CN1090228C - Fine preparation method for gas - Google Patents

Fine preparation method for gas Download PDF

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Publication number
CN1090228C
CN1090228C CN98109828A CN98109828A CN1090228C CN 1090228 C CN1090228 C CN 1090228C CN 98109828 A CN98109828 A CN 98109828A CN 98109828 A CN98109828 A CN 98109828A CN 1090228 C CN1090228 C CN 1090228C
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gas
mentioned
burning
ammoniacal liquor
ammonia
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CN1206735A (en
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多谷淳
越智英次
洲崎诚
冲野进
本城新太郎
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Mitsubishi Heavy Industries Ltd
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Mitsubishi Heavy Industries Ltd
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/04—Breaking emulsions
    • B01D17/047—Breaking emulsions with separation aids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/02—Foam dispersion or prevention
    • B01D19/04—Foam dispersion or prevention by addition of chemical substances
    • B01D19/0404—Foam dispersion or prevention by addition of chemical substances characterised by the nature of the chemical substance
    • B01D19/0409—Foam dispersion or prevention by addition of chemical substances characterised by the nature of the chemical substance compounds containing Si-atoms
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D19/00—Degasification of liquids
    • B01D19/02—Foam dispersion or prevention
    • B01D19/04—Foam dispersion or prevention by addition of chemical substances
    • B01D19/0404—Foam dispersion or prevention by addition of chemical substances characterised by the nature of the chemical substance
    • B01D19/0413—Foam dispersion or prevention by addition of chemical substances characterised by the nature of the chemical substance compounds containing N-atoms
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G33/00—Dewatering or demulsification of hydrocarbon oils
    • C10G33/04—Dewatering or demulsification of hydrocarbon oils with chemical means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L1/00—Liquid carbonaceous fuels
    • C10L1/10—Liquid carbonaceous fuels containing additives
    • C10L1/14—Organic compounds
    • C10L1/28—Organic compounds containing silicon
    • C10L1/285—Organic compounds containing silicon macromolecular compounds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M155/00—Lubricating compositions characterised by the additive being a macromolecular compound containing atoms of elements not provided for in groups C10M143/00 - C10M153/00
    • C10M155/02—Monomer containing silicon
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M171/00—Lubricating compositions characterised by purely physical criteria, e.g. containing as base-material, thickener or additive, ingredients which are characterised exclusively by their numerically specified physical properties, i.e. containing ingredients which are physically well-defined but for which the chemical nature is either unspecified or only very vaguely indicated
    • C10M171/004—Foam inhibited lubricant compositions
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2229/00—Organic macromolecular compounds containing atoms of elements not provided for in groups C10M2205/00, C10M2209/00, C10M2213/00, C10M2217/00, C10M2221/00 or C10M2225/00 as ingredients in lubricant compositions
    • C10M2229/04—Siloxanes with specific structure
    • C10M2229/045—Siloxanes with specific structure containing silicon-to-hydroxyl bonds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2229/00—Organic macromolecular compounds containing atoms of elements not provided for in groups C10M2205/00, C10M2209/00, C10M2213/00, C10M2217/00, C10M2221/00 or C10M2225/00 as ingredients in lubricant compositions
    • C10M2229/04—Siloxanes with specific structure
    • C10M2229/046—Siloxanes with specific structure containing silicon-oxygen-carbon bonds
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2229/00—Organic macromolecular compounds containing atoms of elements not provided for in groups C10M2205/00, C10M2209/00, C10M2213/00, C10M2217/00, C10M2221/00 or C10M2225/00 as ingredients in lubricant compositions
    • C10M2229/04—Siloxanes with specific structure
    • C10M2229/047—Siloxanes with specific structure containing alkylene oxide groups
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2229/00—Organic macromolecular compounds containing atoms of elements not provided for in groups C10M2205/00, C10M2209/00, C10M2213/00, C10M2217/00, C10M2221/00 or C10M2225/00 as ingredients in lubricant compositions
    • C10M2229/04—Siloxanes with specific structure
    • C10M2229/048—Siloxanes with specific structure containing carboxyl groups
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2229/00—Organic macromolecular compounds containing atoms of elements not provided for in groups C10M2205/00, C10M2209/00, C10M2213/00, C10M2217/00, C10M2221/00 or C10M2225/00 as ingredients in lubricant compositions
    • C10M2229/04—Siloxanes with specific structure
    • C10M2229/05—Siloxanes with specific structure containing atoms other than silicon, hydrogen, oxygen or carbon
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2229/00—Organic macromolecular compounds containing atoms of elements not provided for in groups C10M2205/00, C10M2209/00, C10M2213/00, C10M2217/00, C10M2221/00 or C10M2225/00 as ingredients in lubricant compositions
    • C10M2229/04—Siloxanes with specific structure
    • C10M2229/05—Siloxanes with specific structure containing atoms other than silicon, hydrogen, oxygen or carbon
    • C10M2229/052—Siloxanes with specific structure containing atoms other than silicon, hydrogen, oxygen or carbon containing nitrogen

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Toxicology (AREA)
  • Dispersion Chemistry (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Treating Waste Gases (AREA)
  • Industrial Gases (AREA)
  • Gas Separation By Absorption (AREA)

Abstract

The invention comprises a scrubbing process which contacts produced gas A1 with ablution B to remove the ammonia-containing impurities, a pH adjusting process which extracts a part of the ablution C and adjusts the pH value to neutral nearby, and an evaporation process which evaporates a part of ablution C1 in evaporating pot 53 and condensates exhaust gas C3 of the evaporating pot 53 to recover the ammonia in gas in aqueous ammonia C6 form and discharge impurity residues in the evaporating pot 53 in solid form C5.

