SY/T 0011-1996 Design specification for natural gas purification plant in gas field
Some standard content:
Petroleum and Natural Gas Industry Standard of the People's Republic of China Design Specification for Natural Gas Conditioning Plant in Gas Field
SY/ T 0011-96
Editor: Sichuan Design Institute of China National Petroleum CorporationApproval Department: Petroleum Industry Press of China National Petroleum Corporation
Beijing, 1996
China National Petroleum CorporationDocument
(96) Zhongyou Jijianzi No. 642
Notice on the Approval and Release of Fourteen Petroleum and Natural Gas Industry Standards including "Design Specification for Gas Field Gas Gathering Engineering"To all relevant units
Fourteen Petroleum and Natural Gas Industry Standards including "Design Specification for Gas Field Gas Gathering Engineering" (Draft): After review and approval, they are now approved as petroleum and natural gas industry standards and are hereby released: The numbers and names of the various standards are as follows:Serial NumberNo.
1SY/T 0010--96
2SY/T 0011-96
3 SY 0043-96
4 SY/T 0091-96
Design specification for gas field gas gathering engineering (replace
SYI 10-86)
Design specification for natural gas purification plant in gas field (replace SYJ 11-35)
Coloring standard for surface pipelines and equipment in oil and gas fields (replace 5YI43-89)
Design specification for oil and gas fields and pipeline computer control systems
Weiyou Petroleum Engineering Thermal Heating Technical Specifications
SY/T0306-96
Weihai Petroleum Engineering Vertical Cylindrical Steel Coal SY/T 0307-96
Technical Specification for Fixed-roof Storage Tanks
SY/T 0308--96
SY/T 0309-96
SY/T 0310-96
10SY/T 0311-96
SY/T 0312-96
SY/T0313-96
13SY/T 031496
14SY/T 0305-96
Weihai Oil Project Water Injection Technical Specification
Weihai Oil Project Water Treatment Technical Specification
Weihai Oil Project Instrumentation and Automatic Control Technical Specification
Weihai Oil Project Communication Technical Specification
Weihai Oil Project Equipment Technical Specification
Tanhai Oil Project Wharf Design and Construction Technical Specification
Weihai Concrete Platform Structure Design and Construction Technical Specification
Weihai Pipeline System Technical Specification
The above standards shall be implemented from January 1, 1997 China National Petroleum Corporation
December 3, 1996
2 Terms
General Provisions
4 Site Selection and General Layout
4.1 Site Selection
4.2 General layout
5 Process equipment
5.1 Process design principles
2 Principles for the selection of purification process methods and parameters 51 Equipment layout
6 Auxiliary and public facilities
6.1 Pea sulfonated packaging and storage
6.3 Other auxiliary facilities
64 Water supply and drainage
65 Steam condensate and softened (desalted) water
6.6 Fuel gas system
6.8 Communication
Construction and HVAC
Construction engineering
Record·This specification uses time description.
Additional statement period
(3)
(24)
(25)
(25)
n00 j 32
(33)
mas [Sl ]
Appendix Gas Field Natural Gas Purification Plant Design Specifications Explanation of Articles (521 General Provisions
1.0.1 In order to ensure that the design quality of gas field natural gas purification plants (hereinafter referred to as purification plants!) is technically advanced, economically reasonable, safe and reliable in production, and convenient in operation and maintenance, this specification is specially formulated.
1.0.2 This specification is applicable to the design, expansion and reconstruction of new onshore gas mountain natural gas purification plants, and the design of natural gas purification stations and skid-mounted natural gas purification devices can refer to it for implementation.
, the design of new devices and new systems of existing purification plants should also be implemented in accordance with the vehicle outline specification.
1.0.3 In addition to implementing this specification, the design of natural gas purification plants should also comply with the relevant provisions of the current national standards.
