CN1090669C - Method of purifying gas - Google Patents
Method of purifying gas Download PDFInfo
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- CN1090669C CN1090669C CN 98115599 CN98115599A CN1090669C CN 1090669 C CN1090669 C CN 1090669C CN 98115599 CN98115599 CN 98115599 CN 98115599 A CN98115599 A CN 98115599A CN 1090669 C CN1090669 C CN 1090669C
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Abstract
The invention relates to a method of purifying coal gas produced by coal or heavy oil. The method absorbs sulfur compounds in the gas and eliminates other impurities. The invention arranges a scrubbing process (column scrubber 7) before guiding the gas A2 into desulphurization tower, wherein the gas A2 contacts with the scrubbing solution B to at least eliminate chlorine-containing compounds and/or nitrogen compounds in the gas A2.
Description
The present invention relates to purifying method by the synthetic gas of generations such as coal gasifying process, particularly relate to a kind of sulfocompound that can absorb in the coal gas, can easily remove the gas purifying method of processing to the chlorine-containing compound in the coal gas, nitrogenous compound and smoke-like material (subparticle) again simultaneously.
In recent years because the exhaustion of petroleum resources and oil price surging, people are appealing the variation of fuel, now, the exploitation that utilizes technology of coal and heavy oil is carried out, a kind of technology that wherein comes into one's own be with after coal or the heavy oil gasification as the technology of fuel used to generate electricity or synthesis material.In addition, use and generated electricity by the coal gas that gasification obtained, its efficient also just comes into one's own from the viewpoint of effectively utilizing limited resources than using coal or oil to carry out the efficient height of thermal power generation before.
Yet, as this synthetic gas that obtains by gasification, the sulfocompound (hydrogen sulfide etc.) that wherein contains several 100～number 1000ppm is in order to prevent public hazards that these sulphur compounds cause or to the corrosion of upstream device (for example internal combustion turbine etc.) etc., must to be removed.As the method for removing, known example has, and opens shown in the flat 7-48584 communique the spy of Japan, makes coal gas and absorption liquid carry out the wet type gas purifying method of gas-to-liquid contact.
But, with regard to above-mentioned existing gas purifying method, do not have to consider specially chlorine-containing compound (HCl) and nitrogenous compound (NH contained in synthetic gas
3) and smoke-like material objectionable impuritiess such as (subparticles), and people wish this situation is improved.
That is to say, usually in the coal gas that is produced by coal gasifying process etc., contain for example NH about 100～1500ppm
3With the HCl about 100ppm, in addition, when the heat that folds into back and forth with heat exchanger etc. in the coal gas, contain the mist that forms by ammonium chloride etc. in the coal gas in interchanger, in order to make gas purification, these impurity must be removed certainly.
Have again; wherein as the HCl of chlorine-containing compound; it is a kind of strong acid; even stainless material is also had corrodibility, consider from the viewpoint of protection equipment and materials, must be as much as possible be removed at the upstream side of equipment; simultaneously; in the waste gas that the back of being burnt by synthetic gas forms, contain chlorine-containing compound in equipment such as internal combustion turbine,, also must be removed in order to reduce the quantity that is discharged into the chlorine-containing compound in the atmosphere as far as possible.
In addition, ammonia as nitrogenous compound, when in the thionizer that uses the absorption liquid (alkalescence) that forms by amine compound, carrying out the gas-to-liquid contact processing usually, almost can not be removed, when coal gas in internal combustion turbine etc. during burning, ammonia just is transformed into deleterious oxynitride, has so just increased the load of the denitrification apparatus that is arranged on downstream sides such as internal combustion turbine usually.
In addition, the smoke-like material is difficult to remove in thionizer, when it with smoke-like when the internal combustion turbine, not only to cause the problem of material corrosion, and because incendiary effect and thermolysis becomes objectionable impurities (nitrogenous compound and chlorine-containing compound etc.).These objectionable impuritiess will enter in the atmosphere, therefore must as much as possible it be removed at upstream side.
The purpose of this invention is to provide a kind of sulfocompound that can absorb in the coal gas, can easily remove the gas purifying method of processing to the chlorine-containing compound in the coal gas, nitrogenous compound and smoke-like material again simultaneously.
