CN107789969A - The processing method and device of a kind of sour gas - Google Patents
The processing method and device of a kind of sour gas Download PDFInfo
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- CN107789969A CN107789969A CN201610773555.9A CN201610773555A CN107789969A CN 107789969 A CN107789969 A CN 107789969A CN 201610773555 A CN201610773555 A CN 201610773555A CN 107789969 A CN107789969 A CN 107789969A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/77—Liquid phase processes
- B01D53/78—Liquid phase processes with gas-liquid contact
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—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
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B17/00—Sulfur; Compounds thereof
- C01B17/22—Alkali metal sulfides or polysulfides
- C01B17/32—Hydrosulfides of sodium or potassium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/30—Alkali metal compounds
- B01D2251/304—Alkali metal compounds of sodium
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
- B01D2251/604—Hydroxides
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
Abstract
The invention discloses a kind for the treatment of method and apparatus of sour gas, including following content：Absorption tower from top to bottom sets I order reactions area, II order reactions area and III level reaction zone, sodium hydroxide solution is entered as poor absorbing liquid by reactor head, sour gas is entered by reactor lower part multiple spot, sodium hydroxide solution in sour gas from down to up in I, II and III level reaction zone from top to bottom step by step with reacting, purified gas at the top of absorption tower by discharging, NaHS in rich absorbing liquid is separated out in the form of crystal in III level reaction zone, through sock filtration, filtrate is held liquid bath into bottom of towe and recycled, and solid is as Product recycling；Wherein the reaction temperature in I order reactions area is 50~80 DEG C, and the reaction temperature in second order reaction area is 70~90 DEG C, and the reaction temperature of III level reaction zone is 40~50 DEG C.Processing method of the present invention can be by H in purified gas2S concentration is controlled in 5~20mg/Nm3, while satisfaction can be produced《Industrial NaHS》The NaHS products of the solid Grade As of GB23937 2009 requirement.
Description
Technical field
The invention belongs to exhaust gas treatment technology, more particularly to a kind of sour gas and processing method and device.
Background technology
In hydrofinishing, it is hydrocracked, in the crude oil secondary processing process such as catalytic cracking, the testing sulphide in crude oil is when big
Hydrogen sulfide is partially converted into, and is present in sour gas.When as fuel or raw material, pipeline and equipment can be caused
Corrosion, and hydrogen sulfide therein is also the raw material for manufacturing sulphur and sulfuric acid.At present, the widely used alkanolamine solution of oil plant is to refinery
Sour gas carries out depriving hydrogen sulphide processing, and the dry gas after depriving hydrogen sulphide is incorporated to gas pipe network, and hydrogen sulfide is then used to manufacture sulphur.By
In alkanolamine solution to H2S and CO2Selectivity it is limited, the H containing high concentration is removed in the sour gas after processing2Outside S, also
CO containing higher concentration2, general hydrogen sulfide content 85% or so, carbon dioxide content accounts for 10%, in addition also a small amount of hydro carbons
Gas, including methane and ethane etc..
Big-and-middle-sized sour gas is mainly for the production of sulphur, and common technology has two kinds, and one kind is Claus techniques, another
Kind is the LO-CAT techniques of MERICHEM companies of U.S. exploitation.Claus techniques are using low-temperature catalyzed turn conventional of thermal response+two level
Micronizing technology produces sulphur, and its advantage is technical maturity, is adapted to the device for producing more than sulphur 5000t per year, sulfur recovery rate is most
High energy reaches more than 99%, but still has part sulphur with SO2Form be discharged into air, so need increase exhaust gas processing device.LO-
CAT techniques make H using the iron catalyst of multicomponent chelate2S is converted into elementary sulfur, H2S removal efficiency is more than 99.9%.LO-CAT
Technique can be adapted to acid tolerance to fluctuate various operating modes of the larger and hydrogen sulfide content 0~100%, but due to operating cost
Costliness, the sulfur purity and color and luster of production, which are slightly worse than caused drusen in claus process, and production process, to be occurred
Clogging etc., in middle-size and small-size refinery, the Technical Economy is not so good as Claus techniques.For small-sized refinery, because acid
Tolerance is little, and for many years, sour gas is discharging directly into atmosphere after burning mostly, wastes substantial amounts of Sulphur ressource, also result in tighter
The atmosphere pollution of weight.With the raising of national environmental standard, the Acidic Gas Treating of small-sized refinery increasingly draws attention.
