CN114440549A - Computer control method for natural gas cryogenic denitrification process - Google Patents

Computer control method for natural gas cryogenic denitrification process Download PDF

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CN114440549A
CN114440549A CN202011212442.4A CN202011212442A CN114440549A CN 114440549 A CN114440549 A CN 114440549A CN 202011212442 A CN202011212442 A CN 202011212442A CN 114440549 A CN114440549 A CN 114440549A
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gas
computer control
flow
liquid
additive
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CN114440549B (en
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梁尚斌
战征
翟科军
赵毅
汤晟
周勇
赵德银
崔瑞雪
钟荣强
姚丽蓉
常小虎
任广欣
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China Petroleum and Chemical Corp
Sinopec Northwest Oil Field Co
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China Petroleum and Chemical Corp
Sinopec Northwest Oil Field Co
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Abstract

A computer control method for a cryogenic denitrification process of natural gas relates to the technical field of natural gas impurity removal. The method comprises the following steps: firstly, receiving real-time gas flow and liquid flow data by computer control equipment to form a gas flow and liquid flow function; secondly, detecting the liquid content condition of the input raw material gas by computer control equipment; and thirdly, dynamically adjusting the content of the additive by the computer control equipment according to the liquid content condition of the input raw material gas. The computer control technology for the cryogenic denitrification process of the natural gas has the advantages of high production efficiency, high impurity removal rate and capability of performing flexible treatment on sudden change of natural gas components in time.

Description

Computer control method for natural gas cryogenic denitrification process
Technical Field
The invention relates to the technical field of natural gas impurity removal, in particular to a computer control method for a cryogenic denitrification process of natural gas.
Background
The natural gas is used as a high-quality fuel and an important chemical raw material, the application of the natural gas increasingly draws attention of people, and the trend of accelerating the development of the natural gas industry is in the world at present. However, natural gas produced in many oil and gas fields often contains a large amount of nitrogen, and natural gas with high nitrogen content has low calorific value and large energy consumption in the gathering and transportation process, and cannot be directly used as fuel. Therefore, denitrification of natural gas is an important condition for making full use of natural gas. The natural gas denitrification processes currently used in industry include: solvent absorption, pressure swing adsorption, selective adsorption and cryogenic methods.
The solvent absorption method denitrification has mild operation conditions, does not need to remove carbon dioxide, and most of equipment and pipelines are made of carbon steel, so that the operation flexibility is high, and the solvent absorption method denitrification process has good application prospects, but the solvent absorption method denitrification process usually has the following defects: 1) in the process of absorbing methane by the solvent, a small amount of nitrogen components are inevitably absorbed, so that in order to improve the denitrification efficiency and the product quality of the natural gas, the gas flow which is discharged from the first-stage flash tank and has high nitrogen content is compressed and then returns to the absorption tower for secondary absorption; in this case, if the nitrogen content of the feed gas stream changes, for example: the nitrogen content is obviously increased, and the nitrogen content in the product gas of the whole denitrification system is obviously increased due to the reflux of the gas discharged from the first-stage flash tank to the absorption tower, namely, the prior art is too sensitive to the composition mutation of the raw material gas flow and is not suitable for maintaining the output of the product gas with stable composition; 2) the above method also has a technical scheme that the gas discharged from the first-stage flash tank is not refluxed to the absorption tower, but the technical scheme directly discharges the gas discharged from all the first-stage flash tanks, so that the method causes more production loss and is not beneficial to controlling the cost.
The pressure swing adsorption process utilizes the characteristic that the adsorption capacity of each component in natural gas has obvious difference along with the pressure difference to achieve the purpose of separation, and in order to ensure the continuity of the process, the process needs to adopt a multi-tower process, for example, Chinese patent application 201610758279.9 discloses a novel oilfield associated gas denitrification device and process, the denitrification device comprises a liquid-gas separator, a dewatering device, a cooler, a gas-liquid separator, a refrigeration system, a heating furnace, a pressure swing adsorption denitrification tower, a vacuum pump, a storage tank and the like, the denitrification process is to firstly remove water vapor and C2+ light hydrocarbon in mixed gas, avoid the pollution to an adsorbent and then carry out pressure swing adsorption to remove nitrogen, the nitrogen content of the enriched product gas is less than or equal to 3 percent, thereby achieving the commercial quality requirement, but the adsorbent can be used in the adsorption process and is easy to be polluted, therefore, carbon dioxide needs to be used in the removal process, Removing C2+ light hydrocarbon.
