CN209475945U - Low-temp methanol elutes strengthen the system - Google Patents
Low-temp methanol elutes strengthen the system Download PDFInfo
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- CN209475945U CN209475945U CN201920062506.3U CN201920062506U CN209475945U CN 209475945 U CN209475945 U CN 209475945U CN 201920062506 U CN201920062506 U CN 201920062506U CN 209475945 U CN209475945 U CN 209475945U
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Abstract
The utility model provides a kind of low-temp methanol elution strengthen the system, including methanol washing absorption tower, rich methanol heat exchanger, ammonia cooler and flash tank；Methanol flash line is drawn from Mathanol regenerating pipeline, the other end of methanol flash line is communicated to the inlet of flash tank；The leakage fluid dram of flash tank is connected to one end of half poor methanol feed-line；The other end of half poor methanol feed-line separates two branches, and line is in charge of in the conveying of respectively half poor methanol first and line is in charge of in the conveying of half poor methanol second；The other end that line is in charge of in the conveying of half poor methanol first is communicated to the 3rd CO2The top of absorber portion (10)；The other end that line is in charge of in the conveying of half poor methanol second is communicated to the top of desulfurization section.Advantage are as follows: (1) CO in unstripped gas can be effectively removed2Gas and sulfurous gas, to guarantee that the purified gas of discharge is up to standard；(2) it ensure that qualified when semi lean solution is drawn, make semi lean solution normal use.
Description
Technical field
The utility model belongs to gas scrubbing processing technology field, and in particular to a kind of low-temp methanol elution strengthen the system.
Background technique
Rectisol system is to remove CO2、H2S/SO2Effective means, be now widely used for chemical industry, energy industry.
In existing rectisol system, the upper and lower two parts of methanol washing absorption tower point, lower tower section is mainly used for
Desulfurization, upper tower section are mainly used for de- CO2, its working principle is that: contain CO2With the unstripped gas of sulphur from the bottom of methanol washing absorption tower
Portion enters the inside of methanol washing absorption tower, and bottom-up flowing；Meanwhile -60 DEG C or so of poor methanol is washed from methanol
The inside of methanol washing absorption tower is entered at the top of absorption tower, and is flowed from up to down；For unstripped gas, pass through first
Lower tower desulfurization section, the sulfurous gas being flowed into the methanol cleaning solution absorption unstripped gas of lower tower desulfurization section；Then, after basic desulfurization
Unstripped gas continue up flow to tower take off CO2Section, upper tower take off CO2The methanol cleaning solution of section absorbs the CO in unstripped gas2, most
Eventually, desulfurization takes off CO2Gas be purified gas, and from the top of methanol washing absorption tower be discharged；And for methanol cleaning solution,
In its from up to down flow process, firstly, -60 DEG C or so of poor methanol absorbs the CO in the gas after desulfurization2Gas；With
Poor methanol flow downward, constantly absorption CO2Gas will lead to the raising of methanol cleaning solution temperature；As absorption CO2Methanol cleaning solution
When beginning to flow into lower tower desulfurization section, temperature is -17 DEG C or so；Then, -17 DEG C or so of methanol cleaning solution absorbs unstripped gas
In sulfurous gas, finally obtain sulfur-bearing containing CO2Rich methanol cleaning solution, and from the bottom of methanol washing absorption tower to outlet
Out.
In above process, inventors have found that the prior art has at least the following problems:
For methanol cleaning solution, temperature is lower, to CO2The absorbability of gas and sulfurous gas is stronger.When being
When load of uniting is larger, since the methanol cleaning solution temperature for reaching lower tower desulfurization section is higher, in lower tower desulfurization section, to original
Expect that the sulphur removal effect of sulfurous gas in gas is poor, it is difficult to the sulfurous gas in unstripped gas is completely removed, to make finally to be discharged
Gas can not be up to standard；In addition, due to taking off CO in upper tower2Section, methanol cleaning solution temperature are also gradually got higher, and also reduce its removing
CO2The effect of gas, to keep the gas being finally discharged up to standard.