To increase added value of product, many little refinery plants produce NaHS using sour gas as raw material, but due to acid
Property gas in contained hydrogen sulfide and carbon dioxide belong to sour gas, property is similar, and the content of carbon dioxide is spread out to hydrogen sulfide
The quality and production cost of product have a great influence, and because the crystallization of sodium carbonate etc. causes the blocking of pipeline and valve etc.,
Huge difficulty is brought to the normal production operation of device, NaHS product purity is also greatly affected.Therefore, ensureing
H in sour gas2On the premise of S qualified discharges, the blocking of pipe valve and instrument etc. during solution NaHS production operation
Had very important significance with the utilization for sour gas such as product purity is improved.
CN201310396214.0 is absorbed, two by the use of the methyl diethanolamine that concentration is 50% as extractant by two-stage
, can be by H in sour gas after level regeneration and heat exchange and condensation2S concentration is promoted to more than 99%.But the techniqueflow is longer, equipment is thrown
Provide larger, and consume a large amount of steam.Admixture of gas is removed acid therein by CN200880002473.8 with absorbing liquid first
Property gas, so as to obtain acid solution, is then obtained by the regeneration to acid solution and the compression of regenerator overhead gases
The hydrogen sulfide and carbon dioxide of higher concentration.The technology is applied to the relatively low gas mixing of the higher and acid gas concentration of hydrocarbonaceous concentration
The processing of thing.CN201010210208.8 produces using carbon monodixe conversion gas as unstripped gas by absorbent of low-temperature methanol solution
Carbon dioxide.After absorption and desorption, go out H in the H 2 S-containing gas of Mathanol regenerating column overhead2S concentration about 27%, is available for Ke Lao
This sulfur recovery unit sulphur or hydrogen sulfide relieving haperacidity.The technology is suitable to low concentration H2The concentration of S gases, flow is longer, is related to
The equipment such as multiple towers, heat exchanger and pump, therefore invest higher.CN103721531A is using membrane technology in sour gas two
Carbonoxide and hydrogen sulfide are separated and absorbed production NaHS and the shortcomings such as efficiency is low be present.CN103754833A is with hypergravity
Technical finesse oil refinery dry gas, and produce the NaHS product of higher degree, product and accessory substance crystallization easily cause overweight
The operating of power machine is unbalance, is difficult to realize with hypergravity machine processing sour gas production NaHS technology.CN104826463A、
There is the problem of same with CN103754833A in CN104826466A etc., and acid-base neutralization reaction occurs in revolving bed, instead
Hot also it should produce immediately, it is necessary to which adding substantial amounts of carrier gas just can guarantee that temperature needed for reaction, it is more difficult to realize.
The content of the invention
In view of the shortcomings of the prior art, the present invention proposes the processing method and device of a kind of sour gas.The present invention
Processing method can be by H in purified gas2S concentration is controlled in 5~20mg/Nm3, it is directly discharged into torch or gas pipe network, while this hair
Bright processing method can produce NaHS, and NaHS products meet《Industrial NaHS》The requirement of GB23937-2009 solids Grade A.
The processing method of the sour gas of the present invention, including following content：Absorption tower from top to bottom sets I order reactions
Area, II order reactions area and III level reaction zone, sodium hydroxide solution are entered as poor absorbing liquid by reactor head, and refinery is acid
Gas is entered by reactor lower part multiple spot, sodium hydroxide solution from top to bottom step by step with sour gas from down to up in I order reactions
Area, II order reactions area and III level reaction zone are reacted, and final purification gas at the top of absorption tower by discharging, in rich absorbing liquid
NaHS is separated out in the form of crystal in III level reaction zone, and through sock filtration, filtrate is held liquid bath into bottom of towe and recycled, solid
As Product recycling；Wherein the reaction temperature in I order reactions area be 50~80 DEG C, preferably 70 ~ 80 DEG C, the reaction temperature in second order reaction area
Spend for 70~90 DEG C, the reaction temperature of III level reaction zone is 40~50 DEG C.
