CN111500331A - Natural gas decarburization experimental device with semi-barren solution logistics - Google Patents
Natural gas decarburization experimental device with semi-barren solution logistics Download PDFInfo
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- CN111500331A CN111500331A CN202010343897.3A CN202010343897A CN111500331A CN 111500331 A CN111500331 A CN 111500331A CN 202010343897 A CN202010343897 A CN 202010343897A CN 111500331 A CN111500331 A CN 111500331A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
Abstract
A natural gas decarburization experimental device with semi-barren solution logistics belongs to the technical field of natural gas decarburization research. The invention comprises an absorption tower, a regeneration tower, a reboiler, a gas-liquid separator, a first solution storage tank, a flash tank, a second solution storage tank, a cross heat exchanger and CO2Gas storage tank, N2A gas storage tank and a venting header pipe. The absorption tower is designed to be multi-point feeding, the absorption or regeneration feeding temperature can be regulated and controlled by the preheater, the absorption sample is collected by the high-pressure sampler, the multi-point real-time monitoring can be realized on the operating conditions such as the temperature and the pressure in the absorption tower and the regeneration tower, and the dynamic automatic collection of all data in the experimental process can be realized.
Description
Technical Field
The invention relates to a natural gas decarburization experimental device with a semi-barren solution material flow, and belongs to the technical field of natural gas decarburization research.
Background
The purification of natural gas is an important link for utilizing natural gas, and the exploited natural gas generally contains various acid gases such as CO2、H2S, etc. which can cause corrosion of pipelines and equipment, catalyst poisoning, accelerated hydrate formation, impact on the calorific value of commodity gas, etc. during storage and transportation of natural gas. The alcohol amine method decarburization is one of the most commonly applied technologies in the natural gas treatment industry, and is economical and effective for large-scale acid gas removal. Therefore, in the alcohol amine decarburization process, the research on the aspects of absorbent performance evaluation, formula screening, process parameter optimization and the like has great significance.
At present, the experimental research method aiming at the alcohol amine decarburization mainly focuses on a small-sized reaction kettle device, a laboratory scale packed tower, a field experiment and the like. The main equipment of the small reaction kettle device is a high-pressure reaction kettle, and the device can be applied to screening and purification performance analysis of the absorbent, but cannot simulate the flow and gas-liquid contact in a tower. At present, most of laboratory-scale packed towers are designed at low pressure, other influences such as flash evaporation and the like formed by high-pressure absorption are easily ignored, then the absorption process and the regeneration process are separately researched, so that the actual circulating operation process of a factory cannot be simulated, and the semi-lean liquid process in the factory is rarely involved at present. The field test has low efficiency, poor controllability, large using absorbed dose, high shutdown cost and incapability of researching various process structures and process parameters due to the limitation of the device.
Therefore, it is necessary to provide a natural gas decarbonization experimental apparatus with a semi-lean liquid stream to solve the above technical problems.
Disclosure of Invention
The invention was developed to solve the problems of low efficiency, poor controllability, and large amount of used absorbent, which are caused by the fact that most of the laboratory-scale packed towers are currently designed at low pressure, and the other effects such as flash evaporation formed by absorption at high pressure are easily ignored, and the invention is briefly summarized below to provide a basic understanding of some aspects of the invention. It should be understood that this summary is not an exhaustive overview of the invention. It is not intended to determine the key or critical elements of the present invention, nor is it intended to limit the scope of the present invention.
The technical scheme of the invention is as follows:
a natural gas decarburization experimental device with semi-barren solution material flow comprises an absorption tower, a regeneration tower, a reboiler, a gas-liquid separator, a first solution storage tank, a flash tank, a second solution storage tank, a cross heat exchanger, CO2Gas storage tank, N2Gas storage tank and emptying header, N2The gas storage tank respectively provides N for the absorption tower and the flash tank2，CO2The gas storage tank respectively provides CO for the absorption tower and the flash tank2The gas-liquid separator is respectively connected with the absorption tower, the first solution storage tank and the second solution storage tank are installed through pipeline connection, the first solution storage tank is installed through pipeline connection with the absorption tower, the absorption tower is installed through pipeline connection with the flash tank and the second solution storage tank respectively, the flash tank is installed through pipeline connection with the cross heat exchanger, the second solution storage tank and the cross heat exchanger are installed through pipeline connection, the cross heat exchanger is installed through pipeline connection with the regeneration tower and the reboiler respectively, the regeneration tower is installed through pipeline connection with the reboiler, the main emptying pipe is provided with a plurality of branch circuits respectively and the absorption tower, the regeneration tower, the reboiler, the gas-liquid separator, the first solution storage tank, the flash tank, the second solution storage tank and the main emptying pipe are communicated through pipelines.
