CN203454606U - Device for recycling synthesis ammonia off gas to produce LNG (liquefied natural gas) - Google Patents
Device for recycling synthesis ammonia off gas to produce LNG (liquefied natural gas) Download PDFInfo
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- CN203454606U CN203454606U CN201320529658.2U CN201320529658U CN203454606U CN 203454606 U CN203454606 U CN 203454606U CN 201320529658 U CN201320529658 U CN 201320529658U CN 203454606 U CN203454606 U CN 203454606U
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Abstract
The utility model belongs to a device for recycling synthesis ammonia off gas to produce LNG (liquefied natural gas). The device comprises a gas inlet buffering tank connected with a first raw material gas inlet of a first heat exchanger by a pipeline; a first raw material gas outlet of the first heat exchanger is respectively connected with an expansion end inlet of a turbo expander and a raw material gas inlet of a reboiler by a pipeline; an expansion end outlet of the turbo expander is connected with a raw material gas inlet of a gas-liquid separator by a pipeline; the raw material gas inlet of the reboiler is communicated with a raw material outlet of the reboiler of which the raw material gas outlet is connected with an inlet in the upper part of a rectifying tower by a second raw material gas inlet of a second heat exchanger, a second raw material gas outlet of the second heat exchanger and a third throttle valve. The device for recycling synthesis ammonia off gas to produce the LNG has the advantages of adoption of dual-expansion for refrigeration, simple process flow, simple and convenient operation, stable operation and low power consumption.
Description
Technical field
The utility model belongs to the technical field of producing LNG, is specifically related to the two swell refrigerations of a kind of employing, technological process is simple, easy and simple to handle, and recovery synthetic ammonia tailgas stable and low energy consumption is produced the device of LNG.
Background technology
Nineteen forty-one has built up the first in the world and has overlapped plant-scale LNG device in U.S. Cleveland, liquefying power is 8500m
3/ d.Since the sixties, LNG industry has obtained fast development, and scale is increasing, and Basicloadtype liquefying power is at 2.5 * 104m
3/ d.According to data introduction, the LNG device that go into operation in various countries has at present reached cover more than 160, and the LNG total volume of exports has surpassed 46.18 * 106t/a.
One, take the methane (LNG or CNG) that natural gas is unstripped gas produces flow process
To produce LNG technology quite ripe as raw material to take at present natural gas, and corresponding LNG Lquified Process Flow is also more, comprises purification, precooling, liquefaction, crosses cold four large steps, and feed gas methane content is generally more than 95%.The cold-producing medium adopting according to technique and refrigeration unit, technological process is mainly divided into: superposition type liquefaction cycle (or step by step formula, stepwise), mix refrigerant liquefaction cycle, the circulation of (propane) precooling mix refrigerant, double-mixed refrigerant kind of refrigeration cycle and with the kind of refrigeration cycle of decompressor.But owing to being subject to the restriction of gas source component and energy consumption index, all there is certain deficiency in above technological process.
Two, gas employing methanation of coke oven is produced the technological process of methane
Along with coke-stove gas exits mathematical model, with coke-stove gas, produce CNG or LNG and start to rise.With gas employing methanation of coke oven, produce the technological process of methane (CNG), comprise compression, desulfurization, hydrodesulfurization, the desulfurization of zinc oxide essence, heat exchange, methanation Waste Heat Recovery, cooling, separated, the production by pressure swing adsorption product natural gas of oven gas.In this technological process, most important step is pressure-variable adsorption and methanation.Methanation reaction is by the H in tail gas
2, CO
2, CO changes into CH
4thereby, the productive rate of raising methane.Pressure-variable adsorption is purified the unstripped gas through methanation, produces standard compliant CNG.The compressed natural gas of producing can be supplied with gas again, also can be used as transportation and energy Gong Duangei CNG gas station.