In the inventive method, I order reactions area, II order reactions area and III level reaction zone from top to bottom in described absorption tower
Inside altogether set 4 ~ 40 layers of tower tray, preferably 10 ~ 30 layers, the mesh of tower tray perforate 10~10000, preferably 6000 ~ 10000 mesh, every grade of tower tray
It is provided with downflow weir and descending liquid area.Tower tray number corresponding to reaction zones wherein at different levels can be adjusted according to reaction needs, excellent
Select the tower tray number between reaction zones at different levels to differ and be no more than 2 layers.In general described I order reactions area, II order reactions area and III
Order reaction area corresponds to the upper, middle and lower on absorption tower respectively.In the inventive method, described tower tray is according to suitable from top to bottom
Ordered pair tower tray carries out 1 ~ N（Most last layer）Sequence, the tower tray number of plies is the tower tray number of plies of some reaction zone unless stated otherwise, remaining
In the case of the tower tray number of plies in terms of the tower tray number of plies on absorption tower.
In the inventive method, H in the sour gas2S volumetric concentrations 50%~95%, CO2Volumetric concentration 5%~20%, its
It is the organic matters such as hydro carbons；Described NaOH solution（Poor absorbing liquid）Mass concentration be 10%~60%, preferably 20%~40%.
In the inventive method, the reactiveness in described reaction zones at different levels is as follows：
Sour gas in I order reactions area contains the CO of higher concentration2With the H of low concentration2S, NaOH solution（Absorbing liquid）With acid
H in property gas2S and CO2Chemically react, it is Na to mainly generate thing2S、Na2CO3And NaHCO3；Set on I order reactions area tower tray
It is equipped with recirculating cooling water system, it is ensured that H in sour gas2S reaction is complete；
H in sour gas in II order reactions area2S concentration raises, the Na in absorbing liquid2S、Na2CO3And NaHCO3With in sour gas
H2S reactions are converted into Na2S and NaHS；Recirculating cooling water system is not provided with the tower tray in II order reactions area, passes through autoreactivity
Heat release can maintenance reaction temperature, while liquid phase is concentrated by evaporation, and makes solution that hypersaturated state be presented, into III level reaction zone；
There is fresh acidic gas to be passed through in III level reaction zone, and sour gas contains excessive H2S, the Na in absorbing liquid2S and NaHS
It is converted into NaHS；Recirculating cooling water system is provided with III level reaction zone tower tray, supersaturated absorbing liquid enters III level reaction zone
Cooled by chilling, the NaHS in liquid phase is separated out with granular form.
In the inventive method, in each order reaction, the residence time of gas phase is 1~20s, preferably 1~5s.
In the inventive method, described absorbing liquid is added by the first layer tower tray liquid phase entrance in I order reactions area, and refinery is acid
Gas is distinguished at 2~10 points in the reaction of absorption tower III level and added by the gas phase entrance on the downside of corresponding tower tray.
In the inventive method, by the 3rd ~ most last layer, preferably any one floor or more in 3 ~ II order reactions area last layer tower tray
The liquid that partially absorbs of layer is recycled back to top liquid phase entrance, so that NaOH is fully utilized in absorbing liquid, and keeps liquid layer on tower tray
Depth, to ensure gas-liquid mass transfer effect；Circulating fluid volume is 2~30 times, preferably 4~15 times of poor absorbing liquid addition.
In the inventive method, bottom of towe holds times that absorbing liquid in liquid bath is recycled back into absorption tower II levels and/or III level reaction zone
Anticipate one or more layers tower tray, to ensure Na in absorbing liquid2S is completely converted into NaHS, and reaches hypersaturated state.
In the inventive method, on the 2nd layer of tower tray liquid phase PH valve be 10~12, by adjust fresh NaOH solution addition come
It is controlled, makes to be discharged into H in the purified gas of torch2S is maintained at 5~20mg/Nm3, to ensure SO in torch gas2Qualified discharge.