Preferably: CO is arranged on a pipeline for connecting the gas-liquid separator and the emptying main pipe2Concentration detectionThe instrument comprises a condenser arranged on a pipeline connecting a gas-liquid separator and a first solution storage tank, an absorption tower feed pump and a preheater arranged on a pipeline connecting the first solution storage tank and an absorption tower, a preheater and an absorption tower feed pump arranged on a pipeline connecting the absorption tower and a second solution storage tank, and CO2CO is arranged at the air outlet of the air storage tank2The mass flow controller is characterized in that a condenser is installed on a pipeline connected with the flash tank and the emptying header in parallel, a regeneration tower feed pump is installed on a pipeline connected with the flash tank and the cross heat exchanger, a condenser is installed on a pipeline connected with the second solution storage tank and the cross heat exchanger, a preheater is installed on a pipeline connected with the cross heat exchanger and the regeneration tower, a regeneration tower extraction pump is installed on a pipeline connected with the cross heat exchanger and the reboiler, and a condenser is installed on a pipeline connected with the emptying header in parallel.
Preferably: the absorption tower is provided with a multi-point feeding hole, and the operating pressure is 0-5 MPa; the absorption tower comprises two sections of tower sections, and each section is provided with three temperature measuring ports extending into the absorption tower, so that the temperature in the absorption tower can be accurately measured; the top of the absorption tower is provided with a high-precision pressure transmitter and a temperature measuring thermocouple, and the high-precision pressure transmitter and the temperature measuring thermocouple respectively measure the gas phase pressure and the temperature at the top end of the absorption tower; the absorption tower also comprises an absorption tower kettle which is respectively connected with the high-pressure sampler and the flash tank through pipelines, and the absorption tower kettle is provided with a kettle temperature measuring point and a pressure gauge for measuring the gas phase pressure and the solution temperature of the absorption tower kettle; the side part of the tower kettle of the absorption tower is provided with a differential pressure type liquid level meter, and the liquid level meter and a pneumatic regulating valve are interlocked to control the automatic extraction of the heavy phase of the tower kettle of the absorption tower to a flash tank.
Preferably: the regeneration tower comprises two sections of tower sections, each section is provided with three temperature measuring ports extending into the regeneration tower, and the temperature in the regeneration tower is accurately measured; the top end of the regeneration tower is provided with a high-precision pressure transmitter and a temperature measuring thermocouple, and the high-precision pressure transmitter and the temperature measuring thermocouple are used for respectively measuring the gas phase pressure and the temperature at the top end of the regeneration tower; a differential pressure transmitter is arranged at the side part of the regeneration tower and used for monitoring the pressure drop of the regeneration tower; the regeneration tower top end gaseous phase pipe is provided with the sample connection, and the sample connection carries out the analysis of taking a sample through the sampler, the regeneration tower still include regeneration tower cauldron, both ends pass through the pipeline intercommunication with the reboiler respectively about the regeneration tower cauldron.
Preferably: the pipeline is provided with a plurality of pneumatic control valves, and the front and the back of each pneumatic control valve are provided with sampling ports.
Preferably: the top of the gas-liquid separator is provided with a pressure gauge, and the side part of the gas-liquid separator is provided with a differential pressure liquid level meter for monitoring the liquid level change in the gas-liquid separator in real time.
Preferably: the flash tank is provided with an on-site display liquid level meter, and the top of the flash tank is provided with a pressure gauge and a pressure transmitter.
