CN101679037A - Process and apparatus for mixing gases - Google Patents
Process and apparatus for mixing gases Download PDFInfo
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- CN101679037A CN101679037A CN200880019767A CN200880019767A CN101679037A CN 101679037 A CN101679037 A CN 101679037A CN 200880019767 A CN200880019767 A CN 200880019767A CN 200880019767 A CN200880019767 A CN 200880019767A CN 101679037 A CN101679037 A CN 101679037A
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- 238000002156 mixing Methods 0.000 title claims abstract description 31
- 238000000034 method Methods 0.000 title claims description 30
- 239000007789 gas Substances 0.000 title abstract description 95
- 239000000203 mixture Substances 0.000 claims abstract description 18
- 238000004891 communication Methods 0.000 claims description 6
- 230000002411 adverse Effects 0.000 claims description 4
- 239000008246 gaseous mixture Substances 0.000 claims description 3
- 239000003054 catalyst Substances 0.000 abstract description 3
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 description 10
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 8
- GNTDGMZSJNCJKK-UHFFFAOYSA-N divanadium pentaoxide Chemical compound O=[V](=O)O[V](=O)=O GNTDGMZSJNCJKK-UHFFFAOYSA-N 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000006096 absorbing agent Substances 0.000 description 2
- 230000002349 favourable effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000001771 impaired effect Effects 0.000 description 1
- 239000000411 inducer Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000002427 irreversible effect Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 238000009827 uniform distribution Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
- C01B17/76—Preparation by contact processes
- C01B17/80—Apparatus
- C01B17/803—Converters
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
- B01F23/10—Mixing gases with gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F25/00—Flow mixers; Mixers for falling materials, e.g. solid particles
- B01F25/30—Injector mixers
- B01F25/31—Injector mixers in conduits or tubes through which the main component flows
- B01F25/313—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit
- B01F25/3132—Injector mixers in conduits or tubes through which the main component flows wherein additional components are introduced in the centre of the conduit by using two or more injector devices
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0446—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0461—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
- B01J8/0469—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being superimposed one above the other
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0492—Feeding reactive fluids
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/69—Sulfur trioxide; Sulfuric acid
- C01B17/74—Preparation
- C01B17/76—Preparation by contact processes
- C01B17/765—Multi-stage SO3-conversion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00194—Tubes
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Inorganic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
When mixing two gases of different temperature and/or composition in a converter for producing SO3 from an SO2-containing gas, a first SO2-containing gas flow is introduced into the converter througha central supply pipe and passed through an integrated heat exchanger arranged around the central supply pipe, which is traversed by the first gas flow from the bottom to the top. A second gas flow issupplied via a ring conduit arranged above the integrated heat exchanger, from which the second gas flow is discharged through a plurality of openings and is fed into the first gas flow, so that it mixes with the same. Then, the gas mixture obtained is supplied to a contact stage of the converter, in which the SO2 is at least partly converted to SO3 on a catalyst.
Description
Technical field
The present invention relates to a kind of using and contain SO by the gas that in convertor, mixes two kinds of differing tempss and/or composition
2Gas generation SO
3Method and the device of realizing this method.
Background technology
The present invention relates to vitriolic production.Normally, sulfuric acid is mainly produced by so-called double suction method, and this method is rolled up the 635th to 700 page at the 5th edition A25 of industrial chemistry encyclopaedia (Encyclopedia ofIndustrial Chemistry) of Ullmann description.At first, the beginning gas that comprises sulfurous gas in a plurality of Continuous Contact levels of convertor at least in part with the oxygen reaction, according to following formula to obtain sulphur trioxide.
