CN208115448U - A kind of pre- upgrading system of sour gas - Google Patents
A kind of pre- upgrading system of sour gas Download PDFInfo
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- CN208115448U CN208115448U CN201721418310.0U CN201721418310U CN208115448U CN 208115448 U CN208115448 U CN 208115448U CN 201721418310 U CN201721418310 U CN 201721418310U CN 208115448 U CN208115448 U CN 208115448U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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Abstract
The utility model relates to a kind of pre- upgrading systems of sour gas, including concentrate unit and hot recycling unit；Concentrate unit, the sulfur-rich absorbent to receive upstream carry out concentrate operation, including flash column and stripping tower, hot recycling unit, and the regeneration of absorbent, including hot recycling tower are carried out to receive the sulfur-rich absorbent after pre- concentrate cell processing；The entrance of the flash column connects sulfur-rich absorbent conveyance conduit to be processed, the entrance of the liquid-phase outlet connection stripping tower of the flash column by heat exchanger, and the liquid-phase outlet of the stripping tower connects the hot recycling unit；It is provided with concentrate unit before hot recycling unit and heat-exchanger rig is set before concentrate unit, sulfur-rich absorbent is after heating, successively pass through the flash column and stripping tower of concentrate unit again, the carbon dioxide in sulfur-rich absorbent can be made further to desorb, to significantly improve H therein2The concentration of S, and then desorbed by hot recycling unit containing high H2Crouse's gas of S concentration.
Description
Technical field
The utility model relates to chemical plant installations more particularly to a kind of pre- upgrading systems of sour gas.
Background technique
Purified synthesis gas is mainly used for removing the H in crude synthesis gas2S、COS、CO2, so that production meets the net of technique requirement
Change gas.Common purified synthesis gas technique is generally divided into thermal method and cold process according to the difference for absorbing temperature in industry.In thermal method with
Selexol technique and MDEA technique are the most famous, and cold process is then using low-temp methanol washing process as representative.Low-temp methanol washing process is 50
A kind of purified synthesis gas technique developed jointly at the beginning of age by German Linde Co and Lucci corporation.The technique is to absorb with methanol
Solvent, using methanol at low temperature to the great good characteristic of sour gas solubility, using in Physical Absorption removing unstripped gas
Sour gas.
The above method is also lacked to H in outlet sour gas at present2The Effective Regulation means of S concentration.In production operation, no
Same sulfur recovery technology is to H in sour gas2The concentration of S has different requirements.As H in sour gas2When S concentration is lower, sulfur recovery dress
Setting will be unable to operates normally for a long time.It is to increase by the way of by partially acidic gas recycled back up-stream system in the prior art
H in sour gas2S concentration, however the purified synthesis gas device built for part are limited to its flow setting, entrance synthesis
The factors such as gas sulfur content fluctuation improve H in sour gas by increasing sour gas internal circulating load2Additional increased investment needed for S concentration,
Energy consumption is higher, and economy is bad.
Utility model content
For the current state of the art, the technical problem to be solved by the utility model is to provide one kind, low energy consumption, and
H in system outlet sour gas can be significantly improved2The concentration of S, convenient for adjusting H2The sour gas concentration unit of S concentration.
