CN202297536U - Water and heavy hydrocarbon removing device for producing liquefied natural gas (LNG) by using methane-rich mixed gas - Google Patents
Water and heavy hydrocarbon removing device for producing liquefied natural gas (LNG) by using methane-rich mixed gas Download PDFInfo
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- CN202297536U CN202297536U CN 201120367298 CN201120367298U CN202297536U CN 202297536 U CN202297536 U CN 202297536U CN 201120367298 CN201120367298 CN 201120367298 CN 201120367298 U CN201120367298 U CN 201120367298U CN 202297536 U CN202297536 U CN 202297536U
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Abstract
The utility model relates to a water and heavy hydrocarbon removing device for producing liquefied natural gas (LNG) by using methane-rich mixed gas. The device comprises a first drying tower (T1), a second drying tower (T2), a third drying tower (T3) (namely an auxiliary drying tower), a heater (E1), a gas-liquid separator (T4) and a cooler (E2), wherein the first drying tower and the second drying tower are involved in the drying process and the regeneration process alternately. By the device, the deacidified methane-rich mixed gas is divided into two parts, one part is subjected to the drying process, the other part is subjected to the regeneration process, the methane-rich mixed gas subjected to the drying process is dried, water and heavy hydrocarbon in the gas are removed in an adsorbent composite bed of each drying tower simultaneously, the water is removed until the atmospheric dew point is less than or equal to -76 DEG C, and a heavy hydrocarbon component with more than 6 carbon atoms is removed until the content is less than or equal to 217ppm; and the methane-rich gas subjected to the regeneration process is taken as regeneration gas of the regeneration process of each drying tower, and the regeneration gas is returned to process gas of a system after being subjected to the regeneration process. The device has a good purification effect; and compared with the conventional process device, the device has the advantages that: the investment cost of equipment and the subsequent energy consumption of the system are reduced, the utilization rate of raw materials is improved, and each operation index is clearer and more easily controlled.
Description
Technical field
The utility model belongs to the front end purification treatment technology of methane-rich gas low-temperature liquefaction, is specifically related to from the mixed gas that is rich in methane, produce the dehydration de-heavy hydrocarbon apparatus of natural gas liquids.
Background technology
Under the pressure of environmental protection and energy cost pressure, Sweet natural gas promotes at social every field proportion as primary energy source just gradually, and its market demand also just increases sharply.The defeated method of supplying of traditional pipe still is a main flow; But limited by material condition and user distribution; There is quite a few resource can't carry out pipe long-distance and carries, need to select the mode of liquefaction, change methane into liquid and adopt again flexibly that mode of transport is sent to user terminal with it.Natural gas liquids (LNG) volume has only with 1/625 of amount gas volume, can reduce after the liquefaction and store and transportation cost, and can improve the combustion value of unit volume.
For the industrialized unit that from the mixed gas that is rich in methane, obtains natural gas liquids (LNG); Before gas mixture carries out cryogenic liquefying all need with wherein contained acid gas components, water and high-carbon hydrocarbon (>=C6) etc. be removed to the required precision of liquefaction, could guarantee liquefying separation process and device security steady running.According to the domestic a few cover LNG device running conditions that put into operation; The purification part of the front end gas mixture acid gas that adopt remove the unit more; Dry absorbing unit and take off heavy hydrocarbon unit etc. and progressively remove impurity composition; The shortcoming of this situation is that its facility investment expense is higher, and its system energy consumption is also higher under the nominal situation.
