CN104826464B - Novel acidic gas treating process and apparatus - Google Patents
Novel acidic gas treating process and apparatus Download PDFInfo
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- CN104826464B CN104826464B CN201410046323.4A CN201410046323A CN104826464B CN 104826464 B CN104826464 B CN 104826464B CN 201410046323 A CN201410046323 A CN 201410046323A CN 104826464 B CN104826464 B CN 104826464B
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Abstract
The invention provides a novel acidic gas treating process and apparatus. The acidic gas treating process employs a gas-liquid two-phase countercurrent absorption reaction and uses a NaOH solution as an absorption liquid to treat acidic gas so as to produce NaHS. According to the process, a primary liquid reaction product and a secondary liquid reaction product are cyclically used, the secondary liquid reaction product is used a tertiary reaction absorption liquid, and an MDEA solution is used as a fourth-stage reaction absorption liquid; thus, the purpose of replacement of CO2 with H2S is achieved, the generation amounts of Na2CO3 and NaHCO3 in a liquid phase product are reduced, precipitation of crystals is prevented, and long cycle operation of the apparatus is guaranteed. The acidic gas treating process provided by the invention is simple and can achieve the dual objectives of purification of acidic gas and reclamation of pollutants.
Description
Technical field
The present invention provides a kind of Acidic Gas Treating technique and device, belongs to sour gas field of purification, more particularly to a kind of suitable
In the purification containing sulfohydrate sour gas and the treating method and apparatus of pollutant resources.
Background technology
Sour gas mostly come from the devices such as sewage stripping, desulphurization of recycle hydrogen, dry gas desulfurization, main in sour gas
Containing H2S、CO2.The sour gas of current most of small-sized refinery is substantially using the processing method discharged after burning.This method one
Aspect causes the waste of resource, on the other hand brings huge pressure to environmental protection, influences the development space of enterprise.It is protection ring
Border and ensure making full use of for resource, it is imperative that the sour gas of small-sized refinery recycle.
The treatment of big-and-middle-sized sour gas, mainly uses sour gas to prepare sulphur, and the more commonly used at present has two kinds
Technology, one kind is two grades of Claus+ tail gas hydrogenation reduction+solvent absorption process technologies；Another kind is U.S. Merichem public
The LO-CAT technologies of gas technology Products Co., Ltd of department exploitation.
Two grades of Claus+ tail gas hydrogenation reduction+solvent absorption technical matters maturations, stable operation, product sulphur quality are steady
It is fixed, but because long flow path, investment are big, Claus techniques can only process the sour gas of high concentration, generally as the H in unstripped gas2S
When volume fraction is less than 20%, device is just difficult to operate.Therefore, Claus techniques are suitable for producing per year the dress of more than sulphur 5000t
Put.
LO-CAT techniques make H using the iron catalyst of multicomponent chelate2S is converted into elementary sulfur, H2The removal efficiency of S exceedes
99.9%.LO-CAT techniques can be adapted to the larger and H of acid tolerance fluctuation2Various operating modes of the S contents 0~100%, raw material is fitted
Answer condition wide in range, adapt to the actual conditions of sour gas fluctuating change.And LO-CAT liquid redox treatment schemes do not make
With any poisonous chemicals, and any harmful exhaust gas by-products will not be produced, environmentally safe catalyst can be with
It is constantly regenerating in processing procedure.But because there is operating cost high, sulfur purity and color and luster slightly worse than Crouse in LO-CAT
Technique, and the sulphur particle meeting blockage phenomenon for producing in process of production, therefore, LO-CAT techniques are producing sulphur per year
Economy is poor in below 5000t scales（Relative to two grades of Claus+ tail gas hydrogenation reduction+solvent absorption technologies）.
For small-sized refinery, because acid tolerance is relatively small, using two grades of Claus+ tail gas hydrogenations reduction+solvents
There is long flow path, complex operation, investment greatly in absorption techniques technique, scale and benefit are poor.And there is also one using LO-CAT technologies
Secondary investment is larger, the problems such as catalyst and patent royalties higher.
It is smaller for the total tolerance of small-sized sour gas, can be using the less new desulfurization process of investment, by H2S reclaims system
Standby sulphite, carries out burning generation SO by sour gas first2, being then fed into absorption tower carries out chemical absorbing generation sulphite
Solution, then solution and alkaline absorbent are reacted, prepare sulphite fluid product, or generation sulphite crystal, warp
The operation such as separation, dry is prepared into sulphite solid product.The device flow is shorter, and reaction is simple, and operating flexibility is big, can fit
Influence of the small-sized sour gas fluctuation to production process is answered, solid or liquid product can be produced by selecting different operations
Product, select different absorbents to produce different types of sulphite, and realize tail gas qualified discharge by three sections of absorptions, real
The purpose of existing cleaning of off-gas.But it is serious to there is equipment corrosion in actual production process, maintenance cost determination higher.
CN101143714A discloses a kind of method that sour gas of utilization high hydrocarbon-containing prepares sulfuric acid, acid hydrogen sulfide gas
Burning in first, second sulfureted hydrogen burning stove is respectively enterd in proportion, from the first combustion furnace high-temperature furnace gas out, by furnace gas
Cooler, uniform temperature is cooled to by air, subsequently into the second combustion furnace with supplement sulfide hydrogen sour gas continue with
The combust of surplus air one in furnace gas, the second combustion furnace high-temperature furnace gas out enter waste heat boiler heat accumulation, enter back into purification work
Section, conversion section, dry absorption section carry out conventional relieving haperacidity.This process can only produce 98% industrial sulphuric acid, it is impossible to which productive value is more
Oleum high, simultaneously as the transport of sulfuric acid, storage acquire a certain degree of difficulty, therefore, the market of stabilization needs near oil plant
Seeking Truth limits the key factor of its development.
CN1836767A discloses a kind of processing method of oil-extraction plant acidic gas, by the use of sour gas as cement plant shaft kiln
Fuel, when sour gas burns in kiln, H therein2There is chemical reaction with cement material and generate CaSO in S compositions4, other are harmful to
Composition is also sintered and converts, fundamentally solve Acidic Gas Treating problem, meanwhile, sour gas as a kind of gaseous fuel,
Make cement plant energy-saving fuel, realize environmental protection and solve the dual purpose of fuel, but, this method has certain limitation
Property, it is not easy to promote.
In a kind of methods for preparing NaHS of CN101337661A, caustic soda is first respectively adopted and milk of lime absorbs and contains sulphur
Change interstitial fluid in the sour gas generation of hydrogen and carbon dioxide, then mixed in proportion, obtain the NaHS product of low-carbon (LC) acid group.
The method does not require that sour gas is purer hydrogen sulfide gas, but flow is more long, and automaticity is low.
