CN104357118A - Method for increasing recycling rate of liquefied natural gas - Google Patents
Method for increasing recycling rate of liquefied natural gas Download PDFInfo
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- CN104357118A CN104357118A CN201410585254.4A CN201410585254A CN104357118A CN 104357118 A CN104357118 A CN 104357118A CN 201410585254 A CN201410585254 A CN 201410585254A CN 104357118 A CN104357118 A CN 104357118A
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Abstract
The invention relates to the field of liquefied natural gases, and in particular to a method for recycling methane from an uncondensed gas of a liquefied natural gas purifying column by using a pressure swing adsorption method so as to increase the recycling rate of methane in the liquefied natural gas. According to the method, a raw material gas conveying pipe, the liquefied natural gas purifying column, the uncondensed gas discharged from the liquefied natural gas purifying column, and an adsorption tower are included. The method is characterized by comprising the following steps: adsorbing, vacuuming and increasing the pressure of the uncondensed gas, thereby obtaining a methane-rich gas, feeding back the methane-rich gas to the raw material gas conveying pipe or the liquefied natural gas purifying column to be recycled, adjusting the adsorption time so as to control the content of methane in a waste gas adsorbed by a pressure swing adsorption device, and achieving the purpose of increasing the recycling rate of methane of the liquefied natural gas purifying column. The method is simple to operate, the cost is reduced, the energy consumption is reduced, and the recycling rate of the liquefied natural gas is greater than 99.8%.
Description
Technical field
The present invention relates to natural gas liquids and reclaim field, particularly relate to a kind of method utilizing pressure swing absorption process to reclaim methane recovery in methane raising natural gas liquids from natural gas liquids purification tower noncondensable gas.
Background technology
Particularly containing in the source of the gas preparing liquefied natural gas technique of the noncondensable gas such as more hydrogen and nitrogen at coke-oven gas etc. from methane rich gas mixture preparing liquefied natural gas (being called for short LNG), in order to reduce the methane carried secretly in natural gas liquids purification tower tower top noncondensable gas, improve the rate of recovery of natural gas liquids, the method of usual employing reduces natural gas liquids purification tower tower top temperature, even employing increase take liquid nitrogen as the water cooler of cryogen, however, natural gas liquids tower top still can carry a small amount of methane secretly in dropping a hint, it is the important factor affecting liquefied natural gas plant methane recovery.And along with the reduction of natural gas liquids tower top heat exchanger efficiency, tower top middle methane of dropping a hint can increase, and reduces the rate of recovery of liquefied natural gas plant methane, unit lng production energy consumption is caused to increase.
A kind of in Chinese patent application publication No. CN102079999A take coke-oven gas as the method for raw material production natural gas liquids and synthetic gas, disclose and the methane rich of drying is sent into ice chest liquefaction, obtain natural gas liquids, non-condensable gas is sent into pressure-variable adsorption enrich methane unit entrance and is mixed with purification coal gas the H2 will purified in coal gas by pressure-variable adsorption, N2, CO and methane carry out being separated the method obtaining synthetic gas and methane-rich gas, the coal gas that noncondensable gas and methane content due to natural gas liquids ice chest are several times as much as noncondensable gas mixes the raw material as pressure-variable adsorption enrich methane unit, make still can carry a part of methane secretly in the synthetic gas obtained through pressure-swing absorption apparatus, fail to play and improve natural gas liquids methane recovery, reduce the effect of natural gas liquids energy consumption.
Coke-oven gas is utilized to produce the method for natural gas liquids in Chinese patent application publication No. CN102942972A, disclose noncondensable gas PSA molecular sieve and remove wherein N2, vacuum desorption is by the methane of PSA molecular sieve adsorption, in desorb, methane content more than 90% returns the method for coke-oven gas recycle, because methane content in stripping gas is up to 90%, from absorption waste gas release portion methane, thus methane recovery can be reduced.Fail equally to solve the problem improving the natural gas liquids rate of recovery.
