CN207121425U - A kind of NaHS automatic control production system - Google Patents
A kind of NaHS automatic control production system Download PDFInfo
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- CN207121425U CN207121425U CN201720315233.XU CN201720315233U CN207121425U CN 207121425 U CN207121425 U CN 207121425U CN 201720315233 U CN201720315233 U CN 201720315233U CN 207121425 U CN207121425 U CN 207121425U
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Abstract
The utility model provides a kind of NaHS automatic control production system,Including raw material air pump,Sour gas liquid separation tank,Absorption tower,Absorb column bottoms pump,Rich solution heat exchanger,Regenerator,Regenerator condenser,Regeneration overhead condenser,Regenerator return tank,Regenerator reflux pump,Regenerator Bottom Reboiler,Poor amine liquid cooler,Poor flow container,Lean pump,Fractionating column top material inlet pump,Bottom of towe heat exchanger,Fractionating column,Water sealed tank,Raw material water tank,Raw material water pump,Stripper,Purified water secondary heat exchanger,Purified water first-class heat exchanger,Purify water cooler,Clarified water pump,Cold feed heater,Acid Gas Cooler,Sour gas knockout drum,Gas overhead reflux pump,3rd absorbing reaction kettle,NaHS sends pump outside,Circulating pump,Second absorbing reaction kettle,First absorbing reaction kettle,Cooler,NaOH feed pumps,NaOH storage tanks,Gas separates cooling tank,The utility model can be controlled whole production technology in real time,NaHS cell process technology in high-quality NaHS process units,The utility model uses the continuous NaHS production technology of three autoclave 45%.
Description
Technical field
NaHS production technical field is the utility model is related to, system is produced more particularly to a kind of NaHS automatic control
System.
Background technology
At this stage, production NaHS in China's is separate sets equipment, and this complete set of equipments production cost is high, and pollution is tight
Weight, and this project is a unit in combining aromatic hydrocarbons project at 1,600,000 tons/year, to existing work on the basis of certain production
Skill reduces production cost from process modification is carried out, while reduces sewage discharge, and the pre- hydrogenation unit of continuous catalytic reforming is produced
Raw sulfuric acid gas, containing sour desulfuration of liquefied gas technique it is usually to utilize monoethanolamine, diethanol amine, two different hydramine or methyl two
Monoethanolamine equal solvent, at normal temperatures by dissolving and absorbing reaction, the sour gas such as hydrogen sulfide in gas can be absorbed, reaches purification gas
Purpose.There is advanced and mature technology in China in desulfurization unit and sewage stripping cell process technical elements at present,
Level reaches international most advanced level.Due to state's inner desulfurization technology and sewage stripping category conventional machining means, its technology is
Highly developed, level is reached advanced world standards.
Utility model content
In order to solve the above-mentioned technical problem, the purpose of this utility model is to provide a kind of NaHS automatic control production system.
