CN103173256A - Natural gas multi-tower external cycle anaerobic regeneration dewatering method - Google Patents
Natural gas multi-tower external cycle anaerobic regeneration dewatering method Download PDFInfo
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- CN103173256A CN103173256A CN2013101346303A CN201310134630A CN103173256A CN 103173256 A CN103173256 A CN 103173256A CN 2013101346303 A CN2013101346303 A CN 2013101346303A CN 201310134630 A CN201310134630 A CN 201310134630A CN 103173256 A CN103173256 A CN 103173256A
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 72
- 238000000034 method Methods 0.000 title claims abstract description 41
- 239000003345 natural gas Substances 0.000 title claims abstract description 32
- 230000008929 regeneration Effects 0.000 title claims abstract description 23
- 238000011069 regeneration method Methods 0.000 title claims abstract description 23
- 238000001179 sorption measurement Methods 0.000 claims abstract description 58
- 239000007789 gas Substances 0.000 claims abstract description 50
- 230000008569 process Effects 0.000 claims abstract description 25
- 238000001816 cooling Methods 0.000 claims abstract description 14
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 13
- 238000010926 purge Methods 0.000 claims abstract description 11
- 238000010438 heat treatment Methods 0.000 claims abstract description 9
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 8
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 7
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 7
- 238000004064 recycling Methods 0.000 claims abstract description 3
- 229920006395 saturated elastomer Polymers 0.000 claims abstract description 3
- 239000012535 impurity Substances 0.000 claims abstract 2
- 239000002594 sorbent Substances 0.000 claims description 22
- 235000009508 confectionery Nutrition 0.000 claims description 16
- 238000010521 absorption reaction Methods 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 12
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 6
- 239000000203 mixture Substances 0.000 claims description 4
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 238000003795 desorption Methods 0.000 claims 1
- 239000003463 adsorbent Substances 0.000 abstract description 5
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000003949 liquefied natural gas Substances 0.000 abstract 2
- 230000006837 decompression Effects 0.000 abstract 1
- 238000002360 preparation method Methods 0.000 abstract 1
- 230000002035 prolonged effect Effects 0.000 abstract 1
- 239000007787 solid Substances 0.000 description 9
- 238000006243 chemical reaction Methods 0.000 description 8
- 230000018044 dehydration Effects 0.000 description 8
- 238000006297 dehydration reaction Methods 0.000 description 8
- 239000002904 solvent Substances 0.000 description 5
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 4
- 239000012530 fluid Substances 0.000 description 4
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 3
- 239000002808 molecular sieve Substances 0.000 description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 3
- 230000003245 working effect Effects 0.000 description 3
- 239000004229 Alkannin Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000002151 riboflavin Substances 0.000 description 2
- 239000000741 silica gel Substances 0.000 description 2
- 229910002027 silica gel Inorganic materials 0.000 description 2
- 239000004149 tartrazine Substances 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000002156 adsorbate Substances 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 238000007429 general method Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 229940074869 marquis Drugs 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- NMJORVOYSJLJGU-UHFFFAOYSA-N methane clathrate Chemical compound C.C.C.C.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O.O NMJORVOYSJLJGU-UHFFFAOYSA-N 0.000 description 1
- VBUNOIXRZNJNAD-UHFFFAOYSA-N ponazuril Chemical compound CC1=CC(N2C(N(C)C(=O)NC2=O)=O)=CC=C1OC1=CC=C(S(=O)(=O)C(F)(F)F)C=C1 VBUNOIXRZNJNAD-UHFFFAOYSA-N 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
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Abstract
The invention relates to a natural gas multi-tower external cycle anaerobic regeneration dewatering method, and particularly relates to a natural gas dewatering device and a technique of an LNG (liquefied natural gas) preparation station for large-scale concentrated treatment of natural gas pipeline transportation. The dewatering method is characterized by comprising the steps of absorbing moisture in gas in saturated gas by an adsorbent under a normal-temperature condition through an adsorption tower; carrying out anaerobic regeneration on the adsorbent in the adsorption tower by external regenerated gas, utilizing in a recycling manner, and desorbing impurity components such as water and heavy hydrocarbon adsorbed on the adsorbent, so as to carry out the next adsorption process by the adsorption tower, wherein each adsorption tower passes through the processes of adsorption, decompression, purging, heating, cooling and boosting. The technique has the characteristics of simple flow, high dewatering efficiency, low energy consumption and the like; the service life of the adsorbent is prolonged; and the operating cost is reduced.
Description
Technical field
The invention belongs to the natural gas conditioning field, particularly the technical field of Oilfield Natural Gas Plant dehydration.
