CN1098918C - Gas refinishing process and gas refinishing equipment - Google Patents

Abstract

A gas refining device is disclosed. For a combustion room for burning a sulfur compound more than one heat storage bodies(122)are built and combustion is done heating the regenerated gas(E2)by recovered heat of the flue gas(E3)using the heat storage bodies as media by continuing an operation comprising contacting a specific one of these heat storage bodies with a flue gas(E3)after burning to heat the body and, at the same time, contacting other heat storage bodies with a regenerated gas(E2)before burning to heat the regenerated gas by switching the heat storage body by turns.

Description

Fine preparation method for gas and gas refinishing equipment

The invention relates to and from generation gases such as coal gasifying process, remove sulfide, this sulfide is changed into the fine preparation method for gas that reclaims with gypsum behind the sulfur dioxide gas, more detailed saying, be to have realized low cost about the combustion enginnering that the sulfide that will remove changes into sulfur dioxide gas, but the fine preparation method for gas of practical application.

In recent years, because the exhaustion of petroleum resources and price is surging, more and more higher to the diversified cry of fuel, and the technology of utilizing of coal and mink cell focus has been carried out a large amount of development researches, the technology that one of them is paid close attention to is coal and mink cell focus to be gasified make fuel used to generate electricity and synthesis material.Owing to utilize the generating of gasification gas, before being superior to, efficient utilizes the thermal power generation of coal and oil, so concentrating on effectively, focus utilizes on the limited resources.

Yet this gasification generates and contains the sulfide (mainly be hydrogen sulfide) of hundreds of to several thousand ppm in gas, for preventing to cause public hazards, or prevents to corrode the machine (for example, steam turbine) that flows through later, so must remove.

For example, known method such as spy open flat 6-293888 communique or the spy opens in the flat 7-48584 communique disclosed, make gas carry out gas-to-liquid contact, by liquid-absorbent sulfide, to remove the sulfide in the gas, simultaneously the absorption liquid that has absorbed sulfide is heated, exclude contained sulfide, make Gas reclamation, make the absorption liquid wet type fine preparation method for gas of reprocessing cycle use successively.

Equally, as the sulfide treatment process in the above-mentioned regeneration gas that produces in this fine preparation method for gas, as shown in above-mentioned communique, having burns this regeneration gas is transformed into the smoke evacuation that contains sulfur dioxide gas, utilize wet type lime stone-gypsum method again, absorb the sulfur dioxide gas in this smoke evacuation, obtain the method for by product gypsum.

According to the fine preparation method for gas in above-mentioned past, more may reach purification than dry type fine preparation method for gas, simultaneously, advantage is to have obtained useful gypsum.Yet, according to inventors' research as can be known, in order to implement the above-mentioned gas process for purification more economically.The place that also has following further improvement.

(1) the burning means of regeneration gas generally will be used roasting kiln, must use auxiliary fuel, and not only fuel cost increases, and exhaust smoke level also expands greatly, and the installed capacity after the operation that causes burning greatly maximizes, and has increased running cost greatly.

That is, though the concentration of hydrogen sulfide in the regeneration gas is according to the kind of gasified raw material difference to some extent.Discontinuous input auxiliary fuel for example is 20Vol%, uses general roasting kiln, if also just can not continue burn steadily.For this reason, add the burning regeneration gas and the air of hydrogen sulfide content wherein in roasting kiln, must drop into the air of auxiliary fuel and burning auxiliary fuel, the smoke evacuation flow that produces in the operation of burning must be very big.Like this, when the smoke evacuation flow increases, constitute the later smoke evacuation flow path channel of burning operation and can maximize more with all equipment such as absorption tower that absorb sulfur dioxide gas, simultaneously, the running cost of supply gas fan and gas blower etc. also increases greatly.

(2) when low temperature burns resurgent gases down, the SO in the smoke evacuation ₃Concentration increases, thus must take the erosion resistance of special measure with the later equipment configuration of raising burning operation, thus the increase that brings equipment cost.That is, when burning hydrogen sulfide, react, mainly produce SO according to following reaction formula (1) ₂(sulfur dioxide gas) in addition, also produces SO by reaction formula (2) ₃

(1)

(2)

The SO of reaction formula (2) wherein ₃The formation reaction ratio, shown in Figure 8 as described later, temperature of combustion is low more, the SO in the burning and gas-exhausting ₃Concentration increases more.Under the low temperature of common funnel temperature, owing to form the very strong fumes of sulphuric acid of corrodibility, so the breather line that the burning operation is later and the component parts of thionizer must be made with the expensive erosion resistance material of acidic fog resistance, perhaps, with maintenances such as whole breather lines at high temperature, make it not produce fumes of sulphuric acid, perhaps in smoke evacuation, inject a large amount of ammonias and neutralize, or the like need the special processing measure.Therefore, the most important thing is SO ₃Generation be controlled at bottom line.

In addition, if hydrogen sulfide dense, even do not have auxiliary fuel or use general roasting kiln, for example, under 600～700 ℃ low temperature, though can burn, in this case, as mentioned above, because SO ₃Generation increase, consider it is disadvantageous with regard to the problem of above-mentioned (2) from economic aspect, on the other hand,,, must provide auxiliary fuel if improve temperature of combustion in order to solve this class problem for this reason, with regard to the problem of above-mentioned (1), economic and practical is very poor.

The objective of the invention is to consider to provide more practical fine preparation method for gas and gas refinishing equipment from economic aspect, to eliminate the problems referred to above in the relevant burning operation, be to generate the gas from gasification processing to remove sulfide, burn after this sulfide changes into sulfur dioxide gas the fine preparation method for gas and the gas refinishing equipment that reclaim with gypsum.

In order to achieve the above object, relevant fine preparation method for gas of the present invention, be that the generation gas that is obtained by coal or oil gasification is carried out the purified fine preparation method for gas, its feature comprises following operation, carry out gas-to-liquid contact by the absorption liquid that will generate gas and sulfide, absorb the desulfurization process of removing institute's sulfur compound in the above-mentioned generation gas, heating absorbs the absorption liquid of sulfide in this desulfurization process, discharge the step for regeneration of sulfur compound regeneration gas, the regeneration gas that produces in the burning step for regeneration, change into burning operation that contains the sulfur dioxide gas smoke evacuation and the gypsum recovery process that produces the by product gypsum by the sulfur dioxide gas in the wet type lime stone-gypsum method absorption burning operation generation smoke evacuation;

For the combustion chamber of carrying out above-mentioned burning operation, a plurality of heat storages are set, in these heat storages, any one specific heat storage all contacts with above-mentioned smoke evacuation, when this specific heat storage of heating, simultaneously, make resurgent gases and the above-mentioned regeneration gas of other heat storage Contact Heating before the burning, by the operation of continuously switching heat storage successively, one side with above-mentioned heat storage as media, heat above-mentioned regeneration gas with the heat that reclaims from above-mentioned smoke evacuation, Yi Bian carry out above-mentioned burning operation.