SO
2+1/2O
2→SO
3+98KJ
The gas of producing then that comprises sulphur trioxide is fed in the resorber, and is converted into sulfuric acid at that.Sulfurous gas carries out having under the situation of catalyzer to the oxidation of sulphur trioxide, and catalyzer comprises the Vanadium Pentoxide in FLAKES as activeconstituents usually, and working range is about 380 ℃ to 640 ℃.When surpassing 640 ℃, irreversible damage can take place in vanadium pentoxide catalyst, and when being lower than 380 ℃, Vanadium Pentoxide in FLAKES is inactive.Because the strong heat release of process, the gas inlet temperature that enters the contact level is about 400 ℃.Under obviously low temperature in, instead would not begin, and under a very high temperature in, thereby temperature rising catalyzer can be damaged in reaction process.Yet, also can use other catalyzer with high working temperature, for example EP1047497B1 or DE10023178A1 are described.In order to obtain high output, reaction divides several levels to finish, and between each level, process gas all passes through integrated interchanger cooling, thinks that next contact level obtains suitable gas inlet temperature.Usually, this convertor comprises four to five contact levels, and in the biabsorption method above-mentioned, the process gas that passes a plurality of (for example being three) contact level offers intermediate absorber, SO in intermediate absorber
3Change sulfuric acid, oleum or liquid SO into
3, so SO in the process gas
3Concentration reduce again.After being heated to desired technological temperature, process gas offers other contact level of convertor, absorption to the end after this then.
Offer the amount and the SO of the process gas of convertor
2The concentration frequent fluctuation.In the convertor of routine, owing to the high temperature that is reached in first catalytic stages, SO
2Concentration is limited at about 12 volume % usually, in the described technology of DE10249782A1, by the SO that comprises of recirculation
3Gas, use higher SO
2Concentration.Limit recirculation the reaction of the first contact level, heat here produces as a result.
Owing to the fluctuation of inlet gas, need the temperature of control contact substance ingress.This is by providing the cold SO that comprises via bypass ducts
2Gas realize.The SO that comprises above-mentioned
3In the recirculation of gas, ratio of mixture also must be adjusted.Therefore, the gas of differing temps and/or composition must mix by different points in convertor.Even with the gas of sample ingredient, temperature head can cause different viscosity, and this can make and mix difficulty.Yet the efficient for technology needs homogeneous gas mixture.If do not reach the abundant uniformity of gas at the inlet of contact substance, will have such zone, in these zones when passing the contact level SO
2Can not change into SO
3, so the efficient of convertor is with impaired.Containing too much SO
2The zone in, overheatedly may cause catalyst damage.It is found that in the conduit of sulfuric acid apparatus the gas that mixes differing temps be not one fast, spontaneous process.Because what different viscosity, gas were parallel to each other each other flows, and does not mix (so-called laminar flow).
In order to address this problem, present state of the art provides local pressure loss, and this causes having highly fluidised turbulent flow.But because the obtainable or integral pressure loss that allows is because device technique former thereby be restricted or must be restricted in the system, therefore this under many circumstances solution is inadequate.
Summary of the invention
Therefore, the objective of the invention is to improve in the convertor gas blended uniformity of two kinds of differing tempss and/or composition, reduce or prevent so-called laminar flow.
This purpose realizes basically by the present invention, wherein comprises SO
2First air communication cross central supply-pipe and be incorporated into convertor, pass and be arranged on central supply-pipe integrated interchanger on every side, second air communication is crossed the loop pipe that directly was arranged in the convertor and is supplied with before or after integrated interchanger, second air communication is crossed a plurality of openings and is discharged from ring pipe, and send into first air-flow, therefore mixes with first air-flow, the gaseous mixture that is obtained is provided to the contact level of convertor then, in this contact grade on catalyzer SO
2Be converted into SO at least in part
3Therefore, by loop pipe, second air-flow is sent into first air-flow at a plurality of points, therefore the mixing of finishing.Because second air-flow is (for example for comprising SO
2Cryogenic gas) only partly pass the device that is arranged on the convertor upstream, therefore can obtain higher pressure with respect to mixture, the pressure-losses also can be increased and/or control whereby.By this this adjustment or control to the pressure or the pressure-losses, therefore mixing and mixing quality can be adjusted or control.If second gas is the sulphur trioxide of recirculation, then its pressure can be increased by gas blower or analogue, therefore, compares with ordinary method, can obtain the higher pressure with respect to mixture here equally, and the pressure-losses can increase.By this gas blower, also can regulate or regulate and control the pressure or the pressure-losses selectively.By such adjustment or the control pressure or the pressure-losses, mixing quality also can be adjusted and control.Preferably, the pressure-losses in the mixing device is optimised, and obtaining sufficient turbulent flow and mixing quality, and does not have the big pressure-losses.
