CN205235725U

CN205235725U - A manufacturing equipment and refinery for making process gas denitrogenation

Info

Publication number: CN205235725U
Application number: CN201520638878.8U
Authority: CN
Inventors: M·特莱夫森; P·莫辛; M·R·尼尔森; T·斯拉比亚克; M·莫勒霍杰; M·利克
Original assignee: Haldor Topsoe AS
Current assignee: Topsoe AS
Priority date: 2014-08-21
Filing date: 2015-08-21
Publication date: 2016-05-18
Anticipated expiration: 2025-08-21

Abstract

The utility model relates to a make the manufacturing equipment of process gas denitrogenation and include manufacturing equipment's refinery. Manufacturing equipment includes NH3 and the H2S's of NOx source and combination source, NOx conversion unit, H2S conversion unit, SO2 conversion unit and is used for the device of sulphuric acid production.

Description

For making process equipment and the refinery of process gas denitrogenation

Technical field

The present invention relates to remove in combination sulphur compound (H from refining waste stream₂S、SO₂、SO₃) and NO_x(NO+NO₂) technique.

Background technology

Refinery practice is usually directed to from crude oil, remove the hetero atom such as nitrogen and sulphur by hydrodenitrogeneration and hydrodesulfurization, wherein makes hydrogen replace the hetero atom (nitrogen and sulphur) in crude oil, produces waste product NH₃And H₂S. These waste products are water miscible, and remove as sour water stream from product.

In order to reduce the impact of this technique on environment, must from sour water stream, remove NH₃And H₂S, it can be undertaken by stripping process, wherein makes the gas of sour water stream be released into gas phase as sour water stripping (SWS) tower gas (sourwaterstrippergas, SWS gas).

But when there being H₂S and do not have NH₃Time, can be by basis (1) by H₂S burning is SO₂And H₂O and be oxidized to subsequently SO₃And extraction H₂SO₄(sulfuric acid) and remove gaseous state H₂S。

H₂S+1.5O₂->SO₂+H₂O+518kJ/moleH₂S(1)

In addition, never containing H₂In the air-flow of S, remove NH₃Known. This can, by decomposing and carry out in flame under controlled condition, make NH₃Be converted into N₂And H₂O。

Conventionally, at NH₃There is lower H₂The burning of S can occur in and cause less desirable NO_xAt the temperature forming, this NO_xIf be present in sulfuric acid, form the nitrosyl sulphuric acid of less desirable highly corrosive and the unacceptable discharge to atmosphere.

Utility model content

But, according to the present invention, determine at H₂S and NH₃Combination exist under, can use NH₃To avoid NO_xClean release because NH₃Can be according to following reaction for NO under catalytically-active materials (SCR catalyst) exists_xSCR (SCR):

4NO+4NH₃+O₂->4N₂+6H₂O+408kJ/moleNO(2)

NO+NO₂+2NH₃->2N₂+3H₂O+758kJ/moleNO(3)

In these techniques, for the NH of above-mentioned reaction₃Be added into process gas in SCR-catalyst upstream; NH₃Conventionally from the tank supply of anhydrous ammonia or the aqueous solution (being generally 25wt%). With comprise NO_xProcess gas mix before by NH₃Evaporation and heating.

SCR technology is ripe, and has preparation and anhydrous NH about SCR catalyst₃、NH₃The aqueous solution and such as other NH of urea₃The production in source and numerous patents of injection.

According to the present invention, use continuous NH₃Source, for example so-called sour water stripping (SWS) tower gas (SWS gas) is as the NH for catalytic reaction₃Source. SWS gas is approximately equimolar NH₃And H₂S and H₂The mixture of O and be waste stream very common in oil plant. H₂S and NH₃Releases such as the hydrotreatment by crude oil and being trapped in water then discharge from so-called sour water stripping (SWS) tower. SWS gas can be used as the stream of continuous generation, makes not need for storing anhydrous NH₃、NH₃The aqueous solution or another NH₃The tank in source. Correspondingly, can reduce equipment cost, avoid NH simultaneously₃The safety problem and the logistical problem that store.

The present invention is particularly suitable for and sulfur process combination, wherein makes to be not used in the de-NO of SCR_x(deNO_x) amount of SWS gas of reaction burns to form SO₂, it is further oxidized to SO₃(it is hydrated), makes the H in SWS gas₂S is converted into coml sulfuric acid. In addition, via NH₃Stream is added into the H of SCR catalyst₂S is converted into sulfuric acid.

The present invention is applicable to contain NH₃Many waste stream, its device context in sulfuric acid plant is produced continuously. Contain NH₃Waste stream whether can be as the NH of SCR reactor₃The definite composition of gas is depended in source, and must evaluate the chemical side reactions of the component in waste stream and discharge limit, and considers for being inflammable and having a potential volatile NH₃And H₂The correct processing of S.

As used herein, the bed of term catalyst area, catalytically-active materials and catalytic bed should be construed as and to be equal to.

As used herein, catalytically-active materials can be the catalyst of any form and shape, includes but not limited to catalyst pellet, the catalyst of extruding, entirety (monolithic) catalyst and catalysis hardware.

As used herein, the dew-point temperature of component is the temperature that this component starts condensation from admixture of gas. Dew-point temperature depends on pressure and the composition of admixture of gas. Term " more than dew point " is construed as the uncondensable temperature of admixture of gas, and similar " below dew point " is construed as the temperature of admixture of gas (part) condensation.

As used herein, term fluid communication is construed as any substantial uncrossed connection between two process components, include but not limited to via pipe, via the connection of the same side of heat exchanger, but do not comprise the connection of the reactor of filling by catalyst.

Hereinafter, the Nm of unit³Be construed as standard cubic meter, that is, and the occupied volume of amount of gas under 0 DEG C and 1atm.

In the time that concentration is explained with % or vol%, this is construed as volume % (being the molar percentage of gas). Similarly, ppmv is construed as each volume parts of 1,000,000 parts.

Use word upstream and downstream according to the relative position in the direction technique flowing in routine operation. The connection between processing step do not given in this word, because may also there is middle process step.

