the character of for example desirable chemical reaction, liquids and gases and related amount of substance.
Fig. 1 is the side cutaway view on an absorption tower.
Fig. 2 is the cutaway view of getting along 2-2 line among Fig. 1.
Fig. 3 is the enlarged perspective of the part on absorption tower illustrated in figures 1 and 2.
The present invention relates to former mandate is U.S.4, the improvement of 263,021 patents.The present invention is based upon on this technology, therefore, only describes below with respect to the specification of previous patent and the improvement part of accompanying drawing.
In illustrated embodiment of the present invention, it can be circular, square, rectangular or arbitrary shape that gas enters contact tower 10(from external air source through admission line 11) lower part.These gases are up discharged from the outlet that is formed on tower 10 tops by tower 10 backs.Gas contacts with liquid countercurrent that each shower nozzle 13 by downward spray is sprayed in by the process of tower 10, and shower nozzle 13 is contained on the intermediate altitude of tower, and on the top of sieve shape tower tray that one or more perpendicular separations are provided with or sieve plate 14 and 16 or below.The suspension gravitate passes through each sieve plate downwards one by one, and then the optional shower nozzle from tower 10 bottoms 18 17 is discharged.
Though tower tray 14 and 16 all has the perforate of the uniform consistent size of spacing usually so that gas passes through tower 10 equably; Yet people also are not familiar with or the spacing of knowing these perforates can be that these perforates on the different or whole tower tray need not be measure-alike so far.This is because believe, since by gas and liquid evenly being mixed could promote absorption, for gas and the better of liquid contact, needs the uniform airflow distribution.Yet situation is not necessarily so, because it is found that recently, opens area by the change tower tray distribution of gas is improved, and then absorb improvement and improve the gas flow section at downstream liquid conveying equipment (being demister) front end place.
In order to accomplish this change of tower tray 14 and 16, can be by at a required regional hole diameter enlargement or increase hole count or increase the area of opening of tower tray 14 and 16 with bigger hole.On the contrary, if need, can with less or less hole the area of opening of tower tray 14 and 16 be reduced by another specific region in tower tray 14 and 16.
In the past, the unified about 1 3/8 inches hole of internal diameter of adopting on the whole tower tray 14 and 16.But will adopt inside diameter ranges now on the tower tray 14 and 16 is from about 9/16 inch to 2 inches or bigger hole (or area is about 0.25 to 3.14 square inch perforate), so that reach better absorption as mentioned above.Determine in addition, by on the tower tray of the scrubbing tower that is used for the gas phase diffusion controlled reaction, adopting the perforate of large-size, the absorption efficiency of sulfur dioxide can reach with whole tower tray on be that 1 3/8 inches the situation in hole is the same with internal diameter, but can reduce many (about 10%) by the pressure drop of tower tray.In the past, adopt and to open the tower tray that area is about 25-50%, and now, known that opening low 17% the tower tray of reaching of area just can satisfy the technical process requirement.In fact, according to these technical process requirements, the opening area and can change of tower tray in the 5-60% scope.
In addition, test shows that to a kind of tower tray of fixedly physical dimension, air velocity departs from the 7-8 feet per second in the tower, and absorbing state but can be improved.This is according to flow velocity SO when being about the 7-8 feet per second 2Clearance rate be minimum result of the test.Surpass or be lower than this numerical example at flow velocity as being 12.5 feet per seconds or when bigger, SO 2Absorptivity sharply increases.
Along with on the sieve plate 14 and 16 and above regional gas contact equably with liquid, gas rises by can carry away the liquid of drop form from the liquid spraying of shower nozzle 13.Some bigger drops may be in tower feed flow give shower nozzle arm 20 above be separated, but under any circumstance all gas all passes through the drop removal equipment 21 of all nidos as is well known labyrinth demister and so on, is minimum and make the liquid that is discharged in the atmosphere.Shower nozzle 22 and the import of 23 flushing demisters 21 and the surface of outlet by arm 24 and 25 feed flows.
The spray liquid that is used to absorb can contain active suspended particulate to form suspension.The chemically active absorbing medium of this class can be a liquid solution, and perhaps the chemically active absorbing medium of this class can be the mixture of suspended particulate and liquid solution.Usually, liquid will be water, but also available other liquid.
In the past, chemically active suspension or solution contained the suspended particulate of 5-10%.But recognize that now tower tray 14 and 16 can be bordering on using with inactive suspension and solution of zero activity that changes to about 40% scope with solid total concentration (i.e. dissolving with suspend).
And, adopt the tower tray and the identical basic SO that has before application this class co-catalyst, buffer and/or additive in helping catalysis system, (promptly adopting the system of buffers such as magnesium salts such as alkalescence, organic acid) 2The spray column of absorptivity is compared, and has made SO 2Absorptivity has increased.This is that the reaction on the tower tray in the foaming layer has been strengthened because of the buffer capacity owing to additive.
Although mention about 20GPM/FT before all knowing 2The fluid flow of (every square feet of gallon per minute), but in the present embodiment, created for the low 5GPM/FT that reaches of sodium based system fluid flow 2, and surpass 75GPM/FT for limestone system 2Record.In addition, at the scene in the oxidation lime stone wet scrubbing system, the pH value of liquid is normally than low 0.2 to 2.2 pH value unit of pH value of the big quantity of fluid of scrubbing tower inner loop on the tower tray.This reduction of pH value increases the utilization rate of reactant, and the effect of the buffer that can work preferably under low pH value is strengthened.
As shown in the figure, each sieve shape tower tray or sieve plate 14 and 16 were all made several compartments in 31 minutes by vertical dividing plate.These dividing plates 31 are spaced apart in the horizontal direction to form the identical or different many compartments 33 of size as required.Fig. 3 shows in order to establish and maintenance sieve plate 14 and the 16 appropriate configuration supporting members 32 at it.Clearly, supporting member 32 is fixed in each wall of tower 10, and sieve plate 14 and 16 extends laterally across tower 10 and extends into little or big member, and these members constitute a perforated baffle to air-flow that makes progress by tower 10 and downward liquid stream.
In this object lesson of described lime stone scrubbing tower so far, tower 10 is to be used for removing sulfur dioxide gas from the flue gas that the combustion of sulfur fossil fuel are produced.The temperature that is entered the flue gas of tower 10 by admission line 11 generally is about Fahrenheit 200 degree or higher.But after passing through shower nozzle 13, flue gas roughly is the saturation temperature that is in about Fahrenheit 110-140 degree.A kind of suspension that used liquid or active absorbent preferably contain calcium carbonate activated or calcium hydroxide in the tower 10, and be mixed with general inactive calcium sulfite and/or calcium sulfate.In the present embodiment, absorbent suspension is sent into through arm 20.Some suspension of discharging from tower 10 bottoms 18 is recycled to arm 20 owing to have at least, thereby has inactive particle to exist in the suspension.Optional spout system 17 is used for air is introduced bottom 18 to produce calcium sulfate.
The mixture of the suspension of contact and gas will form a kind of liquefied material of liquids and gases in each compartment 33, and the apparent upper surface of this material will be the roughly two or three times of the expection activating surface of only suspension.Bubble or the apparent upper surface of foaming substance generally will exceed about 1/2 to 10 inch of the upper surface of sieve plate 14 or 16.

