CN104971597B - A kind of sour gas produces NaHS process and device - Google Patents
A kind of sour gas produces NaHS process and device Download PDFInfo
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- CN104971597B CN104971597B CN201410141475.2A CN201410141475A CN104971597B CN 104971597 B CN104971597 B CN 104971597B CN 201410141475 A CN201410141475 A CN 201410141475A CN 104971597 B CN104971597 B CN 104971597B
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Abstract
The invention discloses a kind of sour gas production NaHS device, described device includes reacting pipe, and reacting pipe one end is sour gas entrance, and the other end is exported for sour gas；Reacting pipe is divided into fourth-order reaction area by setting dividing plate, and first order reaction area, second order reaction area, third-order reaction area and fourth-order reaction area are followed successively by according to gas flow direction；Liquid phase spray equipment is respectively provided with per order reaction area, lower section per order reaction area is correspondingly arranged fluid reservoir, every grade of fluid reservoir top is respectively provided with fluid-tight component, and every grade of fluid reservoir is respectively provided with absorbing liquid entrance, the outlet of generation liquid and circulation fluid outlet, and circulation fluid outlet is connected through pipeline with liquid phase spray equipment.Sour gas of the present invention produces NaHS method, is absorbing liquid treatment sour gas production NaHS with NaOH solution.Sour gas production NaHS process of the invention and device have small scale, energy consumption low and are not easily blocked feature, are capable of achieving the double goal of sour gas purification and resource.
Description
Technical field
The present invention relates to a kind of sour gas production NaHS process and device, it is adaptable to which sour gas gas purification is led
Domain, is particularly suited for the purification containing sour gas such as sulfohydrates 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.
Sulfuric acid is widely used in all trades and professions as one of basic industrial chemicals.Made with the hydrogen sulfide contained in sour gas
It is raw material, many processing steps can be saved, that is, save investment, cost is reduced again, can also effectively recycles sulphur
Resource.Because small-sized sour gas tolerance is smaller, the industrial sulphuric acid of low concentration can only be produced, it is impossible to which productive value is higher
Oleum, economic benefit is not high, simultaneously as the transport of sulfuric acid, storage acquire a certain degree of difficulty, therefore, it is steady near oil plant
The fixed market demand is the key factor for limiting its development.
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 is absorbed 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.
Sour gas can also be used to hydrogen manufacturing etc., separately have document to disclose a kind of method generated electricity by sour gas, with sulfur-bearing
Change the method that the gas stream of hydrogen generates electricity, and when being combined with sulfuric acid apparatus, methods described is particularly useful.But, this technique side
Method operational efficiency is not high, and generated energy is limited, and economic benefit is poor.
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 and sour gas reactor.
The content of the invention
In view of the shortcomings of the prior art, the present invention provides a kind of sour gas production NaHS process and device, with
Prior art is compared, and apparatus of the present invention are simple, and equipment scale is small, and energy consumption is low, and operating cost is few, and has preferable economic benefit,
Realize the double goal of sour gas purification and pollutant resources, it is adaptable to the treatment of sour gas.
The present invention provides a kind of sour gas production NaHS device, and described device includes reacting pipe, reacting pipe one
It is sour gas entrance to hold, and the other end is exported for sour gas；Reacting pipe is divided into fourth-order reaction area by setting dividing plate, according to gas
Flow direction is followed successively by first order reaction area, second order reaction area, third-order reaction area and fourth-order reaction area；It is respectively provided with per order reaction area
Liquid phase spray equipment, the lower section per order reaction area is correspondingly arranged fluid reservoir, and every grade of fluid reservoir top is respectively provided with fluid-tight component, often
Level fluid reservoir is respectively provided with absorbing liquid entrance, the outlet of generation liquid and circulation fluid outlet, and circulation fluid outlet sprays dress through pipeline and liquid phase
Put connection.
In sour gas production NaHS device of the present invention, fluid reservoir is correspondingly arranged below every order reaction area, according to gas
Body flow direction is followed successively by one-level fluid reservoir, two grades of fluid reservoirs, three-level fluid reservoir and level Four fluid reservoirs.