In order to achieve the above object, method according to one of the present invention's gas purification, the synthetic gas that gasification by coal or heavy oil etc. is obtained imports in the thionizer, make itself and this interior absorption liquid of thionizer carry out gas-to-liquid contact, remove sulfocompound contained in above-mentioned synthetic gas thereby absorb, it is characterized in that
Before above-mentioned synthetic gas is imported above-mentioned thionizer, a washing procedure is set, in this operation, make above-mentioned synthetic gas and washings carry out gas-to-liquid contact, remove chlorine-containing compound contained in this coal gas and/or nitrogenous compound thereby absorb at least.
In addition, two gas purifying method according to the present invention is characterized in that, adds acid as required in above-mentioned washings so that the pH value of above-mentioned washings maintained and can suppress the low numerical value that above-mentioned washings absorbs above-mentioned sulfocompound.
In addition, three gas purifying method according to the present invention, it is characterized in that, above-mentioned synthetic gas is imported in the 1st washing tower and the 2nd washing tower in turn, divided for 2 stages carried out above-mentioned washing procedure, the pH value of washings in above-mentioned the 1st washing tower is maintained the numerical value that is suitable for absorbing chlorine-containing compound most, and the pH value with washings in above-mentioned the 2nd washing tower maintains the numerical value that is suitable for absorbing nitrogenous compound most simultaneously.
In addition, four gas purifying method according to the present invention, it is characterized in that, above-mentioned synthetic gas is imported in the 1st washing tower and the 2nd washing tower in turn, divided for 2 stages carried out above-mentioned washing procedure, set each washing tower operating temperature so that the temperature of gas that derives by above-mentioned the 1st washing tower in above-mentioned the 2nd washing tower, reduce.
Fig. 1 is illustrated in the refining plant that is used for implementing the present invention's the 1st embodiment, as the formation of the washing portion of major portion.
Fig. 2 is illustrated in the desulfurization portion of the refining plant that is used for implementing the present invention's the 1st embodiment and the formation of gypsum recoverer.
Fig. 3 is illustrated in the refining plant that is used for implementing the present invention's the 2nd embodiment, as the formation of the washing portion of major portion.
Fig. 4 is illustrated in the refining plant that is used for implementing the present invention's the 3rd embodiment, as the formation of the washing portion of major portion.
In each figure, 7 and 7a represent washing tower, 27 the expression thionizers, 51 the expression water coolers, A and A1～A5 represent synthetic gas, B and B1 represent washings, F represents absorption liquid.
Explain embodiment of the present invention below with reference to the accompanying drawings.
Embodiment 1
At first explain embodiment 1.Fig. 1 is illustrated in the refining plant that is used for implementing gas purifying method embodiment 1 of the present invention, and as the formation of the gas washing portion of major portion, Fig. 2 is illustrated in the desulfurization portion in this device and the formation of gypsum recoverer.
At first explain the formation and the basic role thereof of gas washing portion.As shown in Figure 1, in vapourizing furnace 1, for example with air as vaporized chemical with gasification, produce with carbon monoxide and hydrogen synthetic gas A as principal constituent.
Like this, with coal as raw material and the synthetic gas A that obtains as vaporized chemical with air in, contain the H about 1000～1500ppm usually
2COS (sulfocompound) about S (sulfocompound) and 100ppm also contains the NH about 100～1500ppm in addition
3(nitrogenous compound) and a 100ppm left side HCl (chlorine-containing compound).In addition, be generally 1000 ℃～2000 ℃ in the temperature that exports the synthetic gas of downstream part near vapourizing furnace, but common outlet side at vapourizing furnace is provided with a steam heater (omitting among the figure) and reclaims its heat, thereby its temperature for example is cooled to about 350 ℃, and its pressure for example is about 26ata.
This synthetic gas A is at first imported in cyclonic separator 2 and the porous filter 3 in turn, and they separate respectively and remove particle diameter is bigger in the synthetic gas dust and fine dust.Be provided with heat exchanger 4 in the downstream of porous filter 3, utilize the coal gas A4 after heat among the coal gas A1 that is derived by porous filter 3 adds thermal purification.Coal gas A1 is seized heat upstream in this heat exchanger 4, thereby is cooled to for example about 230 ℃.