Its technical scheme is as follows：
A kind of NaHS automatic control production system, including raw material air pump, sour gas liquid separation tank, absorption tower, absorb column bottoms pump,
Rich solution heat exchanger, regenerator, regenerator condenser, regeneration overhead condenser, regenerator return tank, regenerator reflux pump, regeneration
Bottom reboiler, poor amine liquid cooler, poor flow container, lean pump, fractionating column top material inlet pump, bottom of towe heat exchanger, fractionating column, sour gas
Knockout drum, fractionation tower top coagulate cooler, fractionation return tank of top of the tower, fractionation tower top reflux pump, desulfurization liquefaction Gas Cooler, Fractionator Bottom
Reboiler, water sealed tank, raw material water tank, raw material water pump, stripper, purified water secondary heat exchanger, purified water first-class heat exchanger, purification
Water cooler, clarified water pump, cold feed heater, acid Gas Cooler, sour gas knockout drum, gas overhead reflux pump,
3rd absorbing reaction kettle, NaHS send pump, circulating pump, the second absorbing reaction kettle, the first absorbing reaction kettle, cooler, NaOH outside and entered
Expect pump, NaOH storage tanks, gas separation cooling tank, the raw material air pump is connected with sour gas liquid separation tank by conveyance conduit, material
Indicating controller table LIC is connected with sour gas liquid separation tank bottom, and sour gas liquid separation tank is connected by pipeline with absorption tower, analysis inspection
Side valve AV, which is arranged on, to be led in the connection of absorption tower；Absorb column bottoms pump and be arranged on absorption tower bottom, and be connected with rich solution heat exchanger, it is rich
Liquid heat exchanger is connected by pipeline with regenerator condenser, and bottom of towe heat exchanger is connected by pipeline with absorption tower；
The regenerator is connected by pipeline with absorption tower, absorption column bottoms pump rich solution heat exchanger, regenerator condenser respectively,
Second material instruction instrumentation LIC is arranged on regenerator bottom, is connected with Regenerator Bottom Reboiler,
The lean pump is connected to the middle part of regenerator, the instruction control of the first temperature by pipeline and poor flow container, cooler
Instrument TIC is arranged on poor amine liquid cooler and entered on the pipeline of regenerator, and sour gas knockout drum is flowed back by pipeline and regenerator
Tank is connected, and analysis indicating meter AI is arranged on sour gas knockout drum, and the 3rd flow indicating controller table FIC is arranged on sour gas
Knockout drum, regenerator return tank pipeline on；
The fractionating column top material inlet pump, bottom of towe heat exchanger, fractionating column are respectively connected together, and fractionating column is by pipeline with dividing
Bottom reboiler connection is evaporated, fractionation tower top reflux pump coagulates cooler with Fractionator Bottom reboiler, fractionation tower top by pipeline and is connected to
The top of regenerator condenser, 3 material indicating controller table LIC are arranged on fractionation tower top reflux pump and condensed towards regenerator
The top of device, temperature indicating controller (TIC) table are arranged on regenerator condenser with being fractionated on the pipeline of return tank of top of the tower；
The desulfurization liquefaction Gas Cooler is connected by pipeline with the middle part of regenerator condenser, and desulfurization is liquefied into production
Tank field；
The raw material water pump is connected by pipeline with water sealed tank, raw material water tank, and is connected to stripper top, and cold feed adds
Hot device is by Pipe installing on the pipeline of raw material water pump to stripper；
Temperature indicating controller (TIC) table TIC is arranged on stripper top；
On the clarified water pump, purification water cooler, purified water first-class heat exchanger, purified water secondary heat exchanger and stripper
Portion is connected, and the 5th flow quantity control instrument table FC, which is arranged on, to be led on raw material water pump to the pipeline of purified water first-class heat exchanger；
The gas overhead reflux pump is connected by pipeline with sour gas knockout drum, and Liquid level instrument LC is arranged on
The right top of sour gas knockout drum.
The sour gas knockout drum, acid Gas Cooler are connected by pipeline, are connected to stripper top again；
The NaHS sends pump outside and is connected by pipeline with the 3rd absorbing reaction kettle, temperature instruction chain control instrument TIS peaces
Mounted in the 3rd absorbing reaction kettle bottom；
The circulating pump is connected by pipeline with the 3rd absorbing reaction kettle, and is connected with circulating pump and the second absorbing reaction kettle
Connect, temperature instruction chain control instrument TIS is arranged on the second absorbing reaction kettle bottom；
The second absorbing reaction kettle is connected further through pipeline with the first absorbing reaction kettle, temperature instruction chain control instrument
TIS is arranged on the first absorbing reaction kettle bottom.
Control instrumentation CV, liquid level instruction analysis analysis meter LIA, the second absorbing reaction kettle is separately mounted to first
On the pipeline of absorbing reaction kettle, Stress control analysis meter PIA, control instrumentation CV are separately mounted to the 3rd suction by pipeline
Reactor, circulating pump are received, such first absorbing reaction kettle, the second absorbing reaction kettle, the 3rd absorbing reaction kettle are connected by pipeline
Together.