In wide in range embodiment, the present invention relates to a kind of process equipment, it comprises NO_xThe NH of source and combination₃And H₂The source of S; NO_xConversion unit, it comprises for making NO_xSCR is to N₂There is catalytic activity and for making H₂S is oxidized to SO₂The optional activated material of tool; H₂S conversion unit, it comprises for making H₂S is oxidized to SO₂There is the material of catalytic activity, if NO_xConversion unit is for making H₂S is oxidized to SO₂Activated, described H₂S conversion unit is optional; SO₂Conversion unit, it comprises for making sulfur dioxide catalytic oxidation have the material of catalytic activity; Described reaction member has one or more entrances and one or more outlet; With the device for gas washing in SA production, it has process gas entrance, process gas outlet and concentrated sulfuric acid outlet; Wherein said NO_xSource and NO_xThe entrance of conversion unit is fluid communication; The NH of wherein said combination₃And H₂The source of S and H₂The entrance of S conversion unit is fluid communication, if or omission H₂S conversion unit with NO_xThe entrance of conversion unit is fluid communication; If wherein do not omit described H₂S conversion unit, described H₂The outlet of S conversion unit and described NO_xThe entrance of conversion unit is fluid communication; Wherein said NO_xThe outlet of conversion unit and SO₂The entrance of conversion unit is fluid communication; Wherein SO₂The outlet of conversion unit is fluid communication with the process gas entrance of the device for gas washing in SA production, the process gas outlet that is used for the device of gas washing in SA production is fluid communication with waste line, and the sulfuric acid outlet for the device of gas washing in SA production is set to extract (withdrawal) sulfuric acid, and relevant benefit is: such process equipment provides the NO of Environmental security under the outside supply of minimized chemicals_x、NH₃And H₂The removal of S and the associated production of sulfuric acid.

In further embodiment, this process equipment also comprises the burner in the source with one or more entrance and exits and oxygen rich gas, the NH of wherein said combination₃And H₂The stream that it is fluid communication that the source of S is split as with burner inlet and the stream that is fluid communication with pre-inversion unit, comprise NO described in the outlet stream of wherein said burner forms_xAt least a portion of stream, relevant benefit is: such process equipment provides the NO of Energy Efficient_x、NH₃And H₂The removal of S.

In further embodiment, this process equipment comprises carrier gas source and hybrid element, optionally comprises and mixes intensifier (feature), has two entrance and exits, the NH of wherein said combination₃And H₂An entrance of the stream of S and hybrid element is fluid communication, and another entrance of carrier gas source and hybrid element is fluid communication, and the outlet of hybrid element and NO_xConversion unit or H₂S conversion unit is fluid communication, makes to guide to NO_xConversion unit or H₂The NH of the combination of S conversion unit₃And H₂The stream of S is diluted, and relevant benefit is: the NH of carrier gases dilute combination₃And H₂S stream and reduction are used the technique risk of sour water stripping (SWS) tower gas.

In further embodiment, process equipment comprises H₂S conversion unit, and the NH of diluted combination₃And H₂The stream of S and H₂The entrance of S conversion unit is fluid communication, and H₂The outlet of S conversion unit and NO_xThe entrance of conversion unit is fluid communication, and relevant benefit is: always self-selectively Reduction of NO_xH₂In the exothermic oxidation of S, separate the heat discharging.

In further embodiment, this process equipment also comprises the heat exchanger being set to for heating first-class and cooling second, wherein said first-class be the NH combining₃And H₂The NH of stream, carrier gas stream or the diluted combination of S₃And H₂Any one in the stream of S, and described second is hot process flow, for example, from NO_xThe outlet stream of conversion unit or from H₂The outlet stream of S conversion unit, relevant benefit is: the more process equipment of Energy Efficient is provided.

In further embodiment, device for gas washing in SA production is condensation of sulfuric acid device, this condensation of sulfuric acid utensil has process gas entrance, process gas outlet, cooling medium entrance, cooling medium outlet and concentrated sulfuric acid outlet, cooling medium entrance and cooling medium source are fluid communication, and relevant benefit is: passing through oxidation NH₃And H₂Technique with Energy Efficient under the existence of the water that S forms provides sulfuric acid.

In further embodiment, cooling medium source is atmospheric air, and cooling medium outlet be set to supply any one or its in oxygen rich air body source and carrier gas both, relevant benefit is: provide to the heat energy of burner or due to the SO of heat exchanger₂Condensation in side and reduce corrosion risk.

In further embodiment, be SO for the device of gas washing in SA production₃Absorber, this SO₃Absorber has process gas entrance, process gas outlet, concentrated sulfuric acid entrance and the further outlet of concentrated sulfuric acid, the entrance and the concentrated sulfuric acid source that wherein absorb sulfuric acid are fluid communication, and relevant benefit is: such technique avoids using corrosion resistance condenser.

Another aspect of the present invention relates to a kind of refinery, and it comprises process equipment as above and sour water stripping (SWS) tower, and this sour water stripping (SWS) tower has the NH that forms described combination₃And H₂The outlet of the sour water stripping (SWS) tower gas in the source of S, relevant benefit is: such refinery has effectively and the processing of Environmental security for less desirable waste gas in producing sulfuric acid.

In wide in range embodiment, the present invention relates to from comprising NO_x、NH₃And H₂The combination of the process gas of S provides the method for purified process gas, said method comprising the steps of:

A. provide and comprise NO_xProcess gas,

B. provide and comprise NH₃Selective reduction agent gas and by described process gas and described selective reduction agent combination of gases,

C. described process gas and described selective reduction agent gas group are synthesized to the gas for purifying, in described process gas and described selective reduction agent gas, at least one comprises H₂S and at least one comprise O₂，

D. make the described gas for purifying under the technological temperature of at least 250 DEG C for making NO_xIt is lower and to making H that the material that SCR has a catalytic activity exists₂There is lower reaction in the material that S oxidation has catalytic activity,

E. extract the NO that contains lower concentration than the combination of gas_xPurified process gas.

Provide continuously the associated benefits of selective reduction agent gas to be: the method avoids storing the demand of ammonia, provides simultaneously and does not basically contain H₂S and NO_xOr its concentration is reduced at least 50%, 80% or 95% purified gas.

In further embodiment, with respect to NH₄HSO₄(NH₄)₂SO₄, the technological temperature under each described method step is that relevant benefit is higher than at least 20 DEG C of dew points that are present in the gas under described method step: avoid the NH that is cured₄HSO₄(NH₄)₂SO₄Block the risk of the passage of for example integer catalyzer.

In further embodiment, process gas comprises the product that burns sour water stripping (SWS) tower gas, and relevant benefit is: the burning of this sour water stripping (SWS) tower gas provides energy and in oil plant, removes the Potential feasibility of waste product.

In further embodiment, selective reduction agent gas comprises sour water stripping (SWS) tower gas, and relevant benefit is: this sour water stripping (SWS) tower gas is that appearance is facile in refinery processes.

In further embodiment, the method comprises the step that described selective reduction agent gas is provided, and this is by being incorporated into lower than the composition of the LEL at least 2 at the temperature of described method step or 4 times and diluting and comprise NH with carrier gas₃Gas as sour water stripping (SWS) tower gas, relevant benefit is: reduced the technique risk that uses described sour water stripping (SWS) tower gas.

