CN211079068U - Natural gas denitrification device - Google Patents
Natural gas denitrification device Download PDFInfo
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- CN211079068U CN211079068U CN201920617977.6U CN201920617977U CN211079068U CN 211079068 U CN211079068 U CN 211079068U CN 201920617977 U CN201920617977 U CN 201920617977U CN 211079068 U CN211079068 U CN 211079068U
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Abstract
The utility model relates to a natural gas denitrification device, including raw materials natural gas precooling cold box (1), raw materials natural gas evaporimeter (2), absorption tower (3), high pressure flash distillation tower (4), middling pressure flash distillation tower (5), low pressure flash distillation tower (6), ordinary pressure flash distillation tower (7), solvent circulating pump (8), solvent evaporator (9), high pressure flash distillation gas compressor (10), high pressure flash distillation gas evaporimeter (11), low pressure flash distillation gas compressor (12), low pressure flash distillation gas air cooler (13). The utility model discloses do not need the heating, only need the electric energy, total energy consumption is low, and the operating cost is low.
Description
Technical Field
The utility model belongs to natural gas processing field especially relates to a N in desorption natural gas2The apparatus of (1).
Background
Natural gas is a gaseous hydrocarbon production substance of petroleum and is a high-quality fuel and a chemical raw material. Natural gas contains a majority of methane, small amounts of ethane, propane and butane, and generally also H2S、CO2、H2O, etc., some natural gases contain N2, others contain argon and neon, etc. Containing N2Too high natural gas can also reduce the heat value of the natural gas, so that the natural gas cannot meet the requirements specified by the technical indexes of commodity natural gas in China. Thus, it is possible to provideIt is necessary to enrich natural gas with N2Effective removal is performed.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a flow is simple, the energy consumption is low, the flow is short, N2High-removal-rate natural gas N removal2The device belongs to a physical solvent method. The device is adopted to carry out natural gas N2By low-temperature absorption and N removal2The intermediate dehydration is carried out, the heating is not needed, only the electric energy is needed, the total energy consumption is low, the operation cost is low, and the inert gases such as Ne and Ar can be removed simultaneously. The technical scheme is as follows:
a natural gas denitrification device comprises a raw material natural gas precooling cold box 1, a raw material natural gas evaporator 2, an absorption tower 3, a high-pressure flash tower 4, a medium-pressure flash tower 5, a low-pressure flash tower 6, a normal-pressure flash tower 7, a solvent circulating pump 8, a solvent evaporator 9, a high-pressure flash vapor compressor 10, a high-pressure flash vapor evaporator 11, a low-pressure flash vapor compressor 12 and a low-pressure flash vapor air cooler 13,
after the raw material natural gas is preliminarily pre-cooled by a raw material natural gas pre-cooling cold box 1, the raw material natural gas is further cooled by a raw material natural gas evaporator 2 and then is sent to the middle part of an absorption tower 3; n is a radical of2The discharge pipeline is positioned at the top of the absorption tower 3 and connected with the raw material natural gas pre-cooling cold box 1, and the N after reheating is2The gas in the discharge pipeline is discharged;