The circulating pump is connected with cooler；Piping connects between the NaOH feed pumps are logical, but with the cooler
Connection；The gas separation cooling tank connects the first absorbing reaction kettle top by pipeline, and the liquid level indicates analyzer
Table LIA is arranged in the middle part of gas separation cooling tank, and pressure indicator controller table PIC is arranged on the pipe towards the first absorbing reaction kettle
On road；7th flow indicating controller table FIA is arranged on circulating pump to the pipeline of cooler.
The NaOH feed pumps are connected with the cooler, and the 8th flow instruction analysis meter FIA is installed on this pipeline；
Liquid level indicator alarm table LIA and temperature indicating control switch instrument TIS is installed on the NaOH storage tanks；The gas separation
9th flow indicating controller table FIC is installed in cooling tank lower pipeline.
First flow indicating controller table is installed on pipeline between the raw material air pump and sour gas liquid separation tank
FIC, throttling control instrument COZ；First analysis instrumentation AV, the second analysis instrumentation AV, the 3rd analysis instrumentation AV
It is connected in parallel on absorption tower；First material detection control instrument LIC is arranged on the absorption column bottoms pump and the absorption tower
On pipeline, second material detection control instrument LIC is arranged between the rich solution heat exchanger and the regenerator condenser tubes；
The lean pump is connected in the middle part of the absorption tower by pipeline, the 4th analysis detection Table A V and second flow instrumentation FV,
Pressure instruction instrumentation PIC connects and is connected in the lean pump and the absorption tower upper pipe.
Second temperature indicating controller table TIC is arranged on the fractionating column bottom, and the fractionating column and the 3rd temperature indicate
Control instrument TIC is arranged on the pipeline for connecting the Fractionator Bottom reboiler.
4th flow quantity control instrument table FC, the 4th temperature control instrument TC are separately mounted to the cold feed heater, described
On raw material water pump to the pipeline of the stripper；
6th flow quantity control instrument table FC is arranged on the gas overhead reflux pump to the stripper conduit upper.
The utility model can carry out sulphur in control, high-quality NaHS process units in real time to whole production technology and hydrogenate
Sodium cell process technology, the utility model use the continuous NaHS production technology of three autoclave 45%.The advantages of technology is：
（1）Using three reactive absorption kettles, alignment, the continuous production of sodium hydrosulfide is realized.
（2）Raw material hydrogen sulfide and sodium hydroxide solution backward feed mode, absorb, hydrogen sulfide is obtained at utmost step by step
Absorption and conversion, the gas of discharge can be made farthest to be purified.
（3）Raw material uses high-pure hydrogen sulfide gas in this technology, it can be ensured that impurity content is not exceeded in product, can give birth to
The high-quality NaHS product of output 45%.
（4）Technology is simple, and operation is easy.
Brief description of the drawings
Fig. 1 is the systematic schematic diagram of the utility model desulfurization unit；
Fig. 2 is the systematic schematic diagram of the utility model sewage stripping unit；
Fig. 3 is the systematic schematic diagram of the utility model NaHS unit.
Embodiment
The utility model is described in detail below in conjunction with accompanying drawing and specific embodiment, herein signal of the present utility model
Property embodiment and explanation be used for explaining the utility model, but be not intended as to restriction of the present utility model.
The drawing of reference picture 13, the purpose of this utility model there is provided a kind of high-quality NaHS production system, including
There are desulfurization unit, sewage stripping unit and NaHS unit.
Desulfurization unit
The sulfurous fuels gas and the recyclegas from NaHS workshop section for being hydrogenated with workshop section in advance from continuous catalytic reforming mix
Enter sour gas liquid separation tank 2 after the MPa of 1 pressure of raw material air pump 1.2 boostings after conjunction and carry out gas-liquid separation, gas enters absorption tower
3 middle and upper parts, the bottom liquid phase of sour gas liquid separation tank 2 deliver to sour gas stripping process.It is hydrogenated with containing for workshop section in advance from continuous catalytic reforming
Sulphur liquefied gas enters the middle part of absorption tower 3.Sulfurous gas and sulfur-bearing liquefied gas are carried out with the poor absorbing liquid from the top of absorption tower 3
Hydrogen sulfide turns into rich absorbing liquid after being absorbed by poor absorbing liquid in counter current contacting, gas and liquefied gas.