In further embodiment, H in sour water stripping (SWS) tower gas₂S and NH₃Ratio be 0.5 to 2, the associated benefits of this sour water stripping (SWS) tower gas is: balance exist H₂S and NH₃。

In further embodiment, the described material that selective reduction is had to catalytic activity is for H₂S oxidation also has activity, and relevant benefit is: can use identical catalytically-active materials to remove H₂S and NO_x。

In further embodiment, the described material that selective reduction is had to a catalytic activity comprises one or more oxides of the metal of taking from the vanadium on carrier, chromium, tungsten, molybdenum, cerium, niobium, manganese and copper, this carrier comprises one or more oxides of the metal of taking from aluminium, silicon and titanium, and relevant benefit is: described material is effectively for catalytic oxidation hydrogen sulfide at low temperatures and is activated for SCR.

In further embodiment, make described selective reduction agent gas described step (c) before with for H₂S oxidation has the material contact of catalytic activity, and relevant benefit is: pass through H₂The heat of oxidation of S makes selective reduction agent gas-heated, makes without adding energy in the situation that temperature more than temperature required.

In further embodiment, the SO in described purified process gas₂Under the existence of material for the oxidation of sulphur or sulfur dioxide with catalytic activity, be oxidized to SO₃So that the process gas of oxidation to be provided, this material with catalytic activity for example comprises and is supported in SiO₂The V promoting on carrier material and by the alkali metal such as K, Na and/or Cs₂O₅Material, relevant benefit is: the process gas of oxidation is provided, and it is suitable for being directed to sulfuric acid production process before being disposed to atmosphere.

In further embodiment, described purified process gas was cooled before contacting the material for the oxidation of sulphur or sulfur dioxide with catalytic activity, and relevant benefit is: due to lower temperature, provide for the equilibrium-limited still less transforming.

In further embodiment, described cooling be by with selective reduction agent gas, sour water stripping (SWS) tower gas and carrier gas in one or more heat exchange carry out, relevant benefit is to provide preheating of described gas, it reduces the NH from SWS gas₃With SO₃Reaction is to form the risk of ammonium hydrogen sulfate (ABS), and ammonium hydrogen sulfate can solidify on the injection nozzle for SWS gas, and causes the obstruction on catalyst or solidify and obstruction flowing and/or path to avtive spot.

Another aspect of the present invention relates to the method for producing the concentrated sulfuric acid, and it comprises SO₂To SO₃Described oxidation, and SO₃To H₂SO₄Hydration and H₂SO₄Cooling and condensation or at H₂SO₄Middle absorption SO₃In any processing step, relevant benefit is to provide for making one or more waste gas streams be converted into the technique of purified gas and the coml concentrated sulfuric acid.

As mentioned, the present invention relates to for merging and remove NO from process gas_x、NH₃And H₂The technique of S. Contain NH₃And H₂The major part of the SWS gas of S is burned, has given NO to provide_xThe load of concentration has SO₂Process gas. Most of NH in SWS gas₃Be thermal decomposited as N₂And H₂O, but according to burning condition (as temperature, local O₂Concentration, fractional combustion), can form the NO of the highest thousands of ppm_x. As the rule of thumb, the NO of 95% left and right_xTo be NO, remaining 5% will be NO₂。

NO in the gas of burning_xConcentration determines, by being directed to the amount of SWS gas of SCR catalyst, to make to realize desired NH at SCR catalyst place₃With NO_xRatio.

NO_xRemoval by making NO_xWith so-called selective reduction agent as NH₃Or NH₃Precursors reaction and be N by its SCR (SCR)₂And obtain. This needs NH₃Or another selective reduction agent, and to NO_xSelective reduction there is the existence of the material of catalytic activity.

Normally overall structure of SCR catalyst, wherein catalytically-active materials is to have WO₃/TiO₂As the V of carrier and promoter₂O₅, but can comprise one or more oxides of the metal of taking from the vanadium on carrier, chromium, tungsten, molybdenum, cerium, niobium, manganese and copper, one or more oxides that this carrier comprises the metal of taking from aluminium, silicon and titanium. Except well-known SCR reaction (1+2), under the existence of such catalytically-active materials, H₂S is also oxidized to SO via reaction (3)₂, as shown in european patent application 13/195222.

Due to V in SCR catalyst₂O₅Existence, be present in a small amount of SO in gas₂To be oxidized to SO₃。

Importantly, NH in process gas₃With NO_xRatio be uniform; Otherwise SCR reaction will be not reductive NO completely_x(there is low NH₃With NO_xThe process gas volume of ratio in) maybe will have a large amount of NH₃Overflow and (there is high NH from catalyst₃With NO_xThe process gas volume of ratio).

The purified process gas that leaves SCR catalyst contains SO₂(before gas can be discharged into atmosphere, must be removed), but only contain the very NO of low concentration_x。SO₂Removal can be by being oxidized to SO₃And form and remove sulfuric acid and carrying out. For SO₂The typical material that oxidation has catalytic activity is to load on the V promoting on silica support materials and by the alkali metal such as K, Na and/or Cs₂O₅. This SO₂Oxidation catalyst is by H₂S chemistry inactivation, therefore, it is essential that SCR catalyst is for making H₂S is oxidized to SO₂Be activated, make leading to SO₂The porch of oxidation reactor does not almost have H₂S exists.

Contain oxygen and form explosive mixture with the process gas of the diluent air (carrier gas) for SWS gas together with SWS gas, this must be avoided. In practice, SWS gas be diluted to LEL (LEL) 25% to 50% between, this LEL can be by well known to a person skilled in the art that LeChateliers mixing rule calculates from the LEL of pure component.

In addition, by SWS gas is mixed to the hot surface that makes SWS gas be kept away from carrier gas heater with carrier gas in heater downstream, can reduce the risk of blast, because H₂S can be oxidized and cause gas superheat on hot metal surface.

Because process gas contains SO₃So, there is the NH from SWS gas₃Can with SO₃Reaction is to form the risk of ammonium hydrogen sulfate, and it can solidify and cause obstruction on the nozzle for SWS gas. ABS also can condensation in the hole of SCR catalyst/solidifies, make catalysqt deactivation. The reaction that forms ABS is

NH₃+SO₃+H₂O<->NH₄HSO₄(g)<->NH₄HSO₄(s)(4)

Body phase dew point (bulkdewpoint) temperature of ABS (guide to SCR and from the dew point in the process gas of SCR) depends on the composition of gas, but it can be 200 to 350 DEG C conventionally, and all associated temperature must be kept above this and limit to avoid curing. In Fig. 1 and Fig. 2, provide ABS body phase dew-point temperature, SO₃Concentration and NH₃Relation between concentrated. In gas, contain the H of 10vol%₂Under O and atmospheric pressure, calculate all curves. Due to capillarity, in the pore structure of SCR catalyst by than body mutually in the temperature of high about 20 DEG C to issue raw food solidifying, this depends on the pore-size distribution of catalyst.

