CN208748034U - A kind of converter and/or blast furnace gas deoxygenation fine de-sulfur device - Google Patents
A kind of converter and/or blast furnace gas deoxygenation fine de-sulfur device Download PDFInfo
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- CN208748034U CN208748034U CN201821186428.XU CN201821186428U CN208748034U CN 208748034 U CN208748034 U CN 208748034U CN 201821186428 U CN201821186428 U CN 201821186428U CN 208748034 U CN208748034 U CN 208748034U
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- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 50
- 239000011593 sulfur Substances 0.000 title claims abstract description 50
- 238000006392 deoxygenation reaction Methods 0.000 title claims abstract description 26
- 239000003034 coal gas Substances 0.000 claims abstract description 48
- 230000007062 hydrolysis Effects 0.000 claims abstract description 42
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 42
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 38
- 238000006477 desulfuration reaction Methods 0.000 claims description 28
- 230000023556 desulfurization Effects 0.000 claims description 28
- 239000003054 catalyst Substances 0.000 claims description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 14
- 238000000746 purification Methods 0.000 claims description 9
- 239000003463 adsorbent Substances 0.000 claims description 6
- 238000001179 sorption measurement Methods 0.000 claims description 6
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 5
- 229910052799 carbon Inorganic materials 0.000 claims description 5
- 239000012716 precipitator Substances 0.000 claims description 5
- 239000003245 coal Substances 0.000 claims description 2
- 230000003301 hydrolyzing effect Effects 0.000 claims 1
- 239000007789 gas Substances 0.000 abstract description 146
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 abstract description 34
- 239000001301 oxygen Substances 0.000 abstract description 34
- 229910052760 oxygen Inorganic materials 0.000 abstract description 34
- 238000000034 method Methods 0.000 abstract description 14
- 230000008569 process Effects 0.000 abstract description 8
- 239000000203 mixture Substances 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000008246 gaseous mixture Substances 0.000 abstract description 2
- 230000008929 regeneration Effects 0.000 abstract description 2
- 238000011069 regeneration method Methods 0.000 abstract description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 12
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 8
- 239000000428 dust Substances 0.000 description 8
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 7
- 238000002156 mixing Methods 0.000 description 7
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 6
- XYFCBTPGUUZFHI-UHFFFAOYSA-N Phosphine Chemical compound P XYFCBTPGUUZFHI-UHFFFAOYSA-N 0.000 description 6
- 229910002092 carbon dioxide Inorganic materials 0.000 description 6
- 239000001569 carbon dioxide Substances 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 6
- 229910052739 hydrogen Inorganic materials 0.000 description 6
- 239000012535 impurity Substances 0.000 description 5
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 description 4
- WQOXQRCZOLPYPM-UHFFFAOYSA-N dimethyl disulfide Chemical compound CSSC WQOXQRCZOLPYPM-UHFFFAOYSA-N 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 229910000831 Steel Inorganic materials 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 125000001741 organic sulfur group Chemical group 0.000 description 3
- 230000009467 reduction Effects 0.000 description 3
- 239000010959 steel Substances 0.000 description 3
- 238000010792 warming Methods 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000011049 filling Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 238000004064 recycling Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- QENGPZGAWFQWCZ-UHFFFAOYSA-N Methylthiophene Natural products CC=1C=CSC=1 QENGPZGAWFQWCZ-UHFFFAOYSA-N 0.000 description 1
- YTPLMLYBLZKORZ-UHFFFAOYSA-N Thiophene Chemical compound C=1C=CSC=1 YTPLMLYBLZKORZ-UHFFFAOYSA-N 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 125000000118 dimethyl group Chemical group [H]C([H])([H])* 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 230000010354 integration Effects 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000009628 steelmaking Methods 0.000 description 1
- 238000005496 tempering Methods 0.000 description 1
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Abstract
A kind of converter and/or blast furnace gas deoxygenation fine de-sulfur device include hydrolysis desulfurizing tower, deoxidation reactor and fine de-sulfur tower；The entrance of hydrolysis desulfurizing tower is connected to converter and/or blast furnace gas gas holder, outlet is connected to the entrance of deoxidation reactor, two branches of deoxidation reactor outlet setting, one branch is connected to the pipeline connection for being connected to hydrolysis desulfurizing tower outlet and deoxidation reactor entrance, another branch with the entrance of fine de-sulfur tower.The converter of the utility model and/or blast furnace gas deoxygenation fine de-sulfur device mix the higher coal gas of the oxygen content coal gas low with oxygen content, mixed coal gas is subjected to deoxidation treatment, obtain qualified regeneration gas, a part of coal gas is recycled simultaneously, it is mixed for the higher coal gas of oxygen content, gaseous mixture, simple process is made, energy consumption is small, can real-time online continuously to coal gas carry out deoxidation treatment.