Rich absorbing liquid filters through absorbing the pressure 1.2MPa of column bottoms pump 4 extractions through rich solution filter 5, through being exchanged heat with poor rich solution
Device 7 enters regenerator 6 after exchanging heat.The tower gas phase of regenerator 6 enters regenerator return tank 9 after the condensation of regeneration overhead condenser 8,
The sour gas that tank deck gas phase is isolated through sour gas knockout drum 19 delivers to NaHS workshop section and makees raw material, tank bottom liquid phase and regeneration
The liquid phase of tower return tank 9 is all sent regenerator 6 back to after the MPa of 10 pressure of regeneration overhead reflux pump 1.2 boostings and flowed back.Regenerator 6
The lean solution of bottom of towe is sent into poor flow container 13 after rich solution heat exchanger 5 exchanges heat, poor amine liquid cooler 12 cools down, and lean solution is through lean pump 14
The top of absorption tower 3 is delivered to after the MPa of 5 pressure of rich solution heat exchanger 1.2 boostings to recycle.
The logistics at the top of absorption tower 3 is entered after being fractionated into the MPa of 15/ pressure of tower top feed pump 1.2 boostings through fractionating column 17
Material/bottom of towe heat exchanger 16 delivers to the middle part of fractionating column 17 after exchanging heat.The gas phase of the top of fractionating column 17 out is fractionated into overhead condensation
Enter fractionating column top return tank 20 after the condensation cooling of device 19, tank deck gas is desulfurized fuel gas, delivers to fuel gas pipe network and heats
Stove fuel is used, and tank bottom liquid phase is all delivered to fractionating column 17 and returned after being fractionated into the MPa of 21 pressure of overhead reflux pump 1.2 boostings
Stream.The overhead stream of fractionating column 17 is used as desulfurization liquefied gas after bottom of towe heat exchanger 16 exchanges heat, desulfurization liquefaction Gas Cooler 22 cools down
Deliver to product tank field.
The thermal source of Regenerator Bottom Reboiler 11 uses 0.6MPa（G）Steam, the thermal source of Fractionator Bottom reboiler 23 use steam
Condensate hot water.
Prevailing operating conditions：
Absorb temperature：40℃
Regeneration temperature：115
Cut point：65℃
Absorb pressure tower： 0.2MPa
Regenerate pressure tower： 0.2MPa
It is fractionated pressure tower：1.9 MPa
Amine liquid concentration： 50%
Sour gas steam stripping unit is hydrogenated with sour water raw material water tank 25, the raw material first of workshop section from continuous catalytic reforming in advance
Water pot 25 keeps pressure constant using water sealed tank 24, and acid water is divided into two strands after the boosting of raw material water pump 26 in tank, one material
The tower top of stripper 27 is delivered to after being heated by cold feed heater 32, another strand of material with raw water-purified water one-level by changing
Hot device 29, raw water-purified water secondary heat exchanger 28 deliver to the middle and upper part of stripper 27 after exchanging heat.Top gaseous phase is gas-cooled through acidity
But sour gas knockout drum 34 is entered after the condensation of device 33 cooling, gas phase delivers to NaHS workshop section and makees raw material in tank.On in tower
Portion's gas phase enters sour gas knockout drum 34 through the MPa of 35 pressure of gas overhead reflux pump 1.2.
The tower top purified water of stripper 27 passes through and raw water-purified water first-class heat exchanger 29, raw water-purified water secondary heat exchange
Sewage network is delivered in device 28, the purification heat exchange cooling of water cooler 30, the purified boosting of water pump 31.
