CN109351144A - The purification production system and technique of converter gas - Google Patents
The purification production system and technique of converter gas Download PDFInfo
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- CN109351144A CN109351144A CN201811454529.5A CN201811454529A CN109351144A CN 109351144 A CN109351144 A CN 109351144A CN 201811454529 A CN201811454529 A CN 201811454529A CN 109351144 A CN109351144 A CN 109351144A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/485—Sulfur compounds containing only one sulfur compound other than sulfur oxides or hydrogen sulfide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8603—Removing sulfur compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/10—Single element gases other than halogens
- B01D2257/104—Oxygen
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
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- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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Abstract
The present invention relates to be related to the technical field of converter gas production ethylene glycol purification process, the specially purification production system and technique of converter gas, dust removing means, compression set, temp.-changing adsorption exclusion device, the thick desulfurizer of deoxygenation, fine de-sulfur device, pressure-changeable adsorption decarbonization device and hydramine method decarbonization device including being sequentially connected in series setting；When system works, coal gas of converter import is passed through coal gas of converter, and coal gas of converter enters dust removing means, removes 70% ~ 80% dust in coal gas of converter；The pressurized gas of 40 DEG C of temperature, pressure 1.0MPaG is obtained through compression set；It by the COS hydrolysis in the coal gas that cleans is H through deoxygenation desulfurizer through temp.-changing adsorption exclusion device2S, and then remove H2S, and slough the oxygen in removal of impurities coal gas；Deoxygenation desulfurization coal gas removes mercaptan and dimethyl disulphide through fine de-sulfur device；Fine de-sulfur coal gas is by pressure-changeable adsorption decarbonization device removing sulfide and CO2；CO is further removed through hydramine method decarbonization device2, mechanical admixture and free fluid, be purified coal gas.
Description
Technical field
The present invention relates to the technical field of converter gas production ethylene glycol purification process is related to, the specially purification of converter gas is raw
Production system and technique.
Background technique
Refinery's tail gas of converter contains 50% or so CO, can produce ethylene glycol using it as raw material.Have compared to coal-ethylene glycol and throws
Money province, huge advantage at low cost.And for steel, coking industry, this is also abundant excavation coke oven tail gas, converter tail
The potential of the tail gas such as gas, blast furnace tail gas produces the chemical products of high added value, be steel, coking industry cost efficiency it is fine
Selection.But contain tar, dust, inorganic sulfur, organic sulfur, oxygen, fluoride, hydrogen phosphide and carbon dioxide etc. in tail gas of converter
Impurity needs to be purified by the processes such as cleaning, purifying.Because of organic sulfur type complexity, hydrogen phosphide, oxygen content in tail gas
The selection of height, purification process process and catalyst is extremely important.
Summary of the invention
In order to realize the purification of converter gas, the present invention provides the purification production system and technique of a kind of converter gas；It realizes and turns
Furnace gas removal of impurities, deoxidation, desulfurization, dephosphorization, decarburization etc., can effectively reduce operating cost under the premise of safe and stable, under satisfaction
Swim the requirement of glycol unit carbonylation, carbon monoxide purity.
Specific technical solution is the purification production system of converter gas, dust removing means, pressure including being sequentially connected in series setting
Compression apparatus, temp.-changing adsorption exclusion device, deoxygenation desulfurizer, pressure-changeable adsorption decarbonization device and hydramine method decarbonization device.
The dust removing means includes the electrostatic precipitator A10 and electrostatic precipitator B11 being arranged in parallel.
The compression set includes the screw compression mechanism for being sequentially connected in series setting, cooler 22 and gas-liquid separator I 23.
The temp.-changing adsorption exclusion device includes oil removing tower 30 and 10 or more temperature-change adsorption tower 31, and described 10 or more become
It connects after warm 31 parallel connection of adsorption tower with oil removing tower 30.
The deoxygenation desulfurizer includes the thick desulfurizer of concatenated deoxygenation and fine de-sulfur device.
The thick desulfurizer of deoxygenation includes the coal gas of converter heat exchanger 40 for being sequentially connected in series setting, hydrolysis desulfurizing tower A41, water
Solve desulfurizing tower B42 and deoxidation reactor 43；The outlet at bottom of the deoxidation reactor 43 is divided into two-way, has been sequentially connected in series follows all the way
Ring air water cooler 44, circulating air liquid separation tank 45 and coal gas of converter recycle compressor 46, the coal gas of converter recycle compressor 46 go out
Mouth pipeline is connected to 43 top inlet of deoxidation reactor；Another way by pipeline be connected to the shell side of coal gas of converter heat exchanger 40 into
Mouthful；The shell-side outlet of the coal gas of converter heat exchanger 40 is connected to the import of purified gas water cooler by pipeline；The hydrolysis desulfurizing tower
A41 and hydrolysis desulfurizing tower B42 set organic sulfur hydrolyst bed and desulfurizing agent bed from bottom to top.
The fine de-sulfur device includes the fine de-sulfur tower A50 and fine de-sulfur tower B51 being arranged in parallel.
The pressure-changeable adsorption decarbonization device includes the gas-liquid separator II 60, decarburization adsorbing mechanism and purified gas being sequentially connected in series
Surge tank 62, the decarburization adsorbing mechanism includes the decarburization absorber 61 of 8 more parallels setting, in every decarburization absorber 61
It is filled with silica type adsorbent.The hydramine method decarbonization device includes converter air filter 70, the converter gas for being sequentially connected in series setting
Absorption tower 71, converter Gas Cooler 72, converter gas separating device 73 and converter gas tower top filter 74, the converter gas absorption tower 71
Top spray equipment N methyldiethanol amine import is connected to by pipeline.