In the inventive method, bottom of towe controls the liquid layer depth of orlop tower tray by fluid level controller, to produce fluid-tight, prevents
Only H2S is leaked in environment from liquid-phase outlet.
In the inventive method, demister is provided with the top of described absorption tower, bottom of towe, which is provided with, holds liquid bath.Described removes
Day with fog can be a kind of in fiber mist eliminator, material filling type demister or mesh mist eliminator.
In the inventive method, upper level tower tray downflow weir lower surface is inserted into below next stage tower tray absorbing liquid liquid level, with
Prevent that sour gas is short-circuit.
In the inventive method, the purified gas of discharge also contains 5~20mg/Nm of concentration at the top of absorption tower3H2S, fire can be discharged into
Torch or gas train.
The processing unit of the sour gas of the present invention, including：Absorption tower 3, primary cycle slurries pump 11, secondary cycle slurry
Liquid pump 15, pH value on-line checking and control system 12 and tank level control system 10；Wherein absorption tower 3 include demister 7, tower tray 4,
Downflow weir 5, descending liquid area 6 and bottom of towe hold liquid bath 17；The entrance of primary cycle slurries pump 11 is through pipeline and the tower tray of absorption tower 3 circulation liquid phase
Outlet connection, primary cycle slurries pump 11, which exports to be connected after pipeline merges with NaOH solution feeding line, is connected to first order tower
Disk liquid phase entrance；The entrance of two level slurry circulating pump 15 is held the liquid-phase outlet of liquid bath 17 with bottom of towe through pipeline and is connected, export through pipeline with
The circulation liquid phase entrance connection of the tower tray of absorption tower 3；Absorption tower bottom most last layer tower tray descending liquid area 6 is provided with tank level control system 10,
Descending liquid area 6 sets filter bag 18 through pipeline connecting valve 20, the lower section of valve 20, and filter bag 18 is connected to bottom of towe through liquid channel 21 and holds liquid
Groove 17.
Compared with prior art, the invention has the advantages that：
（1）The III level reaction zone of absorption tower bottom sets multiple spot air inlet, make on tower/I, II order reaction area at middle part is continuously generated
Na2CO3、NaHCO3And Na2H in the sour gas that S enters with multiple spot step by step2S reacts, and is eventually converted into NaHS so that NaHS
Constantly it is purified, bottom tower tray outlet NaHS purity greatly improves；
（2）The fluidizing agent of liquid phase in absorption tower is that sour gas, from top to bottom I, II and III level reaction zone are in fluidized state,
It completely avoid the Na generated in reaction2The depositing crystalline of S or NaHS particles and coalescence, the blocking of reactor or pipeline is prevented,
Micro-bubble on tower trays at different levels considerably increases gas-liquid-solid three-phase contact surface area, and reaction is more quick, uniform thorough；
（3）Different temperature control modes is respectively adopted in I, II and III level reaction zone in absorption tower so that I order reactions area is maximum
The effect for improving absorption of limit, the supersaturated absorbing liquid that II order reactions area obtains enter the cooled precipitation in third-order reaction area,
I, II and III level reaction zone coordinate step by step, have effectively purified sour gas while have produced the NaHS products of high-purity, have been advantageous to
Commercial Application.
Brief description of the drawings
Fig. 1 is the processing method and device flow chart of the sour gas of the present invention.
Wherein：1st, sour gas；2nd, NaOH solution；3rd, absorption tower；4th, tower tray；5th, downflow weir；6th, descending liquid area；7th, demisting
Device；8th, make-up cooling water；9th, circulating backwater；10th, fluid level controller；11st, primary cycle slurries pump；12nd, pH detectors；13rd, purify
Gas；14th, regulating valve；15th, secondary cycle slurries pump；16th, NaHS circulating absorption solutions；17th, liquid bath is held；18th, filter bag；19th, NaHS is solid
Body product；20th, switch valve；21st, liquid channel；
I, I order reactions area；II, II order reaction area；III, III level reaction zone.