Summary of the invention
In order to solve above technical problem, the invention provides a kind of method improving the natural gas liquids rate of recovery, from the noncondensable gas that natural gas liquids purification tower discharges, reclaiming methane, simple to operate, save cost, reduce energy consumption, the rate of recovery of natural gas liquids can reach more than 99.8%.
Solve a kind of method improving the natural gas liquids rate of recovery in the present invention of above technical problem, comprise unstripped gas transfer lime, natural gas liquids purification tower, the non-condensable gas that natural gas liquids purification tower discharges, adsorption tower, it is characterized in that: described non-condensable gas is successively through absorption, vacuumize, methane-rich gas is obtained after boosting step, methane-rich gas turns back in unstripped gas transfer lime or natural gas liquids purification tower again and recycles, and methane content in pressure-swing absorption apparatus absorption waste gas is controlled by the adjustment of adsorption time, reach the object improving natural gas liquids purification tower methane recovery.
In the present invention, prioritization scheme can be between described absorption and vacuum step and is provided with equal pressure drop and inverse put step, vacuumizes and be provided with between boosting step equal voltage rise step.
Further optimization, is provided with between described adsorption step and inverse put step and forward bleeds off pressure step.
Wherein, described equal voltage drop step >=1 time, equal voltage rise step >=1 time.
Describedly forward bleed off pressure step >=1 time.
In described adsorption tower, sorbent material is housed, sorbent material be in gac, activated alumina, silica gel and molecular sieve one or more.
Described adsorption tower >=2.
Described adsorption step pressure is greater than 0.15MPa, and inverse put step pressure is greater than 0.1Mpa, and evacuation step pressure is 0.001 ~ 0.06MPa.
Before unstripped gas is transported to other device, be also provided with unstripped gas stating step in described method, such as carry out standing gas with raw material gas holder, make unstripped gas react more stable in ensuing each step.
In above-mentioned pressure swing absorption process, the adsorption step pressure of pressure-swing absorption apparatus is greater than 0.15MPa, usually operates under natural gas liquids purification tower noncondensable gas discharges pressure.Inverse put step pressure is greater than 0.1Mpa, and evacuation step pressure is 0.001 ~ 0.06MPa.(pressure all represents by absolute pressure)
From natural gas liquids purification tower tower top noncondensable gas, adopt pressure swing adsorption device to control pressure-variable adsorption absorption waste gas methane content in the present invention, reclaim the method for methane in noncondensable gas to improve natural gas liquids methane recovery, reduce the method for natural gas liquids unit consumption of energy.
In the present invention, concrete steps detailed process is as follows:
(1) adsorption step: the natural gas liquids purification tower noncondensable gas containing methane enters adsorption bed from adsorption tower import, methane in noncondensable gas is by the adsorbent loaded in adsorption tower, and the noncondensable gas not easily adsorbed is discharged from adsorption column outlet and is called as absorption waste gas.This step realizes being separated of methane and other noncondensable gas components.In usual absorption waste gas, methane content controls 0.05% ~ 0.5%.
(2) forward step is bled off pressure: being the adsorption tower that adsorption step is completed or equal adsorption towers of completing of voltage drop step suddenly along strideing, discharge by the exit end of the gas in adsorption tower from adsorption tower by pipeline and sequencing valve, reduction adsorption column pressure.
(3) equal voltage drop step: all voltage drop step is the adsorption tower or the suitable adsorption tower suddenly completed of strideing that are completed by adsorption step, be communicated with the adsorption tower entering equal voltage rise step with sequencing valve by pipeline, reduce the methane component in the equal voltage drop step of pressure recovery of equal voltage drop step adsorption tower.Equal voltage drop step can be arranged to 1 time according to adsorptive pressure, or repeatedly as one all falls E1D and two and all falls E2D.
(4) inverse put step: adsorption step is completed or adsorption step complete after carried out again equal voltage drop step or along to stride rapid adsorption tower, open the sequencing valve connecting adsorption tower unstripped gas inlet end, discharge the gas in adsorption tower, reduce the pressure of adsorption tower, make the methane moiety solution sucking-off sorbent material be adsorbed in adsorption tower, obtain methane rich product, after inverse put step completes, adsorption column pressure is 0.1Mpa ~ 0.15 Mpa.