1..4 Reference standards:
GB 5749 Sanitary standard for drinking water
GB S5004I Design code for boiler room
GB50052 Design code for power supply and distribution system
GB50058 Design code for power installations in explosive and fire hazardous environmentsGB50060 Design code for 3~110kV high-voltage distribution equipmentGB50160 Design fire protection code for petrochemical enterprisesGB50183 Design fire protection code for crude oil and natural gas engineeringGB5C191 Code for seismic design of structures
GBJ2 Coordinated unified standard for building modulus
GBI6 Coordinated standard for factory building modulus
GBI9 Load visual representation of building structure
GBJI Code for seismic design of buildings
GBI3 Design code for outdoor water supply
GBJ[4 Design code for outdoor drainage
GBJ16 Comply with building Fire protection code for design
GBJ19 Design code for heating, ventilation and air conditioning GBJ29 Design code for compressed air station
GBJ40 Design code for power machinery foundation
GBJ42 Design code for industrial enterprise communication
GBJ50 Design code for industrial circulating cooling water treatment GBJ87 Design code for noise control in industrial enterprises GBI102 Design code for industrial circulating water cooling
Labor Code No. [1990] 8 Safety Technical Supervision Regulations for Pressure Vessels Ministry of Labor Issued No. [1996] 276 Safety Technical Supervision Regulations for Steam Boilers TJ 36 Industrial enterprise design hygiene standards
SYJ12 Requirements for metal materials resistant to sulfide stress cracking of natural gas surface facilitiesSYJ34 Energy-saving technical regulations for gas field surface engineering designSYJ48 General layout design specifications for crude oil and natural gas engineering construction stations (plants)SY 0025 Classification of electrical installations in petroleum facilitiesSY/T 0076 Natural gas dehydration design specifications
SYJ1007 Technical regulations for the design of central laboratories in refineriesSYJ1030 Technical regulations for heating, ventilation and air conditioning design in refineries and injection plantsSHI30 Design specifications for tower equipment foundations in petrochemical enterprisesSHI29 Design specifications for exhaust pipes and fire towers in petrochemical enterprisesSHi3077 Design specifications for steel structure cold exchange frames in petrochemical enterprisesSDGJ9 Technical regulations for heating, ventilation and air conditioning design in thermal power plants (trial implementation)
APIRP 521 Guidelines for oil pressure systems and pressure relief systems 2
2 Terminology
2.0.1 Natural gas purificationnaturalgas Conditioninglani is a plant with a large production capacity, and the types of equipment include natural gas desulfurization, dehydration, sulfur recovery, tail gas treatment or part of them. 2.0.2 Natural gas conditioning station is an independent natural gas purification facility dispersed on the gas field with a small production capacity and (or) a single process.
2.0.3 Process unit (i.e. process production unit) processunit is a combination of production units and storage equipment, buildings (structures) that complete at least one product or intermediate product according to the production process, such as desulfurization unit, dehydration unit, sulfur recovery unit, tail gas treatment unit. 2.0.4 Combined unit (i.e. process combined production unit) combined unit is a combination of two or more units combined to simplify the process flow and reduce process equipment.
2.0.5 Tail-gas
refers to the gas leaving the last sulfur collector of the Claus sulfur recovery unit.
2.0.6 Process gas process-gas
2.0.6.1 In Claus sulfur recovery unit, the gas in the system from the mixing of acid gas and air in the main combustion furnace to the outlet of the last sulfur trap; 2.0.6.2 In the reduction absorption tail gas treatment unit, the gas in the system from the mixing of tail gas and reducing gas in the reducing gas generator (or reheating furnace) to the outlet of the device's absorption tower top separator.
2.0.7 Reduction gas refers to the hydrogen or gas containing hydrogen and carbon monoxide introduced into the tail gas treatment device for reducing carbon dioxide in the tail gas in the reduction recovery method. 3 -
2.1s Blow gas refers to the gas leaving the exhaust gas treatment device suction tower pre-separator that does not require further treatment and can be discharged after burning, the acid gas discharged from the desulfurization device or the tail gas from the sulfur recovery device.
3 General provisions
3.0.1 The design of the purification plant must be carried out in accordance with the contents, specifications and requirements specified in the approved design task book.
3.0.2 Based on resource conditions, the principles determined by the development plan and the overall process of the gas gathering system and the connection status of the purified gas pipeline network, the relationship between the purification plant and the gas gathering, gas transmission or user should be handled well, and the plant scale, number of similar devices and the pre-design processing capacity of a single device should be reasonably determined.
3.0.3 Purification! The design pressure is determined by the overall flow of the gas field gathering system, and the design operating pressure of the desulfurization device absorption equipment is used as the design pressure of the purification plant. When the purification plant is not equipped with a desulfurization device but only with a dehydration device, the design operating pressure of the dehydration device absorption equipment should be used as the design pressure of the purification plant. Note: The pressure in this specification is the gauge pressure unless otherwise specified. 3. The design processing capacity of the purification plant is calculated by gas volume. It is the raw gas volume processed per working day under the design pressure.
Note: The gas volume used in this specification is the volume under the state of 2FC101,35 kPa unless otherwise specified.
3.0.5 The annual operation days of each process unit of the purification plant are set at 330 days. 3:8.6 The design capacity of each process unit, auxiliary production facilities and public facilities of the purification plant shall be based on the results of the comprehensive balance of materials and energy of the whole plant, and coordination and balance shall be achieved.
3.0.7 When the purification plant is constructed in phases, its auxiliary production facilities and public facilities shall be constructed at one time according to the technical and economic demonstration, except for those that are reasonable: they should be constructed along with the process units, but the site for continued construction shall be considered and the connection of each phase of the project shall be taken into account. 3.0.8 Advanced technology shall be actively adopted and new scientific research results shall be absorbed. The new process and new technology adopted in the design must be tested and identified in the medium-sized test or proved to be effective in production practice.