Relevant fine preparation method for gas of the present invention in its preferred plan, is taken as the temperature of combustion of resurgent gases in the above-mentioned burning operation more than 1000 ℃.

Stress face as another, the present invention carries out the purified purification apparatus to generating gas by coal or oil gasification gained, it is characterized in that comprising as follows, promptly, have and make above-mentioned generation gas and sulfide absorption liquid carry out gas-to-liquid contact, absorb the thionizer of removing institute's sulfur compound in the above-mentioned generation gas, absorb the absorption liquid of sulfide in the heating thionizer, discharge the regenerator column of sulfur compound resurgent gases, the regeneration gas that produces in the burning regenerator column changes into the heat-accumulation type hot exchange roasting kiln that contains the sulfur dioxide gas smoke evacuation, with absorb the sulfur dioxide gas that produces in this heat-accumulation type hot exchange roasting kiln in the smoke evacuation by wet type lime stone-gypsum method, produce the desulfurizer of gypsum by product

Above-mentioned heat-accumulation type hot exchange roasting kiln is made of combustion chamber and a plurality of heat exchange streams that each heat storage that is communicated with side by side is installed in the combustion chamber, the structure of above-mentioned heat exchange stream is for above-mentioned combustion chamber, the importing pipeline of above-mentioned regeneration gas or can switch successively as the escape route of above-mentioned smoke evacuation.

Fig. 1 is the structural representation of the gas scrubbing part of the present invention's one routine gas refinishing equipment.

Fig. 2 is the structural representation of desulfurization regeneration part in the same equipment.

Fig. 3 is the structural representation of burning cooling segment in the same equipment.

Fig. 4 is the structural representation of gypsum recovery part in the same equipment.

Fig. 5 is the structural representation of draining treating part in the same equipment.

Fig. 6 is the roasting kiln structure detailed maps of same equipment.

Fig. 7 is the roasting kiln running synoptic diagram of same equipment.

Fig. 8 is the sulfur dioxide gas concentration of expression burning hydrogen sulfide generation and the illustration intention of temperature of combustion correlationship data.

Example of the present invention below is described with reference to the accompanying drawings.

Fig. 1 to Fig. 5 is a gas refinishing equipment of implementing the present invention's one example.Below for convenience of explanation, equipment is divided into a plurality of parts and describes (gas scrubbing part, desulfurization regeneration part, burning cooling segment, gypsum recovery part and draining treating part).In addition, Fig. 1 is a gas scrubbing part-structure synoptic diagram, and Fig. 2 is a desulfurization regeneration part-structure synoptic diagram, and Fig. 3 is a burning cooling segment structural representation, and Fig. 4 is a gypsum recovery part structural representation, and Fig. 5 is that the part-structure synoptic diagram is handled in draining.The recovery part of gypsum shown in Fig. 4 is equivalent to desulfurizer of the present invention.

At first, according to Fig. 1 the structure and the running of gas scrubbing part are described.In the vapourizing furnace of elliptical, for example, as vaporized chemical, coal is gasified air in diagram, producing with carbon monoxide and hydrogen is the generation gas A1 of main component.

, air is made vaporized chemical generate among the gas A1 coal as raw material this, contain the H about 1000～1500ppm usually ₂COS (sulfide) about S (sulfide) and 100ppm, and then contain NH about 1000～1500ppm ₃With the HCl about 100ppm.

Generate gas A, just be generally 1000 ℃～2000 ℃ behind the outlet of still, utilize the steam radiator (diagram is omitted) that is located at the outlet of still side to carry out recovery of heat usually, for example be cooled to 350 ℃, its pressure for example is about 26ata.

This generates gas A1, after elliptical tornado dust collector and porous filter carry out dust removal process in the diagram, as shown in Figure 1, enters in the heat exchanger 1 of hollow end tubular structure.In this heat exchanger 1, purified gas A4 is heated by the heat that generates gas A1, and gas A1 for example, is cooled to about 230 ℃ by the reverse heat of capturing.

In the stream of the back of this heat exchanger 1, be provided with two and loaded COS (sulfuration phosphinylidyne) is changed into H this moment ₂The convertor 2 of the catalyzer of S, herein, the COS that generates among the gas A1 almost all changes into H ₂S.

In the stream of the back of this convertor 2, the heat exchanger 3 of hollow end tubular structure is set, by the heat heating purified gas A4 of convertor 2 eluting gas A2.

Equally, in the stream of the back of heat exchanger 3, make gas A2 and washings B1 or B2 carry out gas-to-liquid contact, set gradually and remove HCl and NH ₃Deng the washing tower 4a of foreign material, 4b.

Washing tower 4a, 4b, be so-called filling type vapour-liquid contacting column in this case, its formation is, to store, by recycle pump 5 suctions, from jet pipe 6 sprays on tower top at the water of tower bottom washings B1 or B2 as principal constituent, with the gas A2 that injects and rise by the tower bottom, carry out gas-to-liquid contact on one side, via packing material 7 flow down on one side, tower bottom is returned in recirculation.

In the part of this washings B1 or B2, this moment, 5b discharged, and discharges as draining B3 from the stream 5a of discharge side branch of recycle pump 5.The washing tower 4b tower bottom of stream side in the back suitably infeeds the make up water B4 of amount as a supplement and replenishes moisture as draining B3 discharges or gas is carried under one's arms away.

On the tower top of each washing tower 4a, 4b, the jet pipe 9 that separates the smoke purifier 8 of removing smog in the gas and the spray washing water B5 that is provided with in this smoke purifier 8 is set, it is smoke suppression to low amount that the back effusive what is called of stream side is accompanied.At this moment, washing water B5 flows to the part that tower bottom constitutes washings downwards.

Owing to can will be stored in the tower bottom that acid in the groove 10 (being sulfuric acid this moment) is fed to each washing tower 4a, 4b by pump 11, by elliptical control device among the figure, pH detected value according to each washings is adjusted the sulfuric acid amount of infeeding, and for example the pH of each washings adjusts by following.

That is, the pH value of the washings B1 among the washing tower 4a is at taken in excess H not ₂Maintain the value (for example, slightly acidic zone or neutral region) that optimum HCl absorbs in the scope of S, the pH with washings B2 among the washing tower 4b maintains optimum NH simultaneously ₃Absorb than low value (for example, strongly-acid zone or slightly acidic zone).

When adjusting the pH value like this, in washing tower 4a, almost all sponge HCl, in washing tower 4a, do not have to absorb and residual NH ₃, can in washing tower 4b, almost completely absorb and get rid of.Even HCl and NH ₃Content when changing individually, also can the pH of each washing tower be adjusted to optimum value according to this variation, and then, the internal circulating load of washings is adjusted to necessary minimum in each washing tower, running cost is maintained inferior limit, and simultaneously, these nuisances almost can both be absorbed removal.

In addition, in this example, will be discharged the part of washings B2 by washing tower 4b, the stream 5C of branch that discharges side by recycle pump 5 sends into washing tower 4a, can reduce total water displacement.