Description
Technical field
The utility model relates to field of gas purification, and in particular to a kind of converter and/or blast furnace gas deoxygenation fine de-sulfur dress
It sets.
Background technique
Steel mill turns, blast furnace gas is before recycling, to pass through electric precipitation workshop section, therefore in view of recycling safety, controls coal gas
Middle oxygen content index is less than 1%.Domestic major steel mill turns, for CO content in 40-50%, oxygen content is universal in blast furnace gas
Between 0.5~1.5%.Turn, the general service of blast furnace gas is to generate electricity or be used as other fuel therefore not do deoxidation substantially
Processing.With the propulsion that steel industry energy-saving and emission-reduction, depth are taped the latent power, tempering coproduction project gradually increases, the raw material of Chemical Manufacture
Gas is gradually substituted by coal gas by steel-making tail gas, and in order to be able to satisfy the needs of Chemical Manufacture, the oxygen content in unstripped gas needs
Removing and control.
Existing deoxidation mode, which has, carries out deoxidation treatment using deoxidation reactor or gas conversion technique, but due to turning, it is high
The too high oxygen level of producer gas directly takes conventional treatment means to will cause reactor temperature runaway, catalyst and deoxidier inactivation etc.
Accident, therefore, existing deoxidation mode can not be suitable for turn, blast furnace gas deoxidation.
Summary of the invention
The technology of the utility model solves the problems, such as: overcoming the deficiencies of the prior art and provide a kind of converter and/or blast furnace coal
Gas deoxygenation fine de-sulfur device.
The technical solution of the utility model is: a kind of converter and/or blast furnace gas deoxygenation fine de-sulfur device, including water
Solve desulfurizing tower, deoxidation reactor and fine de-sulfur tower；The entrance of hydrolysis desulfurizing tower is connected to converter and/or blast furnace gas gas holder, out
Mouthful be connected to the entrance of deoxidation reactor, deoxidation reactor outlet is arranged two branches, and a branch hydrolyzes desulfurizing tower with being connected to
The pipeline connection of outlet and deoxidation reactor entrance, another branch are connected to the entrance of fine de-sulfur tower.
Further, the outlet of connection deoxidation reactor and connection hydrolysis desulfurizing tower outlet and deoxidation reactor entrance pipe
Branch road is exported in connection hydrolysis desulfurizing tower outlet and the pipeline direction of deoxidation reactor entrance, successively from deoxidation reactor
It is provided with circulating air water cooler, circulating air liquid separation tank and converter and/or blast furnace gas recycle compressor.
Further, the device includes coal gas of converter heat exchanger and purified gas water cooler, and coal gas of converter heat exchanger is set
It sets between the entrance and converter and/or blast furnace gas gas holder of hydrolysis desulfurizing tower, while the setting of coal gas of converter heat exchanger is being connected to
The branch road of deoxidation reactor outlet and fine de-sulfur tower entrance, purified gas water cooler are arranged in coal gas of converter heat exchanger and fine de-sulfur
Branch road between tower.
Further, the device includes going into operation heater and hydrolysis desulfurization goes into operation heater, connection hydrolysis desulfurizing tower
Entrance and converter and/or blast furnace gas gas holder pipeline on be provided with the branch that goes into operation, the heater that goes into operation is arranged in the branch that goes into operation
On, it is provided with hydrolysis desulfurization in connection hydrolysis desulfurizing tower outlet and the pipeline of deoxidation reactor entrance and goes into operation branch, hydrolyzes desulfurization
The heater that goes into operation setting goes into operation on branch road in hydrolysis desulfurization.
Further, deoxidation reactor includes shell, upper cover, lower head, several heat exchanger tubes, atmolysis cylinder, manhole pipe orifice,
Catalyst self-unloading mouth, air inlet, gas outlet and relief valve；Shell and upper cover and lower head connect and compose pressure shell；It is several
Heat exchanger tube is set in shell and is fixedly connected with atmolysis cylinder, and atmolysis cylinder is fixedly connected in lower head, air inlet, gas outlet and
Catalyst self-unloading mouth is respectively fixedly connected in lower head outer surface, and air inlet is connected to atmolysis cylinder entrance, if atmolysis cylinder outlet with
The connection of dry heat exchanger tube, gas outlet and catalyst self-unloading mouth are connected to lower head inside, manhole pipe orifice and relief valve respectively with upper envelope
Head outer surface is fixedly connected and is connected to upper cover inside.
Further, it is provided with before converter and/or blast furnace gas deoxygenation fine de-sulfur device net at the beginning of converter and/or blast furnace gas
Makeup is set, and just purification device includes sequentially connected dedusting detar device for converter and/or blast furnace gas, and compressor and TSA inhale
Adsorption device.