3.0.9 The purification plant must be based on the composition of the raw gas. Strict product quality standards and comprehensive process use, energy conservation, environmental protection and other requirements, and reasonable selection of process methods: determine the overall process of the purification plant, so that the purification plant can maintain a good operating state after it is put into production to obtain the best economic benefits
3.010 The design quality standards of purification products should comply with the current national product standards. . In special circumstances, it is allowed to stipulate other specifications of products with users in a contract form
3.0.11 The automatic control design of the purification plant should reasonably determine the automation level based on the number of sets of equipment designed for the purification plant, process characteristics and production requirements. For important control parameters related to product quality, yield, safety and environmental protection, it is advisable to set up online analytical instruments to monitor the production process. 3.0.12 The purification plant should have an analytical laboratory: responsible for the analytical and testing work of the entire plant's process equipment, auxiliary production facilities and public facilities. Operators must be aware of the production and equipment operation at any time. For test items that can be tested by operators themselves, it is advisable to set up simple analytical instruments in the weak operating area. 3.0.13 The design of the purification plant shall comply with the current national "Technical Regulations for Energy Saving in Gas Field Surface Engineering Design"
3.0.14 The content and depth of environmental protection design shall comply with the current relevant national regulations.
3.0.15 The prevention and control of "three wastes" shall be based on the rational selection of process flow and equipment, to reduce the generation of waste gas, waste water, and wheat residue, and to do a good job in comprehensive management, to maximize the recycling rate, so that the purification plant, under normal production conditions, meets the "three wastes" emission standards stipulated by the state or local government
3.0.16 In the design of the purification plant, the plane layout should be reasonably carried out: low-noise equipment should be selected, and effective measures should be taken to control environmental noise. The environmental noise standard of the purification plant, the noise requirements and protective measures of the main equipment shall be implemented in accordance with the relevant provisions of the current national standard "Design Specifications for Noise Control of Industrial Enterprises". 3.0.17 The design of occupational safety and health shall comply with the provisions of the current national standard "Design Hygiene Standards for Industrial Enterprises". Effective measures should be taken to prevent accidents such as poisoning, falls, burns and electric shocks.
For devices that produce toxic media, gas masks should be equipped and there should be special storage areas. 3.0.18 In the design of purification plants, the following measures should be taken to prevent corrosion: (1) Select appropriate process parameters
(2) Have complete anti-corrosion technical facilities
(3) Correctly select materials
(4) Determine reasonable equipment structure and manufacturing process 3.0.19 For equipment, containers, pipelines, etc. exposed to the acidic environment defined in the "Requirements for Materials for Anti-Chemical Stress Cracking of Natural Gas Surface Facilities", the selection of materials, manufacturing processes and construction requirements shall comply with the relevant provisions of this standard. 3.0.20 For equipment, pipelines, etc. that are in contact with alcohol amine (including monoethanolamine, diisopropanolamine, methyldiethanolamine, cyclobutane sulfone-diisopropanolamine, cyclobutane sulfone-methyldiethanolamine, etc.) solution: when the metal wall temperature is higher than 90℃, measures should be taken to prevent alkaline stress corrosion cracking during material selection, manufacturing and construction. 3.0.21 For equipment, containers, pipelines, etc. that are in contact with high-temperature hydrogen sulfide and sulfur vapor, measures should be taken to prevent high-temperature sulfidation corrosion: For equipment, containers and pipelines that are in contact with media containing carbon dioxide, the metal wall temperature should be controlled to prevent acid condensation corrosion. 3.0.22 Nitrogen protection systems should be installed for sulfur recovery, tail gas treatment and other devices, and purified natural gas can also be used instead of nitrogen.
3.0.23 The external engineering design of the purification plant should be coordinated with the relevant system of the gas field.
4 Site selection and general layout
4.1 Site selection
4.1.1 The site should be selected within the construction area determined by the overall plan for ground construction of the gas field.
4.1.2 The site should be determined by comprehensive technical and economic analysis and comparison based on the production characteristics of the purification plant, combined with the geological, meteorological, water source, power supply, transportation, safety, environmental protection and dust welfare factors of the proposed site. 4.1.3 Attention should be paid to saving land, occupying less cultivated land, and making full use of wasteland and inferior land. 4.1.4 The site selection should avoid areas with poor geological conditions, and an engineering geological evaluation should be made on the stability and suitability of the proposed site. 4.1.5 The site selection should avoid areas affected by floods. The flood control standard should be based on the scale and weight of the chemical plant. Importance: The flood level with a recurrence period of not less than 25 years is used as the calculation flood level.
4.1.6 The water supply source must be reliable and the water quality must meet the requirements. When determining the water intake point, the local agricultural, industrial and domestic water use conditions should be fully understood, and the consent of the relevant departments should be obtained.