At this moment, utilize elliptical control device among the figure, for example,, the liquid level of washing tower 4a is controlled within the specific limits by adjusting the flow of stream 5a and stream 5c.By adjusting the flow of supplementary feed B4, the liquid level of washing tower 4b is controlled within the specific limits.

In this example, as shown in Figure 1, the water cooler 12 of each washings B1, B2 of cooling is set in each washing tower.This water cooler 12 is provided in a side of the heat exchanger in the washings circulation stream, for example, feeds cooling washingss such as process water.

Like this, in this example, utilize above-mentioned water cooler 12, the temperature of gas and washings is adjusted to the temperature that the optimum foreign material absorb, simultaneously, in the 2nd washing tower 4b, reduce, with the control operating temperature by the 1st washing tower 4a expellant gas temperature.

When carrying out like this, produce the submicron particles that ammonium chloride that the cooling of gas A2 separates out etc. forms smoke-like, under in washing tower 4b, can capturing effectively by condensed water by heat exchanger 3 and washing tower 4a.

Promptly, owing to form state of saturation from washing tower 4a expellant gas institute moisture vapor, so when the temperature of this gas reduces in washing tower 4b, must produce condensed water, this is owing to be that the submicron particles in the gas is condensed as core, among the washings B2 of most submicron particles in this condensed water is captured in washing tower 4b.

Followingly according to Fig. 2 the structure and the running of desulfurization regeneration part are described, the desulfurization part mainly comprises thionizer 21 and regenerator column 22.

Thionizer 21 is return-flow type vapour-liquid contacting columns, and retention is aspirated by recycle pump 93 at the hydrogen sulfide absorption liquid C1 of the tower bottom of regenerator column 22, after the cooling, sends in this thionizer 21 in absorption liquid heat exchanger 24 and absorption liquid water cooler 25.The absorption liquid C1 that infeeds and send into thionizer 21 bottom ascending gas A3 and carry out gas-to-liquid contact absorbs the H in the gas ₂S, and flow downward via packing material 26.Equally, be trapped in the absorption liquid C1 of thionizer 21 bottoms, turn back in the regenerator column 22 via absorption liquid heat exchanger 24 by pipeline 21a.

On the other hand, gas A3 by packing material 26 risings, upwards flow via being located at packing material 26 top shelf sections 27 and packing material 28 successively, carry out gas-to-liquid contact, removing H with the absorption liquid C2 (for example process water) that supplies with shower 29 sprays from the outside ₂Behind S and the submicron particles,, discharge from top of tower as the gas A4 after refining via smoke purifier 30.

Absorption liquid heat exchanger 24 is via the pipeline 22a that said pump 23 is set, from regenerator column 22 infeed the absorption liquid C1 of thionizer 21 and via above-mentioned pipeline 21a between thionizer 21 turns back to absorption liquid C1 the regenerator column 22, carry out the heat exchanger of the hollow end tubular structure of heat exchange.

Absorption liquid water cooler 25 is the heat exchangers that the absorption liquid C1 that is infeeded thionizer 21 by regenerator column 22 carried out refrigerative hollow end tubular structure, can feed the water C3 of process water etc. as cold medium.

The shelf section 27 of thionizer 21 is arranged on the top, supply position that is higher than absorption liquid C1, be for stopping dirty absorption liquid C2, will be divided into the dividing plate of horizontal interval in the thionizer 21, having a plurality of so-called bubble-caps (not shown), gas A3 by bubble-cap rises blows out from above with blister.

Be trapped in the absorption liquid C2 of these shelf section 27 upper face sides, infeed above-mentioned shower 29, circulate by pump 31 suctions, simultaneously, surpass the part of certain hold-up, send into above-mentioned pipeline 21a by upflow tube 21b, a part that finally becomes absorption liquid C1 is sent into regenerator column 22.

By pump 31 in the middle of the stream that shower 29 is supplied with, be provided with water cooler 32 with cooling and absorbing liquid C2 such as process waters.When this water cooler 32 is set, can further cool off with the contacted gas temperature of spray quinoline pipe 29 spray absorption liquid C2 on thionizer 21 tower tops, residue in submicron particles in the gas owing to condensing of moisture increases, and be captured down.

Gas A4 after refining after above-mentioned heat exchanger shown in Figure 13 and heat exchanger 1 heating, as processed gas A5, for example, infeeds in the gas-turbine of gasification gas generating set.Equally, the pressure of this fine gas A5 for example is about 25.5ata, and its temperature can reach about 300 ℃, the composition (H of its sulphur ₂The concentration of S and COS) below 10ppm.

The absorption liquid C1 of sulfide hydrogen absorption agent adds to (suction side of said pump 23) in the above-mentioned pipeline 22a by pump 33 from absorbing liquid bath 34.

The part of absorption liquid C1 is sent in the neutralizing well 36 via the pipeline 35 that branches out from above-mentioned pipeline 22a (the discharge side of said pump 23), after the neutralization, is turned back in the regenerator column 22 by pump 37 in this neutralizing well 36 again.

From neutralizing well 36, the part of the absorption liquid C1 that is sent by pump 37 in well heater 38, after water vapor D1 heating, turns back in the regenerator column 22.In regenerator column 22, be trapped in the absorption liquid C1 of thionizer 21 bottoms, via above-mentioned pipeline 21a, after 24 heating of absorption liquid heat exchanger, infeed material 39 upper face sides that are configured in the tower middle body, contact with absorption composition (discharging gas) with the steam of the absorption liquid C1 that rises in the tower, flow downward via packing material 39 simultaneously.

The absorption liquid C1 of these regenerator column 22 bottoms by the heating of the water vapor D2 in the well heater 40, like this, absorbs composition H ₂S is emitted in this regenerator column 22 in gas one side.Like this, contain this H ₂The discharging gas E1 of S is via smoke purifier 41 that is located at regenerator column 22 tops or backflow part, as the H that contains of greater concn ₂S resurgent gases E2 (principal constituent CO ₂), send into gypsum recovery part described later.

Said herein backflow part is discharging gas E1, generate by water cooler 42 coolings, store the condensation water C4 of the discharging gas E1 in groove 43, infeed the top of tower of regenerator column 22 by pump 44, flow downward via packing material 45, like this, the steam among the discharging gas E1 can liquefy morely, on the other hand, the absorption composition H in the liquid ₂S can discharge morely, for example in volume percent, can obtain containing the high density H about 20% ₂The resurgent gases E2 of S.

Infeeding among the absorption liquid C4 at regenerator column 22 tops by pump 44, sneaking into the absorption liquid C2 (for example process water) that infeeds from the outside.The part of absorption liquid C4 is by the discharge side of pump 44, mixes via take-off line 46 with from the draining B3 of above-mentioned washing tower, sends into burning cooling segment described later as draining B4.

Water cooler 42 is the heat exchangers by the hollow end tubular structure of heat-eliminating medium C5 such as process water cooling discharging gas E1.