Description

Fine preparation method for gas
The present invention is the relevant process for purification that utilizes generation gases such as gasification flow process, in detail, be in the relevant sulfide in absorbing gas, can remove ammoniated impurity simply, and, need not therefore and the fine preparation method for gas that the draining of the complexity that produces is handled.
In recent years, because petroleum resources are exhausted day by day, price increase, therefore so-called fuel variation, the technology of utilizing of coal, heavy oil is continually developed, one of them, with coal or heavy oil gasification, very noticeable as the technology of fuel used to generate electricity or synthesis material.In addition, utilize gasification burning to generate electricity, with the thermal power generation that in the past utilized coal or oil relatively, its efficient height, can effectively utilize the limited resources this point and also make one notice.
But, in the generation gas of these gasifications, contain the sulfide (hydrogen sulfide etc.) of hundreds of～several thousand ppm, for preventing public hazards and, needing to remove to the corrosion of the follow-up equipment in the flow process (as internal combustion turbine etc.).
As the removal method, there for example have the spy to open flat 7-48584 communique to be pointed like that, and known have in absorption liquid, the wet type fine preparation method for gas that gas is contacted with absorption liquid.
Yet, in above-mentioned fine preparation method for gas in the past, but do not have special relevant HCl and the NH that contains in the gas that generate that consider 3Deng impurity, therefore need to improve.
Promptly in the gas that in general gasification flow process etc., produces, owing to containing for example NH about 100～1500ppm 3With the HCl about 100ppm,, need be removed for further refining.
In addition, wherein muriate HCl is a strong acid, and stainless material is corrosive, and from the viewpoint of protection equipment and materials, requires to remove at the flow process forebody as far as possible.Meanwhile, the discharge of burning in internal combustion turbine of the gas of generation in order to reduce the chloride amount to airborne release, also requires to remove.
Have again, nitride ammonia generally is almost can't remove when gas-liquid is handled in the thionizer of the absorption liquid of being made up of amine compound (alkalescence), burning becomes deleterious oxynitride in internal combustion turbine etc., so caused the problem of the denitrification apparatus load increase that is arranged on the internal combustion turbine rear portion.
As the method for removing these impurity, so-called thionizer is with the generation gas in other clean tower, carries out gas-to-liquid contact and clean in ablution, and these objectionable impuritiess are dissolved, and absorbs the method for removal.But, at this moment prevent above-mentioned impurity savings, need to discharge a part of above-mentioned ablution, become the problem of aftertreatment.
I.e. water of discharging from above-mentioned clean tower is owing to contain HCl, NH 3Deng and heavy metal, H 2S, COS, multiple harmful substances such as CN, the drainage processing method as the past adopts, for example as shown in Figure 5, operation is many, the equipment cost height, this point also wishes to improve.
In addition, in Fig. 5, the deamination operation is to heat when draining, disengages dissolved NH 3Operation; The F treatment process is the operation by removal fluorochemicals such as the precipitator method; In addition, N, H 2S, the CN treatment process is by biochemical treatment, decomposing N, H 2S, CN etc. reach innoxious or handle to the amount below the limits value.It then is in order to adjust for example physical chemistry processing that COD carries out under limits value that COD handles.
The objective of the invention is, in the sulfide in absorbing gas, can remove other impurity easily, and the process for purification that does not need complicated draining to handle therefrom is provided.
In addition, purpose provides the process for purification that the ammonia in the impurity after realizing removing effectively utilizes in addition.
In order to achieve the above object, gas purification mode of the present invention, be to import thionizer by gases that gasification produced such as coal or oil, the gas-to-liquid contact that absorption liquid in utilization and the thionizer carries out, the sulfide that is contained in the above-mentioned generation gas is removed in absorption, meanwhile, the absorption liquid that has absorbed sulfide is heated in regenerator column, regeneration contains the regeneration gas of sulfide, again with this regeneration gas burning, convert the smoke discharging that contains sulphurous acid gas to, and then the sulphurous acid gas in this smoke discharging is absorbed by-product gypsum by the wet gypsum method.
This fine preparation method for gas is characterized in that being provided with following operation: make above-mentioned generation gas and washings gas-to-liquid contact, thereby absorb the clean operation of removing the impurity ammonia that is contained in the above-mentioned gas; The above-mentioned a part of ablution of extracting, near the pH that the pH value is adjusted to neutral adjusts operation; The part of the above-mentioned ablution after the adjustment operation is evaporated in evaporating pot, the vapor condensation that evaporating pot is discharged, ammonia in the above-mentioned generation gas is reclaimed with the ammoniacal liquor form, simultaneously with the impurity in the generation gas residual in the above-mentioned evaporating pot, with the evaporization process of solid form discharge.
In fine preparation method for gas of the present invention, be provided with to make and generate gas and ablution gas-to-liquid contact, absorb and remove the clean operation that generates ammoniated impurity in the gas and the above-mentioned ablution of part of extracting, adjust the pH value near neutral pH adjustment operation, and the part evaporation that after pH adjusts operation, in evaporating pot, makes above-mentioned ablution, the vapor condensation that evaporating pot is discharged, ammonia in the above-mentioned generation gas is reclaimed with the ammoniacal liquor form, remain in the evaporization process that the impurity in the generation gas in the evaporating pot is then discharged with solid form.
