CN110835556A - Blast furnace gas wet desulphurization system and method - Google Patents
Blast furnace gas wet desulphurization system and method Download PDFInfo
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- 238000000034 method Methods 0.000 title claims abstract description 16
- 238000006460 hydrolysis reaction Methods 0.000 claims abstract description 111
- 230000007062 hydrolysis Effects 0.000 claims abstract description 85
- 238000005070 sampling Methods 0.000 claims abstract description 79
- 238000010521 absorption reaction Methods 0.000 claims abstract description 58
- 239000003054 catalyst Substances 0.000 claims abstract description 25
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910052717 sulfur Inorganic materials 0.000 claims abstract description 13
- 239000011593 sulfur Substances 0.000 claims abstract description 13
- 230000000694 effects Effects 0.000 claims abstract description 9
- 239000007789 gas Substances 0.000 claims description 206
- 238000006477 desulfuration reaction Methods 0.000 claims description 39
- 230000023556 desulfurization Effects 0.000 claims description 39
- 239000003034 coal gas Substances 0.000 claims description 19
- 238000006243 chemical reaction Methods 0.000 claims description 18
- 238000010926 purge Methods 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 15
- PVXVWWANJIWJOO-UHFFFAOYSA-N 1-(1,3-benzodioxol-5-yl)-N-ethylpropan-2-amine Chemical compound CCNC(C)CC1=CC=C2OCOC2=C1 PVXVWWANJIWJOO-UHFFFAOYSA-N 0.000 claims description 8
- QMMZSJPSPRTHGB-UHFFFAOYSA-N MDEA Natural products CC(C)CCCCC=CCC=CC(O)=O QMMZSJPSPRTHGB-UHFFFAOYSA-N 0.000 claims description 8
- 239000003795 chemical substances by application Substances 0.000 claims description 6
- 230000000382 dechlorinating effect Effects 0.000 claims description 6
- 238000001514 detection method Methods 0.000 claims description 4
- 230000000903 blocking effect Effects 0.000 claims description 3
- 230000003197 catalytic effect Effects 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 3
- 239000011261 inert gas Substances 0.000 claims description 3
- 230000003301 hydrolyzing effect Effects 0.000 claims description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 6
- 239000003546 flue gas Substances 0.000 description 6
- 238000005457 optimization Methods 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- CDBYLPFSWZWCQE-UHFFFAOYSA-L sodium carbonate Substances [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 2
- 229910000029 sodium carbonate Inorganic materials 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 239000005864 Sulphur Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 230000002708 enhancing effect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000001802 infusion Methods 0.000 description 1
- 150000002500 ions Chemical class 0.000 description 1
- 229910044991 metal oxide Inorganic materials 0.000 description 1
- 150000004706 metal oxides Chemical class 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/002—Removal of contaminants
- C10K1/003—Removal of contaminants of acid contaminants, e.g. acid gas removal
- C10K1/004—Sulfur containing contaminants, e.g. hydrogen sulfide
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
- C10K1/124—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors containing metal compounds other than alkali- or earth-alkali carbonates, hydroxides- or oxides- or salts of inorganic acids derived from sulfur
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/34—Purifying combustible gases containing carbon monoxide by catalytic conversion of impurities to more readily removable materials
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- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to the technical field of gas wet desulphurization, and provides a blast furnace gas wet desulphurization system, which comprises a hydrolysis reactor for performing hydrolysis reaction on gas and a solution absorption tank for absorbing sulfur-containing gas, wherein a hydrolysis catalyst is filled in the hydrolysis reactor, a gas inlet pipeline is arranged at a gas inlet of the hydrolysis reactor, a gas outlet pipeline is arranged at a gas outlet of the hydrolysis reactor, a first gas sampling port and a second gas sampling port are respectively arranged on the gas inlet pipeline and the gas outlet pipeline, the solution absorption tank is communicated with the hydrolysis reactor through the gas outlet pipeline, a gas outlet of the solution absorption tank is provided with a gas exhaust pipeline, and a third gas sampling port is arranged on the gas exhaust pipeline. Also provides a blast furnace gas wet desulphurization method. The invention firstly adopts the hydrolysis reactor to carry out hydrolysis reaction, and then adopts the solution absorption tank to absorb sulfur-containing gas, thereby having good wet desulphurization effect.