Preferably: the preheater is a coil type preheater, a brass heating module is arranged in the preheater, and the temperature is controlled by adopting a silicon controlled rectifier.
The invention has the following beneficial effects:
1. the absorption tower is designed by multipoint feeding, the absorption/regeneration feeding temperature can be regulated and controlled by a preheater, a high-pressure sampler is adopted for collecting absorption samples, and the multipoint real-time monitoring can be realized on the operating conditions such as the temperature, the pressure and the like in the tower;
2. the natural gas decarburization experimental device with the semi-barren solution logistics can realize dynamic automatic acquisition of all data in the experimental process, and has the advantages of complete design and manufacturing functions, high automation degree, safety, reliability and simplicity and convenience in operation.
Drawings
FIG. 1 is a process flow diagram of a natural gas decarbonization experimental facility with a semi-lean liquid stream;
in the figure, 1-absorption tower, 1-1-absorption tower kettle, 2-regeneration tower, 2-1-regeneration tower kettle, 3-reboiler, 4-gas-liquid separator, 5-first solution storage tank, 6-flash tank, 7-second solution storage tank, 8-cross heat exchanger, 9-CO2 gas storage tank, 10-N2 gas storage tank, 11-emptying header pipe and 12-pneumatic control valve.
Detailed Description
In order that the objects, aspects and advantages of the invention will become more apparent, the invention will be described by way of example only, and in connection with the accompanying drawings. It is to be understood that such description is merely illustrative and not intended to limit the scope of the present invention. Moreover, in the following description, descriptions of well-known structures and techniques are omitted so as to not unnecessarily obscure the concepts of the present invention.
The connection mentioned in the invention is divided into fixed connection and detachable connection, the fixed connection is non-detachable connection and includes but is not limited to folding edge connection, rivet connection, bonding connection, welding connection and other conventional fixed connection modes, the detachable connection includes but is not limited to threaded connection, snap connection, pin connection, hinge connection and other conventional detachment modes, when the specific connection mode is not clearly limited, at least one connection mode can be found in the existing connection modes by default to realize the function, and the skilled person can select according to the needs. For example: the fixed connection selects welding connection, and the detachable connection selects hinge connection.
The first embodiment is as follows: the embodiment is described with reference to fig. 1, and the natural gas decarburization experimental facility with a semi-lean liquid stream of the embodiment comprises an absorption tower 1, a regeneration tower 2, a reboiler 3, a gas-liquid separator 4, a first solution storage tank 5, a flash tank 6, a second solution storage tank 7, a cross heat exchanger 8, CO2Gas storage tank 9, N2Gas tank 10 and discharge main 11, N2The gas storage tank 10 supplies N to the absorption tower 1 and the flash tank 6 respectively2，CO2The gas storage tank 9 respectively supplies CO to the absorption tower 1 and the flash tank 62The gas-liquid separator 4 is respectively connected and installed with the absorption tower 1, the first solution storage tank 5 and the second solution storage tank 7 through pipelines, the first solution storage tank 5 is connected and installed with the absorption tower 1 through a pipeline, the absorption tower 1 is respectively connected and installed with the flash tank 6 and the second solution storage tank 7 through pipelines, the flash tank 6 is connected and installed with the cross heat exchanger 8 through a pipeline, the second solution storage tank 7 and the cross heat exchanger 8 are connected and installed through a pipeline, the cross heat exchanger 8 is respectively connected and installed with the regeneration tower 2 and the reboiler 3 through a pipeline, the regeneration tower 2 is connected and installed with the reboiler 3 through a pipeline, the emptying header 11 is provided with a plurality of branches, a plurality of branches on the emptying main pipe 11 are respectively communicated with the absorption tower 1, the regeneration tower 2, the reboiler 3, the gas-liquid separator 4, the first solution storage tank 5, the flash tank 6, the second solution storage tank 7 and the emptying main pipe 11 through pipelines.