Prevailing operating conditions：
Strip tower top/bottom temperature：40/160℃
Stripper operating pressure：0.6MPa
NaHS unit
Sour gas from desulfurization workshop section enters the 3rd after being mixed with the sour gas come from sewage stripping workshop section and absorbed
The bottom of reactor 36 with by the second absorbing reaction kettle 39 reaction mass further react, bottom obtains the sulphur of product 45%
Sodium hydride delivers to tank field.
The gas of the top of 3rd absorbing reaction kettle 36 out enters the bottom of the second absorbing reaction kettle 39 and through circulating pump 38
The reaction mass for the first absorbing reaction kettle 40 squeezed into continues absorbing reaction, the kettle top unreacting gas of the second absorbing reaction kettle 39
Body enters the first absorbing reaction bottom portion 40, and kettle base solution sends pump 37 outside through NaHS and squeezes into the 3rd absorbing reaction kettle 36.
Gas is not fully absorbed in the kettle of the first absorbing reaction bottom portion 40 with coming from from the second absorbing reaction kettle 39
The 48%NaOH liquid that NaOH storage tanks boost through NaOH feed pumps 42 is fully absorbed, and R-4301 kettle top gas bodies are through gas point
Recyclegas after being cooled down from cooling tank 44 goes to desulfurization workshop section, and kettle base solution continues to absorb into the second absorbing reaction kettle 39.
First absorbing reaction kettle 40, the second absorbing reaction kettle 39 and the reaction temperature of the 3rd absorbing reaction kettle 36 pass through cooling
Cooling water is adjusted in device 41.
Prevailing operating conditions
Absorbing reaction kettle temperature degree：60℃
Absorbing reaction kettle pressure：0.2 Mpa
Artwork explanation
The utility model process units control system uses distributed control system.Process data is focused on, completes number
According to systemic-functions such as collection, information processing, process control, security alarm.The major parameter of process units technical process is sent into
DCS is adjusted, records, shows, alarmed, and DCS progress is sent into the running status of main pump equipment in process units
Display；For parameter it is too low or it is too high by influence normal operating parameter alert detecting is carried out on DCS, this process units
DCS and other devices DCS are integrated, not only relatively independent but also data sharing, and connect with the plant information management net on upper strata
Connect, form control, the detection of a whole plant, management system, realize factory's full-automation.
The raw material air pump 1 is connected with sour gas liquid separation tank 2 by conveyance conduit, material indicating controller table LIC and acid
Property the bottom connection of qi leel flow container 2, first flow instruction is installed on the pipeline between raw material air pump 1 and sour gas liquid separation tank 2
Control instrument FIC101, throttling control instrument COZ102；Sour gas liquid separation tank 2 is connected by pipeline with absorption tower 3, analysis detection
Valve AV103, which is arranged on, to be led in the connection of absorption tower 3；First analysis instrumentation AV104, the second analysis instrumentation AV 105,
3rd analysis instrumentation AV 106 is connected in parallel on absorption tower 3；Absorb column bottoms pump 4 and be arranged on the bottom of absorption tower 3, and with richness
Liquid heat exchanger 5 is connected, and rich solution heat exchanger 5 is connected by pipeline with regenerator condenser 7, first material detection control instrument
LIC107 is arranged on the pipeline for absorbing column bottoms pump 4 and absorption tower 3, and second material detection control instrument LIC110 is arranged on rich solution
Between heat exchanger 5 and the pipeline of regenerator condenser 7；Lean pump 14 is connected to the middle part of absorption tower 3, the 4th analysis detection by pipeline
Table A V104 connects with second flow instrumentation FV108, pressure instruction instrumentation PIC107 and is connected to lean pump 14 with inhaling
Receive in the upper pipe of tower 3；Bottom of towe heat exchanger 16 is connected by pipeline with absorption tower 3；
Regenerator 6 is connected by pipeline and absorption tower 3, absorption column bottoms pump 4 rich solution heat exchanger 5, regenerator condenser 7 respectively
