CN101126041A - Cascade connection method for preparing liquefied natural gas - Google Patents
Cascade connection method for preparing liquefied natural gas Download PDFInfo
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Abstract
The invention discloses a cascading style preparation method of liquefied natural gas, comprising the following steps: (1) pretreatment: that carbon dioxide, sulfureted hydrogen and water contain in raw gas are removed; (2) raw gas primary cooling treatment: the raw gas passes through a first multi-level heat exchanging and a separating device of a first refrigeration cycle system to finish the primary cooling treatment; (3) raw gas secondary cooling treatment: the raw gas is sent by a second multi-level heat exchanging and the separating device of a second refrigeration cycle system in sequence to finish the secondary cooling treatment; (4) raw gas tertiary cooling treatment: the raw gas is sent by a third multi-level heat exchanging and the separating device of a third refrigeration cycle system in sequence to finish the tertiary cooling treatment; (5) finished product making: the raw gas is made to expand and then the temperature of the raw material is lowered to -162 DEG C to -163 DEG C, thereafter a combination of liquefied nature gas and gaseity nature gas is made; the combination passes through a gas-liquid separating tower to make the final product of the liquefied natural gas. The invention has the advantages that beneficial by-products can be obtained in the process of natural gas liquefaction.
Description
Technical field
The invention belongs to the technical field of producing the preparation natural gas liquids, be specifically related to a kind of method for preparing natural gas liquids.
Background technology
When the volume of natural gas liquids (LNG) is gaseous state 1/600, the efficiency of storage height, transportation flexibly, be used as aspects such as city transmission ﹠ distribution gas System Expansion, peak regulation, compare the advantage of having more with other modes such as underground natural gas storage, gas storage holders, and have that construction investment is little, construction period weak point, instant effect, be subjected to advantages such as external influence factors is little.In addition, natural gas liquids also can be used as the fine vehicle fuel, compares with vehicle fuel, and natural gas liquids has advantages such as octane value height, anti-knocking property are good, burning is complete, exhaust pollution is few, engine life is long, running cost is low; (CNG) compares with compressed natural gas, and natural gas liquids has then that efficiency of storage is higher, continual mileage is long, storage bottle pressure is low, building a station is not subjected to the advantages such as restriction of gas transmission pipeline net work.
The main component of Sweet natural gas is a methane, and it is different with a spot of propane, butane in the Sweet natural gas, and can not pressurize at normal temperatures becomes liquid, can only it be liquefied with low temperature, refrigerating method.In the liquefying plant of existing Sweet natural gas, large-scale plant mainly adopts the natural gas liquefaction device of cascade refrigeration and adopts hybrid refrigeration machine refrigerating natural gas liquefaction device, these two kinds of apparatus features are that output is big, energy consumption is lower, but unit is huge, the equipment complexity, operating maintenance is all inconvenient, middle-size and small-size natural gas liquefaction device mainly contains the pressure reduction that utilizes Sweet natural gas main pipe line and small transfer line, adopt the liquefying plant of decompressor with the Sweet natural gas swell refrigeration, this apparatus structure is simple, and owing to utilized the pressure of Sweet natural gas itself, so need consumed power hardly, but the production fluid rate is lower, has only about 10% usually.
The liquefaction of Sweet natural gas belongs to deep refrigeration, does not reach the purpose of liquefaction by one section refrigeration.The method of conventional lng is to adopt syllogic to lower the temperature to obtain very low temperature, but mostly the purpose of the method for traditional natural gas liquids is merely not have to make full use of multistage refrigerating process and to obtain useful byproduct in order to obtain natural gas liquids.
Summary of the invention
The purpose of this invention is to provide the method that a kind of a kind of compact cascade type that also can obtain useful byproduct in making the process of natural gas liquefaction prepares natural gas liquids.