The deep cooling process has large treatment capacity on natural gas, high nitrogen removal rate and mature and reliable technology. For example, chinese patent application 201410311707.4 discloses a process for removing nitrogen from natural gas, which comprises the steps of: BOG gas in the LNG storage tank enters a BOG pressurization system after being reheated by a BOG cold box, and is pressurized to 0.6-1.5 Mpa; then, BOG is cooled to-154 to-165 ℃ liquid after passing through a BOG cold box and a liquefaction cold box in sequence, then enters a denitrification heat exchanger to be further cooled to-168 to-176 ℃, the temperature is reduced to-178 to-185 ℃ after throttling expansion, nitrogen which is separated by nitrogen removal equipment is discharged at a high point, purified natural gas is recycled to an LNG storage tank, however, the cryogenic process has strict requirements on the natural gas pretreatment process, carbon dioxide, water and other particle impurities in raw natural gas must be removed, otherwise, the impurities can be solidified or hydrate at the cryogenic temperature, and pipeline blockage accidents are caused. The existing pretreatment process is lack of computer intervention, has low automation degree, reduces the production efficiency and the removal rate of impurities, is operated according to a fixed set parameter according to a set program although a computer is adopted, and has hidden danger due to the lack of a flexible treatment mechanism in emergency.
Therefore, it is necessary to develop a device and a computer control technology for a cryogenic denitrification process of natural gas, which has high production efficiency and high impurity removal rate and can perform flexible treatment on sudden change of natural gas components in time.
Disclosure of Invention
Based on the defects and shortcomings in the prior art, the invention aims to provide equipment and a computer control technology for a natural gas cryogenic denitrification process, which have high production efficiency and high impurity removal rate and can perform flexible treatment on sudden change of natural gas components in time.
The technical scheme adopted by the invention for solving the technical problems is as follows:
a computer control method for a cryogenic denitrification process of natural gas relates to a device comprising a pretreatment module.
A computer control method for a cryogenic denitrification process of natural gas comprises the following steps:
firstly, receiving real-time gas flow and liquid flow data by computer control equipment to form a gas flow and liquid flow function;
specifically, the computer control apparatus measures real-time gas flow G1 and liquid flow L1 via the centrifugal separator gas flow measurement apparatus and liquid flow measurement apparatus and forms gas flow and liquid flow functions G1(t) and L1(t) over time;
secondly, detecting the liquid content condition of the input raw material gas by computer control equipment;
specifically, the computer control device measures and sets the time difference Δ t1 between the gas entering the centrifugal separator and the liquid falling into the collector by means of experiment or the like. For example, the point in time of gas flow can be determined during initial aeration by sudden changes in a barometer or flow meter at a critical location on the pipeline. This time difference is substantially fixed because the pressure of the natural gas is tightly controlled during its transit in the pipeline. Thus. The ratio of G1(t)/L1(t + delta t1) is calculated, and the historical average value of the ratio is calculated, namely the liquid content condition of the input raw material gas is detected.
Thirdly, dynamically adjusting the content of the additive by the computer control equipment according to the liquid content condition of the input raw material gas;
specifically, when the absolute value of the difference between the ratio of G1(t)/L1(t + Δ t1) and the historical average value is within a first preset range, which may be preferably within 10% of the historical average value, the computer control apparatus controls the total flow rate of the additive flow meters of the plurality of nozzles at the time point of t + Δ t1+ Δ t2 to be the first flow rate F1. Here, Δ t2 is a time difference between when the gas flows out through the centrifugal separator exhaust port and then flows into the mixer inlet via the dryer, and this time difference is measured and set by a method such as an experiment. For example, the time point at which the gas flows may be determined by sudden changes in a barometer or a flow meter at a critical position on the pipeline during the initial ventilation, or may be estimated by bernoulli's law using parameters such as the size of the pipeline and the gas pressure. This time difference is substantially fixed because the pressure of the natural gas is tightly controlled during its transit in the pipeline.
Wherein the content of the first and second substances,
Figure BDA0002759263040000031
wherein qg is the loss amount of the inhibitor with the injection concentration of c1 in a gas phase, kg/d;
cl is the concentration,% (w) of injected inhibitor
qw is the amount of liquid water produced in the embodiment in unit time, kg/d;
cm the concentration after inhibitor loss after inhibitor injection is% (w).
