CN111471494A - Wet catalyst oxidation desulfurization system based on hypergravity bed - Google Patents
Wet catalyst oxidation desulfurization system based on hypergravity bed Download PDFInfo
- Publication number
- CN111471494A CN111471494A CN202010314860.8A CN202010314860A CN111471494A CN 111471494 A CN111471494 A CN 111471494A CN 202010314860 A CN202010314860 A CN 202010314860A CN 111471494 A CN111471494 A CN 111471494A
- Authority
- CN
- China
- Prior art keywords
- desulfurization
- tank
- solution
- liquid
- lean
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Images
Classifications
-
- 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
-
- 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
- B01D53/8612—Hydrogen sulfide
-
- 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
- B01D53/869—Multiple step processes
-
- 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
- C10K1/122—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 only carbonates, bicarbonates, hydroxides or oxides of alkali-metals (including Mg)
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a wet catalyst oxidation desulfurization system based on a supergravity bed, which comprises a rotational flow plate desulfurization tower, a combined supergravity desulfurization tower, a pregnant solution tank, a regeneration tank, a first barren solution tank, a second barren solution tank and a barren solution allocation tank, wherein the rotational flow plate desulfurization tower and the combined supergravity desulfurization tower form a second-stage desulfurization unit of a series gas furnace, a desulfurization pregnant solution generated after desulfurization of each stage of desulfurization unit is circulated back to each stage of desulfurization unit through the pregnant solution tank, the regeneration tank, the first barren solution tank and the second barren solution tank, and the barren solution allocation tank intermittently replenishes fresh desulfurization liquid into the first barren solution tank and the second barren solution tankAnd (4) liquid stoste, and discharging an equal amount of unrecyclable desulfurization waste liquid from the first lean liquid tank and the second lean liquid. The desulfurization system has small resistance and is not easy to generate salt blockage or sulfur blockage, and the content of the hydrogen sulfide in the purified coal gas is lower than 20mg/Nm3And the discharged waste liquid is less, and the consumption of soda ash and catalyst is low.
Description
Technical Field
Belongs to the technical field of desulphurization and decyanation of coke oven gas, and particularly relates to a wet catalyst oxidation desulphurization system based on a hypergravity bed.
Background
The method for desulfurizing and decyanating coke oven gas mainly includes dry method and wet method, the dry method system is invented by England people of 1809 years, and mainly utilizes solid adsorbent, such as ferric hydroxide, active carbon and molecular sieve, etc. to remove hydrogen sulfide from gas, but its equipment is large in floor area, and can treat coke oven gas whose flow rate is less than 5000m3And/h is not suitable for scenes with large generation amount of modern coke oven gas. Modern large-scale coke plants all adopt wet systems, which are divided into absorption methods and oxidation methods, and specific representative methods are shown in table 1.
Among them, the ADA method, PDS method, HPF method are widely used in China, and usually consist of a packed absorption tower and a self-absorption regeneration oxidation tower, and the desulfurization barren solution absorbs H of coke oven gas in the packed absorption tower2After S and HCN, the desulfurization rich solution is introduced into an oxidation regeneration tower to be oxidized to form sulfur foam and regenerated lean solution, the regenerated lean solution returns to a filler absorption tower to be used as absorption solution, the sulfur foam is discharged and refined, and the desulfurization efficiency of a wet oxidation method is higher under an ideal state of using new absorption solution, but in practical application, the desulfurization rich solution can form byproducts in the regeneration oxidation tower, such as byproducts formed by a PDS method and an HPF method: NH (NH)4SCN、(NH4)2S2O3、(NH4)2SO4(ii) a The ADA process forms by-products: NaSCN, Na2S2O3、Na2SO4(ii) a Na in the desulfurization solution2S2O3Or (NH)4)2S2O3The increase in (b) will increase the desulfurization solution density resulting in NaHCO3The solubility of the catalyst is reduced, the viscosity and the surface tension of the desulfurization solution are increased, and the pH value of the desulfurization solution is reduced, so that the desulfurization efficiency of the catalyst is reduced, and the outlet H of the filler absorption tower is enabled to be2S content increases and O is hindered2The mass transfer in the desulfurization solution is carried out,the regeneration speed of the catalyst is reduced, the sulfur particle flotation is not facilitated, the dosage of the catalyst is increased, and when the content of the secondary salt exceeds 200 g/L, the change of the concentration of the catalyst is not obvious to improve the desulfurization effect;
because the existing coking plant mostly uses the packing absorption tower for desulfurization, the packing tower is large in volume, the height of the regenerative oxidation tower depends on the length of the self-suction air injection oxidation device, the length of the self-suction air injection oxidation device is calculated by factors such as self-suction air quantity, desulfurization rich liquid flow and the like, the height of the self-suction air injection oxidation device is usually 2-3 times that of the packing tower, the equipment cost is high, and the coal gas treatment capacity of the packing tower is limited by the height of the regenerative oxidation tower.
The Liu Zhi team of the university of middle and north has published a rotary packed bed in CN2870957, the lean absorption liquid is made to move along the radial outside of packing layer under the action of centrifugal force by the packing layer, contact with sulfur-containing gas and carry out mass transfer during the period, the gas-liquid mass transfer is strengthened, the gas-liquid two-phase completes the absorption of hydrogen sulfide gas under the action of high turbulence and strong mixing, thereby the volume of the packed tower is greatly reduced, the generation amount of desulfurization rich liquid, the height of the regenerative oxidation tower is also reduced, numerous domestic coking plants use the system, but the problem of packed bed blockage often occurs during use, therefore, the maximum processing coke oven gas amount of the packed bed of the team is not more than 10000m3The main reason is still that after part of sulfur particles (suspended sulfur content is about 0.5 g/L) and secondary salt products generated in the regeneration oxidation process are transferred to the barren solution, when the sulfur particles and the secondary salt products are accumulated to a certain degree, the viscosity of the desulfurization solution is increased, and simultaneously, crystals are separated out and even solidified in the packed bed to cause blockage, the surface area of the packed bed is reduced, the desulfurization effect is reduced, the higher the treatment capacity of the coke oven gas is, the higher the accumulation rate of the sulfur particles and the secondary salt products in the barren solution is, so that the existing packed tower or packed bed can treat the 30000m per hour of a wet oxidation regeneration desulfurization system by using a wet oxidation method3The working time of the packed column or bed does not exceed 3 months, and the packing has to be cleaned.
Disclosure of Invention
The invention aims to provide a wet catalyst oxidation desulfurization system based on a supergravity bed, which utilizes a cyclone plate desulfurization tower to carry out coarse desulfurization and combined supergravity bed fine desulfurization, introduces desulfurization rich liquid of two towers into a low-level regeneration tank to carry out oxidation regeneration, respectively introduces regenerated barren liquid into two barren liquid tanks to carry out detection, and respectively sends the barren liquid and the barren liquid raw material into the cyclone plate desulfurization tower and the combined supergravity bed after being blended so as to meet the parameter index of the desulfurization barren liquid.