When system works, coal gas of converter import is passed through coal gas of converter, and coal gas of converter enters dust removing means, removes converter
70% ~ 80% dust in coal gas, obtains dedusting coal gas；Dedusting coal gas obtains 40 DEG C of temperature, pressure through compression set
The pressurized gas of 1.0MPaG；Pressurized gas through temp.-changing adsorption exclusion device, the preliminary oil removed in pressurized gas, dust, water,
Hydrogen phosphide and hydrogen fluoride obtain removal of impurities coal gas；Removal of impurities coal gas through deoxygenation desulfurizer by clean coal gas in COS hydrolysis be
H2S, and then remove H2S, and the oxygen in removal of impurities coal gas is sloughed, obtain deoxygenation desulfurization coal gas；Deoxygenation desulfurization coal gas is filled through fine de-sulfur
Removing mercaptan and dimethyl disulphide are set, fine de-sulfur coal gas is obtained, sulfur content is less than 0.1ppm, oxygen in the fine de-sulfur coal gas
Content is less than 30ppm；Fine de-sulfur coal gas is by pressure-changeable adsorption decarbonization device removing sulfide and CO2, obtain decarburization coal gas；Decarburization
Coal gas further removes CO through hydramine method decarbonization device2, mechanical admixture and free fluid, be purified coal gas, the purification coal
The dust content < 0.1ppm(m% of gas), total sulfur content < 0.1ppm(m%), oxygen content is less than 30ppm(v%) and, CO2Content≤
20ppm(v%), hydrogen phosphide, hydrogen fluoride content < 0.1ppm(v%)；It purifies CO content in coal gas and is greater than 60%.
Further, the electrostatic precipitator A10 in the dust removing means and electrostatic precipitator B11 is that cellular electrostatic removes
The outlet at bottom of dirt device, electrostatic precipitator A10 and electrostatic precipitator B11 pass through the underground that pipeline is connected in underground tank respectively
Slot pump 12.
Further, the compression mechanism includes 5 helical-lobe compressors being arranged in parallel 20, and every power is 1866KW, institute
The import series connection for stating compression mechanism is equipped with admission air silencer 25 and air intake filter 24, and the outlet of compression mechanism is equipped with exhaust noise silencing
Device 21.
Further, the top of every temperature-change adsorption tower 31 pass through pipeline be connected to regenerator heater I 32 go out
Mouthful, the bottom of every temperature-change adsorption tower 31 passes through the import that pipeline is connected to regenerator heater I 32；The regenerator heating
Device I 32 is shell-and-tube heat exchanger.
Further, the tempreture organic sulphur hydrolysis of the hydrolysis desulfurizing tower A41 in the thick desulfurizer of the deoxygenation and hydrolysis desulfurizing tower B42
Catalyst bed fills activity Al2O3, additive, promotor；Desulfurizing agent bed is filled with active carbon activating agent and auxiliary agent.
Further, the top inlet of the fine de-sulfur tower A50 and fine de-sulfur tower B51 passes through pipeline respectively and is communicated with regeneration gas
Fuel gas pipe network is connected by pipeline in heater II 52, top；The regeneration hot-air heater II 52 is shell-and-tube heat exchanger.
Further, the pressure-changeable adsorption decarbonization device further includes 2 equalizer tanks 63, and each equalizer tank 63 is respectively and each de-
Carbon adsorption device 61 is in parallel, and water-ring vacuum pump 64 is connected by pipeline in the bottom of each decarburization absorber 61.
Further, converter gas absorption tower 71, converter gas separating device 73 and the converter gas tower in the hydramine method decarbonization device
Extraneous desorption unit is connected in the bottom for pushing up filter 74 by pipeline.
It further include the purification production technology of the purification production system of converter gas, specifically includes the following steps:
(1) dust removes
Converter gas respectively enters electrostatic precipitator A10 and electrostatic precipitator B11, the dust of removing 70% ~ 80%；Obtain dedusting coal
Gas, dedusting gas temperature is 20 DEG C, pressure 0.003MPaG.
(2) it compresses
Dedusting coal gas enters compression set, by dedusting gas compression to 1.0MPaG；Dedusting coal gas goes out compression set successively through being subcooled
But device 22 is cooled to 40 DEG C, through I 23 liquid separation of gas-liquid separator；Obtain pressurized gas and coal gas of converter lime set.
(3) temp.-changing adsorption removal of impurities (TSA removal of impurities)
Pressurized gas is passed through oil removing tower 30 from tower bottom, oil, dust, water in pressurized gas is removed, obtains except oil gas；Oil removing
If coal gas respectively enters the tower bottom of 6 temperature-change adsorption towers 31 in parallel, except hydrogen phosphide, the hydrogen fluoride in oil gas be adsorbed it is de-
It removes；Obtain removal of impurities coal gas.