(5) vacuum step: utilize vacuum pump to find time to the adsorption tower after inverse put, the pressure of further reduction adsorption tower, make the methane be adsorbed in sorbent material separate sucking-off sorbent material further, obtain methane rich product, after inverse put step completes, adsorption column pressure is 0.001 ~ 0.06MPa.
(6) equal voltage rise step:
Adsorption tower after evacuation step is completed, be connected with the adsorption tower being in equal voltage drop step with sequencing valve by pipeline, gas in the equal voltage drop step adsorption tower making pressure higher enters the adsorption tower of equal voltage rise, to raise the pressure of equal voltage rise adsorption tower, and the methane in the equal pressure drop gas of recovery part.Equal voltage rise step can be arranged to 1 time according to adsorptive pressure, or repeatedly as two all rise E2R and and all rise E1R.
(7) boosting step: utilize absorption waste gas to boost to the adsorption tower after equal voltage rise step completes, make it to reach adsorptive pressure, prepare to enter adsorption step.
The method of the raising natural gas liquids rate of recovery of the present invention is applicable to from coal preparing liquefied natural gas, coke-oven gas preparing liquefied natural gas, blue carbon tail gas preparing liquefied natural gas etc. that other contain the liquefied natural gas plant of noncondensable gas.
For existing natural gas liquefaction device, methane recovery can bring up to more than 99.8% by 94% ~ 96%, and in the not solidifying hydrogen rich gas of tower top, methane content is reduced to less than 0.2% by 3% ~ 5%.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of embodiment 1 in the present invention
Fig. 2 is the process flow sheet of embodiment 2 in the present invention
embodiment
Below by way of the embodiment of embodiment, the present invention is further detailed explanation.But this should be interpreted as that the scope of the above-mentioned theme of the present invention is only limitted to following embodiment.Without departing from the idea case in the present invention described above, the various replacement made according to ordinary skill knowledge and customary means or change, include within the scope of the invention.
Embodiment 1
The present embodiment is take coke-oven gas as the device of raw material preparing liquefied natural gas after methanation, and liquefied natural gas (LNG)-throughput is 100,000 tons/year.In an embodiment, coke-oven gas enters methanation conversion reactor after desulfurizing and purifying, in methanator, carbon monoxide, carbonic acid gas and hydrogen reaction generate methane, gas after methanation reaction removes water through purification, LNG cold purification tower is entered after the impurity such as traces of carbon dioxide and mercury, low temperature purification tower adopts the two refrigerants circularly cooling of MRC refrigerant cycle refrigeration and liquid nitrogen cryogen, methane recovery is improved to reduce purification tower top temperature, methane recovery is 98.5% in this case, tower top hydrogen rich gas pressure 1.3Mpa, methane content about 1.5% in nitrogen-rich gas, pressure 0.6Mpa, in order to improve methane recovery further, the gas hydrogen-rich gas that tower top of being purified by LNG cold discharges mixes with nitrogen-rich gas, after mixing, methane content is 1.74%, introduce by 5 adsorbers, sequencing valve, the pressure-variable adsorption of PLC control system and vacuum pump composition reclaims methane unit and adsorption tower.Methane in noncondensable gas by the adsorbent loaded in adsorption tower, from adsorption column outlet obtain methane content lower than 0.12% rich hydrogen and nitrogen-rich gas discharger for fuel or other purposes.From inverse put and finding time obtain gas ~ the methane rich stripping gas of 9% returns the methane recovery that the coke-oven coal gas holder raw materials recovery methane wherein mixed with coke-oven gas as gas employing methanation of coke oven preparing liquefied natural gas device increases whole device, methane recovery 99.9%.Natural gas liquids 1400 tons can be increased production every year.