Document《Hydrogen sulfide is absorbed with sodium hydroxide solution produce vulcanized sodium industrial technology》(Shangfang is given birth,《Inorganic chemicals industry》,
The 2nd phase of volume 44,2 months 2012) hydrogen sulfide sodium hydroxide solution absorbs and produces the production technology of vulcanized sodium by the technique,
Hydrogen sulfide is absorbed in packed tower with 380~420g/L sodium hydroxide solutions, control of reaction end point vulcanized sodium mass concentration is 330
~350g/L, hydrogen sulfide absorption rate is up to 95%~98%.The technique not only can effective environmental protection, and effect can be created for enterprise
Benefit.But, this process products vulcanized sodium is apt to deteriorate, and is difficult storage.
At present, it is necessary to a kind of consider the factors such as safe and environment-friendly, economy for small-sized sour gas
Acidic Gas Treating method.
The content of the invention
For deficiency of the prior art, the present invention provides a kind of Acidic Gas Treating process and device, with existing skill
Art is compared, and Acidic Gas Treating process of the present invention and device are produced while sour gas qualified discharge is realized and meet what is required
NaHS products, realize the double goal of sour gas purification and pollutant resources.
Acidic Gas Treating technique of the present invention, with NaOH solution as absorbing liquid, treatment sour gas production NaHS, including following step
Suddenly：
（1）Sour gas enters first-stage reactor, is contacted with the reaction solution of second reactor and is reacted, reaction generation
Liquid point two-way, the first via is discharged as product, and the second tunnel loops back first-stage reactor；
（2）By step（1）Reacted sour gas enters second reactor, the life with NaOH solution and third-stage reactor
Reacted into liquid contact；Reaction solution point tertiary road, the first via enters first-stage reactor, the circulation of the second tunnel as absorbing liquid
Second reactor is returned, the 3rd tunnel enters third-stage reactor as absorbing liquid；
（3）By step（2）Reacted sour gas enters third-stage reactor, is connect with the 3rd road second reactor generation liquid
Touch and reacted, reaction solution point two-way, the first via enters second reactor, and the second tunnel loops back third-stage reactor；
（4）By step（3）Reacted sour gas enters level four reaction apparatus, anti-with methyl diethanolamine (MDEA) solution
Should, reacted sour gas discharge, reaction solution regeneration Posterior circle is used.
In present invention process, step（1）In, loop back the second road reaction solution and first-stage reactor of first-stage reactor
The volume flow ratio of overall reaction generation liquid is 1/3~9/10, preferably 5/6~8/9.
In present invention process, step（2）In, loop back the second road reaction solution and second reactor of second reactor
The volume flow ratio of overall reaction generation liquid is 1/3~9/10, preferably 1/2~8/9.
In present invention process, step（2）In, the 3rd road reaction solution and two of third-stage reactor is entered as absorbing liquid
The volume flow ratio of stage reactor overall reaction generation liquid is 1/6~1/2, preferably 1/5~1/4.
In present invention process, step（3）In, loop back the second road reaction solution and third-stage reactor of third-stage reactor
The volume flow ratio of overall reaction generation liquid is 1/3~9/10, preferably 1/5~1/4.
In present invention process, step（4）In, MDEA solution is 8L/m with the liquid-gas ratio of sour gas3~15L/m3Between, preferably
It is 10L/m3~12L/m3.The mass concentration of MDEA solution is 20% ~ 50%, preferably 30% ~ 40%.
In present invention process, the consumption of NaOH solution is design load, according to H in sour gas2S, CO2The fixation that content determines
Value, according to the amount of sour gas, according to H in sour gas2S and CO2NaOH solution amount needed for complete Response calculation, design load is for needed for
The 80 ~ 99% of NaOH solution consumption, preferably 85 ~ 95%.
In present invention process, the addition of NaOH solution passes through step（4）Hydrogen sulfide content is adjusted in sour gas after treatment
Section, by adjusting valve regulation NaOH solution addition, it is ensured that by step（4）Hydrogen sulfide content is 5- in sour gas after treatment
30mg/Nm3, and ensureing H2NaOH solution is not excessive in the case of S qualified discharges.
In present invention process, by step（4）Sour gas after treatment is further discharged after coalescer demisting.By step
Suddenly（4）Hydrogen sulfide content is 5-30 mg/Nm in sour gas after treatment3。
In present invention process, the reaction temperature of first-stage reactor and second reactor is 70 DEG C~100 DEG C, preferably 80 DEG C
~95 DEG C.
In present invention process, reaction temperature is 60 DEG C~90 DEG C, preferably 65 DEG C in third-stage reactor and level four reaction apparatus
~80 DEG C.
In present invention process, first-stage reactor, second reactor, third-stage reactor, level four reaction apparatus are that gas-liquid mass transfer is anti-
Answer equipment, specially bubbling column reactor, filler tower reactor, impact flow reactor, rotary drill reactor and venturi reaction
One or more in device.
In present invention process, third-stage reactor, level four reaction apparatus are rotary drill reactor.
In present invention process, third-stage reactor and level four reaction apparatus use rotary drill reactor, three-level rotary drill reactor
It it is 50~5000 revs/min, preferably 150~2000 revs/min with the rotating speed of the revolving bed of level Four rotary drill reactor.
In present invention process, third-stage reactor and level four reaction apparatus use rotary drill reactor, reaction mass to be revolved in three-level
The residence time is 2~600 seconds, preferably 10~100 seconds in rotated bed reactor and level Four rotary drill reactor.
In present invention process, first-stage reactor, second reactor are venturi reactor.
In present invention process, the venturi reactor from top to bottom divides three sections, and epimere is liquid phase storage tank, and stage casing is straight tube
Reaction tube, hypomere is gas-liquid separation cylinder；The straight tube reaction tube is from top to bottom followed successively by feed zone, contraction section, trunnion section, expansion
Section and discharging section；Feed zone top forms sleeve structure with liquid phase storage tank, and discharging pars infrasegmentalis is connected with gas-liquid separation cylinder, liquid phase storage
Groove is provided with gas phase entrance, and gas phase entry position is provided with circulation fluid entrance higher than end entrance on feed zone, liquid phase storage groove sidewall；Directly
The tube wall of cylinder reaction tube is provided with absorbing liquid entrance, and absorbing liquid entrance is located at trunnion top；Gas-liquid separation cylinder be provided with gaseous phase outlet and
Liquid-phase outlet.
In present invention process, the second tunnel loops back the reaction solution of first-stage reactor respectively from circulation fluid entrance and absorption
Liquid entrance enters first-stage reactor.
In present invention process, the reaction solution for entering first-stage reactor from circulation fluid entrance enters with from absorbing liquid entrance
The reaction solution volume flow ratio of first-stage reactor is 1/6~1/2, preferably 1/4~1/3.
In present invention process, the second tunnel loops back the reaction solution of second reactor respectively from circulation fluid entrance and absorption
Liquid entrance enters first-stage reactor.