Utility model content
In view of the defects existing in the prior art, the utility model provides a kind of low-temp methanol elution strengthen the system, can be effective
It solves the above problems.
The technical solution adopted in the utility model is as follows:
The utility model provides a kind of low-temp methanol elution strengthen the system, including methanol washing absorption tower (1), rich methanol change
Hot device (2), ammonia cooler (3) and flash tank (4)；
Bottom connection unstripped gas admission line (5) of the methanol washing absorption tower (1) and sulfur-rich methanol tapping line
(6)；The top of the methanol washing absorption tower (1) is connected to purified gas exhaust line (7)；
In the inside of the methanol washing absorption tower (1), from top to bottom, respectively the first CO2Absorber portion (8), the 2nd CO2
Absorber portion (9), the 3rd CO2Absorber portion (10), the 4th CO2Absorber portion (11) and desulfurization section (12)；
Wherein, the first CO2The top of absorber portion (8) is connected to poor methanol feed liquor pipeline (13)；In the 2nd CO2
The first catch tray (C1) is arranged in the bottom of absorber portion (9)；The leakage fluid dram of first catch tray (C1) is communicated to the rich methanol
First heat source inlet of heat exchanger (2), after heat exchange cooling, the first cold source leakage fluid dram of the rich methanol heat exchanger (2) is logical
It crosses the first cold source pipeline (14) and is communicated to the 3rd CO2The top of absorber portion (10)；
3rd CO2The second catch tray (C2) is arranged in the bottom of absorber portion (10)；The row of second catch tray (C2)
Liquid mouth is communicated to the heat source inlet of the ammonia cooler (3), and after heat exchange cooling, the cold source leakage fluid dram of the ammonia cooler (3) is again
It is communicated to the Secondary Heat Source inlet of the rich methanol heat exchanger (2), after heat exchange cooling, the rich methanol heat exchanger (2)
Second cold source leakage fluid dram is communicated to the 4th CO by the second cold source pipeline (15)2The top of absorber portion (11)；
4th CO2Third catch tray (C3) is arranged in the bottom of absorber portion (11)；The row of the third catch tray (C3)
Liquid mouth is connected to Mathanol regenerating pipeline (16)；Also, methanol at reflux pipeline is drawn from the Mathanol regenerating pipeline (16)
(17), the other end of the methanol at reflux pipeline (17) is communicated to the top of the desulfurization section (12)；In the methanol at reflux pipe
1st valve (P1) is installed on line (17)；
It is also drawn methanol flash line (18) from the Mathanol regenerating pipeline (16), the methanol flash line (18)
The other end is communicated to the inlet of the flash tank (4)；The leakage fluid dram of the flash tank (4) and half poor methanol feed-line (19)
One end connection；The other end of the half poor methanol feed-line (19) separates two branches, and respectively half poor methanol first is defeated
Send be in charge of line (20) and half poor methanol second conveying be in charge of line (21)；The another of line (20) is in charge of in the conveying of half poor methanol first
End is communicated to the 3rd CO2The top of absorber portion (10) is in charge of on line (20) in half poor methanol first conveying and installs the
2 valves (P2)；The other end that line (21) is in charge of in the conveying of half poor methanol second is communicated to the top of the desulfurization section (12),
It is in charge of the 3rd valve (P3) of installation on line (21) in half poor methanol second conveying.
Low-temp methanol elution strengthen the system provided by the utility model has the advantage that
(1) CO in unstripped gas can be effectively removed2Gas and sulfurous gas, to guarantee that the purified gas of discharge is up to standard；
(2) it ensure that qualified when semi lean solution is drawn, make semi lean solution normal use.
Detailed description of the invention
Fig. 1 is the structural schematic diagram that low-temp methanol provided by the utility model elutes strengthen the system.