When the absolute value of the difference between the ratio of G1(t)/L1(t + Δ t1) and the historical average value exceeds a first preset range, but the ratio of G1(t)/L1(t + Δ t1) does not exceed a second threshold range, preferably, the second preset value may be 15% or less, and the computer control apparatus controls the total flow rate of the additive flow meters of the plurality of nozzles at the time point of t + Δ t1+ Δ t2 to be a second flow rate F2. The second flow rate F2 is greater than the first flow rate F1, and preferably the ratio of the second flow rate to the first flow rate may be the ratio of the historical average of G1(t)/L1(t + Δ t1) to G1(t)/L1(t + Δ t 1).
When the ratio of G1(t)/L1(t + Δ t1) exceeds the second threshold range (in this case, the absolute value of the difference between the ratio of G1(t)/L1(t + Δ t1) and the historical average value has certainly exceeded the first preset range), the computer control apparatus controls the total flow rate of the additive flow meters of the plurality of nozzles at the time point of t + Δ t1+ Δ t2 to be the third flow rate F3, and the computer control apparatus increases the temperature of the heaters with which the nozzles are provided by 20% to 30%.
Wherein, the value of F3 can be {1+ [ historical average value of G1(t)/L1(t + delta t1)/G1(t)/L1(t + delta t1) } F1+ qg,
Figure BDA0002759263040000041
wherein qg is the loss amount of an inhibitor (such as methanol) with the concentration of cl injected into the system in a gas phase, kg/d;
cm concentration after inhibitor loss after inhibitor injection is% (w);
cl is the concentration of injected inhibitor,% (w);
qnG is the natural gas flow in the system, m3/d。
In the implementation process, the loss amount of the additive is increased due to the fact that the heating temperature is increased by improving the adding efficiency of the additive, so that the loss item of the additive needs to be considered when the moisture is extremely high, and in other cases, the total amount of the additive is not large and the heating temperature is not high, and the loss item can be ignored and is not remembered.
In the working process, firstly, the raw material gas is treated by a pretreatment module and then enters a raw material-product heat exchanger, and the natural gas is cooled to-124 ℃ and then enters a high-pressure tower for primary separation; the tower is internally provided with a rectifying section, and the operating pressure is 2.4 MPa. And (3) extracting a gas flow from the top of the high-pressure tower, further cooling the gas flow to-168 ℃ in a condenser/reboiler, and returning the gas flow to the high-pressure tower for gas-liquid separation. The separated gas phase fraction was crude nitrogen with a purity of about 50% with a recovery of about 90%. The low-pressure column is operated at 0.24MPa, the temperature at the top of the column being about-187 ℃ and the temperature at the bottom of the column being about-157 ℃. After the fluid discharged from the bottom of the high-pressure tower is rectified by the low-pressure tower, the volume fraction of nitrogen in the liquefied natural gas (LNC) is reduced to be below 3 percent, and the LNG recovery rate is more than 99.5 percent. And the nitrogen with higher purity discharged from the top of the low-pressure tower is discharged to the air or is utilized after cold energy is recovered.
The pretreatment module is connected with a centrifugal separator, additive injection equipment and molecular sieve equipment in sequence from the direction from the natural gas feed gas inlet end to the outlet end, and the centrifugal separator and the additive injection equipment are connected with computer control equipment.
The centrifugal separator comprises a main body, a raw material gas inlet, a lower discharge port, a lower discharge pipeline, a liquid collector and a gas discharge port;
the main body is in a funnel shape with a big top and a small bottom, a raw material gas inlet is formed in the upper portion of the side wall of the main body of the centrifugal separator, and a gas flow measuring device is arranged at the raw material gas inlet and connected with a computer control device and transmits data in real time.
The lower discharge port is positioned at the bottom of the separator body, and the gas discharge port is positioned at the top of the separator body.
A lower discharge pipeline and a collector are arranged at the lower part of the lower discharge port;
the lower drainage pipeline is connected with the lower drainage port through a screw buckle, so that the replacement and the maintenance are convenient; the internal diameter of the lower drainage pipeline is not more than 2 cm, a filter screen is arranged in the lower drainage pipeline, and the filter screen is arranged at the top, the bottom or the interruption of the lower drainage pipeline; the filter screen is used for filtering solid particles in the discharged impurities, and the diameter of a filter hole of the filter screen is less than 10 microns.