Connecing, second material instruction instrumentation LIC110 is arranged on the bottom of regenerator 6, is connected with Regenerator Bottom Reboiler 11,
Lean pump 14 is connected to the middle part of regenerator 6, the instruction control of the first temperature by pipeline and poor flow container 13, cooler 12
Instrument TIC114 processed be arranged on poor amine liquid cooler 12 enter regenerator 6 pipeline on, sour gas knockout drum 18 by pipeline with
Regenerator return tank 9 is connected, and analysis indicating meter AI118 is arranged on sour gas knockout drum 18, the 3rd flow indicating controller
Table FIC117 is arranged on the pipeline of sour gas knockout drum 18, regenerator return tank 9；
Fractionating column top material inlet pump 15, bottom of towe heat exchanger 16, fractionating column 17 link together, and fractionating column 17 is by pipeline with dividing
Evaporate bottom reboiler 23 to connect, second temperature indicating controller table TIC116 is arranged on the bottom of fractionating column 7, fractionating column 17 and the 3rd
Temperature indicating controller (TIC) table TIC124 is arranged on the pipeline of connection Fractionator Bottom reboiler 23；
Fractionation tower top reflux pump 21 coagulates cooler 19 and is connected to regeneration by pipeline and Fractionator Bottom reboiler 20, fractionation tower top
The top of tower condenser 7, it is cold towards regenerator that 3 material indicating controller table LIC121 is arranged on fractionation tower top reflux pump 21
The top of condenser 7, temperature indicating controller (TIC) table are arranged on regenerator condenser 7 with being fractionated on the pipeline of return tank of top of the tower 20；
Desulfurization liquefaction Gas Cooler 22 is connected by pipeline with the middle part of regenerator condenser 7, and desulfurization is liquefied into production
Tank field；
Raw material water pump 26 is connected by pipeline with water sealed tank 24, raw material water tank 25, and is connected to the top of stripper 27, and the 4th
Flow quantity control instrument table FC208, the 4th temperature control instrument TC205 be separately mounted to cold feed heater 32, raw material water pump 26 to
On the pipeline of stripper 27；Cold feed heater 32 is by Pipe installing on the pipeline of raw material water pump 26 to stripper 27；
Temperature indicating controller (TIC) table TIC202 is arranged on the top of stripper 27；
Clarified water pump 31, purification water cooler 30, purified water first-class heat exchanger 29, purified water secondary heat exchanger 28 and stripping
The top of tower 27 connects, and the 5th flow quantity control instrument table FC207, which is arranged on, leads to raw material water pump 26 to purified water first-class heat exchanger 29
On pipeline；
Gas overhead reflux pump 35 is connected by pipeline with sour gas knockout drum 34, Liquid level instrument LC210 peaces
Mounted in 34 right top of sour gas knockout drum.
Sour gas knockout drum 34, acid Gas Cooler 33 are connected by pipeline, are connected to the top of stripper 27 again；
6th flow quantity control instrument table FC 209 is arranged on gas overhead reflux pump 35 to the conduit upper of stripper 27；
NaHS sends pump 37 outside and is connected by pipeline with the 3rd absorbing reaction kettle 36, temperature instruction chain control instrument TIS310
Installed in the bottom of the 3rd absorbing reaction kettle 36；
Circulating pump 38 is connected by pipeline with the 3rd absorbing reaction kettle 36, but with the absorbing reaction kettle 39 of circulating pump 38 and second
Connection, temperature instruction chain control instrument TIS319 are arranged on the bottom of the second absorbing reaction kettle 39；
Second absorbing reaction kettle 39 is connected further through pipeline with the first absorbing reaction kettle 40, temperature instruction chain control instrument
TIS311 is arranged on the bottom of the first absorbing reaction kettle 40；
Control instrumentation CV, liquid level instruction analysis analysis meter LIA313, it is separately mounted to the second absorbing reaction kettle 39
To the pipeline of the first absorbing reaction kettle 40, Stress control analysis meter PIA309, control instrumentation CV are distinguished by pipeline
Installed in the 3rd absorbing reaction kettle 36, circulating pump 38, such first absorbing reaction kettle 40, the second absorbing reaction kettle the 39, the 3rd are inhaled
Reactor 36 is received to link together by pipeline；