two ends of a flash liquid discharge pipeline at the bottom of the absorption tower are respectively positioned at the bottom of the absorption tower 3 and the top of the high-pressure flash tower 4, two ends of a high-pressure flash liquid discharge pipeline are respectively positioned at the bottom of the high-pressure flash tower 4 and the top of the medium-pressure flash tower 5, two ends of the high-pressure flash gas discharge pipeline are respectively connected with the top of the high-pressure flash tower 4 and a high-pressure flash gas pipeline of a raw natural gas pre-cooling cold box 1 discharge cold box and connected to an inlet of a high-pressure flash gas compressor 10, a discharge pipeline after compression of high-pressure flash gas is connected to a high-pressure flash gas evaporator 11, and a discharge pipeline after; two ends of the medium-pressure flash liquid discharge pipeline are respectively positioned at the bottom of the medium-pressure flash tower 5 and the top of the low-pressure flash tower 6, two ends of the medium-pressure flash gas discharge pipeline are respectively connected with the top of the medium-pressure flash tower 5 and the raw material natural gas pre-cooling cold box 1, and gas in the medium-pressure flash gas pipeline reheated by the raw material natural gas pre-cooling cold box 1 is discharged as purified natural gas; two ends of a low-pressure flash evaporation liquid discharge pipeline are respectively positioned at the bottom of the low-pressure flash evaporation tower 6 and the top of the atmospheric flash evaporation tower 7, two ends of the low-pressure flash evaporation gas discharge pipeline are respectively connected with the top of the low-pressure flash evaporation tower 6 and the raw material gas pre-cooling cold box 1, and the low-pressure flash evaporation gas pipeline reheated by the raw material natural gas pre-cooling cold box 1 is connected with a medium-pressure flash evaporation gas pipeline; the two ends of an atmospheric flash liquid discharge pipeline are respectively positioned at the bottom of the atmospheric flash tower 7 and the inlet of the solvent circulating pump 8, the two ends of the atmospheric flash gas discharge pipeline are respectively connected with the top of the atmospheric flash tower 7 and the raw material gas pre-cooling cold box 1, the atmospheric flash gas pipeline reheated by the raw material natural gas pre-cooling cold box 1 enters a low-pressure flash gas compressor 12, a natural gas pipeline pressurized by the low-pressure flash gas compressor 12 is connected to a low-pressure flash gas air cooler 13, and the cooled pipeline is communicated to a medium-pressure flash gas pipeline; the outlet and discharge pipeline of the solvent circulating pump is respectively connected with the outlet of the solvent circulating pump 8 and the inlet of the solvent evaporator 9, and the evaporator absorption solvent discharge pipeline is connected to the top of the absorption tower 3.
Preferably, the plant further comprises a high pressure hydraulic turbine 14, an intermediate pressure hydraulic turbine 15, wherein the high pressure hydraulic turbine 14 is disposed on the absorption column bottom flash liquid discharge line S3 and the intermediate pressure hydraulic turbine 15 is disposed on the high pressure flash liquid discharge line S4.
The utility model has the advantages and positive effects that:
1. low energy consumption, the utility model discloses only consume the electric energy, compressor export natural gas cooler can adopt the air cooler, or adopt the method of air cooler earlier with propane refrigeration later, and the technology energy consumption is far less than pure L NG liquefaction rectification and takes off N2Energy consumption of the process;
2. the absorbent is regenerated only by flash evaporation without heating;
3. removing product N2The gas has high purity up to 95%, and can remove inert gases such as helium (He), neon (Ne), argon (Ar) and the like from natural gas, the combustible natural gas has less components, and N2The recovery rate of the method can reach 99 percent;
4. high recovery rate of purified natural gasLess product loss, CH4The recovery rate can reach 99 percent.
Drawings
FIG. 1 is a schematic view of the device of the present invention
In the figure:
equipment:
1. a raw material natural gas pre-cooling cold box; 2. a raw natural gas evaporator; 3. an absorption tower; 4. a high pressure flash column; 5. a medium pressure flash column; 6. a low pressure flash column; 7. an atmospheric flash column; 8. a solvent circulation pump; 9. a solvent evaporator; 10. a high-pressure flash gas compressor; 11. a high-pressure flash evaporation gas evaporator; 12. a low pressure flash gas compressor; 13. a low-pressure flash evaporation gas air cooler; 14. a high pressure hydraulic turbine; 15. a low pressure hydraulic turbine.