In present invention process, the reaction solution for entering second reactor from circulation fluid entrance enters with from absorbing liquid entrance
The reaction solution volume flow ratio of second reactor is 1/6~1/2, preferably 1/4~1/3.
In present invention process, the venturi reactor, feed zone upper end opens up teeth groove, tooth slot structure be fan-shaped teeth groove,
One kind in square teeth groove and triangle teeth groove, preferably lance tooth slot structure.
In present invention process, the venturi reactor, absorbing liquid entrance connection liquid phase distributor, liquid phase distributor is set
On straight tube reaction tube center line, absorbing liquid is sprayed from top to bottom, liquid phase distributor is settable 1 ~ 10, preferably 4 ~ 6.
In present invention process, the sour gas is hydrogen sulfide containing gas, can be various sources containing H2S sour gas,
CO in the sour gas2Volume fraction be less than 7%, preferably smaller than 5%.The NaOH solution mass concentration is 20%~60%, excellent
Elect 32%~38% as.
In present invention process, control first-stage reactor discharge liquid phase be NaHS solution, products pot through analysis detection it is qualified after,
Start, through product pump carrying device, to realize continuous discharge.
A kind of Acidic Gas Treating device of the present invention, described device includes that first-stage reactor, second reactor, three-level are anti-
Answer device, level four reaction apparatus, three-level pans, level Four pans, wherein, first-stage reactor, second reactor, third-stage reactor and
Level four reaction apparatus are respectively provided with gas phase entrance, gaseous phase outlet, liquid phase entrance and liquid-phase outlet, and sour gas suction line is anti-with one-level
Device gas phase entrance is answered to connect, the gaseous phase outlet of first-stage reactor is connected with the gas phase entrance of second reactor, second reactor
Gaseous phase outlet is connected with the gas phase entrance of third-stage reactor, the gaseous phase outlet of third-stage reactor and the gas phase entrance of level four reaction apparatus
Connection, level four reaction apparatus gaseous phase outlet is connected with clean gas outlet pipeline, and hydrogen sulfide content is provided with clean gas outlet pipeline
Detection means；The liquid phase entrance of second reactor is connected with alkali liquor inlet pipeline, and the liquid phase entrance of level four reaction apparatus is molten with MDEA
Liquid suction line is connected；Third-stage reactor liquid-phase outlet after three-level pans respectively with third-stage reactor liquid phase entrance and two grades
Reactor liquid phase entrance is connected；Second reactor liquid-phase outlet respectively with first-stage reactor liquid phase entrance, second reactor liquid phase
Entrance and third-stage reactor liquid phase entrance are connected；First-stage reactor liquid-phase outlet respectively with first-stage reactor liquid phase entrance and product
Discharging pipeline connection.
Acidic Gas Treating device of the present invention, is provided between level four reaction apparatus gaseous phase outlet and clean gas outlet pipeline
Coalescer, the coalescer is cylindrical tube, and end socket includes upper cover and low head, and inside sets cylindric screen cloth.
Acidic Gas Treating device of the present invention, the first-stage reactor, second reactor, third-stage reactor, level Four are anti-
Answer device for gas-liquid mass transfer consersion unit, specially bubbling column reactor, filler tower reactor, impact flow reactor, revolving bed is anti-
Answer the one kind in device and venturi reactor.
Acidic Gas Treating device of the present invention, the first-stage reactor, second reactor are venturi reactor, three-level
Reactor, level four reaction apparatus are rotary drill reactor.
Another Acidic Gas Treating device of the present invention, described device includes first-stage reactor, second reactor, three-level
Reactor, level four reaction apparatus, three-level pans, level Four pans, wherein, first-stage reactor, second reactor are that venturi is anti-
Device, three sections of the venturi reactor point are answered, epimere is liquid phase storage tank, and stage casing is straight tube reaction tube, and hypomere is gas-liquid separation cylinder；
The straight tube reaction tube is from top to bottom followed successively by feed zone, contraction section, trunnion section, expansion segment and discharging section；Feed zone top with
Liquid phase storage tank forms sleeve structure, and discharging section is connected with gas-liquid separation cylinder, and liquid phase storage tank is provided with gas phase entrance, gas phase entry position
Higher than end entrance on feed zone, liquid phase storage groove sidewall is provided with circulation fluid entrance；The tube wall of straight tube reaction tube is provided with absorbing liquid and enters
Mouthful, absorbing liquid entrance is located at trunnion top；Gas-liquid separation cylinder is provided with gaseous phase outlet and liquid-phase outlet；Third-stage reactor and level Four are anti-
Device is answered to be respectively provided with gas phase entrance, gaseous phase outlet, absorbing liquid entrance and liquid-phase outlet, sour gas suction line and first-stage reactor
Gas phase entrance is connected, and the gaseous phase outlet of first-stage reactor is connected with the gas phase entrance of second reactor, the gas phase of second reactor
Outlet is connected with the gas phase entrance of third-stage reactor, and the gaseous phase outlet of third-stage reactor connects with the gas phase entrance of level four reaction apparatus
Connect, level four reaction apparatus gaseous phase outlet is connected with clean gas outlet pipeline, hydrogen sulfide content inspection is provided with clean gas outlet pipeline
Survey device；The absorbing liquid entrance of second reactor is connected with alkali liquor inlet pipeline respectively, level four reaction apparatus absorbing liquid entrance with
MDEA solution inlets pipeline is connected；Third-stage reactor liquid-phase outlet enters with third-stage reactor absorbing liquid respectively after three-level pans
Mouth and the connection of second reactor absorbing liquid entrance；Second reactor liquid-phase outlet respectively with first-stage reactor absorbing liquid entrance, two
Stage reactor absorbing liquid entrance, the connection of second reactor circulation fluid entrance and the connection of third-stage reactor absorbing liquid entrance；One-level is anti-
Device liquid-phase outlet is answered to connect with first-stage reactor circulation fluid entrance, first-stage reactor absorbing liquid entrance and product discharge pipeline respectively
Connect.
Acidic Gas Treating device of the present invention, the venturi reactor, feed zone upper end is to open up teeth groove, teeth groove knot
Structure is the one kind in fan-shaped teeth groove, square teeth groove and triangle teeth groove, preferably lance tooth slot structure.
Acidic Gas Treating device of the present invention, the venturi reactor, absorbing liquid entrance connection liquid phase distributor, liquid
Distributed mutually device is arranged on straight tube reaction tube center line, and absorbing liquid is sprayed from top to bottom, and liquid phase distributor is settable 1 ~ 10, excellent
Select 4 ~ 6.
Acidic Gas Treating device of the present invention, absorbing liquid entrance is arranged on the straight tube reaction pipe outer wall on contraction section top
On, it is preferably provided between liquid phase storage tank bottom and contraction section.