4.1.7 When the plant is built near a river, the drainage outlet of the purification plant wastewater and site rainwater cannot be selected within the range of 1000m upstream and 10m downstream of the intake point. 4.1.8 The north of the plant should be selected where there is a highway or a place that is convenient for building an access road. 4.1.9 It is strictly forbidden to select a plant site in the protection area of important construction projects and cultural relics and historical sites protected by the state. 4.1.10 When selecting! The living area of the purification plant should also be selected. The location of the living area should be close to Towns, and should be selected on the leeward side of the annual minimum wind direction of the factory area. There should be a sanitary protection distance between the living area and the purification plant. The sanitary protection distance should be calculated and determined according to the local meteorological and topographical conditions and the waste gas emissions of the chemical plant, in accordance with the maximum allowable concentration of harmful substances in the atmosphere of residential areas stipulated in the current national standard "Industrial Enterprise Design Hygiene Standard".
4.1.11 The layout of fire protection in the external area of the purification plant shall comply with the provisions of the current national standard "Fire Protection Code for Crude Oil and Natural Gas Engineering Design". 4.2 General plan layout
4.21 The general plan layout shall be compatible with the production process of the purification plant, ensure smooth material flow, convenient external transportation, meet safety and hygiene requirements, and integrate the process equipment, auxiliary production facilities, and public facilities of the entire plant. The facilities should be combined into a reasonable organic whole, and the whole building group should be properly handled to make it coordinated and beautiful. 4.2.2 The general layout should make good use of natural conditions such as terrain and geology to achieve compact placement, save land and reduce earthwork. 4.2.3 The layout of process equipment should meet the following requirements. 4.2.3.1 The process equipment of the whole plant should be arranged in one area, and the related equipment should be close to each other according to the process sequence. 4.2.3.2 The pipelines including the raw gas entering the plant and the purified gas leaving the plant should be as short as possible. 4.2.4 The layout of the centralized control room should meet the following requirements: 4.2.4.1 Close to the main operation area of the process equipment: and should comply with the requirements of the current national standard "Code for Fire Protection Design of Crude Oil and Natural Gas Engineering" 4.2.4.2 The layout should be downwind of the annual minimum predicted wind direction of the process equipment. 14.2.4.3 There should be no continuous vibration source with a vibration of 0.1mm and a frequency of more than 25Hz on the indoor floor around, otherwise anti-vibration measures should be taken; when using electronic instruments, there should be no frequent electromagnetic interference sources with a frequency of more than 400A/m on the instruments in the control room around. 4.2.4.4 It should not be arranged beside the main transportation trunk road in the city; otherwise, it should be not less than 15m away from the edge of the road; the noise in the control room should not be greater than 65dBiA 4.2.4.5 It should be arranged in a north-south direction to avoid western exposure 4.2.5 The layout of auxiliary and public facilities should meet the following requirements: 4.2.5.1 The maintenance room and laboratory should be located on the leeward side of the annual minimum frequency wind direction of the device or facility that emits harmful gas, mist and water mist 4.2.5.2 The laboratory should be away from places that emit harmful gas, mist or strong vibration. It should be located in an area that is convenient for production, preferably facing north and south, and avoiding the west; 4.2.5.3 Chemical agents should be stored separately near the place of use, and no centralized chemical warehouse should be set up. 4.2.5.4 The sludge warehouse should be located adjacent to the sulfur molding facilities and should comply with the relevant provisions of the current national standard "Code for Fire Prevention Design of Crude Oil and Natural Gas Engineering" 4.2.5.5 The main transformer (distribution) station should be located in a device or facility that may emit corrosive gas, dust and water mist. The leeward side of the wind direction with the lowest annual frequency should be as close to the load center as possible, and there should be convenient conditions for the high-voltage overhead power lines to enter and exit.
4.2.5.6 The layout of the compressed air station should comply with the relevant provisions of the current national standard "Compressed Air Station Design Code"
4.2.5.7 The layout of the boiler room should comply with the relevant provisions of the current national standard "Boiler Room Design Code",
4.2.5.8 The water supply facilities should be close to the water source. When arranged in the area, they should be arranged Located at the edge of the plant area, with a clean environment, short water supply pipelines, and short branches to major users
4.2.5.9 The circulating water facility is close to process equipment with high water consumption, and the layout of the cooling tower should comply with the relevant provisions of the current national standard "Industrial Circulating Water Cooling Design Code" 4.2.5.10 The sewage treatment device should be located at the edge of the plant area with low terrain, and arranged on the windward side of the annual minimum frequency wind direction of the process equipment 4.2.6 In addition to complying with the above provisions, the general layout of the purification plant shall also comply with the provisions of the current national standards "Crude Oil and Natural Gas Engineering Construction Station (Square) General Plan Design Code", "Crude Oil and Natural Gas Engineering Design Fire Code" and "Classification of Electrical Installation Sites in Petroleum Facilities"
5 Process Equipment
5.1 Process Design Principles
5.1.1 The design of the device should adopt advanced process methods and complete supporting facilities: to ensure safe and normal operation within the specified operation period and meet the requirements specified in the design.