In the downstream of this heat exchanger 4, a convertor 5 is set, wherein be filled with and be used for COS (carbonyl sulfide) is changed into H
2The catalyzer of S, the COS among the synthetic gas A1 almost all are converted to H herein
2S.
In addition, in the downstream of this convertor 5, a heat exchanger 6 is set, the heat among the coal gas A2 that is derived by convertor 5 also is utilized to add the coal gas A4 behind the thermal purification.
Then, a washing tower 7 is set,, in washing tower 7, carries out gas-to-liquid contact with washings B so that make coal gas A2 be imported into following thionizer 21 (referring to Fig. 2) before the dirty of heat exchanger 6.
In addition, washing tower 7 is a kind of device that is called convection type in the case, and the coal gas A2 that is imported by the tower bottom rises in tower according to the direction opposite with the washings B that flows down, and is removing NH as described as follows
3Deng after, as the washing after coal gas A3 discharge from top of tower.
Herein, the part of washings B is drawn out of by small transfer line from the discharge side of recycle pump 8 in this case, and C is discharged into outside the system as draining.In addition, can supply supplementary feed D aptly,, and supply with sour E (H for example so that remedy owing to as draining C or be entrained in the moisture that is discharged from the coal gas at the anywhere of the circulation approach of washings B
2SO
4), so that adjust the pH value of washings B as described as follows.
In addition, a mist eliminator 11 is set on the tower top of washing tower 7, so that separate the droplet of removing in the coal gas, so just can be effusive from the downstream side, the droplet amount that what is called is carried secretly suppresses extremely very low degree.
Explain the formation and the effect of desulfurization portion below according to Fig. 2.Desulfurization portion mainly is made of thionizer 21 and regenerator column 22.
Thionizer 21 is vapour-liquid contacting columns same with above-mentioned washing tower 7, the hydrogen sulfide absorption liquid F that is stored in regenerator column 22 bottoms is recycled pump 23 suctions upwards, after being absorbed liquid heat exchanger 24 coolings, injection spray pipe 25 ejections from tower top, carry out gas-to-liquid contact with coal gas A3 on one side, via packing material 26 flow downward on one side.
In addition, be removed H owing to carrying out gas-to-liquid contact with absorption liquid F
2Coal gas A4 after the S removes the droplet of wherein carrying secretly by mist eliminator 27, discharges from the top of tower of this thionizer 21 then, then by above-mentioned heat exchanger 6 and heat exchanger 4 heating, thereby becomes the coal gas A5 of purification.
In addition, the pressure that purifies coal gas A5 for example is about 25.5ata, and its temperature is about 300 ℃, sulphur content (H wherein
2The concentration of S and COS) below 10ppm.
On the other hand, being constructed as follows of regenerator column 22, the absorption liquid F that is stored in the tower bottom of thionizer 21 is recycled pump 28 suctions upwards, after being absorbed liquid heat exchanger 24 heating, injection spray pipe 29 ejections from tower top, contact with absorption composition (waste gas) with the steam of the absorption liquid F that in tower, rises on one side, via packing material 30 flow downward on one side.
The absorption liquid F of the tower bottom of this regenerator column 22 is heated by water vapour G in reboiler 31, like this, and as the H that absorbs composition
2S waves in this regenerator column 22 and looses to gas one side.
Then, this H that contains
2The waste gas H of S is removed droplet in mist eliminator 32 after, process is arranged on the backflow portion at the top of regenerator column 22, as containing greater concn H
2(principal constituent is CO to the waste gas H1 of S
2) be sent to following gypsum recoverer.
In addition, in the backflow portion that is arranged at regenerator column 22 tops, waste gas H forms the phlegma I of waste gas H owing to device 33 coolings that are cooled and is stored in the basin 34, this phlegma I is by pump 35 force feeds and from injection spray pipe 36 ejections, so just make the steam among the waste gas H liquefy more, and make in liquid as the H that absorbs composition
2S waves diffusing more, thereby obtains a kind of for example high density H of 20% left and right sides percent by volume that contains
2The waste gas H of S
1
The formation and the effect thereof of explained later gypsum recoverer.The gypsum recoverer of the present embodiment is combined by roasting kiln 41 and desulfurizer, in this roasting kiln 41, and waste gas H1 and air J reaction and make H contained in the waste gas
2S burns, thereby makes waste gas H1 become combustion exhaust H2, and in desulfurizer, utilizes wet type lime stone-gypsum method to absorb from combustion exhaust H2 and remove SO
2Oxysulfides such as (sulphur dioxides).