Therefore, according to the present invention in order to be provided for removing NO_x、H₂S and NH₃Successful operating procedure, expect balance many factors; Temperature must be applicable to occurring SCR reaction, and SCR is reacted to the material with catalytic activity for H₂S oxidation also must have activity, and more than temperature and process gas composition must guarantee to operate in the dew-point temperature of ABS formation, and the SWS gas composition of dilution must be safe aspect blast restriction.

Brief description of the drawings

Fig. 1 is illustrated in low SO₃Ammonium hydrogen sulfate dew point under concentration.

Fig. 2 is illustrated in higher SO₃Ammonium hydrogen sulfate dew point under concentration.

Fig. 3 illustrates the application's embodiment, wherein SO₂And NO_xBe converted.

Fig. 4 illustrates according to the sulphuric acid device of the application's embodiment.

Fig. 5 illustrates according to the sulphuric acid device of the application's embodiment, and its heat being suitable in SCR reactor wherein discharges high situation.

Fig. 6 illustrates according to the sulphuric acid device of the application's embodiment, and it is suitable for the wherein very important situation of capital cost.

Fig. 7 illustrates according to the sulphuric acid device of the application's embodiment, and it is suitable for the wherein high situation of feed variation.

The numeral relating in figure

Carrier gas line (2)

Heater (4)

The carrier gas line (2) of preheating

SWS gas line (8)

Static mixing device (10)

Selective reduction agent gas line (12)

For the process gas pipeline (14) of purifying

Mixing arrangement (16)

Group technology gas line (18)

There is the reactor (20) of SCR catalyst

Purified process gas pipeline (22).

Oxygen or air line (26)

SWS gas line (28)

Feeding line (29)

Burner (30)

Process gas pipeline (32)

Waste heat boiler (34).

Selective reduction agent gas line (38)

Carrier gas line (40)

Heater (42)

Gas/gas-heat exchanger (43)

The carrier gas line (44) of preheating

Static mixing device (46)

The H of heat₂The SWS gas (47) of the dilution that S exhausts

The SWS gas line (48) of the dilution of heat

H₂S oxidation reactor (49)

Load has SO₂Process gas pipeline (36)

Composition gas pipeline (50)

H₂The SWS gas (51) of the dilution that S exhausts

Static mixing device (52)

For the gas line (54) of purifying

There is the reactor (56) of SCR catalyst

Process gas pipeline (58)

Input process gas (59)

SO₂Oxidation reactor (60)

Catalyst bed (62,66)

The outlet (63) of the first catalyst bed

Heat exchanger (64,68)

Through the process gas pipeline (70) transforming

Condensation of sulfuric acid device (72)

Concentrated sulfuric acid pipeline (76)

Cleaning procedure gas line (74)

Atmospheric air feeding line (78)

The air line (80) of preheating

Detailed description of the invention

In Fig. 3, the carrier gas (2) of preheating in heater (4) mixes with SWS gas (8), and selective reduction agent gas (12) is provided. Heater (4) is for example electric heater or common charging-effluent heat exchanger. Carrier gas is generally atmospheric air, but can be also such as N of inert gas₂、CO₂Or from the recirculating process gas of downstream sulphuric acid device, but that it must have is enough for SCR technique and H₂The oxygen of S oxidation. For guaranteeing the mixing completely of two streams, make admixture of gas through static mixing device (10). Selective reduction agent gas (12) is then added into the NO that comprises for purifying of high flow rate_xProcess gas (14). In order to ensure the mixing completely of these two streams, should use mixing arrangement (16), it is static mixer or injection grille. Then the process gas (18) of combination enters the reactor (20) that is mounted with SCR catalyst, and above-mentioned SCR reaction and H occur on this catalyst₂The oxidation of S, provides purified process gas (22).

In Fig. 4, sulphuric acid device and use SWS gas are as NH₃The SCR combination of reactors in source. SWS gas (28) from oil plant is introduced into sulphuric acid device; The major part of stream is directed to burner (30) via pipeline (29), and part is walked around burner via pipeline (38) simultaneously. For the oxygen that is applied to burning, in most cases use air via pipeline (26). If feasible, air can preheating, for example, from the hot cooling-air (80) of sulphuric acid device. Contain sulphur compound as H₂S、COS、CS₂And/or other feed gas of elementary sulfur can be supplied to burner (30) via pipeline (24). In combustion chamber (30), all sulphur compounds are converted into SO₂, sub-fraction (being conventionally less than 2%) is wherein further oxided into SO₃, and most NH₃Be thermal decomposited into N₂And H₂O, but depend on the condition in combustion chamber, can form the NO of the highest thousands of ppmv_x. Common 95% NO_xBe NO, all the other are NO₂。

The temperature of leaving the process gas of burner via pipeline (32) is 950 DEG C to 1200 DEG C, and in waste heat boiler (34), is cooled to 350 DEG C to 450 DEG C.

The bypass SWS gas that forms selective reduction agent gas mixes with carrier gas (44) via pipeline (38), normally air of this carrier gas, if but can obtain excess of oxygen from other source, this carrier gas can be also for example N₂、CO₂Or from the recirculating process gas of sulphuric acid device. Before mixing with SWS gas (38), carrier gas (40) can preheating in heater (42), and this heater can be electric heater or common charging/effluent (gas/gas) heat exchanger. For little flow velocity, electric heater will be most economical scheme.

In order to strengthen the mixing of two streams, make the stream mixing through static mixing device (46). The diluted SWS gas (48) of heat is added into load and has SO₂Process gas (36), and the gas (50) of combination is guided to static mixing device (52), make to realize uniform NH in the gas (54) that enters the reactor (56) with SCR catalyst₃With NO_xRatio. Alternative static mixer by several for by the injection grille forming to the nozzle of process gas pipe through dilution SWS gas feed. On SCR catalyst, NO_xBe reduced into N₂And H₂S is oxidized to SO₂. Then process gas (58) enters SO₂Oxidation reactor (60), it is by heat exchanger (64, the 68) composition between one or several catalyst bed (62,66) and catalyst bed, and this heat exchanger is for being cooled to best catalyst operating temperature by process gas. Between catalyst bed and bed, the number of heat exchanger depends on and leads to SO₂The SO of the porch of reactor₂Concentration and desired SO₂Transformation efficiency, uses 1 to 3 catalyst bed and heat exchanger conventionally.

Enter condensation of sulfuric acid device (72), wherein SO through the process gas (70) transforming₃Be combined to form sulfuric acid vapor with steam. Then steam be condensed into the concentrated sulfuric acid, and it extracts via pipeline (76), and clean process gas leaves to be discharged in atmosphere via pipeline (74). Conventionally use atmospheric air as the cooling medium in condensation of sulfuric acid device (72); It enters via pipeline (78) and leaves via pipeline (80). Can be used as the carrier gas in combustion air and the pipeline (40) in pipeline (26) from the hot-air of condensation of sulfuric acid device.

