CN116538428A - Carbon dioxide dense-phase pressurizing system - Google Patents
Carbon dioxide dense-phase pressurizing system Download PDFInfo
- Publication number
- CN116538428A CN116538428A CN202310462919.1A CN202310462919A CN116538428A CN 116538428 A CN116538428 A CN 116538428A CN 202310462919 A CN202310462919 A CN 202310462919A CN 116538428 A CN116538428 A CN 116538428A
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- China
- Prior art keywords
- expander
- pump
- carbon dioxide
- dense
- phase
- Prior art date
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Links
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 56
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 28
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 27
- 239000007788 liquid Substances 0.000 claims description 16
- 238000002347 injection Methods 0.000 abstract description 17
- 239000007924 injection Substances 0.000 abstract description 17
- 230000000694 effects Effects 0.000 abstract description 6
- 230000007613 environmental effect Effects 0.000 abstract description 2
- -1 expander Chemical compound 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 230000005611 electricity Effects 0.000 abstract 1
- 238000006073 displacement reaction Methods 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 230000009919 sequestration Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000002513 implantation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 238000009877 rendering Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/005—Pipe-line systems for a two-phase gas-liquid flow
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/02—Pipe-line systems for gases or vapours
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D1/00—Pipe-line systems
- F17D1/02—Pipe-line systems for gases or vapours
- F17D1/065—Arrangements for producing propulsion of gases or vapours
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17D—PIPE-LINE SYSTEMS; PIPE-LINES
- F17D3/00—Arrangements for supervising or controlling working operations
- F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
Abstract
The application belongs to the technical field of environmental protection equipment, and particularly relates to a carbon dioxide dense-phase pressurizing system. CO 2 The development of pipeline transportation, while saving costs, has also presented new problems. CO transported by pipeline 2 Most of the injection stations are in supercritical state, and the pressurization effect cannot be achieved by using an injection pump, so that there is a need for supercritical/dense phase CO used in the injection stations 2 The pressurizing system meets the production requirement. The application provides a dense-phase pressurization system of carbon dioxide, including expander, booster pump and the ejector pump that connects gradually, expander, backpressure valve, heat exchanger with the ejector pump connects gradually, the heat exchanger with the booster pump is connected. The expander, the booster pump and the injectionThe components such as the pump are combined, and the expander is used as a power source to realize CO without electricity consumption 2 Dense-phase supercharging saves a large amount of electric energy, utilizes an ejector pump to recycle the expanded low-pressure carbon dioxide, and avoids CO 2 Inflow into the atmosphere increases the greenhouse effect.
Description
Technical Field
The application belongs to the technical field of environmental protection equipment, and particularly relates to a carbon dioxide dense-phase pressurizing system.
Background
The Carbon Capture, utilization and sequestration of the ccs (Carbon Capture, utilization and Storage) is one of the key technologies for global climate change, and its emission reduction contribution is expected to reach 6-16 hundred million tons of CO in 2050 2 . Tens of CCUS demonstration projects are also planned and built in China at present, wherein CO 2 Oil displacement is undoubtedly the best choice for utilization and sequestration. Pipeline transportation has become an indispensable link in the engineering, and at present, the world-wide pipeline transportation pressure is not more than 15MPa, which is far lower than that of using CO 2 The pressure of the flooding is carried out. Thus, CO is injected between the pipe end and wellhead through the booster injection station 2 And (5) pressurizing and well injection are carried out.