The utility model solves technical solution used by above-mentioned technical problem：A kind of pre- upgrading system of sour gas,
Including concentrate unit and hot recycling unit；
Concentrate unit, the sulfur-rich absorbent to receive upstream carries out concentrate operation, including flash column and stripping tower, described
The entrance of flash column connects sulfur-rich absorbent conveyance conduit to be processed by heat exchanger, and first gas phase that is equipped with of the flash column goes out
Mouthful, first gaseous phase outlet connects the first outlet pipe, and the first outlet pipe, which is equipped with to be used to adjust in the flash column, to be dodged
The control valve of steam pressure power；The entrance of the liquid-phase outlet connection stripping tower of the flash column；
The lower part of the stripping tower connects gas stripping gas conveyance conduit, and the top of the stripping tower is equipped with the second gaseous phase outlet,
The liquid-phase outlet of the stripping tower connects the hot recycling unit；
Hot recycling unit carries out the regeneration of absorbent, including heat to receive the sulfur-rich absorbent after concentrate cell processing
Regenerator, the hot recycling tower include the I section being arranged above and below and II sections of two parts, and the lower part of I sections of the hot recycling tower is connected with output
The first outlet tube of lean absorbent road, the lower part of II sections of the hot recycling tower is connected with for providing the reboiler of hot recycling heat, described
The bottom of hot recycling tower is connected with the second outlet tube road of conveying aqueous solutions of absorbent.
It is provided with concentrate unit before hot recycling unit and heat exchanger is set before concentrate unit, it is sulfur-rich in this way
Absorbent carries out flash distillation using flash column and stripping tower carries out air lift, can make CO after heat exchanger heats up2Equal gas
Body is further desorbed from solution, to significantly improve H therein2The concentration of S, and then desorbed by hot recycling unit
Contain high H2Crouse's gas of S concentration；Wherein first outlet pipe is equipped with control valve, can be used to adjust flash column
Interior flashing pressure carries out different degrees of flash distillation concentrate, so that sulfur-rich absorbent generates various concentration after hot recycling
Crouse's gas meet the requirement of downstream sulfur recovery workshop section.
As an improvement, above-mentioned heat exchanger may include the First Heat Exchanger being serially connected and the second heat exchanger, described first
Outlet tube road is sequentially connected second heat exchanger and First Heat Exchanger.Before entering concentrate unit, sulfur-rich absorbent difference
It is effectively exchanged heat by First Heat Exchanger and the second heat exchanger with the lean absorbent from hot recycling tower, realize energy has
Effect utilizes, and reduces production cost.
Further, the sulfur-rich absorbent conveyance conduit is sequentially connected the First Heat Exchanger and second heat exchanger
Tube side, first outlet tube road is sequentially connected the shell side of second heat exchanger and First Heat Exchanger；Certainly, described sulfur-rich
Absorbent conveyance conduit connects the shell side of the First Heat Exchanger and the second heat exchanger, and the first outlet tube road is sequentially connected described
The tube side or sulfur-rich absorbent conveyance conduit of two heat exchangers and First Heat Exchanger and the first outlet tube road difference interconnection the
The tube side and shell side of one heat exchanger and the second heat exchanger can also reach same heat exchange purpose.
It is further improved, the first bypass, the both ends of first bypass can also be equipped on first outlet tube road
Mouth is located at the upstream and downstream of the heat exchanger, and first bypass is equipped with the first valve；The sulfur-rich absorbent conveying
Pipeline is equipped with the second bypass, and the two-port of second bypass is located at the First Heat Exchanger or second heat exchanger
Upstream and downstream, and it is described second bypass be equipped with the second valve.The first bypass is equipped on the first outlet tube road respectively,
Sulfur-rich absorbent conveyance conduit is equipped with the second bypass, and is respectively equipped with the first valve and the in the first bypass and the second bypass
Two valves can efficiently control the temperature for entering the sulfur-rich absorbent of flash column, carry out different degrees of flash distillation concentrate, in turn
So that its Crouse's gas for generating various concentration after hot recycling meets the requirement of downstream sulfur recovery workshop section.
Preferably, the two-port of first bypass can be located at the First Heat Exchanger or second heat exchange
The upstream and downstream of device.
As an improvement, before carrying out concentrate operation, sulfur-rich absorbent with from hot recycling tower lean absorbent or other
Hot-fluid stock can achieve medium temperature control range after being exchanged heat, reach it to further increase the flash temperature of sulfur-rich absorbent
To high-temperature control range, and then improve the H of sulfur-rich absorbent2S concentration, can be between heat exchanger and the entrance of the flash column
It is connected with superheater.