The technical scheme that realizes the object of the invention is: a kind of compact cascade type prepares the method for natural gas liquids, has following steps:
1. pre-treatment; Remove carbonic acid gas, hydrogen sulfide and water in the unstripped gas;
2. the one-level cooling is handled; Make pretreated unstripped gas through first multi-stage heat exchanger and tripping device in first cooling cycle system, handle pretreated unstripped gas is carried out the one-level cooling, make unstripped gas be cooled to subzero 35～subzero 41 ℃, air pressure is 3.8MPa to 4.1MPa;
3. the secondary cooling is handled; Make the unstripped gas that passes through after 2. step is handled successively through second multi-stage heat exchanger and tripping device in second cooling cycle system, so that being carried out the secondary cooling, handles the unstripped gas after 2. handling through step, make unstripped gas be cooled to subzero 95～subzero 100 ℃, air pressure is 3.8MPa to 4.1MPa;
4. three grades of coolings are handled; Make the unstripped gas that passes through after 3. step is handled successively through the 3rd multi-stage heat exchanger and tripping device in the 3rd cooling cycle system, handle the unstripped gas of 3. handling through step is carried out three grades of coolings, make unstripped gas be cooled to subzero 155～subzero 161 ℃, air pressure is 3.8MPa to 4.1MPa;
5. the throttling step-down is handled: the unstripped gas after 4. the process step is handled is expanded, make unstripped gas be cooled to subzero 162 ℃～163 ℃ and become the mixture that contains natural gas liquids and gaseous natural gas, make material through the gas-liquid separation tower then, make liquify natural gas separate, thereby obtain the finished product natural gas liquids with gaseous natural gas.
Carrying out pretreated purpose mainly is to remove carbonic acid gas, hydrogen sulfide and water, make the dew point of unstripped gas reach subzero 70 ℃, in order to avoid when the liquefaction of gasiform unstripped gas was the natural gas liquids of liquid state, too much carbonic acid gas and water formed assimilate and occluding device and pipeline.
Above-mentioned steps 1. in, be that 3.5MPa to 6MPa and temperature are the pre-treatment that under 5 ℃ to 40 ℃ the condition unstripped gas is removed carbonic acid gas, hydrogen sulfide and water at air pressure.
The pretreated preferred version that above-mentioned steps removes carbonic acid gas, hydrogen sulfide and water in 1. is that to make unstripped gas be that 4MPa to 5MPa and temperature are under 10 ℃ to 25 ℃ the condition at air pressure, successively first absorption tower by the ethanolamine solutions that is used to remove carbonic acid gas and hydrogen sulfide is housed, second absorption tower of ethylene glycol and aluminium glue is housed and the packing tower of the adsorbent of molecular sieve that is used to remove moisture is housed.
Above-mentioned steps 2. in, described first multi-stage heat exchanger and tripping device comprise successively first interchanger, the first gas-liquid separation tower, second interchanger and the second gas-liquid separation tower of polyphone; Refrigeration agent in described first cooling cycle system is the mixture of propane or propane and butane.
Making pretreated unstripped gas is subzero 30 ℃～subzero 35 ℃ through the temperature of first interchanger, is preferably subzero 32 ℃～subzero 34 ℃, will be from the first gas-liquid separation tower isolated liquid material as gasoline or diesel oil; Temperature through second interchanger is subzero 40 ℃～subzero 41 ℃, is preferably subzero 40 ℃, will be from the second gas-liquid separation tower isolated liquid material as the refrigeration agent in first refrigeration cycle.
Above-mentioned steps 3. in, described second multi-stage heat exchanger and tripping device comprise successively the 3rd interchanger, the 3rd gas-liquid separation tower, the 4th interchanger, the 4th gas-liquid separation tower, the 5th interchanger and the 5th gas-liquid separation tower of polyphone; Refrigeration agent in described second cooling cycle system is an ethene.
Above-mentioned steps 3. in, making unstripped gas is subzero 65 ℃～subzero 70 ℃ through the temperature of the 3rd interchanger, is preferably subzero 68 ℃～subzero 70 ℃; Temperature through the 4th interchanger is subzero 80 ℃～subzero 85 ℃, is preferably subzero 84 ℃～subzero 85 ℃; Temperature through the 5th interchanger is subzero 95～subzero 100 ℃, is preferably subzero 98 ℃～subzero 100 ℃, will be from the 5th gas-liquid separation tower isolated liquid material as the refrigeration agent in second cooling cycle system.