The utility model content
In view of the above problems, a purpose of the utility model provides a kind of dehydration de-heavy hydrocarbon apparatus that is used for producing from the mixed gas that is rich in methane natural gas liquids, and this device comprises:
First drying tower and second drying tower, the two alternately is in drying process and regenerative process first drying tower and second drying tower,
The 3rd drying tower (that is, the drying aid tower),
Well heater,
Gas-liquid separator and
Water cooler,
Each drying tower has one or two or a plurality of sorbent material composite bed, 3-20 bed for example, and 4-18 bed, 5-16 bed, 6-14 bed or 8-12 bed,
The transfer lime of the gas that is rich in methane after the depickling (virgin gas or process gas) is divided into two branch roads i.e. first branch road and second branch road, and first valve (being regulating valve) wherein is set on first branch road; After first valve, divide three the tunnel to lead to liquefaction system via ingress pipe (ingress pipe when referring to that this tower is in drying process), first drying tower and the 3rd valve of second valve, first drying tower respectively again; Ingress pipe, second drying tower and the 5th valve via the 4th valve, second drying tower lead to liquefaction system, and are connected to the derivation port of water cooler via the ingress pipe of the delivery line of optional valve (not shown), gas-liquid separator, gas-liquid separator, gas-liquid separator; Above-mentioned second branch road is connected to the ingress pipe of water cooler respectively via the tenth valve and the 11 valve with via the 12 valve and the 13 valve; Between first drying tower and the 3rd valve, draw arm and between second drying tower and the 5th valve, draw arm; These two arms are respectively via converging an end (port or lower port) that is connected to well heater after the 8th valve and the 9th valve; The other end of well heater is connected to an end (port or lower port) of the 3rd drying tower, the other end of drying tower via pipe connection on the pipeline between the 12 valve and the 13 valve; Between first drying tower and second valve, draw arm and between second drying tower and the 4th valve, draw arm, these two arms are connected on the pipeline between the tenth valve and the 11 valve via converging after the 6th valve and the 7th valve respectively.
Control the carrying out of each process by means of each valve.
Each sorbent material composite bed of each drying tower loads one or both or the multiple sorbent material that is selected from 3A or 4A molecular sieve, activated alumina, gac and the water-fast silica gel independently; Wherein 3A molecular sieve, 4A molecular sieve or activated alumina are as dehydrated adsorbent, and gac or water-fast silica gel are as taking off the heavy hydrocarbon sorbent material.
Preferably; Each drying tower has two sorbent material composite beds that load dehydrated adsorbent respectively and take off the heavy hydrocarbon sorbent material, preferred three, four, five, six, seven, eight, nine, ten, 11,12,13,14,15 or 16 beds at least.
The compound de-heavy hydrocarbon apparatus of drying and dehydrating of from the mixed gas that is rich in methane, producing natural gas liquids of the utility model; Make the utility model simpler and reach good decontamination effect improving than common process device; And reduced the scavenging process energy consumption, and each unit operation index is more clear, be prone to control.
The compound de-heavy hydrocarbon apparatus of drying and dehydrating of from the mixed gas that is rich in methane, producing natural gas liquids that the utility model provides adopts the composite bed heavy hydrocarbon that dewaters simultaneously; Methane-riched gas mixture after depickling is handled through the isobaric drying treatment of three towers, adopts the sorbent material composite bed to remove moisture and heavy hydrocarbon in the gas simultaneously; Moisture removal to dew points at normal pressure≤-76 ℃, the above heavy hydrocarbon component of C6 are removed to≤and 217ppm (preferred≤200ppm, more preferably≤100ppm; Further preferably≤50ppm; Further preferably≤30ppm, more further preferably≤20ppm, most preferably≤10ppm); With the part methane-rich gas as regeneration gas, accomplish regeneration step after, in this part resurgent gases retrieval system process gas.
The advantage of the utility model:
1, utilizes composite bed to remove moisture and heavy hydrocarbon simultaneously, reduced facility investment expense and later stage system energy consumption.
2, adopt isobaric drying and dehydrating to take off heavy hydrocarbon, the almost operation under same pressure of the absorption of drying tower, heating and cooling process, the life-span of having improved program-controlled valve.
3, resurgent gases does not need independent pure gas but adopting process gas, and flow process is simple, owing to be an independently system, the start-stop car is convenient simultaneously.