Three, take the methane (LNG or CNG) that synthetic ammonia tailgas is unstripped gas produces flow process
Can predict, within the time of following 10-20, LNG will become the main force in Natural Gas In China market.At present the domestic LNG process unit that synthetic ammonia tailgas is unstripped gas of take of having invested to build only has five, six covers, and scale is less, and technical merit falls behind.Methane content in synthetic ammonia tailgas is lower, generally in 25% left and right, with respect to take the production technology that gas accumulations develop is unstripped gas, has obvious inferior position.Yet China often daily has a large amount of synthetic ammonia tailgas to be discharged into the serious waste that atmosphere causes energy resources, aggravates the greenhouse effects of atmosphere, contaminated environment simultaneously.The energy resource structure of China be take coal as main, and oil, natural gas only account for very little ratio, and the LNG production technology of China is also in the stage at the early-stage at present, well below world average level.Along with the continuous growth of country to energy demand, introduce LNG by optimizing Chinese energy resource structure, effectively solve the dual problem of the energy safety of supply, ecological environmental protection, realize economy and social sustainable development and play a significant role.
Utility model content
The purpose of this utility model is to overcome defect of the prior art and provides the two swell refrigerations of a kind of employing, technological process simple, easy and simple to handle, and recovery synthetic ammonia tailgas stable and low energy consumption is produced the device of LNG.
The purpose of this utility model is achieved in that and comprises air inlet surge tank, air inlet surge tank is connected with the first raw material gas inlet of First Heat Exchanger by pipeline, the first unstripped gas outlet of First Heat Exchanger is connected with the expanding end import of booster expansion machine and the raw material gas inlet of reboiler respectively by pipeline, the expanding end outlet of booster expansion machine is connected with the raw material gas inlet of gas-liquid separator by pipeline, the gaseous phase outlet at gas-liquid separator top is connected with the raw material gas inlet of the second heat exchanger by pipeline, the unstripped gas outlet of the second heat exchanger is connected with the raw material gas inlet of compressor by the second raw material gas inlet of First Heat Exchanger and the second unstripped gas outlet of First Heat Exchanger, the outlet of compressor is connected with the pressurized end of booster expansion machine, the pressurized end of booster expansion machine is connected with the tube side of liquefied ammonia cooler, the tube side of liquefied ammonia cooler is connected by the pipeline between the first raw material gas inlet of pipeline and air inlet surge tank and First Heat Exchanger, the liquid-phase outlet of gas-liquid separator bottom is connected with the import at rectifying column middle part by first throttle valve, the on-condensible gas outlet at rectifying column top by pipeline successively with the first tail gas import of the second heat exchanger, the first tail gas outlet of the second heat exchanger, decompressor, the second tail gas import of the second heat exchanger, the second tail gas outlet of the second heat exchanger is connected with the first tail gas import of First Heat Exchanger, the first tail gas outlet of First Heat Exchanger is connected with converter entrance, the bottom liquid phases outlet of rectifying column is connected with the second methane import of the second choke valve and the second heat exchanger respectively by pipeline, the second choke valve by pipeline successively with the first methane import of the second heat exchanger, the first methane outlet of the second heat exchanger, the first methane import of First Heat Exchanger, the first methane outlet of First Heat Exchanger, methane compressor, the second methane import of the tube side of carbon dioxide cooler and First Heat Exchanger is connected, the second methane outlet of First Heat Exchanger is connected with the methane import of reboiler, the methane outlet of reboiler by pipeline successively with the leucoaurin import of the second heat exchanger, the leucoaurin outlet of the second heat exchanger, the 4th choke valve is connected with LNG storage tank, the second methane import of described the second heat exchanger is connected with LNG storage tank with the 5th choke valve by the second methane outlet of the second heat exchanger, the raw material gas inlet of described reboiler is connected with the outlet of the unstripped gas of reboiler, the unstripped gas outlet of reboiler is successively by the second raw material gas inlet of the second heat exchanger, and the second unstripped gas outlet of the second heat exchanger is connected with the import of rectifier with the 3rd choke valve.
Described compressor is two-stage compression, between its one-level compression section exhaust outlet and the air inlet of two-stage compression workshop section, is provided with the first water cooler, and the exhaust outlet of two-stage compression workshop section is provided with the second water cooler.