Further, the dedusting detar device is electrical tar precipitator.
Further, compressor is reciprocating compressor.
Further, TSA adsorbent equipment is alternating temperature carbon adsorption device.
The utility model compared with prior art the advantages of be:
The utility model is using the higher coal gas of the oxygen content qualified coal gas low with oxygen content is mixed, then
Mixed coal gas is passed through deoxidation reactor and carries out deoxidation treatment, obtains qualified regeneration gas, while a part of coal gas being passed through
Recycle compressor is recycled, and is mixed for the higher coal gas of oxygen content, be made gaseous mixture, entire simple process,
Energy consumption is small, can real-time online continuously to coal gas carry out deoxidation treatment.
Detailed description of the invention
Fig. 1 is the converter of the utility model and/or the schematic diagram of blast furnace gas deoxygenation fine de-sulfur device.
Fig. 2 is the flow chart that converter and/or blast furnace gas deoxygenation fine de-sulfur are realized using the device of the utility model.
Fig. 3 is that the structure of deoxidation reactor in the converter and/or blast furnace gas deoxygenation fine de-sulfur device of the utility model is shown
It is intended to.
Specific embodiment
In the description of the present invention, it should be understood that term " center ", " longitudinal direction ", " transverse direction ", " length ", " width
Degree ", " thickness ", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom" "inner", "outside", " suitable
The orientation or positional relationship of the instructions such as hour hands ", " counterclockwise ", " axial direction ", " radial direction ", " circumferential direction " is orientation based on the figure
Or positional relationship, be merely for convenience of describing the present invention and simplifying the description, rather than the device of indication or suggestion meaning or
Element must have a particular orientation, be constructed and operated in a specific orientation, therefore should not be understood as the limit to the utility model
System.In addition, defining " first ", the feature of " second " can explicitly or implicitly include one or more of the features.
In the description of the present invention, unless otherwise indicated, the meaning of " plurality " is two or more.
In the description of the present invention, it should be noted that unless otherwise clearly defined and limited, term " is pacified
Dress ", " connected ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or integrally
Connection；It can be mechanical connection, be also possible to be electrically connected；Can be directly connected, can also indirectly connected through an intermediary,
It can be the connection inside two elements.For the ordinary skill in the art, above-mentioned art can be understood with concrete condition
The concrete meaning of language in the present invention.
As shown in Figure 1-3, a kind of method of converter and/or blast furnace gas deoxygenation fine de-sulfur, the converter and/or blast furnace coal
The flow of gas is 28000-30000Nm3/ h, pressure 0.95-1Mpa, temperature are 38-42 DEG C；In effective component, carbon monoxide
Volume fraction be 40-60%, the volume fraction of carbon dioxide is 20-26%, and the volume fraction of nitrogen is 20-28%, hydrogen
Volume fraction be 1-4%, the volume fraction of oxygen is 0.6-1%, and the content of hydrogen phosphide is 100-250mg/kg, tar and ash
The content of dirt is not higher than 0.1mg/Nm3, the content of sulfide is 16-18mg/Nm3.Using deoxygenation fine de-sulfur device to the converter
And/or blast furnace gas deoxygenation fine de-sulfur.
The deoxygenation fine de-sulfur device includes coal gas of converter heat exchanger 301, and go into operation heater 302, circulating air water cooler
303, purified gas water cooler 304, hydrolysis desulfurization goes into operation heater 305, hydrolyzes desulfurizing tower, fine de-sulfur tower, deoxidation reactor 350,
Converter and/or blast furnace gas recycle compressor 360, circulating air liquid separation tank 370, wherein the hydrolysis desulfurizing tower includes structure phase
Same the first hydrolysis desulfurizing tower 310 and the second hydrolysis desulfurizing tower 320, the first hydrolysis desulfurizing tower 310 and the second hydrolysis desulfurization
Tower 320 is normally produced as serial flow using that can go here and there and can and be arranged, and when more catalyst changeout using parallel operation, the essence is de-
Sulphur tower includes identical first fine de-sulfur tower 330 of structure and the first fine de-sulfur tower 340, first fine de-sulfur tower 330 and first
Fine de-sulfur tower 340 is arranged in parallel, and one opens one standby, and tower is provided with desulfurizing agent, removes mercaptan and dimethyl two remaining in gas
Sulfide.