In sour gas production NaHS device of the present invention, the generation liquid of the level Four fluid reservoir is exported through pipeline and three-level
The absorbing liquid entrance connection of fluid reservoir, the generation liquid outlet of three-level fluid reservoir connects through pipeline and two grades of absorbing liquid entrances of fluid reservoir
Connect, the generation liquid outlet of two grades of fluid reservoirs is connected through pipeline with the absorbing liquid entrance of one-level fluid reservoir, and level Four fluid reservoir life
Absorbing liquid entrance into liquid outlet port higher than three-level fluid reservoir, the generation liquid outlet port of three-level fluid reservoir is higher than two grades of liquid storages
The absorbing liquid entrance of tank, the two grades of absorbing liquid entrances of generation liquid outlet port higher than one-level fluid reservoir of fluid reservoir.
In sour gas production NaHS device of the present invention, the absorbing liquid entry position of every grade of fluid reservoir is above generating liquid
Outlet port.
In sour gas production NaHS device of the present invention, two grades of the absorbing liquid entrances of fluid reservoir, suctions of three-level fluid reservoir
Liquid entrance is received to be connected with NaOH solution suction line.
In sour gas production NaHS device of the present invention, two grades of fluid reservoir circulation fluid outlets also absorb with level Four fluid reservoir
Liquid entrance is connected, and second order reaction is generated liquid as absorbing liquid feeding fourth-order reaction area.
In sour gas production NaHS device of the present invention, sour gas outlet line is provided with hydrogen sulfide content detection dress
Put, by discharging hydrogen sulfide content in gas, adjust NaOH solution addition.
In sour gas production NaHS device of the present invention, the generation liquid outlet of one-level fluid reservoir is stored up through the pipeline that discharges with product
Tank is connected, and level control device is provided with the discharging pipeline.
In sour gas production NaHS device of the present invention, the liquid phase spray equipment includes feed tube and nozzle, nozzle
Spray direction perpendicular to gas access direction, inversely contacted with gas flow direction, nozzle is preferably provided at reacting pipe axle
To center, absorbing reaction spray liquid-gas ratio is 3 ~ 20L/m in every section of reaction zone3, preferably 5 ~ 10 L/m3。
In sour gas production NaHS device of the present invention, the dividing plate is fixed on the inwall of reacting pipe bottom, every
Plate is highly 1/4 ~ 3/4, preferably the 1/3 ~ 1/2 of reacting pipe diameter.
In sour gas of the present invention production NaHS device, the fluid-tight component include one-level fluid-tight disk, one-level downflow weir,
Two grades of fluid-tight disks and two grades of downflow weirs；Wherein one-level fluid-tight disk is fixed on liquid storage top tank structure one end, and one-level downflow weir is arranged on one
Level fluid-tight disk bottom is simultaneously fixed on the fluid reservoir other end relative with one-level fluid-tight disk；Two grades of fluid-tight disks connect with one-level downflow weir
Connect, two grades of fluid-tight disk bottoms set two grades of downflow weirs, and two grades of downflow weirs are fixed on liquid storage top tank structure one end, the two-stage fluid-tight disk
Between have certain space.
In sour gas production NaHS device of the present invention, the tank body outside of the fluid reservoir sets chuck, divides on chuck
Heat transferring medium entrance and heat transferring medium outlet are not provided with, and the heat transferring medium can be water, lithium bromide, dry ice, ethanol etc..
In sour gas production NaHS device of the present invention, the fluid reservoir sets heat-pipe elements, and heat-pipe elements pass through storage
Flow container, in chuck, remainder heat-pipe elements are in fluid reservoir for heat-pipe elements part.
In sour gas production NaHS device of the present invention, the heat-pipe elements are along the axially arranged some rows of fluid reservoir, tool
Body can be 2 ~ 8 rows, and preferably 4 ~ 6 rows, heat-pipe elements are uniformly arranged along fluid reservoir circumferencial direction, often arrange settable 10~30
Heat-pipe elements, preferably 12 ~ 16.
In sour gas production NaHS device of the present invention, the circulation fluid outlet is located under liquid storage pot bottom or chuck
On the liquid storage tank wall in portion, it is preferably placed on the liquid storage tank wall of chuck bottom.
In sour gas production NaHS device of the present invention, the absorbing liquid entrance is located at the liquid storage tank wall on chuck top
On, it is preferably provided on the liquid storage tank wall between two grades of fluid-tight disks and two grades of downflow weirs.