With the development of CCUS engineering construction, CO 2 Pipeline transportation becomes a main transportation mode, and CO is used at the tail end of the pipeline 2 The injection pump pumps CO 2 Further pressurizing and injecting into underground oil displacement or sealing. The pipeline transportation saves the cost and simultaneously brings new problems. At the end of the pipeline, CO 2 Is generally near the near critical point, and dense phase liquid and supercritical states may exist simultaneously. Existing CO 2 Injection processes, generally described in patent CN 107355680A, using plunger pumps for supercritical CO 2 The incoming flow of the pipeline is pressurized and injected into the well. When the incoming flow of the pipeline is in a supercritical state, CO 2 Has lower density, viscosity similar to gas, especially in hot summer, the temperature of the tail end of the pipeline is higher, and CO 2 Most of which is in the supercritical gaseous state, this gives CO 2 The injection pump brings great challenges, if the refrigerating unit is used for condensing and cooling CO2 before entering the pump, the power consumption of the injection system can be increased, and meanwhile, the equipment investment in the early stage and the subsequent operation and maintenance cost are correspondingly increased. The injection station is generally built near the wellhead, the power grid arrangement is difficult, and the power consumption of the injection system should be as high as possibleCan be small. Thus, there is a need for a supercritical/dense phase CO for use in an implantation station 2 The pressurizing system meets the production requirement.
Disclosure of Invention
1. Technical problem to be solved
Based on CO in CCUS engineering 2 Pipeline transportation becomes a main transportation mode, and CO is used at the tail end of the pipeline 2 The injection pump pumps CO 2 Further pressurizing and injecting into underground oil displacement or sealing. The pipeline transportation saves the cost and simultaneously brings new problems. At the end of the pipeline, CO 2 Is generally near the near critical point, and dense phase liquid and supercritical states may exist simultaneously. Especially in summer with hot weather, the temperature of the tail end of the pipeline is higher, and CO 2 In a supercritical state, this gives CO 2 Injection pumps present a significant challenge, and existing centrifugal pumps for plunger pumps are used to boost supercritical CO 2 The ideal pressure can not be reached in all cases, and supercritical CO 2 Cavitation of the pump is easily caused, rendering it inoperable. If the refrigeration system is used to supply CO to the pipeline before the pump is started 2 The cooling is needed to increase extra power consumption, and meanwhile, the problem of increasing investment cost is also brought, so that the application provides a carbon dioxide dense-phase supercharging system for solving the problem.
2. Technical proposal
In order to achieve the above-mentioned purpose, the application provides a dense-phase pressurization system of carbon dioxide, including expander, booster pump and the ejector pump that connects gradually, expander, backpressure valve, heat exchanger with the ejector pump connects gradually, the heat exchanger with the booster pump is connected.
Another embodiment provided herein is: the expander is a liquid expander.
Another embodiment provided herein is: the booster pump is coaxially connected with the expander, the expander is used as a power source of the booster pump, and the ejector pump recovers the expanded low-pressure carbon dioxide.
Another embodiment provided herein is: the booster pump, the second flow control valve and the ejector pump are sequentially connected.
Another embodiment provided herein is: the expansion machine is connected with a transportation pipeline through a first flow control valve, and the transportation pipeline is connected with the heat exchanger.
3. Advantageous effects
Compared with the prior art, the dense-phase pressurizing system for carbon dioxide has the beneficial effects that:
the carbon dioxide dense-phase pressurizing system provided by the application is CO near a critical point 2 The problem of pressurizing the incoming flow of tubing within the injection station provides a solution.
The application provides a dense-phase pressurization system of carbon dioxide combines components such as expander, booster pump, ejector pump, realizes the CO of no power consumption 2 Dense phase supercharging saves a great amount of electric energy.
The carbon dioxide dense-phase supercharging system provided by the application only utilizes the pressure energy of fluid, does not need additional electric power input, and compared with the traditional dense-phase supercharging process, the carbon dioxide dense-phase supercharging system has the advantages that the early equipment investment cost is increased, the electric power cost of subsequent operation is not needed, and the cost is lower than that of the traditional equipment along with the increase of the operation time.
The application provides a dense-phase pressurization system of carbon dioxide, avoids traditional CO 2 The dense phase pump is used for pumping supercritical CO 2 Cavitation phenomenon appears at the time, has improved pumping efficiency, and then has promoted the productivity effect.
The application provides a dense-phase pressurization system of carbon dioxide, the concatenation of ejector pump has prevented a large amount of CO 2 And the evacuation of air flow avoids the aggravation of greenhouse effect.