Background technology
The Sweet natural gas that well head flows out is nearly all the gas phase saturation water, even can carry a certain amount of liquid water.In Sweet natural gas, the existence of moisture tends to cause serious consequence: contain CO
2And H2
SSweet natural gas in the situation that there is water exist to form acid and corrosion pipeline and equipment; Form gas hydrate under certain condition and stop up valve, pipeline and equipment; Reduce pipeline transmission capacity, cause unnecessary power consumption.Moisture is very disadvantageous thing in the existence of Sweet natural gas, therefore, needs the requirement of dehydration more strict.
The method of gas dehydration generally comprises low temperature process, solvent absorption, solid absorption method, chemical reaction method and membrane separation process etc.The low temperature process dehydration utilizes high-pressure natural gas throttling expansion cooling or utilizes the gas wave machine expansion lower the temperature and realize, this technique is suitable for high-pressure natural gas; And for low pressure natural gas, must supercharging if will use, thus the economy of process affected.Solvent absorption and solid absorption method are used more extensive at present in gas industry.The solvent absorption dehydration is one of the most general method of using in present gas industry.It utilizes principle of absorption, adopts a kind of hydrophilic solvent fully to contact with Sweet natural gas, thereby makes water be delivered to the purpose that reaches dehydration in solvent.When liquid contacts with the solid surface of porous, due to the interaction between fluid molecule and solid surface molecule, fluid molecule can be attracted on solid surface, causes fluid molecule content on solid surface to increase, and this phenomenon is called the adsorption phenomena of solid surface.The solid absorption method is exactly to utilize the solid, porous particles material that optionally the fluid-absorbent Semi-polarity is strong to be attached on its surfaces externally and internally, thus the method that fluid mixture is separated.Solid material with certain adsorptive power is called sorbent material, and the material that is adsorbed is called adsorbate.Absorption method sorbent material commonly used has molecular sieve, silica gel and activated alumina at present.
CN102703151A, CN101508928B, CN201692757U, all adopted part Sweet natural gas before dewatering or the part Sweet natural gas after dehydration to carry out thermal regeneration as resurgent gases in these patents such as CN2456821Y, dehydrated adsorbent commonly used has molecular sieve at present, silica gel and activated alumina, during except silica regeneration, temperature is lower, only have outside 180-230 ℃, the regeneration temperature of molecular sieve and activated alumina is all higher, be generally 220-310 ℃, owing to containing the oxygen of a large amount of hydrogen sulfide and trace in the Sweet natural gas before not dewatering, in the thermal regeneration process, the oxygen of hydrogen sulfide and trace is at the mesopore inside diameter surface generation claus reaction of sorbent material, reaction equation following (1):
3H
2S+3/2O
2=3/xS
x+3H
2O+615KJ/mol
S due to the claus reaction generation
xBe attached to before this bore surface of sorbent material, then be the outside surface that is attached to sorbent material, along with time lengthening, the dewatering efficiency that causes sorbent material descended and must change sorbent material, the dewatering system resistance drop increases and impacts to follow-up workshop section, has increased Financial cost.
Summary of the invention
The purpose of this invention is to provide a kind of simple flow, reduce investment outlay, the Sweet natural gas multitower outer circulation anaerobic regeneration dewatering of occupation of land and working cost, prevent that the claus reaction in adsorption tower from generating, effectively extended the work-ing life of sorbent material.
The object of the present invention is achieved like this, Sweet natural gas multitower outer circulation anaerobic regeneration dewatering, and the method comprises the steps:
1) absorption: saturated gas is utilized the moisture of tower internal adsorption agent in absorbed natural gas by adsorption tower under normal temperature condition, its adsorption time is 7-8 hour;
2) step-down: after completing adsorption process, adsorption tower carries out pressure in the reverse tower of releasing to 0-0.6MPa by pipeline and valve;
3) purge: after the step-down process is completed, adopt resurgent gases that adsorption tower is purged, purge time 3-10 minute;
4) heating: resurgent gases is heated to 260-310 ℃ of scope, enter adsorption tower bottom adsorption tower, with be adsorbed on sorbent material the moisture thermal regeneration out, its heating regeneration gas is through being cooled to 30-40 ℃, separate and return to supercharger after its liquid water and heavy hydrocarbon and recycle, be 4-4.5 hour heat-up time;
5) cooling: after thermal regeneration is completed, namely pass into the normal temperature resurgent gases to adsorption tower, by the normal temperature resurgent gases, the heat in adsorption tower is shifted out, make the temperature of adsorption tower drop to 30-50 ℃, be 3-3.5 hour cooling time;
6) boost: with cooling rear adsorption tower port closing, introduce partial raw gas and enter into this tower, the press process that makes its pressure reach raw natural gas is the process of boosting.
Described adsorption tower number is 2-10.
Described resurgent gases is nitrogen or the methane of oxygen-free component.