As an improvement, the flash column and the stripping tower can share same tower body, the first end socket is used between the two
It is isolated, and the flash column is located at the top of the stripping tower, the liquid-phase outlet of the flash column and the entrance of stripping tower
It is connected by exterior line, the liquid-phase outlet of the stripping tower connects the entrance of the hot recycling tower by first circulation pump.It dodges
It steams tower and stripping tower uses same housing structure, be isolated between the two using the first end socket, liquid passes through self gravity
It flows into stripping tower below, eliminates the conveying cost of fluid, save energy；Meanwhile two equipment being stacked together,
Occupied area is small, and flashing operation and stripping operation on the other hand can be enabled to carry out step by step；Certainly, as the behaviour in flash column
Make pressure it is sufficiently high when, first circulation pump can also be saved, liquid phase can be fed directly to hot recycling tower entrance.
Another kind improves, and the flash column and the stripping tower are shared same tower body, be isolated between the two using tower tray,
The flash column is located at the top of the stripping tower；The tower tray, which is equipped with, enters the flash column for gas phase in the stripping tower
Riser, which constitutes second gaseous phase outlet on the stripping tower top, is additionally provided on the tower tray for the sudden strain of a muscle
Steam the downspout that the liquid phase in tower enters the stripping tower；The liquid-phase outlet of the stripping tower passes through described in first circulation pump connection
The entrance of hot recycling tower.Flash column and stripping tower use same housing structure, between the two using equipped with riser and downspout
Tower tray be isolated, both eliminated the conveying cost of fluid, saved energy, and make flashing operation and stripping operation in flash column
It can carry out simultaneously.
It is further improved, the flash column, the stripping tower and the hot recycling tower share same tower body, the flash column
It is isolated between the stripping tower by the first end socket, passes through the second end socket phase between the stripping tower and the hot recycling tower
Isolation, and stripping tower described in the flash column and the hot recycling tower are sequentially arranged from top to bottom；
It is connected between the liquid-phase outlet of the flash column and the entrance of stripping tower by exterior line, the liquid of the stripping tower
Mutually connected between outlet and the entrance of the hot recycling tower by outer fluid line.
Another kind improves, and the flash column, the stripping tower and the hot recycling tower share same tower body；The flash column
The stripping tower and the hot recycling tower are sequentially arranged from top to bottom；Pass through tower tray phase between the flash column and the stripping tower
Isolation, the tower tray are equipped with the riser for entering the flash column for gas phase in the stripping tower, which constitutes institute
Second gaseous phase outlet on stripping tower top is stated, is additionally provided on the tower tray and enters the stripping tower for the liquid phase in the flash column
Downspout；It is isolated between the stripping tower and the hot recycling tower by the second end socket, the liquid-phase outlet of the stripping tower
It is connect between the entrance of the hot recycling tower by outer fluid line.
Flash column, stripping tower and hot recycling tower share the structure of same tower body, can save stripping tower and hot recycling tower it
Between the fluid pressure conveyer device of first circulation pump reached energy conservation in the conveying cost for reducing fluid to a certain degree
The purpose of consumption reduction, meanwhile, three equipment are stacked together, occupied area is dramatically saved.