The second embodiment is as follows: referring to fig. 1, the present embodiment is described, and based on the first embodiment, the pipeline connecting the gas-liquid separator 4 and the discharge main 11 is provided with CO2Concentration detector, CO2Real-time online monitoring of CO in tail gas by concentration detector2The content can be changed according to the range requirement, a condenser is arranged on the pipeline of the gas-liquid separator 4 connected with the first solution storage tank 5, a feed pump and a preheater of the absorption tower are arranged on the pipeline of the first solution storage tank 5 connected with the absorption tower 1, a feed pump and a feed pump of the absorption tower are arranged on the pipeline of the absorption tower 1 connected with the second solution storage tank 7, and CO is discharged from the absorption tower2CO is arranged at the air outlet of the gas storage tank 92The mass flow controller, parallelly connected the installing condenser on the pipeline that flash tank 6 and evacuation house steward 11 are connected, install regeneration tower charge-in pump on the pipeline that flash tank 6 and cross heat exchanger 8 are connected, install the condenser on the pipeline that second solution storage tank 7 and cross heat exchanger 8 are connected, install the pre-heater on the pipeline that cross heat exchanger 8 and regeneration tower 2 are connected, install regeneration tower extraction pump on the pipeline that cross heat exchanger 8 and reboiler 3 are connected, parallelly connected the installing condenser on the pipeline that regeneration tower 2 and evacuation house steward 11 are connected.
The third concrete implementation mode: the embodiment is described with reference to fig. 1, and the natural gas decarburization experimental facility with a semi-barren solution stream of the embodiment is provided with a multi-point feeding hole in an absorption tower 1, and the operating pressure is 0-5 MPa; the absorption tower 1 comprises two sections of tower sections, each section is provided with three temperature measuring ports extending into the absorption tower 1, and the temperature in the absorption tower 1 is accurately measured; the top of the absorption tower 1 is provided with a high-precision pressure transmitter and a temperature measuring thermocouple, and the high-precision pressure transmitter and the temperature measuring thermocouple respectively measure the gas phase pressure and the temperature at the top end of the absorption tower 1; the absorption tower also comprises an absorption tower kettle 1-1, the absorption tower kettle 1-1 is respectively connected with the high-pressure sampler and the flash tank 6 through pipelines, the absorption tower kettle 1-1 is provided with an in-kettle temperature measuring point and a pressure gauge for measuring the gas phase pressure and the solution temperature of the absorption tower kettle 1-1; the side part of the tower kettle 1-1 of the absorption tower is provided with a differential pressure type liquid level meter which can monitor the liquid level change in the tower kettle 1-1 of the absorption tower in real time, and the liquid level meter and a pneumatic regulating valve are interlocked to control the automatic extraction of the heavy phase in the tower kettle 1-1 of the absorption tower to a flash tank 6.
The fourth concrete implementation mode: referring to fig. 1 to illustrate the present embodiment, in the present embodiment, a natural gas decarbonization experimental apparatus with a semi-lean liquid stream, the regeneration tower 2 includes two sections, each of which is provided with three temperature measurement ports extending into the regeneration tower 2, so as to accurately measure the temperature in the regeneration tower 2; the top end of the regeneration tower 2 is provided with a high-precision pressure transmitter and a temperature measuring thermocouple, and the high-precision pressure transmitter and the temperature measuring thermocouple are used for respectively measuring the gas phase pressure and the temperature at the top end of the regeneration tower 2; a differential pressure transmitter is arranged on the side part of the regeneration tower 2, and the pressure drop of the regeneration tower 2 is monitored; the gas phase pipe at the top end of the regeneration tower 2 is provided with a sampling port, the sampling port carries out sampling analysis through a sampler, the regeneration tower 2 further comprises a regeneration tower kettle 2-1, and the upper end and the lower end of the regeneration tower kettle 2-1 are respectively communicated with the reboiler 3 through pipelines.