In preferred aspects of the invention, when the second air-flow adverse current is sent into first air-flow, obtain good especially mixing resultant.Additional like this turbulent flow produces, and this has promoted mixing.Yet, can also or additionally send into second gas in the same way and flow in first air-flow.Described as DE10249782A1, comprising SO
3The recirculation of gas in, first air-flow comprises the SO that surpasses 13 volume %
2, second air-flow comprises the SO of 3-40 volume %
3, according to improvement of the present invention, the SO of 5-25 volume % preferably
3First air-flow also can comprise SO
3, the SO of 1-10 volume % for example
3, still preferably comprise SO less than 1 volume %
3
In another embodiment of the present invention, the air-flow of mixing section can be directed, and for example by the gas inlet of guide plate or loop pipe, therefore, for example the logistics as whirlpool produces in mixing section.
If do not comprise SO
3The recirculation of gas, the temperature in of the convertor first contact level is by second gas flow-regulating according to the present invention, second air-flow comprises the SO that reaches 30 volume %
2, especially reach the SO of 12 volume %
2, and have 0 to 400 ℃ temperature, be preferably 80 to 300 ℃, more preferably 100 to 120 ℃.This air-flow can be used as branch road and flows through around conventional interchanger, and to improve the temperature of first gas, therefore, it has the pressure higher than first gas.In branch road, can incorporate the device of control or adjusting pressure into, for example gas blower or throttling valve or Fluistor mix whereby and can be controlled extraly.
According to the present invention, the volumetric flow rate of second air-flow is the 20-60% of first air-flow less than the volumetric flow rate of first air-flow, be preferably≤50%, more preferably≤30%.
Be used at the convertor mixing two gas with comprising SO
2Gas generation SO
3Device of the present invention, especially be used for carrying out the device of aforesaid method, comprise supply-pipe that is used for first gas and the loop pipe that is used for second gas, this first gas is introduced in the convertor, and pass integrated interchanger, and this integrated interchanger is around central supply-pipe setting, and this loop pipe directly was arranged in the mixing section before or after interchanger in convertor, wherein loop pipe comprises a plurality of openings, so that second gas is discharged in the mixing section.
In a preferred embodiment of the invention, first gas from above or below be incorporated into the convertor, and after turning to, pass the integrated interchanger that preferably is arranged on around the central supply-pipe, enter the mixing section that is arranged in the interchanger top then.Yet, gas can from above or below introduce interchanger with linear fashion, and do not turn to.Loop pipe also preferred arrangements around the central supply-pipe that is used for first gas.Except simple guide of flow, this is of compact construction convertor and mixing device.
Enter first air-flow for adverse current guides second air-flow, the hole in the loop pipe is towards interchanger.Therefore, second air-flow is preferably discharged downwards from loop pipe.If second air-flow is sent into first air-flow in the same way, then the hole in the loop pipe is back to interchanger, and therefore, second air-flow is discharged upward from loop pipe.Certainly, opening (it can be designed pore-forming or seam etc.) can not only be arranged in the bottom surface of loop pipe but also be arranged in cyclic end face or side accordingly.Opening can be arranged to several rows side by side, so that the amount of second air-flow that is provided to be provided.Preferably, opening has 20 to 70 inclination angles of spending with respect to vertical direction, especially preferably 30 to 60 degree.Opening can have different sizes or shape, for example according to the distance of supply-pipe and difference.Also can change opening or change by other device (for example baffle plate, weld seam or the like) around opening or from the air-flow of opening.This variation also can only relate to single opening or single group opening.Can be single opening in addition or singly organizing opening provides closing device, regulates or control device to have, especially in partial load operation.