Described methane compressor is two-stage compression, between its one-level compression section exhaust outlet and the air inlet of two-stage compression workshop section, is provided with methane water cooler, between the exhaust outlet of two-stage compression workshop section and the tube side of carbon dioxide cooler, is provided with liquefied ammonia cooler.
Described First Heat Exchanger is provided with First Heat Exchanger carbon dioxide inlet and the outlet of First Heat Exchanger carbon dioxide being connected with carbon dioxide reservoir, and described First Heat Exchanger carbon dioxide outlet is connected with carbon dioxide condenser.
The shell side two ends of described liquefied ammonia cooler are connected with screw ammonia refrigerating compressor with liquid ammonia storage tank respectively.
The shell side two ends of described carbon dioxide cooler are connected with carbon dioxide condenser with carbon dioxide reservoir respectively.
The utility model adopts liquefied ammonia, liquid CO
2with methane three the kind of refrigeration cycle overlappings that are cold-producing medium, adopt two circularly cooling technique expanding fully effectively to reclaim and distribution system in cold, realize being cooled step by step of material, condensation liquefaction and excessively cold.The utility model overcomes traditional concept, and the propane by cold-producing medium in traditional handicraft and ethene change liquefied ammonia, liquid CO into
2, when significantly reducing refrigeration cost, improved the safety coefficient in its production.
The utlity model has and adopt two swell refrigerations, technological process simple, easy and simple to handle, the advantage of stable and low energy consumption.
Accompanying drawing explanation
Fig. 1 is the utility model structural representation.
The specific embodiment
As shown in Figure 1, the utility model comprises air inlet surge tank 41, air inlet surge tank 41 is connected with the first raw material gas inlet 37 of First Heat Exchanger 1 by pipeline, the first unstripped gas outlet 38 of First Heat Exchanger 1 is connected with the raw material gas inlet of reboiler 2 with the expanding end import of booster expansion machine 10 respectively by pipeline, the expanding end outlet of booster expansion machine 10 is connected with the raw material gas inlet of gas-liquid separator 8 by pipeline, the gaseous phase outlet at gas-liquid separator 8 tops is connected with the raw material gas inlet 30 of the second heat exchanger 3 by pipeline, the unstripped gas outlet 23 of the second heat exchanger 3 is connected with the raw material gas inlet of compressor 9 by the second raw material gas inlet 19 of First Heat Exchanger 1 and the second unstripped gas outlet 15 of First Heat Exchanger 1, the outlet of compressor 9 is connected with the pressurized end of booster expansion machine 10, the pressurized end of booster expansion machine 10 is connected with the tube side of liquefied ammonia cooler 11, the tube side of liquefied ammonia cooler 11 is connected by the pipeline between the first raw material gas inlet 37 of pipeline and air inlet surge tank 41 and First Heat Exchanger 1, the liquid-phase outlet of gas-liquid separator 8 bottoms is connected with the import at rectifying column 4 middle parts by first throttle valve 13, the on-condensible gas outlet at rectifying column 4 tops by pipeline successively with the first tail gas import 35 of the second heat exchanger 3, the first tail gas outlet 28 of the second heat exchanger 3, decompressor 7, the second tail gas import 36 of the second heat exchanger 3, the second tail gas outlet 29 of the second heat exchanger 3 is connected with the first tail gas import 21 of First Heat Exchanger 1, the first tail gas outlet 17 of First Heat Exchanger 1 is connected with converter 42 entrances, the bottom liquid phases outlet of rectifying column 4 is connected with the second methane import 32 of the second choke valve 14 and the second heat exchanger 3 respectively by pipeline, the second choke valve 14 by pipeline successively with the first methane import 31 of the second heat exchanger 3, the first methane outlet 24 of the second heat exchanger 3, the first methane import 20 of First Heat Exchanger 1, the first methane outlet 16 of First Heat Exchanger 1, methane