5.1.2 The design of the device should meet the needs of normal start-up, shutdown and emergency accident handling.
51.3 Each process device in the purification plant should be designed as a combined device. 5.1.4 The process equipment should be designed based on the material balance and heat balance of the device, and reasonable design parameters that can be achieved in production practice should be selected for calculation; according to the calculation results, the corresponding specifications in the equipment standard series should be selected, and no margin should be added. 5.1.5 Metering devices should be set for raw materials, products, water, electricity, steam, fuel gas, etc. entering and leaving the device.
5.1.6 Devices using solvent desulfurization, dehydration, and tail gas treatment should be equipped with steel vertical solvent tanks. The number of tanks should be two. The capacity of a single tank should be able to store all the solvents discharged from the device during maintenance. The filling coefficient of the tank is calculated as 0.85. For solvents stored at ambient temperature, when the viscosity is large and affects the extraction, a steam heating coil should be installed in the tank.
For solvents that are easily oxidized and deteriorated when exposed to air: their storage tanks should be equipped with nitrogen or purified natural gas protection facilities.
5.1.7 For hammer-loaded cyclobutane, diisopropanolamine and other chemical agents, when stored at ambient temperature, they will thicken or solidify: special heating facilities should be installed. 5.1.8 For devices that use solvent desulfurization, dehydration, and tail gas treatment: there should be no solution low-level venting pipeline and low-level tank.
5.1.9 Centrifugal pumps should be used for pumps used in process equipment. When selecting a pump, the flow rate and head parameters required should be determined based on the results of material balance and hydraulic calculations plus 5% to 10%. 5.1.10 The rated power of the pump prime mover should not be less than the calculated value according to the following formula: Pe Kr·K Ps
Wherein, P is the calculated value of the power required by the prime mover, in kW: Ps-the calculated shaft power of the pump, in kW; determined based on the flow rate, head (pressure head) and pump efficiency determined in Article 5.1.9)
K is the prime mover power safety factor, selected according to Table 5.1.10-1. K is the transmission coefficient, selected according to Table 5.1.16-2. Prime mover power safety factor K
General centrifugal pump
Power P(W) >75:2~ 3~1831 <3
Safety factor
, 1.10 1.15[.25~13: 1.50
Table 5.1.10-1
Open volume
Swallow pump. Pump
233 11.6~ 25 1,1~1.23
Note: Gas compressor (or blower) is a system product and the prime mover should be supplied by the manufacturer. When it is necessary to calculate whether the prime mover power meets the process requirements, the corresponding safety factor transmission factor K can be selected according to the table
Transmit to the seller
Reciprocating compressor
Centrifugal compressor
0.90~0.95
0.96~ 0.9
0.97~0.99
Table 5.1.11-2
0.70~0.75
5.1.11 In purification plants with high and medium pressure steam systems, fans and pumps should use back-pressure steam turbines as prime movers and spare fans. The pump should use an electric motor as the prime mover. 5.1.12 A standby pump must be set up for a continuously operating pump. It is advisable to set up two pumps and one standby pump. When there is only one pump in continuous operation, consider setting up one standby pump. Liquid sulfur pumps should be set up as one standby pump. 5.1L.13 The pipelines entering and exiting the device must be consistent with the pipeline coordination channel of the purification plant system and conform to the flow direction of the factory's overall process. 5.1.14 A shutoff valve should be set up on the steam main pipe entering the device, and a shutoff valve should also be set up on the branch pipeline from the steam main pipe. The location of the shutoff valve should be close to the steam outlet point. 5.1.15 Steam used by important equipment such as steam turbines, steam ejectors, and fire extinguishing steam should be separately led out from the steam main pipe. 5.1.16 The temperature of the equipment during the circulating water outlet cooling period should not exceed 4C. The pressure loss of circulating water in the device should not be greater than 0.2MPa
5.1.17 When the device is shut down for maintenance, the total water consumption of the equipment should not be greater than 3 times the actual volume of the flushing system pipeline and the equipment, and the solvent content in the flushing water should be reduced as much as possible.
5.1.18 Under abnormal conditions, the following parts that may be over-pressurized should be equipped with safety valves (1) Containers with top operating pressure greater than 0.07MPa (2) The outlets of each section of reciprocating compressors or electric reciprocating pumps, gear pumps, screw pumps and other positive displacement pumps (except those with safety valves in the equipment itself) (3) When the equipment connected to the outlet of the blower, centrifugal compressor, centrifugal pump or steam reciprocating pump cannot withstand its maximum pressure, the outlet of the above-mentioned pumps: (4) Flammable gases or liquids that expand due to heat may exceed the pressure of the device. Equipment or pipelines that measure pressure:
51.19 In the same pressure system, if there is a safety valve at the pressure source, other equipment may not be equipped with safety valves: Steam should not be used as a pressure source. 5.1.20 Liquefied petroleum gas and natural gas condensate storage tanks should be equipped with safety valves. When the storage tank capacity is greater than 100ml, it is advisable to install a safety valve: Each safety valve should be able to withstand the full discharge volume:
5.1.21 Smoke tube waste heat boilers should be equipped with safety valves in accordance with the current "Steam Boiler Safety Technical Supervision Regulations".