At NO_xDense and need in the situation of very high NO transformation efficiency, it can be useful carrying out denitrogenation with two steps, that is, and and with two catalyst beds and two diluted SWS co-feeding gas points.

In Fig. 5, in useful process schematic representation, sulphuric acid device and use SWS gas are as NH₃The SCR combination of reactors in source, the in the situation that especially in SCR reactor, heat release being very high. SWS gas (28) from oil plant is introduced into sulphuric acid device; The major part of stream is directed to burner (30) via pipeline (29), and part is walked around burner via pipeline (38) simultaneously. For the oxygen that is applied to burning, in most cases use air via pipeline (26). If feasible, air can preheating, for example, from the hot cooling-air (80) of sulphuric acid device. Contain sulphur compound as H₂S、COS、CS₂And/or other feed gas of elementary sulfur can be supplied to burner (30) via pipeline (24). In combustion chamber (30), all sulphur compounds are converted into SO₂, sub-fraction (being conventionally less than 2%) is wherein further oxided into SO₃, and most NH₃Be thermal decomposited into N₂And H₂O. Depend on the condition in combustion chamber, can form the NO of the highest thousands of ppmv_x. Common 95% NO_xBe NO, all the other are NO₂。

The temperature of leaving the process gas of burner via pipeline (32) is 950 DEG C to 1200 DEG C, and in waste heat boiler (34), is cooled to 350 to 450 DEG C.

The bypass SWS gas that forms selective reduction agent gas mixes with carrier gas (44) via pipeline (38), normally air of this carrier gas, if but can obtain excess of oxygen from other source, this carrier gas can be also for example N₂、CO₂Or from the recirculating process gas of sulphuric acid device. Before mixing with SWS gas (38), carrier gas (40) can be by the process gas in gas/gas-heat exchanger (58) preheating. In another embodiment, carrier gas can be heated by carrying out heat exchange with the process gas that for example leaves burner via pipeline (32) or (36).

In order to strengthen the mixing of two streams, the stream of mixing can pass through static mixing device (46). Diluted SWS gas (48) is added into load and has SO₂Process gas (36), and the gas (50) of combination is guided to static mixing device (52), make to realize uniform NH in the gas (54) that enters the reactor (56) with SCR catalyst₃With NO_xRatio. Alternative static mixer by several injection grilles for diluted SWS gas feed is formed to the nozzle of process gas pipe. On SCR catalyst, NO_xBe reduced into N₂And H₂S is oxidized to SO₂. If H₂S's is dense, and in gas/gas-heat exchanger, (43) middle cool process gas (58) then sets it as input process gas (59) and guides to SO₂Oxidation reactor (60) can be useful, this SO₂Oxidation reactor (60) is by heat exchanger (64, the 68) composition between one or several catalyst bed (62,66) and catalyst bed, and this heat exchanger is for being cooled to best catalyst operating temperature by process gas. Between catalyst bed and bed, the number of heat exchanger depends on and leads to SO₂The SO of the porch of reactor₂Concentration and desired SO₂Transformation efficiency, uses 1 to 3 catalyst bed and heat exchanger conventionally. SO is observed in exit in the first catalyst bed (63)₂The maximum temperature of oxidation reaction, and for the risk of mitigate corrosion, this temperature remains lower than 550 DEG C.

Enter condensation of sulfuric acid device (72), wherein SO through the process gas (70) transforming₃Be combined to form sulfuric acid vapor with water vapour. Then steam be condensed into the concentrated sulfuric acid, and it extracts via pipeline (76), and clean process gas leaves to be discharged in atmosphere via pipeline (74). Conventionally use atmospheric air as the cooling medium in condensation of sulfuric acid device (72); It enters via pipeline (78) and leaves via pipeline (80). Can be used as the carrier gas in combustion air and the pipeline (40) in pipeline (26) from the hot-air of condensation of sulfuric acid device.

In Fig. 6, in process schematic representation, sulphuric acid device and use SWS gas are as NH₃The SCR combination of reactors in source, the capital cost that it does not need expensive gas/gas-heat exchanger and therefore has minimizing. SWS gas (28) from oil plant is introduced into sulphuric acid device; The major part of stream is directed to burner (30) via pipeline (29), and part is walked around burner via pipeline (38) simultaneously. For the oxygen that is applied to burning, in most cases use air via pipeline (26). If feasible, air can preheating, for example, from the hot cooling-air (80) of sulphuric acid device. Contain sulphur compound as H₂S、COS、CS₂And/or other feed gas of elementary sulfur can be supplied to burner (30) via pipeline (24). In combustion chamber (30), all sulphur compounds are converted into SO₂, sub-fraction (being conventionally less than 2%) is wherein further oxided into SO₃, and most NH₃Be thermal decomposited into N₂And H₂O, but depend on the condition in combustion chamber, can form the NO of the highest thousands of ppmv_x. Common 95% NO_xBe NO, all the other are NO₂。

The bypass SWS gas that forms selective reduction agent gas mixes with carrier gas (40) via pipeline (38), normally air of this carrier gas, if but can obtain excess of oxygen from other source, this carrier gas can be also for example N₂、CO₂Or from the recirculating process gas of sulphuric acid device.

In order to strengthen the mixing of two streams, the stream of mixing can pass through static mixing device (46). The diluted SWS gas (48) of heat is guided to H₂S oxidation reactor (49) (it can be also SCR reactor) forms H₂The diluted SWS gas (51) that S exhausts, being then added into load has SO₂Process gas (36), and the gas (50) of combination is directed to static mixing device (52), makes to realize uniform NH in the gas (54) that enters the reactor (56) with SCR catalyst₃With NO_xRatio.

Alternative static mixer by several injection grilles for diluted SWS gas feed is formed to the nozzle of process gas pipe. On SCR catalyst, NO_xBe reduced into N₂And H₂S is oxidized to SO₂. Process gas (58) then enters SO₂Oxidation reactor (60), this SO₂Oxidation reactor (60) is by heat exchanger (64, the 68) composition between one or several catalyst bed (62,66) and catalyst bed, and this heat exchanger is for being cooled to best catalyst operating temperature by process gas. Between catalyst bed and bed, the number of heat exchanger depends on and leads to SO₂The SO of the porch of reactor₂Concentration and desired SO₂Transformation efficiency, uses 1 to 3 catalyst bed and heat exchanger conventionally. SO is observed in exit in the first catalyst bed (63)₂The maximum temperature of oxidation reaction, and for the risk of mitigate corrosion, this temperature remains lower than 550 DEG C.

In Fig. 6, disclosed process schematic representation is especially useful, and wherein technique is well controlled, because require to keep condition (temperature and the SO in (49)₃Concentration), make temperature more than ABS dew point.