Acidic Gas Treating device of the present invention, the gas-liquid separation cylinder of the venturi reactor sets and takes hot facility, controls
Temperature processed is 85 DEG C~120 DEG C, preferably 90 DEG C~95 DEG C, prevents intermediate product from crystallizing.
Compared with prior art, sour gas absorption technique of the present invention and device have the following advantages that：
1st, Acidic Gas Treating process of the invention, using level Four gas-liquid two-phase counter-current absorption course of reaction, there is provided
The self-loopa of reaction solution reabsorbs operation, improves reaction depth, material is fully contacted with sour gas, it is ensured that NaHS liquid
Phase product meets national product quality standard, Na in product NaHS2The content of S is less than 4%；Circulated by reaction mass, make alkali lye
Fully contacted with sour gas so that H in purified gas2S contents are less than 30 mg/Nm3, it is ensured that the weary gas after Acidic Gas Treating is realized reaching
Mark the target of discharge.
2nd, Acidic Gas Treating process of the present invention, with NaOH solution, MDEA solution biabsorption liquid as absorbent, reduces system
Alkali lye is to CO in system2Absorption, and ensure H in tail gas2S contents realize qualified discharge.NaOH alkali is added by second reactor
Liquid, reduces alkali lye to CO2Absorption depth, reduce alkali lye to CO2Uptake, level four reaction apparatus add the double of MDEA absorbing liquids
Absorbing liquid method, using the short characteristic of rotary drill reactor gas-liquid contact time, H is absorbed using MDEA solvent selectivities2S, carries
MDEA selective absorbings H high2The ability of S, it is ensured that purified gas qualified discharge.Reduce CO2Suction rate, makes CO altogether2Major part stays in purification
In gas outside discharger system, so as to reduce CO in system2Overreaction, and product Na2CO3、NaHCO3Growing amount,
Prevent crystallization from separating out.
3rd, Acidic Gas Treating process of the present invention, by obtaining second order reaction rich in Na2CO3The reaction life of solution
Used into third-stage reactor as absorbing liquid into liquid, realize further absorbing H2S simultaneously displaces CO simultaneously2Purpose, reduce inhale
Receive the CO in sour gas2, reduce the Na in liquid-phase product2CO3、NaHCO3Growing amount, prevent crystallization separate out, it is ensured that device is long
Periodic duty.
4th, using venturi reactor of the present invention as first-stage reactor and second reactor, reaction solution passes through literary mound
In reactor circulation fluid entrance enter reactor liquid phase storage tank, when circulation fluid position be higher than feed zone entrance when, circulation it is anti-
Liquid should be generated and form overflow, be distributed with wall manifold state in whole wall of reactor, uniform liquid is formed in reactor wall
Film, with liquid film as division board, not only prevents crystal from separating out adhesive reaction device inwall, meanwhile, with liquid film as heat-absorbing medium, take out
Reaction heat, effectively prevents reaction solution excessive vaporization.
5th, Acidic Gas Treating system of the present invention is using high-gravity rotating bed as gas-liquid reactor, be capable of achieving to improve mass transfer with
The target of reaction efficiency, rotary drill reactor is efficient mass transfer equipment, it is ensured that reaction is quickly carried out, and reduces the generation of side reaction,
Reduce impurity content in product.Meanwhile, because rotary drill reactor mass-transfer efficiency is the hundreds of of common tower reactor mass-transfer efficiency
Times, reactor scale is greatly reduced.And by CO in sour gas2When being reacted with NaOH, nano level Na is generated2CO3Crystalline solid, from
And Na when preventing fluid from conveying2CO3Crystalline solid blocks pipeline.Material on the bed component inwall of high-speed rotation, acutely hit by formation
Hit, realize reinforcing mixing；Material is constantly cut into drop, brin and liquid film when bed is flowed through by bed, greatly realizes
The Surface Renewal of high-viscosity material with mix, eliminate concentration difference, generate nano level Na2CO3Crystalline solid.
6th, Acidic Gas Treating process of the present invention, H is absorbed in level four reaction apparatus using MDEA solution-selectives2S, is reduced
CO2Suction rate, takes full advantage of rotary drill reactor efficient mass transfer altogether, and the short characteristic of gas-liquid contact time improves the choosing of MDEA solution
Selecting property absorbs H2The ability of S, reduces CO2Suction rate altogether.
7th, novel acid gas disposal process of the present invention and device are particularly suited for processing small-sized sour gas, and existing
There is technology to compare, equipment scale is small, energy consumption is low, operating cost is few, the NaHS that generation can be used for the industries such as printing and dyeing, papermaking is produced
Product, are readily transported, and have certain market value.
Brief description of the drawings
Fig. 1 is a kind of Acidic Gas Treating process of the invention and schematic device.
Fig. 2 is present invention another kind Acidic Gas Treating process and schematic device.
Fig. 3 is venturi reactor schematic diagram in Acidic Gas Treating process shown in the present invention and device.
Specific embodiment
Acidic Gas Treating process of the present invention and device, with NaOH solution as absorbing liquid, treatment oil-extraction plant acidic gas life
NaHS products are produced, using level Four gas-liquid two-phase counter-current absorption course of reaction.
As shown in figure 1, Acidic Gas Treating device shown in the first implementation method of the invention, described device includes first order reaction
Device 3, second reactor 4, third-stage reactor 6, level four reaction apparatus 8, three-level pans 7, level Four pans 9, wherein, first order reaction
Device 3, second reactor 4, third-stage reactor 6 and level four reaction apparatus 8 be respectively provided with gas phase entrance, gaseous phase outlet, liquid phase entrance and
Liquid-phase outlet, sour gas suction line 1 is connected with first-stage reactor gas phase entrance, and the gaseous phase outlet of first-stage reactor and two grades are anti-
The gas phase entrance of device is answered to connect, the gaseous phase outlet of second reactor is connected with the gas phase entrance of third-stage reactor, third-stage reactor
Gaseous phase outlet be connected with the gas phase entrance of level four reaction apparatus, level four reaction apparatus gaseous phase outlet is through pipeline and clean gas outlet pipeline
13 connections, are provided with hydrogen sulfide content detection means 5 on clean gas outlet pipeline；Liquid phase entrance and the alkali lye of second reactor enter
Mouth pipeline 10 is connected, and the liquid phase entrance of level four reaction apparatus is connected with MDEA solution inlets pipeline 11, third-stage reactor liquid-phase outlet
Point two-way after three-level pans, 19 is connected with third-stage reactor liquid phase entrance all the way, another road 20 and second reactor liquid phase
Entrance is connected；Second reactor liquid-phase outlet point three tunnels, 15 are connected with second reactor liquid phase entrance all the way, and all the way 16 and one-level
Reactor liquid phase entrance is connected, and 17 is connected with third-stage reactor liquid phase entrance all the way；First-stage reactor liquid-phase outlet point two-way, one
Road 18 and first-stage reactor liquid phase entrance, 14 are connected with product discharge pipeline all the way.