The collector is located at the lower end of the downcomer and is used to collect the filtered downcomer liquid (mostly water). The collector is provided with a liquid flow measuring device, so that the collector has the function of measuring the liquid flow.
In some preferred embodiments, a water level measuring device or a water flow measuring device can be arranged in the collector.
The liquid flow measuring device is connected with the computer control device through a data line, and the liquid flow data is transmitted to the computer control device in real time through the data line.
Because the inertia of the large liquid drops formed by the particles and the water in the raw material gas is larger than the effective component molecules in the natural gas, the centrifugal separator throws the large liquid drops formed by the impurity particles and the water in the raw material gas to the inner wall of the main body under the action of inertial centrifugal force so as to be separated from the gas flow, the large liquid drops slide to the lower discharge port at the bottom of the main body along the inner wall to be discharged, and the purified gas spirally moves from bottom to top near the central shaft and is finally discharged from the gas discharge port at the top.
The gas discharged through the gas discharge port enters the additive injection device, which includes an additive reservoir, an additive delivery device (pump and flow meter), and a mixing tower.
The upper part of the mixing tower is provided with a raw material gas inlet, the middle part of the mixing tower is provided with a plurality of baffles, and the inner cavity of the mixing tower is divided into continuous S-shaped passages through the baffles, so that gas can be fully contacted with the additive.
The additive storage device is positioned below the mixing tower and is used for storing an additive, and the additive can be methanol.
The additive storage device is connected with the mixing tower through a pipeline, and a pump and an additive flow meter are arranged on the pipeline; the pump is used for pumping out the additive; the pump and the flowmeter are both connected with computer control equipment; the flow meter and the pump are controlled by the computer control device.
The pipeline extends to the side wall of the mixing tower, the height direction of the pipeline is completely overlapped with the side wall of the mixing tower, a plurality of nozzles are arranged at the tail end of the pipeline, the nozzles are uniformly distributed on the height and extend into the mixing tower, and the additive is uniformly provided for the mixing tower. The nozzles are provided with heating devices, the heating devices are used for heating the additives to gasify the additives and spray the additives into the mixing tower, and the heating devices are connected to and controlled by the computer control equipment.
Preferably, the gas output of the nozzle may decrease from top to bottom, and since the gas flows from top to bottom, a high concentration of additive above may facilitate good mixing.
In some preferred embodiments, the heating device is installed at a position far away from the mixing tower and does not influence the gasification.
And a gas outlet is also formed below the mixing tower, and the mixed raw material gas is discharged from the gas outlet.
And the gas output port is connected with the inlet of the molecular sieve equipment.
The feed gas discharged through the gas outlet is then passed through a molecular sieve device to remove as much as possible residual moisture or moisture due to the addition of additives, and a molecular sieve having a molecular sieve pore size of 3.9 angstroms is selected for screening because the molecular size of methanol and methane is about 3.8 angstroms and the molecular size of water is 4 angstroms. The raw material gas passing through the molecular sieve can be used as gas to be treated and enters the cryogenic process equipment for denitrification.
Compared with the prior art, the invention has the beneficial effects that:
(1) in the implementation process, the content of the additive can be flexibly adjusted in real time through real-time detection and control of computer control equipment according to the change of the water content of the natural gas, so that the generation of hydrates in the subsequent process is further prevented;
(2) the necessary parameters such as pressure and flow rate in the invention can be measured and controlled by arranging a corresponding pressure gauge or flowmeter in the pipeline;
(3) the computer control technology for the cryogenic denitrification process of the natural gas has the advantages of high production efficiency, high impurity removal rate and capability of performing flexible treatment on sudden change of natural gas components in time.
Drawings
FIG. 1 is a structural view of an apparatus for cryogenic denitrification of natural gas according to embodiment 1 of the present invention;
FIG. 2 is a schematic structural diagram of a pretreatment module of a cryogenic denitrification process for natural gas according to embodiment 2 of the invention;
FIG. 3 is a flow chart of a computer control method of the cryogenic denitrification process for natural gas according to embodiment 3 of the invention.