In Fig. 7, sulphuric acid device and use SWS gas are as NH₃The SCR combination of reactors in source. SWS gas (28) from oil plant is introduced into sulphuric acid device; The major part of stream is directed to burner (30) via pipeline (29), and part is walked around burner via pipeline (38) simultaneously. For the oxygen that is applied to burning, in most cases use air via pipeline (26). If feasible, air can preheating, for example, from the hot cooling-air (80) of sulphuric acid device. Contain sulphur compound as H₂S、COS、CS₂And/or other feed gas of elementary sulfur can be supplied to burner (30) via pipeline (24). In combustion chamber (30), all sulphur compounds are converted into SO₂, sub-fraction (being conventionally less than 2%) is wherein further oxided into SO₃, most NH₃Be thermal decomposited into N₂And H₂O, but depend on the condition in combustion chamber, can form the NO of the highest thousands of ppmv_x. Common 95% NO_xBe NO, all the other are NO₂。

The bypass SWS gas that forms selective reduction agent gas mixes with carrier gas (44) via pipeline (38), normally air of this carrier gas, if but can obtain excess of oxygen from other source, this carrier gas can be also for example N₂、CO₂Or from the recirculating process gas of sulphuric acid device.

In order to strengthen the mixing of two streams, the stream of mixing can pass through static mixing device (46). Diluted SWS gas (48) is heated in gas/gas-heat exchanger (90) and guide to H₂S oxidation reactor (49) (it can be also SCR reactor), wherein H₂S is oxidized, and this reaction is heat release. The hot H obtaining₂The diluted SWS gas (47) that S exhausts is used to heat diluted SWS gas (48), cooling H₂Then the diluted SWS gas (51) that S exhausts be added into load SO₂Process gas (36), and the gas (50) of combination is directed to static mixing device (52), makes to realize uniform NH in the gas (54) that enters the reactor (56) with SCR catalyst₃With NO_xRatio.

Alternative static mixer by several injection grilles for diluted SWS gas feed is formed to the nozzle of process gas pipe. On SCR catalyst, NO_xBe reduced into N₂And H₂S is oxidized to SO₂. Then process gas (58) enters SO₂Oxidation reactor (60), this SO₂Oxidation reactor (60) is by heat exchanger (64, the 68) composition between one or several catalyst bed (62,66) and catalyst bed, and this heat exchanger is for being cooled to best catalyst operating temperature by process gas. Between catalyst bed and bed, the number of heat exchanger depends on and leads to SO₂The SO of the porch of reactor₂Concentration and desired SO₂Transformation efficiency, uses 1 to 3 catalyst bed and heat exchanger conventionally. SO is observed in exit in the first catalyst bed (63)₂The maximum temperature of oxidation reaction, and for the risk of mitigate corrosion, this temperature remains lower than 550 DEG C.

In Fig. 7, disclosed process schematic representation is especially useful, and wherein owing to operating under dew point, technique is controlled is not so good. But it is owing to needing gas/gas-heat exchanger to relate to extra capital cost.

Embodiment 1

Use in the present embodiment SWS gas as NH₃Flue gas is processed in source in SCR reactor. NO concentration in flue gas is that 300ppmv and needed NO removal efficiency are 92%. In table 1, provide gas flow and composition for related streams, number with reference to figure 3 for stream.

Flue gas can be from the burning of fuel with low sulfur content. Directly extract SWS gas from sour water stripping (SWS) tower unit, the SWS gas part that is not used as the selective reduction agent of SCR reaction can be in another process equipment, for example, in Claus type sulphur forming unit or another H₂S/NH₃In separative element.

Carrier gas is carried out to preheating before mixing with SWS gas or before being added into a large amount of flue gas streams.

SCR reacts (2 and 3) and H₂The oxidation reaction (1) of S is heat release, and the heat discharging raises 8 DEG C the temperature of flue gas. H₂The oxidation of S on SCR catalyst makes SO₂Concentration is increased to 463ppmv from 193ppmv, and this is most possibly considered to too high for being directly discharged into atmosphere.

Table 1

Embodiment 2

In the present embodiment, require to remove 95% NO from the flue gas of the burning of for example high-sulfur combustor. High NO_xRemoval efficiency requires NH₃/NO_xRatio be 1.05, that is, will have in this case NH₃Superfluous. NO relative concentration in flue gas is higher. SCR reacts in the burned situation of unwanted SWS gas and can have high like this concentration therein; NH₃Burning can significantly improve NO_xConcentration. Compared with embodiment 1, NH₃And SO₃The increase of concentration has improved ABS dew-point temperature and has therefore raise for diluted SWS gas required minimum temperature and the effluent gas temperature of going to SCR.

For keep below diluted SWS gas LEL 25%, be necessary to SWS co-feeding gas 8,305Nm³The air of/h. After mixing with flue gas, body phase (bulk) (in gas phase) ABS dew-point temperature is 304 DEG C; For safety, selecting the temperature of diluted SWS gas is 330 DEG C.

ABS dew-point temperature in SCR catalyst pores is calculated as 329 DEG C, therefore at the effluent gas temperature of 357 DEG C of porch that leads to SCR catalyst far above ABS condensation and solidification temperature, this is necessary, because hole is stopped up and will be made SCR catalysqt deactivation by liquid or solid ABS.

On SCR catalyst, will both there is SCR reaction H will also occur₂S oxidation. SCR reaction and H₂The reaction enthalpy of S oxidation makes effluent gas temperature improve 23 DEG C. The NO of this temperature rising and required removal_xPpmv number be directly proportional. Purified gas vent from SCR catalyst can still contain some NH₃And SO₃, this means for ABS condensation and should take preventive measures. All H₂S is all oxidized to SO₂, make SO₂Concentration is increased to 2990ppmv from 2260ppmv. Be with or without the NH for SCR reactor by SWS gas₃In two kinds of situations in source, high SO in flue gas₂Concentration requirement was being carried out desulfurized step by gas discharging before atmosphere.

Table 2

Embodiment 3

In this embodiment, with being equipped with the wet type sulphuric acid device of SCR reactor to process from 10 of oil plant, 000Nm³The SWS gas of/h. Except SWS stream, also in sulphuric acid device, process the concentrated H from oil plant₂S gas.

Most important flow velocity and the composition of in table 3, collecting stream, the identification of numbering for stream is with reference to figure 4.

In burner, concentrated H₂S gas and most of SWS be air (cold atmospheric air or the preheated air from condensation of sulfuric acid device) burning for gas. In this embodiment, concentrated H₂S burning of gas discharges so many heat, makes to use the cold combustion air of large volume, to avoid burner temperature to exceed 1200 DEG C. As a rule of thumb, approximately 2% SO₂In burner, be oxidized to SO₃. Process gas is cooled to 400 DEG C in waste heat boiler.