4, adopt three-column process flow, can be during cold blowing with the transfer of heat of the drying tower that has heated to next tower, system energy consumption is low.
Description of drawings
Fig. 1 is that composite dewatering takes off the heavy hydrocarbon process device figure.
Embodiment
With reference to accompanying drawing 1, the dehydration de-heavy hydrocarbon apparatus of from the mixed gas that is rich in methane, producing natural gas liquids of the utility model comprises:
First drying tower (T1) and second drying tower (T2), the two alternately is in drying process and regenerative process first drying tower and second drying tower,
The 3rd drying tower (T3) (that is, the drying aid tower),
Well heater (E1),
Gas-liquid separator (T4) and
Water cooler (E2),
Each drying tower has one or two or a plurality of sorbent material composite bed, 3-20 bed for example, and 4-18 bed, 5-16 bed, 6-14 bed or 8-12 bed,
The transfer lime of the gas that is rich in methane after the depickling (virgin gas or process gas) is divided into two branch roads i.e. first branch road and second branch road, and first valve V1 wherein is set on first branch road; After first valve V1, divide three the tunnel to lead to liquefaction system via ingress pipe (ingress pipe when referring to that this tower is in drying process), the first drying tower T1 and the 3rd valve V3 of second valve V2, the first drying tower T1 respectively again; Ingress pipe, the second drying tower T2 and the 5th valve V5 via the 4th valve V4, the second drying tower T2 lead to liquefaction system, and are connected to the derivation port of water cooler E2 via the ingress pipe of the delivery line of optional valve (not shown), gas-liquid separator T4, gas-liquid separator T4, gas-liquid separator T4; Above-mentioned second branch road is connected to the ingress pipe of water cooler E2 respectively via the tenth valve V10 and the 11 valve V11 with via the 12 valve V12 and the 13 valve V13; Between first drying tower T1 and the 3rd valve V3, draw arm and between second drying tower T2 and the 5th valve V5, draw arm; These two arms are respectively via converging an end (port or lower port) that is connected to well heater E1 after the 8th valve V8 and the 9th valve V9; The other end of well heater is connected to the end (port or lower port) of the 3rd drying tower T3, the other end of drying tower T3 via pipe connection on the pipeline between the 12 valve V12 and the 13 the valve V13; Between first drying tower T1 and second valve V2, draw arm and between second drying tower (T2) and the 4th valve (V4), draw arm, these two arms are connected on the pipeline between the tenth valve V10 and the 11 valve V11 via converging after the 6th valve V6 and the 7th the valve V7 respectively.
Use the compound heavy hydrocarbon technology of taking off of drying and dehydrating of from the mixed gas that is rich in methane, producing natural gas liquids of this device to comprise: to adopt the sorbent material composite bed to take off heavy hydrocarbon; Methane-riched gas mixture after depickling is handled; Through the isobaric drying treatment of three towers, adopt composite bed to remove moisture and heavy hydrocarbon in the gas simultaneously, moisture removal to dew points at normal pressure≤-76 ℃; The above heavy hydrocarbon component of C6 and C6 is removed to≤and 217ppm is (preferred≤200ppm; More preferably≤100ppm, further preferably≤50ppm, most preferably≤10ppm); With the part methane-rich gas as regeneration gas, accomplish regeneration step after, in this part resurgent gases retrieval system process gas.
With reference to accompanying drawing 1, explaining that drying and dehydrating is compound takes off the heavy hydrocarbon technical process:
The compound device that takes off heavy hydrocarbon of drying and dehydrating is made up of three drying tower T1, T2 and T3, a well heater E1, a water cooler E2, a gas-liquid separator T4; Two is dryer tower T1, T2 in three drying towers, a drying aid tower T3; Dryer tower drying and regeneration hocket; Regeneration divides heating and cooling two steps; Product gas dew points at normal pressure≤-76 after dry composite is taken off heavy hydrocarbon ℃, the above heavy hydrocarbon component of C6 and C6 are removed to≤and 217ppm (preferred≤200ppm, more preferably≤100ppm, further preferred≤50ppm, most preferably≤10ppm).
