CN206375869U - Wet desulphurization device - Google Patents
Wet desulphurization device Download PDFInfo
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- CN206375869U CN206375869U CN201621365547.2U CN201621365547U CN206375869U CN 206375869 U CN206375869 U CN 206375869U CN 201621365547 U CN201621365547 U CN 201621365547U CN 206375869 U CN206375869 U CN 206375869U
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Abstract
The utility model provides a kind of wet desulphurization device, including：The gas-liquid separator of interconnection, absorption plant, regenerating unit and retracting device, separator air inlet and separator gas outlet are provided with the gas-liquid separator, the air inlet connection of separator gas outlet and absorption plant, the liquid outlet of absorption plant and the first inlet of regenerating unit are connected, first liquid outlet of regenerating unit is connected by the inlet of sulphur stock pump and retracting device, the liquid outlet of retracting device is connected by the second inlet of booster pump and regenerating unit, second liquid outlet of regenerating unit and the inlet of absorption plant are connected, and separator air inlet is used to input pending gas, the sulphur of retracting device is exported for exporting sulphur.Secondary pollution will not be produced after the technical scheme, desulfurization pretreatment, desulfurization process cost is low, desulfuration efficiency is high.
Description
Technical field
The utility model is related to gas purification technique field, more particularly to a kind of wet desulphurization device.
Background technology
A kind of special gas reservoir of carbonate gas reservoirs, with in-place permeability is relatively low, initial production is high, the rate of decay
Hurry up, life cycle is short, sulfide hydrogen the features such as.Due to this particularity of carbonate gas reservoirs so that gas well is producing shorter
Natural gas cannot be directly entered collection transmission pipe network, it is necessary to by that could enter after compressor boost after time, and be transported to specified
Equipment is handled.Simultaneously because the universal hydrogen sulfide gas containing higher concentration in the individual well natural gas of carbonate rock gas field, such as
Do not handle, the hydrogen sulfide in such natural gas will corroded pipeline and equipment, therefore, natural gas enter compressor before, need
Suitable desulfurizer is selected to carry out desulfurization pretreatment to the natural gas collected very crucial.
At present, carbonate gas reservoirs individual well selexol process uses dry desulfurization device, and it is de- that dry desulfurization device is used
Sulfur absorbent is main based on sponge iron, absorbs the hydrogen sulfide gas in natural gas using the sponge iron in desulfuration adsorbent, enters
And reach the purpose for removing hydrogen sulfide gas in natural gas gas.But the Sulfur capacity rate of desulfuration adsorbent, than relatively low, this to do
The secondary pollution object amount that method sulfur method is produced after desulfurization pretreatment is big, and desulfurization process cost is high, and desulfuration efficiency is low.
Utility model content
The utility model provides a kind of wet desulphurization device, to solve existing carbonate gas reservoirs single well dry desulfurization
The problem of device desulfurization process cost is high, desulfuration efficiency is low.
A kind of wet desulphurization device that the utility model is provided, including：The gas-liquid separator of interconnection, absorption plant,
Regenerating unit and retracting device；
Separator air inlet and separator gas outlet, the separator gas outlet and institute are provided with the gas-liquid separator
The air inlet connection of absorption plant is stated, the liquid outlet of the absorption plant is connected with the first inlet of the regenerating unit, institute
The first liquid outlet for stating regenerating unit is connected by sulphur stock pump with the inlet of the retracting device, and the retracting device goes out
Liquid mouthful is connected by booster pump with the second inlet of the regenerating unit, and the second liquid outlet of the regenerating unit is inhaled with described
The inlet connection of receiving apparatus；
The separator air inlet is used to input pending gas, and the retracting device also includes sulphur and exported, the sulphur
Sulphur is exported for exporting sulphur.
In an embodiment of the present utility model, the retracting device, including：Filter and filtrate knockout drum；
First liquid outlet of the regenerating unit is connected by sulphur stock pump with the inlet of the filter, the filtering
The liquid outlet of machine is connected with the inlet of the filtrate knockout drum, the liquid outlet of the filtrate knockout drum by the booster pump with
The second inlet connection of the regenerating unit.
In another embodiment of the present utility model, the regenerating unit includes oxidizing tower；The wet desulphurization device, also
Including：Air blower；
The air blower is connected with the first air inlet of the oxidizing tower, and the air blower exists for providing absorbent solution
The power of regeneration in the oxidizing tower.
In above-described embodiment of the present utility model, the wet desulphurization device, in addition to：Air compressor and buffering
Tank；
The air compressor is connected by the surge tank with the second air inlet of the oxidizing tower.