The fifth concrete implementation mode: referring to fig. 1, the embodiment will be described, and the absorption tower 1, the regeneration tower 2, the reboiler 3, the gas-liquid separator 4, the first solution storage tank 5, the flash tank 6, the second solution storage tank 7 and the cross heat exchanger 8 of the natural gas decarburization experimental device with the semi-lean liquid material flow of the embodiment are all provided with a plurality of pneumatic control valves 12, and CO is supplied to the absorption tower 1, the regeneration tower 2, the reboiler 3, the gas-liquid separator 4, the second solution storage tank2 Pneumatic control valve 12 is arranged on the connecting pipeline of gas storage tank 9 and absorption tower 1, pneumatic control valve 12 is arranged on the connecting pipeline of absorption tower 1 and flash tank 6, pneumatic control valve 12 is arranged on the connecting pipeline of absorption tower 1 and second solution storage tank 7, pneumatic control valve 12 is arranged on the connecting pipeline of flash tank 6 and cross heat exchanger 8, pneumatic control valve 12 is arranged on the connecting pipeline of regeneration tower 2 and emptying header 11, pneumatic control valve 12 is arranged on the connecting pipeline of regeneration tower 2 and reboiler 3, a plurality of pneumatic control valves 12 are arranged on all the pipelines, sampling ports are arranged around pneumatic control valve 12, and high-pressure full-component sampling can be realized.
The sixth specific implementation mode: the embodiment is described with reference to fig. 1, and the natural gas decarburization experiment device with a semi-lean liquid stream of the embodiment is characterized in that a pressure gauge is arranged at the top of the gas-liquid separator 4, a differential pressure liquid level gauge for monitoring liquid level change in the gas-liquid separator in real time is arranged at the side part of the gas-liquid separator 4, and condensed gas is discharged from a backpressure valve through the top of the gas-liquid separator 4; the condensed liquid is collected in the gas-liquid separator 4, and can be intermittently discharged into the first solution storage tank 5 and the second solution storage tank 7 from the bottom, and is switched to use through a pneumatic regulating valve.
The seventh embodiment: the embodiment is described with reference to fig. 1, and the natural gas decarburization experiment device with semi-lean liquid flow of the embodiment is provided with a field display liquid level meter on the flash tank 6, a pressure meter and a pressure transmitter are arranged on the top of the flash tank 6, the flow of the flash tank 6 is controlled by the tower kettle liquid level meter and a pneumatic regulating valve in an interlocking manner, and is measured by a high-pressure metal rotor flow meter, and the feeding amount is controlled by a feeding pump.
The specific implementation mode is eight: the embodiment is described with reference to fig. 1, and the natural gas decarburization experimental facility with a semi-lean liquid material flow of the embodiment is a coil type preheater, a brass heating module is arranged in the preheater, and the temperature is controlled by adopting a thyristor.
The specific implementation method nine: the embodiment is described with reference to fig. 1, and the working process of the natural gas decarburization experimental device with a semi-lean liquid stream of the embodiment is as follows:
step a, a raw material natural gas purification process: CO22Gas storage tanks 9 and N2The gas in the gas storage tank 10 is depressurized by a pneumatic regulating valve through a pipeline and then enters CO2The mass flow controller enters the absorption tower 1 through a pipeline to be fully contacted with the alcohol amine solution, then flows into the gas-liquid separator 4 through a pipeline at the top of the absorption tower 1 through a condenser, and flows through CO after gas-liquid separation2The tail gas enters an emptying header pipe 11 after the detector is detected, the tail gas is treated, and N is adopted in consideration of the safety of the experimental process2And CO2The mixed gas cylinder is used as raw material gas;