compressor 5, the second methane import 39 of the tube side of carbon dioxide cooler 6 and First Heat Exchanger 1 is connected, the second methane outlet 40 of First Heat Exchanger 1 is connected with the methane import of reboiler 2, the methane outlet of reboiler 2 by pipeline successively with the leucoaurin import 27 of the second heat exchanger 3, the leucoaurin outlet 34 of the second heat exchanger 3, the 4th choke valve 45 is connected with LNG storage tank 44, the second methane import 32 of described the second heat exchanger 3 is connected with LNG storage tank 44 with the 5th choke valve 43 by the second methane outlet 25 of the second heat exchanger 3, the raw material gas inlet of described reboiler 2 is connected with the unstripped gas outlet of reboiler 2, the second unstripped gas outlet 33 that the second raw material gas inlet 26, the second heat exchangers 3 of the second heat exchanger 3 are passed through in the unstripped gas outlet of reboiler 2 is successively connected with the import on rectifying column 4 tops with the 3rd choke valve 12.Described compressor 9 is two-stage compression, and the exhaust outlet that is provided with the first water cooler 52， two-stage compression workshop section between its one-level compression section exhaust outlet and the air inlet of two-stage compression workshop section is provided with the second water cooler 53.Described methane compressor 5 is two-stage compression, is provided with between the exhaust outlet of methane water cooler 54， two-stage compression workshop section and the tube side of carbon dioxide cooler 6 and is provided with liquefied ammonia cooler 55 between its one-level compression section exhaust outlet and the air inlet of two-stage compression workshop section.Described First Heat Exchanger 1 is provided with First Heat Exchanger 1 carbon dioxide inlet 22 and the First Heat Exchanger 1 carbon dioxide outlet 18 being connected with carbon dioxide reservoir 46, and described First Heat Exchanger 1 carbon dioxide outlet 18 is connected with carbon dioxide condenser 47.The shell side two ends of described liquefied ammonia cooler 11 are connected with screw ammonia refrigerating compressor 49 with liquid ammonia storage tank 48 respectively.The shell side two ends of described carbon dioxide cooler 6 are connected with carbon dioxide condenser 47 with carbon dioxide reservoir 46 respectively.
Reclaim synthetic ammonia tailgas and produce a process of LNG, this process comprises the steps:
Step 1: the unstripped gas in air inlet surge tank 41 exports the 38 rear raw material gas inlet that enter respectively expanding end and the reboiler 2 of booster expansion machine 10 by the first raw material gas inlet 37 of First Heat Exchanger 1 and the first unstripped gas of First Heat Exchanger 1, the composition of described unstripped gas is: methane, nitrogen, argon gas and hydrogen; The temperature of described unstripped gas when the first raw material gas inlet 37 of First Heat Exchanger 1 is: 8 ℃～10 ℃, unstripped gas in the temperature of the first unstripped gas outlet 38 of First Heat Exchanger 1 is :-110 ℃, gas phase fraction is 1;
Step 2: the expanding end 50 of the unstripped gas described in above-mentioned steps one by booster expansion machine 10 entered and carry out gas-liquid separation in gas-liquid separator 8, after gas-liquid separation, its gas phase enters in the second heat exchanger 3 by the raw material gas inlet 30 of the second heat exchanger 3, and its liquid phase enters in rectifying column 4 by the import at first throttle valve 13 and rectifying column 4 middle parts; The temperature of described unstripped gas after booster expansion machine 10 expanding ends is :-146.7 ℃, gas phase fraction is 0.96; After described gas-liquid separation, the temperature of gas phase is :-146.7 ℃～-147 ℃, methane molar content is 22.1%;