(4) the thick desulfurization of deoxygenation
Removal of impurities coal gas is changed the heat exchange of coal gas of converter heat exchanger 40, and temperature is that 60 DEG C of removal of impurities coal gas sequentially enters hydrolysis desulfurizing tower
A41 and hydrolysis desulfurizing tower B42, acting on through hydrolyzation catalysis by COS hydrolysis is H2S, then through in fine de-sulfur removing gas
H2S obtains desulfurization coal gas；Oxygen is removed through deoxidation reactor 43 after desulfurization coal gas and the mixing of deoxidation circulating air, obtains deoxygenation desulfurization
Coal gas；Deoxygenation desulfurization coal gas is divided into two-way, and deoxygenation desulfurization coal gas cools through circulating air water cooler 44 to 40 DEG C all the way, then passes through
Circulating air liquid separation tank 45 goes converter gas recycle compressor to be pressurized to 0.95MPag after separation water outlet, obtains the participation of deoxidation circulating air
System circulation；Another way deoxygenation desulfurization coal gas enters coal gas of converter heat exchanger 40, is cooled to 60 DEG C through heat exchange and goes to fine de-sulfur work
Sequence.
(5) fine de-sulfur
The purified air water cooler of deoxygenation desulfurization coal gas removes fine de-sulfur tower A50 or fine de-sulfur tower B51 after being cooled to 40 DEG C；Fine de-sulfur tower
A50 and fine de-sulfur tower B51 is equipped with desulfurizing agent, removes mercaptan and dimethyl disulphide remaining in deoxygenation desulfurization coal gas, obtains
To fine de-sulfur coal gas；The fine de-sulfur coal gas sulfur content is less than 0.1ppm, and oxygen content is less than 30ppm.
(6) pressure swing adsorption decarbonization (PSA-CO2)
Fine de-sulfur coal gas enters gas-liquid separator II 60 at 0.85MPa, isolates saturation moisture, obtains dehydration fine de-sulfur coal
Gas；Dehydration fine de-sulfur coal gas respectively enters the bottom of 8 decarburization absorbers 61 in parallel, the adsorbent bed of the decarburization absorber 61
Inside it is filled with silica type adsorbent；The impurity composition CO being dehydrated in fine de-sulfur coal gas2It is adsorbed by adsorbent, weakly stable matter component is
H2、N2、CO、CH4From bottom to top by adsorbent bed, is flowed out in pressure 0.8MPa condition from 61 top of decarburization absorber, obtain decarburization
Coal gas.
(7) hydramine method decarburization (MDEA)
Through converter air filter 70 at pressure 0.8MPaG, primary filtration removes free fluid, obtains gas I decarburization coal gas；Gas
Body I enters 71 bottom of converter gas absorption tower, with top-down activation N methyldiethanol amine (MDEA) solution in absorption tower
Reverse contact heat-exchanging, the CO in gas I2It is absorbed into liquid phase, obtains gas II；Gas II flows at the top of converter gas absorption tower 71
Out, converter gas separator 73, isolated gas III are entered after converter Gas Cooler 72 is cooled to 40 DEG C；Gas III is from converter
It is flowed out at the top of gas separating device 73, into converter gas tower top filter 74, completely removes trip through the separation of converter gas tower top filter 74
Chaotropic body is purified coal gas, the dust content < 0.1ppm(m% of the purification coal gas), total sulfur content < 0.1ppm(m%),
Oxygen content is less than 30ppm(v%), CO2Content≤20ppm(v%), hydrogen phosphide, hydrogen fluoride < 0.1ppm(v%), purify in coal gas
The content of CO is greater than 60%；The purification coal gas goes to downstream pressure-variable adsorption and mentions CO workshop section.
Further, at 120~180 DEG C, the adsorbent in temperature-change adsorption tower 31 is regenerated；Fine de-sulfur tower A50 and essence
The regeneration of desulfurizing tower B51, which is used, is heated to 200 DEG C of regeneration for regeneration gas；The regeneration of decarburization absorber 61 uses water circulating type vacuum pump
It extracts decarburization and parses agent.
The beneficial effect comprise that
(1) present invention realizes the purification of converter gas, tar, dust content < 0.1ppm(m% in purified converter gas), total sulfur
Content < 0.1ppm(m%), oxygen content is less than 30ppm(v%), CO2Content≤20ppm(v%), PH3< 25ppm(v%), purify coal
CO content is greater than 60% in gas, mentions CO by downstream pressure-variable adsorption, meets the purity requirement as ethylene glycol unstripped gas.
(2) design of converter gas deaerating type of cycles use after deoxidation gas low temperature loop control coal gas of converter oxygen content 0.7% with
Under, reaction temperature rising is reduced, CO is avoided and disproportionated reaction (2CO=C+CO2, while releasing a large amount of heat) occurs, increase system peace
While full property, energy consumption is reduced.
(3) pressure swing adsorption decarbonization is in conjunction with MDEA method decarburization, than using MDEA method to remove CO merely2, saving steam 20 ~
25%, so that system energy consumption is greatly reduced, to save operating cost.
Detailed description of the invention
Fig. 1 is that dust removes system diagram.
Fig. 2 is compressibility figure.
Fig. 3 is temp.-changing adsorption removal of impurities (TSA) system diagram.
Fig. 4 is deoxygenation fine de-sulfur system diagram.
Fig. 5 is deoxygenation fine de-sulfur system diagram.
Fig. 6 pressure swing adsorption decarbonization (PSA-CO2) system diagram.
Fig. 7 hydramine method (MDEA) decarbonization system figure.
Fig. 8 converter gas purification process system diagram.