Described recycling is that resurgent gases is pressurized to 0.1-0.6MPa by supercharger, then through heating/enter adsorption tower after cooling, adsorption tower out after again after cooling, gas-liquid separation, resurgent gases is returned to the import of supercharger, so consist of circulation loop, make the resurgent gases recycle.A small amount of resurgent gases loss is arranged in purge, increase resurgent gases and fill into pipeline with the resurgent gases of replenish loss on supercharger ingress or gas-liquid separation equipment.
In sum, advantage of the present invention is:
1) adopt the anaerobic resurgent gases that sorbent material is regenerated, prevent that effectively claus reaction from occuring, and improves dewatering efficiency;
2) increase the work-ing life of sorbent material, saved running cost; Simultaneously, owing to adopting the anaerobic resurgent gases, sorbent material is regenerated, prevent that effectively claus reaction from occuring, avoided being attached to due to the Sx that claus reaction generates the bore surface of sorbent material, then be the outside surface that is attached to sorbent material, cause the dewatering efficiency of sorbent material to descend and the necessary defective of changing sorbent material.Sorbent material will be changed in general 2 years to 3 years in present dehydration project both domestic and external, and sorbent material work-ing life to 5 can be extended in the application to 6 years.
3) resurgent gases after supercharging directly is connected in series with interchanger, and resurgent gases recycles, and has reduced energy consumption;
4) have security of system, surely write, simple to operate, the characteristics that level of automation is high.
Description of drawings
Fig. 1 is the schematic flow sheet of the present embodiment.
Embodiment
Referring to Fig. 1, for convenience of narration, the below illustrates the present invention as an example of four adsorption towers of T101A ~ D example.Wherein, two towers of adsorption tower T101A and adsorption tower T101B are in adsorption process, and adsorption tower T101C is in heat-processed, and adsorption tower T101D is in process of cooling.
Adsorption process
What the present embodiment adopted is double tower absorption in parallel, and namely in office when the marquis has two towers to be in adsorption step, and the feed time of two towers differs adsorption cycle half.
Raw natural gas (containing saturation water) enters from the top of adsorption tower T101A and T101B through valve K1a and K1b under normal temperature condition, out send out-of-bounds through valve K2a and K2b from the bottom of adsorption tower T101A and T101B, water, heavy hydrocarbon in this process Raw gas (are mainly C
4+-hydrocarbon is adsorbed agent absorption, and the methane that is not adsorbed, nitrogen, ethane, propane etc. are sent out-of-bounds through valve K2a and K2b, and its adsorption time is 7-8 hour;
The step-down process
Complete the adsorption tower T101B of adsorption process, through valve K6b against the direction of absorption with the pressure decreased of adsorption tower T101B to 0-0.6MPa, have a small amount of moisture and heavy hydrocarbon this moment along with the Sweet natural gas of step-down is discharged, this part low pressure natural gas is discharged the battery limit (BL) use that can directly act as a fuel;
Purge
Adsorption tower T101B is after the step-down process is completed, entering a small amount of resurgent gases by valve K3b in the bottom of adsorption tower T101B purges it, hydrogen a small amount of in raw natural gas between absorbent particles is displaced, and resurgent gases is nitrogen or the methane of oxygen-free component, purge time 3-10 minute;
Heat-processed
Resurgent gases is heated to 260-310 ℃ by well heater E101, enter bottom adsorption tower T101B through valve K4b, with be adsorbed on sorbent material the moisture thermal regeneration out, resurgent gases after heating is being carried moisture and a small amount of heavy hydrocarbon and is being entered water cooler E103 through valve K5b and be cooled to 30-40 ℃, then enter gas-liquid separator V101 and recycle except return to supercharger C101 after liquid water and heavy hydrocarbon, be 4-4.5 hour heat-up time;
Process of cooling
After adsorption tower T101B thermal regeneration is completed, to enter into through the resurgent gases that supercharger C101 is pressurized to 0.1-0.6MPa water cooler E102 heat exchange to 30 ~ 50 ℃, then enter adsorption tower T101B through valve K4b, heat in tower is shifted out by valve K5b, make the temperature of adsorption tower T101B drop to 30-50 ℃, this process further removes the moisture in tower, and be 3-3.5 hour cooling time;
The process of boosting
Cooled adsorption tower T101B outlet valve is closed, introduce partial raw gas and enter into adsorption tower T101B through valve K6b, make its pressure reach the pressure of raw natural gas.
So far, realized the circulation of adsorption tower T101B from the adsorption process-step-down process-purge-heat-processed-process of cooling-process of boosting.Four adsorption towers all consist of circulation by top step, have guaranteed the continuously feeding of unstripped gas and the continuous wave output of product.