Above-mentioned steps 4. in, described the 3rd multi-stage heat exchanger and tripping device comprise successively the 6th interchanger, the 6th gas-liquid separation tower, the 7th interchanger, the 7th gas-liquid separation tower, the 8th interchanger and the 8th gas-liquid separation tower of polyphone; Refrigeration agent in described the 3rd cooling cycle system is methane or natural gas liquids.
Above-mentioned steps 4. in, making unstripped gas is subzero 120 ℃～subzero 130 ℃ through the temperature of the 6th interchanger, is preferably subzero 128 ℃～subzero 130 ℃; Temperature through the 7th interchanger is subzero 140 ℃～subzero 145 ℃, is preferably subzero 144 ℃～subzero 145 ℃; Temperature through the 8th interchanger is subzero 155 ℃～subzero 161 ℃, is preferably subzero 160 ℃～subzero 161 ℃.
Above-mentioned steps 5. in, make through the unstripped gas of step after 4. handling by the throttling tower, make the air pressure of unstripped gas drop to 0.09MPa to 0.11MPa; Prepared natural gas liquids can be used as refrigeration agent in the 3rd cooling cycle system.
The present invention has positive effect: (1) compact cascade type of the present invention prepares the method for natural gas liquids, by a plurality of interchanger are set, make the gasiform unstripped gas experience the multi-stage type chilling process, and be provided with the gas-liquid separation tower respectively at suitable temperature section, thereby obtain the by product of multiple beneficial, have favorable economic benefit.(2) in the inventive method, the refrigeration agent in each grade refrigeration cycle can be single pure material, also can be the meticulous mix refrigerant of preparation, and is applied widely; When selecting single pure material for use, no proportioning problem, and because Refrigeration Technique is comparatively ripe, whole process flow is comparatively stable, the reliability height.(3) energy consumption of the inventive method is lower, and the part by product that obtains can add in the recycle system separately directly as refrigeration agent, thereby has reduced the refrigeration cost.
Description of drawings
Fig. 1 is the process flow sheet of the inventive method.
Be labeled as shown in the accompanying drawing: first cooling cycle system 1, condenser 11, refrigeration agent 12, throttling valve 13, throttling valve 14;
First multi-stage heat exchanger and tripping device 2, the first interchanger 21, the first gas-liquid separation towers 22, the second interchanger 23, the second gas-liquid separation towers 24;
Second cooling cycle system, 3, the second multi-stage heat exchangers and tripping device 4, the three interchanger 41, the three gas-liquid separation towers 42, the four interchanger 43, the four gas-liquid separation towers 44, the five interchanger 45, the five gas-liquid separation towers 46;
The 3rd cooling cycle system 5, the three multi-stage heat exchangers and tripping device 6, the six interchanger 61, the six gas-liquid separation towers 62, the seven interchanger 63, the seven gas-liquid separation towers 64, the eight interchanger 65, the eight gas-liquid separation towers 66; Throttling tower 7, gas-liquid separation tower 8; 91, the second absorption towers 92, pretreatment system 9, the first absorption towers, packing tower 93.
Embodiment
(embodiment 1)
See Fig. 1, present embodiment is the method that a kind of compact cascade type prepares natural gas liquids, has following steps:
1. pre-treatment; Unstripped gas in the present embodiment is the oil field Sweet natural gas from pipe-line transportation, and its air pressure is 3.24MPa, and temperature is 37.8 ℃; The component molar fraction is 83% methane, 10%C
2+ above alkane, 7% nitrogen.Unstripped gas is compressed to 4.1MPa through centrifugal compressor earlier, cool off with seawater, make its temperature reduce to 20 ℃, make then unstripped gas successively first absorption tower 91 by the ethanolamine solutions that is used to remove carbonic acid gas and hydrogen sulfide is housed, second absorption tower 92 of ethylene glycol and aluminium glue is housed and the packing tower 93 of the adsorbent of molecular sieve that is used to remove moisture is housed.