Pressure 0.6Mpa flow 14868Nm after the mixing of LNG cold purification tower top noncondensable gas
3/ h composition is in table 1
Table 1 purify tower top noncondensable gas composition
Pressure-variable adsorption reclaims methane unit and is formed by connecting by 5 adsorption towers, program-controlled valve and corresponding pipeline.Each working cycle experience absorption A, all falls that ED2, inverse put D all fall in ED1, two, the V that finds time, two all rises ER2, and all rises ER1, final boosting FR eight steps, and its each tower runs sequential in table 2.
Table 2 PSA cell operation time-scale
Now for adsorption tower A, describe each processing step:
Absorption A
The unstripped gas that noncondensable gas from natural gas liquids tower top makes recovery unit enters adsorption tower A, and wherein methane component is preferentially adsorbed and stays in adsorption bed, containing the absorption waste gas take-off equipment of the impurity such as weakly stable component H2, N2.
One equal pressure drop E1D
Gas in adsorption tower A and adsorption tower C carry out pressure equalization, and when two pressure towers are substantially equal, this step terminates.
Two equal pressure drop E2D
Gas in adsorption tower A and adsorption tower D carry out pressure equalization, and when two pressure towers are substantially equal, this step terminates.
Inverse put D
In adsorption tower A, gas carries out reverse bleeding off pressure against the direction of absorption, against being deflated to inverse put gas surge tank.
Find time V
Vacuum pump directly vacuumizes adsorption tower A, and half product gas that vacuum pump is extracted out enters half gas product surge tank and mixes with inverse put gas phase after water cooler is chilled to 40 DEG C.Pressure process drops to-0.085MPa by 0.02MPa.
Two equal voltage rise E2R
In adsorption tower C, gas flows into adsorption tower A, and carry out pressure equalization, when two pressure towers are substantially equal, this step terminates.
One equal voltage rise E1R
In adsorption tower D, gas flows into adsorption tower A, and carry out pressure equalization, when two pressure towers are substantially equal, this step terminates.
Final boosting FR
Absorption waste gas enters adsorption tower A and finally boosts.When adsorption tower A pressure is substantially close to adsorptive pressure, this step terminates.
So far, all eight steps of adsorption tower A in one-period are all finished, and start to enter and circulate next time, and other step performed by 4 adsorption towers is identical with adsorption tower A, just mutually staggers in time, to ensure that sepn process is carried out continuously.
Each adsorption column pressure is periodical change with the change of processing step, and according to actually operating situation, adsorptive pressure can suitably adjust, then other step pressure is corresponding changes.
High methane gas scale of construction 1561Nm after concentrated
3/ h, forms as shown in table 3
Methane-rich gas composition after table 3 is concentrated
Export hydrogen rich gas amount 11485 Nm of concentrating unit
3/ h, forms as shown in table 4
Methane-rich gas composition after table 4 is concentrated
Embodiment 2
The present embodiment is take coke-oven gas as the device of raw material preparing liquefied natural gas (natural gas liquids) after methanation, and liquefied natural gas (LNG)-throughput is 80,000 tons/year.In an embodiment, coke-oven gas enters methanation conversion reactor after desulfurizing and purifying, in methanator, carbon monoxide, carbonic acid gas and hydrogen reaction generate methane, gas after methanation reaction removes water through purification, LNG cold purification tower is entered after the impurity such as traces of carbon dioxide and mercury, low temperature purification tower adopts MRC refrigerant cycle refrigeration, methane recovery is 96%, tower top hydrogen rich gas pressure 1.3Mpa, wherein methane content 4.5%, in order to improve methane recovery further, the hydrogen-rich gas that tower top of being purified by LNG cold speeds to put is introduced by 6 adsorbers, sequencing valve, the pressure-variable adsorption of PLC control system and vacuum pump composition reclaims methane unit.Methane in noncondensable gas, by the adsorbent loaded in adsorption tower, obtains methane content lower than 0.52% hydrogen-rich gas discharger for fuel or other purposes from adsorption column outlet.Compressed natural gas liquids (natural gas liquids) the purification tower recovery methane wherein that returns to 1.5Mpa of methane rich stripping gas obtaining about 3.2% from inverse put and gas of finding time increases methane recovery, methane recovery 99.6%.Annual increase liquefied natural gas (LNG)-throughput 2917 tons.