According to a preferred aspect of the present invention, provide two to seven, three concentric annular pipes especially are provided, second gas is therefrom discharged.Therefore also can increase the amount of second air-flow.Loop pipe can be positioned at different vertical height.
Switch in order to help device, loop pipe links to each other with the common supply-pipe that is used for second gas according to the present invention.The common supply-pipe that discovery is used for second gas is favourable around the central supply-pipe guiding of first gas at least in part, and the pipe connecting of a plurality of downward guiding connects supply-pipe and loop pipe is favourable.As a result, second gas is introduced in convertor simultaneously at a plurality of points, wherein realizes the preferred symmetrical configurations of convertor and flows preferred symmetry guiding.Yet main points are that gas mixes and the uniform distribution in convertor quite uniformly for purposes of the invention, for this purpose, and in case of necessity can be asymmetric.
According to the present invention, each pipe connecting links to each other with all loop pipe by supplying opening, to supply with comparalive ease.
According to a further aspect in the invention, this device has conduit to supply with gas in mixing tank, and volumetric flow rate and/or the pressure and/or the pressure-losses of the air-flow in the conduit can be regulated or control to described conduit.This control can realize by the device (for example being inducer, nozzle or Fluistor) of gas blower etc. and/or control pressure loss.
Improvement of the present invention, advantage and possible application can obtain by the description and the accompanying drawing of following specific embodiment.Described and/or illustrated all features itself or anyly be combined to form theme of the present invention are independent of their inclusion of claim or their reference background document.
Description of drawings
Fig. 1 illustrates the usefulness that has a device of mixed gas according to embodiments of the invention and contains SO
2Gas generation SO
3The constructed profile of convertor, air-flow shown in the figure;
Fig. 2 illustrates the zone of second air-flow being introduced first air-flow;
Fig. 3 illustrates the part vertical view according to the loop pipe of device of the present invention; And
Fig. 4 illustrates along the sectional view of the intercepting of the IV-IV line among Fig. 3 loop pipe.
Embodiment
Shown in Figure 1 with SO
2Be converted into SO
3Convertor 1 comprise from K1 to K5 five contact levels altogether, catalyzer (specifically being the catalyzer that comprises Vanadium Pentoxide in FLAKES) is arranged on wherein, with SO
2Be converted into SO
3After passing from K1 to K3 three contact levels, what obtained comprises SO
3Gas supply to not shown heat reclamation device and intermediate absorption device, from process gas, to remove sulphur trioxide at least in part.Comprise SO then
2Process gas supply to convertor once more in the bottom, to pass contact level K4 and K5.The K1 that the present invention is mainly used in the first area of convertor 1 realizes that to K3 contact level therefore the description below is limited in this zone.In alternate embodiments (not shown), blending means of the present invention also can realize at the second area (the contact level from K4 to K5) of convertor.
Comprise SO
2Gas supply in the convertor 1 by central supply-pipe 2, this comprises SO
2Gas from the top to the bottom, pass supply-pipe, and turn to 180 ° by baffle plate 3 in the lower end of supply-pipe.Therefore, first gas passes the first interchanger WT1 from bottom to top, and is discharged to the mixing section 4 that is arranged on the interchanger WT1, and this first interchanger specifically constitutes tubular heat exchanger.