In above-described embodiment of the present utility model, temperature controller, the temperature control are provided with the regenerating unit
Device processed is used for the temperature for controlling solution in the regenerating unit.
In above-described embodiment of the present utility model, the oxidizing tower is normal pressure conical vessel.
In any of the above-described embodiment of the present utility model, the absorption plant includes multiple；
The separator gas outlet be connected with the air inlet of each absorption plant, and the separator gas outlet with often
Switching valve is provided between the air inlet of the individual absorption plant.
In above-described embodiment of the present utility model, the liquid outlet of each absorption plant respectively with the regenerating unit
The first inlet connection.
In any of the above-described embodiment of the present utility model, vane type mist eliminator is provided with the gas-liquid separator.
The wet desulphurization device that the utility model embodiment is provided, including the gas-liquid separator of interconnection, absorption plant,
Regenerating unit and retracting device, input pending gas, by the way that separator is gone out by the separator air inlet of gas-liquid separator
The air inlet connection of gas port and absorption plant, the liquid outlet of absorption plant and the first inlet of regenerating unit are connected, regeneration dress
The first liquid outlet put is connected by the inlet of sulphur stock pump and retracting device, the liquid outlet of retracting device by booster pump with
The second inlet connection of regenerating unit, the second liquid outlet of regenerating unit and the inlet of absorption plant are connected, and are reclaimed
The sulphur outlet output sulphur of device.The technical scheme, energy consumption is low, simple to operate, effectively reduce high sulfur-containing natural gas recovery
Processing cost, desulfuration efficiency is high, and the exploitation for the outlying sour well in oil field provides technological reserve.
Brief description of the drawings
, below will be to embodiment in order to illustrate more clearly of the utility model embodiment or technical scheme of the prior art
Or the accompanying drawing used required in description of the prior art is briefly described, it should be apparent that, drawings in the following description are
Some embodiments of the present utility model, for those of ordinary skill in the art, are not paying the premise of creative labor
Under, other accompanying drawings can also be obtained according to these accompanying drawings.
The structural representation for the wet desulphurization device embodiment one that Fig. 1 provides for the utility model；
The structural representation for the wet desulphurization device embodiment two that Fig. 2 provides for the utility model.
Embodiment
It is new below in conjunction with this practicality to make the purpose, technical scheme and advantage of the utility model embodiment clearer
Accompanying drawing in type embodiment, the technical scheme in the utility model embodiment is clearly and completely described, it is clear that retouched
The embodiment stated is a part of embodiment of the utility model, rather than whole embodiments.Based on the implementation in the utility model
Example, the every other embodiment that those of ordinary skill in the art are obtained under the premise of creative work is not made is belonged to
The scope of the utility model protection.
The reason for existing dry desulfurization device desulfurization process cost is high, desulfuration efficiency is low mainly has at following 2 points：
First, there is environmental pollution and safety problem.Dry desulfurization adsorbent is main based on sponge iron, absorbs hydrogen sulfide
Sponge iron discarded object afterwards can not be reused, and directly discharge can be caused in secondary pollution, and sponge iron discarded object to environment
Ferrous sulfide is may also contain, because ferrous sulfide under certain condition can be with spontaneous combustion, the sponge iron containing ferrous sulfide is discarded
Thing exposure easily produces nature in atmosphere, serious there may be fire, if dealt with improperly, it is possible to create security incident,
There is certain threat to the personal safety and safety of property of people.
Second, secondary pollution object amount is bigger.Because the Sulfur capacity rate of sponge iron is generally 15~18%, that is, absorbing 1 ton
Hydrogen sulfide needs the secondary pollutions such as the sponge iron discarded object of 6~7 tons of generation, and desulfuration efficiency is low, therefore processing 1 ton of hydrogen sulfide takes
With about in 8~90,000 yuan (including desulfurization expense, freight, labour cost and secondary pollution processing cost etc.), running cost
With very high.
Therefore, existing dry desulfurization device is primarily adapted for use in hydrogen sulfide stripping of the latent sulfur content in below 20kg/d, if treated
When the concentration of hydrogen sulfide contained in the natural gas of processing reaches 200,000 ppm, the secondary pollution object amount of generation is very huge, with place
The increase of reason amount, desulfurization process cost increases severely.
In view of the above-mentioned problems, the utility model provides a kind of wet desulphurization device, for solving existing carbonate rock gas
Single well is hidden with the problem of dry desulfurization device desulfurization process cost is high, desulfuration efficiency is low.Below, by specific embodiment to this
The technical scheme of application is described in detail.