Desulfurizer has gypsum heating units 45 such as equipment for separating liquid from solid 44, roasting kiln such as reactor 42, air feeder (omitting among the figure), separating centrifuge.This reactor 42 is used to make and contains high density by H
2S burns and the SO of formation
2Combustion exhaust H2 carry out gas-to-liquid contact with the slurry K that supplies to inside reactor and contain calcium cpd and then with its discharge; This air feeder is used for oxidation is blown the slurry that sprays in this reactor 42 with air L with the state of many micro bubbles.This equipment for separating liquid from solid 44 is used for the slurry M (gypsum slurry) that discharges from reactor 42 is carried out solid-liquid separation; This gypsum heating unit 45 is used for the solids component M1 (gypsum filter cake of dihydrate gypsum) that obtains from this equipment for separating liquid from solid 44 is heated to about 120 ℃～150 ℃, thereby makes it become semi-hydrated gypsum.
In addition, the device of representing with symbol 46 in Fig. 2 is a water cooler, and it is used for combustion exhaust H2 is cooled to and helps absorbing SO
2Temperature Deng material.In addition, the dried up M3 of the branch that in equipment for separating liquid from solid 44, produces owing to solid-liquid separation, the moisture as constituting slurry in the reactor 42 directly returns in the reactor 42 in this case.
This reactor 42 can be made of the circulating so-called absorption tower of a kind of slurry, specifically, has the slurry pot that is used to be blown into oxidation usefulness air L at tower bottom, the tower top of flowing through at combustion exhaust H2 has the slurry that is used to spray in the slurry pot, belongs to the gas-to-liquid contact portion of filling type, spraying type or fluid column formula etc.Perhaps also a kind of device of so-called bubbling style of this reactor 42, this device are in the slurry in the two is blown into jar simultaneously with air L and combustion exhaust H2 with oxidation, thereby make SO
2Deng absorption and oxidizing reaction all in jar, carry out.
In a word, in reactor 42, for example carry out by the reaction shown in the following reaction formula (1) to (3), its effect mainly is to absorb SO
2And generation dihydrate gypsum.
In addition, the slurry that supplies in the reactor 42 can be used for example Wingdale (CaCO
3) wait calcium cpd to mix with process water etc. in the slurry pot of elliptical in the drawings and make, but also the solid state of calcium cpd according to miniaturization directly can be supplied in the reactor 42.In addition, also can save gypsum heating unit 45 (gypsum heating process) and the solid matter of the dihydrate gypsum that obtains in equipment for separating liquid from solid 44 directly is used as byproduct.
In addition, the feed rate of calcium cpd can decide according to the amount of answering absorbed sulphur dioxide basically, but waiting, pH value that can be by slurry in test example such as the reactor 42 in actual motion and unreacted limestone concentration controllably finely tune this feed rate, so that this feed rate is remained on the numerical value of suitable absorption reaction etc.In addition, oxidation with the feed rate of air L preferably the redox potential by slurry in test example such as the reactor 42 etc. decide supply with so that its minimum by necessity limited the quantity of.
At length explain below in the gas cleaning device that constitutes as mentioned above, be used to implement the major portion of gas purifying method of the present invention.
In the present embodiment, can utilize above-mentioned washing tower 7 to realize as the washing procedure of feature of the present invention.That is to say that in washing tower 7, the coal gas A2 as the synthetic gas before importing thionizer 21 carries out gas-to-liquid contact with the washings B that with water is principal constituent, therefore, the contained big NH of solubleness in coal gas A2
3(nitrogenous compound) and HCl (chlorine-containing compound), do not need ad hoc to carry out the pH value adjust to wait can have a great deal of to be absorbed among the washings B and finally be exhausted from system as draining C outside.Therefore, the final coal gas A5 that obtains just becomes a kind of H wherein
2The NH of S and a great deal of
3With HCl all be absorbed remove, inaccessiable cleaning coal gas of past.