Compared with prior art, the advantages of the utility model：Concentrate unit is set before hot recycling unit and is being mentioned
Heat-exchanger rig is set before dense unit, sulfur-rich absorbent is after heating, then successively passes through the flash column and stripping tower of concentrate unit,
The carbon dioxide in sulfur-rich absorbent can be made further to desorb, to significantly improve H therein2The concentration of S, in turn
It is desorbed by hot recycling unit containing high H2Crouse's gas of S concentration；On the other hand, sulfur-rich before entering concentrate unit
Absorbent passes through First Heat Exchanger and the second heat exchanger respectively and is effectively exchanged heat with the lean absorbent from hot recycling tower, realizes
The effective use of energy reduces production cost；The first bypass is equipped on the first outlet tube road respectively, it is defeated in sulfur-rich absorbent
It send pipeline to be equipped with the second bypass, and is respectively equipped with the first valve and the second valve can be effective in the first bypass and the second bypass
Ground control enters the temperature of the sulfur-rich absorbent of flash column, while by the way that control valve is arranged on first outlet pipe, adjusting
The flashing pressure in flash column is saved, ensure that sulfur-rich absorbent carries out different degrees of concentrate under suitable temperature and pressure,
So that its Crouse's gas for generating various concentration after hot recycling meets the requirement of downstream sulfur recovery workshop section；Finally, institute
The structure that flash column, stripping tower and the hot recycling tower share same tower body is stated, circulation pump can be saved, to a certain degree
The conveying cost for reducing fluid, has achieved the purpose that energy-saving.
Detailed description of the invention
Fig. 1 is the schematic diagram of the utility model embodiment 1；
Fig. 2 is the schematic diagram of the utility model embodiment 2；
Fig. 3 is the schematic diagram of the utility model embodiment 3；
Fig. 4 is the schematic diagram of the utility model embodiment 4
Fig. 5 is the schematic diagram of the utility model embodiment 5
Fig. 6 is the schematic diagram of the utility model embodiment 6
Fig. 7 is the schematic diagram of the utility model embodiment 7
Fig. 8 is the schematic diagram of the utility model embodiment 8.
Specific embodiment
The utility model is described in further detail below in conjunction with figure embodiment.
Embodiment 1,
As shown in Figure 1, the pre- upgrading system of sour gas includes concentrate unit and hot recycling unit；
Concentrate unit, the sulfur-rich absorbent to receive upstream carry out concentrate operation, including flash column 2 and stripping tower 3, dodge
It steams tower 2 and stripping tower 3 shares same tower body, be isolated between the two using the first end socket 21, and flash column 2 is located at stripping tower
3 top, the liquid-phase outlet of flash column 2 connect the entrance of stripping tower 3 by outer fluid line；
Hot recycling unit carries out the regenerative operation of absorbent, packet to receive the sulfur-rich absorbent after concentrate cell processing
Hot recycling tower 1 is included, hot recycling tower 1 includes the I section being arranged above and below and II sections of two parts, is separated between two sections by rising gas cap, should
The lower part of the I section of hot recycling tower 1 is connected with the first outlet tube road of output lean absorbent, and the lower part of the II section of the hot recycling tower 1 is set
Have for providing the reboiler 8 of hot recycling heat, the bottom of the II section of hot recycling tower 1 is connected with the of conveying aqueous solutions of absorbent
Two outlet tube roads, the top of hot recycling tower 1 are connected with Crouse's gas gas pipeline, the Crouse's gas desorbed send after cooling to
Downstream sulfur recovery workshop section, condensate liquid are back to hot recycling tower.
The entrance of flash column 2 connects sulfur-rich absorbent conveyance conduit to be handled, is sequentially connected in series setting on the conveyance conduit
There are First Heat Exchanger 5 and the second heat exchanger 4, specifically, sulfur-rich absorbent conveyance conduit is sequentially connected First Heat Exchanger 5 and second
The tube side of heat exchanger 4, the first outlet tube road of hot recycling tower are sequentially connected the shell side of the second heat exchanger 4 and First Heat Exchanger 5, and
And first outlet tube road be equipped with the first bypass, the two-port of the first bypass is located at the upstream and downstream of First Heat Exchanger 5,
First bypass is equipped with the first valve 12；The second bypass, the two-port point of the second bypass are additionally provided on sulfur-rich absorbent conveyance conduit
Not Wei Yu the second heat exchanger 4 upstream and downstream, and second bypass be equipped with the second valve 13；First valve 12 and the second valve 13 divide
Lean absorbent Yong Lai not controlled and sulfur-rich absorbent enters the flow of First Heat Exchanger 5 and the second heat exchanger 4, and then effectively
Control enters the temperature of the sulfur-rich absorbent of flash column 2, carries out different degrees of flash distillation concentrate.Certainly, sulfur-rich absorbent is walked
Shell side, lean absorbent walks tube side or two stream stocks intersect to walk tube side and shell side and the first bypass and the second bypass is all disposed within
On sulfur-rich absorbent transfer pipeline or the first outlet tube road can also reach same heat exchange purpose.