Reference numerals: m-pretreatment module, N0-raw material-product heat exchanger, N1-plate-warping heat exchanger, K1-high pressure tower, K2-low pressure tower, Q-condenser/reboiler, W-LNG pump;
an A-flow meter, a B-air inlet, a C-centrifugal separator, a D-additive injection device, an E-gas outlet, an E-lower discharge port, an F-lower discharge pipeline, a Y-filter, an L-main body, a z-collector, a P-mixing tower, a U-baffle, an X-nozzle, an R-heater, an a-air outlet, a B-additive storage device, an F-molecular sieve filtering device and a v-computer control device.
Detailed Description
The equipment and the computer control technology for the cryogenic denitrification process of the natural gas of the invention are further described in detail below.
The present invention will now be described in more detail with reference to the accompanying drawings, in which preferred embodiments of the invention are shown, it being understood that one skilled in the art may modify the invention herein described while still achieving the beneficial results of the present invention. Accordingly, the following description should be construed as broadly as possible to those skilled in the art and not as limiting the invention.
In the interest of clarity, not all features of an actual implementation are described. In the following description, well-known functions or constructions are not described in detail since they would obscure the invention in unnecessary detail. It will of course be appreciated that in the development of any such actual embodiment, numerous implementation-specific details must be set forth in order to achieve the developer's specific goals.
EXAMPLE 1 apparatus for cryogenic Denitrification of Natural gas
Referring to fig. 1, in the working process, firstly, the raw material gas is treated by a pretreatment module M, enters a raw material-product heat exchanger N0, cools the natural gas to-124 ℃, and enters a high-pressure tower K1 for preliminary separation; the tower is internally provided with a rectifying section, and the operating pressure is 2.4 MPa. A gas flow is extracted from the top of the high-pressure tower K1 and is further cooled to-168 ℃ in a condenser/reboiler Q, and then the gas flow returns to the high-pressure tower K1 for gas-liquid separation. The separated gas phase fraction was crude nitrogen with a purity of about 50% with a recovery of about 90%. The low-pressure column K2 was operated at 0.24MPa, with a head temperature of about-187 ℃ and a bottom temperature of about-157 ℃. After the fluid discharged from the bottom of the high-pressure tower K1 is rectified by the low-pressure tower K2, the volume fraction of nitrogen in liquefied natural gas (LNC) is reduced to below 3 percent, and the LNG recovery rate is more than 99.5 percent. The nitrogen with higher purity discharged from the top of the low-pressure tower K2 is discharged to the air or used after cold energy is recovered.
Embodiment 2A pretreatment Module as described in embodiment 1
Referring to fig. 2, the pretreatment module M is sequentially connected with a centrifugal separator C, an additive injection device D and a molecular sieve device f from the natural gas feed gas inlet end to the outlet end, and the centrifugal separator C and the additive injection device D are connected with a computer control device v.
The centrifugal separator C comprises a main body L, a raw material gas inlet B, a lower discharge port E, a lower discharge pipeline F, a liquid collector z and a gas discharge port E;
the main body L is in a funnel shape with a large upper part and a small lower part, a raw material gas inlet B is formed in the upper part of the side wall of the main body L of the centrifugal separator, a gas flow measuring device is arranged at the raw material gas inlet B, and the gas flow measuring device is connected with a computer control device v and transmits data in real time.
The lower discharge port E is positioned at the bottom of the separator body L, and the gas discharge port E is positioned at the top of the separator body L.
A lower drainage pipeline F and a collector z are arranged at the lower part of the lower drainage port e;
the lower drainage pipeline F is connected with the lower drainage port e through a screw buckle, so that the replacement and the maintenance are convenient; the lower drainage pipeline F is a pipeline with the inner diameter not more than 2 cm, a filter screen is arranged in the lower drainage pipeline F, and the filter screen is arranged at the top, the bottom or interrupted part of the lower drainage pipeline F; the filter screen is used for filtering solid particles in the leaked impurities, and the diameter of a filter hole of the filter screen is less than 10 micrometers.
The collector z is located at the lower end of the downcomer F and is used to collect the filtered downcomer liquid (mostly water). The collector z is provided with a liquid flow rate measuring device, so that the collector z has a function of measuring a liquid flow rate.
The collector z may be provided with a water level measuring device or a water flow measuring device.
The liquid flow measuring device is connected with the computer control device v through a data line, and the liquid flow data is transmitted to the computer control device v through the data line in real time.