In sour gas production NaHS device of the present invention, the generation liquid outlet of the one-level fluid reservoir is arranged on fluid reservoir
Bottom or bottom, are preferably provided on the liquid storage tank wall of chuck bottom.
The present invention provides a kind of sour gas production NaHS process, and sulphur is produced using the above-mentioned sour gas of the present invention
Sodium hydride device, with NaOH solution as absorbing liquid, treatment sour gas production NaHS.
Sour gas of the present invention produces NaHS process, and sour gas is hydrogen sulfide containing waste gas, can be various next
Source containing H2S sour gas.Alkali lye mass concentration is 20%~60%, preferably 32%~38%.
Sour gas of the present invention produces NaHS process, and reaction temperature is 70~100 DEG C, preferably 80~95 DEG C.
Sour gas of the present invention produces NaHS process, and absorbing liquid is with the liquid-gas ratio of sour gas in every order reaction area
3~20L/m3, preferably 5~10 L/m3。
Sour gas of the present invention produces NaHS process, and the reaction for entering correspondence reaction zone through circulation fluid outlet is generated
Liquid is 1/6~1/2, preferably 1/4~1/3 with the reaction solution volume ratio discharged through generating liquid outlet.
Sour gas of the present invention produces NaHS process, and temperature is 85 DEG C~120 DEG C, preferably 90 DEG C in fluid reservoir
~95 DEG C.
Compared with prior art, sour gas production NaHS process of the present invention and device have the following advantages that：
1st, sour gas production NaHS process and device of the invention, anti-using level Four gas-liquid two-phase counter-current absorption
Process is answered, there is provided the self-loopa of reaction solution reabsorbs operation, reaction depth is improve, material is fully connect with sour gas
Touch, it is ensured that NaHS liquid-phase products meet national product quality standard, Na in product NaHS2The content of S is less than 4%；By reactant
Material circulation, makes alkali lye fully be contacted with sour gas so that H in purified gas2S contents are less than 30 mg/Nm3, it is ensured that Acidic Gas Treating
Weary gas afterwards realizes the target of qualified discharge.
2nd, sour gas production NaHS process and device of the present invention, by being rich in of obtaining second order reaction
Na2CO3The reaction solution of solution, loops back level four reaction apparatus and is used as absorbing liquid, realizes absorbing H2S replaces CO2Mesh
, reduce the CO absorbed in sour gas2, Na in reduction system2CO3、NaHCO3Growing amount, prevent crystallization separate out, it is ensured that device
Long-term operation.
3rd, sour gas of the present invention production NaHS process and device, NaOH alkali lye is added by being classified, respectively to
Second reactor, third-stage reactor filling NaOH alkali lye, adjust response intensities at different levels, and peak clipping treatment, homogenizing are carried out to reaction heat
Reaction heat, it is ensured that temperature of reactor at different levels in the reasonable scope, prevent heat spot, cause it is local-crystalized, cause reaction eventually
Only.
4th, sour gas production NaHS device of the present invention is pipeline reactor, and equipment is simple, and equipment scale is small.Absorb
Flow container entrance sets fluid-tight structure, prevents sour gas short circuit, realizes that purified gas are up to standard.Set using reacting pipe and fluid reservoir subregion
Put, realize absorbing liquid automatic overflow between level, reduce conveying pump and pipeline, prevent radiating and cooling from causing pump and line clogging,
Ensure that reaction is quick, steadily carry out, equipment is simple, and reactor scale is greatly reduced.
5th, the method for the present invention is more suitable for small-sized sour gas handling process.Set in fluid reservoir and take hot measure, no
Different with reaction zone internal cause response intensity, exothermic heat of reaction is different, and stage-by-stage heat exchange is realized using heat-pipe elements, realizes that high temperature section is reacted
Heat is progressive step by step to low-temperature zone reaction heat, it is ensured that reaction heat unification homogenizing, it is ensured that temperature is uniform in liquid phase storage tank, reaction heat and
When take out, prevent product liquid cross thermal evaporation, crystallization separate out.
Brief description of the drawings
Fig. 1 is sour gas production NaHS process and schematic device of the present invention.