Acidic Gas Treating process of the present invention, the sour gas from sour gas suction line 1 initially enters first order reaction
Device 3, with the generation liquid haptoreaction from second reactor, reaction solution is divided into two-way, wherein all the way 18 and first order reaction
Device liquid phase entrance is connected, and another road 14 and product discharge pipeline are connected.Enter two by the sour gas after first-stage reactor treatment
Stage reactor 4, with the generation liquid from third-stage reactor and NaOH alkali lye haptoreactions, reaction solution is divided into three tunnels, all the way
Generation liquid 16 enters first-stage reactor as absorbing liquid through first-stage reactor liquid phase entrance, liquid 15 is generated all the way and enters second order reaction
Device, generates liquid 17 and enters third-stage reactor as absorbing liquid all the way.Enter three-level by the reacted sour gas of second reactor
Reactor 6, with second reactor generation liquid reaction, reacted generation liquid enters three-level pans 7, then divides two-way, first
Road 20 enters second reactor through pipeline as absorbing liquid, and the second tunnel 19 loops back third-stage reactor through pipeline；It is anti-by three-level
The reacted sour gas of device is answered to enter level four reaction apparatus 8, and MDEA solution haptoreactions from MDEA solution inlets pipeline 11,
Through purifying the qualified discharge of gas pipeline 13 after the further demisting of reacted sour gas coalescer 2, reacted generation liquid enters four
Enter MDEA solution regeneration systems after level pans 9, MDEA solution is recycled after regeneration.
As shown in Fig. 2 Acidic Gas Treating device shown in second implementation method of the invention, described device includes first order reaction
Device 3, second reactor 4, third-stage reactor 6, level four reaction apparatus 8, three-level pans 7, level Four pans 9, wherein, first order reaction
Device, second reactor divide three sections, and epimere is liquid phase storage tank 34, and stage casing is straight tube reaction tube 30, and hypomere is gas-liquid separation cylinder 41；Institute
State straight tube reaction tube and be from top to bottom followed successively by feed zone 33, contraction section 37, trunnion section 38, expansion segment 39 and discharging section 40；Charging
Section top forms sleeve structure with liquid phase storage tank, and discharging section 40 is connected with gas-liquid separation cylinder 41, and liquid phase storage tank is provided with gas phase entrance
31, gas phase entry position is provided with circulation fluid entrance 32 higher than end entrance on feed zone, liquid phase storage groove sidewall；Straight tube reaction tube
Tube wall is provided with absorbing liquid entrance 35, and absorbing liquid entrance is located at trunnion top；Gas-liquid separation cylinder is provided with gaseous phase outlet 42 and liquid phase goes out
Mouth 43；Third-stage reactor and level four reaction apparatus are respectively provided with gas phase entrance, gaseous phase outlet, absorbing liquid entrance and liquid-phase outlet, acid
Property gas suction line 1 be connected with first-stage reactor gas phase entrance, the gaseous phase outlet of first-stage reactor and the gas phase of second reactor
Entrance is connected, and the gaseous phase outlet of second reactor is connected with the gas phase entrance of third-stage reactor, the gaseous phase outlet of third-stage reactor
It is connected with the gas phase entrance of level four reaction apparatus, level four reaction apparatus gaseous phase outlet is connected with clean gas outlet pipeline 11, and purified gas go out
Hydrogen sulfide content detection means 5 is provided with mouth pipeline；The liquid phase entrance of second reactor is connected with alkali liquor inlet pipeline 10, and four
The liquid phase entrance of stage reactor is connected with MDEA solution inlets pipeline 11, level four reaction apparatus liquid-phase outlet after pans 12 with
MDEA solution regeneration systems are connected, third-stage reactor liquid-phase outlet point two-way after three-level pans, and all the way 19 and third-order reaction
Device absorbing liquid entrance is connected, and another road 20 is connected with second reactor absorbing liquid entrance；Four tunnels of second reactor liquid-phase outlet point,
15 it is connected with second reactor absorbing liquid entrance all the way, 21 is connected with second reactor circulation fluid entrance all the way, all the way 16 and one
Stage reactor absorbing liquid entrance is connected, and 17 is connected with third-stage reactor absorbing liquid entrance all the way；First-stage reactor liquid-phase outlet point
Three tunnels, 18 are connected with first-stage reactor absorbing liquid entrance all the way, 22 are connected with first-stage reactor circulation fluid entrance all the way, and all the way 14
It is connected with product discharge pipeline.
Acidic Gas Treating process of the present invention, the sour gas from sour gas suction line 1 initially enters first order reaction
Device 3, with the generation liquid haptoreaction from second reactor, reaction solution is divided into three tunnels, wherein all the way 18 and first order reaction
Device liquid phase entrance is connected, and another road 14 and product discharge pipeline are connected, 22 be connected with first-stage reactor circulation fluid entrance all the way, its
In, first order reaction generation liquid 22 enters reactor liquid phase storage tank by the circulation fluid entrance of venturi reactor, when circulation liquid level
Put during higher than feed zone entrance, the reaction solution of circulation forms overflow, is carried out with wall manifold state in whole wall of reactor
Distribution, uniform liquid film is formed in reactor wall, with liquid film as division board, not only prevents crystal from separating out in adhesive reaction device
Wall, meanwhile, with liquid film as heat-absorbing medium, reaction heat is taken out, reaction solution excessive vaporization is effectively prevented, prevent crystallization.One-level
Sour gas after reactor for treatment enters second reactor 4, is contacted instead with generation liquid and NaOH alkali lye from third-stage reactor
Should, reaction solution is divided into four tunnels, and it is anti-into one-level through first-stage reactor liquid phase entrance as absorbing liquid that the first via generates liquid 16
Device, the second tunnel generation liquid 15 is answered to enter second reactor, the 3rd tunnel generation liquid 17 enters third-stage reactor, the 4th tunnel generation liquid 21
It is connected with second reactor circulation fluid entrance；Wherein, the 4th tunnel generation liquid 21 into second reactor is in second reactor
Downflow weir is formed, is distributed with wall manifold state on whole second reactor wall, uniform liquid film is formed in reactor wall,
With liquid film as division board, not only prevent crystal from separating out adhesive reaction device inwall, meanwhile, with liquid film as heat-absorbing medium, take out anti-
Should be hot, effectively prevent Na2S solution excessive vaporizations, prevent crystallization.Enter three-level by the reacted sour gas of second reactor anti-
Device 6 is answered, with second reactor generation liquid reaction, reacted generation liquid enters three-level pans 7, then divides two-way, the first via
20 enter second reactor through pipeline as absorbing liquid, and the second tunnel 19 loops back third-stage reactor through pipeline；By third-order reaction
The reacted sour gas of device enters level four reaction apparatus 8, and MDEA solution haptoreactions from MDEA solution inlets pipeline 11, instead
Through purifying the qualified discharge of gas pipeline 13 after the further demisting of sour gas coalescer 21 after answering, reacted generation liquid enters level Four
Enter MDEA solution regeneration systems after pans 9, MDEA solution is recycled after regeneration.