The compound heavy hydrocarbon technology of taking off of isobaric drying and dehydrating, resurgent gases adopting process gas returns process gas after regenerative process, compare traditional technology, has reduced the process gas loss, has improved the liquefied fraction of gas; The compound heavy hydrocarbon unit that takes off of drying and dehydrating adopts the sorbent material composite bed, removes moisture and heavy hydrocarbon simultaneously, has reduced facility investment expense and later stage system energy consumption; The almost operation under same pressure of the absorption of its drying tower, heating and cooling process has improved equipment life.
Be adsorbed as example with drying tower T1, its operating process is described at present:
The methane rich gas mixture that removes behind the sour gas at first is divided into two-way, and the flow of two-way air-flow is regulated through regulating valve V1: the one tunnel as resurgent gases, and one the tunnel as mainstream gas.Wherein mainstream gas is directly removed drying tower T1 through valve V2, and siccative that loads among the drying tower T1 and heavy hydrocarbon remove agent moisture in the gas and heavy hydrocarbon are absorbed, and gas is accomplished to purify through valve V3 and gone postorder liquefaction operation.
Another drying tower T2 is in regenerative process, and the regenerative process of drying tower T2 comprises heating and two steps of cold blowing:
In the thermal regeneration step; Resurgent gases is successively through valve V12, drying tower T3, well heater E1, valve V9, drying tower T2, valve V7, valve V11, water cooler E2, gas-liquid separator T4; Converge with the process gas that is about to enter into the drying tower T1 that is in adsorption process again; Get into the drying tower T1 that is in adsorption process through valve V2, accomplish heat-processed drying tower T2.
Resurgent gases is taken from process gas, does not need external any carrier gas in the thermal regeneration process, and resurgent gases is returned process gas after regeneration step.When drying tower T2 was heated, regeneration gas cooled off predrying tower T3, drying tower T3 internal adsorption agent and material accumulation of heat is taken away got into well heater E1 again, reduced the required energy expenditure of thermal regeneration.Resurgent gases is before entering drying tower T2, and super-dry tower T3 is predrying, and the moisture content in the resurgent gases is (moisture content in the virgin gas has reduced 80-99% usually) seldom, reduces the drying load of drying tower T2.
In the cold blowing step; Resurgent gases is successively through valve V10, valve V7, drying tower T2, valve V9, well heater E1, drying tower T3, valve V13, water cooler E2, gas-liquid separator T4; Converge with the process gas that is about to enter into the drying tower T1 that is in adsorption process again; Be among the drying tower T1 of adsorption process through valve V2 entering, accomplish process of cooling drying tower T2.
Equally, resurgent gases is taken from process gas, does not need external any carrier gas in the thermal regeneration process, and resurgent gases is returned process gas after regeneration step.Drying tower T2 is being carried out refrigerative simultaneously, regeneration gas heats predrying tower T3, drying tower T2 internal adsorption agent and material accumulation of heat is taken away got into well heater E1 again, reduces the required energy expenditure of thermal regeneration.Resurgent gases is before entering drying tower T3, and super-dry tower T2 is predrying, and the moisture content in the resurgent gases seldom reduces the drying load of drying tower T3.
Drying tower T2 waits for getting into adsorption operations next time through after the above-mentioned heating and cooling process.
The regenerative process of the regenerative process of drying tower T1 and drying tower T2 is just the same, just needs the valve numbering of action different.Two drying towers replace absorption regeneration, realize operate continuously processing gas.
The composite bed of each drying tower can load in 3A or the sorbent materials such as 4A molecular sieve, activated alumina, gac and silica gel one or both or multiple.