Description
Technical Field
The invention relates to the technical field of coal gas wet desulphurization, in particular to a blast furnace coal gas wet desulphurization system and a blast furnace coal gas wet desulphurization method.
Background
Along with the stricter and stricter national environmental protection requirements, the problem of the exceeding standard of the sulfur emission of the flue gas caused by the sulfur content of the blast furnace gas is more and more prominent, a plurality of enterprises find that the sulfur content of the flue gas after the blast furnace gas is purely combusted exceeds the standard through monitoring, and the enterprises face the problem that the blast furnace gas needs to be desulfurized after being combusted, so that all combustion users need to carry out the desulfurization of the combustion flue gas, and series of problems such as difficult selection of a flue gas desulfurization system, large occupied area, high investment, large manpower investment and the like are caused. Many steel enterprises also think of enhancing blast furnace desulfurization, and create better conditions for downstream flue gas desulfurization, and even some owners have considered blast furnace gas desulfurization.
The blast furnace gas desulfurization mainly removes COS and H in the blast furnace gas2S, the difficult point and key point are that COS is removed and hydrolyzed into H2S is relatively easy to remove by adopting a wet method. At present, partial catalyst manufacturers have developed a low-temperature hydrolysis catalyst for COS, and whether the catalyst can be combined with wet desulphurization to be applied to blast furnace gas still needs to be tested and verified, and the main problems to be verified are that:
(1) the low-temperature hydrolysis characteristic of the hydrolysis catalyst, the conversion rate at different temperatures and how to verify the service life need to be tested, which is an important index for whether the blast furnace gas desulfurization has economy.
(2) The hydrolysis catalyst is generally metal oxide and is easily affected by the acidic poisoning of the HCl gas in the blast furnace gas, and how to verify the acid resistance of the catalyst and how to mitigate the effect is an important factor that must be considered in the hydrolysis catalyst scheme for the blast furnace gas desulfurization.
(3) For blast furnace gas, after COS hydrolysis, H is removed by wet method2The solution adopted by S is more suitable for absorption and removal, and how to verify CO in the coal gas2Absorb H to the desulfurization solution2The influence of S.
Disclosure of Invention
The invention aims to provide a blast furnace gas wet desulphurization system and a blast furnace gas wet desulphurization method, which can at least solve part of defects in the prior art.
In order to achieve the above purpose, the embodiments of the present invention provide the following technical solutions: the utility model provides a blast furnace gas wet flue gas desulfurization system, includes the hydrolysis reactor that carries out hydrolysis reaction to coal gas and is used for absorbing the solution absorption groove of containing sulphur gas, the intussuseption of hydrolysis reactor is filled with hydrolysis catalyst, the inlet duct is installed to the air inlet of hydrolysis reactor, and the pipeline of giving vent to anger is installed to the gas outlet of hydrolysis reactor, in set up first gas sample mouth and second gas sample mouth on the inlet duct respectively with on the pipeline of giving vent to anger, the solution absorption groove pass through the pipeline of giving vent to anger with the hydrolysis reactor intercommunication, exhaust duct is installed to the gas outlet of solution absorption groove, in set up the third gas sample mouth on the exhaust duct.
Furthermore, a valve before wet absorption capable of blocking a flow path between the hydrolysis reactor and the solution absorption tank is arranged on the gas outlet pipeline.
Further, the solution absorption tank is provided with a liquid discharge port for discharging the solution in the tank and a liquid replenishment port for replenishing the solution in the tank.
Further, a first cooler is installed on the air inlet pipeline, and a hydrolysis reactor thermometer is installed on the hydrolysis reactor.