The first gaseous phase outlet is additionally provided on flash column 2, the first gaseous phase outlet connects the first outlet pipe, the first outlet pipe
It is equipped with the control valve 14 for being used to adjust flashing pressure in flash column 2；The lower part of stripping tower 3 connects gas stripping gas conveyance conduit, tool
Body, gas stripping gas is inert gas, preferably nitrogen, can control the H in sulfur-rich absorbent by the nitrogen amount for adjusting different2S
Concentration；The top of stripping tower 3 is equipped with the second gaseous phase outlet, and the second gaseous phase outlet is connected with above-mentioned first outlet pipe, two gas
Body stream stock is cooling through subcooler 7 after converging, and gas is sent to upstream H2S enriching apparatus, the condensate liquid after separation can be sent to gas
The top of stripper 3 is sprayed, and the H carried secretly in flashed vapour is absorbed2S gas；The liquid phase of stripping tower 3 is added by first circulation pump 11
Hot recycling tower is sent to after pressure, the lean absorbent of the I pars infrasegmentalis from hot recycling tower 1 after 10 pressurization of second circulation pump with sulfur-rich suction
It receives agent sufficiently to be exchanged heat, realizes the effective use of energy, saved production cost.
Embodiment 2,
As shown in Fig. 2, the pre- upgrading system of the sour gas includes concentrate unit and hot recycling unit；Concentrate unit, to
The sulfur-rich absorbent for receiving upstream carries out concentrate operation, including flash column 2 and stripping tower 3, hot recycling unit, to receive concentrate
Sulfur-rich absorbent after cell processing carries out the regeneration of absorbent, including hot recycling tower 1；
Flash column 2 and stripping tower 3 share same tower body, the two to the present embodiment in concentrate unit unlike the first embodiment
Between be isolated using tower tray 9, flash column 2 is located at the top of stripping tower 3；Tower tray 9 is equipped with riser 91 and downspout 92, gas
Gas in stripper 3 is entered directly by riser 91 in the flash column 2 of top, and correspondingly, the liquid phase in flash column 2 passes through
Downspout 92 enters in the stripping tower 3 of lower section, can be avoided additionally increase connection flash column 2 and air lift outside tower body in this way
The pipeline of tower 3, but also flash process can carry out simultaneously with air lift process.In addition to this, the other content in the present embodiment
It is same as Example 1, no longer it is described in detail.
Embodiment 3,
As shown in figure 3, the pre- upgrading system of the sour gas includes concentrate unit and hot recycling unit；Concentrate unit, to
The sulfur-rich absorbent for receiving upstream carries out concentrate operation, including flash column 2 and stripping tower 3, hot recycling unit, to receive concentrate
Sulfur-rich absorbent after cell processing carries out the regeneration of absorbent, including hot recycling tower 1；
Flash column 2, stripping tower 3 and hot recycling tower 1 share same tower body to the present embodiment unlike the first embodiment, flash distillation
It is isolated between tower 2 and stripping tower 3 by the first end socket 21, is separated by between stripping tower 3 and hot recycling tower 1 by the second end socket 31
From, and flash column 2, stripping tower 3 and hot recycling tower 1 are sequentially arranged from top to bottom；The liquid-phase outlet of flash column 2 passes through external stream
The entrance of body piping connection stripping tower 3, the liquid-phase outlet of stripping tower 3 connect the entrance of hot recycling tower 1 by outer fluid line,
Under self gravity and the effect of tower body internal pressure, sulfur-rich absorbent enters stripping tower 3 from flash column 2 and carries out air lift, then again
It enters hot recycling tower 1 and carries out hot recycling process.Thus eliminate the first circulation pump between stripping tower 3 and hot recycling tower 1
11 fluid pressure conveyer device, reduces production cost.In addition to this, the other content in the present embodiment and 1 phase of embodiment
Together, it is no longer described in detail.