Claims (13)

1, a kind of gas-liquid contanct equipment is characterized in that it comprises:
A) tower that the device that an air inlet, a gas outlet and supplied gas therefrom upwards pass through is arranged;
B) be arranged at least one block of plate in the described tower and that cross described gas flow paths, be shaped on sieve aperture on the described plate, its first area has first to open area value, and its second area has second to open area value, described first and second open area value need not to equate, described plate always open area the gross area of described plate about 5% and 60% between;
C) top portion of described plate is divided into the baffle plate device of a plurality of independent compartments in described tower inside;
D) in described tower, be positioned at least one described plate and be arranged to make suspension or solution can accumulate in ejecting device on the described plate, use and help improving the absorptivity of described tower pollutant.
2, gas-liquid contanct equipment as claimed in claim 1 is characterized in that, is shaped on many holes on the described plate, if described hole is round, its size is that internal diameter is in 9/16 inch to 2 inches scope; If described hole is not round, its area is about 0.25 square inch to about 3.14 square inches.
3, gas-liquid contanct equipment as claimed in claim 2, it is characterized in that, there is more hole the described first area of described plate than the described second area of described plate, perhaps as another program, the hole that has size bigger is compared with the described second area of described plate in the described first area of described plate.
4, gas-liquid contanct equipment as claimed in claim 2 is characterized in that, described gas is crossed described tower to be different from the velocity flow of the corresponding flow velocity of minimum pollution thing absorptivity under design point.
5, gas-liquid contanct equipment as claimed in claim 4 is characterized in that, the described and corresponding flow velocity of minimum pollution thing absorptivity is about the 7-8 feet per second.
6, gas-liquid contanct equipment as claimed in claim 4 is characterized in that, described gas through described tower, is not minimum but higher pollutant absorptivity to reach with the velocity flow that is greater than or less than the 7-8 feet per second.
7, gas-liquid contanct equipment as claimed in claim 6 is characterized in that, described gas with the velocity flow more than about 12.5 feet per seconds through described tower.
8, gas-liquid contanct equipment as claimed in claim 6 is characterized in that, this gas-liquid contanct equipment comprises that the buffer of the alkaline magnesium salts of a usefulness and/or organic acid and so on helps the pollutant absorption system of catalysis.
9, gas-liquid contanct equipment as claimed in claim 6 is characterized in that, for the sodium based system or help catalysis system, the fluid flow of described suspension or described solution can hang down and reach every square feet of (GPM/FT of 5 gallons of per minutes 2).
10, gas-liquid contanct equipment as claimed in claim 6 is characterized in that, for lime stone based system or high pollution thing absorptivity system, the fluid flow of described suspension or described solution up to or surpass every square feet of about 75 gallons of per minute.
11, gas-liquid contanct equipment as claimed in claim 6 is characterized in that, the pH value of the liquid on the described tower tray is generally hanged down 0.2 to 2.0 pH value unit than the pH value of described suspension that recycles or described solution in described tower.
12, gas-liquid contanct equipment as claimed in claim 6 is characterized in that, solid concentration total in described suspension or the described solution is in about 0% to 40% scope.
13, gas-liquid contanct equipment as claimed in claim 6 is characterized in that, can remove such as SO with suitable reactant in described suspension 2, NOx, HCl, particulate, CO 2Deng pollutant.
CN93101505A 1992-02-07 1993-02-06 Gas-liquid contact system Expired - Fee Related CN1070729C (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US83255792A 1992-02-07 1992-02-07
US07/832,557 1992-02-07