In addition, common contained NH in coal gas A2
3More than HCl, therefore need not carry out any pH adjustment and can make washings B be alkalescence.When becoming alkalescence, just reduced washings B it to NH
3Absorptive character, and in coal gas A2 contained weakly acidic H
2Therefore S still can be absorbed among the washings B a great deal of, makes to contain these H among the draining C
2S.It is difficult carrying out strict harmless treatment by emission regulation to sulfocompound, therefore, in this case, carry out large-scale draining processing to draining C and just cause expensive problem.
In order to address this problem, in the present embodiment, in the washings B of washing tower 7, to supply with aptly as the sour E of sulfuric acid etc., the pH value with adjustment solution for example makes the pH value of washings B remain on below the weak acid.So just suppressed H contained in draining C
2The quantity of S, thus avoided the draining of trouble to handle, and even in this case, because HCl is a strong acid, therefore also can be absorbed fully in the slightly acidic scope.
But, remove NH in order to absorb more completely
3, preferably the pH value is turned down widely, for example to turn down to the strong acid scope, but in the case, the absorptive character of HCl reduce, therefore, for HCl and NH
3The two is all removed fully, preferably adopts the such double-tower type washing procedure of following embodiment 2.
Explained later embodiment 2.Fig. 3 is illustrated in the device that is used for implementing gas purifying method embodiment 2 of the present invention, as the formation of the gas washing portion of major portion.Should illustrate, put on identical symbol and the repetitive description thereof will be omitted for the parts identical with embodiment 1.
The present embodiment is provided with a washing tower 7a (the 2nd washing tower) who has same formation with washing tower 7 in the downstream side of washing tower 7 (the 1st washing tower), above-mentioned coal gas A2 is imported among washing tower 7 and the 7a in turn, divides for 2 stages carried out washing procedure.
Then, the pH value of the washings B in washing tower 7 left sides is maintained exceedingly do not absorb H
2The scope of S but in the scope (for example slightly acidic scope or neutral range) of the most suitable absorption HCl, the pH value with washings B1 among the washing tower 7a maintains the most suitable absorption of N H simultaneously
3Lower numerical value (for example strongly-acid scope or slightly acidic scope).
In addition, add sour E, as required, also can in washing tower 7, add sour E, so that realize H fully herein though in Fig. 3, only show to the 2nd washing tower 7a
2The absorption of S suppresses.In addition, shown in Figure 3, the draining C1 that is discharged by washing tower 7a is imported in the washing tower 7, so that reduce total displacement as much as possible, but this draining C1 also can be without washing tower 7 and discharge individually, so just can fully independently control the pH value of the washings of washing tower 7 and washing tower 7a etc.
In a word, according to the present embodiment, HCl almost completely is absorbed in washing tower 7, and is not absorbed in washing tower 7 and the NH that left behind
3Then in washing tower 7a, be absorbed fully basically.
In addition, also can change HCl and NH respectively
3Content, so that the content according to them is adjusted to optimum numerical value with the pH value of each washing tower, also the internal circulating load of washings in each washing tower can be adjusted to necessary bottom line in addition, thereby working cost is maintained necessary inferior limit, therefore reached and any material of these objectionable impuritiess can have been absorbed the excellent results of removing basically fully.
In addition, under the situation of the present embodiment, according to inventors' calculating, H among the coal gas A5 after the final purification that obtains
2S, HCl, NH
3Concentration, it is following and below the 10ppm for example to be respectively 5ppm, 1ppm.
Embodiment 3
Explained later embodiment 3.Fig. 4 is illustrated in the device that is used for implementing gas purifying method embodiment 3 of the present invention, as the formation of the gas washing portion of major portion.
Device with respect to embodiment 2 shown in Figure 3 constitutes, and the present embodiment is provided with water cooler shown in Figure 4 51 and cleaning apparatus 52.Water cooler 51 in this case is arranged on the circulation stream of washings B1, for example it can feed process water etc. so that cooling washings B1, in addition, cleaning apparatus 52 can be used for removing the smoke-like subparticle among the coal gas A3 that is derived by washing tower 7a, and concrete example is by the porous filter of ceramic component system and impact type particle collector (impinger).