Converter and/or blast furnace gas gas holder hydrolyze desulfurizing tower, deoxidation reactor 350 successively with coal gas of converter heat exchanger 301
Connection, the deoxidation reactor 350 include shell 351, upper cover 352-1, lower head 352-2, and several heat exchanger tubes 353 divide gas
Cylinder 354, manhole pipe orifice 355, catalyst self-unloading mouth 356, air inlet 357, gas outlet 358 and relief valve 359；The shell 351
Pressure shell is connected and composed with upper cover 352-1 and lower head 352-2；Several heat exchanger tubes 353 are set to the shell 351
Interior and be fixedly connected with the atmolysis cylinder 354, the atmolysis cylinder 354 is fixedly connected in the lower head 352-2, the air inlet
Mouth 357, gas outlet 358 and catalyst self-unloading mouth 356 are respectively fixedly connected in the outer surface the lower head 352-2, the air inlet
Mouthfuls 357 be connected tos with 354 entrance of atmolysis cylinder, and the atmolysis cylinder 354 is exported and is connected to several heat exchanger tubes 353, it is described out
It is connected to inside port 358 and catalyst self-unloading mouth 356 and the lower head 352-2, the manhole pipe orifice 355 and relief valve 359
It is fixedly connected with the outer surface the upper cover 352-1 and is connected to the inside upper cover 352-1 respectively.Deoxidation catalyst is from de-
The manhole pipe orifice 355 of the upper cover 352-1 at 350 top of oxygen reactor is packed into, between several heat exchanger tubes 353 and anti-by deoxidation
356 discharging of catalyst self-unloading mouth for answering the lower head 352-2 of 350 bottom of device, it is further preferred that the catalyst self-unloading mouth
356 dischargings are 2, are arranged in the two sides the lower head 352-2.It is further preferred that the operation pressure of the deoxidation reactor 350
Power is 0.95-1.05Mpa, preferably 1Mpa, and operation temperature is 50-160 DEG C, and preferably 56 DEG C, catalyst filling particle diameter is ф 3-
4mm, 351 internal diameter of shell are 3700mm, and 350 whole height of deoxidation reactor is 8000mm.The outlet of deoxidation reactor 350 is set
Two branches are set, a branch hydrolyzes the pipeline connection of desulfurizing tower outlet and 350 entrance of deoxidation reactor with being connected to, in the branch
On, it is exported in connection hydrolysis desulfurizing tower outlet and the pipeline direction of 350 entrance of deoxidation reactor from deoxidation reactor 350, according to
It is secondary to be provided with circulating air water cooler 303, circulating air liquid separation tank 370 and converter and/or blast furnace gas recycle compressor 360；It is another
Successively with coal gas of converter heat exchanger 301, purified gas water cooler 304 is connected to the entrance of fine de-sulfur tower for branch；It is connected to the water
It solves and is provided with the branch that goes into operation on the entrance and the pipeline of converter and/or blast furnace gas gas holder of desulfurizing tower, the hydrolysis desulfurization goes into operation
The setting of heater 305 goes into operation on branch road described, is connected to the pipeline of hydrolysis desulfurizing tower outlet and 350 entrance of deoxidation reactor
On be provided with hydrolysis desulfurization and go into operation branch, the setting of heater 302 that goes into operation goes into operation on branch road in the hydrolysis desulfurization.
The method of deoxygenation fine de-sulfur includes the following steps:
S1), desulfurization
The converter and/or blast furnace gas are little by coal gas of converter heat exchanger 301 and the volume fraction of oxygen after deoxidation
In 0.7% the heat exchange of deoxidation coal gas be warming up to 55-65 DEG C after enter hydrolysis desulfurizing tower removing organic sulfur and inorganic sulfur, specific mistake
Journey is that converter and/or blast furnace gas will be in converters and/or blast furnace gas by the organic sulfur hydrolyst of hydrolysis desulfurizing tower
COS hydrolysis is H2S removes the H in gas subsequently into the desulfurizing agent bed of hydrolysis desulfurizing tower2S and other sulfide,
Other sulfide include dimethyl disulfide, one of methyl mercaptan and thiophene or multiple combinations.In converter and/or blast furnace gas deoxidation
Preceding carry out desulfurization process, the deoxidation catalyst avoided in the sulfide and deoxidation reactor in converter and/or blast furnace gas are anti-
It answers so that deoxidation catalyst fails.Before converter and/or blast furnace gas desulfurization, converter and/or blast furnace gas heat exchange are heated up, improved
The desulfurization effect of converter and/or blast furnace gas.
S042), mix
It is 0.001-0.005% by the volume fraction of converter and/or blast furnace gas and oxygen after step S1 desulfurization
The mixing of deoxidation circulating gas, control in mixed mixed gas, the volume fraction of oxygen is not more than 0.7%.
S043), deoxidation
The mixed mixed gas deoxidation of step S2, the volume fraction of the oxygen of the deoxidation coal gas after making deoxidation will be passed through
0.001-0.005%.