It should be noted that these specific embodiments can be combined with each other below, for same or analogous concept
Or process may be repeated no more in certain embodiments.
The structural representation for the wet desulphurization device embodiment one that Fig. 1 provides for the utility model.As shown in figure 1, this reality
The wet desulphurization device of example offer is provided, including：Gas-liquid separator 1, absorption plant 2, regenerating unit 3 and the recovery dress of interconnection
Put 4.
Wherein, separator air inlet 101 and separator gas outlet 102 are provided with gas-liquid separator 1, the separator outlet
Mouth 102 is connected with the air inlet 201 of absorption plant 2, the liquid outlet 204 of the absorption plant 2 and the first inlet of regenerating unit 3
301 connections, the first liquid outlet 302 of the regenerating unit 3 is connected by sulphur stock pump 6 with the inlet 401 of retracting device 4, should
The liquid outlet 402 of retracting device 4 is connected by booster pump 7 with the second inlet 303 of regenerating unit 3, and the of the regenerating unit 3
Two liquid outlets 304 are connected with the inlet 203 of absorption plant 2.
The separator air inlet 101 is used to input pending gas, and the retracting device 4 also includes sulphur outlet 403, the sulphur
Sulphur outlet 403 is used to export sulphur.
Specifically, shown in reference picture 1, the first end of gas-liquid separator 1 is provided with separator air inlet 101 and separator goes out
Gas port 102, the second end of gas-liquid separator 1 is provided with separator liquid outlet 103；The first end of absorption plant 2 is provided with air inlet
Mouth 201, gas outlet 202, inlet 203, the second end of absorption plant 2 is provided with liquid outlet 204；The first end of regenerating unit 3
The first inlet 301 and the second inlet 303 are provided with, the second end of regenerating unit 3 is provided with the first liquid outlet 302, second
Liquid outlet 304；Inlet 401 and liquid outlet 402 and sulphur outlet 403 are provided with retracting device 4.
Shown in reference picture 1, the pending gas collected out of individual well (contains H2S natural gas) pass through gas-liquid separator 1
Separator air inlet 101 enter gas-liquid separator 1, by gas-liquid separator 1 separation after natural gas gas pass through absorb dress
The air inlet 201 for putting 2 enters in absorption plant 2, when natural gas gas passes through absorption plant 2, the hydrogen sulfide in natural gas gas
(H2S) absorbed by the absorbent solution in absorption plant 2 and be transformed into sulfur slurry, purified gas by with absorption plant 2
The conveyance conduit that gas outlet 202 is connected is delivered to extraneous Natural gas pipeline system.Absorbent solution in absorption plant 2 has been reacted
It is transported in regenerating unit 3 and is regenerated after.Specifically, absorbent solution by the liquid outlet 204 of absorption plant 2, again
First inlet 301 of generating apparatus 3, which is sent in regenerating unit 3, to be regenerated.
Absorbent solution in absorption plant 2 enters after regenerating unit 3, and the sulfur slurry in absorbent solution is gradually deposited
In the bottom of regenerating unit 3, after the sulfur slurry concentration of the bottom of regenerating unit 3 reaches preset concentration, sulphur stock pump 6 is opened by sulphur
Filtered in sulphur slurry feeding retracting device 4, the sulphur entered in retracting device 4 is recovered device 4 and filtered out, and passes through
Sulphur outlet 403 is exported, and then carries out envelope processing.
Optionally, as shown in figure 1, inlet 301 and regeneration of the liquid outlet 204 of absorption plant 2 with regenerating unit 3
Rich solution pump 5 is also associated between the liquid outlet 304 of device 3 and the inlet 203 of absorption plant 2.Pressure in absorption plant 2
When sufficiently large, the absorbent solution in absorption plant 2 can be directly fed in regenerating unit 3, but in absorption plant 2
When insufficient pressure by the absorbent solution in absorption plant 2 to be pressed into regenerating unit 3, by the rich solution pump 5 by absorption plant 2
Absorbent solution get in regenerating unit 3.
Filtrate in retracting device 4 is sent back in regenerating unit 3 by booster pump 7, filtrate quilt in regenerating unit 3
Oxidation processes, rich solution pump 5 is recycled after the ability that the solution in regenerating unit 3 absorbs hydrogen sulfide gas meets certain condition,
It is delivered in absorption plant 2, and then is realized new by the inlet 203 of the second liquid outlet 304 of regenerating unit 3, absorption plant 2
The absorption of one wheel hydrogen sulfide gas.