LNG cold purification tower top noncondensable gas pressure 1.3Mpa flow 12550Nm
3/ h composition is in table 5
Table 5 purify tower top noncondensable gas composition
Pressure-variable adsorption reclaims methane unit and is formed by connecting by 6 adsorption towers, program-controlled valve and corresponding pipeline.Each working cycle experience absorption A, along putting, PP, all falls that ED2, inverse put D all fall in ED1, two, the V that finds time, two all rises ER2, and all rises ER1, final boosting FR nine steps, and its each tower runs sequential in table 6.
Table 6 PSA cell operation time-scale
Now for adsorption tower A, describe each processing step:
Absorption A
The unstripped gas that noncondensable gas from natural gas liquids tower top makes recovery unit enters adsorption tower A, and wherein methane component is preferentially adsorbed and stays in adsorption bed, containing the absorption waste gas take-off equipment of the impurity such as weakly stable component H2, N2.
Along putting PP
Open the sequencing valve connected along putting pipeline, the gas in the adsorption tower A after being completed by adsorption step discharges adsorption tower from adsorption column outlet end, reduces the pressure of adsorption tower to 0.6Mpa.
One equal pressure drop E1D
Gas in adsorption tower A and adsorption tower D carry out pressure equalization, and when two pressure towers are substantially equal, this step terminates.
Two equal pressure drop E2D
Gas in adsorption tower A and adsorption tower E carry out pressure equalization, and when two pressure towers are substantially equal, this step terminates.
Inverse put D
In adsorption tower A, gas carries out reverse bleeding off pressure against the direction of absorption, against being deflated to inverse put gas surge tank.
Find time V
Vacuum pump directly vacuumizes adsorption tower A, and half product gas that vacuum pump is extracted out enters half gas product surge tank and mixes with inverse put gas phase after water cooler is chilled to 40 DEG C.Pressure process drops to-0.085MPa by 0.02MPa.
Two equal voltage rise E2R
In adsorption tower C, gas flows into adsorption tower A, and carry out pressure equalization, when two pressure towers are substantially equal, this step terminates.
One equal voltage rise E1R
In adsorption tower D, gas flows into adsorption tower A, and carry out pressure equalization, when two pressure towers are substantially equal, this step terminates.
Final boosting FR
Absorption waste gas enters adsorption tower A and finally boosts.When adsorption tower A pressure is substantially close to adsorptive pressure, this step terminates.
So far, all eight steps of adsorption tower A in one-period are all finished, and start to enter and circulate next time, and other step performed by 4 adsorption towers is identical with adsorption tower A, just mutually staggers in time, to ensure that sepn process is carried out continuously.
Each adsorption column pressure is periodical change with the change of processing step, according to actually operating situation, adsorptive pressure and can suitably adjusting along bleeding off pressure power, then other step pressure is corresponding changes.
High methane gas scale of construction 1590Nm after concentrated
3/ h, forms as shown in table 7
Methane-rich gas composition after table 7 is concentrated
Export hydrogen rich gas amount 10960 Nm of concentrating unit
3/ h, forms as shown in table 8
Methane-rich gas composition after table 8 is concentrated
Claims (9)
1. one kind is improved the method for the natural gas liquids rate of recovery, comprise unstripped gas transfer lime, non-condensable gas, adsorption tower that natural gas liquids purification tower, natural gas liquids purification tower discharge, it is characterized in that: described non-condensable gas successively through adsorbing, vacuumizing, after boosting step methane-rich gas, methane-rich gas turns back in feed line or natural gas liquids purification tower the methane reclaimed wherein again.
2. a kind of method improving the natural gas liquids rate of recovery according to claim 1, is characterized in that: be provided with equal pressure drop and inverse put step between described absorption and vacuum step, vacuumizes and be provided with between boosting step equal voltage rise step.