Deoxidation process is specially to pass through the mixed mixed gas of step S2 by 350 bottom lower head 352- of deoxidation reactor
Distribution is described to pass through the mixed mixed gas of step S2 to several heat exchanger tubes 353 after 2 air inlet 357 enters atmolysis cylinder 354
From bottom to top the deoxidation catalyst heat exchange between heat exchanger tube 353, the mixed mixed gas of process step S2 after heat exchange go out
The deoxidation catalyst across heat exchanger tube 353 carries out deoxygenation reaction from top to bottom after heat exchanger tube 353, after deoxygenation reaction, gas
It is discharged by gas outlet 358.Preferably, when the deoxidation reactor 350 exceeds safety value, relief valve 359 is automatically opened, deoxidation
Gas in reactor 350 is discharged by relief valve 359.The deoxidation reactor uses atmolysis cylinder 354 and uniformly distributed several heat exchange
Pipe guarantees to be evenly distributed by the mixed mixed gas deoxidation of step S042 and deoxidation catalyst, improves oxygen removal efficiency
Temperature simultaneously in entire deoxidation reactor is uniform, by the way that catalyst self-unloading mouth is arranged, realizes the self-unloading of deoxidation catalyst, subtracts
The labor intensity of deoxidation catalyst discharging is lacked.
S4), blending and fine de-sulfur
Deoxidation coal gas after step S3 deoxidation is divided into two steps point, and the deoxidation coal gas after a part of deoxidation is by following
Ring air water cooler 303, which cools, carries out gas-liquid separation by circulating air liquid separation tank 370 to after 35-45 DEG C, after gas-liquid separation
Gas is after converter and/or blast furnace gas recycle compressor are pressurized to 0.93-0.98Mpa as the deoxidation circulation in step S2
Coal gas and converter and/or blast furnace gas blending after step S1 desulfurization, guarantee in mixed mixed gas, the body of oxygen
Integration rate is not more than 0.7%, the liquids recovery after gas-liquid separation；Deoxidation coal gas after another part deoxidation is as in step S1
The deoxidation coal gas that the volume fraction of oxygen is 0.001-0.005% is by coal gas of converter heat exchanger 301 and converter and/or blast furnace coal
Gas heat exchange enters fine de-sulfur tower desulfurization after being cooled to 130-150 DEG C after purified gas water cooler 304 is cooled to 35-45 DEG C, takes off
Except mercaptan and dimethyl disulphide remaining in gas, purified gas is formed, the total sulfur content of the purified gas is not higher than
0.1mg/Nm3。
After step S4, the flow of converter and/or blast furnace gas is 28000- for converter and/or blast furnace gas
30000Nm3/ h, pressure 0.8-0.85Mpa, temperature are 38-42 DEG C；In effective component, the volume fraction of carbon monoxide is 45-
60%, the volume fraction of carbon dioxide is 20-26%, and the volume fraction of nitrogen is 20-28%, and the volume fraction of hydrogen is 1-
4%, the volume fraction of oxygen is 0.001-0.005%；The content of hydrogen phosphide is 100-250mg/kg, the content of tar and dust
Not higher than 0.1mg/Nm3, total sulfur content is not higher than 0.1mg/Nm3。
Preferably, circulating fan, the circulating fan and the converter and/or blast furnace gas recycle compressor are provided with
360 are arranged in parallel, and control in mixed mixed gas, and the volume fraction of oxygen is not more than 0.7%, by the deoxidation of step S3
Deoxidation gas temperature afterwards is not higher than 160 DEG C.Since coal gas of converter oxygen content is higher, and oxygen content fluctuation is larger, passes through setting
Circulating fan reduces entrance oxygen content, and the deoxidation catalyst realized in deoxidation reactor is long-term steady at a lower temperature
Fixed operation.
Preferably, converter and/or blast furnace gas deoxygenation fine de-sulfur go into operation when starting, and before step S1, heat the converter
And/or blast furnace gas is to 55-65 DEG C, to improve the desulfurization effect of converter and/or blast furnace gas；Before step S3, heating mixing
Mixed gas afterwards is to 55-65 DEG C, to improve deoxidation effect；During normal production, stop heating the converter and/or blast furnace gas
With mixed mixed gas.
Preferably, furnace and/or blast furnace gas deoxygenation fine de-sulfur go into operation when starting, control enter step S1 converter and/or
The mass flow of blast furnace gas is not more than the limiting value that deoxidation reactor is born, here, converter and/or the blast furnace gas of the application
Mass flow be 56791-88422kg/h, with guarantee and/or blast furnace gas deoxygenation fine de-sulfur go into operation when starting, control enter
The converter of step S1 and/or the mass flow of blast furnace gas are not more than the limiting value that deoxidation reactor is born.