step b, alcohol amine solution absorption and regeneration circulation flow: alcohol amine solution (namely lean solution) is filled into a first solution storage tank 5 and a second solution storage tank 7, respectively flows through preheaters through an absorption tower feed pump to be preheated, respectively flows into the absorption tower 1 from the middle part or the upper part of the absorption tower 1, absorbs and removes gas in the absorption tower 1, then flows into an absorption tower kettle 1-1, liquid in the absorption tower kettle 1-1 flows into a flash tank 6 through a main pipeline through a pneumatic regulating valve, if a sample needs to be collected, the solution flows into a high-pressure sampler through a branch pipeline to be sampled and analyzed, after being subjected to flash evaporation in the flash tank 6, the solution absorbed to saturation, namely rich solution, is pumped into a cross heat exchanger 8 through a regeneration tower feed pump to exchange heat with lean solution or semi-lean solution flowing out of a regeneration tower 2 after being preheated by the preheaters outside the pipeline, enters the regeneration tower 2 to be regenerated, and flows into a regeneration tower kettle 21 after being subjected to primary regeneration through heat exchange with steam in the regeneration tower 2, a pipeline at the bottom of a tower kettle 21 of the regeneration tower is communicated with the bottom of a reboiler 3, rich liquid is regenerated to different degrees by adjusting the temperature of a heating rod in the reboiler 3 to generate lean liquid or semi-lean liquid, generated steam enters a regeneration tower 2 through a pipeline, the liquid level of the reboiler 3 rises along with the continuous flowing of the solution from the regeneration tower 2, the solution overflows to the side of an overflow plate, the solution is conveyed to a cross heat exchanger 8 through a regeneration tower extraction pump to exchange heat with the rich liquid entering the regeneration tower 2, the cooled solution flows into a condenser to exchange heat with cooling water, the cooled solution is discharged into a first solution storage tank 5 and a second solution storage tank 7, and the absorption and regeneration processes of the alcohol amine solution can be completed through the switching of a pneumatic regulating valve;
step c, tail gas centralized collection and treatment process: the purified gas at the top of the absorption tower 1 enters a condenser through a pneumatic regulating valve, and the condensed purified gas is subjected to gas-liquid separation in a gas-liquid separator 4 and then is subjected to emptying treatment; part of CO is mixed with steam at the top of the regeneration tower 22Passing through a condenser, cooling the steam to obtain CO2Through the pipeline and CO in the flash tank 62And (5) collecting and emptying in a centralized manner.
It should be noted that, in the above embodiments, as long as the technical solutions can be aligned and combined without contradiction, those skilled in the art can exhaust all possibilities according to the mathematical knowledge of the alignment and combination, and therefore, the present invention does not describe the technical solutions after alignment and combination one by one, but it should be understood that the technical solutions after alignment and combination have been disclosed by the present invention.
This embodiment is only illustrative of the patent and does not limit the scope of protection thereof, and those skilled in the art can make modifications to its part without departing from the spirit of the patent.
Claims (8)
1. A natural gas decarburization experimental device with semi-barren solution material flow comprises an absorption tower (1), a regeneration tower (2), a reboiler (3), a gas-liquid separator (4), a first solution storage tank (5), a flash tank (6), a second solution storage tank (7), a cross heat exchanger (8), CO2Gas storage tank (9), N2A gas storage tank (10) and a venting header pipe (11), N2The gas storage tank (10) respectively provides N for the absorption tower (1) and the flash tank (6)2，CO2The gas storage tank (9) respectively provides CO for the absorption tower (1) and the flash tank (6)2The gas-liquid separator (4) is respectively connected and installed with the absorption tower (1), the first solution storage tank (5) and the second solution storage tank (7) through pipelines, the first solution storage tank (5) is connected and installed with the absorption tower (1) through pipelines, the absorption tower (1) is respectively connected and installed with the flash tank (6) and the second solution storage tank (7) through pipelines, the flash tank (6) is connected and installed with the cross heat exchanger (8) through pipelines, the second solution storage tank (7) and the cross heat exchanger (8) are connected and installed through pipelines, the cross heat exchanger (8) is respectively connected and installed with the regeneration tower (2) and the reboiler (3) through pipelines, the regeneration tower (2) is connected and installed with the reboiler (3) through pipelines, the emptying header (11) is provided with a plurality of branch circuits, the emptying header (11) is respectively connected and installed with the absorption tower (1), the regeneration tower (2), the reboiler (3), The gas-liquid separator (4), the first solution storage tank (5), the flash tank (6), the second solution storage tank (7) and the emptying header pipe (11) are communicated through pipelines.