In other embodiments, when the compressed machine of unstripped gas compresses, make its air pressure reach 3.8～4.1MPa and be advisable, because low excessively air pressure will cause the insufficient pressure in the subsequent disposal, too high pressure is then very high to equipment requirements, causes the cost costliness.
When with seawater the unstripped gas level being cooled off in other embodiments, making its temperature is 5 ℃ to 40 ℃, is preferably 10 ℃ to 25 ℃.
The mass concentration of the used ethanolamine solutions of present embodiment is 10%, can select 8～12% ethanolamine solutions among other embodiment for use.
The surface-area of the used adsorbent of molecular sieve of present embodiment is 800m
2/ g, bore dia are 0.42nm, and pore volume is 0.27cm
3/ g.Can select surface-area in other embodiments for use is 700～900m
2/ g, bore dia are 0.38～0.45nm, and pore volume is 0.25～0.35cm
3The adsorbent of molecular sieve of/g.
Air pressure through pretreated unstripped gas is 4.0MPa, and its dew-point temperature is reduced to subzero 73 ℃.
2. the one-level cooling is handled; Make pretreated unstripped gas through first multi-stage heat exchanger in first cooling cycle system 1 and tripping device 2, handle pretreated unstripped gas is carried out the one-level cooling;
First step cooling cycle system 1 comprises condenser 11, refrigeration agent 12, first interchanger 21, second interchanger 23, throttling valve 13 and throttling valve 14.1 refrigeration agent is a propane in described first cooling cycle system; In other embodiments, also can adopt the mixture of propane and butane.
First multi-stage heat exchanger and tripping device 2 comprise first interchanger 21, the first gas-liquid separation tower 22, second interchanger 23 and the second gas-liquid separation tower 24.
By temperature control, making pretreated unstripped gas is subzero 33 ℃ through the temperature of first interchanger 21, will be from the first gas-liquid separation tower 22 isolated liquid material as gasoline or diesel oil; Temperature through second interchanger 23 is subzero 40.5 ℃, isolated liquid material from the second gas-liquid separation tower 24 can be added in first cooling cycle system 1 as the refrigeration agent in first refrigeration cycle, also can otherwise processed be used to produce propane.
The air pressure that separates the unstripped gas that obtains from the second gas-liquid separation tower 24 is 3.9MPa, and temperature is subzero 41 ℃.
3. the secondary cooling is handled; Make the unstripped gas that passes through after 2. step is handled successively through second multi-stage heat exchanger in second cooling cycle system 3 and tripping device 4, handle so that the unstripped gas after 2. handling through step is carried out the secondary cooling;
Second stage cooling cycle system 3 comprises condenser 31, refrigeration agent 32, the 3rd interchanger 41, the 4th interchanger 43, the 5th interchanger 45, throttling valve 33, throttling valve 34 and throttling valve 35.Refrigeration agent in described second cooling cycle system 3 is an ethene, and also can select main component in other embodiments for use is the mix refrigerant of ethene.
Described second multi-stage heat exchanger and tripping device 4 comprise the 3rd interchanger 41, the 3rd gas-liquid separation tower 42, the 4th interchanger 43, the 4th gas-liquid separation tower 44, the 5th interchanger 45 and the 5th gas-liquid separation tower 46 of polyphone successively.
By temperature control, making unstripped gas is subzero 65 ℃～subzero 70 ℃ through the temperature of the 3rd interchanger 41; Temperature through the 4th interchanger 43 is subzero 83 ℃; Temperature through the 5th interchanger 45 is subzero 98 ℃; Liquid material that will sub-argument goes out from the 3rd gas-liquid separation tower 42, the 4th gas-liquid separation tower 44 collects, and otherwise processed is produced the alkene series products to be used for making; Isolated liquid material can be used as refrigeration agent and adds in second cooling cycle system 3 from the 5th gas-liquid separation tower 46, but also otherwise processed is rare to be used to produce third.