Before the converter and/or blast furnace gas deoxygenation fine de-sulfur device go into operation, needed before deoxidation catalyst normal use into
Row reduction, detailed process is as follows:
A), start converter and/or blast furnace gas recycle compressor 360 and carry out nitrogen circulation, circulation process be converter and/or
Blast furnace gas 360 → coal gas of converter of recycle compressor heat exchanger 301 → hydrolysis desulfurization go into operation heater 305 → hydrolysis desulfurizing tower →
Go into operation return after heater 302 → deoxidation reactor, 350 → circulating air water cooler 303 → circulating air liquid separation tank 370 converter and/or
Blast furnace gas recycle compressor 360.
B), nitrogen is heated to 170-180 DEG C using heater 302 is gone into operation, deoxidation catalyst is finally warming up to 170 DEG C
Constant temperature afterwards, then gradually fill into converter and/or blast furnace gas.
Preferably, the heater 305 that needs to go into operation to hydrolysis desulfurization before filling into converter and/or blast furnace gas passes through steam
Hydrolysis desulfurizing tower temperature is lifted temperature to 60 DEG C by heating, temperature is then lifted temperature to 180 DEG C, control enters deoxidation reactor 350
CO content, until the volume fraction of CO is to 3-4% and imports and exports CO content and does not change, reduction terminates.
C deoxidation reactor temperature is down to 80 DEG C after) reduction is good, adjusts material gas quantity, starts normal production.
When the converter and/or blast furnace gas deoxygenation fine de-sulfur device are stopped work, gradually reduce and until stop converter and/or
Blast furnace gas enters device, starts circulating fan, increases internal circulating load, and deoxidation reactor 350 is changed to circulation process, and circulation process is
Converter and/or blast furnace gas 360 → coal gas of converter of recycle compressor heat exchanger 301 → hydrolysis desulfurization go into operation 305 → water of heater
It is returned after solution desulfurizing tower → heater 302 → deoxidation reactor, the 350 → circulating air water cooler 303 → circulating air liquid separation tank 370 that goes into operation
Rotary furnace and/or blast furnace gas recycle compressor 360 maintain system pressure, are then gradually down to deoxidation catalyst temperature often
Temperature stops circulating fan.
Preferably, before step S1, purification device at the beginning of using converter and/or blast furnace gas passes through converter and/or blast furnace gas
It crosses converter and/or blast furnace gas just purifies, just the flow of the converter before purification and/or blast furnace gas is 28000-30000Nm3/
H, pressure 0.003-0.005Mpa, temperature are 18-22 DEG C；In effective component, the volume fraction of carbon monoxide is 40-60%,
The volume fraction of carbon dioxide is 20-26%, and the volume fraction of nitrogen is 20-28%, and the volume fraction of hydrogen is 1-4%, oxygen
The volume fraction of gas is 0.6-1%；The content of hydrogen phosphide is 100-250mg/kg, and the content of tar and dust is 0.01-
0.02g/Nm3, the content of sulfide is 16-18mg/Nm3。
Just purification device includes sequentially connected dedusting detar device for the converter and/or blast furnace gas, compressor and
TSA adsorbent equipment；Preferably, the dedusting detar device is electrical tar precipitator, and the compressor is reciprocating compressor, institute
Stating TSA adsorbent equipment is alternating temperature carbon adsorption device.
Converter and/or blast furnace gas, which just purify, to be included the following steps:
S01), dedusting detar
Using dedusting detar device, preferably electrical tar precipitator to the converter and/or dedusting of blast furnace gas and detar,
Dust and tar total amount in the converter and/or blast furnace gas is set to be not higher than 3mg/Nm3。
S02), compress
Using compressor, preferably reciprocating compressor compresses the converter for passing through step S01 and/or blast furnace gas to 0.95-
1Mpa。
S03), clean
Using TSA adsorbent equipment, preferably alternating temperature carbon adsorption device, converter and/or blast furnace gas removal of impurities to step S02,
Make the impurity content in the converter and/or blast furnace gas not higher than 0.1mg/Nm3.The impurity is tar and/or dust.