Second gas (for example is the SO that comprises of recirculation
3Process gas or than first gas temperature low SO that comprises
2Gas) pipe connecting 6 by supply-pipe 5 and adjacency is introduced in mixing section 4 equally, and mixes with first gas, pipe connecting 6 links to each other with the loop pipe 8 that extends around central supply-pipe 2 by supplying opening 7.Here supply-pipe 5 for example in the outside of convertor 1, for example is 3/4ths annulars around central supply-pipe 2 guiding, and wherein pipe connecting divides out branch downwards from supply-pipe 5, and enters convertor 1.The loop pipe 8 that second gas is therefrom discharged is set directly at after the integrated interchanger WT1, i.e. the other device that does not interconnect.
By conduit 9, for example cold or heat in addition comprise SO
2Gas can be supplied to and before entering convertor 1 with comprise SO
3Gas mix.
Gaseous mixture flows through the first contact level K1 then, then pass integrated interchanger WT1, so that in K1 contact level because about 400 ℃ temperature that the temperature of the process gas of thermopositive reaction and elevated temperature is cooled to be fit to enter the second contact level K2, heat simultaneously by what central supply-pipe 2 provided and comprise SO
2First gas.After passing the second contact level K2, process gas passes integrated interchanger WT2 successively, to be cooled to be suitable for 400 ℃ the temperature in of being about of the 3rd contact level K3, after passing the 3rd contact level K3, extract out from convertor 1, and supply to the intermediate absorption device by outlet 10.
Be noted that described above comprising turns to first air-flow before entering interchanger WT1 structure is preferred for the convertor that comprises a plurality of interchanger.Selectable, can from above or below supply gas, wherein the outlet at interchanger mixes.
In Fig. 2 and Fig. 4, show in detail the device that mixes first and second gases.In Fig. 2, first gas enters the first interchanger WT1 from the below, be discharged to then in the mixing section 4.Send into loop pipe 8 through pipe connecting 6 and supplying opening 7, the second gases, be drained into downwards the mixing section 4 by a plurality of openings 11 (with reference to Fig. 4) from this loop pipe.Here opening 11 is arranged to several rounds, the layout that these several rounds can be offset mutually, and therefore second gas is sent into first gas as a plurality of rills, and because adverse current is sent into caused turbulent flow, can easily mix with first gas.In another specific embodiment that does not here show, except opening 11 that is arranged on loop pipe 8 lower surfaces or the opening 11 that replaces being arranged on loop pipe 8 lower surfaces, corresponding opening also can be arranged on the upper surface of loop pipe 8, in the same way second gas is sent in first gas.
Can draw from Fig. 3, three concentric annular pipes 8 arrange around central supply-pipe 2, and loop pipe is supplied with first gas is arranged by being evenly distributed on four pipe connectings 6 around the convertor 1 and supplying opening 7.
By the present invention, can realize the intimate mixing of two kinds of air-flows, the composition and the temperature of process gas that therefore is positioned at the inlet of the first contact level K1 can be easy to adjust.
Before entering convertor, gas mixes two kinds of air-flows within the scope of the present invention.The structure of mixing section 4 and loop pipe 8 before entering convertor 1, mixed gas is provided in this case.
Reference numerals list
1 converter
2 central supply pipes
3 baffle plates
4 mixing chambers
5 supply-pipes
6 pipe connectings
7 supplying openings
8 loop pipes
9 bypass duct
10 outlets
11 openings
K1-K5 contacts level
The integrated interchanger of WT1-WT3
Claims (17)
1, the gas that is used for mixing two kinds of differing tempss and/or composition at convertor is with comprising SO
2Gas generation SO
3Method, wherein comprise SO
2First air communication cross central supply-pipe and be introduced in the convertor, and pass integrated interchanger, wherein second air communication is crossed the loop pipe supply that directly was arranged in the convertor before or after integrated interchanger, second air communication is crossed a plurality of openings and discharge and send into first air-flow from this loop pipe, therefore mix with first air-flow, wherein the gaseous mixture that is obtained is provided to the contact level of convertor subsequently, in this contact level on catalyzer SO
2Be converted into SO at least in part
3
2, the method described in claim 1 is characterized in that the second air-flow adverse current is sent in first air-flow.