Fig. 2 is fluid-tight modular construction schematic diagram of the present invention.
Specific embodiment
As shown in figure 1, sour gas production NaHS device of the present invention includes reacting pipe 1, reacting pipe one end is acid
Property gas entrance 2, the other end is sour gas outlet 3；Reacting pipe is divided into fourth-order reaction area by setting dividing plate 4, according to gas stream
Dynamic direction is followed successively by first order reaction area 5, second order reaction area 6, third-order reaction area 7 and fourth-order reaction area 8；It is all provided with per order reaction area
Liquid phase spray equipment 9 is put, liquid phase spray equipment includes feed tube and nozzle, and the lower section per order reaction area is correspondingly arranged liquid storage
Tank, one-level fluid reservoir 10, two grades of fluid reservoirs 11, three-level fluid reservoir 12 and level Four fluid reservoirs are followed successively by according to gas flow direction
13；Every grade of fluid reservoir top is respectively provided with fluid-tight component 14, the fluid-tight component include one-level fluid-tight disk 31, one-level downflow weir 32,
Two grades of fluid-tight disks 33 and two grades of downflow weirs 34；Wherein one-level fluid-tight disk is fixed on liquid storage top tank structure one end, and one-level downflow weir is set
In one-level fluid-tight disk bottom and it is fixed on the fluid reservoir other end relative with one-level fluid-tight disk；Two grades of fluid-tight disks and one-level downflow weir
Connection, two grades of fluid-tight disk bottoms set two grades of downflow weirs, and two grades of downflow weirs are fixed on liquid storage top tank structure one end.The level Four liquid storage
The generation liquid outlet of tank 13 is connected through pipeline with the absorbing liquid entrance of three-level fluid reservoir 12, the generation liquid outlet of three-level fluid reservoir 12
It is connected with the absorbing liquid entrance of two grades of fluid reservoirs 11 through pipeline, two grades of generation liquid outlets of fluid reservoir 11 are through pipeline and one-level liquid storage
The absorbing liquid entrance of tank 10 is connected, and the generation liquid outlet port of level Four fluid reservoir 13 enters higher than the absorbing liquid of three-level fluid reservoir 12
Mouthful, the generation liquid outlet port of three-level fluid reservoir 12 is higher than two grades of absorbing liquid entrances of fluid reservoir 11, two grades of lifes of fluid reservoir 11
Absorbing liquid entrance into liquid outlet port higher than one-level fluid reservoir 10, two grades of fluid reservoir circulation fluid outlets are also inhaled with level Four fluid reservoir
The connection of liquid entrance is received, second order reaction is generated liquid as absorbing liquid feeding fourth-order reaction area.The absorbing liquid entrance of three-level fluid reservoir 12
It is connected with NaOH solution suction line 22 with two grades of absorbing liquid entrances of fluid reservoir 11, sour gas outlet line is provided with hydrogen sulfide
Content detection device 23, by discharging hydrogen sulfide content in gas, adjusts NaOH solution addition, and the generation liquid of one-level fluid reservoir 10 goes out
Mouth is connected through the pipeline 24 that discharges with product storage tank, and level control device 25 is provided with the discharging pipeline 24.Every grade of fluid reservoir
Absorbing liquid entrance 15, generation liquid outlet 16 and circulation fluid outlet 17 are respectively provided with, circulation fluid outlet is through pipeline and liquid phase spray equipment 9
Connection, the tank body outside of the fluid reservoir sets chuck 18, heat transferring medium entrance 19 is respectively equipped with chuck and heat transferring medium goes out
Mouth 20, also sets up heat-pipe elements 21 on the liquid storage tank, heat-pipe elements pass through fluid reservoir, and heat-pipe elements part is in chuck
It is interior, remainder heat-pipe elements in fluid reservoir, the heat-pipe elements along the axially arranged some rows of fluid reservoir, be specifically as follows 2 ~
8 rows, preferably 4 ~ 6 rows, heat-pipe elements are uniformly arranged along fluid reservoir circumferencial direction, often arrange and 10~30 heat-pipe elements can be set,
Preferably 12 ~ 16.
Reaction effect of the invention is illustrated with reference to embodiment, but is not therefore limited the scope of the invention.