Thereby the generation gas after making with extra care absorbs to have removed and contains sulfide and a considerable amount of ammonia impurity, becomes inaccessible clean air in the past, has solved the problems referred to above that impurity such as ammonia cause.
And, impurity after the absorption, the pH value be adjusted to neutral near after be cured again, except the ammonia that reclaims, owing to be solid form, so can discard, the draining that did not therefore need the sort of in the past multiple operation to form is handled, and cleans the required draining of operation and handles and can be made up of simpler, low-cost device.
Have, according to the present invention, the ammonia that generates in the gas reclaims as ammoniacal liquor in above-mentioned evaporization process, therefore can effectively utilize ammonia again, thereby can reduce operating cost and the utilization by ammonia improves performance.
In addition, in the fine preparation method for gas of the present invention, at least a portion in the ammonia that reclaims in above-mentioned evaporization process by the wet gypsum method, can be supplied with in the absorption liquid that absorbs sulphurous acid gas.
Thus, from the smoke discharging after the regeneration gas burning in the absorption liquid that absorbs sulphurous acid gas wherein, if supply with the ammoniacal liquor that reclaims, then the consumption as the process water of the liquid component of forming above-mentioned absorption liquid can reduce, simultaneously, because the effect of ammonium ion can improve the clearance of sulphurous acid gas, thereby can realize absorbing the miniaturization of sulphurous acid gas equipment and discharge further cleaning of gas from this absorption equipment.
In addition, the denitration that can be used in the smoke discharging that the smoke discharging that produces because of above-mentioned generation burning of gas and the burning of above-mentioned regeneration gas produce of process for purification of the present invention, at least a portion ammoniacal liquor that reclaims in above-mentioned evaporization process is handled.
Like this, when handling because of the denitration of the smoke discharging that generates smoke discharging that burning of gas (for example burning in the internal combustion turbine of gasifying combined generating apparatus) produced and produced because of the burning of regeneration gas (will absorb the burning that sulfide converts sulphurous acid gas to), if can utilize the ammoniacal liquor of recovery, then can cut down when these denitrations are handled and to buy the expense of ammonia, thereby can further lower operating cost.
In addition, fine preparation method for gas of the present invention in the aforementioned evaporation operation, with at least a portion ammoniacal liquor that reclaims, can be used in the neutralizing treatment of the sulphur trioxide in the smoke discharging that is produced because of the regeneration gas burning.
Like this, when the sulphur trioxide neutralizing treatment of the smoke discharging that is produced because of regeneration gas burning, if can utilize the ammoniacal liquor of recovery, then can be lowered into local the solution because of corrosion or the generation of bird nest and and then the exhaust pollution problem that causes of above-mentioned sulphur trioxide due to existing.
In addition, fine preparation method for gas of the present invention, the tail gas that in above-mentioned evaporization process, produces, the portion of air source when can be used as the burning of above-mentioned regeneration gas is supplied with and is handled.
Thus, even contain objectionable constituent in the above-mentioned tail gas, can handle in resurgent gases is burnt the later operation of operation (as the absorption operation of wet type lime stone-gypsum method), and need not to be provided with in addition harmless treatment equipment, this point also makes equipment simple and reduce cost,
In addition, in the fine preparation method for gas of the present invention, at least a portion ammoniacal liquor that reclaims in the above-mentioned evaporization process can be recycled in the above-mentioned vapourizing furnace that gasifies.
Thus, when for example generation has not used up remained ammonia, also handle easily.
And, during such ammoniacal liquor loopback, in vapourizing furnace, the nitrogen of making a living ammonification and consuming and the amount of oxygen just can be cut down, so the waste of effective hydrogeneous composition of the composition that acts as a fuel just can reduce this part only, the consumption of raw materials such as coal reduces, and reduction effect is arranged.
Fig. 1 represents that the main body of the refining plant of one embodiment of the invention cleans the composition diagram of portion;
Fig. 2 represents the desulfurization of same refining plant and the composition diagram of gypsum recoverer;
Fig. 3 represents the composition diagram of ablution draining handling part in the same refining plant;
Fig. 4 is the data plot that confirms effect of the present invention (raising of sulphurous acid gas clearance);
Fig. 5 illustrates the complicated draining treatment process figure that in the past used.
Below according to description of drawings performance of the present invention
Fig. 1 represents that main body in the embodiment device of fine preparation method for gas of the present invention cleans the composition diagram of portion; Fig. 2 represents the composition diagram of desulfurization portion and gypsum recoverer in the same device; Fig. 3 represents the composition diagram of ablution draining handling part in the same device.
At first, clean the composition of portion and do to be used as an explanation with regard to gas.As shown in Figure 1, in vapourizing furnace 1, for example coal gasifies as vaporized chemical with air, and having produced with carbon monoxide and hydrogen is the generation gas A of main component.Like this, be raw material with the coal, air is the generation gas A that vaporized chemical produces, and contains the H about 1000～1500ppm usually 2S (sulfide), the COS about 100ppm (sulfide) also contains the NH about 1000～1500ppm 3With the HCl about 100ppm.In addition, be generally 1000～2000 ℃ when generating gas A fresh baked mouth, reclaim heat by the water vapor well heater (omitting among the figure) that is arranged on outlet of still one side, be cooled to for example 350 ℃, its pressure for example is about 26ata.
, generating the ammonia that contains among the gas A here, is nitrogen and the hydrogen that contained originally in vaporized chemical or the raw material, and reacting by following formula (1) in vapourizing furnace 1 produces.In the present embodiment, because the part of the ammonia C6 described later that will reclaim in the system is recycled to vapourizing furnace 1 circularly, comparison when therefore at all supplying with in the vapourizing furnace 1 with ammonia, only ammonia C6 loopback has not partly suppressed with the reaction shown in the following formula (1).