The air pressure that separates the unstripped gas that obtains from the 5th gas-liquid separation tower 24 is 3.85MPa, and temperature is subzero 95 ℃～subzero 100 ℃.
4. three grades of coolings are handled; Make the unstripped gas that passes through after 3. step is handled successively through the 3rd multi-stage heat exchanger in the 3rd cooling cycle system 5 and tripping device 6, handle the unstripped gas of 3. handling through step is carried out three grades of coolings;
The 3rd cooling cycle system 5 comprises condenser 51, refrigeration agent 52, the 3rd interchanger 61, the 4th interchanger 63, the 5th interchanger 65, throttling valve 53, throttling valve 54 and throttling valve 55.Refrigeration agent in described the 3rd cooling cycle system 5 is a methane, also can adopt the natural gas liquids that makes with the inventive method in other embodiments.
Described the 3rd multi-stage heat exchanger and tripping device 6 comprise the 6th interchanger 61, the 6th gas-liquid separation tower 62, the 7th interchanger 63, the 7th gas-liquid separation tower 64, the 8th interchanger 65 and the 8th gas-liquid separation tower 66 of polyphone successively.
By temperature control, making unstripped gas is subzero 125 ℃ through the temperature of the 6th interchanger 61; Temperature through the 7th interchanger 63 is subzero 143 ℃; Temperature through the 8th interchanger 65 is subzero 160 ℃.Liquid material that will sub-argument goes out from the 6th gas-liquid separation tower 62, the 7th gas-liquid separation tower 64 and the 8th gas-liquid separation tower 66 collects otherwise processed.
The air pressure of the gaseous state material that comes out from the 8th gas-liquid separation tower 66 is 3.8MPa, and temperature is subzero 155 ℃～subzero 161 ℃.
5. the throttling step-down is handled: make the unstripped gas that passes through after 4. step is handled by throttling tower 7, the cooling so that unstripped gas expands under approximate adiabatic condition, the air pressure of unstripped gas drops to 0.10MPa, temperature is reduced to subzero 162 ℃ and become the mixture that contains natural gas liquids and gaseous natural gas, make material through gas-liquid separation tower 8 then, make liquify natural gas separate, thereby obtain the finished product natural gas liquids with gaseous natural gas.
(embodiment 2)
Present embodiment is substantially the same manner as Example 1, and difference is: step 2. in, by temperature control, making pretreated unstripped gas is subzero 30 ℃ through the temperature of first interchanger 21; Temperature through second interchanger 23 is subzero 40 ℃.Step 3. in, by temperature control, making unstripped gas is subzero 65 ℃ through the temperature of the 3rd interchanger 41; Temperature through the 4th interchanger 43 is subzero 80; Temperature through the 5th interchanger 45 is subzero 95 ℃.Step 4. in, by temperature control, making unstripped gas is subzero 120 ℃ through the temperature of the 6th interchanger 61; Temperature through the 7th interchanger 63 is subzero 140 ℃; Temperature through the 8th interchanger 65 is subzero 155 ℃.Step 5. in, unstripped gas is reduced to subzero 162 ℃ by throttling tower 7 back temperature becomes the mixture that contains natural gas liquids and gaseous natural gas.
(embodiment 3)
Present embodiment is substantially the same manner as Example 1, and difference is: step 2. in, by temperature control, making pretreated unstripped gas is subzero 35 ℃ through the temperature of first interchanger 21; Temperature through second interchanger 23 is subzero 41 ℃.Step 3. in, by temperature control, making unstripped gas is subzero 70 ℃ through the temperature of the 3rd interchanger 41; Temperature through the 4th interchanger 43 is subzero 85 ℃; Temperature through the 5th interchanger 45 is subzero 100 ℃.Step 4. in, by temperature control, making unstripped gas is subzero 130 ℃ through the temperature of the 6th interchanger 61; Temperature through the 7th interchanger 63 is subzero 145 ℃; Temperature through the 8th interchanger 65 is subzero 161 ℃.Step 5. in, unstripped gas is reduced to subzero 163 ℃ by throttling tower 7 back temperature becomes the mixture that contains natural gas liquids and gaseous natural gas.