In order to achieve the purpose, the invention provides a wet-type catalyst oxidation desulfurization system based on a hypergravity bed, which comprises a rotational flow plate desulfurization tower, a combined hypergravity desulfurization tower, a pregnant solution tank, a regeneration tank, a first barren solution tank, a second barren solution tank and a barren solution allocation tank, wherein an exhaust pipe of the rotational flow plate desulfurization tower is communicated with an air inlet pipe of the combined hypergravity desulfurization tower, and desulfurization solution collecting pipes of the rotational flow plate desulfurization tower and the combined hypergravity desulfurization tower are both communicated with a pregnant solution inlet pipe of the pregnant solution tank; the pregnant solution tank is communicated with a jet flow liquid inlet of an ejector of the regeneration tank through a pregnant solution pump, an outlet pipe of the regeneration tank is communicated with barren solution inlet pipes of a first barren solution tank and a second barren solution tank, the barren solution inlet pipes of the first barren solution tank and the second barren solution tank are also communicated with a stock solution outlet pipe of the barren solution allocation tank, and the barren solution outlet pipes of the first barren solution tank and the second barren solution tank are respectively communicated with a barren solution input pipe of the rotational flow plate desulfurization tower and the combined type super-gravity desulfurization tower or a barren solution input pipe of the combined type super-gravity desulfurization tower and the rotational flow plate desulfurization tower;
the combined type hypergravity desulfurization tower is provided with a rotating shaft and a plurality of layers of liquid throwing barrel units fixed on the rotating shaft, each layer of liquid throwing barrel unit is provided with a plurality of liquid throwing barrels, a barren solution input pipe penetrates through the inner wall of the combined type hypergravity desulfurization tower and extends to the position above each layer of liquid throwing barrel unit, the rotating speed of each liquid throwing barrel is 350-700 rpm, triangular prism blocks are uniformly distributed on the upper side of the bottom plate of each liquid throwing barrel along the circumferential direction, holes are uniformly distributed on the wall, close to the upper edge, of the barrel of each liquid throwing barrel, the diameter of each hole is 5mm, and the density is 4100-4160 pieces/2。
Preferably, in the supergravity bed-based wet catalyst oxidation desulfurization system: the pregnant solution tank comprises a first pregnant solution tank and a second pregnant solution tank, the regeneration tank comprises a first regeneration tank and a second regeneration tank, and the doctor solution collecting pipe of the cyclone plate desulfurizing tower and the doctor solution collecting pipe of the combined type hypergravity desulfurizing tower are respectively communicated with the pregnant solution inlet pipe of the second pregnant solution tank and the pregnant solution inlet pipe of the first pregnant solution tank; and outlet pipes of the second regeneration tank and the first regeneration tank are respectively communicated with lean solution inlet pipes of the second lean solution tank and the first lean solution tank.
Preferably, the inner periphery of the combined type hypergravity desulfurization tower is positioned at the upper part of each layer of liquid throwing barrel unit, and a suspension component is further arranged on the inner periphery of the combined type hypergravity desulfurization tower and is used for suspending and fixing the cyclone plate and the liquid descending cyclone plate above and at the outer periphery of each layer of liquid throwing barrel unit.
Furthermore, the shell of the cyclone plate desulfurizing tower is internally provided with an inverted cyclone plate, a barren liquor input pipe, a plurality of layers of suspension assemblies of the cyclone plate and the liquid-descending cyclone plate which are alternately arranged, a fixed cyclone plate and the liquid-descending cyclone plate, an air inlet pipe and a desulfurizing liquid collecting pipe from top to bottom in sequence, and the top of the shell is communicated with an exhaust pipe.
Preferably, the whirl plate is fixed through the bracket gusset the casing of whirl plate desulfurizing tower or combination formula hypergravity desulfurizing tower is interior, it is conical distribution to fix below the whirl plate to fall liquid whirl plate, it is fixed through the ring carrier that falls liquid whirl plate bottom, the whirl plate includes whirl blade group and cover barrel, the cover barrel sets up two rings at least from outside to inside at least, cover barrel diameter is progressively reduced once, whirl blade group is around the inner cover barrel along circumference evenly distributed, hang in midair the subassembly including fix annular platform in the casing, be used for supporting the support bracket of annular platform, hang the flange on annular platform, by the oblique inward-turning's of flange inner edge toper fence piece, whirl blade group radial angle is greater than 0 degree, and whirl blade group angle of elevation is 5 ~ 25 degrees, and whirl blade group is inward board around the same direction of rotation of whirl plate centre of a circle, the percent of opening of whirl plate is 30-40%, the opening thread of the liquid-descending rotational flow plate is opposite to the rotational flow blade group, the liquid-descending rotational flow plate is a trapezoidal thin plate, the lower bottom of the liquid-descending rotational flow plate is fixedly connected with the bottom edge of a conical surrounding sheet and the end part of the extending section of the outer side cover cylinder, the liquid-descending rotational flow plate is uniformly distributed along the circumference of the conical surrounding sheet, the height of the conical surrounding sheet is longer than the length of the extending section of the outer side cover cylinder, the radial angle of the opening thread of the liquid-descending rotational flow plate is greater than 0 degree, the radial angle of the opening thread of the liquid-descending rotational flow plate is equal to 0 degree, the upper bottom of the liquid-descending rotational flow plate is connected with an annular support, the cross-sectional diameter of the annular support in the combined type super-gravity desulfurization tower is greater than.
Furthermore, a foam outlet of the regeneration tank is also connected with a sulfur foam tank, exhaust ports of the spiral-flow plate desulfurization tower and the combined type super-gravity desulfurization tower are also respectively connected with a vapor-liquid separator, and a liquid discharge pipe of the vapor-liquid separator is communicated to the pregnant solution tank.
Preferably, the air outlets of the cyclone plate desulfurization tower and the combined supergravity desulfurization tower are respectively connected with a vapor-liquid separator, the liquid discharge pipes of the vapor-liquid separators are respectively communicated with the second rich liquid tank and the first rich liquid tank, and the first lean liquid tank is also provided with a lean liquid outlet pipe communicated with a lean liquid inlet pipe of the second lean liquid tank.