Below, the formation and the running of burning cooling segment are described according to Fig. 3.Be provided with the dashpot 51 of the temporary transient storage of resurgent gases E2 that will partly send from desulfurization regeneration in the burning cooling segment, and make resurgent gases E2 and air F1, F2 or discharging gas B7 described later (as shown in Figure 5) reaction of discharging from this dashpot 51, contained H burns ₂The roasting kiln 52 of S and make in this roasting kiln 52 smoke evacuation E3 that burning resurgent gases E2 forms and the cooling fluid G1 that forms by process water etc. carry out the cooling tower 53 of gas-to-liquid contact.

Roasting kiln 52 is heat-accumulation type hot exchange roasting kilns, in this roasting kiln 52, by gas blower 54,55 air-supplied F1, F2.The detailed structure of this roasting kiln 52 and running, the back is narrated according to Fig. 6,7.

In roasting kiln 52, because little ammonia or the nitrogen among air F1, the F2 among the discharging gas B7 produce oxynitride by burning, the discharge concentration of oxynitride for example, can be provided with the dry type denitrification apparatus in the stream of the back of roasting kiln 52 as requested.

In roasting kiln 52, pass through H ₂The burning of S also generates and SO ₂Amount compare a spot of sulphur trioxide (SO ₃).If sulphur trioxide is placed like this,, form the monoammonium sulfate (NH that very strong being easy to of corrodibility forms bird nest by combining with remaining little ammonia in the gas ₄HSO ₄), perhaps the characteristic according to sulphuric acid dew point forms the very strong sulfuric acid mist of corrodibility.

The sulfuric acid mist that sulphur trioxide condenses and forms, owing to be sub-micron particulate, absorption tower 61 described later (as shown in Figure 4) can not capture, and has to be included among the smoke evacuation E5 described later be discharged in the atmosphere.

Therefore, except that the amount that in above-mentioned denitration is handled, needs, can also contain the sulphur trioxide among the neutralization smoke evacuation E3 and form harmless sulphur the ammonium ((NH that is easy to capture ₄) ₂SO ₄) excess of ammonia inject smoke evacuation E3.As this ammonia, can use the ammoniacal liquor M3 or the M5 (as shown in Figure 5) that reclaim in the aftermentioned draining treating part.

Cooling tower 53, the cooling fluid G1 that utilizes recycle pump 56 suction to be detained the bottom from the cat head spray, and sends into the smoke evacuation E3 that rises on the tower bottom and carries out gas-to-liquid contact, carry out gas-to-liquid contact and refrigerative smoke evacuation E3 with this cooling fluid G1 or aftermentioned supplementary feed G2, discharge from top of tower as cooled smoke evacuation E4.

Discharge side at recycle pump 56 is provided with the water cooler 57 that utilizes refrigeration cycle cooling fluid G1 such as process water.Or infeed supplementary feed G2 such as process water from the top of cooling tower 53, as the moisture that constitutes cooling fluid G1.And then the part of cooling fluid G1 is discharged by discharging side ramose pipeline 58 from recycle pump 56, mixes with the draining B4 that is partly sent by desulfurization regeneration, sends into draining described later treating part as draining B5.

Following formation and the running that gypsum recovery part (desulfurizer) is described according to Fig. 4.The gypsum recovery part of this example is to utilize the pulpous state absorption liquid H1 (to call absorbent slurry H1 in the following text) that contains calcium cpd J1 to absorb the SO that removes from the smoke evacuation E4 of burning cooling segment discharge ₂(sulfur dioxide gas) forms the gypsum by product by desulfurizer.

This desulfurizer comprises: the smoke evacuation E4 and the absorbent slurry H1 that will contain the high density sulfur dioxide gas carry out gas-to-liquid contact, discharge as the smoke evacuation E5 after purifying, simultaneously in the slurries that absorbed sulfur dioxide gas, be blown into a large amount of oxidations air F3 with bubble form, with the sulfurous acid oxidation in the slurries and generate the absorption tower 61 of gypsum, will carry out the equipment for separating liquid from solid 62 of the separating centrifuge etc. of solid-liquid separation by the slurries H2 (gypsum slurries) that discharge on absorption tower 61, the liquid bath 63 of storing the filtrate H3 of equipment for separating liquid from solid 62 generations produces the absorbent slurry storage tank 64 of absorbent slurry H1.

In addition, also can have and to be heated to the gypsum heating unit of roasting kiln of making semi-hydrated gypsum about 120～150 ℃ etc. from equipment for separating liquid from solid 62 isolating solids component J2 (gypsum patty will of dihydrate gypsum).

Absorption tower 61 has the slurry tank 65 of supplying with absorbent slurry H1 at tower bottom, is to be arranged side by side four tower body 66a, 66b, 66c, 66d in the drawings above a slurry tank 65.Equally, utilize the slurries in the recycle pump 67 suction slurry tank 65, from being arranged on the intravital jet pipe of each tower jetting fluid scapus that makes progress, E4 carries out effective gas-to-liquid contact with smoke evacuation.

In four tower bodies, tower body 66a, 66c are the vapour-liquid contacting columns of so-called cocurrent flow type, and tower body 66b, 66d are the vapour-liquid contacting columns of so-called convection type.Processed smoke evacuation E4 sends into from the top of this tower body 66a, then send into the bottom of tower body 66b via the top of slurry tank 65, then enter tower body 66c via the connecting tube 66e that connects tower body 66b and tower body 66c top, then enter the bottom of tower body 66d, finally discharge from the top of tower body 66d via the top of slurry tank 65.

Smoke evacuation E5 outlet conduit 69 places after processing set gradually smoke purifier 70 and vent fan 71.

Smoke purifier 70 is owing to will remove the smog follow, so suitably infeed washing water G4 such as process water, washing material wherein from smoke evacuation E5.Washing water G4 that infeeds and removed liquid branch, finally the lower hopper via smoke purifier 70 enters in the slurry tank 65, forms the part of the loop slurry in the absorption tower 61.

Vent fan 71, owing to want the positive delivery smoke evacuation with the smoke evacuation pressure-losses in 61 grades of counteracting absorption tower, so, for example control its ability according to the detected pressure values in the above-mentioned baffle-box 51.

The smoke evacuation E5 that sends by vent fan 71, by elliptical smoke stack emission among the figure in atmosphere.

In slurry tank 65, be provided with in fixed air bubbler 72 that air F3 is blown into as tiny bubble and the steel basin all stirrers 73 of slurries, absorbing sulfurous gas effectively contacts with the air that is blown into from the slurries that each tower body flows downward, the sulfurous acid that is absorbed is almost all oxidized, further produce neutralization reaction, generate highly purified gypsum with calcium cpd.

Under this steady state, contain the slurries of high density gypsum, discharge in groove 65 by pump 74, send in the solid-liquid separating machine 62 as slurries H2, carry out solid-liquid separation, collect solids component gypsum J2.