Pipeline:
s0 raw material natural gas inlet pipeline
S1, raw material natural gas precooling outlet pipeline
S2 propane refrigeration raw material natural gas discharge pipeline
S3 discharge pipeline of flash liquid at bottom of absorption tower
S4 discharge pipeline of high-pressure flash liquid
S5 discharge pipeline of medium-pressure flash liquid
S6, low-pressure flash liquid discharge pipeline
S7 discharge pipeline of normal-pressure flash liquid
S8 discharge pipeline at outlet of solvent circulating pump
S9 discharge pipeline of evaporator absorption solvent
S10 discharge pipeline of N2 at top of absorption tower
S11 high-pressure flash evaporation gas discharge pipeline
S12 discharge pipeline of medium-pressure flash evaporation gas
S13, low-pressure flash evaporation gas discharge pipeline
S14 atmospheric flash evaporation gas discharge pipeline
S11 air outlet pipeline of circulating compression device
Discharge pipeline after S15 and N2 reheating
S16 discharge pipeline after high-pressure flash steam is reheated
S17 discharge pipeline after low-pressure flash steam reheating
S18 discharge pipeline after medium-pressure flash evaporation gas reheating
S19 discharge pipeline after atmospheric flash evaporation gas reheating
S20, high-pressure flash evaporation gas compressed discharge pipeline
S21, cooling the high-pressure flash gas and then discharging the cooled high-pressure flash gas
S22 discharge pipeline for compressed normal-pressure flash evaporation gas
S23, cooling atmospheric flash gas and then discharging pipeline
Detailed Description
The process steps of the device of the utility model are as follows: containing N2The natural gas raw material is pre-cooled firstly, then propane refrigeration is carried out to the temperature of minus 25 ℃ to minus 30 ℃, and N is carried out under the condition of 3.0-12.0MPaG2Removing, N removed2Discharging from the top of the absorption tower, reheating with natural gas, and discharging N2The content of methane in the product is less than or equal to 5 percent. The rich liquid at the bottom of the absorption tower is subjected to energy recovery by a hydraulic turbine and then enters a high-pressure flash evaporation tower for high-pressure flash evaporation, the pressure of the high-pressure flash evaporation is 1.5-4.0MPaG, the gas obtained by the high-pressure flash evaporation and the raw natural gas are reheated and then enter a high-pressure flash evaporation gas circulation compressor system to circulate to the bottom of the absorption tower to be used as bottom feeding, and the liquid obtained by the high-pressure flash evaporation is subjected to medium-pressure; the medium-pressure flash evaporation pressure is 0.6-1.5MPaG, the gas flashed out at the medium pressure is reheated with the raw material natural gas and then is used as purified gas to be transported out of the system, and the liquid flashed out at the medium pressure is subjected to low-pressure flash evaporation; the low-pressure flash evaporation pressure is 0.3-0.6MPaG, the gas flashed out at low pressure is reheated with the raw material natural gas and then taken as purified gas to be transported out of the system, and the liquid flashed out at low pressure is subjected to normal-pressure flash evaporation; the atmospheric flash pressure is 0.0MPaG, the gas flashed at the atmospheric pressure enters an atmospheric flash gas booster compressor system after being reheated with the raw material natural gas, the gas is used as purified gas to be sent out of a transportation system after being boosted, the liquid flashed at the atmospheric pressure is sent to a solvent circulating pump to be boosted to 3.4-12.4MPaG, and then the liquid is refrigerated to-30 ℃ by propane to be sent to the top of the absorption tower for recycling.
In the process, the gas flashed at high pressure can be compressed by a high-pressure compressor, air-cooled, cooled by propane and refrigerated to-30 ℃, and then circulated to the bottom of the absorption tower, and the medium-pressure flash gas, the low-pressure flash gas and the normal-pressure flash gas are communicated together to be used as purified gas to be sent out of a system. According to the condition of raw material gas, a medium-pressure booster compressor system and a low-pressure booster compressor system can be additionally arranged.
The device of the utility model can remove the inert gases such as helium (He), neon (Ne), argon (Ar) and the like in the natural gas, and the inert gases are removed along with N2.
In order to fully utilize the energy of the system, the rich liquid at the bottom of the absorption tower can be subjected to high-pressure flash evaporation after being subjected to pressure reduction by a high-pressure hydraulic turbine, and the power of the high-pressure hydraulic turbine is provided for a solvent circulating pump; the liquid flashed out at high pressure is decompressed by a medium-pressure hydraulic turbine and then is subjected to medium-pressure flash evaporation, and the power of the medium-pressure hydraulic turbine is provided for a solvent circulating pump.