Embodiment
The inventive method and device are described in more detail below by specific embodiment, but and are not so limited this
Invention.
The processing method of the sour gas of the present invention is carried out as follows：Sour gas 1 is by the bottom of absorption tower 3
III level reaction distinguish multiple spot and enter absorption tower, and from bottom to top from the top first layer tower tray liquid phase entrance addition of absorption tower 3
NaOH solution 2 ensures absorbing liquid temperature in I order reactions area haptoreaction, I order reactions area's tower tray through circulating cooling（That is reaction temperature
Degree）At 50~80 DEG C, the absorbing liquid for reacting to obtain enters II order reactions area, and II order reactions area is not provided with recirculating cooling water system,
By reaction heat, keep reaction temperature to be concentrated by evaporation absorbing liquid at 70~90 DEG C, and be in hypersaturated state, supersaturation is inhaled
Receive liquid and enter III level reaction zone through circulating cooling, tower tray absorbing liquid temperature is at 40~50 DEG C, and NaHS is concentrated knot in absorbing liquid
Crystalline substance, filter bag 18 is entered by valve 20 through descending liquid area 6, filtered NaHS enters as Product recycling, filtrate through liquid channel 21
Enter bottom of towe and hold liquid bath 17；Bottom of towe holds liquid bath（17）Middle absorbing liquid is extracted out by secondary cycle slurries pump 15 and returns to absorption tower；One-level is followed
Absorption tower 3 is partially absorbed liquid and is recycled back to first layer tower tray liquid phase entrance by ring slurries pump 11；Control liquid phase pH on second layer tower tray
Value makes to be discharged into H in the purified gas of torch 10~122S is maintained at 5~20mg/Nm3；Orlop is controlled by fluid level controller 10
Tower tray liquid layer depth, produce fluid-tight.
Embodiment 1
Certain sour gas pressure 0.30MPaG, 30 DEG C of temperature, H in sour gas2S accounts for 55%, CO2Concentration 10%, hydro carbons 35%.
Operating condition：（1）20 grades of tower tray is set in absorption tower, and gas liquid layer residence time on tower trays at different levels is 3s；（2）
Acid 8 strands of qi leel is passed through by gas phase entrance on the downside of the 13rd~20 grade of tower tray, on the 1st~14 grade and the 19th~20 grade of tower tray liquid layer
Recirculating cooling water system is set, keeps 65~75 DEG C of absorbing liquid temperature on tower trays at different levels；（3）Primary cycle slurries pump intake and
6 grades of tower tray liquid-phase outlet connections, serum recycle amount are 4 times of supplement fresh solution amount；（4）Secondary cycle slurries pump intake connects
Self-absorption bottom of towe holds liquid bath liquid-phase outlet, and outlet returns to the 15th grade of absorption tower tower tray liquid phase entrance；（5）Fresh NaOH solution quality
Concentration 30%.
As a result：（1）H in purified gas2S concentration 15mg/Nm3；（2）83 DEG C of the tower tray absorbing liquid temperature in the 15th~18 grade of absorption tower；
（3）NaHS contents 65% in final products NaHS solid particle, reach GB23937-2009《Industrial NaHS》Solid closes
The requirement of lattice product.
Embodiment 2
Certain sour gas pressure 0.30MPaG, 30 DEG C of temperature, H in sour gas2S accounts for 85%, CO2Concentration 10%, hydro carbons 5%.
Operating condition：（1）30 grades of tower tray is set in absorption tower, and gas liquid layer residence time on tower trays at different levels is 3s；（2）
Acid 10 strands of qi leel is passed through by gas phase entrance on the downside of the 21st~30 grade of tower tray, in the 1st~20 grade and the 27th~30 grade of tower tray liquid layer
Upper setting recirculating cooling water system, keep 70~80 DEG C of absorbing liquid temperature on tower trays at different levels；（3）Primary cycle slurries pump intake with
7th grade of tower tray liquid-phase outlet connection, serum recycle amount are 6 times of supplement fresh solution amount；（4）Secondary cycle slurries pump intake connects
It is connected to absorption tower bottom and holds liquid bath liquid-phase outlet, outlet returns to the 21st grade of absorption tower tower tray liquid phase entrance；（5）Fresh NaOH solution matter
Measure concentration 30%.