Furthermore, a purging connecting pipe for connecting inert gas to purge air in the flow path is installed on the air inlet pipeline, and a purging connecting pipe valve is installed on the purging connecting pipe.
Furthermore, a coal gas pressure reduction valve is arranged on the gas outlet pipeline.
The embodiment of the invention provides another technical scheme: the blast furnace gas wet desulphurization method is characterized by comprising the following steps:
s1, respectively installing an air inlet pipeline and an air outlet pipeline at an air inlet and an air outlet of the hydrolysis reactor, and performing hydrolysis reaction by using a hydrolysis catalyst in the hydrolysis reactor;
s2, absorbing sulfur-containing gas on the gas outlet pipeline after the hydrolysis reaction by using a solution absorption tank;
s3, arranging a first gas sampling port on the gas inlet pipeline, arranging a second gas sampling port on the gas outlet pipeline, and arranging a third gas sampling port on the exhaust pipeline of the solution absorption tank;
s4, detecting the concentrations of COS, H2S and CO2 before desulfurization from the first gas sampling port, detecting the concentrations of COS, H2S and CO2 after hydrolysis conversion at the second gas sampling port, and detecting the concentrations of COS, H2S and CO2 after desulfurization at the third gas sampling port;
and S5, calculating the hydrolysis conversion rate according to the gas concentration detected by the first gas sampling port and the gas concentration detected by the second gas sampling port, and calculating the desulfurization rate according to the gas concentration detected by the first gas sampling port and the gas concentration detected by the third gas sampling port.
Further, the absorption liquid in the solution absorption tank is replaced by MDEA solution, and then the steps S1-S5 are carried out, so that the MDEA solution can be used for analyzing and calculating to absorb H in the coal gas2The effect and removal rate of S; and detecting CO after the hydrolysis reaction from the second gas sampling port2Concentration, CO after wet absorption from the third gas sampling port2Concentration, analyzing CO in coal gas according to the concentrations of the two gases2Absorb H to the desulfurization solution2The influence of S.
Further, before the hydrolysis reaction, the temperature of the coal gas entering the hydrolysis reactor is controlled by the first cooler, the steps S1-S5 are carried out, the conversion rate of the hydrolysis catalyst at different temperatures can be calculated according to the concentration of COS detected by the first gas sampling port and the concentration of COS detected by the second gas sampling port, and the performance attenuation characteristics of the hydrolysis catalyst can be obtained through a data curve by continuous detection at different temperatures for a certain time.
Further, by filling the hydrolysis reactor with a dechlorinating agent near the gas inlet pipe and performing the steps of S1 to S5, the catalytic conversion performance of the catalyst can be analyzed and calculated with different amounts of dechlorinating agent.
Compared with the prior art, the invention has the beneficial effects that: firstly, a hydrolysis reactor is adopted for hydrolysis reaction, and then a solution absorption tank is adopted for absorbing sulfur-containing gas, so that the wet desulphurization effect is good. In addition, a first gas sampling port and a second gas sampling port are respectively arranged on a gas inlet pipeline and a gas outlet pipeline of the hydrolysis reactor, the hydrolysis conversion rate can be calculated according to the gas concentration detected by the first gas sampling port and the gas concentration detected by the second gas sampling port, and the desulfurization rate can be calculated according to the gas concentration detected by the first gas sampling port and the gas concentration detected by the third gas sampling port by arranging the third gas sampling port on the gas outlet pipeline of the solution absorption tank.