Embodiment 1
Using process unit as shown in Figure 1, with alkali lye that sour gas and mass concentration are 35% as raw material, two-stage is carried out
Acid-base reaction.
During using inventive pipeline formula reactor for treatment sour gas, sour gas enters first order reaction in reacting pipe through entrance
Area, with the reaction solution from one-level fluid reservoir（The reaction solution that two grades of liquid storage area overflows come）It is absorbing liquid, through nozzle
The liquid film on axis direction is formed in reacting pipe, when sour gas passes through liquid film, neutralization reaction occurs, in the work of gravitational field
Under, liquid film is ejected on reacting pipe tube wall, and one-level fluid reservoir is entered after fluid-tight component along wall.By setting dividing plate,
After preventing liquid film to be ejected into tube wall, liquid crossfire enters in adjacent reaction area.In H2In the case of S excess, Na2S liquid phases and H2S
Reaction, generates NaHS.NaHS in one-level fluid reservoir is partly recycled to first order reaction section and is circulated through pump portion carrying device
Flowing, realizes that absorbing liquid depth absorbs.The reacted sour gas in first order reaction area enters second order reaction area, wherein H2S and CO2It is dense
Degree is substantially reduced, but still is not reaching to emission request.With NaOH solution and from two grades of reaction solutions of liquid storage area（Three-level is stored up
The reaction solution that liquid zone overflow comes）It is absorbing liquid, forms the liquid film of axis direction in pipeline through nozzle, when sour gas is passed through
During liquid film, there is neutralization reaction, in the presence of gravitational field, liquid film is ejected on reacting pipe tube wall, along wall through downspout
Into two grades of fluid reservoirs.In H2In the case that S is slightly excessive, Na2S and NaOH mixed liquors and H2S reacts, and generates Na2S and NaHS is mixed
Close liquid.Reaction solution is circulated flowing through pump circulation to second order reaction area, realizes that absorbing liquid depth absorbs.Second order reaction
The reacted sour gas in area enters third-order reaction area, wherein H2S concentration is greatly reduced, but still be not carried out qualified discharge will
Ask.With NaOH solution and liquid from three-level liquid storage area（The reaction solution that the overflow of level Four liquid storage area comes）It is absorbing liquid, it is raw
Produce Na2S solution, reaction solution is circulated flowing through pump circulation to third-order reaction section, realizes that absorbing liquid depth absorbs.Three
The reacted sour gas in order reaction area enters fourth-order reaction area, wherein H2S concentration is extremely low, basically reaches emission request.Level Four is anti-
Should with second order reaction obtain rich in 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, realizes absorbing H2S replaces CO2Purpose, reduce absorb sour gas in CO2, reduce liquid phase and produce
Na in product2CO3、NaHCO3Growing amount, prevent crystallization separate out, it is ensured that device long-term operation.Realize purified gas row up to standard
Put.Reaction solution is circulated flowing through pump circulation to fourth-order reaction section, realizes that absorbing liquid depth absorbs.
In the present embodiment, CO in sour gas2Volume fraction is 7%, H2S volume fractions are 92%, and hydro carbons volume fraction is 1%.
NaOH solution mass concentration is 35%.Sour gas is slightly excessive in first stage reactor, H in the second stage reactor2S is slightly excessive, and the 3rd
NaOH solution is slightly excessive in order reaction.In Acidic Gas Treating method of the present invention, cyclic absorption process is set up per order reaction, one-level is anti-
Answer area, second order reaction area, circulation ratio is 2 during three-level answers area, fourth-order reaction area:3.Per order reaction, liquid-gas ratio is 5L/ in section
m3.Concrete operations condition is shown in Table 1, and reaction result is shown in Table 1.