As a result：（1）H in purified gas2S concentration 15mg/Nm3；（2）85 DEG C of the tower tray absorbing liquid temperature in the 21st~26 grade of absorption tower；
（3）NaHS contents 65% in final products NaHS solid particle, reach GB23937-2009《Industrial NaHS》Solid closes
The requirement of lattice product.
Embodiment 3
Certain sour gas pressure 0.30MPaG, 30 DEG C of temperature, H in sour gas2S accounts for 92%, CO2Concentration 6%, hydro carbons 2%.
Operating condition：（1）35 grades of tower tray is set in absorption tower, and gas liquid layer residence time on tower trays at different levels is 4s；（2）
Acid 10 strands of qi leel is passed through by gas phase entrance on the downside of the 25th~35 grade of tower tray, in the 1st~24 grade and the 31st~35 grade of tower tray liquid layer
Upper setting recirculating cooling water system, keep 70~80 DEG C of absorbing liquid temperature on tower trays at different levels；（3）Primary cycle slurries pump intake with
9th grade of tower tray liquid-phase outlet connection, serum recycle amount are 8 times of supplement fresh solution amount；（4）Secondary cycle slurries pump intake connects
It is connected to absorption tower bottom and holds liquid bath liquid-phase outlet, outlet returns to the 25th grade of absorption tower tower tray liquid phase entrance；（5）Fresh NaOH solution matter
Measure concentration 35%.
As a result：（1）H in purified gas2S concentration 15mg/Nm3；（2）The 25th~30 grade of absorption tower tower tray absorbing liquid temperature 82
℃；（3）NaHS contents 65% in final products NaHS solid particle, reach GB23937-2009《Industrial NaHS》Gu
The requirement of body certified products.
Claims (12)
1. a kind of processing method of sour gas, including following content：Absorption tower from top to bottom sets I order reactions area, II levels
Reaction zone and III level reaction zone, sodium hydroxide solution are entered as poor absorbing liquid by reactor head, and sour gas is by reacting
Device bottom multiple spot enters, sodium hydroxide solution from top to bottom step by step with it is anti-in I order reactions area, II levels in sour gas from down to up
Area and III level reaction zone is answered to be reacted, final purification gas at the top of absorption tower by discharging, and the NaHS in rich absorbing liquid is with crystal
Form separates out in III level reaction zone, and through sock filtration, filtrate is held liquid bath into bottom of towe and recycled, and solid is as Product recycling；
Wherein the reaction temperature in I order reactions area is 50~80 DEG C, and the reaction temperature in second order reaction area is 70~90 DEG C, III level reaction zone
Reaction temperature be 40~50 DEG C.
2. in accordance with the method for claim 1, it is characterised in that：I order reactions area, II levels from top to bottom in described absorption tower
4 ~ 40 layers of tower tray are set altogether in reaction zone and III level reaction zone, and the mesh of tower tray perforate 10~10000, every grade of tower tray is provided with excessive
Flow weir and descending liquid area.
3. in accordance with the method for claim 1, it is characterised in that：H in the sour gas2S volumetric concentrations 50%~95%,
CO2Volumetric concentration 5%~20%.
4. in accordance with the method for claim 1, it is characterised in that：Circulation is provided with described I levels and III reaction zone tower trays
Cooling water system.
5. in accordance with the method for claim 1, it is characterised in that：The residence time of gas phase is 1~20s in each order reaction.
6. in accordance with the method for claim 1, it is characterised in that：Described sour gas is in absorption tower III level reaction zone
Divide added by the gas phase entrance on the downside of corresponding tower tray at 2~10 points.
7. in accordance with the method for claim 1, it is characterised in that：By in the 3rd ~ most last layer tower tray it is any one or more layers
Partially absorb liquid and be recycled back to top liquid phase entrance, circulating fluid volume is 2~30 times of poor absorbing liquid addition.