Preferably, the regeneration tank increases the mass concentration of the secondary salt in the regenerated desulfurization solution by ng/L compared with the mass concentration of the secondary salt in the rich desulfurization solution, and the first lean solution tank intermittently discharges X1One ton of regenerated desulfurization solution is replenished with equivalent desulfurization solution without secondary salt from a lean solution blending tank, so that the mass concentration of the secondary salt in the regenerated desulfurization solution circularly output from a first lean solution tank is reduced by ng/L compared with the mass concentration of the secondary salt in the regenerated desulfurization solution input to the first lean solution tank, the mass concentration of the secondary salt in the desulfurization rich solution circularly output from the first lean solution tank is not more than 25 g/L, and the synchronous second lean solution tank intermittently discharges X2Supplementing equivalent desulfurization solution without secondary salt from the lean solution blending tank, so that the mass concentration of the secondary salt in the regeneration desulfurization solution sent to the cyclone plate desulfurization tower in the second lean solution tank is equal to the mass concentration of the secondary salt in the regeneration desulfurization solution circularly output from the first lean solution tank, wherein n is the mass concentration of the secondary salt in the regeneration desulfurization solution discharged from the first lean solution tank in the process of discharging X from the first lean solution tank1The mass concentration change rate of the secondary salt in unit time, X, is obtained by periodically measuring the mass concentration change value of the secondary salt in the regenerated desulfurization solution before one ton of regenerated desulfurization solution1＝Q1*n/(n+25)，X1＝Q2N/(n +25) wherein Q1、Q2The flow rates of the desulfurization liquid in the combined type hypergravity desulfurization tower and the swirl plate desulfurization tower are respectively.
Preferably, the first regeneration tank increases the mass concentration of the secondary salt in the regenerated desulfurization solution by n compared with the mass concentration of the secondary salt in the desulfurization rich solution in the first rich solution tank1g/L, the first lean liquid tank intermittently discharges X to the second lean liquid tank1One ton of regenerated desulfurization solution is replenished with equivalent desulfurization solution without secondary salt from the lean solution blending tank, so that the mass concentration of the secondary salt in the regenerated desulfurization solution circularly output from the first lean solution tank is reduced by n compared with the mass concentration of the secondary salt in the regenerated desulfurization solution input to the first lean solution tank1g/L, the mass concentration of the secondary salt in the desulfurization rich solution circularly output by the first lean solution is not more than 25 g/L, and the mass concentration of the secondary salt in the regeneration desulfurization solution is increased by n compared with the mass concentration of the secondary salt in the desulfurization rich solution in the second rich solution tank synchronously by the second regeneration tank2g/L, and intermittently discharging X from the second lean liquid tank2Regenerating desulfurization solution by ton, and supplementing from lean solution blending tank (X)2-X1) The mass concentration of the secondary salt in the regenerated desulfurization solution circularly output from the second lean solution tank is reduced by n compared with the mass concentration of the secondary salt in the regenerated desulfurization solution input to the second lean solution tank2g/L, the mass concentration of the secondary salt in the desulfurization rich liquid output by the second lean liquid circulation is not more than 60 g/L, and n is1、n2The first lean liquor tank and the second lean liquor tank respectively discharge X1、X2The mass concentration change rate of the secondary salt in unit time, X, is obtained by periodically measuring the mass concentration change value of the secondary salt in the regenerated desulfurization solution before one ton of regenerated desulfurization solution1＝Q1*n1/(n1+25)，X2＝Q2*n2/(n2+60) wherein Q1、Q2The flow rates of the desulfurization liquid in the combined type hypergravity desulfurization tower and the swirl plate desulfurization tower are respectively.
The invention has the beneficial effects that: the cyclone plate desulfurization tower is used as a primary desulfurization device to treat hydrogen sulfide with the concentration of about 4-7 g/Nm3The coke oven gas of (1), the coke oven gas dischargedThe content of hydrogen sulfide is reduced to 300-1000 mg/Nm3Then, the combined type hypergravity desulfurizing tower is used for secondary desulfurization, so that the content of the purified hydrogen sulfide is reduced to 20mg/Nm3In the following, the desulfurization rich solution is sent to the ejector of the regeneration tank for jet flow, and self-priming air oxidation regeneration is carried out in the jet flow process, although the following secondary salts are generated according to different catalysts in the regeneration process: PDS and HPF processes form by-products: NH (NH)4SCN、(NH4)2S2O3、(NH4)2SO4(ii) a The ADA process forms by-products: NaSCN, Na2S2O3、Na2SO4(ii) a After the secondary salt-containing regenerated liquid is respectively sent into the first lean liquid tank and the second lean liquid tank to detect the content of the secondary salt according to time and then is mixed and blended with the raw material lean liquid in the lean liquid blending tank, on one hand, the regenerated liquid can be diluted and then sent to the lean liquid of the cyclone plate desulfurizing tower and the combined type super-gravity desulfurizing tower, so that the influence on the desulfurizing efficiency is reduced; on the other hand, as the opening rate of the spiral-flow plate desulfurizing tower and the combined type hypergravity desulfurizing tower is far greater than that of the traditional filler desulfurizing tower and the rotary filler bed desulfurizing tower of the Zhongbei university, the barren solution containing the secondary salt and the residual sulfur particles is difficult to solidify on the spiral-flow blade group or the liquid descending spiral-flow plate or the liquid throwing barrel to cause blockage, the time for keeping high-efficiency desulfurization of the spiral-flow plate desulfurizing tower and the combined type hypergravity desulfurizing tower under a better working condition is longer, and the cleaning is not required to be carried out once every three months like the traditional filler desulfurizing tower and the rotary filler bed desulfurizing tower of the Zhongbei university; finally, due to the matched use of the primary coarse desulfurization and the secondary fine desulfurization, the requirement on the content of hydrogen sulfide in the gas behind the cyclone plate desulfurization tower is not strict, the cyclone plate desulfurization tower can use barren liquor with higher content of secondary salt, the secondary salt can be enriched in one barren liquor tank, the secondary salt can be conveniently refined, the additional value of chemical products is improved, and the other barren liquor tank supplies barren liquor with low content of secondary salt to the combined type supergravity desulfurization tower;
the production data of the device of the invention in a certain coking plant in Sichuan are as follows:
the flow rate of the circulating barren solution of the cyclone plate desulfurizing tower is 1050m3/h；
The flow of the circulating barren solution of the combined type hypergravity desulfurizing tower is 280m3/h；
The treatment capacity of the regeneration barren solution of the regeneration tank is 1700m3/h；
The treatment capacity of the coke oven gas is 37500m3/h；
And (3) feeding the mixture into a combined supergravity desulfurizing tower to circulate barren solution: pH of 8.6 to 8.8 and Na2CO3The content is 3-5 g/L and the content is 0.01-0.04 g/L;
therefore, the matching use of the primary coarse desulfurization and the secondary fine desulfurization can maintain high desulfurization efficiency under the condition of higher content of secondary salt in the regenerated desulfurization solution, and can purify the coke oven gas with higher content of hydrogen sulfide. And simultaneously the content of hydrogen sulfide in the coke oven gas after the secondary fine desulfurization is kept less than 6mg/Nm for a long time3The optimal desulfurization capacity of the combined type hypergravity desulfurization tower is fully exerted, and the continuous effect of desulfurization by using the combined type hypergravity desulfurization tower alone in CN110614013A is far better.