Drawings
FIG. 1 is a schematic diagram of a dense phase pressurization system for carbon dioxide of the present application.
FIG. 2 is a state change of carbon dioxide in various components of the present system in an embodiment of the present application.
Detailed Description
Hereinafter, specific embodiments of the present application will be described in detail with reference to the accompanying drawings, and according to these detailed descriptions, those skilled in the art can clearly understand the present application and can practice the present application. Features from various embodiments may be combined to obtain new implementations or to replace certain features from certain embodiments to obtain other preferred implementations without departing from the principles of the present application.
Referring to fig. 1-2, the application provides a dense-phase pressurizing system for carbon dioxide, which comprises an expander 3, a booster pump 2 and an ejector pump 7 which are sequentially connected, wherein the expander 3, a back pressure valve 4, a heat exchanger 5 and the ejector pump 7 are sequentially connected, and the heat exchanger 5 is connected with the booster pump 2.
The flow rate and the outlet pressure of the expander 3 are controlled by the first flow control valve 1 and the back pressure valve 4.
CO transported in pipeline 2 Incoming flow into CO 2 After the injection station, a branch pipeline is constructed to lead out a part of CO 2 The flow enters the expander 3 to do work, the flow of the expander 3 is regulated and controlled by the first flow control valve 1 in front of the inlet, and the outlet pressure is controlled by the back pressure valve 4 behind the outlet of the expander 3. During operation of the expander, CO 2 The pressure of the branch flow is reduced, the temperature is reduced, and the branch flow becomes CO mixed with gas and liquid 2 Cold flow. Subsequently, CO 2 The cold flow flows into the heat exchanger 5 and is communicated with the main flow CO of the pipeline 2 Exchange heat with each other, CO 2 Cold flow absorbs heat and the gas-liquid state changes into pure gaseous CO 2 CO formation 2 And the air flow is led to a secondary inlet of the ejector pump. Pipeline mainstream CO 2 After heat exchange, the temperature is reduced, the state is in a dense phase liquid state, the dense phase liquid state enters the booster pump 2 to be boosted to a state higher than injection pressure, the booster pump 2 is coaxially connected with the expander 3, and expansion work is utilized to drive the booster pump 2 to work. Pressurized high pressure CO 2 The flow enters the ejector pump 7, and the dense phase CO entering the ejector pump 7 is regulated by a second flow control valve 6 in front of the ejector pump 7 2 Thereby playing a role in regulating and controlling the speed, and through the interconversion of pressure energy and kinetic energy, CO is converted into 2 Mixing and pressurizing the air flow in the suction pump to obtain CO meeting the injection pressure 2 And (3) flow.
Considering the incoming flow CO of a pipeline 2 Typically in a supercritical state or in a dense phase liquid state, the expander 3 is preferably a liquid expander.
The expander 3 not only provides driving force for the booster pump 2, but also can provide driving force for CO 2 The incoming flow supplies the cooling medium such that CO before entering the pump 2 In a dense phase liquid state. The ejector pump 7 is used for cooling medium CO 2 And recycling is carried out, so that the waste is prevented from entering the atmosphere to increase the greenhouse effect.
DETAILED DESCRIPTION OF EMBODIMENT (S) OF INVENTION
In combination with FIG. 2CO 2 The state changes in the respective components of the present application will be described in detail with reference to the technical flow of the present application. As in fig. 2, the pipe comes CO 2 The state of (a) is shown as a point, the pressure is 10MPa, the temperature is 40 ℃, the flow ratio of the carbon dioxide flowing into the expander 3 through the branch pipeline is assumed to be x, the carbon dioxide enters the expander 3 to expand and do work, the state of an expansion outlet is shown as a point b, and the output work of the expander 3 is calculated by using the following formula: w (W) expander ＝q m2 (h se,out -h e,in )η e (1)
W expander Work is output for the expander, kW; q m2 Q for diverting flow to the expander m2 ＝x*q m ,kg/s；h se,out The specific enthalpy value of an outlet after isentropic expansion of the expander is kJ/kg; h is a e,in The specific enthalpy value of an inlet of the expander is kJ/kg; the specific enthalpy value is calculated by software REFPROP, eta e For expander efficiency, this example takes the value 80%.