Drawings
FIG. 1 is a schematic diagram of a wet desulfurization system for blast furnace gas according to an embodiment of the present invention;
FIG. 2 is a flow chart illustrating the steps of a wet desulfurization method for blast furnace gas according to an embodiment of the present invention;
in the reference symbols: 1-connecting a pipeline gate valve; 2-gas flow regulating valve; 3-purging the connecting pipe; 4-a flow meter; 5-a first pressure gauge; 6-a second thermometer; 7-a first gas sampling port; 8-a first cooler; 9-a hydrolysis reactor; 10-hydrolysis reactor thermometer; 11-gas pressure reducing valve; 12-a second cooler; 13-a second thermometer; 14-a second pressure gauge; 15-a second gas sampling port; 16-a bypass valve after hydrolysis reaction; 17-wet pre-absorption valve; 18-a solution absorption tank; 19-wet post-absorption valve; 20-a third gas sampling port; 21-a liquid discharge port; 22-fluid infusion port; 23-a liquid sampling port; 24-diffusion point.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
The first embodiment is as follows:
referring to fig. 1, an embodiment of the present invention provides a blast furnace gas wet desulfurization system, including a hydrolysis reactor 9 for performing a hydrolysis reaction on a gas, and a solution absorption tank 18 for absorbing a sulfur-containing gas, where a hydrolysis catalyst is filled in the hydrolysis reactor 9, an air inlet pipe is installed at an air inlet of the hydrolysis reactor 9, an air outlet pipe is installed at an air outlet of the hydrolysis reactor 9, a first gas sampling port 7 and a second gas sampling port 15 are respectively formed on the air inlet pipe and the air outlet pipe, the solution absorption tank 18 is communicated with the hydrolysis reactor 9 through the air outlet pipe, an air outlet pipe is installed at an air outlet of the solution absorption tank 18, and a third gas sampling port 20 is formed on the air outlet pipe. In this embodiment, the solution absorption tank 18 is filled with Na2CO3And (3) solution. The hydrolysis reaction is carried out by adopting the hydrolysis reactor 9, and then the sulfur-containing gas is absorbed by adopting the solution absorption tank 18, so that the wet desulphurization effect is good. In addition, through the gas sampling ports arranged on a plurality of pipelines, the hydrolysis conversion rate can be calculated according to the gas concentration detected by the first gas sampling port 7 and the gas concentration detected by the second gas sampling port 15, the desulfurization rate can be calculated according to the gas concentration detected by the first gas sampling port 7 and the gas concentration detected by the third gas sampling port 20, and the performance of the system can be controlled. The gas source was about 150kPa and the temperature was about 180 ℃.
As an optimized solution of the embodiment of the present invention, referring to fig. 1, the gas outlet pipe is provided with a wet process pre-absorption valve 17 capable of blocking a flow path between the hydrolysis reactor 9 and the solution absorption tank 18. In this embodiment, the valve 17 before wet absorption is provided to block the flow path between the hydrolysis reactor 9 and the solution absorption tank 18, and the flow path can be controlled according to actual requirements.
Referring to fig. 1, the solution absorbing tank 18 is provided with a liquid discharge port 21 for discharging the solution in the tank and a liquid replenishment port 22 for replenishing the solution in the tank. In this embodiment, the liquid in the solution absorption tank 18 can be replaced by, for example, MDEA solution through the liquid discharge port 21 and the liquid replenishment port 22, and wet desulfurization is performed, so that the MDEA solution for analysis and calculation can absorb H in the gas2The effect and removal rate of S, and detecting CO after the hydrolysis reaction from the second gas sampling port 152Concentration of CO after wet absorption from the third gas sampling port 202Concentration, analyzing CO in coal gas according to the concentrations of the two gases2Absorb H to the desulfurization solution2The influence of S.
Referring to fig. 1, as an optimized solution of the embodiment of the present invention, a liquid sampling port 23 is provided on the solution absorption tank 18. In this embodiment, the sampling port can be used to detect the concentration, pH and related ions of the solution.
Referring to fig. 1, as an optimized solution of the embodiment of the present invention, a first cooler 8 is installed on the gas inlet pipe, and a hydrolysis reactor thermometer 10 is installed on the hydrolysis reactor 9. Before the hydrolysis reaction, the temperature of the coal gas entering the hydrolysis reactor 9 is controlled by adopting a first cooler 8, and then COS and H before desulfurization are detected from the first gas sampling port 72S and CO2COS and H after the hydrolytic conversion are detected at the second gas sampling port 152S and CO2The conversion rate of the hydrolysis catalyst at different temperatures can be calculated, and the performance attenuation characteristics of the hydrolysis catalyst can be obtained through a data curve by continuous detection at different temperatures for a certain time. During the temperature control, the different temperature points are monitored by the hydrolysis reactor thermometer 10, for example every 10One test temperature point was measured in deg.C. The measuring range of the hydrolysis reactor thermometer 10 is 80-200 ℃.