5.1.22 The natural gas main should be equipped with an emergency shut-off valve: A safety valve and vent valve should be installed upstream of the inlet emergency shut-off valve, and the discharge volume should be the full amount of the source gas. -[3-
51.23 Opening pressure of safety valve [fixed pressure] The opening pressure of safety valve shall comply with the following provisions (1) The opening pressure of safety valve shall not be higher than the design pressure of the equipment; (2) The opening pressure of safety valve of smoke tube waste heat boiler shall be determined in accordance with the provisions of the current "Technical Supervision Regulations for Safety of Steam Boiler Protection" (3) The opening pressure of other safety valves shall be determined in accordance with Table 5.1.23. Opening pressure of safety valve (MPa)
Working pressure P
Table 5.1.23
Opening pressure of safety valve
5.1.24 The discharge volume of the flash tank safety valve can be the gas flow rate calculated based on the valve core area when the liquid level regulating valve at the bottom of the absorption tower is fully opened and the pressure difference before and after the adjustment under operating conditions. www.bzxz.net
The discharge volume of the safety valve of the desulfurization regeneration tower (or acid gas separator) should be the maximum gas volume at the top of the tower when the reflux is interrupted.
5.1.25 The safety valve should be selected according to the calculated nozzle area and combined with the standardized product series. Generally, it is not necessary to install it. It is advisable to use two safety valves installed on the raw gas pipeline of the purification plant or process unit, and the sum of their nozzle areas should be equal to or slightly larger than the calculated nozzle area.
5.1.26 A small amount of combustible gas released by the safety valve can be discharged into the atmosphere. The discharge pipe should be vertically upward: the pipe mouth should be more than 2m above the top of the building within 10m; and should be 5m above the ground. 5.1.27 The diameter of the safety valve discharge pipeline shall be calculated and determined according to the following requirements. 5.1.27.1 The diameter of the discharge pipe of a single safety valve shall be determined according to the back pressure not exceeding 10% of the opening pressure of the valve; and shall not be less than the outlet diameter of the safety valve. 5.1.27.2 The diameter of the discharge pipe connecting multiple safety valves shall be determined according to the diameter of these safety valves-14
The back pressure caused by the possible simultaneous release caused by the same source: shall not be greater than 10% of the opening pressure of any safety valve that may release later, and the cross-sectional area of the discharge main pipe shall not be less than the sum of the cross-sectional areas of each branch pipeline
5.1.28 When throttling, the safety valve discharge pipeline that may make the temperature of the discharged medium lower than the freezing point of water or the formation temperature of hydrates of different diameters shall have heat replacement or heating facilities. 5.1.29 For containers and equipment that may explode: the following measures should be taken to prevent damage by overpressure:
5.1.29.1 Increase the set pressure of containers and equipment so that they can withstand the maximum pressure generated by the explosion of the internal medium of the container and equipment: 5.1.29. Install bursting discs on containers and equipment. Bursting discs The design, manufacture and inspection shall comply with the relevant provisions of the current national "Regulations on Safety Technical Supervision of Pressure Vessels".
For Claus sulfur recovery main combustion furnaces, reheat furnaces, etc., it is advisable to increase the design pressure of the equipment to prevent overpressure damage.
5.1 Principles for the selection of purification process methods and parameters 5.2.1 There are many methods for natural gas purification processes (including desulfurization, dehydration, sulfur recovery, and tail gas treatment), and each has its own adaptability. According to domestic production practices and taking into account the current development direction of purification technology, only the selection principles of several process methods and their important design parameters are stipulated.
This specification does not limit the selection of other process methods in engineering design. 5.22-Ethanolamine desulfurization has a wide range of applications and should be used first. .2.3 Where any of the following conditions are met, the cyclobutane iodide-diisopropanolamine or cyclobutane sulfone-methyldiethanolamine method (abbreviated as sulfone-amine method) can be used for desulfurization. (1) The partial pressure of acid gas (including hydrogen sulfide and carbon dicyanide) in the raw gas is relatively high. (2) It is necessary to partially remove the organic sulfide in the raw gas. Note: If only partial removal of carbon dioxide is required, the cyclobutane iodide-methyldiethanolamine method can be used.
5.2.4 When the ratio of carbon dioxide to hydrogen sulfide in the raw gas is relatively large and the carbon dioxide removal rate needs to be limited, the methyldiethanolamine method should be used for desulfurization. [5
5.2.5 The selection of natural gas dehydration process should be based on the gas field gathering and transportation plan, natural gas composition, natural gas condensate recovery process and the required dehydration depth, and should comply with the current national "Design Specification for Natural Gas Dehydration". For lean gas or natural gas that does not use the low-thirst method to recover natural gas condensate, it is advisable to use glycol absorption method for dehydration.