Because the inertia of the large liquid drops formed by the particles and the water in the raw material gas is larger than the effective component molecules in the natural gas, the centrifugal separator C throws the large liquid drops formed by the impurity particles and the water in the raw material gas to the inner wall of the main body by the action of inertial centrifugal force so as to be separated from the gas flow, and the large liquid drops slide to the lower discharge port E at the bottom of the main body along the inner wall for discharge, and the purified gas spirally moves from bottom to top near the central shaft and is finally discharged from the gas discharge port E at the top.
The gas discharged through the gas discharge port E enters the additive injection device D, which includes an additive reservoir b, an additive delivery device (pump and flow meter), and a mixing tower P.
The upper part of the mixing tower P is provided with a raw material gas inlet, the middle part of the mixing tower P is provided with a plurality of baffles U, and the inner cavity of the mixing tower P is divided into continuous S-shaped passages through the baffles U, so that gas can be fully contacted with additives.
The additive storage b is positioned below the mixing tower P and is used for storing an additive, and the additive is methanol.
The additive storage b is connected with the mixing tower P through a pipeline, and a pump and an additive flow meter are arranged on the pipeline; the pump is used for pumping out the additive; the pump and the flowmeter are both connected with computer control equipment; the flow meter and the pump are controlled by the computer control device.
The pipeline extends to the side wall of the mixing tower P, the height direction of the pipeline is completely overlapped with the side wall of the mixing tower P, a plurality of nozzles X are arranged at the tail end of the pipeline, the nozzles X are uniformly distributed on the height and extend into the mixing tower P to uniformly provide additives for the mixing tower P. The nozzles X are respectively provided with a heating device, the heating devices are used for heating the additive to gasify the additive and spray the additive into the mixing tower P, and the heating devices are connected to and controlled by the computer control equipment v.
The gas output of the nozzle X can be reduced from top to bottom, and since the gas flows from top to bottom, a high additive concentration at the top can facilitate thorough mixing.
The heating device is arranged at a position far away from the mixing tower P and does not influence the gasification.
And a gas outlet is also formed below the mixing tower P, and the mixed raw material gas is discharged from the gas outlet E.
And the gas output port E is connected with the inlet of the molecular sieve device f.
The feed gas exiting E through the gas outlet is then passed through a molecular sieve device f to remove as much as possible residual moisture or moisture due to the addition of additives, and a molecular sieve having a molecular sieve pore size of 3.9 angstroms is selected for screening because the molecular size of methanol and methane is about 3.8 angstroms and the molecular size of water is 4 angstroms. The raw material gas passing through the molecular sieve can be used as the gas to be treated and enters the cryogenic process equipment for denitrification.
Embodiment 3 computer control method of cryogenic denitrification process for natural gas
Referring to fig. 3, the method comprises the steps of:
firstly, receiving real-time gas flow and liquid flow data by computer control equipment v to form a gas flow and liquid flow function;
specifically, computer control device v measures gas flow G1 and liquid flow L1 in real time via centrifugal separator C gas flow measurement device and liquid flow measurement device and forms gas flow and liquid flow as a function of time G1(t) and L1 (t);
secondly, detecting the liquid content condition of the input raw material gas by the computer control equipment v;
specifically, the computer control device v determines and sets the time difference Δ t1 between the gas entering the centrifugal separator C and the liquid falling into the collector z by means of experiment or the like; for example, the point in time at which the gas flows can be determined during initial ventilation by sudden changes in the gas pressure gauge or flow meter at strategic locations on the pipeline. This time difference is substantially fixed because the pressure of the natural gas is tightly controlled during its transit in the pipeline. Thus. The ratio of G1(t)/L1(t + delta t1) is calculated, and the historical average value of the ratio is calculated, namely the liquid content condition of the input raw material gas is detected.