(embodiment 4)
Present embodiment is substantially the same manner as Example 1, and difference is: step 2. in, by temperature control, making pretreated unstripped gas is subzero 32 ℃ through the temperature of first interchanger 21; Temperature through second interchanger 23 is subzero 40 ℃.Step 3. in, by temperature control, making unstripped gas is subzero 68 ℃ through the temperature of the 3rd interchanger 41; Temperature through the 4th interchanger 43 is subzero 84 ℃; Temperature through the 5th interchanger 45 is subzero 98 ℃.Step 4. in, by temperature control, making unstripped gas is subzero 128 ℃ through the temperature of the 6th interchanger 61; Temperature through the 7th interchanger 63 is subzero 144 ℃; Temperature through the 8th interchanger 65 is subzero 160 ℃.Step 5. in, unstripped gas is reduced to subzero 162 ℃ by throttling tower 7 back temperature becomes the mixture that contains natural gas liquids and gaseous natural gas.
(embodiment 5)
Present embodiment is substantially the same manner as Example 1, and difference is: step 2. in, by temperature control, making pretreated unstripped gas is subzero 34 ℃ through the temperature of first interchanger 21; Temperature through second interchanger 23 is subzero 40 ℃.Step 3. in, by temperature control, making unstripped gas is subzero 68 ℃ through the temperature of the 3rd interchanger 41; Temperature through the 4th interchanger 43 is subzero 84 ℃; Temperature through the 5th interchanger 45 is subzero 98 ℃.Step 4. in, by temperature control, making unstripped gas is subzero 128 ℃ through the temperature of the 6th interchanger 61; Temperature through the 7th interchanger 63 is subzero 144 ℃; Temperature through the 8th interchanger 65 is subzero 160 ℃.Step 5. in, unstripped gas is reduced to subzero 162 ℃ by throttling tower 7 back temperature becomes the mixture that contains natural gas liquids and gaseous natural gas.
Obviously, the above embodiment of the present invention only is for example of the present invention clearly is described, and is not to be qualification to embodiments of the present invention.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here need not also can't give exhaustive to all embodiments.And these belong to conspicuous variation or the change that spirit of the present invention extended out and still are among protection scope of the present invention.
Claims (10)
1. a compact cascade type prepares the method for natural gas liquids, has following steps:
1. pre-treatment; Remove carbonic acid gas, hydrogen sulfide and water in the unstripped gas;
2. the one-level cooling is handled; Make pretreated unstripped gas through first multi-stage heat exchanger in first cooling cycle system (1) and tripping device (2), handle pretreated unstripped gas is carried out the one-level cooling, make unstripped gas be cooled to subzero 35～subzero 41 ℃, air pressure is 3.8MPa to 4.1MPa;
3. the secondary cooling is handled; Make the unstripped gas that passes through after 2. step is handled successively through second multi-stage heat exchanger in second cooling cycle system (3) and tripping device (4), so that being carried out the secondary cooling, handles the unstripped gas after 2. handling through step, make unstripped gas be cooled to subzero 95～subzero 100 ℃, air pressure is 3.8MPa to 4.1MPa;
4. three grades of coolings are handled; Make the unstripped gas that passes through after 3. step is handled successively through the 3rd multi-stage heat exchanger in the 3rd cooling cycle system (5) and tripping device (6), handle the unstripped gas of 3. handling through step is carried out three grades of coolings, make unstripped gas be cooled to subzero 155～subzero 161 ℃, air pressure is 3.8MPa to 4.1MPa;
5. the throttling step-down is handled: the unstripped gas after 4. the process step is handled is expanded, make unstripped gas be cooled to subzero 162 ℃～163 ℃ and become the mixture that contains natural gas liquids and gaseous natural gas, make material through gas-liquid separation tower (8) then, make liquify natural gas separate, thereby obtain the finished product natural gas liquids with gaseous natural gas.