3. a kind of method improving the natural gas liquids rate of recovery according to claim 2, is characterized in that: be provided with between described adsorption step and inverse put step and forward bleed off pressure step.
4. a kind of method improving the natural gas liquids rate of recovery according to claim 2, is characterized in that: described equal voltage drop step >=1 time, equal voltage rise step >=1 time.
5. a kind of method improving the natural gas liquids rate of recovery according to claim 3, is characterized in that: describedly forward bleed off pressure step >=1 time.
6. a kind of method improving the natural gas liquids rate of recovery according to any one of claim 1-5, is characterized in that: in described adsorption tower, sorbent material is housed, sorbent material be in gac, activated alumina, silica gel and molecular sieve one or more.
7. a kind of method improving the natural gas liquids rate of recovery according to any one of claim 1-5, is characterized in that: described adsorption tower >=2.
8. a kind of method improving the natural gas liquids rate of recovery according to any one of claim 1-5, it is characterized in that: the adsorption step pressure of described pressure-variable adsorption is greater than 0.15MPa, inverse put step pressure is greater than 0.1Mpa, and evacuation step pressure is 0.001 ~ 0.06MPa.
9. a kind of method improving the natural gas liquids rate of recovery according to claim 1, is characterized in that: be also provided with unstripped gas stating step in described method.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113091818A (en) * | 2021-04-06 | 2021-07-09 | 宁夏弘茂特种设备检验检测有限公司 | LNG raffinate recovery unit |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1051459A1 (en) * | 1998-01-27 | 2000-11-15 | Exxon Research And Engineering Company | Hydrodesulfurisation of gas well hydrocarbon liquids using hydrogen produced from syngas |
| CN1330974A (en) * | 2000-06-28 | 2002-01-16 | 四川天一科技股份有限公司 | Vacuum pressure-variable process for removing ethane or hydrocarbons over ethane from gas-state hydrocarbon |
| CN1680002A (en) * | 2005-02-01 | 2005-10-12 | 四川天一科技股份有限公司 | Pressure varying adsorption of recovering effective components from relaxed methanol gas |
| CN101096907A (en) * | 2006-06-27 | 2008-01-02 | 上海标氢气体技术有限公司 | Method for producing natural gas from coal bed gas under low pressure |
| CN102079999A (en) * | 2011-01-21 | 2011-06-01 | 成都赛普瑞兴科技有限公司 | Method for producing liquefied natural gas and synthetic gas by taking coke oven gas as raw material |
| CN102698563A (en) * | 2012-06-11 | 2012-10-03 | 四川亚连科技有限责任公司 | High purity and high recovery rate methane concentration production process and implementing device thereof |
-
2014
- 2014-10-28 CN CN201410585254.4A patent/CN104357118B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| EP1051459A1 (en) * | 1998-01-27 | 2000-11-15 | Exxon Research And Engineering Company | Hydrodesulfurisation of gas well hydrocarbon liquids using hydrogen produced from syngas |
| CN1330974A (en) * | 2000-06-28 | 2002-01-16 | 四川天一科技股份有限公司 | Vacuum pressure-variable process for removing ethane or hydrocarbons over ethane from gas-state hydrocarbon |
| CN1680002A (en) * | 2005-02-01 | 2005-10-12 | 四川天一科技股份有限公司 | Pressure varying adsorption of recovering effective components from relaxed methanol gas |
| CN101096907A (en) * | 2006-06-27 | 2008-01-02 | 上海标氢气体技术有限公司 | Method for producing natural gas from coal bed gas under low pressure |
| CN102079999A (en) * | 2011-01-21 | 2011-06-01 | 成都赛普瑞兴科技有限公司 | Method for producing liquefied natural gas and synthetic gas by taking coke oven gas as raw material |
| CN102698563A (en) * | 2012-06-11 | 2012-10-03 | 四川亚连科技有限责任公司 | High purity and high recovery rate methane concentration production process and implementing device thereof |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN113091818A (en) * | 2021-04-06 | 2021-07-09 | 宁夏弘茂特种设备检验检测有限公司 | LNG raffinate recovery unit |
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