Be that the reaction shown in the following formula (1) is the reversible reaction (balanced reaction) that generally can play contrary orienting response as described in the following formula (2), according to Le Shate column balancing shifting principle, reaction can be carried out to any direction, as long as concentration, pressure is certain, the mole number of each molecule and volumetric molar concentration are also kept certain relation and are carried out like that, and therefore, the ammonia C6 that only is recycled in the vapourizing furnace 1 has partly suppressed the reaction shown in the following formula (1).In other words, as long as the temperature in the vapourizing furnace 1, pressure is certain, no matter whether supply with ammonia in vapourizing furnace 1, vapourizing furnace 1 ammonia concentration interior or generation gas A is almost certain, as present embodiment, when ammonia C6 is recycled to vapourizing furnace 1, can reduce generating the nitrogen (N that this part ammonia uses 2) and hydrogen (H 2) consumption.
(1)
(2)
Above-mentioned generation gas A imports in cyclonic separator 2 and the porous filter 3 at first successively, and its structure is to separate respectively to remove larger-diameter dust and fine dust.The back of porous filter 3 is provided with heat exchanger 4, by the heat of the gas A1 that enters from porous filter 3, and heating purified gas A4, that is, gas A1 has lost heat on the contrary in this heat exchanger 4, for example be cooled to about 230 ℃.
Be provided with in the back of heat exchanger 4 COS (sulfuration carbonyl) is transformed into H 2The convertor that is filled with catalyzer 5 of S, the COS that generates among the gas A1 almost is transformed into H in umformer 5 2S.
In addition, the back of umformer 5 is provided with heat exchanger 6, by the heat heating purified gas A4 of the gas A2 that derives from umformer 5.
Then, heat exchanger 6 what be provided with later is before importing aftermentioned thionizer 21, to make the clean tower 7 of gas A2 and ablution B gas-to-liquid contact.
Cleaning tower 7 at this moment is so-called filling type vapour-liquid contacting column, is that the ablution B of main component is absorbed rising by recycle pump at tower bottom with the water that stores, spray from the jet valve 9 on tower top, with gas A2 gas-to-liquid contact constantly, dirty through filling material 10, return the such loop structure of tower bottom.
In addition, cleaning tower 7 at this moment is again so-called to streaming equipment, and gas A2 that imports down from tower and dirty ablution B oppositely rise in tower, by with the gas-to-liquid contact of ablution B, remove HCl, NH 3Behind impure thing such as grade, discharge as the gas A3 after cleaning from top of tower.
Here, the part of ablution B is discharged from the bypass of discharge one side of recycle pump 8, discharges as draining C, should have the optional position can suitably replenish the amount of supply because of the supplementary feed D that takes away that contains in draining C or the gas in addition in the circulation route of ablution B.
In addition,, be provided with spraying separator 11 for the spraying in the divided gas flow, to suppress to reduce the spray amount that flow to further part on the tower top of cleaning tower 7.
Then, generate gas A by this process for purification purified gas A4, after heat exchanger 6 and heat exchanger 4 heating, as processed gas A5, for example deliver to internal combustion turbine 12, at this moment the gas turbine fuel as gasifying combined generating uses.
In addition, in Fig. 1, shown in the symbol 13 be, for the oxynitride in the disaggregating treatment smoke discharging that above-mentioned processed gas A5 burning causes in internal combustion turbine 12, as required and the denitrification apparatus that is provided with.Shown in the symbol 14 then be, be arranged on denitrification apparatus 13 front and back,, supply with the generation of steam of steam turbine (omitting among the figure) and the waste heat boiler of heating usefulness for compound power-generating for from smoke discharging A6, reclaiming heat.
At this, denitrification apparatus 13 is to use catalyzer, by the ammonia process of contact reduction, and the device of decomposing nitrogen oxide.In this denitrification apparatus 13 or its front side, will outside system, supply with in the past, inject smoke discharging with the ammonia of denitration equivalent adaptive capacity, and originally for example the back is described, then supply with by the ammoniacal liquor C6 that reclaims in the system, thereby, need not to buy for carrying out the ammonia that denitration is handled, thereby reduced this part operating cost.
In addition, remove, contain ammonia among the processed gas A5 hardly, so have the oxynitride (so-called fuel knock) that produces because of the burning of the ammonia in the fuel in the internal combustion turbine 12 hardly by absorbing in the above-mentioned clean tower 7.Oxynitride among the smoke discharging A6 almost becomes the oxidation of the nitrogen that contains in the combustion air of supplying with internal combustion turbine 12 and the oxynitride (so-called heat pinking) that produces.
Therefore, in this example whole amounts of oxynitride with compare minimizing in the past, can realize the minimizing of denitrification apparatus 13 capacity at least.In addition, improving internal combustion turbine 12 combustion positions, when suppressing the generation of heat pinking,, also might remove denitrification apparatus 13 according to the discharge concentration of desired oxynitride etc.
In addition, why its structure places denitrification apparatus 13 in the middle of the waste heat boiler 14, is to handle in institute's preferred temperature range because make smoke discharging temperature in the denitrification apparatus 13 can be set in above-mentioned denitration.
Secondly, the composition and the effect of desulfurization portion are described by Fig. 2.Desulfurization portion mainly is made up of thionizer 29 and regenerator column 22.