By 9,530Nm³The SWS gas of/h is delivered to burner. Combustion temperatures and high NH₃The combination of concentration causes high NO concentration. In order to obtain 0.99 NH₃/ NO ratio, makes 470Nm³The SWS gas of/h is walked around burner the NH as SCR reactor₃Source. By SWS gas and 19,250Nm³The hot-air from condensation of sulfuric acid device of/h mixes (stream 80 in Fig. 4) to obtain 25% the diluted SWS gas of LEL of admixture of gas.

Due to the high SO in process gas₃High NH in concentration and diluted SWS gas₃Concentration, the Potential feasibility that exists very high ammonium hydrogen sulfate (ABS) to form and deposit in nozzle, pipe-line system and catalyst. Body phase ABS dew-point temperature is 339 DEG C, and dew-point temperature in catalyst pores is 365 DEG C of left and right. Form for fear of ABS, process gas temperature is controlled as 398 DEG C, and the temperature of diluted SWS is maintained at 392 DEG C. On SCR catalyst, 97% NO is reduced to N₂, make NO concentration be reduced to 30ppmv, NH₃Overflow as 20ppmv. H₂S on SCR catalyst by complete oxidation. SCR reaction and H₂The reaction enthalpy of S oxidation makes the temperature of process gas improve 31 DEG C. At high like this temperature, the SO of expection 1-2%₂On catalyst, be oxidized. Be further processed in sulphuric acid device because leave the process gas of SCR, therefore without worry.

If ignore dilution to avoid the requirement of risk of explosion, the technique of embodiment 3 can be designed as lower process gas flow rates, as 4,000Nm³/ h, it is by containing abundant oxygen, for SO₂At SO₂Oxidation in converter, and total process gas flow rates is reduced to 10%.

By application LeChatelier mixing rule, then diluted SWS gas composition becomes 110% of LEL at 25 DEG C. LEL raises and declines with temperature, this means that the LEL at 385 DEG C may be about 150% of actual LEL. Such technique needs extremely careful, and to avoid gas contact with spark or hot surface, this may set off an explosion and the excessive damage of equipment, and the while, poisonous SWS gas may be released near zone.

The SCR of table 3 based on SWS and the combination of wet type sulphuric acid device, process from the SWS gas of oil plant and concentrated H₂S gas

Embodiment 4

Do not consider that, for volatile margin of safety, the technique of embodiment 3 also can be designed as lower process gas flow rates.

Under these circumstances, from 19 of embodiment 3,250Nm³The carrier gas flow velocity of/h is reduced to only 4,000Nm³/ h, total process gas flow rates will reduce by 10%, and still have enough oxygen for SO₂At SO₂Oxidation in converter.

By application LeChatelier mixing rule, then diluted SWS gas composition becomes 110% of LEL at 25 DEG C. LEL raises and declines with temperature, this means that the LEL at 385 DEG C may be about 150% of actual LEL. Such technique needs extremely careful, to avoid gas contact with spark or hot surface, its this can set off an explosion and the excessive damage of equipment, the while, poisonous SWS gas may be released near zone.

Embodiment 5

In this embodiment, in the wet type sulphuric acid device that is equipped with SCR reactor, process from 1 of oil plant, 215Nm³The SWS gas of/h. Except SWS stream, also in sulphuric acid device, process the concentrated H from oil plant₂S gas. Most important flow velocity and the composition of in table 4, collecting stream, the identification of numbering for stream is with reference to figure 4.

Temperature in burner is 1200 DEG C, to reduce process gas volume, and due to this high ignition temperature with due to the NH in SWS gas and sour gas₃High-load, the NO of burner outlet_xLevel is higher than in former embodiment. The NO concentration of burner outlet is estimated as 1900ppmv. In this embodiment, make 151Nm³The SWS gas of/h is walked around burner the ammonia source as SCR reactor. Carrier gas is regarded as the effluent from the cooling-air through heating of WSA condenser, and wherein it has been preheated to 259 DEG C. In order to prevent the ABS condensation in diluted SWS gas, carrier gas is further heated in electric heater. Power consumption in electric heater is 158kW. ABS dew point in SCR catalyst pores is 373 DEG C as calculated. In order to prevent forming ABS in SCR catalyst, the inlet temperature of leading to SCR reactor remains 396 DEG C, and it is higher 23 DEG C than the ABS dew point in SCR catalyst pores as calculated. In SCR catalyst, 97% NO is reduced to N₂, make NO concentration be reduced to 42ppmv, simultaneously NH₃Overflow as 10ppmv. H₂S in SCR catalyst by complete oxidation. Reaction enthalpy in SCR catalyst raises 44 DEG C process gas temperature. At SO₂In first of converter, approximately 84% residue SO₂Be converted into SO₃。SO₂The enthalpy of oxidation raises 104 DEG C process gas temperature, and this causes SO₂The outlet temperature of first of converter is 544 DEG C. For mitigate corrosion, SO₂Converter is 550 DEG C of following operations. This embodiment has the surplus of 23 DEG C with respect to the ABS dew point of the entrance that leads to SCR reactor, and with respect to from a SO₂The maximum outlet temperature of reformer bed has the surplus of 6 DEG C.

Table 4

Embodiment 6

SWS gas and sour gas incoming flow are similar to embodiment 5. Most important flow velocity and the composition of in table 5, collecting stream, the identification of numbering for stream is with reference to figure 5.

But, in the present embodiment, from the carrier gas of WSA condenser by make cooling being further heated of exit gas from SCR reactor in gas/gas-heat exchanger. The temperature of carrier gas has been raised to 350 DEG C, and the inlet temperature of consequently leading to SCR reactor is higher 1 DEG C than embodiment 5. Carry out SCR reaction, causing from the outlet temperature of SCR reactor is 441 DEG C similar to Example 5ly. ABS dew point in SCR catalyst pores is 373 DEG C as calculated. Cooling in carrier gas heater of process gas causes leading to SO₂The process gas temperature of converter entrance is 425 DEG C. Owing to leading to a SO₂The inlet temperature of reformer bed is lower, and outlet temperature is reduced to 533 DEG C, simultaneously owing to approaching higher SO₂/SO₃Balance, the SO occurring in this₂Conversion ratio is increased to 86%. Consequently, this embodiment has the surplus of 24 DEG C with respect to the ABS dew point of the entrance that leads to SCR reactor, and with respect to from a SO₂The maximum outlet temperature of reformer bed has the surplus of 17 DEG C. In addition,, with respect to the energy consumption of predicting in embodiment 5, obtained and saved for the energy consumption of electric power carrier gas heater significantly.

Table 5

Embodiment 7

SWS gas and sour gas incoming flow are similar to embodiment 5 and 6. Most important flow velocity and the composition of in table 6, collecting stream, the identification of numbering for stream is with reference to figure 6.