Wherein: 10- electrostatic precipitator A；11- electrostatic precipitator B；12- underground tank pump；20- helical-lobe compressor；21- exhaust
Muffler；22- cooler；23- gas-liquid separator I；24- air intake filter；25- admission air silencer；30- oil removing tower；31- alternating temperature
Adsorption tower；32- regenerator heater I；40- coal gas of converter heat exchanger；41- hydrolyzes desulfurizing tower A；42- hydrolyzes desulfurizing tower B；43- is de-
Oxygen reactor 43；44- circulating air water cooler；45- circulating air liquid separation tank；46- coal gas of converter recycle compressor；47- hydrolyzes desulfurization
Go into operation heater；48- goes into operation heater；50- fine de-sulfur tower A；51- fine de-sulfur tower B；52- regenerates hot-air heater II；60- gas-liquid
Separator II；61- decarburization absorber；62- purified gas surge tank；63- equalizer tank；64- water-ring vacuum pump；70- converter gas mistake
Filter；71- converter gas absorption tower；72- converter Gas Cooler；73- converter gas separating device；74- converter gas tower top filter.
Specific embodiment
In order to make the objectives, technical solutions, and advantages of the present invention clearer, with reference to the accompanying drawings and embodiments, right
The present invention is further elaborated.It should be appreciated that the specific embodiments described herein are only used to explain the present invention,
It is not intended to limit the present invention.
Embodiment 1
The purification production system of converter gas, it is characterised in that: including be sequentially connected in series the dust removing means of setting, compression set,
Temp.-changing adsorption exclusion device, the thick desulfurizer of deoxygenation, fine de-sulfur device, pressure-changeable adsorption decarbonization device and hydramine method decarbonization device.
The dust removing means includes the electrostatic precipitator A10 and electrostatic precipitator B11 being arranged in parallel；The dust is de-
Except in device electrostatic precipitator A10 and electrostatic precipitator B11 be cellular electrostatic precipitator, electrostatic precipitator A10 and electrostatic
The outlet at bottom of deduster B11 passes through the underground tank pump 12 that pipeline is connected in underground tank respectively, electrostatic precipitator A10 and quiet
Electric precipitator B11 specification is 5000 × 12000mm of φ.
The compression set includes the screw compression mechanism for being sequentially connected in series setting, cooler 22 and gas-liquid separator I 23；Institute
Stating compression mechanism includes 5 helical-lobe compressors being arranged in parallel 20, and every power is 1866KW, the import string of the compression mechanism
Connection is equipped with admission air silencer 25 and air intake filter 24, and the outlet of compression mechanism is equipped with muffler 21.
The temp.-changing adsorption exclusion device includes oil removing tower 30 and 10 or more temperature-change adsorption tower 31, and described 10 or more become
It connects after warm 31 parallel connection of adsorption tower with oil removing tower 30；The top of every temperature-change adsorption tower 31 passes through pipeline and is connected to regeneration
The outlet of device heater I 32, the bottom of every temperature-change adsorption tower 31 pass through pipeline be connected to regenerator heater I 32 into
Mouthful；The regenerator heater I 32 is shell-and-tube heat exchanger, and I 32 specification of regenerator heater is 800 × 2500mm of φ, alternating temperature
31 specification of adsorption tower is 2800 × 9000mm of φ.
The thick desulfurizer of deoxygenation includes the coal gas of converter heat exchanger 40 for being sequentially connected in series setting, hydrolysis desulfurizing tower A41, water
Desulfurizing tower B42 and deoxidation reactor 43 are solved, deoxidation reactor 43 uses interior heat exchange type uniform-temperature reactor, can reduce bed temperature rise,
Reduce circulating flow rate.
The outlet at bottom of the deoxidation reactor 43 is divided into two-way, has been sequentially connected in series circulating air water cooler 44, circulation all the way
Gas liquid separation tank 45 and coal gas of converter recycle compressor 46, it is anti-that 46 outlet conduit of coal gas of converter recycle compressor is connected to deoxidation
Answer 43 top inlet of device；Another way is connected to the shell side import of coal gas of converter heat exchanger 40 by pipeline；The coal gas of converter changes
The shell-side outlet of hot device 40 is connected to the import of purified gas water cooler by pipeline；The hydrolysis desulfurizing tower A41 and hydrolysis desulfurizing tower B42
Organic sulfur hydrolyst bed and desulfurizing agent bed are set from bottom to top；Organic sulfur hydrolyst bed filling activity
Al2O3, additive, promotor, desulfurizing agent bed be filled with active carbon activating agent and auxiliary agent；The thick desulfurizer of deoxygenation further includes
Go into operation heat riser, and the heat riser that goes into operation is that hydrolysis desulfurization goes into operation and heater 4847 and goes into operation heater 48, the hydrolysis desulfurization
It goes into operation and is arranged in series in after heater 4847 and valve in parallel between converter gas heat exchanger and hydrolysis desulfurizing tower A41, it is described to go into operation
It is arranged in series in after heater 48 and valve in parallel between hydrolysis desulfurizing tower B42 and deoxidation reactor 43.
The fine de-sulfur device includes the fine de-sulfur tower A50 and fine de-sulfur tower B51 being arranged in parallel；The fine de-sulfur tower A50
Pass through pipeline respectively with the top inlet of fine de-sulfur tower B51 and be communicated with regeneration hot-air heater II 52, top is connected by pipeline fires
Expect gas pipe network；The regeneration hot-air heater II 52 is shell-and-tube heat exchanger, and specification is 600 × 2400mm of φ, in fine de-sulfur device
Fine de-sulfur tower A50 and fine de-sulfur tower B51 specification are 3200 × 11860mm of Φ.