What deserves to be explained is, the absorbent solution in absorption plant 2 is chelated iron catalyst solution, is absorbing stink damp
The chemical agent that will not be produced after body in secondary pollution, chelated iron catalyst solution can be degradable, and reaction speed is fast, sulphur
Rong great；In addition, the chemical agent in chelated iron catalyst solution is renewable, and regeneration condition is simple, at normal temperatures and pressures
Reaction condition is met, energy consumption is low；Simple to operate, desulphurization cost is low, and desulfurization process expense is low.
The wet desulphurization device that the utility model embodiment is provided, including the gas-liquid separator of interconnection, absorption plant,
Regenerating unit and retracting device, input pending gas, by the way that separator is gone out by the separator air inlet of gas-liquid separator
The air inlet connection of gas port and absorption plant, the liquid outlet of absorption plant is connected by the first inlet of rich solution pump and regenerating unit
Connect, the first liquid outlet of regenerating unit is connected by the inlet of sulphur stock pump and retracting device, and the liquid outlet of retracting device leads to
The second inlet for crossing booster pump and regenerating unit is connected, and the second liquid outlet of regenerating unit passes through rich solution pump and absorption plant
Inlet is connected, and the sulphur outlet of retracting device exports sulphur.The technical scheme, energy consumption is low, simple to operate, effective reduction
High sulfur-containing natural gas recycling cost, desulfuration efficiency is high, and exploitation for the outlying sour well in oil field provides technological reserve.
Further, on the basis of above-described embodiment, the wet desulphurization device embodiment that Fig. 2 provides for the utility model
Two structural representation.As shown in Fig. 2 in the utility model embodiment, above-mentioned retracting device 4, including：Filter 41 and filter
Liquid knockout drum 42.
In the present embodiment, the first liquid outlet 302 of regenerating unit 3 passes through sulphur stock pump 6 and the inlet of filter 41
411 connections, the liquid outlet 412 of filter 41 is connected with the inlet 421 of filtrate knockout drum 42, the liquid outlet of filtrate knockout drum 42
422 are connected by booster pump 7 with the second inlet 303 of regenerating unit 3.
Specifically, in absorbent solution regenerative process, after the sulfur slurry of the bottom of regenerating unit 3 reaches preset concentration,
Sulphur slurries are delivered to filter 41 and filtered by startup sulphur stock pump 6.Because sulphur slurries have certain pressure in itself, therefore
In filter 41, multiple stainless steel filtering nets that drusen is set in filter 41 under the effect of the pressure are retained, and
Filter cake is formed on filter screen, filtrate flows to from the liquid outlet 412 of filter 41 through the filtrate conduit in filter 41 through filter screen and filtered
The filtrate clarified in the inlet 421 of liquid knockout drum 42, filtrate knockout drum 42.
Optionally, as shown in Fig. 2 the top of filter 41 is additionally provided with air inlet 413 and pressure gauge 414, filtering is passed through
The air inlet 413 of machine 41, air is transported to the filter cake formed in filter 41 on drying filter screen.
Specifically, when filter 41 is filtered, noting the registration of pressure gauge 414, being maintained at the pressure in filter 41
Certain numerical value, if the phase before filtration, as sulphur slurries increase in filter 41, during pressure increase in filter 41,
The valve of the air inlet 413 of big filter 41 now should be suitably opened, appropriate pressure release makes pressure be maintained at certain numerical value, to be filtered
Illustrate that the sulphur resistance on filter screen is sufficiently large when pressure substantially rises after a period of time, filtering is completed, close filter 41
Imported valve at inlet 411, stops inputting sulphur slurries into filter 41, and utilize the air inlet 413 of filter 41
Air is passed through into filter 41, and then dries up filter cake.
After sulphur cake is dried up, stop being passed through air into filter 41, open the butterfly valve of the bottom of filter 41, started
Vibrator in filter 41, the filter cake on filter screen is shaken, the sulphur through the bottom of filter 41 exports 403 rows using vibrator
Go out, and handle and collect the sulphur that something lost falls in filter 41.
The filtrate that the filtrate produced after being filtered in filter 41 enters in filtrate knockout drum 42, filtrate knockout drum 42 is through supercharging
The circulation conveying of pump 7 is to regenerating unit 3.
In addition, the air inlet 413 of filter 41 is also connected with the inlet 421 of filtrate knockout drum 42, when in filter 41
The height of solution reaches the height of the air inlet 413 of filter 41, shows that filter has filled sulphur slurries and started filtering.
Further, as shown in Fig. 2 above-mentioned regenerating unit 3 includes oxidizing tower 31；The wet desulphurization device, in addition to：Drum
Blower fan 32.