The utility model discloses an absorbent that the device adopted is heptane C7, octane (C8), nonane (C9) and decane C10's mixture, and the mass ratio is 10%, 50%, 20% and 20%.
The utility model discloses a device, as shown in fig. 1, including raw materials natural gas precooling cold box 1, raw materials natural gas evaporimeter 2, absorption tower 3, high pressure flash distillation tower 4, middling pressure flash distillation tower 5, low pressure flash distillation tower 6, ordinary pressure flash distillation tower 7, solvent circulating pump 8, solvent evaporator 9, high pressure flash distillation gas compressor 10, high pressure flash distillation gas evaporimeter 11, low pressure flash distillation gas compressor 12, low pressure flash distillation gas air cooler 13.
After the raw material natural gas is preliminarily pre-cooled by a raw material natural gas pre-cooling cold box 1, the raw material natural gas is further cooled by a raw material natural gas evaporator 2 and then is sent to the middle part of an absorption tower 3; n is a radical of2The discharge pipeline S10 is positioned at the top of the absorption tower 3 and is connected with the raw material natural gas pre-cooling cold box 1, and the N after reheating is2The gas in the discharge pipeline S10 is discharged to the high altitude;
a high-pressure hydraulic turbine 14 is arranged on an absorption tower bottom flash liquid discharge pipeline S3, two ends of an absorption tower bottom flash liquid discharge pipeline S3 are respectively positioned at the bottom of the absorption tower 3 and the top of the high-pressure flash tower 4, a medium-pressure hydraulic turbine 15 is arranged on a high-pressure flash liquid discharge pipeline S4, two ends of a high-pressure flash liquid discharge pipeline S4 are respectively positioned at the bottom of the high-pressure flash tower 4 and the top of the medium-pressure flash tower 5, two ends of a high-pressure flash gas discharge pipeline S11 are respectively connected with the top of the high-pressure flash tower 4 and the high-pressure flash gas pipeline S15 of a raw natural gas precooling cold box 1 and connected to an inlet of a high-pressure flash gas compressor 10, a discharge pipeline S20 is connected to a high-pressure flash gas evaporator 11 after compression of high-pressure flash gas, and a discharge pipeline S21; two ends of an intermediate-pressure flash liquid discharge pipeline S5 are respectively positioned at the bottom of the intermediate-pressure flash tower 5 and the top of the low-pressure flash tower 6, two ends of an intermediate-pressure flash gas discharge pipeline S12 are respectively connected with the top of the intermediate-pressure flash tower 5 and the raw material natural gas pre-cooling cold box 1, and gas in the intermediate-pressure flash gas pipeline S18 after reheating in the raw material natural gas pre-cooling cold box 1 is discharged as purified natural gas; two ends of a low-pressure flash liquid discharge pipeline S6 are respectively positioned at the bottom of the low-pressure flash tower 6 and the top of the atmospheric flash tower 7, two ends of a low-pressure flash gas discharge pipeline S13 are respectively connected with the top of the low-pressure flash tower 6 and the feed gas precooling cold box 1, and a low-pressure flash gas pipeline S17 which is reheated by the feed gas precooling cold box 1 is connected with a medium-pressure flash gas pipeline (S18); the two ends of an atmospheric flash liquid discharge pipeline S7 are respectively positioned at the bottom of an atmospheric flash tower 7 and the inlet of a solvent circulating pump 8, the two ends of an atmospheric flash gas discharge pipeline S14 are respectively connected with the top of the atmospheric flash tower 7 and a raw material gas pre-cooling cold box 1, the atmospheric flash gas pipeline S19 reheated by the raw material natural gas pre-cooling cold box 1 enters a low-pressure flash gas compressor 12, a natural gas pipeline S22 supercharged by the low-pressure flash gas compressor 12 is connected to a low-pressure flash gas air cooler 13, and a cooled pipeline S23 is communicated to an intermediate-pressure flash gas pipeline S18; a solvent circulating pump outlet discharge pipeline S8 is respectively connected with the outlet of the solvent circulating pump 8 and the inlet of the solvent evaporator 9, and an evaporator absorption solvent discharge pipeline S9 is connected to the top of the absorption tower 3.