2. compact cascade type according to claim 1 prepares the method for natural gas liquids, it is characterized in that: above-mentioned steps 1. in, be that 3.5MPa to 6MPa and temperature are the pre-treatment that under 5 ℃ to 40 ℃ the condition unstripped gas is removed carbonic acid gas, hydrogen sulfide and water at air pressure.
3. compact cascade type according to claim 2 prepares the method for natural gas liquids, it is characterized in that: above-mentioned steps 1. in, the pre-treatment that removes carbonic acid gas, hydrogen sulfide and water is that to make unstripped gas be that 4MPa to 5MPa and temperature are under 10 ℃ to 25 ℃ the condition at air pressure, successively first absorption tower (91) by the ethanolamine solutions that is used to remove carbonic acid gas and hydrogen sulfide is housed, second absorption tower (92) of ethylene glycol and aluminium glue is housed and the packing tower (93) of the adsorbent of molecular sieve that is used to remove moisture is housed.
4. compact cascade type according to claim 1 prepares the method for natural gas liquids, it is characterized in that: above-mentioned steps 2. in, described first multi-stage heat exchanger and tripping device (2) comprise successively first interchanger (21), the first gas-liquid separation tower (22), second interchanger (23) and the second gas-liquid separation tower (24) of polyphone; The refrigeration agent of (1) is the mixture of propane or propane and butane in described first cooling cycle system.
5. compact cascade type according to claim 4 prepares the method for natural gas liquids, it is characterized in that: making pretreated unstripped gas is subzero 30 ℃～subzero 35 ℃ through the temperature of first interchanger (21), will be from the first gas-liquid separation tower (22) isolated liquid material as gasoline or diesel oil; Temperature through second interchanger (23) is subzero 40 ℃～subzero 41 ℃, will be from the second gas-liquid separation tower (24) isolated liquid material as the refrigeration agent in first refrigeration cycle.
6. compact cascade type according to claim 1 prepares the method for natural gas liquids, it is characterized in that: above-mentioned steps 3. in, described second multi-stage heat exchanger and tripping device (4) comprise successively the 3rd interchanger (41), the 3rd gas-liquid separation tower (42), the 4th interchanger (43), the 4th gas-liquid separation tower (44), the 5th interchanger (45) and the 5th gas-liquid separation tower (46) of polyphone; Refrigeration agent in described second cooling cycle system (3) is an ethene.
7. compact cascade type according to claim 6 prepares the method for natural gas liquids, it is characterized in that: above-mentioned steps 3. in, making unstripped gas is subzero 65 ℃～subzero 70 ℃ through the temperature of the 3rd interchanger (41); Temperature through the 4th interchanger (43) is subzero 80～subzero 85 ℃; Temperature through the 5th interchanger (45) is subzero 95～subzero 100 ℃, will be from the 5th gas-liquid separation tower (46) isolated liquid material as the refrigeration agent in second cooling cycle system (3).
8. compact cascade type according to claim 1 prepares the method for natural gas liquids, it is characterized in that: above-mentioned steps 4. in, described the 3rd multi-stage heat exchanger and tripping device (6) comprise successively the 6th interchanger (61), the 6th gas-liquid separation tower (62), the 7th interchanger (63), the 7th gas-liquid separation tower (64), the 8th interchanger (65) and the 8th gas-liquid separation tower (66) of polyphone; Refrigeration agent in described the 3rd cooling cycle system (5) is methane or natural gas liquids.
9. compact cascade type according to claim 8 prepares the method for natural gas liquids, it is characterized in that: above-mentioned steps 4. in, making unstripped gas is subzero 120 ℃～subzero 130 ℃ through the temperature of the 6th interchanger (61); Temperature through the 7th interchanger (63) is subzero 140 ℃～subzero 145 ℃; Temperature through the 8th interchanger (65) is subzero 155 ℃～subzero 161 ℃.