The air blower 32 is connected with the first air inlet 311 of oxidizing tower 31, and the air blower 32 is used to provide absorbent solution
The power of regeneration in oxidizing tower 31.
Optionally, the absorbent solution in absorption plant 2 is chelated iron catalyst solution, in the chelated iron catalyst solution
Effective chemical agent for ferrum-based catalyst match solution, therefore, be passed through when in absorption plant 2 containing the natural of hydrogen sulfide gas
After gas, hydrogen sulfide gas is converted into S simple substance, while the Fe3+ in absorbent solution is reduced into Fe2+, therefore, is transported to regeneration
Contain substantial amounts of Fe2+ in sulphur slurries in device 3.So, in order to allow ferrum-based catalyst (Fe3+) to regenerate, by air blower 32
It is connected with the first air inlet 311 of oxidizing tower 31, opens the air intake valve of air blower 32, air enters by the first of oxidizing tower 31
Gas distributor in gas port 311, oxidizing tower 31 is evenly distributed on the cross-sectional area of oxidizing tower 31.The bubble that air is produced
During rising in oxidizing tower 31, ferrum-based catalyst proportioning solution is run into, Fe2+ is by the oxygen in air in the process
Fe3+ is oxidized to, so as to complete the regeneration of ferrum-based catalyst.
Optionally, the first end of oxidizing tower 31 is also associated with exhausting pipeline 312, oxidizing tower 31 discarding air, by this
The row of exhausting pipeline 312 is to air.
Further, since the gas flow that air blower 32 is conveyed is fixed, it is impossible to be arbitrarily adjusted.Therefore, in order to control
Throughput in system input oxidizing tower 31, air blower 32 is connected with oxidizing tower 31 by a three-way pipe and connected with external environment
It is logical, a bleeder valve is installed on the three-way pipeline connected with external environment.According to the demand of oxygen in oxidizing tower 31, it will let out
Portion gas unnecessary in valve one size of opening, the gas flow that air blower 32 is conveyed is put to be emitted into greatly by silencer 37
Gas.The silencer 37 can reduce the sound that air blower 32 discharges air, so as to effectively reduction noise pollution.That is, air
Entered using air blower 32 in oxidizing tower 31, being passed into the air total amount in oxidizing tower 31 can be in the filtrate of regenerating oxidation tower 31
Fe2+, makes its whole be oxidized to ferrum-based catalyst solution.
Further, on the basis of above-described embodiment, as shown in Fig. 2 the wet desulphurization device, in addition to：Air pressure
Contracting machine 33 and surge tank 34.
Air compressor 33 is connected by surge tank 34 with the second air inlet 313 of oxidizing tower 31.
Specifically, the sulphur in the inner absorbent solution of oxidizing tower 31 can be deposited in the bottom of oxidizing tower 31 under gravity
Portion, in order to prevent sulfur slurry from sticking in the bottom tower wall of oxidizing tower 31, the present embodiment is constantly carried using air compressor 33
Purged for factory's wind, sulfur slurry is suspended at the charging aperture of sulphur stock pump 6.
In addition, being additionally provided with surge tank 34 between air compressor 33 and oxidizing tower 31.The surge tank 34 can store sky
The gas that air compressor 33 is sent, allows gas to the enough uninterrupted bottom for being transported to oxidizing tower 31.If do not buffer
Tank 34 carries out gas storage, and the gas that air compressor 33 is sent is probably the gas of interruption when being transported to 31 bottom of oxidizing tower, i.e., not
Continuous gas, therefore, connection surge tank 34 can delay between air compressor 33 and the second air inlet 313 of oxidizing tower 31
Air is rushed, continuing uninterruptedly for gas has been effectively ensured.
Optionally, as shown in Fig. 2 being provided with temperature controller 35 in regenerating unit 3, the temperature controller 35 is used to control
The temperature of solution in regenerating unit 3.
Specifically, because the reaction temperature of solution in oxidizing tower 31 is in preset temperature range (such as, between 25-53 DEG C)
When, therefore the best results of chemical reaction, temperature detector 36 are provided with the side wall of oxidizing tower 31, the temperature detector 36
The temperature of solution in oxidizing tower 31 can be detected, and then makes temperature controller 35 according to the testing result control of the temperature detector 36
The temperature of solution in preparation, regeneration device 3, keeps it in preset temperature range, and then improve reaction efficiency.