Sour gas comprehensive utilization process method of the present invention includes following four process：
（1）Course of reaction in first-stage reactor
Key reaction is as follows in first-stage reactor：Undressed sour gas and second order reaction generation liquid（Na2S、
Na2CO3、NaHCO3Mixture）Reacted, in H2In the case of S excess, the Na in second order reaction generation liquid2CO3、
NaHCO3、Na2S respectively with H2S reacts, and generates NaHS solution.The NaHS solution of generation point two-way, the first via is delivered in finished pot；
Deliver to first-stage reactor in the second road.
（2）Course of reaction in second reactor
The main reaction of second reactor is as follows：Gas phase is " the weary gas " of first order reaction gas phase, wherein H2The reduction of S concentration,
But still it is not reaching to discharge standard；Second order reaction liquid phase is that third-stage reactor generates liquid and NaOH solution.By further anti-
Should, gas phase is purified, and generates certain density Na2S solution, is partly delivered to first-stage reactor and continues anti-as absorbing liquid
Should, second reactor is partly looped back, some enters level four reaction apparatus as absorbing liquid.
（3）Course of reaction in third-stage reactor
Key reaction is as follows in third-stage reactor：Third-order reaction gas phase is " the weary gas " that gas phase is reacted in the second level, wherein
H2S concentration is greatly reduced, but still is not carried out qualified discharge requirement.Third-order reaction is with being rich in that second order reaction is obtained
Na2CO3The reaction solution of solution is absorbing liquid, in H2In the case that S is a small amount of, Na2CO3With H2S reacts, and generates a small amount of Na2S,
Realize absorbing H2S replaces CO2Purpose, reduce absorb sour gas in CO2, reduce the Na in liquid-phase product2CO3、NaHCO3's
Growing amount, prevents crystallization from separating out, it is ensured that device long-term operation.
（4）Course of reaction in level four reaction apparatus
Key reaction is as follows in level four reaction apparatus：Fourth-order reaction gas phase is " the weary gas " that the third level reacts gas phase, wherein
H2S concentration is extremely low, basically reaches emission request, but CO2Content is of a relatively high.Fourth-order reaction is sharp with MDEA solution as absorbing liquid
H is absorbed with MDEA solution-selectives2S, reduces CO2Suction rate, takes full advantage of rotary drill reactor efficient mass transfer, gas-liquid contact altogether
Time short characteristic, improves MDEA solution-selectives and absorbs H2The ability of S, reduces CO2Suction rate altogether.
Reaction effect of the invention is illustrated with reference to embodiment, but is not therefore limited the scope of the invention.
Embodiment 1
Using processing method and processing device as shown in Figure 1, with sour gas and NaOH solution as raw material, reacted.It is acid
CO in gas2Volume fraction is 7%, H2S volume fractions are 92%, and hydro carbons volume fraction is 1%.NaOH solution mass concentration is 38%.
In embodiment 1, first-stage reactor and second reactor use venturi reactor, third-stage reactor and fourth-order reaction
Device uses rotary drill reactor, and the venturi reactor and rotary drill reactor can be that venturi generally in the art reacts
Device and rotary drill reactor.
In embodiment 1, the second road reaction solution and first-stage reactor overall reaction for looping back first-stage reactor generate liquid
Volume flow ratio be 5：6.The the second road reaction solution and second reactor overall reaction for looping back second reactor generate liquid
Volume flow ratio be 1：2.Second order reaction generation liquid into third-stage reactor generates the body of liquid with second reactor overall reaction
Product flow-rate ratio is 1：4.The the second road reaction solution for looping back third-stage reactor generates the body of liquid with third-stage reactor overall reaction
Product flow-rate ratio is 5：6.MDEA solution is 10 L/m with the liquid-gas ratio of sour gas3.The mass concentration of MDEA solution is 30%.
In one-level venturi reactor and two grades of venturi reactors reaction temperature be 80 DEG C, three-level rotary drill reactor and
The reaction temperature of level Four rotary drill reactor is 75 DEG C.The revolving bed of three-level rotary drill reactor and level Four rotary drill reactor
Rotating speed is 1500 revs/min.Three-level rotary drill reactor and level Four rotary drill reactor reaction mass residence time in reactor
It it is 10 seconds, reaction result is shown in Table 1.
Embodiment 2
Using process and system as shown in Figure 2, in embodiment 2, first-stage reactor and second reactor use Fig. 3
Shown venturi reactor, third-stage reactor and level four reaction apparatus use rotary drill reactor.
In embodiment 2, the reaction solution for looping back first-stage reactor through first-stage reactor absorbing liquid entrance is anti-with one-level
The volume flow ratio for answering device overall reaction to generate liquid is 5：8.The anti-of first-stage reactor is looped back through first-stage reactor circulation fluid entrance
The volume flow ratio that liquid should be generated with first-stage reactor overall reaction generation liquid is 5：24.
Reaction solution and the second reactor overall reaction of second reactor are looped back through second reactor absorbing liquid entrance
The volume flow ratio for generating liquid is 1：3.Through second reactor circulation fluid entrance loop back the reaction solution of second reactor with
The volume flow ratio of second reactor overall reaction generation liquid is 1：6.Second order reaction into third-stage reactor generates liquid and two grades
The volume flow ratio of reactor overall reaction generation liquid is 1：4.
The the second road reaction solution for looping back third-stage reactor generates the volume flow of liquid with third-stage reactor overall reaction
Than being 5：6.
MDEA solution is 10 L/m with the liquid-gas ratio of sour gas3.The mass concentration of MDEA solution is 30%.One-level venturi
Reaction temperature is 80 DEG C in reactor and two grades of venturi reactors.Three-level rotary drill reactor and level Four rotary drill reactor
Reaction temperature is 75 DEG C.The rotating speed of the revolving bed of three-level rotary drill reactor and level Four rotary drill reactor is 1500 revs/min.Three
Level rotary drill reactor and level Four rotary drill reactor the reaction mass residence time in reactor are 10 seconds, and reaction result is shown in Table
1。
Comparative example 1
Same as Example 1, difference only uses a kind of absorbing liquids of NaOH not use MDEA solution to absorb.