Thirdly, dynamically adjusting the content of the additive by the computer control equipment according to the liquid content condition of the input raw material gas;
specifically, when the absolute value of the difference between the ratio of G1(t)/L1(t + Δ t1) and the historical average value is within a first preset range, which may be preferably within 10% of the historical average value, the computer control apparatus controls the total flow rate of the additive flow meters of the plurality of nozzles at the time point of t + Δ t1+ Δ t2 to be the first flow rate F1. Here, Δ t2 is a time difference between when the gas flows out through the centrifugal separator exhaust port and then flows into the mixer inlet via the dryer, and this time difference is measured and set by a method such as an experiment. For example, the time point at which the gas flows may be determined by sudden changes in a barometer or a flow meter at a critical position on the pipeline during the initial ventilation, or may be estimated by bernoulli's law using parameters such as the size of the pipeline and the gas pressure. This time difference is substantially fixed because the pressure of the natural gas is tightly controlled during its transit in the pipeline.
Wherein the content of the first and second substances,
Figure BDA0002759263040000101
wherein qg is the loss amount of the inhibitor with the injection concentration of c1 in a gas phase, kg/d;
cl is the concentration,% (w) of injected inhibitor
qw is the amount of liquid water produced in the embodiment in unit time, kg/d;
cm the concentration after inhibitor loss after inhibitor injection is% (w).
When the absolute value of the difference between the ratio of G1(t)/L1(t + Δ t1) and the historical average value exceeds a first preset range, but the ratio of G1(t)/L1(t + Δ t1) does not exceed a second threshold range, preferably, the second preset value may be 15% or less, and the computer control apparatus controls the total flow rate of the additive flow meters of the plurality of nozzles at the time point of t + Δ t1+ Δ t2 to be a second flow rate F2. The second flow rate F2 is greater than the first flow rate F1, and the ratio of the second flow rate to the first flow rate can be the ratio of the historical average of G1(t)/L1(t + Δ t1) to G1(t)/L1(t + Δ t 1).
When the ratio of G1(t)/L1(t + Δ t1) exceeds the second threshold range (in this case, the absolute value of the difference between the ratio of G1(t)/L1(t + Δ t1) and the historical average value has certainly exceeded the first preset range), the computer control apparatus controls the total flow rate of the additive flow meters of the plurality of nozzles at the time point of t + Δ t1+ Δ t2 to be the third flow rate F3, and the computer control apparatus increases the temperature of the heaters with which the nozzles are provided by 20% to 30%.
Wherein, the value of F3 can be {1+ [ historical average value of G1(t)/L1(t + delta t1)/G1(t)/L1(t + delta t1) } F1+ qg,
Figure BDA0002759263040000111
wherein qg is the loss amount of an inhibitor (such as methanol) with the concentration of cl injected into the system in a gas phase, kg/d;
cm concentration after inhibitor loss after inhibitor injection is% (w);
cl is the concentration of injected inhibitor,% (w);
qnG is the natural gas flow in the system, m3/d。
Since the heating temperature is increased by increasing the efficiency of the additive addition, the loss of the additive is increased, so that the loss term of the additive needs to be considered when the moisture is extremely high, and in other cases, the total amount of the additive is not large and the heating temperature is not high, and the loss term can be ignored.
According to the invention, the content of the additive is flexibly adjusted in real time through real-time detection and control of the computer control equipment according to the change of the water content of the natural gas, so that the generation of hydrates in the subsequent process is further prevented.
The necessary parameters of the invention, such as pressure and flow rate, can be measured and controlled by arranging a corresponding pressure gauge or flow meter in the pipeline. Although the air pump, the pressure relief port, and the like necessary for producing or maintaining the air pressure in the piping are omitted for the sake of simplifying the technical solution, those skilled in the art can reasonably determine the position where the above-described necessary component is provided based on the technical knowledge grasped by the present application.
The computer control technology for the cryogenic denitrification process of the natural gas, provided by the invention, has the advantages of high production efficiency, high impurity removal rate and capability of performing flexible treatment on sudden change of natural gas components in time.
The foregoing shows and describes the general principles, essential features and advantages of the invention, which is, therefore, described only as an example of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, which are merely illustrative of the principles of the invention, but rather that the invention includes various equivalent changes and modifications without departing from the spirit and scope of the invention, which fall within the scope of the invention as claimed. The scope of the invention is defined by the appended claims and equivalents thereof.

Claims (10)

1. A computer control method for a cryogenic denitrification process of natural gas is characterized by comprising the following steps: the method comprises the following steps: the device related to the method comprises a preprocessing module; the pretreatment module is connected with a centrifugal separator, additive injection equipment and molecular sieve equipment in sequence from the direction from the natural gas feed gas inlet end to the outlet end, and the centrifugal separator and the additive injection equipment are connected with computer control equipment.