Wherein: 1- methanol washing absorption tower；2- rich methanol heat exchanger；3- ammonia cooler；4- flash tank；5- unstripped gas air inlet pipe
Line；The sulfur-rich methanol tapping line of 6-；7- purified gas exhaust line；The first CO of 8-2Absorber portion；The 2nd CO of 9-2Absorber portion；10-
Three CO2Absorber portion；The 4th CO of 11-2Absorber portion；12- desulfurization section；13- poor methanol feed liquor pipeline；14- the first cold source pipeline；15-
Two cold source pipelines；16- Mathanol regenerating pipeline；17- methanol at reflux pipeline；18- methanol flash line；Half poor methanol delivery pipe of 19-
Line；Line is in charge of in the conveying of half poor methanol first of 20-；Line is in charge of in the conveying of half poor methanol second of 21-；
The first catch tray of C1-；The second catch tray of C2-；C3- third catch tray；
The 1st valve of P1-；The 2nd valve of P2-；The 3rd valve of P3-.
Specific embodiment
The technical issues of in order to keep the utility model solved, technical solution and beneficial effect are more clearly understood, below
In conjunction with accompanying drawings and embodiments, the present invention will be further described in detail.It should be appreciated that specific implementation described herein
Example only to explain the utility model, is not used to limit the utility model.
The utility model provides a kind of low-temp methanol elution strengthen the system, up to standard by the purified gas of desulfurization section to guarantee,
It is directly entered lower tower by introducing the higher semi lean solution of one low temperature, purity, by reducing the temperature of methanol at reflux, is added to reach
Sulphur effect is washed by force, guarantees that rising gas is up to standard, and then semi lean solution is up to standard.Furthermore it is ensured that the purified gas of final discharge is up to standard.
The utility model provides a kind of low-temp methanol elution strengthen the system, with reference to Fig. 1, including methanol washing absorption tower 1, richness
Heat exchange of methanol device 2, ammonia cooler 3 and flash tank 4；
The bottom connection unstripped gas admission line 5 of methanol washing absorption tower 1 and sulfur-rich methanol tapping line 6；Methanol washing
The top on absorption tower 1 is connected to purified gas exhaust line 7；
In the inside of methanol washing absorption tower 1, from top to bottom, respectively the first CO2Absorber portion 8, the 2nd CO2Absorber portion 9,
3rd CO2Absorber portion 10, the 4th CO2Absorber portion 11 and desulfurization section 12；
Wherein, the first CO2The top of absorber portion 8 is connected to poor methanol feed liquor pipeline 13；In the 2nd CO2The bottom of absorber portion 9
First catch tray C1 is set；The leakage fluid dram of first catch tray C1 is communicated to the first heat source inlet of rich methanol heat exchanger 2, through changing
After heat drop temperature, the first cold source leakage fluid dram of rich methanol heat exchanger 2 is communicated to the 3rd CO by the first cold source pipeline 142Absorber portion 10
Top；
3rd CO2The second catch tray C2 is arranged in the bottom of absorber portion 10；It is cold that the leakage fluid dram of second catch tray C2 is communicated to ammonia
The heat source inlet of device 3, after heat exchange cooling, the cold source leakage fluid dram of ammonia cooler 3 is communicated to the second heat of rich methanol heat exchanger 2 again
Source inlet, after heat exchange cooling, the second cold source leakage fluid dram of rich methanol heat exchanger 2 is communicated to the by the second cold source pipeline 15
Four CO2The top of absorber portion 11；
4th CO2Third catch tray C3 is arranged in the bottom of absorber portion 11；The leakage fluid dram and Mathanol regenerating of third catch tray C3
Pipeline 16 is connected to；Also, methanol at reflux pipeline 17 is drawn from Mathanol regenerating pipeline 16, the other end of methanol at reflux pipeline 17 connects
Lead to the top of desulfurization section 12；1st valve P1 is installed on methanol at reflux pipeline 17；
Methanol flash line 18 is also drawn from Mathanol regenerating pipeline 16, the other end of methanol flash line 18 is communicated to sudden strain of a muscle
The inlet of steaming pot 4；The leakage fluid dram of flash tank 4 is connected to one end of half poor methanol feed-line 19；Half poor methanol feed-line
19 other end separates two branches, and line 20 is in charge of in the conveying of respectively half poor methanol first and the conveying of half poor methanol second is in charge of
Line 21；The other end that line 20 is in charge of in the conveying of half poor methanol first is communicated to the 3rd CO2The top of absorber portion 10, in half poor methanol
The 2nd valve P2 of installation on line 20 is in charge of in one conveying；The other end that line 21 is in charge of in the conveying of half poor methanol second is communicated to desulfurization section 12
Top, be in charge of on line 21 the 3rd valve P3 of installation in the conveying of half poor methanol second.