Then, T2 is adsorbed as example with drying tower, and its operating process is described:
The gas mixture that removes the methane rich behind the sour gas at first is divided into two-way, and the flow of two-way air-flow is regulated through regulating valve V1: the one tunnel as resurgent gases, and one the tunnel as mainstream gas.Wherein mainstream gas is directly removed drying tower T2 through valve V4, and siccative that loads among the drying tower T2 and heavy hydrocarbon remove agent moisture in the gas and heavy hydrocarbon are absorbed, and gas is accomplished to purify through valve V5 and gone postorder liquefaction operation.
Another drying tower T1 is in regenerative process, and the regenerative process of drying tower T1 comprises heating and two steps of cold blowing:
In the thermal regeneration step, resurgent gases is successively through valve V12, drying tower T3, well heater E1, valve V
8, drying tower T1, valve V6, valve V11, water cooler E2, gas-liquid separator T4; Converge with the process gas that is about to enter into the drying tower T2 that is in adsorption process again; Get into the drying tower T2 that is in adsorption process through valve V4, accomplish heat-processed drying tower T1.
Resurgent gases is taken from process gas, does not need external any carrier gas in the thermal regeneration process, and resurgent gases is returned process gas after regeneration step.When drying tower T1 was heated, regeneration gas cooled off predrying tower T3, drying tower T3 internal adsorption agent and material accumulation of heat is taken away got into well heater E1 again, reduced the required energy expenditure of thermal regeneration.Resurgent gases is before entering drying tower T1, and it is predrying to have passed through predrying tower T3, and the moisture content in the resurgent gases seldom reduces the drying load of drying tower T1.
In the cold blowing step; Resurgent gases is successively through valve V10, valve V6, drying tower T1, valve V8, well heater E1, drying tower T3, valve V13, water cooler E2, gas-liquid separator T4; Converge with the process gas that is about to enter into the drying tower T2 that is in adsorption process again; Get into the drying tower T2 that is in adsorption process through valve V4, accomplish process of cooling drying tower T1.
Equally, resurgent gases is taken from process gas, does not need external any carrier gas in the thermal regeneration process, and resurgent gases is returned process gas after regeneration step.Drying tower T1 is being carried out refrigerative simultaneously, regeneration gas heats predrying tower T3, drying tower T1 internal adsorption agent and material accumulation of heat is taken away got into well heater E1 again, reduces the required energy expenditure of thermal regeneration.Resurgent gases is before entering drying tower T3, and super-dry tower T1 is predrying, and the moisture content in the resurgent gases seldom reduces the drying load of drying tower T3.
Drying tower T1 waits for getting into adsorption operations next time through after the above-mentioned heating and cooling process.
Each composite bed of each drying tower can load independently in 3A or the sorbent materials such as 4A molecular sieve, activated alumina, gac and water-fast silica gel one or both or multiple.Preferably; Each drying tower has two sorbent material composite beds that load dehydrated adsorbent respectively and take off the heavy hydrocarbon sorbent material, preferred three, four, five, six, seven, eight, nine, ten, 11,12,13,14,15 or 16 at least.