The present invention will be described in detail with reference to the following examples.
Raw material natural gas handling capacity 85 × 104m3/d(0℃，101.325kPaA)
The raw material natural gas comprises the following components:
feed gas composition-content mol/%)
C1：76.71
C2：8.05
C3：0.14
iC4：0.01
nC4：0.02
C5+：0.00
N2：14.30
CO2：0.77
H2S：0.00
The steps are shown in figure 1: 3.2MPaG, 56.7 ℃ N2The raw material natural gas (dehydrated in advance) firstly enters a raw material natural gas pre-cooling cold box 1, is pre-cooled to-22 ℃ by the cold box, is further cooled to-30 ℃ by an evaporator (plate-fin cold box), enters the middle lower part of an absorption tower 3 through a pipeline S1 and contacts with a cold absorbent injected from the top of the absorption tower, and is subjected to N removal under the pressure of 3.0MPaG2Hydrocarbons, CO2Absorbed, non-solvent absorbed N2After being discharged from a pipeline S10 at the top of the absorption tower, the inert gas is reheated by a natural gas precooling cold box 1 as a raw material and then is discharged at high altitude by a pipeline S15; the rich liquid at the bottom of the absorption tower is depressurized by a high-pressure hydraulic turbine 14 and then enters a high-pressure flash tower 4 for high-pressure flash evaporation through a pipeline S3, the pressure of the high-pressure flash evaporation is 1.68MPaG, the gas flashed at high pressure enters a raw material natural gas precooling cold box 1 for reheating through a pipeline S11 and then enters a high-pressure flash evaporation gas compressor 10 through a pipeline S16, the gas is cooled by air and propane for refrigeration to-30 ℃ and then is recycled to the bottom of the absorption tower 3, the liquid flashed at high pressure is depressurized by a medium-pressure hydraulic turbine 15 and then enters a medium-pressure flash tower 5 for medium-pressure flash evaporation through a pipeline S4, the pressure of the medium-pressure flash evaporation gas is 0.6MPaG, the gas flashed at medium pressure enters the raw material natural gas precooling cold box 1 for reheating through a pipeline S12 and then is discharged as purified gas through a pipeline S18, the liquid flashed at medium pressure is depressurized and then enters a low-pressure flash evaporation tower 6 for low-pressure flash evaporation through a pipeline S563268 and then enters a low-pressure flash evaporation gas through a pipeline S3526 and and (4) discharging. The liquid flashed out at low pressure is sent to an atmospheric flash tower 7 through a pipeline S6, the atmospheric flash pressure is 0.0MPaG, the gas flashed out at atmospheric pressure enters a raw material natural gas precooling cold box 1 through a pipeline S14 to be reheated, then is sent to a low-pressure flash gas compressor 12 through a pipeline S19, is pressurized to 0.3MPaG, is air-cooled to 45 ℃, and then is connected to a purified gas pipeline S18 through a pipeline 23. After low-pressure flash evaporationThe solvent is used as a circulating absorbent, the pressure is increased to 3.4MPaG by a solvent circulating pump 8, and the solvent is circulated to the top of the absorption tower 1 by a pipeline S9.
The recovery rate of C1 is 99%, and the recovery rate of C2 is 98.5%;
purifying N in natural gas20.5% of (A);
discharge of N2In N2The purity of the gas is 94.3%, CH4The concentration of (2) is 4.7%;
product N2The gas amount of (A) is 12.8 × 104m3/d(0℃，101.325kPaA)；
Purified natural gas 72.2 × 104m3/d(0℃，101.325kPaA)。
The refrigeration medium of each evaporator used in this example was propane, which was refrigerated to-30 ℃.