The pressure-changeable adsorption decarbonization device includes the gas-liquid separator II 60, decarburization adsorbing mechanism and purified gas being sequentially connected in series
Surge tank 62, the decarburization adsorbing mechanism includes the decarburization absorber 61 of 8 more parallels setting, in every decarburization absorber 61
It is filled with silica type adsorbent；The pressure-changeable adsorption decarbonization device further includes 2 equalizer tanks 63, and each equalizer tank 63 is respectively and often
A decarburization absorber 61 is in parallel, and water-ring vacuum pump 64 is connected by pipeline in the bottom of each decarburization absorber 61, each
61 specification of decarburization absorber is 3000 × 12000mm of Φ.
The hydramine method decarbonization device includes the converter air filter 70 for being sequentially connected in series setting, converter gas absorption tower 71, turns
Burner-gas cooler 72, converter gas separating device 73 and converter gas tower top filter 74, the top spray on the converter gas absorption tower 71
Device is connected to N methyldiethanol amine import by pipeline；Converter gas absorption tower 71, converter gas separating device 73 and converter gas tower
Extraneous desorption unit is connected in the bottom for pushing up filter 74 by pipeline.
When system works, coal gas of converter import is passed through coal gas of converter, and coal gas of converter enters dust removing means, removes converter
70% ~ 80% dust in coal gas, obtains dedusting coal gas；Dedusting coal gas obtains 40 DEG C of temperature, pressure through compression set
The pressurized gas of 1.0MPaG；Pressurized gas through temp.-changing adsorption exclusion device, the preliminary oil removed in pressurized gas, dust, water,
Hydrogen phosphide and hydrogen fluoride obtain removal of impurities coal gas；Removal of impurities coal gas through deoxygenation desulfurizer by clean coal gas in COS hydrolysis be
H2S, and then remove H2S, and the oxygen in removal of impurities coal gas is sloughed, obtain deoxygenation desulfurization coal gas；Deoxygenation desulfurization coal gas is filled through fine de-sulfur
Removing mercaptan and dimethyl disulphide are set, fine de-sulfur coal gas is obtained, sulfur content is less than 0.1ppm, oxygen in the fine de-sulfur coal gas
Content is less than 30ppm；Fine de-sulfur coal gas is by pressure-changeable adsorption decarbonization device removing sulfide and CO2, obtain decarburization coal gas；Decarburization
Coal gas further removes CO through hydramine method decarbonization device2, mechanical admixture and free fluid, be purified coal gas, the purification coal
The dust content < 0.1ppm(m% of gas), total sulfur content < 0.1ppm(m%), oxygen content is less than 30ppm(v%) and, CO2Content≤
20ppm(v%), hydrogen phosphide, hydrogen fluoride content < 0.1ppm(v%)；It purifies CO content in coal gas and is greater than 60%.
Embodiment 2
According to the production technology of the purification production system of the converter gas of embodiment 1, specifically includes the following steps:
(1) dust removes
Converter gas respectively enters electrostatic precipitator A10 and electrostatic precipitator B11, the dust of removing 70% ~ 80%；Obtain dedusting coal
Gas, dedusting gas temperature is 20 DEG C, pressure 0.003MPaG.
(2) it compresses
Dedusting coal gas enters compression set, by dedusting gas compression to 1.0MPaG；Dedusting coal gas goes out compression set successively through being subcooled
But device 22 is cooled to 40 DEG C, through I 23 liquid separation of gas-liquid separator；Obtain pressurized gas and coal gas of converter lime set.
(3) temp.-changing adsorption removal of impurities (TSA removal of impurities)
Pressurized gas is passed through oil removing tower 30 from tower bottom, oil, dust, water in pressurized gas is removed, obtains except oil gas；Oil removing
If coal gas respectively enters the tower bottom of 6 temperature-change adsorption towers 31 in parallel, except hydrogen phosphide, the hydrogen fluoride in oil gas be adsorbed it is de-
It removes；Obtain removal of impurities coal gas；It is in parallel in this step alternately to adsorb and regenerate equipped with 10 temperature-change adsorption towers 31, wherein 6 changes
Warm adsorption tower 31 is in running order simultaneously, and 4 are in reproduced state, and the regeneration of temperature-change adsorption tower 31 is that temperature is 120~180
DEG C, the adsorbent in temperature-change adsorption tower 31 is regenerated.
(4) the thick desulfurization of deoxygenation
Removal of impurities coal gas is changed the heat exchange of coal gas of converter heat exchanger 40, and temperature is that 60 DEG C of removal of impurities coal gas sequentially enters hydrolysis desulfurizing tower
A41 and hydrolysis desulfurizing tower B42, two towers are normally produced as serial flow, use when more catalyst changeout using that can go here and there and can and be arranged
Parallel operation；Acting on through hydrolyzation catalysis by COS hydrolysis is H2S, then through the H in fine de-sulfur removing gas2S obtains desulfurization
Coal gas；Oxygen is removed through deoxidation reactor 43 after desulfurization coal gas and the mixing of deoxidation circulating air, obtains deoxygenation desulfurization coal gas；Deoxygenation desulfurization
Coal gas is divided into two-way, and deoxygenation desulfurization coal gas cools through circulating air water cooler 44 to 40 DEG C all the way, then through circulating air liquid separation tank
45, it goes converter gas recycle compressor to be pressurized to 0.95MPag after separation water outlet, obtains deoxidation circulating air and participate in system circulation；It is another
Road deoxygenation desulfurization coal gas enters coal gas of converter heat exchanger 40, is cooled to 60 DEG C through heat exchange and goes to fine de-sulfur process.