With regard to the present embodiment, constitute according to this device, the temperature of gas that is derived by the 1st washing tower 7 will reduce in the 2nd washing tower 7a, therefore should adjust to the operating temperature that is lower than washing tower 7 to the operating temperature of washing tower 7a.
Like this, formed the subparticle of smoke-like owing to the cooling of heat exchanger 6 and 7 couples of coal gas A2 of washing tower makes its ammonium chloride of separating out etc., these particles water that is condensed in washing tower 7a captures energetically.
That is to say, by contained water vapor in the gas of washing tower 7 derivation is state of saturation, therefore, when temperature of gas among the washing tower 7a reduces, certainly lead to water of condensation, this is because the above-mentioned subparticle in the coal gas condenses as core, therefore, above-mentioned subparticle almost is trapped in the washings in the washing tower 7a in company with water of condensation all together.
In addition, with regard to the situation of the present embodiment, even by still having the smoke-like material of a small amount of collection at large after capturing, the cleaning apparatus 52 that they also can be set at washing tower 7a downstream captures in above-mentioned washing tower 7a, thereby reached the purification of higher degree.But, according to the rate etc. of removing of desired smoke-like material, even it is also passable that cleaning apparatus 52 is not set.
Should illustrate, the invention is not restricted to above-mentioned the 1st～the 3rd embodiment, various schemes can be arranged.For example, utilizing the 1st washing tower and the 2nd washing tower to divide under the situation that 2 stages carried out washing procedure, a water cooler that is used to cool off the washings of the 1st washing tower can be set, its operating temperature is controlled at is energetically for example helping the temperature range that HCl absorbs.
In addition, also can not adopt the desulfurization that utilizes the lime stone-gypsum method to handle and adopt the monomeric scheme of recovery sulphur from the absorbed sulphur composition in thionizer right side.
Gas purifying method according to one of the invention described above, a washing procedure was set before synthetic gas is imported thionizer, and this operation absorbs at least and removes chlorine-containing compound contained in synthetic gas and/or nitrogenous compound by carrying out gas-to-liquid contact with washings.Therefore, in the final coal gas that obtains, the chlorine-containing compound of sulfocompound and a great deal of and nitrogenous compound all have been absorbed and have removed, the purified product that this coal gas becomes up to now to fail to reach, thus solved because chlorine-containing compound and the caused the problems referred to above of nitrogenous compound.
In addition,, add acid to washings as required, can make washings to the repressed low value scope of the absorption of sulfocompound so that the pH value of washings maintained according to the present invention's two gas purifying method.Therefore, the amount of contained sulfocompound is suppressed in the draining from washing tower, thereby has avoided the draining of trouble to handle.
In addition, three gas purifying method according to the present invention, synthetic gas is imported in the 1st washing tower and the 2nd washing tower in turn, divided for 2 stages carried out washing procedure, the pH value of washings in the 1st washing tower is maintained the numerical value that is suitable for absorbing chlorine-containing compound most, and the pH value with washings in the 2nd washing tower maintains the numerical value that is suitable for absorbing nitrogenous compound most simultaneously.Therefore, chlorine-containing compound almost completely is absorbed in the 1st washing tower, is not absorbed the nitrogenous compound that left behind and then almost completely is absorbed in the 2nd washing tower in the 1st washing tower.
In addition, also can change the content of chlorine-containing compound and nitrogenous compound respectively, so that the content according to them is adjusted to optimum range with the pH value of each washing tower, and the bottom line that the internal circulating load of the washings in each washing tower is adjusted to necessity, and working cost maintained necessary inferior limit, reach simultaneously and in these objectionable impuritiess any all fully can be absorbed the excellent results of removing basically.
In addition, four gas purifying method according to the present invention, synthetic gas is imported in the 1st washing tower and the 2nd washing tower in turn, divided for 2 stages carried out washing procedure, the mode that will reduce in the 2nd washing tower according to the temperature of gas that is derived by the 1st washing tower is set the operating temperature of each washing tower.Like this, the water that just is condensed in the 2nd washing tower of the smoke-like subparticle in the synthetic gas captures energetically.That is to say, by contained water vapor in the coal gas of the 1st washing tower derivation is state of saturation, therefore, when gas temperature in the 2nd washing tower reduces, certainly lead to water of condensation, this is because the above-mentioned subparticle in the coal gas condenses as core, therefore, above-mentioned subparticle almost is trapped in the washings in the 2nd washing tower in company with water of condensation all together.