Circulating pump 38 is connected with cooler 41；Piping connects between NaOH feed pumps 42 are logical, and is connected with cooler 41；
Gas separates cooling tank 44 and connects the top of the first absorbing reaction kettle 40, liquid level instruction analysis meter by pipeline
LIA305 is arranged on the middle part of gas separation cooling tank 44, and pressure indicator controller table PIC307, which is arranged on, leads to the first absorbing reaction
On the pipeline of kettle 40；7th flow indicating controller table FIA320 is arranged on circulating pump 38 to the pipeline of cooler 41；
NaOH feed pumps 42 are connected with cooler 41, and the 8th flow instruction analysis meter FIA300 is installed on this pipeline；
Liquid level indicator alarm table LIA301 and temperature indicating control switch instrument TIS302 is installed on NaOH storage tanks 43；
The 9th flow indicating controller table FIC306 is installed in the gas separation lower pipeline of cooling tank 44
The technical scheme provided above the utility model embodiment is described in detail, used herein specifically
Individual example is set forth to the principle and embodiment of the utility model embodiment, and the explanation of above example is only applicable to help
Assistant solves the principle of the utility model embodiment；Meanwhile for those of ordinary skill in the art, implement according to the utility model
Example, the there will be changes in embodiment and application, in summary, this specification content should not be construed as
To limitation of the present utility model.
Claims (3)
1. a kind of NaHS automatic control production system, it is characterized in that, including raw material air pump, sour gas liquid separation tank, absorption tower, absorption
Column bottoms pump, rich solution heat exchanger, regenerator, regenerator condenser, regeneration overhead condenser, regenerator return tank, regenerator backflow
Pump, Regenerator Bottom Reboiler, poor amine liquid cooler, poor flow container, lean pump, fractionating column top material inlet pump, bottom of towe heat exchanger, fractionation
Tower, sour gas knockout drum, fractionation tower top coagulate cooler, fractionation return tank of top of the tower, fractionation tower top reflux pump, desulfurization liquefaction air cooling
Device, Fractionator Bottom reboiler, water sealed tank, raw material water tank, raw material water pump, stripper, purified water secondary heat exchanger, purified water one-level
Heat exchanger, purification water cooler, clarified water pump, cold feed heater, acid Gas Cooler, sour gas knockout drum, gas
Overhead reflux pump, the 3rd absorbing reaction kettle, NaHS send pump, circulating pump, the second absorbing reaction kettle, the first absorbing reaction kettle, cold outside
But device, NaOH feed pumps, NaOH storage tanks, gas separation cooling tank, the raw material air pump pass through delivery pipe with sour gas liquid separation tank
Road is connected, and material indicating controller table LIC is connected with sour gas liquid separation tank bottom, and sour gas liquid separation tank passes through pipeline and absorption tower
Connection, analysis detection valve AV, which is arranged on, to be led in the connection of absorption tower；Absorb column bottoms pump and be arranged on absorption tower bottom, and changed with rich solution
Hot device connection, rich solution heat exchanger are connected by pipeline with regenerator condenser, and bottom of towe heat exchanger is connected by pipeline with absorption tower；
The regenerator is connected by pipeline with absorption tower, absorption column bottoms pump rich solution heat exchanger, regenerator condenser respectively, and second
Material instruction instrumentation LIC is arranged on regenerator bottom, is connected with Regenerator Bottom Reboiler,
The lean pump is connected to the middle part of regenerator, the first temperature indicating controller (TIC) table by pipeline and poor flow container, cooler
TIC is arranged on poor amine liquid cooler and entered on the pipeline of regenerator, and sour gas knockout drum is connected by pipeline and regenerator return tank
Connect, analysis indicating meter AI is arranged on sour gas knockout drum, and the 3rd flow indicating controller table FIC separates installed in sour gas
Tank, regenerator return tank pipeline on；
The fractionating column top material inlet pump, bottom of towe heat exchanger, fractionating column are respectively connected together, and fractionating column passes through pipeline and fractionating column