5.2.6 The sulfur recovery process flow shall be selected according to the following principles: 5.2.6.1 When the concentration of hydrogen sulfide in the acid gas is relatively high and can maintain stable explosion in the main combustion furnace, the straight-through flow method in which all the acid gas enters the main combustion furnace shall be adopted. 5.2.6.1 When the concentration of hydrogen sulfide in the acid gas is relatively low and cannot maintain stable combustion in the main combustion furnace, the diverter flow method in which part of the acid gas enters the main combustion furnace shall be adopted. In the diverter flow method, the amount of acid gas entering the main combustion furnace may not be limited to one-third of the total acid gas amount. When the stable combustion of the main combustion furnace can be maintained and the construction investment is not increased too much, the amount of acid gas entering the main combustion furnace shall be increased as much as possible. 5.2.7 The selection of tail gas treatment methods should be based on the requirements of environmental protection laws and regulations: When the conventional Claus method for direct combustion of tail gas emissions cannot meet local environmental protection requirements, the flash low-temperature Claus method or super Claus method can be used; when it still cannot meet local environmental protection requirements, the reduction absorption method can be used to treat the tail gas. 5.2.8 The exhaust gas shall be discharged into the atmosphere after being burned. 5.2.9 The concentration of the solution and the acid gas (including hydrogen sulfide and carbon dioxide) load of the monoethanolamine method and the methyldiethanolamine method shall meet the following requirements. 5.2.9.1 The mass percentage concentration of the monoethanolamine solution shall be 15%. 5.2.9.2 The mass percentage concentration of the methyldiethanolamine solution shall be 20%~50%. 5.2.9.3 The acid gas load of the solution shall be determined based on the operating conditions of the absorber and the composition of the raw gas. When carbon steel equipment is used, the acid gas load shall not exceed 0.3~0 mol/mol (acid gas/amine). 5.2.10 The main temperature parameters of the desulfurization of the ethanolamine method and the methyldiethanolamine method shall meet the following requirements: 5.2.10.1 The temperature of the lean solution entering the absorber shall not be higher than 45°C. 5.2.10.2 The temperature of the solution in the reboiler at the bottom of the regeneration tower shall be lower than 120°C, with a maximum of 16
shall not exceed 127℃: for the north: when the reboiler is heated by steam, it is advisable to use saturated water vapor with a pressure not higher than .3MPa: when heated by a fire tube heater: the average heat flux density of the fire tube shall not be greater than 35kW/m
5.2.11: The design pressure of the absorption tower and regeneration tower of the monoethanolamine method and the methyldiethanolamine method shall meet the following requirements
5.2.11.1 The absorption tower and regeneration tower should adopt floating valve tower. When the tower diameter is less than 0.8m, a packed tower can be used; the absorption tower should have good demisting facilities. 5.2.11.2 When a floating valve tower is used, the number of monoethanolamine absorption plates should be 20. The number of plates of the diethanolamine absorption tower is determined by calculation based on the purified gas quality standard and the requirements for CO absorption rate: the number of plates in the desorption section of the regeneration tower should be 13, and the number of plates in the reflux section should be 3; the plate spacing between the absorption tower and the regeneration tower should be 0.6m. 5.2.11.3 The design empty tower gas velocity of the packed tower should not be greater than 60% of the flooding point velocity. The packing height is determined by the required theoretical number of plates.
5.2.11.4 The reflux ratio of the regeneration tower should not be greater than 25.2.12 When the ~ethanolamine and methyldiethanolamine desulfurization processes are adopted, when the central control content of the acid gas is greater than 2% (volume), a rich liquid meat steamer should be installed in accordance with Article 5.2.15 of this Code.
5.2.13 The composition of the diamine desulfurization solution should be determined by experimental data according to the composition of different raw gas. The following mass ratio can be used: cyclopentadienol: diisopropanolamine (or methyldiethanolamine): water = 40, 45: 15.5.2.14 The design of the regeneration tower of the amine desulfurization absorption tower shall be carried out in accordance with the provisions of Sections 5, 2.11.1 to 5.2.11.3 of this specification. The reflux ratio of the regeneration tower should not be greater than 1. When it is required to remove more organic sulfides, the number of plates or the height of the packing in the absorption tower should be increased.
5.2.15 When the amine desulfurization method is used, the rich liquid out of the absorption tower should be depressurized and flashed. The design of the flash tank should ensure that the hydrocarbon content in the acid gas entering the Claus sulfur recovery unit is not more than 4% (volume). When the raw gas contains natural gas condensate, the flash tank is equipped with an oil spill port.