3, the method described in claim 1 or 2 is characterized in that second air-flow is sent in first air-flow in the same way.
4, as any described method of above-mentioned claim, it is characterized in that first air-flow comprises the SO more than 13 volume %
2, second air-flow comprises the SO of 5 to 25 volume %
3
5,, it is characterized in that second air-flow comprises the SO up to 13 volume % as each described method of claim 1 to 3
2, have 80 to 300 ℃ temperature, be preferably 100 to 120 ℃.
6,, it is characterized in that second air-flow is less than first air-flow as any one described method of above-mentioned claim.
7, be used at convertor (1) mixing two gas with comprising SO
2Gas generation SO
3Device, especially carry out the device of the described method of above-mentioned any one claim, comprise supply-pipe (2) that is used for first gas and the loop pipe (8) that is used for second gas, this first gas is introduced in the convertor (1), and pass integrated interchanger (WT1), this loop pipe directly was arranged on before or after integrated interchanger (WT1) in the mixing section (4), and wherein loop pipe (8) comprises a plurality of openings (11), so that second gas is discharged in the mixing section (4).
8, device as claimed in claim 7 is characterized in that first gas is introduced in the convertor (1), passes integrated interchanger (WT1), and this integrated interchanger preferably is provided with around central supply-pipe (2).
9,, it is characterized in that loop pipe (8) is provided with around the central supply-pipe (2) that is used for first gas as claim 7 or 8 described devices.
10, as each described device of claim 7 to 9, it is characterized in that mixing section (4) is arranged on the interchanger (WT1) or under.
11,, it is characterized in that opening (11) in the loop pipe (8) is towards interchanger (WT1) as each described device of claim 7 to 10.
12,, it is characterized in that opening (11) in the loop pipe (8) is back to interchanger (WT1) as each described device of claim 7 to 11.
13, as each described device of claim 7 to 12, it is characterized in that the upper surface of loop pipe (8) and/or lower surface are provided with a row or multi-row hole, second gas is discharged by these holes.
14, as each described device of claim 7 to 13, it is characterized in that, be provided with a plurality ofly, specifically is three concentric loop pipes (8), and second gas is discharged from loop pipe.
15,, it is characterized in that loop pipe (8) is connected with the common supply-pipe (5) that is used for second gas as each described device of claim 7 to 14.
16, device as claimed in claim 15, the common supply-pipe (5) that it is characterized in that being used for second gas is at least in part around central supply-pipe (2) guiding that is used for first gas, and the pipe connecting of a plurality of downward extensions (6) connects common supply-pipe (5) and loop pipe (8).
17, device as claimed in claim 16 is characterized in that pipe connecting (6) all is connected with all loop pipe (8) by supplying opening (7).