Step 3: make the unstripped gas entering in the second heat exchanger 3 in above-mentioned steps two export 23 by the unstripped gas of the second heat exchanger 3 successively, the second raw material gas inlet 19 of First Heat Exchanger 1, the second unstripped gas outlet 15 of First Heat Exchanger 1, compressor 9, the pressurized end 51 of booster expansion machine 10 and the tube side of liquefied ammonia cooler 11 enter in the pipeline between the first raw material gas inlet 37 of air inlet surge tank 41 and First Heat Exchanger 1, the temperature that the unstripped gas of described the second heat exchanger 3 exports 23 o'clock unstripped gas is :-132 ℃, the temperature that the second unstripped gas of First Heat Exchanger 1 exports 15 o'clock unstripped gas is: 4.8 ℃～7 ℃, during compressor 9 outlet, the temperature of unstripped gas is: 35 ℃～55 ℃, the temperature of booster expansion machine 10 pressurized end 51 outlet unstripped gas is: 66 ℃～88 ℃, the temperature of liquefied ammonia cooler 11 outlet unstripped gas is: 8 ℃～10 ℃,
Step 4: make to enter in step 1 reboiler 2 raw material gas inlet unstripped gas successively the unstripped gas outlet by reboiler 2, the second unstripped gas outlet 33, the three choke valves 12 of the second raw material gas inlet 26 of the second heat exchanger 3, the second heat exchanger 3 and the import on rectifying column 4 tops enter in rectifying column 4; The unstripped gas temperature of the unstripped gas outlet of reboiler 2 is :-128 ℃～-130 ℃, gas phase fraction is 0.9～0.97; The unstripped gas temperature of the second unstripped gas outlet 33 of the second heat exchanger 3 is :-162 ℃～-165 ℃, gas phase fraction is 0.29～0.31; After the 3rd choke valve 12 reducing pressure by regulating flows, unstripped gas temperature is :-177 ℃～-179 ℃, gas phase fraction is 0.45～0.5;
Step 5: make the unstripped gas that enters rectifying column 4 in step 2 and step 4 carry out rectification and purification, gas phase after rectification and purification enters the inside of the second heat exchanger 3 by the on-condensible gas outlet at rectifying column 4 tops and the first tail gas import 35 of the second heat exchanger 3, liquid phase after rectification and purification enters the inside of the second heat exchanger 3 by a bottom liquid phases outlet part for rectifying column 4 by the first methane import 31 of the second choke valve 14 and the second heat exchanger 3, another part enters the inside of the second heat exchanger 3 by the second methane import 32 of the second heat exchanger 3; The on-condensible gas that the on-condensible gas outlet at described rectifying column 4 tops is discharged is tail gas, the temperature of tail gas is :-171 ℃～-172 ℃, the liquid phase substance that the bottom liquid phases outlet of described rectifying column 4 is discharged is methane, and the temperature of methane is :-131.9 ℃, and methane molar content 99.2%; The temperature of described methane after by the second choke valve 14 reducing pressure by regulating flows is :-154.7 ℃, gas phase fraction is 0.178;
Step 6: make the first tail gas import 35 by the second heat exchanger 3 in step 5 enter the tail gas of the second heat exchanger 3 inside by the first tail gas outlet 28, decompressor 7, the second tail gas import 36 of the second heat exchanger 3, the second tail gas outlet 29 of the second heat exchanger 3 of pipeline successively the second heat exchanger 3, the first tail gas outlet 17 of the first tail gas import 21 of First Heat Exchanger 1 and First Heat Exchanger 1 is connected, and the first tail gas outlet 17 is connected with converter 42 entrances; Described tail gas exports the temperature of 28 o'clock at the first tail gas of the second heat exchanger 3 :-144 ℃, described exhaust temperature after decompressor 7 swell refrigerations is :-185 ℃, gas phase fraction is 1; Temperature when described tail gas is discharged from the second tail gas outlet 29 of the second heat exchanger 3 is :-132 ℃; Temperature when described tail gas is discharged from the first tail gas outlet 17 of First Heat Exchanger 1 is: 4.8 ℃～7 ℃; In tail gas, contain methane, nitrogen, argon gas and hydrogen, wherein, methane accounts for 8% of methane in unstripped gas, argon gas be in unstripped gas argon gas 97%, nitrogen and hydrogen are nitrogen and hydrogen whole in unstripped gas;