According to top step, resurgent gases is pressurized to 0.1-0.6MPa by supercharger C101, then through after well heater E101/ water cooler E102, each adsorption tower being carried out purge, heating cycle process, refrigeration cycle process, the resurgent gases of adsorption tower after out is cooled to 30-40 ℃ through supercooler E103 and enters gas-liquid separator V101, resurgent gases after gas-liquid separation out is back to the import of supercharger C101 afterwards from gas-liquid separator V101 top, so consist of circulation loop, make the resurgent gases recycle.
A small amount of resurgent gases loss is arranged in purge, increase resurgent gases and fill into pipeline with the resurgent gases of replenish loss on supercharger ingress or gas-liquid separation equipment.
As above institute's art, can implement the present invention preferably.
Claims (5)
1. Sweet natural gas multitower outer circulation anaerobic regeneration dewatering, it is characterized in that comprising the moisture that saturated gas is utilized under normal temperature condition by adsorption tower in sorbent material adsorbed gas, then adopt extraneous resurgent gases to carry out anaerobic regeneration to the sorbent material in adsorption tower, and recycle, make the impurity composition desorptions such as the water that is adsorbed on sorbent material, heavy hydrocarbon out, so that adsorption tower carries out adsorption process next time, each adsorption tower will be through absorption, step-down, purging, heating, the cooling and process of boosting.
2. Sweet natural gas multitower outer circulation anaerobic regeneration dewatering as claimed in claim 1, is characterized in that described adsorption tower number is 2-10.
3. Sweet natural gas multitower outer circulation anaerobic as claimed in claim 1 regeneration dewatering, it is characterized in that described anaerobic be regenerated as utilize the extraneous gas that oxygen-free gas composition is provided to adsorption tower purge, heating, process of cooling.
4. Sweet natural gas multitower outer circulation anaerobic as claimed in claim 3 regeneration dewatering, the gas that it is characterized in that described oxygen-free gas composition is nitrogen or methane.
5. Sweet natural gas multitower outer circulation anaerobic as claimed in claim 1 regeneration dewatering is characterized in that described recycling is that the gas after regeneration is so consisted of closed-circuit system and recycles by pressurization, heating/cooling, regeneration, cooling, gas-liquid separation, pressurization.
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| CN201310134630.3A CN103173256B (en) | 2013-04-18 | 2013-04-18 | Natural gas multi-tower external cycle anaerobic regeneration dewatering method |
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| CN103173256B CN103173256B (en) | 2014-06-25 |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103483150A (en) * | 2013-08-31 | 2014-01-01 | 安徽淮化股份有限公司 | Method and device for producing and synthesizing ethylene glycol by using coal as raw material |
| CN103642552A (en) * | 2013-12-25 | 2014-03-19 | 新地能源工程技术有限公司 | Heavy hydrocarbon removing process and device of natural gas |
| CN104368221A (en) * | 2014-11-14 | 2015-02-25 | 杰瑞石油天然气工程有限公司 | Device for dewatering and dealkylating methane-rich gas |
| CN105251321A (en) * | 2015-11-13 | 2016-01-20 | 北京中科瑞奥能源科技股份有限公司 | Dehydration method of coalbed methane and dehydration system |
| CN107961649A (en) * | 2017-11-30 | 2018-04-27 | 南通星球石墨设备有限公司 | A kind of HCl gas-drying systems |
| CN108048146A (en) * | 2017-11-09 | 2018-05-18 | 无锡联合超滤净化设备科技有限公司 | The regenerated high-pressure natural gas drying process of alternating temperature transformation closed cycle |
| CN109603421A (en) * | 2018-11-06 | 2019-04-12 | 杨皓 | A kind of activation method of dechlorination pressure-variable adsorption carbon molecular sieve |
| CN109603420A (en) * | 2018-11-06 | 2019-04-12 | 杨皓 | A kind of activation method of decarburization pressure-swing absorber silica gel |
| CN112705018A (en) * | 2020-12-10 | 2021-04-27 | 西南化工研究设计院有限公司 | Efficient temperature swing adsorption gas drying method |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108048146A (en) * | 2017-11-09 | 2018-05-18 | 无锡联合超滤净化设备科技有限公司 | The regenerated high-pressure natural gas drying process of alternating temperature transformation closed cycle |
| CN107961649A (en) * | 2017-11-30 | 2018-04-27 | 南通星球石墨设备有限公司 | A kind of HCl gas-drying systems |
| CN109603421A (en) * | 2018-11-06 | 2019-04-12 | 杨皓 | A kind of activation method of dechlorination pressure-variable adsorption carbon molecular sieve |
| CN109603420A (en) * | 2018-11-06 | 2019-04-12 | 杨皓 | A kind of activation method of decarburization pressure-swing absorber silica gel |
| CN112705018A (en) * | 2020-12-10 | 2021-04-27 | 西南化工研究设计院有限公司 | Efficient temperature swing adsorption gas drying method |
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