The reaction condition of 1 embodiment of table 1 and reaction result
Claims (31)
1. a kind of sour gas produces NaHS device, it is characterised in that：Described device includes reacting pipe, reacting pipe one end
It is sour gas entrance, the other end is exported for sour gas；Reacting pipe is divided into fourth-order reaction area by setting dividing plate, according to gas stream
Dynamic direction is followed successively by first order reaction area, second order reaction area, third-order reaction area and fourth-order reaction area；Liquid is respectively provided with per order reaction area
Phase spray equipment, fluid reservoir is correspondingly arranged per the lower section in order reaction area, according to gas flow direction be followed successively by one-level fluid reservoir,
Two grades of fluid reservoirs, three-level fluid reservoir and level Four fluid reservoirs；Every grade of fluid reservoir top is respectively provided with fluid-tight component, and every grade of fluid reservoir is all provided with
Absorbing liquid entrance, the outlet of generation liquid and circulation fluid outlet are put, circulation fluid outlet is connected through pipeline with liquid phase spray equipment, described two
The level absorbing liquid entrance of fluid reservoir and the absorbing liquid entrance of three-level fluid reservoir are connected with NaOH solution suction line, one-level liquid storage
Tank generation liquid outlet is connected through the pipeline that discharges with product storage tank, and the generation liquid outlet of the level Four fluid reservoir is stored up through pipeline and three-level
The absorbing liquid entrance connection of flow container, the generation liquid outlet of three-level fluid reservoir connects through pipeline and two grades of absorbing liquid entrances of fluid reservoir
Connect, the generation liquid outlet of two grades of fluid reservoirs is connected through pipeline with the absorbing liquid entrance of one-level fluid reservoir, and level Four fluid reservoir life
Absorbing liquid entrance into liquid outlet port higher than three-level fluid reservoir, the generation liquid outlet port of three-level fluid reservoir is higher than two grades of liquid storages
The absorbing liquid entrance of tank, the two grades of absorbing liquid entrances of generation liquid outlet port higher than one-level fluid reservoir of fluid reservoir, described two grades
The outlet of fluid reservoir circulation fluid is also connected with level Four fluid reservoir absorbing liquid entrance.
2. according to the device described in claim 1, it is characterised in that：The absorbing liquid entry position of every grade of fluid reservoir is above generation
Liquid is exported.
3. according to the device described in claim 1, it is characterised in that：The sour gas outlet line is provided with hydrogen sulfide content inspection
Survey device.
4. according to the device described in claim 1, it is characterised in that：One-level fluid reservoir generation liquid outlet connects with product storage tank
Level control device is provided with the discharging pipeline for connecing.
5. according to the device described in claim 1, it is characterised in that：The liquid phase spray equipment includes feed tube and nozzle, spray
The spray direction of mouth inversely contacts perpendicular to gas access direction with gas flow direction.
6. according to the device described in claim 5, it is characterised in that：The nozzle is arranged on reacting pipe axial centre.
7. according to the device described in claim 1, it is characterised in that：The dividing plate is fixed on the inwall of reacting pipe bottom,
Divider height is the 1/4 ~ 3/4 of reacting pipe diameter.
8. according to the device described in claim 7, it is characterised in that：The dividing plate is fixed on the inwall of reacting pipe bottom,
Divider height is the 1/3 ~ 1/2 of reacting pipe diameter.
9. according to the device described in claim 1, it is characterised in that：The fluid-tight component includes one-level fluid-tight disk, one-level overflow
Weir, two grades of fluid-tight disks and two grades of downflow weirs；Wherein one-level fluid-tight disk is fixed on liquid storage top tank structure one end, and one-level downflow weir is arranged on
One-level fluid-tight disk bottom is simultaneously fixed on the fluid reservoir other end relative with one-level fluid-tight disk；Two grades of fluid-tight disks connect with one-level downflow weir
Connect, two grades of fluid-tight disk bottoms set two grades of downflow weirs, and two grades of downflow weirs are fixed on liquid storage top tank structure one end.
10. according to the device described in claim 1, it is characterised in that：The tank body outside of the fluid reservoir sets chuck, on chuck
Heat transferring medium entrance and heat transferring medium outlet are respectively equipped with, the heat transferring medium is water, lithium bromide, dry ice or ethanol.
11. according to the device described in claim 10, it is characterised in that：The fluid reservoir sets heat-pipe elements, and heat-pipe elements are worn
Fluid reservoir is crossed, in chuck, remainder heat-pipe elements are in fluid reservoir for heat-pipe elements part.
12. according to the device described in claim 11, it is characterised in that：The heat-pipe elements are axially arranged some along fluid reservoir
Row, heat-pipe elements are uniformly arranged along fluid reservoir circumferencial direction, and often row sets 10~30 heat-pipe elements.