The embodiment of table 1 and comparative example reaction result
Claims (48)
1. a kind of Acidic Gas Treating technique, with NaOH solution as absorbing liquid, processes sour gas production NaHS, comprises the following steps：
（1）Sour gas enters first-stage reactor, is contacted with the reaction solution of second reactor and is reacted, reaction solution point
Two-way, the first via is discharged as product, and the second tunnel loops back first-stage reactor；
（2）By step（1）Reacted sour gas enters second reactor, with NaOH solution and the generation liquid of third-stage reactor
Contact is reacted；Reaction solution point tertiary road, the first via enters first-stage reactor as absorbing liquid, and the second tunnel loops back two
Stage reactor, the 3rd tunnel enters third-stage reactor as absorbing liquid；
（3）By step（2）Reacted sour gas enters third-stage reactor, contacted with the 3rd road second reactor generation liquid into
Row reaction, reaction solution point two-way, the first via enters second reactor, and the second tunnel loops back third-stage reactor；
（4）By step（3）Reacted sour gas enters level four reaction apparatus, with MDEA solution reactions, reacted sour gas
Discharge, reaction solution regeneration Posterior circle is used；
Wherein, first-stage reactor, second reactor are venturi reactor, and the venturi reactor from top to bottom divides three sections,
Epimere is liquid phase storage tank, and stage casing is straight tube reaction tube, and hypomere is gas-liquid separation cylinder；The straight tube reaction tube is from top to bottom followed successively by
Feed zone, contraction section, trunnion section, expansion segment and discharging section；Feed zone top forms sleeve structure with liquid phase storage tank, under discharging section
Portion is connected with gas-liquid separation cylinder, and liquid phase storage tank is provided with gas phase entrance, and gas phase entry position is higher than end entrance on feed zone, liquid phase storage
Groove sidewall is provided with circulation fluid entrance；The tube wall of straight tube reaction tube is provided with absorbing liquid entrance, and absorbing liquid entrance is located at trunnion top；
Gas-liquid separation cylinder is provided with gaseous phase outlet and liquid-phase outlet.
2. according to the technique described in claim 1, it is characterised in that：Step（1）In, the second tunnel for looping back first-stage reactor is anti-
The volume flow ratio that liquid should be generated with first-stage reactor overall reaction generation liquid is 1/3~9/10.
3. according to the technique described in claim 2, it is characterised in that：Step（1）In, the second tunnel for looping back first-stage reactor is anti-
The volume flow ratio that liquid should be generated with first-stage reactor overall reaction generation liquid is 5/6~8/9.
4. according to the technique described in claim 1, it is characterised in that：Step（2）In, the second tunnel for looping back second reactor is anti-
The volume flow ratio that liquid should be generated with second reactor overall reaction generation liquid is 1/3~9/10.
5. according to the technique described in claim 4, it is characterised in that：Step（2）In, the second tunnel for looping back second reactor is anti-
The volume flow ratio that liquid should be generated with second reactor overall reaction generation liquid is 1/2~8/9.
6. according to the technique described in claim 1, it is characterised in that：Step（2）In, enter third-stage reactor as absorbing liquid
3rd road reaction solution is 1/6~1/2 with the volume flow ratio of second reactor overall reaction generation liquid.
7. according to the technique described in claim 6, it is characterised in that：Step（2）In, enter third-stage reactor as absorbing liquid
3rd road reaction solution is 1/5~1/4 with the volume flow ratio of second reactor overall reaction generation liquid.
8. according to the technique described in claim 1, it is characterised in that：Step（3）In, the second tunnel for looping back third-stage reactor is anti-
The volume flow ratio that liquid should be generated with third-stage reactor overall reaction generation liquid is 1/3~9/10.
9. according to the technique described in claim 8, it is characterised in that：Step（3）In, the second tunnel for looping back third-stage reactor is anti-
The volume flow ratio that liquid should be generated with third-stage reactor overall reaction generation liquid is 5/6~8/9.
10. according to the technique described in claim 1, it is characterised in that：The addition of NaOH solution passes through step（4）After treatment
Hydrogen sulfide content regulation in sour gas, by adjusting valve regulation NaOH solution addition, it is ensured that by step（4）Acid after treatment
Property gas in hydrogen sulfide content be 5-30 mg/Nm3, and ensureing H2NaOH solution is not excessive in the case of S qualified discharges.
11. according to the technique described in claim 1, it is characterised in that：By step（4）Sour gas after treatment is further through poly-
Discharged after knot device demisting.
12. according to the technique described in claim 1, it is characterised in that：By step（4）Hydrogen sulfide contains in sour gas after treatment
It is 5-30 mg/Nm to measure3。
13. according to the technique described in claim 1, it is characterised in that：The reaction temperature of first-stage reactor and second reactor is
70 DEG C~100 DEG C.
14. according to the technique described in claim 13, it is characterised in that：The reaction temperature of first-stage reactor and second reactor is
80 DEG C~95 DEG C.
15. according to the technique described in claim 1, it is characterised in that：Reaction temperature is in third-stage reactor and level four reaction apparatus
60 DEG C~90 DEG C.
16. according to the technique described in claim 15, it is characterised in that：Reaction temperature is in third-stage reactor and level four reaction apparatus
65 DEG C~80 DEG C.
17. according to the technique described in claim 1, it is characterised in that：MDEA solution is 8L/m with the liquid-gas ratio of sour gas3~15L/
m3。
18. according to the technique described in claim 17, it is characterised in that：MDEA solution is 10L/m with the liquid-gas ratio of sour gas3~
12L/m3。
19. according to the technique described in claim 1, it is characterised in that：Third-stage reactor, level four reaction apparatus are reacted for gas-liquid mass transfer
Equipment, specially bubbling column reactor, filler tower reactor, impact flow reactor, rotary drill reactor and venturi reactor
In one or more.
20. according to the technique described in claim 19, it is characterised in that：Third-stage reactor, level four reaction apparatus are rotating bed reaction
Device.
21. according to the technique described in claim 19, it is characterised in that：Third-stage reactor and level four reaction apparatus are anti-using revolving bed
Answer device, the rotating speed of the revolving bed of three-level rotary drill reactor and level Four rotary drill reactor is 50~5000 revs/min.
22. according to the technique described in claim 21, it is characterised in that：Three-level rotary drill reactor and level Four rotary drill reactor
Revolving bed rotating speed be 150~2000 revs/min.
23. according to the technique described in claim 19, it is characterised in that：Third-stage reactor and level four reaction apparatus are anti-using revolving bed
Device is answered, reaction mass residence time in three-level rotary drill reactor and level Four rotary drill reactor is 2~600 seconds.
24. according to the technique described in claim 23, it is characterised in that：Reaction mass revolves in three-level rotary drill reactor and level Four
The residence time is 10~100 seconds in rotated bed reactor.
25. according to the technique described in claim 1, it is characterised in that：Second tunnel loops back the reaction solution of first-stage reactor
Enter first-stage reactor from circulation fluid entrance and absorbing liquid entrance respectively.