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102007027881A DE102007027881B4 (en) | 2007-06-13 | 2007-06-13 | Method and apparatus for mixing gases |
| DE102007027881.2 | 2007-06-13 | ||
| PCT/EP2008/004510 WO2008151758A2 (en) | 2007-06-13 | 2008-06-06 | Process and apparatus for mixing gases |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101679037A true CN101679037A (en) | 2010-03-24 |
| CN101679037B CN101679037B (en) | 2015-03-04 |
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| CN200880019767.1A Active CN101679037B (en) | 2007-06-13 | 2008-06-06 | Process and apparatus for mixing gases |
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| Country | Link |
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| CN (1) | CN101679037B (en) |
| AU (1) | AU2008261290B2 (en) |
| CL (1) | CL2008001718A1 (en) |
| DE (1) | DE102007027881B4 (en) |
| MX (1) | MX340510B (en) |
| PE (1) | PE20090270A1 (en) |
| WO (1) | WO2008151758A2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102745654A (en) * | 2012-07-31 | 2012-10-24 | 阳谷祥光铜业有限公司 | Conversion device for acid-making with smoke, system and method for heating conversion device for acid-making with smoke |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108046221B (en) * | 2017-12-12 | 2020-10-02 | 中国恩菲工程技术有限公司 | Method for preparing acid by smelting flue gas |
Family Cites Families (13)
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|---|---|---|---|---|
| US2104858A (en) * | 1935-01-23 | 1938-01-11 | Gen Chemical Corp | Manufacture of sulphuric acid |
| NL205521A (en) * | 1951-10-10 | |||
| DE1151341B (en) * | 1961-03-21 | 1963-07-11 | Schmidt Sche Heissdampf | Installation of additional firing systems for introducing and mixing the fresh heating gas into exhaust gas ducts through which low-temperature exhaust gases flow |
| DE1926239U (en) * | 1964-01-31 | 1965-11-04 | Uhde Gmbh Friedrich | DEVICE FOR MIXING GASES OF DIFFERENT DENSITY. |
| US3661165A (en) * | 1970-07-21 | 1972-05-09 | Nat Distillers Chem Corp | System for mixing gases and sparger valve for accomplishing same |
| DE7242602U (en) * | 1972-11-20 | 1976-04-29 | Hoogovens Ijmuiden B.V., Ijmuiden (Niederlande) | |
| US4152407A (en) * | 1977-02-02 | 1979-05-01 | Warren Fuchs | Process and apparatus for exothermic reactions |
| CA1159229A (en) * | 1980-09-19 | 1983-12-27 | John Mcfarland | Converter |
| US5480620A (en) * | 1994-08-17 | 1996-01-02 | Cameron; Gordon M. | Catalytic converter |
| DE19800800C2 (en) | 1998-01-13 | 2001-05-23 | Metallgesellschaft Ag | Process for the production of sulfuric acid |
| DE10023178A1 (en) | 2000-05-11 | 2001-11-15 | Mg Technologies Ag | Two-stage catalytic production of sulfur trioxide gas with low sulfur dioxide content from high sulfur dioxide-content gas comprises use of two catalyst layers with temperature at each layer controlled |
| DE10249782A1 (en) | 2002-10-24 | 2004-05-06 | Outokumpu Oyj | Process and plant for the production of sulfuric acid from sulfur dioxide-rich gases |
| DE10359744A1 (en) * | 2003-12-19 | 2005-07-14 | Uhde Gmbh | Method and device for injecting oxygen into a synthesis reactor |
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2007
- 2007-06-13 DE DE102007027881A patent/DE102007027881B4/en active Active
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2008
- 2008-06-06 MX MX2009013478A patent/MX340510B/en active IP Right Grant
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- 2008-06-11 PE PE2008000998A patent/PE20090270A1/en active IP Right Grant
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102745654A (en) * | 2012-07-31 | 2012-10-24 | 阳谷祥光铜业有限公司 | Conversion device for acid-making with smoke, system and method for heating conversion device for acid-making with smoke |
Also Published As
| Publication number | Publication date |
|---|---|
| DE102007027881A1 (en) | 2008-12-18 |
| AU2008261290B2 (en) | 2013-07-04 |
| MX340510B (en) | 2016-07-11 |
| WO2008151758A3 (en) | 2009-06-11 |
| DE102007027881B4 (en) | 2012-02-16 |
| AU2008261290A1 (en) | 2008-12-18 |
| WO2008151758A2 (en) | 2008-12-18 |
| CN101679037B (en) | 2015-03-04 |
| CL2008001718A1 (en) | 2008-08-01 |
| PE20090270A1 (en) | 2009-03-19 |
| MX2009013478A (en) | 2010-01-18 |
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Correction item: Patentee Correct: Metso Altutai Finland|Tampere False: Meizhuo Metal Co., Ltd.|Espoo, Finland Number: 14-01 Volume: 40 |