Referring to fig. 1, as an optimized solution of the embodiment of the present invention, a second cooler 12 is installed on the air outlet pipeline. In this embodiment, the second cooler 12 is provided to cool the gas after passing through the hydrolysis reactor 9, and then the gas is discharged into the solution absorption tank 18 or directly discharged.
Referring to fig. 1, as an optimized scheme of the embodiment of the present invention, a gas flow regulating valve 2 is installed on the gas inlet pipe. In the present embodiment, the gas flow rate control valve 2 is attached to the gas inlet pipe, whereby the amount of gas introduced can be controlled.
Referring to fig. 1 as an optimized scheme of the embodiment of the present invention, a purge connection pipe 3 for introducing an inert gas to purge air in a flow path is installed on the gas inlet pipeline, and a valve of the purge connection pipe 3 is installed on the purge connection pipe 3. In the embodiment, before the gas starts to be introduced, nitrogen is introduced into the pipeline through the purging connection pipe 3, specifically, the first stage is to open the valves of the hydrolysis reactor 9 only, namely, to purge the air in the gas inlet pipeline and the gas outlet pipeline, and after the purging, the valve 17 before wet absorption and the valve 19 after wet absorption are opened, namely, to purge the air in the gas outlet pipeline.
Referring to fig. 1, as an optimized solution of the embodiment of the present invention, a flow meter 4 is installed on the intake pipe. In the present embodiment, the gas inflow can be monitored by the flow meter 4.
Referring to fig. 1, as an optimized solution of the embodiment of the present invention, a first pressure gauge 5 and a first temperature gauge are installed on the intake pipe. In this embodiment, by installing the first pressure gauge 5 and the first temperature gauge, the gas inlet parameters can be monitored. These data, including other monitored data, can be used as the basis for experimental calculations and need to be recorded. Similarly, the outlet pipe is provided with a second pressure gauge 14 and a second temperature gauge 136, which are monitored after the hydrolysis reactor 9.
As an optimized scheme of the embodiment of the present invention, please refer to fig. 1, a coal gas pressure reducing valve 11 is installed on the gas outlet pipeline. In this embodiment, the opening degree of the gas pressure reducing valve 11 needs to be controlled according to different stages, for example, before the preparation operation, the gas pressure reducing valve 11 is in a small opening degree (less than 5%) state, and in the process, the opening state of the gas pressure reducing valve is also controlled at any time.
Referring to fig. 1, as an optimized scheme of the embodiment of the present invention, a bypass valve 16 after hydrolysis reaction is installed on the gas outlet pipeline. In this embodiment, the bypass valve 16 is provided to directly discharge the gas in the hydrolysis reactor 9 when necessary, for example, after the solution absorption tank 18 is saturated, and it is needless to say that the flow path may be blocked when not necessary. Preferably, a bleed point 24 is provided after the by-pass valve 16 after the hydrolysis reaction, the bleed point 24 being 4m above the system.
As an optimized solution of the embodiment of the present invention, please refer to fig. 1, a valve 19 after wet absorption is installed on the exhaust pipe. In this embodiment, the valve 19 after wet absorption is provided to control the gas treated by the solution absorption tank 18 to be discharged.
As an optimized scheme of the embodiment of the present invention, please refer to fig. 1, an inlet pipe gate valve 1 is installed on the outlet pipe. In this embodiment, the inlet pipe gate valve 1 can control the gas inlet. Preferably, a bleed point is provided after the pipe gate valve 1 is switched in, the bleed point being 4m above the system. The blast furnace gas is taken from the front of the blast furnace residual pressure power generation device, and is connected with the connecting pipeline gate valve 1 after being connected.