10. compact cascade type according to claim 1 prepares the method for natural gas liquids, it is characterized in that: above-mentioned steps 5. in, make through the unstripped gas of step after 4. handling by throttling tower (7), make the air pressure of unstripped gas drop to 0.09MPa to 0.11MPa; Prepared natural gas liquids can be used as refrigeration agent in the 3rd cooling cycle system (5).
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102559236A (en) * | 2010-12-16 | 2012-07-11 | 王建基 | Oil field gas recovering (mixed hydrocarbon recovering, liquefied natural gas recovering) process technology |
| CN104279838A (en) * | 2013-07-09 | 2015-01-14 | 王建基 | Oilfield associated gas stable mixed hydrocarbon recycling and natural gas liquefaction combined technology |
| CN105605882A (en) * | 2015-12-23 | 2016-05-25 | 中石化石油工程技术服务有限公司 | Method for composite refrigeration natural gas liquefaction |
| CN104515362B (en) * | 2013-09-30 | 2017-02-15 | 神华集团有限责任公司 | Method for producing liquid carbon dioxide |
| CN106524665A (en) * | 2015-09-14 | 2017-03-22 | 安瑞科(廊坊)能源装备集成有限公司 | Liquefaction and recovery device and method of LNG container evaporation gas |
| CN115790078A (en) * | 2022-11-29 | 2023-03-14 | 北京恒泰洁能科技有限公司 | CO (carbon monoxide) 2 Liquefaction process and cold box |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4911741A (en) * | 1988-09-23 | 1990-03-27 | Davis Robert N | Natural gas liquefaction process using low level high level and absorption refrigeration cycles |
| US5615561A (en) * | 1994-11-08 | 1997-04-01 | Williams Field Services Company | LNG production in cryogenic natural gas processing plants |
| CN2315506Y (en) * | 1997-10-27 | 1999-04-21 | 中国科学院低温技术实验中心 | Multi-stage throttling natural gas liquefying device |
| CN1095496C (en) * | 1999-10-15 | 2002-12-04 | 余庆发 | Process for preparing liquefied natural gas |
| GB0006265D0 (en) * | 2000-03-15 | 2000-05-03 | Statoil | Natural gas liquefaction process |
| DE10344030A1 (en) * | 2003-09-23 | 2005-04-14 | Linde Ag | Liquefying hydrocarbon-rich gas e.g. natural gas involves flowing of gas through three refrigeration stages, each having a circuit and compressor, so that a part flow of refrigerant from the second circuit pre-cools the gas in first stage |
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2007
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102559236A (en) * | 2010-12-16 | 2012-07-11 | 王建基 | Oil field gas recovering (mixed hydrocarbon recovering, liquefied natural gas recovering) process technology |
| CN104279838A (en) * | 2013-07-09 | 2015-01-14 | 王建基 | Oilfield associated gas stable mixed hydrocarbon recycling and natural gas liquefaction combined technology |
| CN104515362B (en) * | 2013-09-30 | 2017-02-15 | 神华集团有限责任公司 | Method for producing liquid carbon dioxide |
| CN106524665A (en) * | 2015-09-14 | 2017-03-22 | 安瑞科(廊坊)能源装备集成有限公司 | Liquefaction and recovery device and method of LNG container evaporation gas |
| CN105605882A (en) * | 2015-12-23 | 2016-05-25 | 中石化石油工程技术服务有限公司 | Method for composite refrigeration natural gas liquefaction |
| CN105605882B (en) * | 2015-12-23 | 2018-06-05 | 中石化石油工程技术服务有限公司 | A kind of compound-refrigerating natural gas liquefaction |
| CN115790078A (en) * | 2022-11-29 | 2023-03-14 | 北京恒泰洁能科技有限公司 | CO (carbon monoxide) 2 Liquefaction process and cold box |
| CN115790078B (en) * | 2022-11-29 | 2023-09-29 | 北京恒泰洁能科技有限公司 | CO (carbon monoxide) 2 Liquefying process and cold box |
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