The filtrate H3 that is produced by above-mentioned solid-liquid separation temporarily is stored in the filtrate receiver 63, suitably extracts out with pump 75, is sent in slurry tank 65 or the absorbent slurry groove 64, and any filtrate finally all will be returned in the slurry tank 65, to recycle.

In absorbent slurry groove 64, mix to stir the calcium cpd J1 (for example Wingdale) that infeeds by elliptical silo among the figure and with the filtrate H3 of this compound amount of adapting, be modulated into certain density absorbent slurry H1.Absorbent slurry H1 in this absorbent slurry groove 64 for example, according to the detected value of handling the sulfur dioxide gas scale of construction among the gas smoke evacuation E4, controls its supply flow rate, is sent in the slurry tank 65 by pump 76.

To evaporation in absorption tower 61, as the steam in the smoke evacuation and the moisture that is pulled away and contain water or planar water and moisture outside the discharge system as gypsum J2, must replenish, for example supplementary feed G3 such as process water are infeeded in the slurry tank 65, the liquid level in the slurry tank 65 is remained in certain scope.

Be attached in the general desulfurizer such as steam power plant, in order to prevent that sulfur dioxide gas is accumulated in the formation liquid of loop slurry with the impurity such as chlorine that absorb in the slurries, can take following measure, for example a part of filtrate in the filtrate receiver be discharged and emitted or re-use after handling outside the system, with draining etc.

Yet, in this example, there is no need to carry out this draining and handle.Why saying so, is that among the smoke evacuation E4 that handles in this example, this impurity exists seldom, outside discharge systems such as gypsum J2, thereby has prevented liquid branch accumulating this impurity because compare with the smoke evacuation of being discharged by steam power plant.

As part or all branch of above-mentioned supplementary feed G3, can use ammoniacal liquor M3 described later or M5 (shown in Figure 5).Inject this ammonia, when ammonium ion concentration in the loop slurry of desulfurizer increases, can notify the removal efficient that improves sulfur dioxide gas more.

Following formation and the running that the draining treating part is described according to Fig. 5.

Above-mentioned draining B5 (shown in Figure 3) by the burning cooling segment is discharged at first in pH treatment trough 81, for example adds calcium hydroxide (Ca (OH) ₂) wait alkali K, pH is transferred to neutrality after, send in the recycle system of evaporating pot 83 (one-level concentrating unit) by pump 82 as draining B6.

Owing to be roughly normal atmosphere in the pH treatment trough 81,,, change to atmospheric pressure state from high pressure conditions partly waiting the process of delivering to this pH treatment trough 81 from above-mentioned gas washing part and desulfurization regeneration to the draining B5 that wherein sends into.Thus, gases such as the ammonia that a dissolves in part can be fallen in spontaneous evaporation, and this gas is emitted in the gas phase side in pH treatment trough 81, and this gas is discharged by vent fan 81a as discharging gas B7 at this moment, as mentioned above, is blended among the resurgent gases E2 that sends in the roasting kiln 52.

Evaporating pot 83, evaporation process draining B6 is separated into concentrated solution L1 and contain ammonia steam M1, and at this moment, the concentrated solution L1 that is detained the bottom after well heater 85 heating, sprays from top by recycle pump 84 suctions and the draining B6 that newly sends into together.Well heater 85 is heat exchangers, for example, utilizes in the power generation system high-temperature steam D3 that extracts from the part of steam cycle, and circulation fluid is heated to ammonia carries out dissipation as gas temperature.

Equally, the concentrated solution L1 that discharges from the recycle system of evaporating pot 83 is in groove 86 and pump 87 are sent into the solid-liquid separating machine 88 that separates gypsum.By solid-liquid separating machine 88 contained gypsum J3 among the separation concentrated solution L1 selectively.This gypsum J3 is by infeeding the sulfate ion that exists in the draining and the calcium ion that adds in conjunction with forming in pH treatment trough 81 by groove 10 in the gas scrubbing part.Solid-liquid separating machine 88 is vacuum belt filter for example, and the filtrate L2 of suction sends in the filtrate receiver 92 via vacuum chamber 89 and pump 90.

And then the filtrate L2 of filtrate receiver 92 is sent in the pulley type secondary concentrating unit 94 by pump 93 and dewaters, and discharges as mud J4.The solids component that contains solid-liquid separating machine 88 indissociable trickle particle diameters among the mud J4.

By secondary concentrating unit 94 isolating liquid branches, stream side (evaporating pot 83 etc.) is handled before for example being sent to again.

In addition, contain the steam M1 of the ammonia of discharging from evaporating pot 83 tops, at first, be cooled to coagulation temperature by water cooler 95 after, send in the liquid bath 96 that condenses, carry out temporary storage as containing ammonia condensed water (ammoniacal liquor M2).Ammoniacal liquor M2 in this liquid bath 96 that condenses extracts out with pump 97, in heat exchanger 98 is sent into distillation tower 99, is separated into weak ammonia M3 and concentrated liquor M5.

Distillation tower 99 for example is so-called section towers such as bubble-plate column, and above-mentioned ammoniacal liquor M2 infeeds the top of tower behind heat exchanger 98 internal heating, flow downward to contact with the steam M4 that contains high strength ammonia that rises in tower.

The lower concentration weak ammonia M3 that is trapped in these distillation tower 99 bottoms is heated by water vapor D4 in well heater 100, and dissolved gases composition ammonia is to gas side dissipation like this.The steam that contains dissipation ammonia is sent in the concentrated ammonia groove 101 as the steam M5 that contains greater concn ammonia through being located at the backflow part at these distillation tower 99 tops.

So-called herein backflow part, 102 cooling steam M4 generate by water cooler, be stored in the concentrated liquor M5 in the groove 103, infeed the top of distillation tower 99 by pump 104, like this among the steam M4 except that ammonia, steam (for example water vapor) overwhelming majority is liquefied, on the other hand, the most of dissipation of ammonia in the liquid is come out, and obtains the ammoniacal liquor M5 of greater concn.

Water cooler 102 is the heat exchangers that utilize the hollow end tubular structure of heat-eliminating medium G7 cooling steam M4 such as process water.

Be trapped in the lower concentration weak ammonia M3 of distillation tower 99 bottoms, wherein a part is suitably discharged by take-off line 106 by the discharge side of recycle pump 105, after heat exchanger 98 and water cooler 107 coolings, is sent in the diluted ammonia groove 108.

Be stored in the concentrated liquor M5 and the weak ammonia M3 that concentrate in ammonia groove 101 and the diluted ammonia groove 108, can be applied to the denitration processing of above-mentioned roasting kiln 52 back flow processs or the neutralizing treatment of sulphur trioxide, or the denitration in the steam turbine back flow process of gasifying gas generating is handled, perhaps, slurries formation liquid as sulfur dioxide gas absorption tower 61 utilizes, owing to be separated into this condensed water and dilution water, be convenient to the corresponding suitable ammonia concentration that requires and separately use.