Example two:
referring to fig. 2, an embodiment of the present invention provides a blast furnace gas wet desulphurization method, including the following steps: s1, respectively installing an air inlet pipeline and an air outlet pipeline at an air inlet and an air outlet of the hydrolysis reactor 9, and performing hydrolysis reaction by using a hydrolysis catalyst in the hydrolysis reactor 9; s2, absorbing sulfur-containing gas on the gas outlet pipeline after the hydrolysis reaction by using a solution absorption tank 18; s3, arranging a first gas sampling port 7 on the gas inlet pipeline, arranging a second gas sampling port 15 on the gas outlet pipeline, and arranging a gas sampling valve on the gas inlet pipelineA third gas sampling port 20 is formed in an exhaust pipeline of the solution absorption tank 18; s4, detecting the concentrations of COS, H2S and CO2 before desulfurization from the first gas sampling port 7, the concentrations of COS, H2S and CO2 after hydrolysis conversion at the second gas sampling port 15, and the concentrations of COS, H2S and CO2 after desulfurization at the third gas sampling port 20; and S5, calculating the hydrolysis conversion rate according to the gas concentration detected by the first gas sampling port 7 and the gas concentration detected by the second gas sampling port 15, and calculating the desulfurization rate according to the gas concentration detected by the first gas sampling port 7 and the gas concentration detected by the third gas sampling port 20. In this embodiment, the solution absorption tank 18 is filled with Na2CO3And (3) solution. The hydrolysis reaction is carried out by adopting the hydrolysis reactor 9, and then the sulfur-containing gas is absorbed by adopting the solution absorption tank 18, so that the wet desulphurization effect is good. In addition, through the gas sampling ports arranged on a plurality of pipelines, the hydrolysis conversion rate can be calculated according to the gas concentration detected by the first gas sampling port 7 and the gas concentration detected by the second gas sampling port 15, the desulfurization rate can be calculated according to the gas concentration detected by the first gas sampling port 7 and the gas concentration detected by the third gas sampling port 20, and the performance of the system can be controlled.
As an optimization scheme of the embodiment of the invention, the absorption liquid in the solution absorption tank 18 is replaced by the MDEA solution, and then the steps S1-S5 are carried out, so that the MDEA solution for analysis and calculation can absorb H in the coal gas2The effect and removal rate of S; and detecting CO after the hydrolysis reaction from the second gas sampling port 152Concentration of CO after wet absorption from the third gas sampling port 202Concentration, analyzing CO in coal gas according to the concentrations of the two gases2Absorb H to the desulfurization solution2The influence of S.
As an optimization scheme of the embodiment of the invention, before the hydrolysis reaction, the first cooler 8 is adopted to control the temperature of the coal gas entering the hydrolysis reactor 9, and then the steps S1-S5 are performed, so that the conversion rate of the hydrolysis catalyst at different temperatures can be calculated according to the concentration of COS detected from the first gas sampling port 7 and the concentration of COS detected from the second gas sampling port 15, and the performance decay characteristics of the hydrolysis catalyst can be obtained through a data curve by continuous detection for a certain time and at different temperatures.
As an optimization scheme of the embodiment of the invention, dechlorinating agent is filled in the hydrolysis reactor 9 close to the gas inlet pipeline, and the steps S1-S5 are carried out, so that the catalytic conversion performance of the catalyst under the condition of filling different amounts of dechlorinating agent can be analyzed and calculated.
As for other components, please refer to the first embodiment, which will not be described in detail.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. A blast furnace gas wet desulphurization system is characterized in that: the gas hydrolysis device comprises a hydrolysis reactor for performing hydrolysis reaction on coal gas and a solution absorption tank for absorbing sulfur-containing gas, wherein a hydrolysis catalyst is filled in the hydrolysis reactor, a gas inlet pipeline is installed at a gas inlet of the hydrolysis reactor, a gas outlet pipeline is installed at a gas outlet of the hydrolysis reactor, a first gas sampling port and a second gas sampling port are respectively formed in the gas inlet pipeline and the gas outlet pipeline, the solution absorption tank is communicated with the hydrolysis reactor through the gas outlet pipeline, an exhaust pipeline is installed at a gas outlet of the solution absorption tank, and a third gas sampling port is formed in the exhaust pipeline.