Thionizer 21 is the same with aforesaid clean tower 7, is vapour-liquid contacting column.The hydrogen sulfide absorption liquid F that stores at regenerator column 22 tower bottoms draws rising by recycle pump 23, and is after the cooling, from jet valve 25 injections on tower top, with the continuous gas-to-liquid contact of gas A3, dirty through filling material 26 again in absorption liquid heat exchanger 24.
In addition, with absorption liquid F gas-to-liquid contact, removed H 2The gas A4 of S after separator 27 removes spraying by spraying, discharges from the top of tower of thionizer 21, be heated as processed gas A5 through above-mentioned heat exchanger 6 and heat exchanger 4 again, the pressure of processed gas for example is 25.5ata, and its temperature is about 300 ℃, and the content (H of sulphur 2The concentration of S and COS) below 10ppm.
On the other hand, the structure of regenerator column 22 is, the absorption liquid F that stores at thionizer 21 tower bottoms is by the rising of drawing of recycle pump 28, after in absorption liquid heat exchanger 24, heating, spray from the jet valve 29 on tower top, the steam of the absorption liquid F that rises in the tower constantly contacts with absorbing composition (tail gas), and is dirty through filling material 30 again.
The absorption liquid F of these regenerator column 22 tower bottoms by water vapor G heating, thus, absorbs composition H in reboiler 31 2S discharges at regenerator column 22 gas sides.Then, contain H 2The tail gas H (regeneration gas) of S removes spraying in spraying separator 32 after, the backflow portion through being located at regenerator column 22 tops becomes contains greater concn H 2(main component is CO to the tail gas H1 of S 2), deliver to gypsum recoverer described later again.
In addition, the effect that is arranged on the backflow portion at regenerator column 22 tops is that tail gas H produces by water cooler 33 coolings, the phlegma I that stores the waste gas H in basin 34 sprays from jet valve 36 by pump 35, and like this, the steam among the waste gas H liquefies more, and on the other hand, the absorption composition H in the liquid 2S discharges more, for example can obtain containing volume percent and be about 20% high density H 2The waste gas H1 of S.
Secondly, the composition and the effect of gypsum recoverer are described by Fig. 2.This routine gypsum recoverer is made up of roasting kiln 41 and desulfurizer.Roasting kiln 41 is with tail gas H1 and air J or waste gas C4 described later, and the C7 reaction makes the H that contains 2The S burning.Desulfurizer is with in roasting kiln 41, and the burning gas H2 that waste gas H1 burning becomes removes SO from wherein absorbing 2Hydrosulfates such as (sulphur dioxides) becomes the wet gypsum method of harmless exhaust H3 discharging.
In roasting kiln 41, waste gas C4, few ammonia or the nitrogen among the air J produce oxynitride because of burning among the C7, the discharge concentration of oxynitride as requested, as shown in Figure 2, the dry type denitrification apparatus 41a the same with above-mentioned denitrification apparatus 13 is set at the rear portion of roasting kiln 41, in this device, carries out the denitration processing of the above-mentioned oxynitride among the combustion gases H2.
In addition, in roasting kiln 41, because H 2The S burning is with SO 2Compare, only generation sulphur trioxide (SO seldom 3), if this sulphur trioxide is not handled such existence,, will become the bird nest monoammonium sulfate (NH of severe corrosive owing to combine with residual little ammonia in the gas 4HSO 4), perhaps according to vitriolic dew point characteristic, will produce the bird nest of severe corrosive in coolings such as aftermentioned heat exchangers 46, become sulfuric acid mist.In addition, the sulfuric acid mist that this sulphur trioxide condensation becomes is because submicron particle normally so desulfurizer described later can't capture, can only be contained among the exhaust H3 to airborne release.
In this example, need to add the denitrification apparatus denitration and handle necessary amount, in and the sulphur trioxide of burning gas H2, become sulphur ammonium ((NH harmless, easy capture as also containing 4) 2SO 4) ammonia of volume of amount, inject burning gas H2, and this ammonia is as described later, as shown in Figure 2, be the ammoniacal liquor C6 of recovery system in, under this occasion, can supply with the follow-up equipment of roasting kiln 41.
In addition, above-mentioned ammonia also can do denitration handle with or in and sulphur trioxide usefulness, in gas, inject goodly at different positions in addition, at this moment as in the sulfurous gas and the time spent, injecting gas is good in the follow-up flow process of denitrification apparatus 41a.Above-mentioned ammonia injects good in denitrification apparatus 41a.In addition, the sulphur ammonium that at this moment produces in the gas is the bigger particle of diameter, in the absorption liquid K of other impurity in aforesaid denitrification apparatus, almost all can capture simultaneously, for example is contained in the by-produced gypsum processed.At this moment, sulphur ammonium amount is compared seldom with gypsum, so can not constitute problem to gypsum quality.
Secondly, desulfurizer also is equipped with as lower device, for example H 2S burns to become and contains high density SO 2Burning gas H2 carry out gas-to-liquid contact with the inner pulpous state absorption liquid K that contains the calcium cpd of supply, the reactor 42 of Pai Chuing then, with add and to be blown into air supply means (omitting among the figure) in the reactor 42 for oxidation is volume micro-bubble form with air L, and the slurry M (calcium plaster) that will extract from reactor 42 carries out the solid-liquid separation means such as whizzer 44 of solid-liquid separation.To be heated to about 120～150 ℃ through the solids component M1 of these solid-liquid separation means 44 gained (plaster block of dihydrate gypsum) in addition, become the gypsum heating units 45 such as roasting kiln of semi-hydrated gypsum M2.