Embodiment 4,
As shown in figure 4, the pre- upgrading system of the sour gas includes concentrate unit and hot recycling unit；Concentrate unit, to
The sulfur-rich absorbent for receiving upstream carries out concentrate operation, including flash column 2 and stripping tower 3, hot recycling unit, to receive concentrate
Sulfur-rich absorbent after cell processing carries out the regeneration of absorbent, including hot recycling tower 1；
Flash column 2, stripping tower 3 and hot recycling tower 1 share same tower body to the present embodiment unlike the first embodiment, flash distillation
It is isolated between tower 2 and stripping tower 3 by tower tray 9, is isolated between stripping tower 3 and hot recycling tower 1 by the second end socket 31, and
And 2 stripping tower 3 of flash column and hot recycling tower 1 are sequentially arranged from top to bottom；Tower tray 9 is equipped with riser 91 and downspout 92, gas
Gas in stripper 3 is entered directly by riser 91 in the flash column 2 of top, and correspondingly, the liquid phase in flash column 2 passes through
Downspout 92 enters in the stripping tower 3 of lower section, can be avoided increase connection flash column 2 and stripping tower 3 outside tower body in this way
Pipeline, but also flash process can carry out simultaneously with air lift process.The liquid-phase outlet of stripping tower 3 passes through outer fluid line
The entrance for connecting hot recycling tower 1, under self gravity and the effect of tower body internal pressure, sulfur-rich absorbent enters gas from flash column 2
Stripper 3 carries out hot recycling process then into hot recycling tower 1.Thus eliminate between stripping tower 3 and hot recycling tower 1
The fluid pressure conveyer device of one circulating pump 11, reduces production cost.In addition to this, the other content and reality in the present embodiment
It is identical to apply example 1, is no longer described in detail.
Embodiment 5,
As shown in figure 5, the pre- upgrading system of the sour gas includes concentrate unit and hot recycling unit；Concentrate unit, to
The sulfur-rich absorbent for receiving upstream carries out concentrate operation, including flash column 2 and stripping tower 3, hot recycling unit, to receive concentrate
Sulfur-rich absorbent after cell processing carries out the regeneration of absorbent, including hot recycling tower 1；
The present embodiment is also connected with overheat between the second heat exchanger 4 and the entrance of flash column 2 unlike the first embodiment
Device 6 can further increase the flash temperature of sulfur-rich absorbent in this way, and reach a high temperature control range, and then improve sulfur-rich absorption
The H of agent2S concentration.In addition to this, the other content in the present embodiment is same as Example 1, is no longer described in detail.
Embodiment 6,
As shown in fig. 6, the pre- upgrading system of the sour gas includes concentrate unit and hot recycling unit；Concentrate unit, to
The sulfur-rich absorbent for receiving upstream carries out concentrate operation, including flash column 2 and stripping tower 3, hot recycling unit, to receive concentrate
Sulfur-rich absorbent after cell processing carries out the regeneration of absorbent, including hot recycling tower 1；
The present embodiment is also connected with overheat between the second heat exchanger 4 and the entrance of flash column 2 as different from Example 2
Device 6 can further increase the flash temperature of sulfur-rich absorbent in this way, and reach a high temperature control range, and then improve sulfur-rich absorption
The H of agent2S concentration.In addition to this, the other content in the present embodiment is same as Example 2, is no longer described in detail.