Low-temp methanol provided by the utility model elutes strengthen the system, its working principle is that:
(1) methanol washing absorption tower from top to bottom, is divided into the first CO2Absorber portion 8, the 2nd CO2Absorber portion 9, the 3rd CO2
Absorber portion 10, the 4th CO2Absorber portion 11 and desulfurization section 12；
Containing CO2Unstripped gas with sulphur enters methanol from unstripped gas admission line 5 from the bottom of methanol washing absorption tower
The inside of washing absorption tower, and bottom-up flowing；Since absorbability of the methanol cleaning solution to sulphur is much larger than to CO2Absorb energy
Power, therefore, the sulfurous gas in desulfurization section 12, basic absorbable unstripped gas；Then, the unstripped gas after basic desulfurization continue to
Upper flowing passes sequentially through the 4th CO2Absorber portion 11, the 3rd CO2Absorber portion 10, the 2nd CO2Absorber portion 9 and the first CO2Absorber portion 8
It carries out except CO2Operation finally removes CO2Purified gas with sulphur is from the top of methanol washing absorption tower, i.e., from purified gas exhaust pipe
Line 7 discharges；
(2) for methanol cleaning solution, since absorbability of the methanol cleaning solution to sulphur is much larger than to CO2Absorb energy
Therefore power, therefore only needs tower to absorb CO when 12 desulfurization of desulfurization section2Part methanol solution；So the 4th CO2The bottom of absorber portion
Third catch tray C3 is arranged in portion, and then by the 4th CO2Absorber portion bottom absorbs CO2Methanol solution pass through Mathanol regenerating pipeline
It draws, the temperature of methanol solution is -17 DEG C or so at this time；For -17 DEG C of methanol solution, three branches are divided into, a branch is logical
The top that methanol at reflux pipeline 17 is driven into desulfurization section again is crossed, removes sulphur for continuing to the gas in methanol washing absorption tower
Operation；Another branch is transported to Mathanol regenerating equipment, carries out Mathanol regenerating processing；Another branch passes through methanol flash line
18, which are transported to flash tank 4, carries out flash distillation except CO2Operation, obtains -60 DEG C or so of half poor methanol liquid after flash distillation；The half of -60 DEG C is poor
Methanol solution is divided into two branches, and a branch is in charge of line 20 by the conveying of half poor methanol first and is driven into the 3rd CO2Absorber portion 10
Top；Another branch is in charge of the top that line 21 is driven into desulfurization section 12 by the conveying of half poor methanol second；
- 60 DEG C or so of poor methanol is driven into the first CO by poor methanol feed liquor pipeline 132The top of absorber portion 8, -60
DEG C or so poor methanol flow from above to below and absorb CO2, therefore, the temperature of poor methanol gradually rises；As the 2nd CO of arrival2It inhales
When receiving the bottom of section 9, temperature reaches -17 DEG C or so；At this point, in the 2nd CO2The first catch tray is arranged in the bottom of absorber portion 9, into
And by the 2nd CO2The methanol cleaning solution of -17 DEG C of 9 bottom of absorber portion is drawn, and -17 DEG C of methanol cleaning solution of extraction, which is transported to, to be the richest in
Heat exchange cooling is carried out in alcohol heat exchanger 2, -38 DEG C or so of methanol cleaning solution is obtained after cooling, then pass through the first cold source pipeline 14
It is driven into the 3rd CO2- 60 DEG C or so that line 20 is squeezed into of half poor methanol is in charge of at the top of absorber portion with the conveying of half poor methanol first
After liquid mixing, it is further continued for flowing downward；
When methanol solution is from the 3rd CO2The top of absorber portion 10 flows to the 3rd CO2When the bottom of absorber portion 10, due to absorbing
CO2And temperature increases, in the 3rd CO2The bottom of absorber portion 10, methanol solution temperature are increased to -17 DEG C；In the 3rd CO2Absorber portion 10
Bottom be arranged the second catch tray C2, therefore, -17 DEG C of methanol solution, which is introduced into ammonia cooler, to cool down, cool to -33 DEG C or so,