In addition, in Fig. 2, shown in the symbol 46 is the heat exchanger that reclaims heat from burning gas H2, and for example the heat by reclaiming makes discharging gas H3 be heated to temperature desired again to airborne release.In addition, the dried up M3 of branch that produces through solid-liquid separation in the solid-liquid separation means 44, at this moment the moisture as forming slurries in the reactor 42 can directly be recycled in the reactor 42.
Specifically, reactor 42 is for example to be blown into the soup compound basin of oxidation with air L at tower bottom, tower top in burning gas H2 circulation is equipped with the gas-to-liquid contact portions such as filling type, spraying type or fluid column formula of spraying the slurry in the slurries basin, can be made up of the circulating so-called absorption tower of slurries.
Perhaps, this reactor 42 also can be blown into oxidation in the slurry of basin with air L and burning gas H2 SO 2Good Deng the what is called that absorbs and oxidation all can be carried out in the basin formula that froths.
In a word, in the reactor 42, for example can carry out the reaction as following reaction formula (3)～(5) form, mainly be to absorb SO 2, generate dihydrate gypsum.
(3)
(4)
(5)
In addition, the absorption liquid K of supply response device 42, for example Wingdale (CaCO 3) wait calcium cpd, be in the drawings in the elliptical slurry jar and process water or ammoniacal liquor C6 described later mix and form, but the certainly small direct supply response device 42 of solid state of calcium cpd.Remove gypsum heating unit 45 (gypsum heating process) in addition, the solids component of the dihydrate gypsum of solid-liquid separation means 44 gained also can be used as by-product utilization.
In addition, the moisture of anabolic reaction device 42 entoplasms because burned gas H2 etc. take away, reduces as placing then, usually so need supply.Be to replenish this part moisture, for example the also moisture of the above-mentioned absorption liquid K of supply indirectly also can directly be supplied to reactor 42.
In this example, the also available ammoniacal liquor C6 described later of part or all of this supplementary feed.Shown in Fig. 2 is the direct supply response device 42 of ammoniacal liquor C6.In addition, from the aftermentioned data as can be known, such injection ammonia, the circulation fluid of desulfurizer (at this moment being absorption liquid K) if in ammonium ion concentration increase, then the clearance of sulphurous acid gas will significantly improve.
In addition, the feed rate of calcium cpd is by the decision of the sulphur dioxide scale of construction of this absorption basically, but when real-world operation, for example the pH value of detection reaction device 42 entoplasms or the concentration of unreacted Wingdale, should make this value remain on the value of optimum absorption reaction, it is good coming the inching feed rate.
In addition, oxidation air L, the redox potentials of the slurry in for example preferred controlling reactor 42 etc. are only supplied with necessary minimum and are limited the quantity of.
Have again,,, be set to capture removal burning gas H in the fronts such as absorption tower of anabolic reaction device 42 in order to reach the purpose that improves by-produced gypsum purity 2In the electric dust precipitator of dust or the other vapour-liquid contacting column different with above-mentioned absorption tower, it is also passable to take and capture the method for distinguishing of removing the dust that contains above-mentioned sulphur ammonium and other impurity.
Secondly, the composition and the effect of ablution Drainage Division are described by Fig. 3.
By cleaning the above-mentioned draining C that tower 7 is discharged, at first in pH treatment trough 51, be adjusted to neutral near after, as the recycle system of draining C1 by pump 52 importing evaporating pots 53, evaporating pot 53 is with draining C1 evaporation process, and concentrated solution C2 is separated with ammoniated steam C3.At this moment the concentrated solution C2 that is trapped in the bottom draws rising by recycle pump 54, with the draining C1 of new importing simultaneously by after well heater 55 heating, spray from the jet valve 56 on top, well heater 55 for example is the high temperature and high pressure steam of bleeding by the part of the steam cycle from power generation system in addition, circulation fluid is heated to the heat exchanger of emission intensity temperature.
Then, the concentrated solution C2 that extracts from evaporating pot 53 recycle systems imports vaporizer 57, and then by evaporation process, separates tail gas C4 and mud C5.Vaporizer 57 is by heating means such as elliptical electric heaters among the figure, heats the concentrated solution C2 that is trapped in bottom, importing and the equipment that carries out evaporation process.At this moment be detained in the bottom and be impregnation state configuration revolving drum 58, the solid in the stagnant liquid that adheres to around the tube 58 is sent continuously, discharges as mud C5.
In addition, the ammoniated steam C3 that derives from evaporating pot 53 tops, after being cooled to condensing temperature by water cooler 59, import condensate drum 60, the water of condensation (being ammoniacal liquor C6) that contains ammonia separates with tail gas C7, then, the delay ammoniacal liquor C6 of condensate drum 60 bottoms draws by pump 61, liquid component as the slurry of gypsum recoverer, deliver to reactor 42 as previously mentioned, meanwhile, supply with the front portion of denitrification apparatus 13 and 41a as described above, can be used for the neutralizing treatment of above-mentioned denitration processing or sulphur trioxide.In addition, the residue part of ammoniacal liquor C6 can be back to vapourizing furnace 1 as previously mentioned.
Below in aforementioned such refining plant of forming, just implement process for purification of the present invention and action effect thereof and be illustrated.
In this example, clean operation of the present invention is carried out by aforementioned clean tower 7, and promptly in clean tower 7, import the generation gas A2 before the thionizer 21 and be the ablution B gas-to-liquid contact of main component with water, so the NH of the high-dissolvability that contains among the gas A2 3, HCl even especially do not adjust the pH value, also has considerablely to be absorbed by ablution B.Therefore, the generation gas (at this moment being gas A5) after refining absorbs has removed H 2S and considerable NH 3Or HCl, the clean air that this is in the past to be can not get.