It wherein further include the heating process that goes into operation, going into operation to connect hydrolysis desulfurization when heating up and go into operation heater 47 and goes into operation heater
48, hydrolysis desulfurization go into operation heater 47 heating removal of impurities coal gas to 60 DEG C go to hydrolysis desulfurizing tower A41 and hydrolysis desulfurizing tower B42；It opens
Work heater 48 will enter the gas heat temperature raising of deoxidation reactor 43.
(5) fine de-sulfur
The purified air water cooler of deoxygenation desulfurization coal gas removes fine de-sulfur tower A50 or fine de-sulfur tower B51, parallel two towers after being cooled to 40 DEG C
Setting, one opens one standby, and the regeneration of fine de-sulfur tower A50 and fine de-sulfur tower B51, which are used, is heated to 200 DEG C of regeneration for regeneration gas；Essence is de-
Sulphur tower A50 and fine de-sulfur tower B51 is equipped with desulfurizing agent, removes mercaptan and dimethyl disulfide remaining in deoxygenation desulfurization coal gas
Object obtains fine de-sulfur coal gas；The fine de-sulfur coal gas sulfur content is less than 0.1ppm, and oxygen content is less than 30ppm.
(6) pressure swing adsorption decarbonization (PSA-CO2)
Fine de-sulfur coal gas enters gas-liquid separator II 60 at 0.85MPa, isolates saturation moisture, obtains dehydration fine de-sulfur coal
Gas；Dehydration fine de-sulfur coal gas respectively enters the bottom of 8 decarburization absorbers 61 in parallel, and parallel connection is equipped with 8 decarburization absorbers 61,
Wherein 2 work are in running order, and 6 are in reproduced state, and regeneration extracts decarburization using water circulating type vacuum pump and parses agent；
Silica type adsorbent is filled in the adsorbent bed of the decarburization absorber 61；The impurity composition being dehydrated in fine de-sulfur coal gas
CO2It is adsorbed by adsorbent, weakly stable matter component, that is, H2、N2、CO、CH4From bottom to top by adsorbent bed, in pressure 0.8MPa condition
It is flowed out from 61 top of decarburization absorber, obtains decarburization coal gas.
(7) hydramine method decarburization (MDEA)
Through converter air filter 70 at pressure 0.8MPaG, primary filtration removes free fluid, obtains gas I decarburization coal gas；Gas
Body I enters 71 bottom of converter gas absorption tower, with top-down activation N methyldiethanol amine (MDEA) solution in absorption tower
Reverse contact heat-exchanging, the CO in gas I2It is absorbed into liquid phase, obtains gas II；Gas II flows at the top of converter gas absorption tower 71
Out, converter gas separator 73, isolated gas III are entered after converter Gas Cooler 72 is cooled to 40 DEG C；Gas III is from converter
It is flowed out at the top of gas separating device 73, into converter gas tower top filter 74, completely removes trip through the separation of converter gas tower top filter 74
Chaotropic body is purified coal gas, the dust content < 0.1ppm(m% of the purification coal gas), total sulfur content < 0.1ppm(m%), oxygen
Content is less than 30ppm(v%), CO2Content≤20ppm(v%), hydrogen phosphide, hydrogen fluoride < (v%) purify the content of CO in coal gas
Greater than 60%；The purification coal gas goes to downstream pressure-variable adsorption and mentions CO workshop section；The liquid that wherein tower top filter is isolated is with MDEA
Solution goes to regenerate together.
As it will be easily appreciated by one skilled in the art that the foregoing is merely illustrative of the preferred embodiments of the present invention, not to
The limitation present invention, any modifications, equivalent substitutions and improvements made within the spirit and principles of the present invention should all include
Within protection scope of the present invention.