Claims (2)
1. dehydration de-heavy hydrocarbon apparatus of from the mixed gas that is rich in methane, producing natural gas liquids is characterized in that this device comprises:
First drying tower (T1) and second drying tower (T2), the two alternately is in drying process and regenerative process first drying tower and second drying tower,
The 3rd drying tower (T3),
Well heater (E1),
Gas-liquid separator (T4) and
Water cooler (E2),
Each drying tower has one or two or a plurality of sorbent material composite bed,
The transfer of gas pipe that is rich in methane after the depickling is divided into two branch roads i.e. first branch road and second branch road, and first valve (V1) wherein is set on first branch road; Divide three the tunnel to lead to liquefaction system via ingress pipe, the first drying tower T1 and the 3rd valve (V3) of second valve (V2), first drying tower (T1) respectively afterwards again at first valve (V1); Ingress pipe, second drying tower (T2) and the 5th valve (V5) via the 4th valve (V4), second drying tower (T2) lead to liquefaction system, and are connected to the derivation port of water cooler (E2) via the ingress pipe of the delivery line of optional valve, gas-liquid separator (T4), gas-liquid separator (T4), gas-liquid separator (T4); Above-mentioned second branch road is connected to the ingress pipe of water cooler (E2) respectively via the tenth valve (V10) and the 11 valve (V11) with via the 12 valve (V12) and the 13 valve (V13); Draw arm between first drying tower (T1) and the 3rd valve (V3) and between second drying tower (T2) and the 5th valve (V5), drawing arm; These two arms converge an end that is connected to well heater (E1) via the 8th valve (V8) and the 9th valve (V9) respectively afterwards; The other end of well heater (E1) is connected to an end of the 3rd drying tower (T3), the other end of drying tower (T3) via pipe connection on the pipeline between the 12 valve (V12) and the 13 valve (V13); Drawing arm between first drying tower (T1) and second valve (V2) and between second drying tower (T2) and the 4th valve (V4), drawing arm, these two arms converge afterwards via the 6th valve (V6) and the 7th valve (V7) respectively and are connected on the pipeline between the tenth valve (V10) and the 11 valve (V11).
2. the dehydration de-heavy hydrocarbon apparatus of from the mixed gas that is rich in methane, producing natural gas liquids according to claim 1; It is characterized in that: each sorbent material composite bed of each drying tower loads one or both or the multiple sorbent material that is selected from 3A or 4A molecular sieve, activated alumina, gac and the water-fast silica gel independently; Wherein 3A molecular sieve, 4A molecular sieve or activated alumina are as dehydrated adsorbent, and gac or water-fast silica gel are as taking off the heavy hydrocarbon sorbent material.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120367298 CN202297536U (en) | 2011-09-30 | 2011-09-30 | Water and heavy hydrocarbon removing device for producing liquefied natural gas (LNG) by using methane-rich mixed gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201120367298 CN202297536U (en) | 2011-09-30 | 2011-09-30 | Water and heavy hydrocarbon removing device for producing liquefied natural gas (LNG) by using methane-rich mixed gas |
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| Publication Number | Publication Date |
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| CN202297536U true CN202297536U (en) | 2012-07-04 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201120367298 Withdrawn - After Issue CN202297536U (en) | 2011-09-30 | 2011-09-30 | Water and heavy hydrocarbon removing device for producing liquefied natural gas (LNG) by using methane-rich mixed gas |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013044732A1 (en) * | 2011-09-30 | 2013-04-04 | 新地能源工程技术有限公司 | Water removal and heavy-hydrocarbon removal process in liquefied natural gas production from mixed gas rich in methane |
| CN115382362A (en) * | 2022-09-19 | 2022-11-25 | 清华四川能源互联网研究院 | Hydrogen drying system |
-
2011
- 2011-09-30 CN CN 201120367298 patent/CN202297536U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2013044732A1 (en) * | 2011-09-30 | 2013-04-04 | 新地能源工程技术有限公司 | Water removal and heavy-hydrocarbon removal process in liquefied natural gas production from mixed gas rich in methane |
| CN103031168A (en) * | 2011-09-30 | 2013-04-10 | 新地能源工程技术有限公司 | Dehydration and de-heavy hydrocarbon technology for production of liquefied natural gas from methane-rich mixed gas |
| CN103031168B (en) * | 2011-09-30 | 2014-10-15 | 新地能源工程技术有限公司 | Dehydration and de-heavy hydrocarbon technology for production of liquefied natural gas from methane-rich mixed gas |
| CN115382362A (en) * | 2022-09-19 | 2022-11-25 | 清华四川能源互联网研究院 | Hydrogen drying system |
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| AV01 | Patent right actively abandoned |
Granted publication date: 20120704 Effective date of abandoning: 20141015 |
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