2. The natural gas decarburization experimental facility with a semi-barren solution stream as claimed in claim 1, wherein: CO is arranged on a pipeline connecting the gas-liquid separator (4) with the emptying header pipe (11)2A condenser is arranged on a pipeline connecting a gas-liquid separator (4) and a first solution storage tank (5), an absorption tower feed pump and a preheater are arranged on a pipeline connecting the first solution storage tank (5) and an absorption tower (1), a preheater and an absorption tower feed pump are arranged on a pipeline connecting the absorption tower (1) and a second solution storage tank (7), and CO is discharged from a CO gas-liquid separator2CO is arranged at the air outlet of the air storage tank (9)2Mass flow controller, flash tank (6) and emptyingThe pipeline that house steward (11) is connected is gone up the parallel arrangement and is had the condenser, install regeneration tower charge-in pump on the pipeline that flash tank (6) and cross heat exchanger (8) are connected, install the condenser on the pipeline that second solution storage tank (7) and cross heat exchanger (8) are connected, install the pre-heater on the pipeline that cross heat exchanger (8) and regenerator column (2) are connected, install the regenerator column on the pipeline that cross heat exchanger (8) and reboiler (3) are connected and adopt the pump, parallel arrangement has the condenser on the pipeline that regenerator column (2) and unloading house steward (11) are connected.
3. The natural gas decarburization experimental facility with a semi-barren solution stream as claimed in claim 2, wherein: the absorption tower (1) is provided with a multi-point feeding hole, and the operating pressure is 0-5 MPa; the absorption tower (1) comprises two sections of tower sections, and each section is provided with three temperature measuring ports extending into the absorption tower (1) so as to accurately measure the temperature in the absorption tower (1); the top of the absorption tower (1) is provided with a high-precision pressure transmitter and a temperature measuring thermocouple, and the high-precision pressure transmitter and the temperature measuring thermocouple are used for respectively measuring the gas phase pressure and the temperature at the top end of the absorption tower (1); the absorption tower also comprises an absorption tower kettle (1-1), and the absorption tower kettle (1-1) is respectively connected with the high-pressure sampler and the flash tank (6) through pipelines. The absorption tower kettle (1-1) is provided with a kettle internal temperature measuring point and a pressure gauge for measuring the gas phase pressure and the solution temperature of the absorption tower kettle (1-1); the side part of the tower kettle (1-1) of the absorption tower is provided with a differential pressure type liquid level meter, and the liquid level meter and a pneumatic regulating valve are interlocked to control the automatic extraction of the heavy phase of the tower kettle (1-1) of the absorption tower to a flash tank (6).
4. The natural gas decarburization experimental facility with a semi-barren solution stream as claimed in claim 2, wherein: the regeneration tower (2) comprises two sections of tower sections, each section is provided with three temperature measuring ports extending into the regeneration tower (2), and the temperature in the regeneration tower (2) is accurately measured; the top end of the regeneration tower (2) is provided with a high-precision pressure transmitter and a temperature measuring thermocouple, and the high-precision pressure transmitter and the temperature measuring thermocouple are used for respectively measuring the gas phase pressure and the temperature at the top end of the regeneration tower (2); a differential pressure transmitter is arranged on the side part of the regeneration tower (2) to monitor the pressure drop of the regeneration tower (2); the top gas phase pipe of the regeneration tower (2) is provided with a sampling port, the sampling port carries out sampling analysis through a sampler, the regeneration tower (2) further comprises a regeneration tower kettle (2-1), and the upper end and the lower end of the regeneration tower kettle (2-1) are respectively communicated with the reboiler (3) through pipelines.
5. The natural gas decarbonization experimental facility with the semi-lean liquid stream according to any one of claims 1 to 4, characterized in that: a plurality of pneumatic regulating valves (12) are arranged on the absorption tower (1), the regeneration tower (2), the reboiler (3), the gas-liquid separator (4), the first solution storage tank (5), the flash tank (6), the second solution storage tank (7) and the cross heat exchanger (8), and CO is discharged from the absorption tower2The device is characterized in that a pneumatic regulating valve (12) is arranged on a connecting pipeline of the gas storage tank (9) and the absorption tower (1), a pneumatic regulating valve (12) is arranged on a connecting pipeline of the absorption tower (1) and the flash tank (6), a pneumatic regulating valve (12) is arranged on a connecting pipeline of the absorption tower (1) and the second solution storage tank (7), a pneumatic regulating valve (12) is arranged on a connecting pipeline of the flash tank (6) and the cross heat exchanger (8), a pneumatic regulating valve (12) is arranged on a connecting pipeline of the regeneration tower (2) and the emptying header pipe (11), a pneumatic regulating valve (12) is arranged on a connecting pipeline of the regeneration tower (2) and the reboiler (3), and sampling ports are arranged in the front and.