Claims (10)
1. the purification production system of converter gas, it is characterised in that: dust removing means, compression dress including being sequentially connected in series setting
It sets, temp.-changing adsorption exclusion device, deoxygenation desulfurizer, pressure-changeable adsorption decarbonization device and hydramine method decarbonization device；
The dust removing means includes the electrostatic precipitator A(10 being arranged in parallel) and electrostatic precipitator B(11)；
The compression set includes the screw compression mechanism for being sequentially connected in series setting, cooler (22) and gas-liquid separator I (23)；
The temp.-changing adsorption exclusion device includes oil removing tower (30) and 10 or more temperature-change adsorption tower (31), and described 10 or more become
It connects after warm adsorption tower (31) is in parallel with oil removing tower (30)；
The deoxygenation desulfurizer includes the thick desulfurizer of concatenated deoxygenation and fine de-sulfur device；
The thick desulfurizer of deoxygenation include the coal gas of converter heat exchanger (40) for being sequentially connected in series setting, hydrolysis desulfurizing tower A(41), water
Solve desulfurizing tower B(42) and deoxidation reactor (43)；The outlet at bottom of the deoxidation reactor (43) is divided into two-way, successively goes here and there all the way
Circulating air water cooler (44), circulating air liquid separation tank (45) and coal gas of converter recycle compressor (46), the coal gas of converter is associated with to follow
Ring compressor (46) outlet conduit is connected to deoxidation reactor (43) top inlet；Another way is connected to coal gas of converter by pipeline
The shell side import of heat exchanger (40)；The shell-side outlet of the coal gas of converter heat exchanger (40) is connected to purified gas water cooler by pipeline
Import；The hydrolysis desulfurizing tower A(41) and hydrolysis desulfurizing tower B(42) to set organic sulfur hydrolyst bed and essence from bottom to top de-
Sulphur agent bed；
The fine de-sulfur device includes the fine de-sulfur tower A(50 being arranged in parallel) and fine de-sulfur tower B(51)；
The pressure-changeable adsorption decarbonization device includes that the gas-liquid separator II (60), decarburization adsorbing mechanism and purified gas being sequentially connected in series delay
It rushes tank (62), the decarburization adsorbing mechanism includes the decarburization absorber (61) of 8 more parallels setting, every decarburization absorber
(61) silica type adsorbent is filled in；
The hydramine method decarbonization device includes the converter air filter (70) for being sequentially connected in series setting, converter gas absorption tower (71), turns
Burner-gas cooler (72), converter gas separating device (73) and converter gas tower top filter (74), the converter gas absorption tower (71)
Top spray equipment is connected to N methyldiethanol amine import by pipeline；
When system works, coal gas of converter import is passed through coal gas of converter, and coal gas of converter enters dust removing means, removes coal gas of converter
In 70% ~ 80% dust, obtain dedusting coal gas；Dedusting coal gas obtains 40 DEG C of temperature, pressure 1.0MPaG through compression set
Pressurized gas；Pressurized gas is through temp.-changing adsorption exclusion device, preliminary oil, dust, water, hydrogen phosphide and the fluorine removed in pressurized gas
Change hydrogen, obtains removal of impurities coal gas；COS hydrolysis in the coal gas that cleans is H through deoxygenation desulfurizer by removal of impurities coal gas2S, so it is de-
Except H2S, and the oxygen in removal of impurities coal gas is sloughed, obtain deoxygenation desulfurization coal gas；Deoxygenation desulfurization coal gas removes sulphur through fine de-sulfur device
Alcohol and dimethyl disulphide obtain fine de-sulfur coal gas, and sulfur content is less than 0.1ppm in the fine de-sulfur coal gas, and oxygen content is less than
30ppm；Fine de-sulfur coal gas is by pressure-changeable adsorption decarbonization device removing sulfide and CO2, obtain decarburization coal gas；Decarburization coal gas is through alcohol
Amine method decarbonization device further removes CO2, mechanical admixture and free fluid, be purified coal gas, the dust of the purification coal gas
Content < 0.1ppm(m%), total sulfur content < 0.1ppm(m%), oxygen content is less than 30ppm(v%) and, CO2Content≤20ppm
(v%), hydrogen phosphide, hydrogen fluoride < 0.1ppm(v%)；It purifies CO content in coal gas and is greater than 60%.
2. the purification production system of converter gas according to claim 1, it is characterised in that: in the dust removing means
Electrostatic precipitator A(10) and electrostatic precipitator B(11) be cellular electrostatic precipitator, electrostatic precipitator A(10) and electrostatic precipitation
Device B(11) outlet at bottom pass through the underground tank pump (12) that pipeline is connected in underground tank respectively.
3. the purification production system of converter gas according to claim 1, it is characterised in that: the compression mechanism include 5 simultaneously
Join the helical-lobe compressor (20) of setting, every power is 1866KW, and the import series connection of the compression mechanism is equipped with admission air silencer
(25) and air intake filter (24), the outlet of compression mechanism are equipped with muffler (21).
4. the purification production system of converter gas according to claim 1, it is characterised in that: every temperature-change adsorption tower (31)
Top pass through the outlet that pipeline is connected to regenerator heater I (32), the bottom of every temperature-change adsorption tower (31) passes through
Pipeline is connected to the import of regenerator heater I (32)；The regenerator heater I (32) is shell-and-tube heat exchanger.
5. the purification production system of converter gas according to claim 1, it is characterised in that: in the thick desulfurizer of deoxygenation
Hydrolyze desulfurizing tower A(41) and hydrolysis desulfurizing tower B(42) organic sulfur hydrolyst bed filling activity Al2O3, additive, rush
Into agent；Desulfurizing agent bed is filled with active carbon activating agent and auxiliary agent.
6. the purification production system of converter gas according to claim 1, it is characterised in that: the fine de-sulfur tower A(50) and essence
Desulfurizing tower B(51) top inlet pass through respectively pipeline be communicated with regeneration hot-air heater II (52), top by pipeline connect combustion
Expect gas pipe network；The regeneration hot-air heater II (52) is shell-and-tube heat exchanger.
7. the purification production system of converter gas according to claim 1, it is characterised in that: the pressure-changeable adsorption decarbonization device is also
Including 2 equalizer tanks (63), each equalizer tank (63) is in parallel with each decarburization absorber (61) respectively, each decarburization absorption
Water-ring vacuum pump (64) are connected by pipeline in the bottom of device (61).
8. the purification production system of converter gas according to claim 1, it is characterised in that: in the hydramine method decarbonization device
Converter gas absorption tower (71), converter gas separating device (73) and the bottom of converter gas tower top filter (74) pass through pipeline and connect outside
The desorption unit on boundary.