Expanded CO 2 In a gas-liquid two-phase state, and then is introduced into the heat exchanger 5 and is communicated with the main flow CO of the pipeline 2 Heat exchange, gas-liquid two-phase CO 2 Is gaseous as shown in state c. After the main flow of the pipeline obtains cold, the main flow becomes a state point d, the pressure is 10MPa, and the temperature is 10 ℃. CO 2 In this state, the booster pump 2 is charged to 30MPa, and the state point e is reached, and the power consumption of the booster pump 2 is represented by the following formula:
W pump ＝q m1 (p p,out -p p,in )/(ρη p ) (2)
W pump the power consumption of the booster pump is kW; q m1 Is the main stream CO 2 Flow rate, q m1 ＝(1-x)*q m ,kg/s；p p,in ,p p,out Respectively are provided withThe pressure is the inlet and outlet pressure of the pump and MPa; ρ is density, kg/m 3 ；η p For booster pump efficiency, this example takes 80%.
The expander 3 is used as a power source of the booster pump 2, and W exists expander ＝W pump By calculating the split ratio x=60% through the relation, namely, using 60% of the pipeline inflow expansion to do work, the pressurization of 40% of the pipeline inflow can be realized. In the current ejector pump 7 technology, the high pressure liquid ejector low pressure gas is very easy because the liquid density is much higher than the gaseous density and the working fluid pressure is much higher than the low pressure gas. The status point f-i is CO 2 Changing in the ejector pump 7, high-pressure liquid CO 2 (State point e of FIG. 2) rapidly expanding to state point f by the ejector nozzle, sucking low-pressure gas CO 2 Enters the ejector pump 7 to carry out thermal mass mixing to be in a state of h, and then the CO is made in a diffusion section 2 Reach state i, up to this point, complete CO 2 Pressurizing.
Although the present application has been described with reference to particular embodiments, those skilled in the art will appreciate that many modifications are possible in the principles and scope of the disclosure. The scope of the application is to be determined by the appended claims, and it is intended that the claims cover all modifications that are within the literal meaning or range of equivalents of the technical features of the claims.
Claims (5)
1. A carbon dioxide dense phase pressurization system, characterized in that: the device comprises an expander, a booster pump and an ejector pump which are sequentially connected, wherein the expander, a back pressure valve, a heat exchanger and the ejector pump are sequentially connected, and the heat exchanger is connected with the booster pump.
2. The carbon dioxide dense phase pressurization system of claim 1, wherein: the expander is a liquid expander.
3. The carbon dioxide dense phase pressurization system of claim 2, wherein: the booster pump is coaxially connected with the expander, the expander is used as a power source of the booster pump, and the ejector pump recovers the expanded low-pressure carbon dioxide.
4. The carbon dioxide dense phase pressurization system of claim 3 wherein: the booster pump, the second flow control valve and the ejector pump are sequentially connected.
5. The carbon dioxide dense phase pressurization system of claim 1, wherein: the expansion machine is connected with a transportation pipeline through a first flow control valve, and the transportation pipeline is connected with the heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310462919.1A CN116538428A (en) | 2023-04-26 | 2023-04-26 | Carbon dioxide dense-phase pressurizing system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202310462919.1A CN116538428A (en) | 2023-04-26 | 2023-04-26 | Carbon dioxide dense-phase pressurizing system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN116538428A true CN116538428A (en) | 2023-08-04 |
Family
ID=87453541
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202310462919.1A Pending CN116538428A (en) | 2023-04-26 | 2023-04-26 | Carbon dioxide dense-phase pressurizing system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN116538428A (en) |
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2023
- 2023-04-26 CN CN202310462919.1A patent/CN116538428A/en active Pending
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