It is further continued for being transported in rich methanol heat exchanger 2 and cool down, cool to -38 DEG C or so, then be driven into the 4th CO2The top of absorber portion 11
Portion；
When -38 DEG C of methanol solutions are from the 4th CO2The top of absorber portion 11 flow to the 4th CO2When the bottom of absorber portion 11, due to
Absorb CO2And temperature increases, in the 4th CO2The bottom of absorber portion 11, methanol solution temperature are increased to -17 DEG C；In the 4th CO2It inhales
Third catch tray C3 is arranged in the bottom for receiving section 11, therefore, after -17 DEG C of methanol solution is drawn by Mathanol regenerating pipeline 16, part -
17 DEG C of methanol solution returns the top of desulfurization section 12 by methanol at reflux pipeline 17 again, and divides with the conveying of half poor methanol second
- 60 DEG C or so of the half poor methanol liquid mixing that pipeline 21 is squeezed into, then flow downward from the top of desulfurization section 12 and absorb unstripped gas
In sulfurous gas；Finally, rich methanol is discharged from sulfur-rich methanol tapping line 6.
In above-mentioned technological process, there is following innovative point:
(1) for desulfurization section, using methanol at reflux and -60 DEG C or so of the half mixed methanol solution of poor methanol liquid to raw material
Sulfurous gas in gas is absorbed, and the temperature of methanol solution is effectively reduced by half poor methanol liquid, to improve in desulfurization
Section methanol solution, can be in desulfurization section by sulfenyl this removal in unstripped gas to the removal efficiency of sulfurous gas, and removal rate can reach
98%；To ensure that the purified gas being finally discharged meets index of correlation；
(2) in de- CO2Section, by de- CO2Section is divided into four absorber portions, and, on the one hand, since -60 DEG C of poor methanols are certainly
On flow downward during, with its constantly absorb CO2And its temperature is caused constantly to increase, and then to CO2Absorbability it is continuous
Decline, therefore, in the application, by the 2nd CO2The methanol solution of absorber portion bottom is drawn, after carrying out heat exchange cooling to it again again
It returns in methanol washing absorption tower；By the 3rd CO2The methanol solution of absorber portion bottom is drawn, and is weighed again after carrying out heat exchange cooling to it
It newly returns in methanol washing absorption tower, to constantly be cooled down to it in methanol solution flow process and improve it and absorb CO2
Ability, improve to CO2Removal efficiency；
On the other hand, since the methanol cleaning solution temperature obtained after heat exchange cooling generally can only achieve -38 DEG C, for more one
Step improves the absorption CO of methanol solution in methanol washing absorption tower2Ability, also in the 3rd CO2The top of absorber portion introduces -60 DEG C of left sides
Half right poor methanol liquid, and then further increase it and absorb CO2Ability, improve to CO2Removal efficiency；
(3) by aforesaid operations, from the 4th CO2The H contained in the methanol solution that the bottom of absorber portion is drawn2S/SO2Amount
It is considerably less, therefore it may only be necessary to can very convenient, low energy consumption the CO removed in methanol solution by flashing operation2, accorded with
The semi lean solution of standardization；
In conclusion low-temp methanol elution strengthen the system provided by the utility model has the advantage that
(1) CO in unstripped gas can be effectively removed2Gas and sulfurous gas, to guarantee that the purified gas of discharge is up to standard；
(2) it ensure that qualified when semi lean solution is drawn, make semi lean solution normal use.
The above is only the preferred embodiment of the utility model, it is noted that for the common skill of the art
For art personnel, without departing from the principle of this utility model, several improvements and modifications can also be made, these improve and
Retouching should also regard the protection scope of the utility model.