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CN1075102A true CN1075102A (en) 1993-08-11
CN1070729C CN1070729C (en) 2001-09-12

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KR (1) KR960004611B1 (en)
CN (1) CN1070729C (en)
CA (1) CA2088880C (en)
TR (1) TR28641A (en)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1118314C (en) * 1999-10-20 2003-08-20 北京化工大学 Gas-liquid contaction equipment under action of centrifugal force field
CN101027386B (en) * 2004-09-27 2011-08-31 龟甲万株式会社 Humidity control air feeder of ventilation koji producing apparatus
CN102772984A (en) * 2011-05-11 2012-11-14 姚茂洪 Washing tower device
CN103638790A (en) * 2013-12-11 2014-03-19 中国神华能源股份有限公司 Method for preventing sulfur dioxide absorption tower from scaling inside
CN103732315A (en) * 2011-09-09 2014-04-16 环球油品公司 Co-current vapor-liquid contacting apparatuses for offshore processes
CN104056851A (en) * 2014-06-06 2014-09-24 常州大学 Integrated device for remediation on volatile pollution soil
CN106912977A (en) * 2017-04-06 2017-07-04 刘海明 A kind of efficient and environment-friendly type tobacco drying plant
CN115854737A (en) * 2022-12-08 2023-03-28 湖南科技大学 Method for determining redundancy critical height of overflow plate of water bath heat exchanger

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CN111644046B (en) * 2020-06-15 2022-05-06 河北建滔能源发展有限公司 Desulfurization and denitrification absorption tower

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Publication number Priority date Publication date Assignee Title
US263021A (en) * 1882-08-22 Treatment of india-rubber and gutta-percha
US4263021A (en) * 1972-12-05 1981-04-21 The Babcock & Wilcox Company Gas-liquid contact system
JPS62168501A (en) * 1986-01-20 1987-07-24 Seiji Michimae Wet gas treatment apparatus
CN2095027U (en) * 1991-04-19 1992-02-05 辽宁师范大学生物工程研究所 Miniature high-efficient energy-saving multifunctional fractionating colaun

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1118314C (en) * 1999-10-20 2003-08-20 北京化工大学 Gas-liquid contaction equipment under action of centrifugal force field
CN101027386B (en) * 2004-09-27 2011-08-31 龟甲万株式会社 Humidity control air feeder of ventilation koji producing apparatus
CN102772984A (en) * 2011-05-11 2012-11-14 姚茂洪 Washing tower device
CN102772984B (en) * 2011-05-11 2016-03-16 姚茂洪 Washing tower device
CN103732315A (en) * 2011-09-09 2014-04-16 环球油品公司 Co-current vapor-liquid contacting apparatuses for offshore processes
CN103732315B (en) * 2011-09-09 2015-08-12 环球油品公司 For the co-current vapor-liquid contact arrangement of operation on the sea
CN103638790A (en) * 2013-12-11 2014-03-19 中国神华能源股份有限公司 Method for preventing sulfur dioxide absorption tower from scaling inside
CN104056851A (en) * 2014-06-06 2014-09-24 常州大学 Integrated device for remediation on volatile pollution soil
CN104056851B (en) * 2014-06-06 2015-11-11 常州大学 Volatile contaminant soil remediation integrated apparatus
CN106912977A (en) * 2017-04-06 2017-07-04 刘海明 A kind of efficient and environment-friendly type tobacco drying plant
CN115854737A (en) * 2022-12-08 2023-03-28 湖南科技大学 Method for determining redundancy critical height of overflow plate of water bath heat exchanger

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TR28641A (en) 1996-12-11
KR960004611B1 (en) 1996-04-09

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