Optionally, temperature controller 35 is arranged on the pipeline between absorption plant 2 and oxidizing tower 31.In an embodiment
In, the temperature controller 35 is electric heater, when the temperature of solution in oxidizing tower 31 is less than the lower bound temperature of preset temperature range
When, solution is heated using the electric heater, so as to improve chemical reaction efficiency.In another embodiment, if oxidation
When solution autoreactivity temperature is higher than the upper temperature limit of preset temperature range in tower 31, the temperature of solution is reduced using the cooler
Degree, so as to keep the temperature of solution in oxidizing tower 31 to be located in preset temperature range.In fact, for the desulfurization process on individual well
In device, oxidizing tower 31 solution autoreactivity temperature be higher than preset temperature range upper temperature limit when possibility it is little.
Optionally, as shown in Fig. 2 oxidizing tower 31 is normal pressure conical vessel.
Specifically, because the regeneration of the absorbent solution in the present embodiment just can be realized at normal temperatures, it is simple and convenient, and
Oxidizing tower 31 in the characteristics of being easier to collect sediment based on conical vessel, the present embodiment selects normal pressure conical vessel, normal pressure
The oxidizing tower 31 of conical vessel, it is easier to make the sulphur slurries in oxidizing tower 31 be deposited on the tapering of oxidizing tower 31, and then suspend
At the mouth of sulphur stock pump 6, it is easy to the collection of sulphur slurries.
Optionally, because absorbent solution (chelated iron catalyst solution) can degrade and empty on a small quantity in transmission oxidizing process
Gas emptying can take part vapor out of, in order to ensure the desulfurized effect of the wet desulphurization device, can manually be added according to actual conditions
Plus corresponding chemical agent and supplement desalted water are in filtrate knockout drum 42, and then make the things such as the chemical agent and desalted water of addition
Matter is conveyed into oxidizing tower 31 through booster pump 7.
Absorbent solution completes to be delivered to absorption plant 2 through rich solution pump 5 after regenerating in oxidizing tower 31, and then will contain again
H2S natural gas transportation carries out desulfurization process next time to absorption plant 2.
Optionally, then as shown in Fig. 2 in the present embodiment, absorption plant 2 includes multiple.
The separator gas outlet 102 of gas-liquid separator 1 is connected with the air inlet 201 of each absorption plant 2, and separator goes out
Switching valve 110 is provided between the air inlet 201 of gas port 102 and each absorption plant 2.
When the number of absorption plant 2 is multiple, then contain H from what the separator gas outlet 102 of gas-liquid separator 1 came out2S
Natural gas enter in one of absorption plant 2, it is specific to utilize separator gas outlet 102 and the air inlet of absorption plant 2
Switching valve 110 between mouthfuls 201 is controlled.
For example, in one embodiment, if absorption plant 2 is two, respectively absorption plant 2A and absorption plant 2B
Two, the switching valve 110 between control separator gas outlet 102 and absorption plant 2A air inlet 201 is opened, and controls separator
Switching valve 110 between gas outlet 102 and absorption plant 2B air inlet 201 is closed, by what is exported from separator gas outlet 102
Containing H2The natural gas of S gases is passed through in absorption plant 2A, after the reaction completely of the absorbent solution in device 2A to be absorbed, will be separated
Switching valve 110 between device gas outlet 102 and absorption plant 2A is closed, and by separator gas outlet 102 and absorption plant 2B
Between switching valve 110 open, containing H2The natural gas of S gases, which is passed into absorption plant 2B, to be proceeded to absorb.
What deserves to be explained is, the H in absorption plant 2A is referred to after the absorbent solution reaction completely in absorption plant 2A2S
S simple substance is fully converted to, while the Fe3+ that the Fe3+ in absorbent solution is reduced into Fe2+, and absorbent solution disappears completely
Consume.Therefore, it is required to be oxidation-reduction potential experiment (Oxidation- in the course of reaction in absorption plant 2A
Reduction Potential, abbreviation ORP), when proving that the Fe3+ in absorbent solution runs out of, then H will be contained2S gases
Natural gas is passed into absorption plant 2B, and reaction principle, the course of reaction in absorption plant 2B are the same with absorption plant 2A, this
Place is repeated no more.
In the present embodiment, after absorption plant 2A intake valve is closed, control absorption plant 2A gas outlet 202 is opened
Relief valve, the pressure in absorption plant 2A and pure natural gas transportation to extraneous transmission pipeline are released, then will
Reacted rich solution is using in the feeding regenerating unit 3 of rich solution pump 5 in absorption plant 2A.I.e. when the absorbent in absorption plant 2A is molten
H can not be reabsorbed after liquid reaction completely2During S, the rich solution in absorption plant 2A is driven into regenerating unit 3 by rich solution pump 5
Carry out reproduction operation, it is to be regenerated after the completion of liquid is returned in absorption plant 2A by rich solution pump 5 again, complete absorption plant 2A
One absorption and regeneration process of interior solution.Similarly, in absorption plant 2B the absorption and regeneration process of solution as absorption plant 2A,
Here is omitted.