The operating pressure of the flash tank should generally be 0.5MPa, but it should be consistent with the full! Fuel gas system pressure coordination
Flash gas should be introduced into the whole plant fuel gas system after desulfurization. 5.2.16 The desulfurization solution system should be equipped with mechanical filters and activated carbon filters. The filtration volume of the mechanical test filter should be the full amount of the system solution circulation volume, and the filtration volume of the activated carbon filter should not be less than 10% of the circulation volume. The solution filter should remove solid impurities above 5irm so that the mass concentration of solid particles in the solution in the system is less than 0.01%. 5.2.17 When using monoethanolamine for desulfurization, the solution system should be equipped with solution resurrection facilities, and the resurrection volume should be 2%~3% of the system solution circulation volume. When using methyldiethanolamine solution or iodineamine solution composed of methyldiethanolamine and cyclobutanone for desulfurization, solution resurrection facilities may not be installed: 5.2.18 The flow rate of the amine desulfurization solution in the pipeline shall meet the following requirements. 5.2.18.1 For monoethanolamine and methyldiethanolamine desulfurization, the liquid in all saddle liquid pipelines The flow rate should be lower than 1m/s: the rich liquid flow rate from the absorption tower to the heat exchanger tube should be 0.6~0.8m/s, and the diameter of the rich liquid pipeline from the heat exchanger to the regeneration tower should be appropriately increased
5.2.18.2 The rich liquid pipeline flow rate of the monoamine desulfurization should be 0.8~1m/5, and the maximum should not exceed 1.5m/5
5.2.19 The sulfur recovery unit should have a good gas-air ratio control system. When the sulfur production of the unit is large or the tail gas emission requirements are strict, an online tail gas analysis feedback control system can be set up: Make the molecular ratio of hydrogen sulfide to sulfur dioxide in the process gas? : 1.5.2.20 The burner of the main combustion furnace should have a good structure. The residence time of the process gas in the combustion furnace should not be greater than 35
52.21 The number of converter stages should be two. When one more stage is added, and the exhaust gas after burning can meet the environmental protection standards, it can be three stages. The amount of catalyst loaded in the converter should be determined based on the performance calculation of the selected catalyst. When using synthetic catalyst: The amount of catalyst loaded can be calculated based on 1m catalyst passing through 1000~1400m process gas per hour: The process gas volume of this article is the delivery volume under the operating state. 5.1.22 The sulphur condenser cooler should have good fog collection facilities. The horizontal sulfur condensing cooler should have an inclination slope of 1 on the liquid outlet side. 5.2.23 Principles and requirements for the setting of liquid sulfur degassing 5.2.23.1 When sulfur products are transported by liquid tank trucks (train tank trucks or truck tank trucks), the liquid sulfur should be degassed continuously. After degassing, the hydrogen sulfide content in kilograms of liquid sulfur shall not be greater than 10 mg. 5.2, 23.2 When sulfur products are transported in solid form, whether to degas shall be determined based on the scale of the factory and the pollution of the liquid sulfur to the environment during molding, packaging and storage; it is best to degas. The hydrogen sulfide content in each kilogram of liquid sulfur after degassing should not be greater than 50 mg. 5.2.24 Steam pressure of the waste heat boiler at the outlet of the sulfur recovery main combustion furnace: It shall be implemented in accordance with Article 6.5.6 of this Code. The steam pressure of other steam generators shall be determined according to the process conditions and the principle of fully utilizing waste heat.
5.2.25 Liquid sulfur pipelines should be insulated with steam jackets. Gravity-flowing liquid sulfur pipelines should have a slope of not less than 2%, sloping towards the sulfur pool or storage tank. 5.2.26 For the reduction absorption method tail gas treatment device, it is advisable to use a reducing gas generator to generate reducing gas and preheat the tail gas.
5.2.27 The design of the reducing gas generator should meet the following requirements: 5.2.27.1 The amount of reducing gas generated should be calculated based on 1.7 times the hydrogen equivalent required to convert all elemental sulfur and other sulfides in the tail gas except hydrogen sulfide into hydrogen sulfide.
5.2.27.2 The ratio of the designed air supply volume to the air volume required for theoretical combustion of the fuel gas should be 0.70~0.75:
5.2.27.3 The combustion section should be equipped with a steam injection port; 5.2.27.4 The burner The structure should meet the process requirements: ensure good pre-reaction 5.2.28 The design of the hydrogenation converter should meet the following requirements 5.2.28.1 Cobalt-Molybdenum catalyst should be selected 5.2.28.2 The bed design temperature should be 300~340℃, and the maximum should not exceed 4000:
5.2.28.3 The amount of catalyst in the converter should be calculated and determined based on 1m catalyst passing 1300~1.600m process gas per hour
5.2.28.4 The converter should have a small pressure drop. Volume: The process gas volume in this article is the volume under the operating state. 5.2.29 The process gas from the waste heat boiler of the reduction absorption tail gas treatment device: It is advisable to use -19 -
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