Embodiment 7,
As shown in fig. 7, the pre- upgrading system of the sour gas includes concentrate unit and hot recycling unit；Concentrate unit, to
The sulfur-rich absorbent for receiving upstream carries out concentrate operation, including flash column 2 and stripping tower 3, hot recycling unit, to receive concentrate
Sulfur-rich absorbent after cell processing carries out the regeneration of absorbent, including hot recycling tower 1；
The present embodiment is also connected with overheat between the second heat exchanger 4 and the entrance of flash column 2 as different from Example 3
Device 6 can further increase the flash temperature of sulfur-rich absorbent in this way, and reach a high temperature control range, and then improve sulfur-rich absorption
The H of agent2S concentration.In addition to this, the other content in the present embodiment is same as Example 3, is no longer described in detail.
Embodiment 8,
As shown in figure 8, the pre- upgrading system of the sour gas includes concentrate unit and hot recycling unit；Concentrate unit, to
The sulfur-rich absorbent for receiving upstream carries out concentrate operation, including flash column 2 and stripping tower 3, hot recycling unit, to receive concentrate
Sulfur-rich absorbent after cell processing carries out the regeneration of absorbent, including hot recycling tower 1；
The present embodiment is also connected with overheat between the second heat exchanger 4 and the entrance of flash column 2 as different from Example 4
Device 6 can further increase the flash temperature of sulfur-rich absorbent in this way, and reach a high temperature control range, and then improve sulfur-rich absorption
The H of agent2S concentration.In addition to this, the other content in the present embodiment is same as Example 4, is no longer described in detail.
Claims (10)
1. a kind of pre- upgrading system of sour gas, it is characterised in that including：
Concentrate unit, the sulfur-rich absorbent to receive upstream carry out concentrate operation, including flash column (2) and stripping tower (3), institute
It states the entrance of flash column (2) and sulfur-rich absorbent conveyance conduit to be processed is connected by heat exchanger, the flash column (2) is equipped with the
One gaseous phase outlet, first gaseous phase outlet connect the first outlet pipe, and the first outlet pipe, which is equipped with, to be used to adjust the sudden strain of a muscle
Steam the control valve (14) of tower (2) interior flashing pressure；The entrance of liquid-phase outlet connection stripping tower (3) of the flash column (2)；
The lower part of the stripping tower (3) connects gas stripping gas conveyance conduit, and the top of the stripping tower (3) is equipped with the second gas phase and goes out
Mouthful, the hot recycling tower of the liquid-phase outlet connection hot recycling unit of the stripping tower (3)；
Hot recycling unit carries out the regeneration of absorbent to receive the sulfur-rich absorbent after pre- concentrate cell processing, including heat is again
Raw tower (1), the hot recycling tower (1) includes I section be arranged above and below and II section of two parts；I pars infrasegmentalis of the hot recycling tower (1)
It is connected with output the first outlet tube of lean absorbent road, II pars infrasegmentalis of the hot recycling tower (1) is equipped with for providing hot recycling heat
Reboiler (8), II section of bottom of the hot recycling tower (1) are connected with the second outlet tube road of conveying aqueous solutions of absorbent.
2. the pre- upgrading system of sour gas according to claim 1, it is characterised in that the heat exchanger includes being serially connected
First Heat Exchanger (5) and the second heat exchanger (4), first outlet tube road is sequentially connected second heat exchanger (4) and
One heat exchanger (5).
3. the pre- upgrading system of sour gas according to claim 2, it is characterised in that the sulfur-rich absorbent conveyance conduit
It is sequentially connected the tube side of the First Heat Exchanger (5) and second heat exchanger (4), first outlet tube road is sequentially connected institute
State the shell side of the second heat exchanger (4) and First Heat Exchanger (5).