6. The natural gas decarburization experimental facility with a semi-barren solution stream as claimed in claim 1, wherein: the top of the gas-liquid separator (4) is provided with a pressure gauge, and the side part of the gas-liquid separator (4) is provided with a differential pressure liquid level meter for monitoring the liquid level change in the gas-liquid separator in real time.
7. The natural gas decarburization experimental facility with a semi-barren solution stream as claimed in claim 1, wherein: the flash tank (6) is provided with a field display liquid level meter, and the top of the flash tank (6) is provided with a pressure meter and a pressure transmitter.
8. The natural gas decarburization experimental facility with a semi-barren solution stream as claimed in claim 2, wherein: the preheater is a coil type preheater, a brass heating module is arranged in the preheater, and the temperature is controlled by adopting a silicon controlled rectifier.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114133969A (en) * | 2021-12-09 | 2022-03-04 | 中国石油大学(北京) | Desulfurization and decarburization method for high-sulfur high-carbon natural gas |
| CN114405246A (en) * | 2021-12-28 | 2022-04-29 | 中国矿业大学 | Is suitable for low partial pressure CO2Energy-saving process for trapping and purifying |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201643963U (en) * | 2009-12-31 | 2010-11-24 | 攀钢集团攀枝花钢铁研究院有限公司 | Acidic component absorption-desorption test device |
| CN203648344U (en) * | 2013-11-25 | 2014-06-18 | 中石化石油工程设计有限公司 | Carbon dioxide capture experiment evaluation testing device |
| CN105664698A (en) * | 2016-04-05 | 2016-06-15 | 江苏大海能源科技有限公司 | Compound liquid desulfurizing agent and application thereof |
| US20160332108A1 (en) * | 2015-05-14 | 2016-11-17 | Chevron U.S.A. Inc. | Process, method, and system for removing mercury from fluids |
| CN108310918A (en) * | 2018-04-27 | 2018-07-24 | 北京石油化工工程有限公司 | A kind of semi lean solution absorbs rectisol system and method |
-
2020
- 2020-04-27 CN CN202010343897.3A patent/CN111500331A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN201643963U (en) * | 2009-12-31 | 2010-11-24 | 攀钢集团攀枝花钢铁研究院有限公司 | Acidic component absorption-desorption test device |
| CN203648344U (en) * | 2013-11-25 | 2014-06-18 | 中石化石油工程设计有限公司 | Carbon dioxide capture experiment evaluation testing device |
| US20160332108A1 (en) * | 2015-05-14 | 2016-11-17 | Chevron U.S.A. Inc. | Process, method, and system for removing mercury from fluids |
| CN105664698A (en) * | 2016-04-05 | 2016-06-15 | 江苏大海能源科技有限公司 | Compound liquid desulfurizing agent and application thereof |
| CN108310918A (en) * | 2018-04-27 | 2018-07-24 | 北京石油化工工程有限公司 | A kind of semi lean solution absorbs rectisol system and method |
Non-Patent Citations (1)
| Title |
|---|
| 唐建峰等: ""大型天然气净化工艺模拟实验装置的研制"", 《实验室研究与探索》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114133969A (en) * | 2021-12-09 | 2022-03-04 | 中国石油大学(北京) | Desulfurization and decarburization method for high-sulfur high-carbon natural gas |
| CN114405246A (en) * | 2021-12-28 | 2022-04-29 | 中国矿业大学 | Is suitable for low partial pressure CO2Energy-saving process for trapping and purifying |
| CN114405246B (en) * | 2021-12-28 | 2022-11-01 | 中国矿业大学 | Is suitable for low partial pressure CO2Energy-saving process for trapping and purifying |
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