Claims (3)
1. A natural gas denitrification device comprises a raw material natural gas precooling cold box (1), a raw material natural gas evaporator (2), an absorption tower (3), a high-pressure flash tower (4), a medium-pressure flash tower (5), a low-pressure flash tower (6), a normal-pressure flash tower (7), a solvent circulating pump (8), a solvent evaporator (9), a high-pressure flash gas compressor (10), a high-pressure flash gas evaporator (11), a low-pressure flash gas compressor (12) and a low-pressure flash gas air cooler (13),
after being preliminarily pre-cooled by a raw natural gas pre-cooling cold box (1), the raw natural gas is further cooled by a raw natural gas evaporator (2) and then is sent to the middle part of an absorption tower (3); n is a radical of2The discharge pipeline is positioned at the top of the absorption tower (3) and connected with the raw material natural gas pre-cooling cold box (1), and the N after reheating is2The gas in the discharge pipeline is discharged;
two ends of a flash liquid discharge pipeline at the bottom of the absorption tower are respectively positioned at the bottom of the absorption tower (3) and the top of the high-pressure flash tower (4), two ends of a high-pressure flash liquid discharge pipeline are respectively positioned at the bottom of the high-pressure flash tower (4) and the top of the medium-pressure flash tower (5), two ends of the high-pressure flash gas discharge pipeline are respectively connected with the top of the high-pressure flash tower (4) and a high-pressure flash gas pipeline of a raw natural gas pre-cooling cold box (1) discharge cold box and are connected to an inlet of a high-pressure flash gas compressor (10), a discharge pipeline after the high-pressure flash gas is compressed is connected to a high-pressure flash gas evaporator (11), and the discharge pipeline after the high-; two ends of the medium-pressure flash liquid discharge pipeline are respectively positioned at the bottom of the medium-pressure flash tower (5) and the top of the low-pressure flash tower (6), two ends of the medium-pressure flash gas discharge pipeline are respectively connected with the top of the medium-pressure flash tower (5) and the raw material natural gas pre-cooling cold box (1), and gas in the medium-pressure flash gas pipeline after reheating by the raw material natural gas pre-cooling cold box (1) is discharged as purified natural gas; two ends of a low-pressure flash evaporation liquid discharge pipeline are respectively positioned at the bottom of the low-pressure flash evaporation tower (6) and the top of the atmospheric flash evaporation tower (7), two ends of the low-pressure flash evaporation gas discharge pipeline are respectively connected with the top of the low-pressure flash evaporation tower (6) and the raw material gas pre-cooling cold box (1), and the low-pressure flash evaporation gas pipeline reheated by the raw material natural gas pre-cooling cold box (1) is connected with a medium-pressure flash evaporation gas pipeline; the two ends of an atmospheric flash liquid discharge pipeline are respectively positioned at the bottom of an atmospheric flash tower (7) and an inlet of a solvent circulating pump (8), the two ends of the atmospheric flash gas discharge pipeline are respectively connected with the top of the atmospheric flash tower (7) and a raw material gas pre-cooling cold box (1), the atmospheric flash gas pipeline reheated by the raw material natural gas pre-cooling cold box (1) enters a low-pressure flash gas compressor (12), a natural gas pipeline pressurized by the low-pressure flash gas compressor (12) is connected to a low-pressure flash gas air cooler (13), and the cooled pipeline is communicated to a medium-pressure flash gas pipeline; the outlet and discharge pipeline of the solvent circulating pump is respectively connected with the outlet of the solvent circulating pump (8) and the inlet of the solvent evaporator (9), and the evaporator absorption solvent discharge pipeline is connected to the top of the absorption tower (3).
2. The apparatus of claim 1, further comprising a high pressure hydraulic turbine (14), the high pressure hydraulic turbine (14) being disposed on the absorption bottoms flash liquid discharge line.
3. An apparatus according to claim 1, characterized in that the apparatus further comprises a medium pressure hydraulic turbine (15), the medium pressure hydraulic turbine (15) being arranged on the high pressure flash liquid discharge line.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920617977.6U CN211079068U (en) | 2019-04-30 | 2019-04-30 | Natural gas denitrification device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920617977.6U CN211079068U (en) | 2019-04-30 | 2019-04-30 | Natural gas denitrification device |
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