Drawings
FIG. 1 is a process flow diagram of example 1 of the present invention;
FIG. 2 is a schematic structural diagram of a combined supergravity desulfurization tower of the present invention;
FIG. 3 is a top view of a top section of a cyclone plate in the tower of the combined type hypergravity desulfurization tower of the present invention, wherein the upper half is a top view of the cyclone plate and the lower half is a top view of the cyclone plate;
FIG. 4 is a schematic top view of the inside of a combined hypergravity desulfurization tower of the present invention;
FIG. 5 is a schematic view of the inside cross-sectional structure of the combined type hypergravity desulfurization tower of the present invention;
FIG. 6 is a schematic side view of a cross-sectional structure of a cyclone plate desulfurization tower according to the present invention;
FIG. 7 is a process flow diagram of a comparative desulfurization system;
FIG. 8 is a process flow diagram of a desulfurization system in example 2 of the present invention.
Detailed Description
The technical solutions in the embodiments of the present invention are 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 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.
Comparative example
With the desulfurization system shown in fig. 7, the water gas is desulfurized in a water gas plant of sichuan province, and the desulfurization system shown in fig. 7 includes: the desulfurization system comprises a cyclone plate desulfurization tower 1, a gas-liquid separator 3, a pregnant solution tank 4, a regeneration tank 5, a second barren solution tank 8 and a barren solution blending tank 9, wherein 15 layers of cyclone plates and liquid-descending cyclone plates are alternately arranged in the cyclone plate desulfurization tower 1, and the flow of water gas introduced into the desulfurization system is 30000m3H in water gas2S content 3g/Nm3The flow rate of the desulfurization solution introduced into the cyclone plate desulfurization tower 1 for circulation is 800m3H, adopting an improved ADA method to desulfurize, wherein the desulfurizing liquid contains Na2CO35g/L of 0.01 g/L of catalyst and 8.7-8.8 of pH value, in order to achieve the desulfurization rate of 98%, emptying 20t of regenerated desulfurization solution in the second lean solution tank 8 every day, and supplementing 20t of initial desulfurization solution without secondary salt from the lean solution adjusting tank 9, namely replacing 0.833t of regenerated desulfurization solution every hour, the content of secondary salt in the regenerated desulfurization solution can be kept not to exceed 20 g/L, and therefore the speed of increasing the content of secondary salt in the regenerated desulfurization solution every hour is Yg/L.
According to the formula, 800 × [ (Y) +20] -0.833 × [ (Y) +20] ═ 800 × 20, and Y is 0.0208 g/L t.
The processing capacity measured by the manufacturing of a tower device such as Shijiazhuang is 30000m3The conventional plate-type packed tower is used as a desulfurizing tower, an improved ADA process is adopted, the desulfurizing efficiency is reduced when the content of the secondary salt in the desulfurized regeneration liquid reaches 20 g/L, the resistance of the desulfurizing tower continuously and rapidly rises when the content of the secondary salt reaches 82 g/L, the desulfurizing liquid needs to be continuously replaced, and the content of the secondary salt in the regenerated desulfurizing liquid is reduced, wherein the recorded speed of increasing the content of the secondary salt in the regenerated desulfurizing liquid per day is 0.418-0.5 g/L.
Example 1
Fig. 1 is a flowchart of a wet catalyst oxidation desulfurization system based on a supergravity bed, which includes a swirl plate desulfurization tower 1, a combined supergravity desulfurization tower 2, a pregnant solution tank 4, a regeneration tank 5, a sulfur foam tank 6, a first lean solution tank 7, a second lean solution tank 8, and a lean solution blending tank 9, wherein an exhaust pipe 12 of the swirl plate desulfurization tower 1 is communicated with an intake pipe 22 of the combined supergravity desulfurization tower 2, and a desulfurization solution collecting pipe 11 of the swirl plate desulfurization tower 1 and a desulfurization solution collecting pipe 21 of the combined supergravity desulfurization tower 2 are both communicated with a pregnant solution inlet pipe 41 of the pregnant solution tank 4; the liquid enrichment tank 4 is communicated with a jet liquid inlet 52 of a jet device 51 of the regeneration tank 5 through a liquid enrichment pump 42, an outlet pipe 53 of the regeneration tank 5 is communicated with lean liquid inlet pipes 70 of a first lean liquid tank 7 and a second lean liquid tank 8, the lean liquid inlet pipes 70 of the first lean liquid tank 7 and the second lean liquid tank 8 are also communicated with a raw liquid outlet pipe 91 of a lean liquid blending tank 9, a lean liquid outlet pipe 71 of the first lean liquid tank 7 and a lean liquid outlet pipe 81 of the second lean liquid tank 8 are respectively communicated to a lean liquid input pipe 23 of the combined type hypergravity desulfurization tower 2 and a lean liquid input pipe 13 of the cyclone plate desulfurization tower 1, and a foam outlet 54 of the regeneration tank 5 is also connected with a sulfur foam tank 6;
the combined type hypergravity desulfurizing tower 2 is provided with a rotating shaft 24, a plurality of layers of liquid throwing barrel units are fixed on the rotating shaft 24, each layer of liquid throwing barrel unit is provided with a plurality of liquid throwing barrels 25, a barren solution input pipe 23 penetrates through the inner wall of the combined type hypergravity desulfurizing tower 2 and extends to the position above each layer of liquid throwing barrel unit, the rotating speed of each liquid throwing barrel 25 is 350-700 rpm, triangular prism blocks 26 are evenly distributed on the upper side of the bottom plate of each liquid throwing barrel 25 along the circumferential direction, as shown in figure 5, eyelets 2132 are evenly distributed on the upper edge of each liquid throwing barrel wall, the diameter of each eyelet 2132 is 5mm, and the density is 4100-4160/m2。
Referring to fig. 2 and 5, the combined-type super-gravity desulfurization tower 2 adopts a cyclone fog curtain absorption tower described in CN110614013A, a suspension assembly is further disposed at the upper part of each layer of liquid-throwing barrel unit at the inner periphery of the combined-type super-gravity desulfurization tower 2, the suspension assembly respectively suspends and fixes the cyclone plate 214 and the liquid-descending cyclone plate 2122 above and around each layer of liquid-throwing barrel unit, the cyclone plate 214 is fixed at the inner periphery of the housing of the combined-type super-gravity desulfurization tower 2 through a bracket rib 225, the liquid-descending cyclone plate 2122 is fixed at the lower part of the cyclone plate 214 in a conical distribution, the bottom end of the liquid-descending cyclone plate 2122 is fixed through a ring-shaped support 2121, the cyclone plate 214 comprises a cyclone blade set 2126 and a cover 2124, the cover 2124 is at least provided with two rings from the outside to the inside, the diameter of the cover 2124 is reduced once, the cyclone blade set 2126 is uniformly distributed around the inner cover along the circumference, the suspension assembly comprises a ring, A flange 226 which is hung on the annular platform, and a conical surrounding sheet 227 which is obliquely and inwards folded from the inner edge of the flange 226.