In this example, pH of the present invention adjusts operation and adjusts groove 51 implementations by pH, draining behind a part of ablution in the aforementioned clean operation of promptly having extracted, at first adjust and add the adjustment agent P that forms by acid (as sulfuric acid) or alkali (as sodium hydroxide) in the groove 51 as required at pH, as pH being adjusted to neutrality or weakly alkaline, then just can prevent the corrosion of equipment in the subsequent handling, also be easy to handle simultaneously mud C5 described later.
In addition, in this example, evaporization process of the present invention is to carry out by aforementioned evaporation jar 53 and vaporizer 57, be the adjusted draining C1 of pH value, at this moment carrying out dual circulation in evaporating pot 53 and vaporizer 57 handles, removed the solvent components of ammonia, discharged as almost being neutral mud C5 (dividing) Gu form.Therefore, mud C6 being carried out harmless treatment by methods such as cement solidifications discards.Its result does not need the draining of the draining C1 of the sort of multiple operation in the past to handle, and the processing of draining C1 is especially simple, can utilize low-cost device.
In addition, in this example, the ammoniated water vapor C3 that produces in the above-mentioned evaporization process recovery that in water cooler 59 and drainer 60, is condensed, the ammoniacal liquor C6 of recovery can be used as the composition of the absorption liquid that absorbs sulphurous acid gas in the aforementioned gypsum recoverer and supplies with use.
Promptly as previously mentioned, for example as shown in Figure 2, ammoniacal liquor C6 is supply response device 42 directly, at this moment can reduce the consumption of process water, can improve simultaneously the clearance of sulphurous acid gas, the absorption equipment of sulphurous acid gas (reactor) can be realized miniaturization, and and then purifying exhaust gas H3.
Why say so, be because of the research according to the contriver, the ammonium salt concentration (ammonium concentration) in the circulation fluid of absorption tower is if rise, even other condition is certain, as shown in Figure 4, the clearance that can learn the sulphurous acid gas in the smoke discharging of absorption tower improves.Therefore, above-mentioned recovery ammoniacal liquor C6 can be used as the liquid component supply of forming the absorption liquid that absorbs sulphurous acid gas.As by this example, absorption tower (at this moment being reactor 42) Miniaturizable, and also the concentration of residual sulphurous acid gas can further reduce among the exhaust H3.
In this example, the ammoniacal liquor C6 of recovery can supply with the front portion of denitrification apparatus 13 and 41a, and the denitration that promptly can be used for the smoke discharging (at this moment being burning gas H2) that smoke discharging (at this moment being smoke discharging A6) due to the processed gas A5 burning and resurgent gases burning produce is handled.
Therefore, when the denitration of denitrification apparatus 13 and 41a is handled, can cut down the expense of buying of required ammonia, thereby can reduce operating cost.
And in this example,, inject the amount of the ammoniacal liquor C6 of burning gas H2 in the front side of denitrification apparatus 41a flow process, and as previously mentioned, can set manyly than the denitrogenation equivalent, also can utilize ammoniacal liquor C6 during sulphur trioxide neutralizing treatment in burning gas H2.
Therefore, can solve above-mentioned because of there being the generation of the burn into bird nest that sulphur trioxide causes, and then the pollution problem of the exhaust H3 that produces, and reduced cost.
In addition, in this example, the tail gas C4, the C7 that in above-mentioned evaporization process, produce, the portion of air that can be used as when making aforementioned tail gas H1 (regeneration gas) burning is supplied with processing, promptly in the roasting kiln 41 in aforesaid gypsum recoverer, tail gas H1 and air J or tail gas C4, C7 are burnt simultaneously.
Therefore, even when in tail gas C4, C7, containing objectionable constituent, can handle roasting kiln 41 later middle removals of operation (for example processing of the denitration among the denitrification apparatus 41a or the gas-to-liquid contact in reactor 42 are handled), need not to be provided with in addition harmless treatment equipment, also can make equipment simple from this point, reduce cost.
And then in this example, the remainder of the ammoniacal liquor C6 of recovery is recycled in the vapourizing furnace 1 circularly, and therefore, unspent remained ammonia is handled in can be by system in above-mentioned denitration processing etc., so the ammoniacal liquor of remainder is also handled easily.
Promptly in close miscellaneous equipment,, then remaining ammoniacal liquor can be supplied with this equipment, can effectively utilize if any the purposes of utilizing ammonia.If there is not the purposes of this respect, in the time can not selling the processing of acquiring an advantage etc., handle if then carry out complicated draining in the past, and draining etc. has only waste treatment, but this for example is recycled to remained ammonia vapourizing furnace 1, need not to carry out complicated draining and handles.
And, during such ammoniacal liquor loopback, as previously mentioned in vapourizing furnace 1, because the nitrogen that generation ammonia is consumed and the amount of hydrogen reduce, the amount that the available hydrogen that acts as a fuel is consumed for no reason can reduce, this part only, the consumption of raw materials such as coal seldom, reduction effect is arranged, promptly when not loopback ammoniacal liquor, the whole ammonia that produce in vapourizing furnace 1 are finally discharged outside the system, and the effective constituent that acts as a fuel hydrogen is given up waste with the form of ammonia, if make its a part of loopback round-robin words at least, only this a part of just can minimizing is given up waste.