Step 7: the first methane outlet 24 by the second heat exchanger 3 is, the first methane import 20 of First Heat Exchanger 1, the first methane outlet 16 of First Heat Exchanger 1, methane compressor 5, the tube side of carbon dioxide cooler 6, the second methane import 39 of First Heat Exchanger 1 successively to make in step 5 inside methane that the first methane import 31 by the second heat exchanger 3 enters the second heat exchanger 3, and the second methane outlet 40 of First Heat Exchanger 1 and the methane import of reboiler 2 enter in reboiler 2; Temperature when described methane is discharged by the first methane outlet 24 of the second heat exchanger 3 is :-132 ℃, gas phase fraction is 1; Temperature when described methane is discharged by the first methane outlet 16 of First Heat Exchanger 1 is: 4.8 ℃～7 ℃; Methane temperature after described methane compresses by methane compressor 5 is: 8 ℃～10 ℃; Described methane by the cooled temperature of carbon dioxide cooler 6 is :-48 ℃～-50 ℃; Temperature when described methane is discharged by the second methane outlet 40 of First Heat Exchanger 1 is :-110 ℃, gas phase fraction is 1;
Step 8: make the methane entering in reboiler 2 in step 7 pass through successively the methane outlet of reboiler 2, the leucoaurin import 27 of the second heat exchanger 3, leucoaurin outlet the 34 and the 4th choke valve 43 of the second heat exchanger 3 enters in LNG storage tank 44, temperature while discharging during the methane outlet of described methane by reboiler 2 is :-129.7 ℃, gas phase fraction is 0; Described methane carried out cold treatment by the second heat exchanger 3, and the methane temperature of crossing after cold treatment is :-157 ℃～-165 ℃, gas phase fraction is 0;
Step 9: make in step 5 inside methane that the second methane import 32 by the second heat exchanger 3 enters the second heat exchanger 3 enter in LNG storage tank 44 by the second methane outlet the 25 and the 5th choke valve 45 of the second heat exchanger 3; Temperature when described methane is discharged by the second methane outlet 25 of the second heat exchanger 3 is :-157 ℃～-165 ℃, gas phase fraction is 0; The product methane purity that described step 8 and step 9 enter in LNG storage tank 44 is: 99.2%, wherein, also contain 0.8% argon gas;
Step 10: the carbon dioxide in carbon dioxide reservoir 46 enters into carbon dioxide condenser 47 by First Heat Exchanger 1 carbon dioxide inlet 22 and First Heat Exchanger 1 carbon dioxide outlet 18, the temperature of the carbon dioxide of described carbon dioxide reservoir 46 outlets is :-48 ℃～-50 ℃, gas phase fraction is 0, described carbon dioxide exports the temperature of 18 o'clock at First Heat Exchanger 1 carbon dioxide: 4.8 ℃～7 ℃, gas phase fraction is 1.
The first raw material gas inlet 37 of the First Heat Exchanger 1 in First Heat Exchanger described in the utility model 1 is connected with the first unstripped gas outlet 38 of First Heat Exchanger 1, the second raw material gas inlet 19 of First Heat Exchanger 1 is connected with the second unstripped gas outlet 15 of First Heat Exchanger 1, the first tail gas import 21 of First Heat Exchanger 1 is connected with the first tail gas outlet 17 of First Heat Exchanger 1, the first methane import 20 of First Heat Exchanger 1 is connected with the first methane outlet 16 of First Heat Exchanger 1, the second methane import 39 of First Heat Exchanger 1 is connected with the second methane outlet 40 of First Heat Exchanger 1, First Heat Exchanger 1 carbon dioxide inlet 22 is connected with First Heat Exchanger 1 carbon dioxide outlet 18, in the second described heat exchanger 3, the raw material gas inlet 30 of the second heat exchanger 3 and the unstripped gas of the second heat exchanger 3 outlet 23 are connected, the first tail gas import 35 of the second heat exchanger 3 is connected with the first tail gas outlet 28 of the second heat exchanger 3, the second tail gas import 36 of the second heat exchanger 3 is connected with the second tail gas outlet 29 of the second heat exchanger 3, the first methane import 31 of the second heat exchanger 3 is connected with the first methane outlet 24 of the second heat exchanger 3, the second methane import 32 of the second heat exchanger 3 is connected with the second methane outlet 25 of the second heat exchanger 3, the second raw material gas inlet 26 of the second heat exchanger 3 is connected with the second unstripped gas outlet 33 of the second heat exchanger 3, the leucoaurin import 27 of the second heat exchanger 3 is connected with the leucoaurin outlet 34 of the second heat exchanger 3, the raw material gas inlet of the reboiler 2 in described reboiler 2 is connected with the outlet of the unstripped gas of reboiler 2, and the methane import of reboiler 2 is connected with the outlet of the methane of reboiler 2, the raw material gas inlet of the gas-liquid separator 8 in described gas-liquid separator 8 is connected with the gaseous phase outlet at gas-liquid separator 8 tops and the liquid-phase outlet of gas-liquid separator 8 bottoms respectively, the import at rectifying column 4 middle parts in described rectifying column 4 and the import on rectifying column 4 tops are connected with the on-condensible gas outlet at rectifying column 4 tops and the bottom liquid phases outlet of rectifying column 4 respectively.