2. A computer control method for a natural gas cryogenic denitrification process of denitrification equipment is characterized by comprising the following steps: the method comprises the following steps:
firstly, receiving real-time gas flow and liquid flow data by computer control equipment to form a gas flow and liquid flow function;
secondly, detecting the liquid content condition of the input raw material gas by computer control equipment;
and thirdly, dynamically adjusting the content of the additive by the computer control equipment according to the liquid content condition of the input raw material gas.
3. The computer-controlled method of claim 1, wherein: the method for receiving real-time gas flow and liquid flow data and forming the gas flow and liquid flow functions in the first step comprises the following steps: the computer control device measures real-time gas flow G1 and liquid flow L1 via the centrifugal separator gas flow measuring device and liquid flow measuring device and forms functions G1(t) and L1(t) of the gas flow and liquid flow with respect to time.
4. The computer-controlled method of claim 2, wherein: the method for detecting the liquid content of the input raw material gas in the second step comprises the following steps: the computer control device depends on the time difference at 1 between the gas entering the centrifugal separator and the liquid falling into the collector.
5. The computer-controlled method of claim 4, wherein: the time difference Δ t1 is measured and set through a test mode; the time point of gas flowing through can be judged by sudden change of a barometer or a flow meter at a key position on a pipeline in the initial aeration process, the ratio of G1(t)/L1(t + delta t1) is calculated, and the historical average value of the ratio is calculated, namely the liquid content condition of the input raw material gas is detected.
6. The computer-controlled method of claim 2, wherein: the third step, the method for dynamically adjusting the content of the additive according to the liquid content of the input raw material gas, comprises the following steps: when the absolute value of the difference between the ratio of G1(t)/L1(t + Δ t1) and the historical average is within a first preset range, which may be within 10% of the historical average, the computer control apparatus controls the total flow rate of the additive flow meters of the plurality of nozzles at the time point of t + Δ t1+ Δ t2 to be a first flow rate F1;
in (1),
Figure FDA0002759263030000021
wherein qg is the loss amount of the inhibitor with the injection concentration of c1 in a gas phase, kg/d;
cl is the concentration,% (w) of injected inhibitor
qw is the amount of liquid water produced in the embodiment in unit time, kg/d;
cm the concentration after inhibitor loss after inhibitor injection is% (w).
7. The computer-controlled method of claim 6, wherein: Δ t2 is the time difference between the gas flowing out through the centrifugal separator exhaust port and flowing into the mixing tower inlet through the dryer.
8. The computer-controlled method of claim 2, wherein: the third step is that the method for dynamically adjusting the content of the additive according to the liquid content of the input raw material gas comprises the following steps: when the absolute value of the difference between the ratio of G1(t)/L1(t + Δ t1) and the historical average value exceeds a first preset range, but the ratio of G1(t)/L1(t + Δ t1) does not exceed a second threshold range, the second preset value may be 15% or less, and the computer control apparatus controls the total flow rate of the additive flow meters of the plurality of nozzles at the time point of t + Δ t1+ Δ t2 to be a second flow rate F2.
9. The computer-controlled method of claim 8, wherein: the second flow rate F2 is greater than the first flow rate F1, and the ratio of the second flow rate to the first flow rate may be the ratio of the historical average values of G1(t)/L1(t + Δ t1) and G1(t)/L1(t + Δ t 1).
10. The computer-controlled method of claim 8, wherein: when the ratio of G1(t)/L1(t + Δ t1) exceeds the second threshold range, in which case the absolute value of the difference between the ratio of G1(t)/L1(t + Δ t1) and the historical average value has necessarily exceeded the first preset range, the computer control apparatus controls the total flow rate of the additive flow meters of the plurality of nozzles at the time point of t + Δ t1+ Δ t2 to be the third flow rate F3,
wherein, the value of F3 can be {1+ [ historical average value of G1(t)/L1(t + delta t1)/G1(t)/L1(t + delta t1) } F1+ qg,
Figure FDA0002759263030000022
wherein qg is the loss amount of an inhibitor (such as methanol) with the concentration of cl injected into the system in a gas phase, kg/d;
cm concentration after inhibitor loss after inhibitor injection is% (w);
cl is the concentration of injected inhibitor,% (w);
qnG is natural in the systemFlow rate of gas, m3/d。
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