Embodiment 1
A kind of method of converter and/or blast furnace gas deoxygenation fine de-sulfur,
Include the following steps:
S0), converter and/or the first purification of blast furnace gas
Just the flow of the converter before purification and/or blast furnace gas is 29000Nm3/ h, pressure 0.005Mpa, temperature 20
℃；In effective component, the volume fraction of carbon monoxide is 48%, and the volume fraction of carbon dioxide is 24.5%, the volume of nitrogen
Dividing rate is 24.37%, and the volume fraction of hydrogen is 2%, and the volume fraction of oxygen is 1%；The content of hydrogen phosphide is 200mg/kg,
The content of tar and dust is 0.015g/Nm3, the content of sulfide is 17.7mg/Nm3。
Converter and/or blast furnace gas, which just purify, to be included the following steps:
S01), dedusting detar
Using electrical tar precipitator to the converter and/or dedusting of blast furnace gas and detar, make the converter and/or blast furnace
Dust and tar total amount in coal gas are not higher than 3mg/Nm3。
S02), compress
The converter for passing through step S01 and/or blast furnace gas are compressed using reciprocating compressor to 1Mpa.
S03), clean
Using alternating temperature carbon adsorption device, converter and/or blast furnace gas removal of impurities to step S02 make the converter and/or height
Impurity content in producer gas is not higher than 0.1mg/Nm3。
The flow of first purified converter and/or blast furnace gas is 29000Nm3/ h, pressure 0.97Mpa, temperature 40
℃；The volume fraction of carbon monoxide is 48% in effective component；The volume fraction of carbon dioxide is 24.5%, the volume point of nitrogen
Rate is 24.37%, and the volume fraction of hydrogen is 2%, and the volume fraction of oxygen is 1%, and the content of hydrogen phosphide is 200mg/kg, tar
Content with dust is 0.015g/Nm3, the content of sulfide is 17.7mg/Nm3。
S01), desulfurization
The converter and/or blast furnace gas are little by coal gas of converter heat exchanger 301 and the volume fraction of oxygen after deoxidation
In 0.7% the heat exchange of deoxidation coal gas be warming up to 60 DEG C after enter hydrolysis desulfurizing tower removing organic sulfur and inorganic sulfur.
S02), mix
The deoxidation for being 0.003% by the volume fraction of converter and/or blast furnace gas and oxygen after step S01 desulfurization
Circulating gas mixing, controls in mixed mixed gas, and the volume fraction of oxygen is not more than 0.7%.
S03), deoxidation
The mixed mixed gas deoxidation of step S02, the volume fraction of the oxygen of the deoxidation coal gas after making deoxidation will be passed through
It is 0.003%.
S04), blending and fine de-sulfur
Deoxidation coal gas after step S03 deoxidation is divided into two steps point, and the deoxidation coal gas after a part of deoxidation passes through
Circulating air water cooler 303 cools to after 40 DEG C and carries out gas-liquid separation by circulating air liquid separation tank 370, the gas after gas-liquid separation
Body after converter and/or blast furnace gas recycle compressor are pressurized to 0.95Mpa as in step S02 deoxidation circulating gas with
Converter and/or blast furnace gas blending after step S01 desulfurization, guarantee in mixed mixed gas, the volume point of oxygen
Rate is not more than 0.7%, the liquids recovery after gas-liquid separation；Deoxidation coal gas after another part deoxidation is as the oxygen in step S01
The deoxidation coal gas that the volume fraction of gas is 0.003% is dropped by coal gas of converter heat exchanger 301 and converter and/or blast furnace gas heat exchange
Temperature removes sulphur remaining in gas to fine de-sulfur tower desulfurization is entered after 140 DEG C after purified gas water cooler 304 is cooled to 40 DEG C
Alcohol and dimethyl disulphide, form purified gas, and the total sulfur content of the purified gas is not higher than 0.1mg/Nm3。
The flow of converter and/or blast furnace gas after step S04 is 29000Nm3/ h, pressure 0.82Mpa, temperature
It is 40 DEG C；In effective component, the volume fraction of carbon monoxide is 48.48%, and the volume fraction of carbon dioxide is 24.75%, nitrogen
The volume fraction of gas is 24.62%, and the volume fraction of hydrogen is 2.02%, and the volume fraction of oxygen is 0.003%；Hydrogen phosphide
Content is 200mg/kg, and the content of tar and dust is not higher than 0.1mg/Nm3, total sulfur content is not higher than 0.1mg/Nm3。
In the description of this specification, reference term " one embodiment ", " some embodiments ", " illustrative examples ",
The description of " example ", " specific example " or " some examples " etc. means specific features described in conjunction with this embodiment or example, knot
Structure, material or feature are contained at least one embodiment or example of the utility model.In the present specification, to above-mentioned art
The schematic representation of language may not refer to the same embodiment or example.Moreover, description specific features, structure, material or
Person's feature can be combined in any suitable manner in any one or more of the embodiments or examples.
While there has been shown and described that the embodiments of the present invention, it will be understood by those skilled in the art that:
These embodiments can be carried out with a variety of variations, modification, replacement in the case where not departing from the principles of the present invention and objective
And modification, the scope of the utility model are defined by the claims and their equivalents.