Claims (6)
1. one kind is reclaimed the device that synthetic ammonia tailgas is produced LNG, comprise air inlet surge tank (41), it is characterized in that: air inlet surge tank (41) is connected with first raw material gas inlet (37) of First Heat Exchanger (1) by pipeline, the first unstripped gas outlet (38) of First Heat Exchanger (1) is connected with the raw material gas inlet of reboiler (2) with expanding end (50) import of booster expansion machine (10) respectively by pipeline, expanding end (50) outlet of booster expansion machine (10) is connected with the raw material gas inlet of gas-liquid separator (8) by pipeline, the gaseous phase outlet at gas-liquid separator (8) top is connected with the raw material gas inlet (30) of the second heat exchanger (3) by pipeline, the unstripped gas outlet (23) of the second heat exchanger (3) is connected with the raw material gas inlet of compressor (9) by second raw material gas inlet (19) of First Heat Exchanger (1) and the second unstripped gas outlet (15) of First Heat Exchanger (1), the outlet of compressor (9) is connected with the pressurized end (51) of booster expansion machine (10), the pressurized end (51) of booster expansion machine (10) is connected with the tube side of liquefied ammonia cooler (11), the tube side of liquefied ammonia cooler (11) is connected with the pipeline between air inlet surge tank (41) and first raw material gas inlet (37) of First Heat Exchanger (1) by pipeline, the liquid-phase outlet of gas-liquid separator (8) bottom is connected with the import at rectifying column (4) middle part by first throttle valve (13), the on-condensible gas outlet at rectifying column (4) top by pipeline successively with the first tail gas import (35) of the second heat exchanger (3), the first tail gas outlet (28) of the second heat exchanger (3), decompressor (7), the second tail gas import (36) of the second heat exchanger (3), the second tail gas outlet (29) of the second heat exchanger (3) and the first tail gas import (21) of First Heat Exchanger (1) are connected, the first tail gas outlet (17) of First Heat Exchanger (1) is connected with converter (42) entrance, the bottom liquid phases outlet of rectifying column (4) is connected with the second methane import (32) of the second choke valve (14) and the second heat exchanger (3) respectively by pipeline, the second choke valve (14) by pipeline successively with the first methane import (31) of the second heat exchanger (3), the first methane outlet (24) of the second heat exchanger (3), the first methane import (20) of First Heat Exchanger (1), the first methane outlet (16) of First Heat Exchanger (1), methane compressor (5), the second methane import (39) of the tube side of carbon dioxide cooler (6) and First Heat Exchanger (1) is connected, the second methane outlet (40) of First Heat Exchanger (1) is connected with the methane import of reboiler (2), the methane outlet of reboiler (2) by pipeline successively with the leucoaurin import (27) of the second heat exchanger (3), the leucoaurin outlet (34) of the second heat exchanger (3), the 4th choke valve (45) is connected with LNG storage tank (44), the second methane import (32) of described the second heat exchanger (3) is connected with LNG storage tank (44) with the 5th choke valve (43) by the second methane outlet (25) of the second heat exchanger (3), the raw material gas inlet of described reboiler (2) is connected with the unstripped gas outlet of reboiler (2), the unstripped gas outlet of reboiler (2) is successively by second raw material gas inlet (26) of the second heat exchanger (3), and the second unstripped gas outlet (33) of the second heat exchanger (3) is connected with the import on rectifying column (4) top with the 3rd choke valve (12).