As shown in fig. 3 and 4, the radial angle of the rotational flow blade group 2126 is greater than 0 degree and is 16.59 degrees, the elevation angle of the rotational flow blade group 2126 is 5 degrees, the rotational directions of the rotational flow blade group 2126 around the center of the rotational flow plate 214 are both inward plates, the aperture ratio of the rotational flow plate 214 is 30-40%, and the rotational directions of the parting lines 57 and 46 of the liquid descending rotational flow plate 2122 are opposite to that of the rotational flow blade group 2126.
The liquid descending rotational flow plate 2122 is a trapezoidal thin plate, the lower bottom 45 is fixedly connected with the bottom edge of the conical surrounding sheet 227 and the end part of the extending section of the outer side cover barrel 2124, the liquid descending rotational flow plate 2122 is uniformly distributed along the circumference of the conical surrounding sheet 227, the height of the conical surrounding sheet 227 is longer than the length of the extending section of the outer side cover barrel 2124, the radial angle of an inner opening line 57 of the liquid descending rotational flow plate 2122 is greater than 0 degree, the radial angle of an outer opening line 46 is equal to 0 degree, and the upper bottom 67 of the liquid descending rotational flow plate 2122 is connected with the annular support 2121. The diameter of the cross section of the annular support 2121 in the combined supergravity desulfurization tower 2 is larger than the outer diameter of the liquid throwing cylinder unit, so that the elevation angle of the liquid descending rotational flow plate 2124 is 20 degrees.
As shown in fig. 6, the swirl plate desulfurization tower 1 adopts a high-efficiency swirl spray desulfurization tower described in CN109224776A, an inverted swirl plate 214, a barren liquor inlet pipe 13, a plurality of layers of alternately arranged swirl plates 214 and precipitation swirl plates 2122, a suspension assembly for fixing the swirl plates 214 and the precipitation swirl plates 2121, an air inlet pipe 14 and a desulfurization solution collecting pipe 11 are sequentially arranged in a shell of the swirl plate desulfurization tower 1 from top to bottom, and the top of the shell is communicated with an exhaust pipe 12. The suspension assembly is the same as that of the combined type hypergravity desulfurization tower 2 as shown in fig. 5, but the elevation angle of the liquid descending swirl plate 2121 in the swirl plate desulfurization tower 1 is 65 degrees, and a blind plate 2127 is flatly laid in the inner layer cover cylinder of the swirl plate 214.
The cyclone plate desulfurization tower 1 and the combined type hypergravity desulfurization tower 2 are not provided with static fillers, the liquid throwing cylinder can generate larger centrifugal force to carry out self-cleaning, the problem of blockage of the desulfurization packed tower can be effectively solved, and secondary salt tolerance in the regenerated desulfurization liquid is improved to 25 g/L while the secondary desulfurization precision is ensured.
Table 1 operating parameters of the system of the invention
The operation is operated under the operation parameters of table 1, the rate of the secondary salt accumulation in the barren solution in the system of the embodiment is 4 × 37500/(3 × 30000) -7 × 37500/(3 × 30000) which is 1.666-2.916 times of that of the comparative example, and the first barren solution tank of the example 1 of table 1 needs to circulate 280t of the regenerated desulfurization solution, and the second barren solution tank needs to circulate 1050t of the regenerated desulfurization solution.
However, in this embodiment, the rate of increase of the content of the secondary salt in the regenerated desulfurization solution per hour is 0.0208 × 1.666.666 to 0.0208 × 2.916, 0.0346 to 0.0606 g/L, and as long as the content of the secondary salt in the regenerated desulfurization solution in the first lean solution tank 7 is reduced by 0.0346 to 0.0606 g/L per hour, the secondary salt in the regenerated desulfurization solution circulated to the combined type super-gravity desulfurization tower 2 can be continuously kept not more than 25 g/L, the desulfurization efficiency is maintained, and the desulfurization re-treatment with the secondary salt more than 25 g/L is discharged per hour from the first lean solution tank with the circulation capacity of 1330tRaw liquid X1t，
280×[(1.666～2.916)×0.0208)+25]-X1×[(1.666～2.916)×0.0208)+25]＝280×25，X10.387 to 0.677t, namely, 9.288 to 16.25t of desulfurized regenerated liquid with the secondary salt of more than 25 g/L is discharged every day.
In the embodiment, the second lean liquor tank 8 discharges the desulfurization regeneration liquid X with the secondary salt more than 25 g/L per hour2t，
1050×[(1.25～2.5)×0.0208)+25]+280×[(1.25～2.5)×0.0208+25]-X2×[(1.25～2.5)×0.0208)+25]-X1×[(1.25～2.5)×0.0208+25]＝1330×25，X21.451-2.539, namely 1.090-2.179 t of the desulfurized regeneration liquid with the secondary salt more than 60 g/L is discharged every day, namely 34.82-60.93 t every day.
The first lean liquid tank and the second lean liquid tank discharge the regenerated desulfurization liquid 44.112-77.18 t in total every day.