The following detailed structure that roasting kiln 52 in the above-mentioned burning water cooler (Fig. 3) is described according to Fig. 6.

Roasting kiln 52, as shown in Figure 6, constitute by body of heater 120 and its attaching device and pipe arrangement pipeline, body of heater 120 has combustion chamber 121, is communicated with side by side with this combustion chamber 121 and loads three heat exchange stream 123a, 123b and the 123c that pottery is made heat storage 122 respectively, 121 top is provided with burner 124 in the combustion chamber.

(for example, LPG) burning together only burns auxiliary fuel N when starting in combustion chamber 121 for air-supplied F2 and auxiliary fuel N when burner 124 starts.

As body of heater 120, specifically can use, for example the roasting kiln of the RTO heat accumulating type deodorization device (RI-3 type) of Cugai Ro Co., Ltd.'s system.

As attaching device and pipe arrangement pipeline, have resurgent gases E2 and air F1 are carried out blended mixing tank 131, utilize these mixing tank 131 blended to handle the water conservancy diversion pipeline 133 that gas P is sent into by fan 132, send into the purge lines 134 of Purge gas Q, the vent line 135 of smoke evacuation E3 is drained in the burning back, divide the pipeline 137 of getting combustion chamber 121 smoke evacuation parts, will be by this pipeline 137 by combustion chamber 121 part smoke evacuation of telling and the E3 blended mixing tank 136 of discharging fume, reclaim the waste heat boiler 138 that heat heating boiler feedwater R produces steam S in the part smoke evacuation that combustion chamber 121 from be located at pipeline 137 is told.

Between line of pipes 133, purge lines 134 and vent line 135 and each heat exchange stream 123a, 123b, 123c, be provided with respectively and open and close valve 141a～141c, 142a～142c, 143a～143c.

These open and close valve 141a～141c, 142a～142c, and 143a～143c controls by order or the program according to the rules of elliptical controller among the figure, to carry out the aftermentioned operation.

Send into part smoke evacuation E3 by elliptical fan among the figure this moment in purge lines 134, this part smoke evacuation E3 utilizes as Purge gas Q.

Below illustrate as an example and in above gas refinishing equipment, implement fine preparation method for gas of the present invention.

At first,,, wash, remove impurity such as muriate in the gas and ammonia generating gas A1 with after generating sulfuration phosphinylidyne among the gas A1 and changing into hydrogen sulfide by washing part shown in Figure 1.

Then, at thionizer shown in Figure 2 21, absorption is removed the absorption liquid that will generate gas A3 and sulfide (hydrogen sulfide) and is carried out sulfide (desulfurization process) contained in the generation gas of gas-to-liquid contact.

Then,, the absorption liquid C1 that has absorbed sulfide in the desulfurization process is heated, discharge the regeneration gas E2 (step for regeneration) that contains sulfide by regenerator column shown in Figure 2 22.

Then,, the resurgent gases E2 that produces in the step for regeneration is fully burnt, change into the smoke evacuation E3 (burning operation) that contains sulfur dioxide gas by the aftermentioned running by Fig. 3 and roasting kiln 52 shown in Figure 6.

Then, in cooling tower shown in Figure 3 53, make smoke evacuation E3 and cooling fluid G1 carry out gas-to-liquid contact, to cool off.

Further,, utilize wet type lime stone-gypsum method, absorb the sulfur dioxide gas among the cooling back smoke evacuation E4, generate by product gypsum (gypsum recovery process) by gypsum recovery part shown in Figure 4.

Partly wait the water of discharging by washing part and desulfurization regeneration, finally compile, handle, reclaim ammonia M3, M5, obtain gypsum J3 by product simultaneously by disintegrating system in waste pipe shown in Figure 5 as draining B5.

In above-mentioned burning operation, by the gas mixture (handling gas P) of burning resurgent gases E2 and air F1 in the combustion chamber 121 of the roasting kiln more than 1000 ℃ 52 (shown in Figure 6), according to above-mentioned reaction formula (1).With the SO that produces ₃Be suppressed at minimum quantity, the hydrogen sulfide (H among the resurgent gases E2 ₂S) almost all change into sulfur dioxide gas (SO ₂).

The following running that the roasting kiln 52 of finishing this burning operation is described with reference to Fig. 7.Among Fig. 7, open and close valve 141a～141c, 142a～142c, among 143a～143c, as shown in the figure, the whole painted blacks of the valve of closing, the valve of breakdown are blank look.

In the roasting kiln 52,,, repeat successively with 60～70 seconds interval respectively with the (a) and (b) among Fig. 7, (c) represented operating state by changing the operating state that respectively opens and closes valve.Reach in the time that is stabilized in 1000 ℃ of design temperatures in the combustion chamber 121 when starting beginning, be blown into LPG and Air mixing gas, form flame 124a by the burner 124 on 121 tops, combustion chamber.Operation to be achieved as follows like this.

Promptly, under state shown in Fig. 7 (a), heat exchange stream 123a constitutes the importing pipeline of mixed regeneration gas E2 and air F1 processing gas P, handle gas P and enter heat exchange stream 123a by opening and closing valve 141a from importing pipeline, after carrying out heat exchange with heat storage 122 among this heat exchange stream 123a, import in the combustion chamber 121.When starting in the transition period that forms standard state, because the heat storage 122 of heat exchange stream 123a is in low temperature, the processing gas P of this importing, fully do not heated in the incendiary process voluntarily with high temperature, when even the concentration of hydrogen sulfide is very low, also can be by the flame 124a of burner 124 in burning more than 1000 ℃.

The heat storage 122 of heat exchange stream 123a, under the previous operating state shown in Fig. 7 (c), owing to heat by the smoke evacuation more than 1000 ℃, so under standard state, in the outside (away from combustion chamber side) is about 300 ℃, and inboard (near combustion chamber side) is about 800 ℃.

Therefore, under standard state, by forming this abundant pyritous heat storage 122, processing gas P by heat exchange stream 123a can be heated to 750 ℃, even concentration of hydrogen sulfide is very low, although stopped the flame 124a of burner 124, handle gas P and also can in combustion chamber 121, burn voluntarily with the temperature more than 1000 ℃.During standard state, when operating state shown in Fig. 7 (a) finishes (before next operating state conversion), the heat storage 122 of heat exchange stream 123a is cooled off by handling gas P on the contrary, this temperature, and the outside is about 200 ℃, the inboard is about 700 ℃.

Under the operating state shown in Fig. 7 (a), heat exchange stream 123c constitutes the importing pipeline of purified gas Q, and heat exchange stream 123b constitutes the escape route of smoke evacuation E3, handle gas P and burn the gas that forms by opening and closing valve 142c, the purified gas Q that flows into from heat exchange stream 123c together, via heat exchange stream 123b, discharge as smoke evacuation E3 from opening and closing valve 143b and vent line 135.