9. the purification production technology of the purification production system of any one converter gas, feature exist according to claim 1 ~ 8
In: specifically includes the following steps:
(1) dust removes
Converter gas respectively enters electrostatic precipitator A(10) and electrostatic precipitator B(11), the dust of removing 70% ~ 80%；Obtain dedusting
Coal gas, dedusting gas temperature is 20 DEG C, pressure 0.003MPaG；
(2) it compresses
Dedusting coal gas enters compression set, by dedusting gas compression to 1.0MPaG；Dedusting coal gas goes out compression set successively through being subcooled
But device (22) is cooled to 40 DEG C, through gas-liquid separator I (23) liquid separation；Obtain pressurized gas and coal gas of converter lime set；
(3) temp.-changing adsorption cleans
Pressurized gas is passed through oil removing tower (30) from tower bottom, oil, the dust, water in pressurized gas is removed, obtains except oil gas；It removes
If oil gas respectively enters the tower bottom of 6 temperature-change adsorption towers in parallel (31), except hydrogen phosphide, the hydrogen fluoride in oil gas are adsorbed
Removing；Obtain removal of impurities coal gas；
(4) the thick desulfurization of deoxygenation
Removal of impurities coal gas is changed coal gas of converter heat exchanger (40) heat exchange, and temperature is that 60 DEG C of removal of impurities coal gas sequentially enters hydrolysis desulfurizing tower
A(41) and hydrolysis desulfurizing tower B(42), through hydrolyzation catalysis effect by COS hydrolysis be H2Then S removes gas through fine de-sulfur
In H2S obtains desulfurization coal gas；Oxygen is removed through deoxidation reactor (43) after desulfurization coal gas and the mixing of deoxidation circulating air, is removed
Oxygen desulfurization coal gas；Deoxygenation desulfurization coal gas is divided into two-way, all the way deoxygenation desulfurization coal gas through circulating air water cooler (44) cool to
40 DEG C, then through circulating air liquid separation tank (45), go converter gas recycle compressor to be pressurized to 0.95MPag after separation water outlet, obtain deoxidation
Circulating air participates in system circulation；Another way deoxygenation desulfurization coal gas enters coal gas of converter heat exchanger (40), is cooled to 60 DEG C through heat exchange
Go to fine de-sulfur process；
(5) fine de-sulfur
The purified air water cooler of deoxygenation desulfurization coal gas removes fine de-sulfur tower A(50 after being cooled to 40 DEG C) or fine de-sulfur tower B(51)；Essence is de-
Sulphur tower A(50) and fine de-sulfur tower B(51) desulfurizing agent is housed, remove mercaptan and dimethyl disulfide remaining in deoxygenation desulfurization coal gas
Compound obtains fine de-sulfur coal gas；The fine de-sulfur coal gas sulfur content is less than 0.1ppm, and oxygen content is less than 30ppm；
(6) pressure swing adsorption decarbonization
Fine de-sulfur coal gas enters gas-liquid separator II (60) at 0.85MPa, isolates saturation moisture, obtains dehydration fine de-sulfur coal
Gas；Dehydration fine de-sulfur coal gas respectively enters the bottom of 8 decarburization absorbers (61) in parallel, the suction of the decarburization absorber (61)
Silica type adsorbent is filled in attached bed；The impurity composition CO being dehydrated in fine de-sulfur coal gas2It is adsorbed by adsorbent, weakly stable matter group
Divide i.e. H2、N2、CO、CH4From bottom to top by adsorbent bed, flows out, obtain from 61 top of decarburization absorber in pressure 0.8MPa condition
Decarburization coal gas；
(7) hydramine method decarburization
Through converter air filter (70) at pressure 0.8MPaG, primary filtration removes free fluid, obtains gas I decarburization coal gas；
Gas I enters converter gas absorption tower (71) bottom, is absorbing with top-down activation N methyldiethanol amine (MDEA) solution
Reverse contact heat-exchanging in tower, the CO in gas I2It is absorbed into liquid phase, obtains gas II；Gas II is from converter gas absorption tower (71)
Top outflow, enters converter gas separator (73) after converter Gas Cooler (72) is cooled to 40 DEG C, isolated gas III；Gas
Body III flows out at the top of converter gas separating device (73), into converter gas tower top filter (74), through converter gas tower top filter
(74) separation completely removes free fluid, is purified coal gas, the dust mass content < 0.1ppm of the purification coal gas, total sulfur
Mass content < 0.1ppm, oxygen volume content are less than 30ppm, CO2Volume content≤20ppm, hydrogen phosphide, fluorination hydrogen volume contain
0.1 ppm of < is measured, the content for purifying CO in coal gas is greater than 60%；The purification coal gas goes to downstream pressure-variable adsorption and mentions CO workshop section.
10. the purification production technology of converter gas according to claim 9, it is characterised in that: at 120~180 DEG C, to change
Adsorbent in warm adsorption tower (31) is regenerated；Fine de-sulfur tower A(50) and fine de-sulfur tower B(51) regeneration use regeneration gas
It is heated to 200 DEG C of regeneration；Decarburization absorber (61) regeneration extracts decarburization using water circulating type vacuum pump and parses agent.
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| CN113621745A (en) * | 2021-08-19 | 2021-11-09 | 中冶赛迪工程技术股份有限公司 | Blast furnace-converter steel production method based on carbon cycle |
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