Therefore, the concentration of the smoke-like material in synthetic gas is more much lower than past, thereby has solved because the caused above-mentioned problem of smoke-like material.
Claims (4)
1. gas purifying method, comprise that the synthetic gas that the gasification by coal or heavy oil etc. is obtained imports in the thionizer, make itself and this interior absorption liquid of thionizer carry out gas-to-liquid contact, remove sulfocompound contained in above-mentioned synthetic gas thereby absorb, it is characterized in that
Before above-mentioned synthetic gas is imported above-mentioned thionizer, a washing procedure is set, in this operation, make above-mentioned synthetic gas and washings carry out gas-to-liquid contact, remove chlorine-containing compound contained in this coal gas and/or nitrogenous compound thereby absorb at least.
2. the purifying method of coal gas as claimed in claim 1 is characterized in that, adds acid as required in above-mentioned washings so that the pH value of above-mentioned washings maintained and can suppress the low numerical value that above-mentioned washings absorbs above-mentioned sulfocompound.
3. gas purifying method as claimed in claim 1, it is characterized in that, above-mentioned synthetic gas is imported in the 1st washing tower and the 2nd washing tower in turn, divided for 2 stages carried out above-mentioned washing procedure, the pH value of washings in above-mentioned the 1st washing tower is maintained the numerical value that is suitable for absorbing chlorine-containing compound most, and the pH value with washings in above-mentioned the 2nd washing tower maintains the numerical value that is suitable for absorbing nitrogenous compound most simultaneously.
4. gas purifying method as claimed in claim 1, it is characterized in that, above-mentioned synthetic gas is imported in the 1st washing tower and the 2nd washing tower in turn, divided for 2 stages carried out above-mentioned washing procedure, set each washing tower operating temperature so that the temperature of gas that derives by above-mentioned the 1st washing tower in above-mentioned the 2nd washing tower, reduce.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP9196530A JPH1119468A (en) | 1997-07-07 | 1997-07-07 | Gas purification |
| JP196530/97 | 1997-07-07 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1206038A CN1206038A (en) | 1999-01-27 |
| CN1090669C true CN1090669C (en) | 2002-09-11 |
Family
ID=16359280
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 98115599 Expired - Fee Related CN1090669C (en) | 1997-07-07 | 1998-07-06 | Method of purifying gas |
Country Status (2)
| Country | Link |
|---|---|
| JP (1) | JPH1119468A (en) |
| CN (1) | CN1090669C (en) |
Families Citing this family (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4658350B2 (en) * | 2001-02-22 | 2011-03-23 | 電源開発株式会社 | Method and apparatus for reducing sulfur compounds |
| KR100488904B1 (en) * | 2002-05-10 | 2005-05-10 | 박수길 | Method and Apparatus for Remove a Bad Smell |
| KR100821463B1 (en) | 2007-04-19 | 2008-04-11 | 현대중공업 주식회사 | Device and method to separate odorants from natural gas |
| CN101708412B (en) * | 2009-11-16 | 2011-12-21 | 浙江大学 | Twin tower type recovering sulfur resource ammonia desulfuration equipment and method |
| CN107653007A (en) * | 2017-11-08 | 2018-02-02 | 中科合肥煤气化技术有限公司 | A kind of high temperature heating gas washes de-dusting cycle device |
| JP7066563B2 (en) | 2018-07-26 | 2022-05-13 | 三菱重工エンジニアリング株式会社 | Gasification gas treatment equipment and gasification gas treatment method |
| CN109529576B (en) * | 2018-12-31 | 2024-03-22 | 南京格洛特环境工程股份有限公司 | Flue gas low temperature desulfurization denitration spray scrubber |
-
1997
- 1997-07-07 JP JP9196530A patent/JPH1119468A/en not_active Withdrawn
-
1998
- 1998-07-06 CN CN 98115599 patent/CN1090669C/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH1119468A (en) | 1999-01-26 |
| CN1206038A (en) | 1999-01-27 |
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