In this embodiment, the H in diluted SWS gas₂S content is optionally oxidized to SO in the catalyst that is similar to SCR catalyst₂. In the time there is not NO in gas, NH₃Can be at H₂Oxidized in S gas reactor, therefore make H₂S is oxidized to SO₂Reaction enthalpy be used to make diluted SWS gas to be heated to 392 DEG C from 253 DEG C.

Table 6

H₂The SO generating in S reactor₂Approximately 2% be further oxided as SO₃, this means the SO that leads to SCR reactor inlet₃Concentration has been increased to 847ppmv. As further result, the ABS dew point in SCR catalyst pores has been increased to 374 DEG C as calculated slightly. But due to the higher temperature of the diluted SWS gas of Partial Conversion, the process gas temperature of leading to SCR reactor inlet has been increased to 407 DEG C. In this case, in SCR reactor, only there is SCR reaction, therefore in SCR reactor because the temperature rise of reaction enthalpy only has 21 DEG C, cause leading to SO₂The inlet temperature of converter is 428 DEG C. The one SO₂Reformer bed outlet temperature is 535 DEG C and approximately 85% residue SO₂Be converted into SO₃. In this embodiment, be 24 DEG C with respect to the surplus of ABS dew point of the entrance that leads to SCR reactor, and with respect to from a SO₂The surplus of the maximum outlet temperature of reformer bed is 17 DEG C.

Embodiment 8

As the alternative scheme of the layout presenting in embodiment 7, diluted SWS gas is being sent to H₂Before S reactor, can in gas/gas-heat exchanger, be preheating to for example 350 DEG C. Illustrating in Fig. 7 of such technique.

At 350 DEG C, needed for H₂The catalyst volume of S reactor can be significantly reduce or abridged completely because at this temperature under oxygen exists H₂S will be oxidized to SO in gas phase₂, as long as the time of staying is enough. Consequently, from H₂The diluted SWS gas of the Partial Conversion of S reactor will be increased to approximately 490 DEG C, but due to the heat exchange of diluted SWS gas, it will be cooled to 392 DEG C, afterwards with process gas mix from burner.

Claims

1. for making a process equipment for process gas denitrogenation, it comprises:

NO_xThe NH of source and combination₃And H₂The source of S,

NO_xConversion unit, it comprises for making NO_xSCR is to N₂There is catalytic activity and for making H₂S is oxidized to SO₂The optional activated material of tool,

H₂S conversion unit, it comprises for making H₂S is oxidized to SO₂There is the material of catalytic activity, if NO_xConversion unit is for making H₂S is oxidized to SO₂Activated, described H₂S conversion unit is optional,

SO₂Conversion unit, it comprises for making sulfur dioxide catalytic oxidation have the material of catalytic activity,

Described NO_xConversion unit, H₂S conversion unit and SO₂Conversion unit has one or more entrances and one or more outlet,

With the device for gas washing in SA production, it has process gas entrance, process gas outlet and concentrated sulfuric acid outlet,

Wherein said NO_xSource and described NO_xThe entrance of conversion unit is fluid communication,

The NH of wherein said combination₃And H₂The source of S and described H₂If the entrance of S conversion unit is fluid communication or omits described H₂S conversion unit with described NO_xThe entrance of conversion unit is fluid communication,

If wherein do not omit described H₂S conversion unit, described H₂The outlet of S conversion unit and described NO_xThe entrance of conversion unit is fluid communication,

Wherein said NO_xThe outlet of conversion unit and described SO₂The entrance of conversion unit is fluid communication,

Wherein said SO₂The process gas entrance of the outlet of conversion unit and the described device for gas washing in SA production is fluid communication, the process gas outlet of the described device for gas washing in SA production is fluid communication with waste line, and the outlet of the sulfuric acid of the described device for gas washing in SA production is set to extract sulfuric acid.

2. process equipment according to claim 1, also comprises the burner in the source with one or more entrance and exits and oxygen rich gas, the NH of wherein said combination₃And H₂The stream that it is fluid communication that the source of S is split as with burner inlet and the stream that is fluid communication with pre-inversion unit, comprise NO described in the outlet stream of wherein said burner forms_xAt least a portion of stream.

3. process equipment according to claim 2, also comprises carrier gas source and hybrid element, and described hybrid element optionally comprises mixing intensifier, has two entrance and exits, the NH of wherein said combination₃And H₂An entrance of the stream of S and described hybrid element is fluid communication, and another entrance of described carrier gas source and described hybrid element is fluid communication, and the outlet of described hybrid element and described NO_xConversion unit or described H₂S conversion unit is fluid communication, makes to guide to described NO_xConversion unit or described H₂The NH of the described combination of S conversion unit₃And H₂The stream of S is diluted.

4. according to the process equipment described in claim 1,2 or 3, comprising described H₂S conversion unit, and the NH of diluted combination₃And H₂The stream of S and described H₂The entrance of S conversion unit is fluid communication, and described H₂The outlet of S conversion unit and described NO_xThe entrance of conversion unit is fluid communication.

5. process equipment according to claim 4, also comprises the heat exchanger being set to for heating first-class and cooling second, wherein said first-class be the NH of described combination₃And H₂The NH of stream, carrier gas or the diluted combination of S₃And H₂Any one in the stream of S, and described second is hot process flow.

6. process equipment according to claim 5, the process flow of wherein said heat is from described NO_xThe outlet stream of conversion unit or from described H₂The outlet stream of S conversion unit.

7. process equipment according to claim 1, the wherein said device for gas washing in SA production is condensation of sulfuric acid device, described condensation of sulfuric acid utensil has process gas entrance, process gas outlet, cooling medium entrance, cooling medium outlet and concentrated sulfuric acid outlet, and described cooling medium entrance and cooling medium source are fluid communication.

8. process equipment according to claim 2, the wherein said device for gas washing in SA production is condensation of sulfuric acid device, described condensation of sulfuric acid utensil has process gas entrance, process gas outlet, cooling medium entrance, cooling medium outlet and concentrated sulfuric acid outlet, and described cooling medium entrance and cooling medium source are fluid communication.

9. process equipment according to claim 8, wherein said cooling medium source is atmospheric air, and wherein said cooling medium outlet be set to supply any one or its in described oxygen rich air body source and carrier gas both.

10. process equipment according to claim 1, the wherein said device for gas washing in SA production is SO₃Absorber, described SO₃Absorber has process gas entrance, process gas outlet, concentrated sulfuric acid entrance and the further outlet of the concentrated concentrated sulfuric acid, and the entrance and the concentrated sulfuric acid source that wherein absorb sulfuric acid are fluid communication.

11. 1 kinds of refineries, comprise according to the process equipment described in claim 1 to 10 and sour water stripping (SWS) tower, and described sour water stripping (SWS) tower has the NH that forms described combination₃And H₂The outlet of the sour water stripping (SWS) tower gas in the source of S.