Bottom reboiler connection, fractionation tower top reflux pump coagulate cooler and are connected to regeneration by pipeline and Fractionator Bottom reboiler, fractionation tower top
The top of tower condenser, 3 material indicating controller table LIC are arranged on fractionation tower top reflux pump and lead to regenerator condenser
Top, temperature indicating controller (TIC) table are arranged on regenerator condenser with being fractionated on the pipeline of return tank of top of the tower；
The desulfurization liquefaction Gas Cooler is connected by pipeline with the middle part of regenerator condenser, and desulfurization is liquefied into production tank
Area；
The raw material water pump is connected by pipeline with water sealed tank, raw material water tank, and is connected to stripper top, cold feed heater
By Pipe installing on the pipeline of raw material water pump to stripper；
Temperature indicating controller (TIC) table TIC is arranged on stripper top；
The clarified water pump, purification water cooler, purified water first-class heat exchanger, purified water secondary heat exchanger and stripper top connect
Connect, the 5th flow quantity control instrument table FC, which is arranged on, to be led on raw material water pump to the pipeline of purified water first-class heat exchanger；
The gas overhead reflux pump is connected by pipeline with sour gas knockout drum, and Liquid level instrument LC is arranged on acidity
The right top of gas knockout drum；
The sour gas knockout drum, acid Gas Cooler are connected by pipeline, are connected to stripper top again；
The NaHS sends pump outside and is connected by pipeline with the 3rd absorbing reaction kettle, and temperature instruction chain control instrument TIS is arranged on
3rd absorbing reaction kettle bottom；
The circulating pump is connected by pipeline with the 3rd absorbing reaction kettle, and is connected with circulating pump and the second absorbing reaction kettle, temperature
Degree instruction chain control instrument TIS is arranged on the second absorbing reaction kettle bottom；
The second absorbing reaction kettle is connected further through pipeline with the first absorbing reaction kettle, temperature instruction chain control instrument TIS
Installed in the first absorbing reaction kettle bottom.
2. NaHS automatic control production system according to claim 1, it is characterized in that, the circulating pump connects with cooler
Connect；Piping connects between the NaOH feed pumps are logical, and is connected with the cooler；The gas separation cooling tank passes through pipe
Road connects the first absorbing reaction kettle top, and liquid level instruction analysis meter LIA is arranged in the middle part of gas separation cooling tank, pressure
Indicating controller table PIC is arranged on towards on the pipeline of the first absorbing reaction kettle；7th flow indicating controller table FIA is installed
On the pipeline of circulating pump to cooler.
3. NaHS automatic control production system according to claim 1 or 2, it is characterized in that, the NaOH feed pumps and institute
Cooler connection is stated, the 8th flow instruction analysis meter FIA is installed on this pipeline；Liquid level instruction is installed on the NaOH storage tanks
Alarming instrument LIA and temperature indicating control switch instrument TIS；The stream of installation the 9th in the gas separation cooling tank lower pipeline
Amount instruction control instrument FIC.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720315233.XU CN207121425U (en) | 2017-03-29 | 2017-03-29 | A kind of NaHS automatic control production system |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201720315233.XU CN207121425U (en) | 2017-03-29 | 2017-03-29 | A kind of NaHS automatic control production system |
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| CN201720315233.XU Expired - Fee Related CN207121425U (en) | 2017-03-29 | 2017-03-29 | A kind of NaHS automatic control production system |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114797411A (en) * | 2022-05-23 | 2022-07-29 | 山东华星石油化工集团有限公司 | Desulfurizing device for reforming pre-hydrogenated liquefied gas |
-
2017
- 2017-03-29 CN CN201720315233.XU patent/CN207121425U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114797411A (en) * | 2022-05-23 | 2022-07-29 | 山东华星石油化工集团有限公司 | Desulfurizing device for reforming pre-hydrogenated liquefied gas |
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