Heat exchange stream 123c, under previous operating state shown in Fig. 7 (c), owing to played the effect that gas P imports pipeline of handling, so can residually handle gas P down in the stream, but under operating state shown in Fig. 7 (a), by purified gas Q this residual processing gas P is sent in the combustion chamber 121, contained hydrogen sulfide burns under the temperature more than 1000 ℃ with importing the hydrogen sulfide of handling the gas P from heat exchange stream 123a.In addition, the heat storage 122 of this heat exchange stream 123c, under previous operating state shown in Fig. 7 (c), owing to handle the cooling performance of gas P, under the standard state, the outside is about 200 ℃, the inboard reaches about 700 ℃, owing to further cool off with the meeting that contacts of purified gas Q, when operating state shown in Fig. 7 (a) finishes, the outside reaches about 180 ℃, and the inboard reaches about 600 ℃.

The heat storage 122 of heat exchange stream 123b under previous operating state shown in Fig. 7 (c), is cooled owing to contacting with purified gas Q, so under standard state, the outside reaches about 180 ℃, the inboard reaches about 680 ℃.Therefore, under operating state shown in Fig. 7 (a), will be cooled to about 300 ℃ by the burning and gas-exhausting E3 of heat exchange stream 123b by this abundant cryogenic heat storage 122.The situation of standard state, when operating state shown in Fig. 7 (a) finished, the heat storage 122 of heat exchange stream 123b was instead heated by smoke evacuation E3, this temperature, the outside is about 300 ℃, the inboard is 800 ℃.

Below, under operating state shown in Fig. 7 (b) and Fig. 7 (c), the running of each above-mentioned shown in Fig. 7 (a) heat exchange stream is converted to the heat exchange stream of adjacent or opposite side, at first, under operating state shown in Fig. 7 (b), the heat exchange stream 123a in left side constitutes the importing pipeline of purified gas Q, and intermediary heat exchange stream 123b constitutes the importing pipeline of handling gas P (resurgent gases E2), the heat exchange stream 123c on right side constitutes the escape route of smoke evacuation E3, carries out identical running.Equally, under the operating state shown in following Fig. 7 (c), the heat exchange stream 123a in left side constitutes the escape route of smoke evacuation E3, intermediary heat exchange stream 123b constitutes the importing pipeline of purified gas Q, the heat exchange stream 123c on right side constitutes the importing pipeline of handling gas P, after still carrying out identical running, return to the operating state shown in Fig. 7 (a) again.

Any one specific heat storage 122 in three heat storages 122 that be provided with this moment, E3 contacts with smoke evacuation, these 122 heated whiles of specific heat storage, other heat storage 122 contacts with the preceding processing gas P that burns, handle the heated operation of gas P, change heat storage 122 successively continuously, heat storage 122 is made medium the most at last, will be by the continuous heating regeneration gas E2 of heat and the air F1 of smoke evacuation E3 recovery, in combustion chamber 121, contained hydrogen sulfide continuous burning under the temperature more than 1000 ℃ among the resurgent gases E2.

Further specify, for example to consider only to have the roasting kiln that has heat exchange with the heat exchanger what is called of the heat heat treated gas of burning and gas-exhausting, but because heat exchange material (pipe or tube sheet or parts etc.) is heated by burning and gas-exhausting, and by handling air cooling but, so must use anti-from 1000 ℃ to normal temperature, this low temperature and the big advanced material of the high temperature temperature difference, its practicality is bad estimation.

On the other hand, heat storage type combustion stove with hot-swap feature of the present invention, because thermal medium, the heating and cooling (recovery of heat) that are heat storage are to carry out separately, so thermal medium is that heat storage is only in 100 ℃～150 ℃ range of temperature, the temperature difference of gas inlet (heating before) and outlet (heating back) suitable greatly, be about 700 ℃.Therefore, the height that thermo-efficiency is suitable under standard state, does not drop into auxiliary fuel N and air F2 such as LPG, can realize the continuous burning under the high temperature more than 1000 ℃.

Stopping to drop under the standard state of auxiliary fuel N, temperature of combustion in the combustion chamber 121, need not anyly operate, the flow by change resurgent gases E2 etc. can change, for example, temperature of combustion when considering this change, when being set in minimum 1000 ℃, when substantially exceeding 1000 ℃, for example, the operations of utilization smoke evacuation flow etc. can remain on about 1000 ℃ to increase the increase that waste heat boiler 138 produces hot yield, inhibition heat storage Heating temperature.Do like this, can keep the said condition of temperature of combustion more than 1000 ℃, the heat resisting temperature (permissible temperature) that constitutes the material of combustion chamber 121 can be controlled at minimum again, thereby avoid the increase of cost.

In this burning operation, temperature of combustion remains on more than 1000 ℃, has the SO that produces by above-mentioned reaction formula (2) ₃Be controlled at the effect of minimum quantity.That is, for example shown in Figure 8 according to inventors' research, SO ₃Generating capacity raise along with temperature of combustion and reduce, and stable gradually, almost do not changing more than 1000 ℃.This tendency, though the concentration of hydrogen sulfide change, the same.Data shown in Fig. 8, concentration of hydrogen sulfide is 14.2% in the processing gas, the oxysulfide (SO in the smoke evacuation _x) concentration is 65000ppm, at this moment, transformation efficiency (SO under 1000 ℃ temperature of combustion ₃/ SO _x), be about 2%, extremely low.

As above-mentioned, according to the gas refinishing equipment or the fine preparation method for gas of this example, remove the sulfide and the various foreign material that generate among the gas A1, obtain very clean processed gas A5, simultaneously, obtain by product gypsum extremely useful in the industry at an easy rate.

And, solved the problem that exists in the above-mentioned relevant burning operation, consider also especially favourable with regard to equipment cost and running cost.

Promptly, even concentration of hydrogen sulfide is very low, at least under standard state, do not drop into auxiliary fuel N and for the burning auxiliary fuel air F2, burning still can be carried out, not only do not need to add auxiliary fuel, nor power such as the pump of needs conveying auxiliary fuel N and air F2 and fan, thereby running cost reduced.

Since do not need to drop into auxiliary fuel N and air F2, thus the flow of smoke evacuation E3 can be reduced, and can reduce the later installed capacity of burning operation significantly, simultaneously, also can reduce the running cost of the later air feed of burning operation with fan and gas blower etc.

In the burning operation of this example, because temperature of combustion is remained on more than 1000 ℃, as previously mentioned, can be with SO ₃Generation be controlled at minimum, also just there is no need implement to improve after the burning operation special measures such as appliance arrangement erosion resistance, with regard to this point, can reduce equipment cost, prevented SO simultaneously reliably ₃Corrosive to device materials is unfavorable.

And, the situation of this example, utilize the recovery of heat amount of adjusting waste heat boiler 138, even the flow of resurgent gases E2 change, by temperature of combustion is fixedly remained on about 1000 ℃, temperature of combustion can be not too high as a result, thereby avoided the so-called unfavorable generation of the combustion chamber 121 component parts losts of life reliably.

The present invention is not limited in above-mentioned form example, and all forms can be arranged.