In addition, like this ammoniacal liquor is recycled to the structure of vapourizing furnace 1, as previously mentioned, the concentration that generates ammonia among the gas A is almost constant, and the load of therefore cleaning tower 7 can not increase.
In addition, the present invention is not limited only to the foregoing description, also various examples can be arranged.
For example in the present invention, utilize method or treatment process as what reclaim ammoniacal liquor, can supply with in the absorption liquid of lime stone-gypsum method desulfurization processing, be used for absorbing the method for sulphurous acid gas, and the denitration treatment process and the neutralizing treatment method that is used for the smoke discharging sulphur trioxide that are used for the smoke discharging of generation in the system, be recycled to vapourizing furnace round-robin method in addition.But there is no need certainly to implement simultaneously, can according to circumstances implement any, can certainly arbitrary combination wherein method implemented.
In addition, clean the ablution in the operation, can throw in acid etc. as required, its pH is adjusted to suitable absorption of N H 3Or the value of HCl.In addition, the clean tower that operation is cleaned in a plurality of implementations can be set, for example the 1st clean tower mainly absorbs HCl, and the 2nd cleans the then main absorption of N H of tower 3
Have again, the water cooler of cooling ablution can be set, make its operating temperature utilize absorption of N H 3Or HCl.

Claims (9)

1. fine preparation method for gas, it is gas importing thionizer with gasification gained such as coal or oil, in thionizer, pass through and the absorption liquid gas-to-liquid contact, absorb and remove the sulfide that is contained in the above-mentioned generation gas, meanwhile, the absorption liquid that has absorbed sulfide is heated in regenerator column, regeneration contains the resurgent gases of sulfide, make this resurgent gases burning, convert the smoke discharging that contains sulphurous acid gas to, and then utilize wet type lime stone-gypsum method, absorb the sulphurous acid gas in the smoke discharging, and produce by-produced gypsum;
It is characterized in that, be provided with and make above-mentioned generation gas gas-to-liquid contact in ablution, the ammonia impurity that contains in the above-mentioned generation gas is absorbed the operation of removing; The part of above-mentioned ablution is extracted, pH is adjusted near neutral pH adjusts operation; Above-mentioned part is evaporated in evaporating pot through the ablution that pH adjusts operation, make the vapor condensation of discharging from evaporating pot, ammonia in the above-mentioned generation gas is reclaimed with the ammoniacal liquor form, remain in simultaneously and generate the evaporization process that the impurity in the gas is discharged with solid form in the evaporating pot.
2. according to the fine preparation method for gas of claim 1 record, it is characterized in that,, be supplied in the absorption liquid by aforementioned lime stone-gypsum method absorption sulphurous acid gas at least a portion ammoniacal liquor that reclaims in the above-mentioned evaporization process.
3. according to claim 1 or 2 fine preparation method for gas of putting down in writing, it is characterized in that, at least a portion ammoniacal liquor that reclaims in the above-mentioned evaporization process is used for the smoke discharging that burning produced of above-mentioned generation gas and/or the denitration of the smoke discharging that produced because of the burning of above-mentioned regeneration gas is handled.
4. according to the fine preparation method for gas of claim 1 or 2 records, it is characterized in that at least a portion ammoniacal liquor that reclaims is used for the neutralizing treatment because of the sulphur trioxide of the above-mentioned regeneration gas burning smoke discharging that produces in the aforementioned evaporation operation.
5. according to the fine preparation method for gas of claim 1 or 2 records, it is characterized in that, the tail gas that produces in the above-mentioned evaporization process, the part of the air source when burning as above-mentioned regeneration gas is supplied with and is handled.
6. according to the fine preparation method for gas of claim 1 or 2 records, it is characterized in that at least a portion ammoniacal liquor that reclaims is recycled in the above-mentioned vapourizing furnace that gasifies in above-mentioned evaporization process.
7. according to the fine preparation method for gas of claim 3 record, it is characterized in that at least a portion ammoniacal liquor that reclaims is used for the neutralizing treatment because of the sulphur trioxide of the above-mentioned regeneration gas burning smoke discharging that produces in the aforementioned evaporation operation.
8. according to the fine preparation method for gas of claim 7 record, it is characterized in that, the tail gas that produces in the above-mentioned evaporization process, the part of the air source when burning as above-mentioned regeneration gas is supplied with and is handled.
9. the fine preparation method for gas of putting down in writing according to Claim 8 is characterized in that at least a portion ammoniacal liquor that reclaims is recycled in the above-mentioned vapourizing furnace that gasifies in above-mentioned evaporization process.
CN98109828A 1997-06-11 1998-06-10 Fine preparation method for gas Expired - Fee Related CN1090228C (en)

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* Cited by examiner, † Cited by third party
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CN1902437B (en) * 2003-11-26 2010-06-16 水技术国际股份有限公司 Method for preparing under-well injection steam used in steam overflow process in oil recovery

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CN112023676B (en) * 2020-09-07 2022-05-17 浙江兰电环保集团有限公司 Desulfurization and denitrification equipment provided with filter screen cylinder and based on negative pressure water absorption and spraying
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Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1053219A (en) * 1990-09-04 1991-07-24 湖南省化肥工业公司 Refining process for synthetic ammonia raw material gas

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1053219A (en) * 1990-09-04 1991-07-24 湖南省化肥工业公司 Refining process for synthetic ammonia raw material gas

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1902437B (en) * 2003-11-26 2010-06-16 水技术国际股份有限公司 Method for preparing under-well injection steam used in steam overflow process in oil recovery

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