8. in accordance with the method for claim 1, it is characterised in that：Bottom of towe holds absorbing liquid in liquid bath and is recycled back into absorption tower II levels
And/or any one layer or multilayer tower tray of III level reaction zone.
9. in accordance with the method for claim 1, it is characterised in that：Liquid phase PH valve is 10~12 on 2nd layer of tower tray.
10. in accordance with the method for claim 1, it is characterised in that：Bottom of towe controls orlop tower tray by fluid level controller
Liquid layer depth；Demister is provided with the top of described absorption tower.
11. in accordance with the method for claim 1, it is characterised in that：Upper level tower tray downflow weir lower surface is inserted into next stage
Below tower tray absorbing liquid liquid level.
A kind of 12. processing unit of sour gas, it is characterised in that including：Absorption tower（3）, primary cycle slurries pump（11）、
Secondary cycle slurries pump（15）, pH value on-line checking and control system（12）And tank level control system（10）；Wherein absorption tower（3）
Including demister（7）, tower tray（4）, downflow weir（5）, descending liquid area（6）Liquid bath is held with bottom of towe（17）Form；Primary cycle slurries pump
（11）Entrance is through pipeline and absorption tower（3）Tower tray circulation liquid-phase outlet connection, primary cycle slurries pump（11）Outlet through pipeline with
NaOH solution feeding line is connected to first order tower tray liquid phase entrance after merging；Two level slurry circulating pump（15）Entrance is through pipe
Line holds liquid bath with bottom of towe（17）Liquid-phase outlet connects, and exports through pipeline and absorption tower（3）The circulation liquid phase entrance connection of tower tray；Inhale
Receive bottom of towe most last layer tower tray descending liquid area（6）It is provided with tank level control system（10）, descending liquid area（6）Through pipeline connecting valve（20）,
Valve（20）Lower section sets filter bag（18）, filter bag（18）Through liquid channel（21）It is connected to bottom of towe and holds liquid bath（17）.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610773555.9A CN107789969B (en) | 2016-08-31 | 2016-08-31 | Method and device for treating refinery acid gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610773555.9A CN107789969B (en) | 2016-08-31 | 2016-08-31 | Method and device for treating refinery acid gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107789969A true CN107789969A (en) | 2018-03-13 |
| CN107789969B CN107789969B (en) | 2020-12-08 |
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| CN201610773555.9A Active CN107789969B (en) | 2016-08-31 | 2016-08-31 | Method and device for treating refinery acid gas |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108729867A (en) * | 2018-07-14 | 2018-11-02 | 西南石油大学 | A kind of hermetic type vibrating screen of pipe chain chip removal |
| CN110548371A (en) * | 2019-10-15 | 2019-12-10 | 谢杰锋 | Analytic tower with measuring apparatu is clear away foam |
| CN116251539A (en) * | 2023-05-15 | 2023-06-13 | 黑龙江莱睿普思环境科技发展有限公司 | Absorption reactor for preparing sodium hydrosulfide from acid gas |
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| CN104971600A (en) * | 2014-04-10 | 2015-10-14 | 中国石油化工股份有限公司 | Acid gas tubular reactor and processing technical method |
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| US4278621A (en) * | 1977-12-22 | 1981-07-14 | Union Carbide Corporation | Vapor-liquid contacting system |
| CN2475459Y (en) * | 2000-12-27 | 2002-02-06 | 程培胜 | Tower tray type overall sucking tower |
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| CN108729867A (en) * | 2018-07-14 | 2018-11-02 | 西南石油大学 | A kind of hermetic type vibrating screen of pipe chain chip removal |
| CN110548371A (en) * | 2019-10-15 | 2019-12-10 | 谢杰锋 | Analytic tower with measuring apparatu is clear away foam |
| CN110548371B (en) * | 2019-10-15 | 2021-11-05 | 山东宜特装备制造有限公司 | Analytic tower with measuring apparatu is clear away foam |
| CN116251539A (en) * | 2023-05-15 | 2023-06-13 | 黑龙江莱睿普思环境科技发展有限公司 | Absorption reactor for preparing sodium hydrosulfide from acid gas |
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| CN107789969B (en) | 2020-12-08 |
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