For example, heat exchange stream and heat storage in the roasting kiln of the present invention are not limited only to three, for example, can be provided with more than four, and each function also can utilize several heat exchange streams and heat storage to carry out stack in time.

Relevant fine preparation method for gas of the present invention in desulfurization process, utilizes absorption liquid to absorb and removes the sulfide that generates in the gas, the processed gas that is purified.Equally, in step for regeneration, discharge and contain the resurgent gases that has absorbed sulfide, this resurgent gases changes into the smoke evacuation that contains sulfur dioxide gas by the burning operation, further in the gypsum recovery process, absorb the sulfur dioxide gas in this smoke evacuation, obtain industrial extremely useful gypsum by product.

And, in above-mentioned burning operation, the specific heat storage of in the heat storage any one with the burning after smoke evacuation contact, to heat this specific heat storage, simultaneously, other heat storage contacts with the preceding above-mentioned resurgent gases of burning, to heat above-mentioned regeneration gas, this operation can be carried out continuously by changing heat storage in turn, heat storage reclaims heat as media from smoke evacuation, with the regeneration gas before the heating flame.

In view of the above, thermal medium, the i.e. heating and cooling of heat storage (recovery of heat), carry out separately, so thermal medium, promptly heat storage only in the range of temperature scope about 150 ℃, the temperature difference between the entrance and exit of heat storage and heat exchange gas is big especially, is about 700 ℃.Therefore, thermo-efficiency is high especially, under standard state, does not drop into auxiliary fuel and combustion airs such as LPG, also can realize continuous burning under the high temperature.

Therefore, solved the problem that exists in the above-mentioned burning operation, considered especially favourable with regard to equipment cost and running cost.

That is, even the concentration of hydrogen sulfide is very low, under standard state, even do not drop into auxiliary fuel and be combustion-supporting air, burning also can be carried out, and neither needs the auxiliary fuel purchase commodity, do not need to carry the power-driven pump and the fan of auxiliary fuel and air again, thereby running cost is minimized.

And, since there is no need to drop into auxiliary fuel and combustion air, thus the smoke evacuation flow after the burning can especially be reduced, and reduce the later installed capacity of burning operation significantly, simultaneously, also can especially reduce the running cost of the later delivering gas of burning operation with fan and gas blower etc.

In fine preparation method for gas of the present invention, when temperature of combustion being remained on more than 1000 ℃, as previously mentioned, can be with SO ₃Generation be controlled at minimum, there is no need to implement to improve the special measure of appliance arrangement erosion resistance after the burning operation, with regard to this point, can reduce equipment cost, simultaneously, can prevent SO reliably again ₃The so-called improper phenomenon of corrosion device takes place.

In gas refinishing equipment of the present invention, in thionizer, absorb the sulfide of removing in the generation gas, the processed gas that is purified with absorption liquid.Equally, in regenerator column, discharge contains resurgent gases, this resurgent gases of having absorbed sulphur compound and changes into the smoke evacuation that contains sulfur dioxide gas by heat-accumulation type hot exchange roasting kiln, further absorbs the sulfur dioxide gas in the smoke evacuation in desulfurizer, obtains industrial utmost point useful byproducts gypsum.

Have a plurality of heat exchange streams that load heat storage respectively that are communicated with side by side as above-mentioned heat-accumulation type hot exchange roasting kiln in the combustion chamber, these heat exchange streams adopt with respect to the combustion chamber and change the structure that resurgent gases imports pipeline or burning back smoke evacuation escape route successively.

Therefore, the heat storage of the heat exchange stream that any one is specific contacts with smoke evacuation, heat this specific heat storage, simultaneously, the heat storage of other heat exchange stream contacts heating regeneration gas, this running with the preceding resurgent gases of burning, by carrying out transition heat exchange stream and heat storage in turn continuously, with heat storage as the regeneration gas of medium before with the heat heating flame that from the back smoke evacuation of burning, reclaims.

In view of the above, because thermal medium is heat storage, independently carry out heating and cooling (recovery of heat), so thermal medium is that heat storage is only in the range of temperature scope about 150 ℃, temperature head between the gas inlet of heat storage and heat exchange and the outlet can be big especially, reaches about 700 ℃.Therefore, thermo-efficiency is high especially, under standard state, does not drop into auxiliary fuel and combustion airs such as LPG, also can realize the continuous burning under the high temperature.

Therefore, solved the problem that relevant above-mentioned roasting kiln exists equally, considered especially favourable with regard to equipment cost and running cost.

Claims (3)

1, a kind of fine preparation method for gas, it is the refining fine preparation method for gas that generates gas by coal and oil gasification gained, comprising utilizing makes generation gas and sulfide absorption liquid carry out gas-to-liquid contact, absorb the desulfurization process of removing institute's sulfur compound in the above-mentioned generation gas, absorbed the absorption liquid of sulfide in the heating desulfurization process, discharge the step for regeneration of sulfur compound resurgent gases, the resurgent gases that produces in the burning step for regeneration, change into the burning operation of the smoke evacuation that contains sulfur dioxide gas, with utilize wet type lime stone-gypsum method to absorb the sulfur dioxide gas that generates in the burning operation in the smoke evacuation, produce the gypsum recovery process of by product gypsum

It is characterized in that for the combustion chamber of carrying out above-mentioned burning operation, a plurality of heat storages are set, in these heat storages, any one specific heat storage contacts with above-mentioned smoke evacuation, heats this specific heat storage, simultaneously, other heat storage and the preceding above-mentioned resurgent gases of above-mentioned resurgent gases Contact Heating of burning carry out this operation continuously by switching heat storage successively, and heat storage is mediated, heat above-mentioned resurgent gases with heat, and carry out above-mentioned burning operation by recovery in the smoke evacuation.

2, according to the fine preparation method for gas of claim 1 record, it is characterized in that in above-mentioned burning operation, the temperature of combustion of resurgent gases is more than 1000 ℃.

3, a kind of gas refinishing equipment, it is the refining gas refinishing equipment that generates gas by coal and oil gasification gained, have by making the absorption liquid that generates gas and sulfide carry out gas-to-liquid contact and absorb the thionizer of removing institute's sulfur compound in the generation gas, absorbed the absorption liquid of sulfide in the heating thionizer, discharge the regenerator column of sulfur compound resurgent gases, the resurgent gases that generates in the burning regenerator column changes into the heat-accumulation type hot exchange roasting kiln that contains the sulfur dioxide gas smoke evacuation, with utilize wet type lime stone-gypsum method to absorb the sulfur dioxide gas that generates in the heat-accumulation type hot exchange roasting kiln in the smoke evacuation, produce the desulfurizer of by product gypsum

It is characterized in that above-mentioned heat-accumulation type hot exchange roasting kiln comprises the combustion chamber, with in this combustion chamber side by side connection load several heat exchange streams of heat storage respectively, the formation of above-mentioned heat exchange stream is can change the importing pipeline of resurgent gases or the escape route of smoke evacuation in turn with respect to the combustion chamber.

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