What deserves to be explained is, the number of the absorption plant in the present embodiment includes but is not limited to 2, and it can be according to reality
Need to be configured, the present embodiment is not limited.
Optionally, the first end of each absorption plant 2 is provided with pressure release gas outlet 205, and the pressure release gas outlet 205 passes through
Conveyance conduit after the solution in by absorption plant 2 is delivered to oxidation unit 3, is opened the pressure release and gone out with going ambient systems to be connected
Gas port 205, is released the pressure in absorption plant 2 by the pressure release gas outlet 205.
Shown in reference picture 2, the liquid outlet 204 of each absorption plant 2 is distinguished in the wet desulphurization device that the present embodiment is provided
It is connected with the first inlet 301 of regenerating unit 3.Specifically, the liquid outlet 204 of each absorption plant 2 passes through rich solution pump 5 respectively
It is connected with the first inlet 301 of regenerating unit 3.
Because the liquid outlet 204 of each absorption plant 2 is connected with the first inlet 301 of regenerating unit 3, therefore, when
After the completion of reaction in each absorption plant 2, the solution in the absorption plant 2 can be driven into again by it by rich solution pump 5
Generating apparatus 3 carries out regeneration treatment, and regenerative process is referring to the record in above-described embodiment, and here is omitted.
Optionally, in the present embodiment, it is provided with vane type mist eliminator 11 in gas-liquid separator 1.
Specifically, vane type mist eliminator 11 is installed at the top of the first end of above-mentioned gas-liquid separator 1, the vane type mist eliminator
11 can collect condensate liquid or solution, and condensate liquid accumulates in the bottom of gas-liquid separator 1.Second side wall of gas-liquid separator 1
On be provided with liquid level instrument 12, the gate out switch valve 13 of the liquid level instrument 12 and the bottom of gas-liquid separator 1 constitutes Liquid level and returned
Road, the liquid level instrument 12 is used to detect the liquid level in gas-liquid separator 1, when the liquid level of gas-liquid separator 1 is raised to certain altitude,
Liquid-level switch valve 13 in its bottom line will be opened, and the condensate in gas-liquid separator 1 is set from the bottom of gas-liquid separator 1
Separator liquid outlet 103 in discharge, enter and carry out subsequent treatment after ambient systems again, when gas-liquid separator 1 liquid level drop
During to certain altitude, the liquid-level switch valve 13 in its bottom line will be closed.
Optionally, exhausting pipeline is additionally provided with the separator air inlet 101 of gas-liquid separator 1, is set on the exhausting pipeline
It is equipped with a switch valve.In general, the switch valve on exhausting pipeline is closed.Only in the present embodiment
Wet desulphurization device break down when, by exhausting pipeline switch valve open, by the pending gas containing hydrogen sulfide gas
Body is transported in other processing units and handled, and can so be prevented effectively from pending gas and be discharged into air, effectively keep away
Environmental pollution that pending gas causes and the waste of natural gas resource are exempted from.
The wet desulphurization device that the utility model embodiment is provided is mainly used on individual well, and absorption plant absorbs natural gas
Middle H2Static absorption process is used during S, chemical agent uses high iron solution, and Sulfur capacity is big, and disposal ability is strong, and regenerating unit is
H will be absorbed2Solution gets to oxidizing tower by rich solution pump after S, and the Fe2+ in solution is oxidized into Fe3 by air blower continuous blast
+, then reach the recycling of chemical agent solution.Retracting device is that the sulfur slurry solution that oxidizing tower is bored into bottom passes through sulfur slurry
Pump is delivered to filter, is come out by filter sulfur filtration, completes sulphur recovery work, and the filtrate that will be obtained after filtering
Regenerating unit is returned, complete the regeneration of absorbent solution.
What deserves to be explained is, compared with existing dry desulfurization device, the suction that the wet desulphurization device in the present embodiment is used
Receive agent solution (chelated iron catalyst solution) and do not produce secondary pollution, chemical agent can be degradable, reaction speed is fast, Sulfur capacity
Greatly；Chemical agent is renewable, and regeneration condition is simple, reaction condition can be met at normal temperatures and pressures, energy consumption is low.In addition, this
The wet desulphurization device of embodiment handles the expense of 1 ton of hydrogen sulfide (including reagent consumption expense, people about below 3.5 ten thousand yuan
The expenses such as expenses of labour use, operating cost) (existing dry desulfurization device handles the expense of 1 ton of hydrogen sulfide about at 8~90,000 yuan), behaviour
Make simple, desulfurization process cost is low.