Example 2
Fig. 8 is a flowchart of a wet catalyst oxidation desulfurization system based on a supergravity bed, which includes a swirl plate desulfurization tower 1, a combined supergravity desulfurization tower 2, a first rich liquid tank 4-1, a second rich liquid tank 4-2, a first regeneration tank 5-1, a second regeneration tank 5-2, a sulfur foam tank 6, a first lean liquid tank 7, a second lean liquid tank 8, and a lean liquid blending tank 9, wherein an exhaust pipe 12 of the swirl plate desulfurization tower 1 is communicated with an intake pipe 22 of the combined supergravity desulfurization tower 2, and a desulfurization liquid collecting pipe 11 of the swirl plate desulfurization tower 1 and a desulfurization liquid collecting pipe 21 of the combined supergravity desulfurization tower 2 are respectively communicated with a rich liquid inlet pipe 41 of the second rich liquid tank 4-2 and the first rich liquid tank 4-1; the first rich liquid tank 4-1 and the second rich liquid tank 4-2 are respectively communicated with the jet liquid inlet 52 of the jet device 51 of the second regeneration tank 5-2 and the first regeneration tank 5-1 through a rich liquid pump 42, the outlet pipes 53 of the second regeneration tank 5-2 and the first regeneration tank 5-1 are respectively communicated with the lean liquid inlet pipes 70 of the second lean liquid tank 8 and the first lean liquid tank 7, the lean liquid inlet pipes 70 of the first lean liquid tank 7 and the second lean liquid tank 8 are also respectively communicated with the raw liquid outlet pipe 91 of the lean liquid blending tank 9, the lean liquid outlet pipe 71 of the first lean liquid tank 7 and the lean liquid outlet pipe 81 of the second lean liquid tank 8 are respectively communicated with the lean liquid input pipe 23 of the combined type hypergravity desulfurization tower 2 and the lean liquid input pipe 13 of the swirl plate desulfurization tower 1, and the foam outlets 54 of the second regeneration tank 5-2 and the first regeneration tank 5-1 are also connected with a sulfur foam tank 6; the first lean liquid tank 7 is further provided with a lean liquid outlet pipe 71 communicated to a lean liquid inlet pipe 70 of the second lean liquid tank 8.
The combined type hypergravity desulfurizing tower 2 is provided with a rotating shaft 24, a plurality of layers of liquid throwing barrel units are fixed on the rotating shaft 24, each layer of liquid throwing barrel unit is provided with a plurality of liquid throwing barrels 25, a barren solution input pipe 23 penetrates through the inner wall of the combined type hypergravity desulfurizing tower 2 and extends to the position above each layer of liquid throwing barrel unit, the rotating speed of each liquid throwing barrel 25 is 350-700 rpm, triangular prism blocks 26 are evenly distributed on the upper side of the bottom plate of each liquid throwing barrel 25 along the circumferential direction, as shown in figure 5, eyelets 2132 are evenly distributed on the upper edge of each liquid throwing barrel wall, the diameter of each eyelet 2132 is 5mm, and the density is 4100-4160/m2。
The system of this example, operating Process H under the operating parameters of Table 12The S content is 4-7 g/Nm3The coke oven gas is used for maintaining the content of hydrogen sulfide at the removal outlet of the combined type hypergravity desulfurizing tower to be lower than 20mg/Nm3In the embodiment, the first lean liquor tank 7 discharges the desulfurization regeneration liquid X with the secondary salt more than 25 g/L per hour1t, the rate of secondary salt accumulation in the first lean liquid tank in the system of the embodiment is 0.4166 times that of 1 × 37500/(3 × 30000) of the comparative example,
280×[(0.4166×0.0208)+25]-X1×[(0.4166×0.0208)+25]＝280×25，X10.0970t, namely discharging 2.328t of desulfurized regeneration liquid with secondary salt more than 25 g/L every day.
And the lean solution adjusting tank 9 is supplemented with new desulfurization solution with the same amount, and the cyclone plate desulfurization tower only needs to keep the content of hydrogen sulfide at the outlet lower than 1000mg/Nm3I.e. the desulfurization efficiency is more than 85%, in the embodiment, the cyclone plate desulfurization tower absorbs H from coke oven gas2The cumulative rate of S is 1.25 to 2.5 times (4-1) 37500/(3X 30000) to (7-1) 37500/(3X 30000) times that of the comparative example, but the tolerance of the secondary salt in the desulfurization circulating liquid in the cyclone desulfurization tower is 3 times that of the comparative example, so that the second lean liquid tank 8 of the present example discharges the desulfurization regeneration liquid X with the secondary salt of more than 60 g/L per hour2t，
1050×[(1.25～2.5)×0.0208)+60]-X2×[(1.25～2.5)×0.0208)+60]＝1050×60，X20.4548-0.909 t, namely, 0.4548-0.909 t of the desulfurization regeneration liquid with the secondary salt more than 60 g/L is discharged every day, namely, 10.915-21.821 t every day.
The total is 13.2432-24.149 t per day.
Or because the first lean liquor tank 7 is also provided with a lean liquor outlet pipe 71 communicated to the lean liquor inlet pipe 70 of the second lean liquor tank 8 through a pump, the first lean liquor tank 7 of the embodiment conveys 2.328t of the desulfurization regeneration liquid with the secondary salt more than 25 g/L to the second lean liquor tank 8 every day, and replenishes new desulfurization liquid from the lean liquor blending tank 9, the second lean liquor tank 8 simultaneously discharges 10.954-21.871 t of the desulfurization regeneration liquid every day, and replenishes new desulfurization liquid 8.587-19.493 t from the lean liquor blending tank 9, so that the cyclone plate desulfurization tower can only keep the content of outlet hydrogen sulfide lower than 1000mg/Nm3Namely, the desulfurization efficiency is 85-90%.
In this embodiment, compared with the desulfurization waste liquid discharged in the embodiment 1 and the comparative example, and the supplemented new desulfurization liquid and the catalyst are greatly reduced, it is described in the literature that when the secondary salt in the regenerated desulfurization liquid reaches 120 g/L, the desulfurization efficiency of the plate-type desulfurization tower still can reach 88% by adopting the improved ADA process, that is, the waste liquid discharged from the second lean solution tank 8 in this embodiment 2 every day can be reduced by 50%, and the secondary salt in the waste liquid discharged from the second lean solution tank 8 can be further enriched, which is more beneficial to refining the secondary salt.