2. recovery synthetic ammonia tailgas according to claim 1 is produced the device of LNG, it is characterized in that: described compressor (9) is two-stage compression, between its one-level compression section exhaust outlet and the air inlet of two-stage compression workshop section, be provided with the first water cooler (52), the exhaust outlet of two-stage compression workshop section is provided with the second water cooler (53).
3. recovery synthetic ammonia tailgas according to claim 1 is produced the device of LNG, it is characterized in that: described methane compressor (5) is two-stage compression, between its one-level compression section exhaust outlet and the air inlet of two-stage compression workshop section, be provided with methane water cooler (54), between the tube side of the exhaust outlet of two-stage compression workshop section and carbon dioxide cooler (6), be provided with liquefied ammonia cooler (55).
4. recovery synthetic ammonia tailgas according to claim 1 is produced the device of LNG, it is characterized in that: described First Heat Exchanger (1) is provided with First Heat Exchanger (1) carbon dioxide inlet (22) and First Heat Exchanger (1) the carbon dioxide outlet (18) being connected with carbon dioxide reservoir (46), and described First Heat Exchanger (1) carbon dioxide outlet (18) is connected with carbon dioxide condenser (47).
5. recovery synthetic ammonia tailgas according to claim 1 is produced the device of LNG, it is characterized in that: the shell side two ends of described liquefied ammonia cooler (11) are connected with screw ammonia refrigerating compressor (49) with liquid ammonia storage tank (48) respectively.
6. recovery synthetic ammonia tailgas according to claim 1 is produced the device of LNG, it is characterized in that: the shell side two ends of described carbon dioxide cooler (6) are connected with carbon dioxide condenser (47) with carbon dioxide reservoir (46) respectively.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103438662A (en) * | 2013-08-21 | 2013-12-11 | 河南心连心深冷能源股份有限公司 | Device and technological method for LNG production through recycling synthesis ammonia tail gas |
| CN105066586A (en) * | 2015-09-14 | 2015-11-18 | 成都深冷液化设备股份有限公司 | Device and method for preparing synthetic ammonia raw material gas and LNG through liquid nitrogen washing |
| CN107024074A (en) * | 2017-05-19 | 2017-08-08 | 河南开元空分集团有限公司 | A kind of nitrogen single-stage expansion refrigeration reclaims methane in methanol-fueled CLC tail gas for LNG devices and methods therefor |
-
2013
- 2013-08-21 CN CN201320529658.2U patent/CN203454606U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103438662A (en) * | 2013-08-21 | 2013-12-11 | 河南心连心深冷能源股份有限公司 | Device and technological method for LNG production through recycling synthesis ammonia tail gas |
| CN105066586A (en) * | 2015-09-14 | 2015-11-18 | 成都深冷液化设备股份有限公司 | Device and method for preparing synthetic ammonia raw material gas and LNG through liquid nitrogen washing |
| CN107024074A (en) * | 2017-05-19 | 2017-08-08 | 河南开元空分集团有限公司 | A kind of nitrogen single-stage expansion refrigeration reclaims methane in methanol-fueled CLC tail gas for LNG devices and methods therefor |
| CN107024074B (en) * | 2017-05-19 | 2022-08-16 | 河南开元空分集团有限公司 | Device and method for preparing LNG (liquefied Natural gas) by recovering methane in methanol synthesis tail gas through nitrogen single-stage expansion refrigeration |
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