Further, the present embodiment causes the hydrogen sulfide in natural gas after processing by studying the wet desulphurization device of individual well
Concentration is controlled within 20ppm, high sulfur-containing natural gas cost recovery is reduced, while the exploitation for the outlying sour well in oil field is provided
Technological reserve.
Finally it should be noted that：Various embodiments above is only limited to illustrate the technical solution of the utility model, rather than to it
System；Although the utility model is described in detail with reference to foregoing embodiments, one of ordinary skill in the art should
Understand：It can still modify to the technical scheme described in foregoing embodiments, or to which part or whole
Technical characteristic carries out equivalent substitution；And these modifications or replacement, the essence of appropriate technical solution is departed from this practicality newly
The scope of each embodiment technical scheme of type.
Claims (9)
1. a kind of wet desulphurization device, it is characterised in that including：Gas-liquid separator, absorption plant, the regenerating unit of interconnection
And retracting device；
Separator air inlet and separator gas outlet are provided with the gas-liquid separator, the separator gas outlet is inhaled with described
The air inlet connection of receiving apparatus, the liquid outlet of the absorption plant is connected with the first inlet of the regenerating unit, it is described again
First liquid outlet of generating apparatus is connected by sulphur stock pump with the inlet of the retracting device, the liquid outlet of the retracting device
It is connected by booster pump with the second inlet of the regenerating unit, the second liquid outlet of the regenerating unit is filled with described absorb
The inlet connection put；
The separator air inlet is used to input pending gas, and the retracting device also includes sulphur and exported, and the sulphur goes out
Mouth is used to export sulphur.
2. device according to claim 1, it is characterised in that the retracting device, including：Filter and filtrate separation
Tank；
First liquid outlet of the regenerating unit is connected by sulphur stock pump with the inlet of the filter, the filter
Liquid outlet is connected with the inlet of the filtrate knockout drum, the liquid outlet of the filtrate knockout drum by the booster pump with it is described
The second inlet connection of regenerating unit.
3. device according to claim 1, it is characterised in that the regenerating unit includes oxidizing tower；The wet desulphurization
Device, in addition to：Air blower；
The air blower is connected with the first air inlet of the oxidizing tower, and the air blower is used to provide absorbent solution described
The power of regeneration in oxidizing tower.
4. device according to claim 3, it is characterised in that the wet desulphurization device, in addition to：Air compressor and
Surge tank；
The air compressor is connected by the surge tank with the second air inlet of the oxidizing tower.
5. device according to claim 3, it is characterised in that temperature controller is provided with the regenerating unit, described
Temperature controller is used for the temperature for controlling solution in the regenerating unit.
6. device according to claim 5, it is characterised in that the oxidizing tower is normal pressure conical vessel.
7. the device according to any one of claim 1~6, it is characterised in that the absorption plant includes multiple；
The separator gas outlet is connected with the air inlet of each absorption plant, and the separator gas outlet and each institute
Switching valve is provided between the air inlet for stating absorption plant.
8. device according to claim 7, it is characterised in that the liquid outlet of each absorption plant respectively with the regeneration
The first inlet connection of device.
9. the device according to any one of claim 1~6, it is characterised in that be provided with blade in the gas-liquid separator
Formula mist eliminator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621365547.2U CN206375869U (en) | 2016-12-13 | 2016-12-13 | Wet desulphurization device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201621365547.2U CN206375869U (en) | 2016-12-13 | 2016-12-13 | Wet desulphurization device |
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| CN206375869U true CN206375869U (en) | 2017-08-04 |
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| CN201621365547.2U Active CN206375869U (en) | 2016-12-13 | 2016-12-13 | Wet desulphurization device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108130147A (en) * | 2017-12-27 | 2018-06-08 | 山东明硕新能源科技有限公司 | A kind of biogas desulfurization purifier |
| CN112642274A (en) * | 2020-12-22 | 2021-04-13 | 山东滨农科技有限公司 | Interlocking control system of device for absorbing hydrogen sulfide by complexing iron |
-
2016
- 2016-12-13 CN CN201621365547.2U patent/CN206375869U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108130147A (en) * | 2017-12-27 | 2018-06-08 | 山东明硕新能源科技有限公司 | A kind of biogas desulfurization purifier |
| CN112642274A (en) * | 2020-12-22 | 2021-04-13 | 山东滨农科技有限公司 | Interlocking control system of device for absorbing hydrogen sulfide by complexing iron |
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