Claims (1)
1. a kind of low-temp methanol elutes strengthen the system, which is characterized in that including methanol washing absorption tower (1), rich methanol heat exchanger
(2), ammonia cooler (3) and flash tank (4)；
Bottom connection unstripped gas admission line (5) of the methanol washing absorption tower (1) and sulfur-rich methanol tapping line (6)；Institute
State top connection purified gas exhaust line (7) of methanol washing absorption tower (1)；
In the inside of the methanol washing absorption tower (1), from top to bottom, respectively the first CO2Absorber portion (8), the 2nd CO2It absorbs
Section (9), the 3rd CO2Absorber portion (10), the 4th CO2Absorber portion (11) and desulfurization section (12)；
Wherein, the first CO2The top of absorber portion (8) is connected to poor methanol feed liquor pipeline (13)；In the 2nd CO2It absorbs
The first catch tray (C1) is arranged in the bottom of section (9)；The leakage fluid dram of first catch tray (C1) is communicated to the rich methanol heat exchange
First heat source inlet of device (2), after heat exchange cooling, the first cold source leakage fluid dram of the rich methanol heat exchanger (2) passes through the
One cold source pipeline (14) is communicated to the 3rd CO2The top of absorber portion (10)；
3rd CO2The second catch tray (C2) is arranged in the bottom of absorber portion (10)；The leakage fluid dram of second catch tray (C2) connects
The heat source inlet for leading to the ammonia cooler (3), after heat exchange cooling, the cold source leakage fluid dram of the ammonia cooler (3) is communicated to again
The Secondary Heat Source inlet of the rich methanol heat exchanger (2), after heat exchange cooling, the second of the rich methanol heat exchanger (2) is cold
Source leakage fluid dram is communicated to the 4th CO by the second cold source pipeline (15)2The top of absorber portion (11)；
4th CO2Third catch tray (C3) is arranged in the bottom of absorber portion (11)；The leakage fluid dram of the third catch tray (C3) with
Mathanol regenerating pipeline (16) connection；Also, methanol at reflux pipeline (17) are drawn from the Mathanol regenerating pipeline (16), described time
The other end of stream methanol line (17) is communicated to the top of the desulfurization section (12)；It is installed on the methanol at reflux pipeline (17)
1st valve (P1)；
Also drawn methanol flash line (18) from the Mathanol regenerating pipeline (16), the methanol flash line (18) it is another
End is communicated to the inlet of the flash tank (4)；The one of the leakage fluid dram of the flash tank (4) and half poor methanol feed-line (19)
End connection；The other end of the half poor methanol feed-line (19) separates two branches, the conveying point of respectively half poor methanol first
Line (21) are in charge of in pipeline (20) and the conveying of half poor methanol second；Half poor methanol first conveys the other end company for being in charge of line (20)
Lead to the 3rd CO2The 2nd valve of installation on line (20) is in charge of in half poor methanol first conveying in the top of absorber portion (10)
(P2)；The other end that line (21) is in charge of in the conveying of half poor methanol second is communicated to the top of the desulfurization section (12), described
The 3rd valve (P3) of installation on line (21) is in charge of in the conveying of half poor methanol second.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920062506.3U CN209475945U (en) | 2019-01-15 | 2019-01-15 | Low-temp methanol elutes strengthen the system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920062506.3U CN209475945U (en) | 2019-01-15 | 2019-01-15 | Low-temp methanol elutes strengthen the system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209475945U true CN209475945U (en) | 2019-10-11 |
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ID=68131077
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| CN201920062506.3U Active CN209475945U (en) | 2019-01-15 | 2019-01-15 | Low-temp methanol elutes strengthen the system |
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| Country | Link |
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Address after: 277527 Mushi Town, Tengzhou City, Zaozhuang City, Shandong Province (resident) Patentee after: Lianhong (Shandong) Chemical Co.,Ltd. Address before: 277527 Mushi Town, Tengzhou City, Zaozhuang City, Shandong Province (resident) Patentee before: XINNENG FENGHUANG (TENGZHOU) ENERGY CO.,LTD. |
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