Claims (9)
1. A wet-type catalyst oxidation desulfurization system based on a hypergravity bed comprises a rotational flow plate desulfurization tower, a combined hypergravity desulfurization tower, a pregnant solution tank, a regeneration tank, a first barren solution tank, a second barren solution tank and a barren solution allocation tank, and is characterized in that an exhaust pipe of the rotational flow plate desulfurization tower is communicated with an air inlet pipe of the combined hypergravity desulfurization tower, and desulfurization solution collecting pipes of the rotational flow plate desulfurization tower and the combined hypergravity desulfurization tower are both communicated with a pregnant solution inlet pipe of the pregnant solution tank; the pregnant solution tank is communicated with a jet flow liquid inlet of an ejector of the regeneration tank through a pregnant solution pump, an outlet pipe of the regeneration tank is communicated with barren solution inlet pipes of a first barren solution tank and a second barren solution tank, the barren solution inlet pipes of the first barren solution tank and the second barren solution tank are also communicated with a stock solution outlet pipe of the barren solution allocation tank, and the barren solution outlet pipes of the first barren solution tank and the second barren solution tank are respectively communicated with a barren solution input pipe of the rotational flow plate desulfurization tower and the combined type super-gravity desulfurization tower or a barren solution input pipe of the combined type super-gravity desulfurization tower and the rotational flow plate desulfurization tower;
the combined type hypergravity desulfurization tower is provided with a rotating shaft and a plurality of layers of liquid throwing barrel units fixed on the rotating shaft, each layer of liquid throwing barrel unit is provided with a plurality of liquid throwing barrels, a barren solution input pipe penetrates through the inner wall of the combined type hypergravity desulfurization tower and extends to the position above each layer of liquid throwing barrel unit, the rotating speed of each liquid throwing barrel is 350-700 rpm, triangular prism blocks are uniformly distributed on the upper side of the bottom plate of each liquid throwing barrel along the circumferential direction, holes are uniformly distributed on the wall, close to the upper edge, of the barrel of each liquid throwing barrel, the diameter of each hole is 5mm, and the density is 4100-4160 pieces/2。
2. The supergravity bed-based wet catalyst oxidation desulfurization system of claim 1, wherein in said supergravity bed-based wet catalyst oxidation desulfurization system: the pregnant solution tank comprises a first pregnant solution tank and a second pregnant solution tank, the regeneration tank comprises a first regeneration tank and a second regeneration tank, and the doctor solution collecting pipe of the cyclone plate desulfurizing tower and the doctor solution collecting pipe of the combined type hypergravity desulfurizing tower are respectively communicated with the pregnant solution inlet pipe of the second pregnant solution tank and the pregnant solution inlet pipe of the first pregnant solution tank; and outlet pipes of the second regeneration tank and the first regeneration tank are respectively communicated with lean solution inlet pipes of the second lean solution tank and the first lean solution tank.
3. The supergravity bed-based wet catalyst oxidation desulfurization system according to any one of claims 1 or 2, wherein a suspension assembly is further provided at an inner periphery of the combined supergravity desulfurization tower at an upper portion of each layer of the liquid-slinger unit, and the suspension assembly suspends and fixes the swirl plate and the down-flow swirl plate above and at an outer periphery of each layer of the liquid-slinger unit, respectively.
4. The supergravity bed-based wet catalyst oxidation desulfurization system of claim 3, wherein the housing of the swirl plate desulfurization tower is provided with an inverted swirl plate, a barren solution inlet pipe, a plurality of layers of alternately arranged swirl plates and falling liquid swirl plates, a suspension assembly for fixing the swirl plates and the falling liquid swirl plates, an air inlet pipe and a desulfurization solution collection pipe from top to bottom in sequence, and the top of the housing is communicated with an exhaust pipe.
5. The wet catalyst oxidation desulfurization system based on the hypergravity bed according to any one of claims 3 or 4, wherein the swirl plate is fixed to the inner periphery of the housing of the swirl plate desulfurization tower or the combined hypergravity desulfurization tower through a bracket rib plate, the liquid-descending swirl plate is fixed below the swirl plate and distributed in a conical shape, the bottom end of the liquid-descending swirl plate is fixed through an annular bracket, the swirl plate comprises a swirl blade group and a cover cylinder, the cover cylinder is at least provided with two rings from outside to inside, the diameter of the cover cylinder is gradually reduced, the swirl blade group is uniformly distributed around the inner cover cylinder along the circumference, the suspension assembly comprises an annular table fixed in the housing, a support bracket for supporting the annular table, a flange hung on the annular table, and a conical surrounding sheet obliquely turned inwards from the inner edge of the flange, and the radial angle of the swirl blade group is greater than 0 degree, the elevation angle of the cyclone blade group is 5-25 degrees, the same direction of rotation of the cyclone blade group around the circle center of the cyclone plate is an inward plate, the aperture ratio of the cyclone plate is 30-40%, the opening line of the falling liquid cyclone plate is rotated to the direction opposite to that of the cyclone blade group, the falling liquid cyclone plate is a trapezoidal thin plate, the lower bottom of the falling liquid cyclone plate is fixedly connected with the bottom edge of a conical surrounding sheet and the end part of an extending section of an outer side cover cylinder, the falling liquid cyclone plate is uniformly distributed along the circumference of the conical surrounding sheet, the height of the conical surrounding sheet is longer than the length of the extending section of the outer side cover cylinder, the radial angle of the opening line of the falling liquid cyclone plate is greater than 0 degree, the radial angle of the outward opening line is equal to 0 degree, the upper bottom of the falling liquid cyclone plate is connected with an annular support, the section diameter of the annular support in the combined supergravity desulfurization tower is greater than the outer diameter of the liquid.
6. The supergravity bed-based wet catalyst oxidation desulfurization system according to claim 1, wherein the foam outlet of the regeneration tank is further connected with a sulfur foam tank, the gas outlets of the swirl plate desulfurization tower and the combined supergravity desulfurization tower are further respectively connected with a vapor-liquid separator, and the liquid discharge pipe of the vapor-liquid separator is communicated with the pregnant solution tank.
7. The system of claim 2, wherein the gas outlets of the cyclone plate desulfurization tower and the combined supergravity desulfurization tower are respectively connected with a gas-liquid separator, the liquid discharge pipes of the gas-liquid separators are respectively communicated with the second rich liquid tank and the first rich liquid tank, and the first lean liquid tank is further provided with a lean liquid outlet pipe communicated with the lean liquid inlet pipe of the second lean liquid tank.
8. The supergravity bed-based wet catalyst oxidation desulfurization system of claim 1, wherein the regeneration tank increases the mass concentration of secondary salts in the regenerated desulfurization solution by ng/L compared to the mass concentration of secondary salts in the desulfurization rich solution, and the first lean solution tank intermittently discharges X1One ton of regenerated desulfurization solution is replenished with equivalent desulfurization solution without secondary salt from a lean solution blending tank, so that the mass concentration of the secondary salt in the regenerated desulfurization solution circularly output from a first lean solution tank is reduced by ng/L compared with the mass concentration of the secondary salt in the regenerated desulfurization solution input to the first lean solution tank, the mass concentration of the secondary salt in the desulfurization rich solution circularly output from the first lean solution tank is not more than 25 g/L, and the synchronous second lean solution tank intermittently discharges X2Supplementing equivalent desulfurization solution without secondary salt from the lean solution blending tank, so that the mass concentration of the secondary salt in the regeneration desulfurization solution sent to the cyclone plate desulfurization tower in the second lean solution tank is equal to the mass concentration of the secondary salt in the regeneration desulfurization solution circularly output from the first lean solution tank, wherein n is the mass concentration of the secondary salt in the regeneration desulfurization solution discharged from the first lean solution tank in the process of discharging X from the first lean solution tank1The mass concentration change rate of the secondary salt in unit time, X, is obtained by periodically measuring the mass concentration change value of the secondary salt in the regenerated desulfurization solution before one ton of regenerated desulfurization solution1＝Q1*n/(n+25)，X1＝Q2N/(n +25) wherein Q1、Q2The flow rates of the desulfurization liquid in the combined type hypergravity desulfurization tower and the swirl plate desulfurization tower are respectively.