4. the pre- upgrading system of sour gas according to claim 3, it is characterised in that the first outlet tube road is equipped with
First bypass, the two-port of first bypass are located at the upstream and downstream of the heat exchanger, set in first bypass
There are the first valve (12)；
The sulfur-rich absorbent conveyance conduit is equipped with the second bypass, and the two-port of second bypass is located at described first
The upstream and downstream of heat exchanger (5) or second heat exchanger (4), and second bypass is equipped with the second valve (13).
5. the pre- upgrading system of sour gas according to claim 4, it is characterised in that the two-port point of first bypass
Not Wei Yu the First Heat Exchanger (5) or second heat exchanger (4) upstream and downstream.
6. the pre- upgrading system of sour gas according to claim 1, it is characterised in that the heat exchanger and the flash column
(2) superheater (6) are also connected between entrance.
7. according to claim 1 to the pre- upgrading system of sour gas described in any claim in 6, it is characterised in that the sudden strain of a muscle
It steams tower (2) and the stripping tower (3) shares same tower body, be isolated between the two using the first end socket (21), and the sudden strain of a muscle
Steam the top that tower (2) are located at the stripping tower (3)；
The liquid-phase outlet of the flash column (2) is connect with the entrance of stripping tower (3) by exterior line, the stripping tower (3)
Liquid-phase outlet connects the entrance of the hot recycling tower (1) by first circulation pump (11).
8. according to claim 1 to the pre- upgrading system of sour gas described in any claim in 6, it is characterised in that the sudden strain of a muscle
It steams tower (2) and the stripping tower (3) shares same tower body, be isolated between the two using tower tray (9), flash column (2) position
In the top of the stripping tower (3)；
The tower tray (9) is equipped with the riser (91) for entering the flash column (2) for the stripping tower (3) interior gas phase, the liter
Tracheae (91) constitutes second gaseous phase outlet on the stripping tower (3) top, is additionally provided on the tower tray (9) for the flash column
(2) liquid phase in enters the downspout (92) of the stripping tower (3)；
The liquid-phase outlet of the stripping tower (3) connects the entrance of the hot recycling tower (1) by first circulation pump (11).
9. according to claim 1 to the pre- upgrading system of sour gas described in any claim in 6, it is characterised in that the sudden strain of a muscle
It steams tower (2), the stripping tower (3) and the hot recycling tower (1) and shares same tower body, the flash column (2) and the stripping tower
(3) it is isolated between by the first end socket (21), passes through the second end socket between the stripping tower (3) and the hot recycling tower (1)
(31) it is isolated, and the flash column (2) described stripping tower (3) and the hot recycling tower (1) are sequentially arranged from top to bottom；
It is connect between the liquid-phase outlet of the flash column (2) and the entrance of stripping tower (3) by exterior line, the stripping tower
(3) it is connect between liquid-phase outlet and the entrance of the hot recycling tower (1) by outer fluid line.
10. according to claim 1 to the pre- upgrading system of sour gas described in any claim in 6, it is characterised in that described
Flash column (2), the stripping tower (3) and the hot recycling tower (1) share same tower body；The flash column (2) stripping tower
(3) it is sequentially arranged from top to bottom with the hot recycling tower (1)；
It is isolated between the flash column (2) and the stripping tower (3) by tower tray (9), the tower tray (9) is equipped with described in confession
Stripping tower (3) interior gas phase enters the riser (91) of the flash column (2), which constitutes the stripping tower (3)
Second gaseous phase outlet on top is additionally provided on the tower tray (9) and enters the stripping tower for the liquid phase in the flash column (2)
(3) downspout (92)；
It is isolated between the stripping tower (3) and the hot recycling tower (1) by the second end socket (31), the stripping tower (3)
It is connect between liquid-phase outlet and the entrance of the hot recycling tower (1) by outer fluid line.
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| CN201721418310.0U CN208115448U (en) | 2017-10-27 | 2017-10-27 | A kind of pre- upgrading system of sour gas |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201721418310.0U CN208115448U (en) | 2017-10-27 | 2017-10-27 | A kind of pre- upgrading system of sour gas |
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