13. according to the device described in claim 11, it is characterised in that：The heat-pipe elements along axially arranged 2 ~ 8 row of fluid reservoir,
Heat-pipe elements are uniformly arranged along fluid reservoir circumferencial direction, and often row sets 12~16 heat-pipe elements.
14. according to the device described in claim 13, it is characterised in that：The heat-pipe elements are along axially arranged 4 ~ 6 row of fluid reservoir.
15. according to the device described in claim 10, it is characterised in that：The circulation fluid outlet is located at liquid storage pot bottom or folder
Cover on the liquid storage tank wall of bottom.
16. according to the device described in claim 15, it is characterised in that：Fluid reservoir of the circulation fluid outlet positioned at chuck bottom
On outer wall.
17. according to the device described in claim 10, it is characterised in that：The absorbing liquid entrance is located at the fluid reservoir on chuck top
On outer wall.
18. according to the device described in claim 17, it is characterised in that：The absorbing liquid entrance is arranged on two grades of fluid-tight disks and two
On liquid storage tank wall between level downflow weir.
19. according to the device described in claim 1, it is characterised in that：The generation liquid outlet of the one-level fluid reservoir is arranged on storage
Flow container bottom or bottom.
20. according to the device described in claim 10, it is characterised in that：The generation liquid outlet of the one-level fluid reservoir is arranged on folder
Cover on the liquid storage tank wall of bottom.
A kind of 21. sour gas production NaHS processes, with NaOH solution as absorbing liquid, treatment sour gas production sulphur hydrogenation
Sodium, it is characterised in that：NaHS device is produced using the sour gas described in any claim in claim 1~20.
22. according to the process described in claim 21, it is characterised in that：Sour gas is hydrogen sulfide containing waste gas, and NaOH is molten
Liquid mass concentration is 20%~60%.
23. according to the process described in claim 22, it is characterised in that：Sour gas is various sources containing H2S sour gas,
NaOH solution mass concentration is 32%~38%.
24. according to the process described in claim 21, it is characterised in that：The reaction temperature is 70~100 DEG C.
25. according to the process described in claim 24, it is characterised in that：The reaction temperature is 80~95 DEG C.
26. according to the process described in claim 21, it is characterised in that：Absorbing liquid and sour gas in every order reaction area
Liquid-gas ratio be 3~20L/m3。
27. according to the process described in claim 26, it is characterised in that：Absorbing liquid and sour gas in every order reaction area
Liquid-gas ratio be 5~10 L/m3。
28. according to the process described in claim 21, it is characterised in that：Enter the anti-of correspondence reaction zone through circulation fluid outlet
It is 1/6~1/2 that liquid should be generated with the reaction solution volume ratio discharged through generating liquid outlet.
29. according to the process described in claim 28, it is characterised in that：Enter the anti-of correspondence reaction zone through circulation fluid outlet
It is 1/4~1/3 that liquid should be generated with the reaction solution volume ratio discharged through generating liquid outlet.
30. according to the process described in claim 21, it is characterised in that：In every grade of fluid reservoir temperature be 85 DEG C~
120℃。
31. according to the process described in claim 30, it is characterised in that：Temperature is 90 DEG C~95 in every grade of fluid reservoir
℃。
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| CN101092576A (en) * | 2006-06-23 | 2007-12-26 | 中国石油化工股份有限公司 | Method for removing acid gases in cracked gas |
| CN101664634A (en) * | 2009-09-18 | 2010-03-10 | 天津渤海化工有限责任公司天津碱厂 | Flue gas desulfurization process by ammonia method |
| CN102765700A (en) * | 2012-08-13 | 2012-11-07 | 成都德美工程技术有限公司 | Technique method for producing sodium bisulfide |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101092576A (en) * | 2006-06-23 | 2007-12-26 | 中国石油化工股份有限公司 | Method for removing acid gases in cracked gas |
| CN101664634A (en) * | 2009-09-18 | 2010-03-10 | 天津渤海化工有限责任公司天津碱厂 | Flue gas desulfurization process by ammonia method |
| CN102765700A (en) * | 2012-08-13 | 2012-11-07 | 成都德美工程技术有限公司 | Technique method for producing sodium bisulfide |
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