Claims (9)
1. a kind of converter and/or blast furnace gas deoxygenation fine de-sulfur device, it is characterised in that:
Including hydrolyzing desulfurizing tower, deoxidation reactor and fine de-sulfur tower；Hydrolyze the entrance and converter and/or blast furnace gas gas of desulfurizing tower
Cabinet connection, outlet be connected to the entrance of deoxidation reactor, deoxidation reactor export is arranged two branches, a branch be connected to water
The pipeline connection of desulfurizing tower outlet and deoxidation reactor entrance is solved, another branch is connected to the entrance of fine de-sulfur tower.
2. the apparatus according to claim 1, it is characterised in that:
It is connected to the branch road of deoxidation reactor outlet and connection hydrolysis desulfurizing tower outlet and deoxidation reactor entrance pipe, from deoxidation
Reactor outlet, on the pipeline direction of deoxidation reactor entrance, is disposed with circulation air water to connection hydrolysis desulfurizing tower outlet
Cooler, circulating air liquid separation tank and converter and/or blast furnace gas recycle compressor.
3. the apparatus according to claim 1, it is characterised in that:
Including coal gas of converter heat exchanger and purified gas water cooler, coal gas of converter heat exchanger is arranged in the entrance of hydrolysis desulfurizing tower and turns
Between furnace and/or blast furnace gas gas holder, while the setting of coal gas of converter heat exchanger is in the outlet of connection deoxidation reactor and fine de-sulfur tower
The branch road of entrance, purified gas water cooler are arranged on the branch road between coal gas of converter heat exchanger and fine de-sulfur tower.
4. the apparatus according to claim 1, it is characterised in that:
Including going into operation heater and hydrolysis desulfurization goes into operation heater, the entrance and converter and/or blast furnace coal of connection hydrolysis desulfurizing tower
Be provided with the branch that goes into operation on the pipeline of gas gas holder, the heater that goes into operation setting is going into operation on branch road, connection hydrolysis desulfurizing tower outlet with
It is provided with hydrolysis desulfurization on the pipeline of deoxidation reactor entrance to go into operation branch, hydrolysis desulfurization goes into operation heater setting in hydrolysis desulfurization
The branch that goes into operation road.
5. the apparatus according to claim 1, it is characterised in that: deoxidation reactor includes shell, upper cover, lower head, if
Dry heat exchanger tube, atmolysis cylinder, manhole pipe orifice, catalyst self-unloading mouth, air inlet, gas outlet and relief valve；Shell and upper cover and under
End socket connects and composes pressure shell；Several heat exchanger tubes are set in shell and are fixedly connected with atmolysis cylinder, and atmolysis cylinder is fixedly connected
In in lower head, air inlet, gas outlet and catalyst self-unloading mouth are respectively fixedly connected in lower head outer surface, air inlet and divide gas
Cylinder entrance connection, atmolysis cylinder outlet are connected to several heat exchanger tubes, are connected to inside gas outlet and catalyst self-unloading mouth and lower head, people
Hole nozzle and relief valve are fixedly connected with upper cover outer surface respectively and are connected to upper cover inside.
6. the apparatus according to claim 1, it is characterised in that:
Converter and/or blast furnace gas just purification device, converter are provided with before converter and/or blast furnace gas deoxygenation fine de-sulfur device
And/or just purification device includes sequentially connected dedusting detar device, compressor and TSA adsorbent equipment to blast furnace gas.
7. device according to claim 6, it is characterised in that: the dedusting detar device is electrical tar precipitator.
8. device according to claim 6, it is characterised in that: compressor is reciprocating compressor.
9. device according to claim 6, it is characterised in that: TSA adsorbent equipment is alternating temperature carbon adsorption device.
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| CN201821186428.XU CN208748034U (en) | 2018-07-25 | 2018-07-25 | A kind of converter and/or blast furnace gas deoxygenation fine de-sulfur device |
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| CN201821186428.XU CN208748034U (en) | 2018-07-25 | 2018-07-25 | A kind of converter and/or blast furnace gas deoxygenation fine de-sulfur device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114317849A (en) * | 2021-11-26 | 2022-04-12 | 清华大学 | Water control equipment for blast furnace gas |
| CN114456848A (en) * | 2022-02-23 | 2022-05-10 | 山西沃能化工科技有限公司 | Device and method for deoxidizing and desulfurizing converter gas |
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2018
- 2018-07-25 CN CN201821186428.XU patent/CN208748034U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114317849A (en) * | 2021-11-26 | 2022-04-12 | 清华大学 | Water control equipment for blast furnace gas |
| CN114456848A (en) * | 2022-02-23 | 2022-05-10 | 山西沃能化工科技有限公司 | Device and method for deoxidizing and desulfurizing converter gas |
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