26. according to the technique described in claim 25, it is characterised in that：The reaction for entering first-stage reactor from circulation fluid entrance is given birth to
It is 1/6~1/2 into liquid and the reaction solution volume flow ratio for entering first-stage reactor from absorbing liquid entrance.
27. according to the technique described in claim 26, it is characterised in that：The reaction for entering first-stage reactor from circulation fluid entrance is given birth to
It is 1/4~1/3 into liquid and the reaction solution volume flow ratio for entering first-stage reactor from absorbing liquid entrance.
28. according to the technique described in claim 1, it is characterised in that：Second tunnel loops back the reaction solution of second reactor
Enter first-stage reactor from circulation fluid entrance and absorbing liquid entrance respectively.
29. according to the technique described in claim 28, it is characterised in that：The reaction for entering second reactor from circulation fluid entrance is given birth to
It is 1/6~1/2 into liquid and the reaction solution volume flow ratio for entering second reactor from absorbing liquid entrance.
30. according to the technique described in claim 29, it is characterised in that：The reaction for entering second reactor from circulation fluid entrance is given birth to
It is 1/4~1/3 into liquid and the reaction solution volume flow ratio for entering second reactor from absorbing liquid entrance.
31. according to the technique described in claim 1, it is characterised in that：The venturi reactor, feed zone upper end opens up tooth
Groove, tooth slot structure is the one kind in fan-shaped teeth groove, square teeth groove and triangle teeth groove.
32. according to the technique described in claim 31, it is characterised in that：The tooth slot structure is lance tooth slot structure.
33. according to the technique described in claim 1, it is characterised in that：The venturi reactor, absorbing liquid entrance connection liquid phase
Distributor, liquid phase distributor is arranged on straight tube reaction tube center line, sprays absorbing liquid from top to bottom, and liquid phase distributor sets 1 ~
10.
34. according to the technique described in claim 33, it is characterised in that：The liquid phase distributor sets 4 ~ 6.
35. according to the technique described in claim 1, it is characterised in that：The sour gas is the hydrogen sulfide containing gas in various sources
Body, CO in sour gas2Volume fraction be less than 7%.
36. according to the technique described in claim 1, it is characterised in that：The NaOH solution mass concentration is 20%~60%,
The mass concentration of MDEA solution is 20% ~ 50%.
37. according to the technique described in claim 36, it is characterised in that：The NaOH solution mass concentration is 32%~38%；
The mass concentration of MDEA solution is 30% ~ 40%.
The sour gas absorption plant of the Acidic Gas Treating technique in 38. use claims 1 to 37 described in any claim, its
It is characterised by：Described device include first-stage reactor, second reactor, third-stage reactor, level four reaction apparatus, three-level pans,
Level Four pans, wherein, first-stage reactor, second reactor are venturi reactor, and the venturi reactor divides three sections, on
Section is liquid phase storage tank, and stage casing is straight tube reaction tube, and hypomere is gas-liquid separation cylinder；The straight tube reaction tube be from top to bottom followed successively by into
Material section, contraction section, trunnion section, expansion segment and discharging section；Feed zone top forms sleeve structure, discharging section and gas with liquid phase storage tank
Liquid cylinder is connected, and liquid phase storage tank is provided with gas phase entrance, and gas phase entry position is higher than end entrance on feed zone, liquid phase storage groove sidewall
It is provided with circulation fluid entrance；The tube wall of straight tube reaction tube is provided with absorbing liquid entrance, and absorbing liquid entrance is located at trunnion top；Gas-liquid point
Gaseous phase outlet and liquid-phase outlet are provided with from cylinder；Third-stage reactor and level four reaction apparatus are respectively provided with gas phase entrance, gaseous phase outlet, suction
Liquid entrance and liquid-phase outlet are received, sour gas suction line is connected with first-stage reactor gas phase entrance, and the gas phase of first-stage reactor goes out
Mouth is connected with the gas phase entrance of second reactor, and the gaseous phase outlet of second reactor is connected with the gas phase entrance of third-stage reactor,
The gaseous phase outlet of third-stage reactor is connected with the gas phase entrance of level four reaction apparatus, level four reaction apparatus gaseous phase outlet and clean gas outlet
Pipeline is connected, and hydrogen sulfide content detection means is provided with clean gas outlet pipeline；The absorbing liquid entrance difference of second reactor
It is connected with alkali liquor inlet pipeline, level four reaction apparatus absorbing liquid entrance is connected with MDEA solution inlet pipelines；Third-stage reactor liquid phase
Outlet is connected with third-stage reactor absorbing liquid entrance and second reactor absorbing liquid entrance respectively after three-level pans；Two grades anti-
Answer device liquid-phase outlet respectively with first-stage reactor absorbing liquid entrance, second reactor absorbing liquid entrance, second reactor circulation fluid
Entrance is connected and the connection of third-stage reactor absorbing liquid entrance；First-stage reactor liquid-phase outlet enters with first-stage reactor circulation fluid respectively
The connection of mouth, first-stage reactor absorbing liquid entrance and product discharge pipeline.
39. according to the device described in claim 38, it is characterised in that：The venturi reactor, feed zone upper end is to open up
Teeth groove, tooth slot structure is the one kind in fan-shaped teeth groove, square teeth groove and triangle teeth groove.
40. according to the device described in claim 39, it is characterised in that：The tooth slot structure is lance tooth slot structure.
41. according to the device described in claim 38, it is characterised in that：The venturi reactor, absorbing liquid entrance connection liquid
Distributed mutually device, liquid phase distributor is arranged on straight tube reaction tube center line, and absorbing liquid is sprayed from top to bottom, and liquid phase distributor is set
1 ~ 10.
42. according to the device described in claim 41, it is characterised in that：The liquid phase distributor sets 4 ~ 6.
43. according to the device described in claim 38, it is characterised in that：The straight tube that absorbing liquid entrance is arranged on contraction section top is anti-
Answer in pipe outer wall.
44. according to the device described in claim 38, it is characterised in that：Absorbing liquid entrance is arranged on liquid phase storage tank bottom and shrinks
Between section.
45. according to the device described in claim 38, it is characterised in that：Level four reaction apparatus liquid-phase outlet connects with MDEA regenerative systems
Connect.
46. according to the device described in claim 38, it is characterised in that：In level four reaction apparatus gaseous phase outlet and clean gas outlet pipe
Coalescer is provided between line, the coalescer is cylindrical tube, and end socket includes upper cover and low head, and inside sets cylindric
Screen cloth.
47. according to the device described in claim 38, it is characterised in that：The third-stage reactor, level four reaction apparatus are passed for gas-liquid
Qualitative response equipment, specially bubbling column reactor, filler tower reactor, impact flow reactor, rotary drill reactor and venturi
One kind in reactor.
48. according to the device described in claim 47, it is characterised in that：The third-stage reactor, level four reaction apparatus are revolving bed
Reactor.
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