2. The blast furnace gas wet desulfurization system according to claim 1, characterized in that: and a valve before wet absorption capable of blocking a flow path between the hydrolysis reactor and the solution absorption tank is arranged on the gas outlet pipeline.
3. The blast furnace gas wet desulfurization system according to claim 1, characterized in that: the solution absorption tank is provided with a liquid discharge port for discharging the solution in the tank and a liquid replenishment port for replenishing the solution in the tank.
4. The blast furnace gas wet desulfurization system according to claim 1, characterized in that: and a first cooler is installed on the air inlet pipeline, and a hydrolysis reactor thermometer is installed on the hydrolysis reactor.
5. The blast furnace gas wet desulfurization system according to claim 1, characterized in that: the air inlet pipeline is provided with a purging connecting pipe used for connecting inert gas to purge air in the flow path, and the purging connecting pipe is provided with a purging connecting pipe valve.
6. The blast furnace gas wet desulfurization system according to claim 1, characterized in that: and a coal gas pressure reducing valve is arranged on the gas outlet pipeline.
7. The blast furnace gas wet desulphurization method is characterized by comprising the following steps:
s1, respectively installing an air inlet pipeline and an air outlet pipeline at an air inlet and an air outlet of the hydrolysis reactor, and performing hydrolysis reaction by using a hydrolysis catalyst in the hydrolysis reactor;
s2, absorbing sulfur-containing gas on the gas outlet pipeline after the hydrolysis reaction by using a solution absorption tank;
s3, arranging a first gas sampling port on the gas inlet pipeline, arranging a second gas sampling port on the gas outlet pipeline, and arranging a third gas sampling port on the exhaust pipeline of the solution absorption tank;
s4, detecting COS and H before desulfurization from the first gas sampling port2S and CO2The concentration of COS and H after the hydrolytic conversion is detected at the second gas sampling port2S and CO2After the desulfurization is detected at the third gas sampling port, COS and H are detected2S and CO2The concentration of (c);
and S5, calculating the hydrolysis conversion rate according to the gas concentration detected by the first gas sampling port and the gas concentration detected by the second gas sampling port, and calculating the desulfurization rate according to the gas concentration detected by the first gas sampling port and the gas concentration detected by the third gas sampling port.
8. The blast furnace gas wet desulfurization method according to claim 7, characterized in that: replacing the absorption liquid in the solution absorption tank with MDEA solution, and performing S1-S5 to analyze and calculate H in the gas absorbed by the MDEA solution2The effect and removal rate of S; and detecting CO after the hydrolysis reaction from the second gas sampling port2Concentration, CO after wet absorption from the third gas sampling port2Concentration, analyzing CO in coal gas according to the concentrations of the two gases2Absorb H to the desulfurization solution2The influence of S.
9. The blast furnace gas wet desulfurization method according to claim 7, characterized in that: before the hydrolysis reaction, the temperature of the coal gas entering the hydrolysis reactor is controlled by adopting a first cooler, the steps S1-S5 are carried out, the conversion rate of the hydrolysis catalyst at different temperatures can be calculated according to the concentration of COS detected by a first gas sampling port and the concentration of COS detected by a second gas sampling port, and the performance attenuation characteristics of the hydrolysis catalyst can be obtained through a data curve by continuous detection for a certain time at different temperatures.
10. The blast furnace gas wet desulfurization method according to claim 7, characterized in that: the performance of catalytic conversion of the catalyst with different amounts of dechlorinating agent can be analytically calculated by filling the hydrolysis reactor with dechlorinating agent near the gas inlet pipe and then performing the steps of S1-S5.
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