9. The supergravity bed-based wet catalyst oxidation desulfurization system of claim 2, wherein the first regeneration tank increases the mass concentration of the secondary salt in the regenerated desulfurization solution by n from the mass concentration of the secondary salt in the desulfurization rich solution in the first rich solution tank1g/L, the first lean liquid tank intermittently discharges X to the second lean liquid tank1One ton of regenerated desulfurization solution is replenished with equivalent desulfurization solution without secondary salt from the lean solution blending tank, so that the mass concentration of the secondary salt in the regenerated desulfurization solution circularly output from the first lean solution tank is reduced by n compared with the mass concentration of the secondary salt in the regenerated desulfurization solution input to the first lean solution tank1g/L, the mass concentration of the secondary salt in the desulfurization rich solution circularly output by the first lean solution is not more than 25 g/L, and the mass concentration of the secondary salt in the regeneration desulfurization solution is increased by n compared with the mass concentration of the secondary salt in the desulfurization rich solution in the second rich solution tank synchronously by the second regeneration tank2g/L, and intermittently discharging X from the second lean liquid tank2Regenerating desulfurization solution by ton, and supplementing from lean solution blending tank (X)2-X1) The mass concentration of the secondary salt in the regenerated desulfurization solution circularly output from the second lean solution tank is reduced by n compared with the mass concentration of the secondary salt in the regenerated desulfurization solution input to the second lean solution tank2g/L, the mass concentration of the secondary salt in the desulfurization rich liquid output by the second lean liquid circulation is not more than 60 g/L, and n is1、n2The first lean liquor tank and the second lean liquor tank respectively discharge X1、X2The mass concentration change rate of the secondary salt in unit time, X, is obtained by periodically measuring the mass concentration change value of the secondary salt in the regenerated desulfurization solution before one ton of regenerated desulfurization solution1＝Q1*n1/(n1+25)，X2＝Q2*n2/(n2+60) wherein Q1、Q2The flow rates of the desulfurization liquid in the combined type hypergravity desulfurization tower and the swirl plate desulfurization tower are respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010314860.8A CN111471494A (en) | 2020-04-21 | 2020-04-21 | Wet catalyst oxidation desulfurization system based on hypergravity bed |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202010314860.8A CN111471494A (en) | 2020-04-21 | 2020-04-21 | Wet catalyst oxidation desulfurization system based on hypergravity bed |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN111471494A true CN111471494A (en) | 2020-07-31 |
Family
ID=71754051
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202010314860.8A Pending CN111471494A (en) | 2020-04-21 | 2020-04-21 | Wet catalyst oxidation desulfurization system based on hypergravity bed |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN111471494A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115287102A (en) * | 2022-08-25 | 2022-11-04 | 南京澳博工业智能科技研究院有限公司 | Wet catalyst oxidation desulfurization system based on hypergravity bed |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202688288U (en) * | 2012-03-28 | 2013-01-23 | 江苏中显集团有限公司 | Tower crane combined gas desulfurization process unit |
| CN109224776A (en) * | 2018-10-20 | 2019-01-18 | 富瑞德化工设备(武汉)有限公司 | A kind of high-efficiency swirl-type FGD by spraying mist tower and its sulfur method |
| CN110614013A (en) * | 2019-07-28 | 2019-12-27 | 恒华源化工设备(武汉)有限公司 | System for removing hydrogen sulfide in coke oven gas and desulfurization method |
-
2020
- 2020-04-21 CN CN202010314860.8A patent/CN111471494A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN202688288U (en) * | 2012-03-28 | 2013-01-23 | 江苏中显集团有限公司 | Tower crane combined gas desulfurization process unit |
| CN109224776A (en) * | 2018-10-20 | 2019-01-18 | 富瑞德化工设备(武汉)有限公司 | A kind of high-efficiency swirl-type FGD by spraying mist tower and its sulfur method |
| CN110614013A (en) * | 2019-07-28 | 2019-12-27 | 恒华源化工设备(武汉)有限公司 | System for removing hydrogen sulfide in coke oven gas and desulfurization method |
Non-Patent Citations (1)
| Title |
|---|
| 乌云: "《煤炭气化工艺与操作》", 31 May 2013, 北京理工大学出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115287102A (en) * | 2022-08-25 | 2022-11-04 | 南京澳博工业智能科技研究院有限公司 | Wet catalyst oxidation desulfurization system based on hypergravity bed |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106693858B (en) | A kind of block-resistant type is high-gravity rotating bed and contains the high-gravity rotating bed system and device of the block-resistant type and application | |
| CN104874235B (en) | A kind of spiral board dedusting demister | |
| CN108671723B (en) | Ultrasonic synchronous desulfurization and dust removal integrated device | |
| CN205598776U (en) | Cigarette tower unification desulphurized flue gas defogging system | |
| CN104941326B (en) | Dedusting demister, treating column and purposes | |
| CN110614013B (en) | System for removing hydrogen sulfide in coke oven gas and desulfurization method | |
| CN202212098U (en) | Self-priming gas-liquid mass transfer reactor | |
| CN105642024A (en) | Swirling de-swirling coupled efficient dedusting and demisting assembly | |
| CN112892174B (en) | Conical tower tray and application thereof | |
| CN201823405U (en) | Cyclone demister exhausting gas down | |
| CN108554151A (en) | A kind of flue gas high-efficiency desulfurization dust separation device | |
| CN108686488A (en) | A kind of suspension bed wet desulphurization and regeneration integral system | |
| CN212283492U (en) | Wet catalyst oxidation desulfurization system based on hypergravity bed | |
| CN111471494A (en) | Wet catalyst oxidation desulfurization system based on hypergravity bed | |
| CN105148716A (en) | Flue gas desulfurization tower for coal-fried boilers | |
| CN204684801U (en) | A kind of spiral board dedusting demister | |
| CN203695230U (en) | Swirler | |
| CN109731474B (en) | A kind of regenerating desulfurization device and its technique | |
| CN206168213U (en) | Calcium method catalytic cracking flue gas desulfurization and dust removal system | |
| CN206587498U (en) | A kind of gas-liquid separator | |
| CN1221307C (en) | Integrative desulfurizing and dedusting tower of ammonia process | |
| CN108179035A (en) | The packing method of adsorbent | |
| CN107626199A (en) | A kind of gas cleaning reactor and flue gas purification system | |
| CN105107311B (en) | Desulfurization device | |
| CN109173694B (en) | Desulfurization reaction tube, desulfurization dust removal system based on desulfurization reaction tube and process of desulfurization dust removal system |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20200731 |
|
| RJ01 | Rejection of invention patent application after publication |